CN221933134U - System for recycling sodium carbonate and aluminum hydroxide from solid waste alkaline calcium leaching solution of electrolytic aluminum factory - Google Patents
System for recycling sodium carbonate and aluminum hydroxide from solid waste alkaline calcium leaching solution of electrolytic aluminum factory Download PDFInfo
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- CN221933134U CN221933134U CN202422416753.2U CN202422416753U CN221933134U CN 221933134 U CN221933134 U CN 221933134U CN 202422416753 U CN202422416753 U CN 202422416753U CN 221933134 U CN221933134 U CN 221933134U
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- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 title claims abstract description 78
- 229910000029 sodium carbonate Inorganic materials 0.000 title claims abstract description 37
- 238000002386 leaching Methods 0.000 title claims abstract description 22
- WNROFYMDJYEPJX-UHFFFAOYSA-K aluminium hydroxide Chemical compound [OH-].[OH-].[OH-].[Al+3] WNROFYMDJYEPJX-UHFFFAOYSA-K 0.000 title claims abstract description 21
- 229910052782 aluminium Inorganic materials 0.000 title claims abstract description 17
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 title claims abstract description 17
- 239000002910 solid waste Substances 0.000 title claims abstract description 14
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 title claims abstract description 12
- 229910052791 calcium Inorganic materials 0.000 title claims abstract description 12
- 239000011575 calcium Substances 0.000 title claims abstract description 12
- 238000004064 recycling Methods 0.000 title claims abstract description 9
- 238000010438 heat treatment Methods 0.000 claims abstract description 21
- 238000000605 extraction Methods 0.000 claims abstract description 18
- 229910003002 lithium salt Inorganic materials 0.000 claims abstract description 6
- 159000000002 lithium salts Chemical class 0.000 claims abstract description 6
- 239000012452 mother liquor Substances 0.000 claims description 19
- 239000002562 thickening agent Substances 0.000 claims description 17
- 239000002002 slurry Substances 0.000 claims description 14
- 238000007599 discharging Methods 0.000 claims description 7
- 239000007788 liquid Substances 0.000 claims description 7
- 239000012065 filter cake Substances 0.000 claims description 3
- 229940001593 sodium carbonate Drugs 0.000 abstract description 31
- 239000000243 solution Substances 0.000 abstract description 24
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 abstract description 12
- WHXSMMKQMYFTQS-UHFFFAOYSA-N Lithium Chemical compound [Li] WHXSMMKQMYFTQS-UHFFFAOYSA-N 0.000 abstract description 10
- 229910052744 lithium Inorganic materials 0.000 abstract description 10
- 239000011734 sodium Substances 0.000 abstract description 9
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 abstract description 8
- 229910052708 sodium Inorganic materials 0.000 abstract description 8
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 abstract description 8
- 239000013078 crystal Substances 0.000 abstract description 7
- MQRJBSHKWOFOGF-UHFFFAOYSA-L disodium;carbonate;hydrate Chemical compound O.[Na+].[Na+].[O-]C([O-])=O MQRJBSHKWOFOGF-UHFFFAOYSA-L 0.000 abstract description 7
- XGZVUEUWXADBQD-UHFFFAOYSA-L lithium carbonate Chemical compound [Li+].[Li+].[O-]C([O-])=O XGZVUEUWXADBQD-UHFFFAOYSA-L 0.000 abstract description 7
- 229910052808 lithium carbonate Inorganic materials 0.000 abstract description 7
- 229940076133 sodium carbonate monohydrate Drugs 0.000 abstract description 7
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 abstract description 6
- 238000001704 evaporation Methods 0.000 abstract description 6
- 230000008020 evaporation Effects 0.000 abstract description 6
- 238000000926 separation method Methods 0.000 abstract description 6
- 238000000034 method Methods 0.000 abstract description 5
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 abstract description 4
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 abstract description 4
- 238000003825 pressing Methods 0.000 abstract description 4
- 238000011084 recovery Methods 0.000 abstract description 4
- 239000001569 carbon dioxide Substances 0.000 abstract description 3
- 229910002092 carbon dioxide Inorganic materials 0.000 abstract description 3
- 238000001035 drying Methods 0.000 abstract description 3
- 239000002244 precipitate Substances 0.000 abstract description 3
- 239000012266 salt solution Substances 0.000 abstract description 3
- 229910001415 sodium ion Inorganic materials 0.000 abstract description 3
- GRYLNZFGIOXLOG-UHFFFAOYSA-N Nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 abstract description 2
- 239000002253 acid Substances 0.000 abstract description 2
- 238000001914 filtration Methods 0.000 abstract description 2
- 229910017604 nitric acid Inorganic materials 0.000 abstract description 2
- 238000002425 crystallisation Methods 0.000 description 5
- 230000008025 crystallization Effects 0.000 description 5
- 238000004519 manufacturing process Methods 0.000 description 5
- KWGKDLIKAYFUFQ-UHFFFAOYSA-M lithium chloride Chemical compound [Li+].[Cl-] KWGKDLIKAYFUFQ-UHFFFAOYSA-M 0.000 description 4
- 239000007787 solid Substances 0.000 description 4
- WMFOQBRAJBCJND-UHFFFAOYSA-M Lithium hydroxide Chemical compound [Li+].[OH-] WMFOQBRAJBCJND-UHFFFAOYSA-M 0.000 description 3
- 239000011259 mixed solution Substances 0.000 description 3
- 239000000047 product Substances 0.000 description 3
- UIIMBOGNXHQVGW-UHFFFAOYSA-M Sodium bicarbonate Chemical compound [Na+].OC([O-])=O UIIMBOGNXHQVGW-UHFFFAOYSA-M 0.000 description 2
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 2
- 238000004891 communication Methods 0.000 description 2
- IIPYXGDZVMZOAP-UHFFFAOYSA-N lithium nitrate Chemical compound [Li+].[O-][N+]([O-])=O IIPYXGDZVMZOAP-UHFFFAOYSA-N 0.000 description 2
- VVNXEADCOVSAER-UHFFFAOYSA-N lithium sodium Chemical compound [Li].[Na] VVNXEADCOVSAER-UHFFFAOYSA-N 0.000 description 2
- 238000000746 purification Methods 0.000 description 2
- 159000000000 sodium salts Chemical class 0.000 description 2
- FKNQFGJONOIPTF-UHFFFAOYSA-N Sodium cation Chemical compound [Na+] FKNQFGJONOIPTF-UHFFFAOYSA-N 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 238000003763 carbonization Methods 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000003792 electrolyte Substances 0.000 description 1
- 239000000706 filtrate Substances 0.000 description 1
- INHCSSUBVCNVSK-UHFFFAOYSA-L lithium sulfate Inorganic materials [Li+].[Li+].[O-]S([O-])(=O)=O INHCSSUBVCNVSK-UHFFFAOYSA-L 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 239000011268 mixed slurry Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- BPLYVSYSBPLDOA-GYOJGHLZSA-N n-[(2r,3r)-1,3-dihydroxyoctadecan-2-yl]tetracosanamide Chemical compound CCCCCCCCCCCCCCCCCCCCCCCC(=O)N[C@H](CO)[C@H](O)CCCCCCCCCCCCCCC BPLYVSYSBPLDOA-GYOJGHLZSA-N 0.000 description 1
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 239000002893 slag Substances 0.000 description 1
- 229910000030 sodium bicarbonate Inorganic materials 0.000 description 1
- 235000017557 sodium bicarbonate Nutrition 0.000 description 1
- 239000011780 sodium chloride Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- RBTVSNLYYIMMKS-UHFFFAOYSA-N tert-butyl 3-aminoazetidine-1-carboxylate;hydrochloride Chemical compound Cl.CC(C)(C)OC(=O)N1CC(N)C1 RBTVSNLYYIMMKS-UHFFFAOYSA-N 0.000 description 1
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- Manufacture And Refinement Of Metals (AREA)
Abstract
The utility model discloses a system for recycling sodium carbonate and aluminum hydroxide from solid waste alkaline calcium leaching solution of an electrolytic aluminum factory, which comprises a heat exchanger, an extraction tank, a carbonizer, a filter press, an MVR evaporator, a heating and pressurizing dewatering tank, a centrifuge and a flash dryer. The advantages are that: the separation of lithium and sodium adopts an extraction process, the recovery rate of lithium is high, the content of sodium ions in the lithium salt solution is extremely low, and the battery grade lithium carbonate is produced. The sodium hydroxide and sodium metaaluminate solution are introduced with carbon dioxide to react mildly, and sodium carbonate solution and aluminum hydroxide precipitate are directly generated, so that the method is safer than adding hydrochloric acid, sulfuric acid, nitric acid and the like, does not generate acid gas, and is environment-friendly. The sodium carbonate solution obtained by filter pressing and separation can be obtained by MVR evaporation; and then adopting a pressurizing and heating mode to dehydrate the sodium carbonate monohydrate into sodium carbonate without crystal water, and rapidly filtering and drying to obtain the heavy sodium carbonate.
Description
Technical Field
The utility model relates to the technical field of solid waste recovery in an electrolytic aluminum factory, in particular to a system for recovering sodium carbonate and aluminum hydroxide from solid waste alkaline calcium leaching liquid in the electrolytic aluminum factory.
Background
The scrapped solid waste (electrolyte blocks, shell surface blocks and overhaul slag blocks) generated by the electrolytic aluminum factory contains metallic lithium and sodium, and is used as one of raw materials for recovering lithium carbonate required by new energy industry when the price of the lithium carbonate is high. At present, lithium carbonate manufacturers only can recover metal lithium, and the same-family element Na is recovered in the form of sodium chloride or sodium aluminum sulfate which are low-value byproducts in the process; if the sodium carbonate is recovered, sodium bicarbonate is recovered first in the soda industry, and then calcined or reformed into sodium carbonate. The main disadvantages of this method are: (1) The sodium carbonate production flow is long and the cost is high, and a soda production system is basically required to be additionally built. (2) The lithium sodium separation is performed by the characteristic of low precipitation rate of lithium chloride, lithium sulfate and lithium nitrate in crystalline sodium salt during evaporation and crystallization, namely, the sodium ion concentration is extremely high during crystallization of lithium carbonate, and high-quality lithium carbonate cannot be obtained. (3) The aluminum cannot be dissolved in the leaching solution during alkaline leaching, otherwise the purification cost increases sharply, and the lithium loss after purification is proportional to the aluminum content. Based on the above, our company developed an alkaline leaching process for recovering lithium sodium from solid waste in an alkaline calcium leaching electrolytic aluminum plant, wherein sodium and lithium exist in the leaching solution in the forms of sodium hydroxide, sodium metaaluminate and lithium hydroxide respectively, and a system for recovering sodium carbonate and aluminum hydroxide for the leaching solution is developed specifically.
Disclosure of utility model
The utility model aims to provide a system for recycling sodium carbonate and aluminum hydroxide from solid waste alkaline calcium leaching solution of an electrolytic aluminum plant.
The utility model is implemented by the following technical scheme: the system for recycling sodium carbonate and aluminum hydroxide from solid waste alkaline calcium leaching solution of an electrolytic aluminum factory comprises a heat exchanger, an extraction tank, a carbonizer, a filter press, an MVR evaporator, a heating and pressurizing dewatering tank, a centrifuge and a flash dryer, wherein a leaching solution feeding pipe is communicated with a high-temperature inlet of the heat exchanger, a high-temperature outlet of the heat exchanger is communicated with an inlet of the extraction tank, a first outlet of the extraction tank is communicated with a lithium salt discharge pipe, a second outlet of the extraction tank is communicated with an inlet of the carbonizer, an outlet of the carbonizer is communicated with an inlet of the filter press, and a filter cake outlet of the filter press is communicated with an aluminum hydroxide discharge pipe; the filter liquor outlet of the filter press is communicated with the inlet of the MVR evaporator, the outlet of the MVR evaporator is communicated with the inlet of the heating and pressurizing dewatering tank, the slurry outlet of the heating and pressurizing dewatering tank is communicated with the inlet of the centrifugal machine, the slurry outlet of the centrifugal machine is communicated with the inlet of the flash dryer, and the outlet of the flash dryer is communicated with a sodium carbonate discharging pipe.
Further, a thickener is arranged between the MVR evaporator and the heating and pressurizing dewatering tank, an outlet of the MVR evaporator is communicated with an inlet of the thickener, and a slurry outlet of the thickener is communicated with an inlet of the heating and pressurizing dewatering tank.
Further, an overflow port of the thickener is communicated with an inlet of a mother liquor tank, and an outlet of the mother liquor tank is communicated with an inlet of the MVR evaporator.
Further, the liquid outlet of the centrifuge is communicated with the inlet of the mother liquor tank, and the outlet of the mother liquor tank is communicated with the inlet of the MVR evaporator.
The utility model has the advantages that: (1) The separation of lithium and sodium adopts an extraction process, the recovery rate of lithium is high, the content of sodium ions in a lithium salt solution is extremely low, and the production of battery grade lithium carbonate is facilitated; and the lithium content in the sodium salt solution after extraction is extremely low, so that the loss of lithium in the produced product is small, and the purity of the product is high. (2) The sodium hydroxide and sodium metaaluminate solution are introduced with carbon dioxide to react mildly, and sodium carbonate solution and aluminum hydroxide precipitate are directly generated, so that the method is safer than adding hydrochloric acid, sulfuric acid, nitric acid and the like, does not generate acid gas, and is environment-friendly. (3) The aluminum hydroxide precipitate separated by filter pressing can be sold to aluminum oxide production enterprises for further processing after being washed and packaged, so that the low-cost recovery of aluminum resources is realized. (4) The sodium carbonate solution obtained by filter pressing and separation can be obtained by MVR evaporation; and then adopting a pressurizing and heating mode to dehydrate the sodium carbonate monohydrate into sodium carbonate without crystal water, and rapidly filtering and drying to obtain the heavy sodium carbonate.
Drawings
FIG. 1 is a schematic diagram of the overall structure of the present utility model;
The device comprises a heat exchanger 1, an extraction tank 2, a carbonizer 3, a filter press 4, an MVR evaporator 5, a heating and pressurizing dewatering tank 6, a centrifuge 7, a flash dryer 8, a leaching liquid feeding pipe 9, a lithium salt discharging pipe 10, an aluminum hydroxide discharging pipe 11, an anhydrous sodium carbonate discharging pipe 12, a thickener 13 and a mother liquor tank 14.
Detailed Description
In the description of the present utility model, it should be noted that, if terms such as "center", "upper", "lower", "left", "right", "vertical", "horizontal", "inner", "outer", and the like are used, the indicated azimuth or positional relationship is based on the azimuth or positional relationship shown in the drawings, only for convenience of description and simplification of the description, and does not indicate or imply that the apparatus or element to be referred must have a specific azimuth, be configured and operated in a specific azimuth, and thus should not be construed as limiting the present utility model. Furthermore, the terms "first," "second," "third," and the like, as used herein, are used for descriptive purposes only and are not to be construed as indicating or implying any relative importance.
As shown in figure 1, the system for recycling sodium carbonate and aluminum hydroxide from solid waste alkaline calcium leaching solution of an electrolytic aluminum plant comprises a heat exchanger 1, an extraction tank 2, a carbonizer 3, a filter press 4, an MVR evaporator 5, a heating and pressurizing dewatering tank 6, a centrifuge 7 and a flash dryer 8,
The leaching solution feeding pipe 9 is communicated with a high-temperature inlet of the heat exchanger 1, a high-temperature outlet of the heat exchanger 1 is communicated with an inlet of the extraction tank 2, a first outlet of the extraction tank 2 is communicated with a lithium salt discharge pipe 10, a second outlet of the extraction tank 2 is communicated with an inlet of the carbonizer 3, an outlet of the carbonizer 3 is communicated with an inlet of the filter press 4, and a filter cake outlet of the filter press 4 is communicated with an aluminum hydroxide discharge pipe 11; the filtrate outlet of the filter press 4 is communicated with the inlet of the MVR evaporator 5, the outlet of the MVR evaporator 5 is communicated with the inlet of the heating and pressurizing dewatering tank 6, the slurry outlet of the heating and pressurizing dewatering tank 6 is communicated with the inlet of the centrifugal machine 7, the slurry outlet of the centrifugal machine 7 is communicated with the inlet of the flash dryer 8, and the outlet of the flash dryer 8 is communicated with the anhydrous sodium carbonate discharging pipe 12.
A thickener 13 is arranged between the MVR evaporator 5 and the heating and pressurizing dewatering tank 6, the outlet of the MVR evaporator 5 is communicated with the inlet of the thickener 13, and the slurry outlet of the thickener 13 is communicated with the inlet of the heating and pressurizing dewatering tank 6.
The overflow port of the thickener 13 is communicated with the inlet of the mother liquor tank 14, and the outlet of the mother liquor tank 14 is communicated with the inlet of the MVR evaporator 5.
The liquid outlet of the centrifuge 7 is in communication with the inlet of the mother liquor tank 14, and the outlet of the mother liquor tank 14 is in communication with the inlet of the MVR evaporator 5.
The production process comprises the following steps:
(1) The alkaline leaching solution sent from the leaching solution feeding pipe 9 is sent into a heat exchanger 1 to be cooled to 40 ℃ by circulating water, and then is sent into an extraction tank 2 to be extracted by adopting an HBL121 or 3938H extractant, so as to obtain layered lithium chloride solution and mixed solution (sodium hydroxide and sodium metaaluminate mixed solution);
(2) The extracted mixed solution is sent into a carbonizer 3, carbon dioxide gas is introduced, the temperature of the solution in the carbonizer 3 is controlled to be 30-150 ℃, the PH is controlled to be 11-13, and the carbonization reaction is carried out to obtain sodium carbonate solution slurry containing aluminum hydroxide solids;
(3) Delivering the slurry discharged from the carbonizer 3 into a filter press 4 for solid-liquid separation to obtain aluminum hydroxide solid and sodium carbonate solution;
(4) Delivering the sodium carbonate solution obtained by filter pressing into an MVR evaporator 5 for evaporation and crystallization to obtain mixed slurry of sodium carbonate mother liquor and sodium carbonate monohydrate;
(5) The sodium carbonate monohydrate crystals discharged from the MVR evaporator 5 are sent into a thickener 13, the solid content of slurry is improved by adopting the thickener 13, and the solid content is controlled to be 20-60%, so that the sodium carbonate monohydrate with high content is obtained;
(6) And (3) conveying the high-content sodium carbonate monohydrate discharged from the thickener 13 into a heating and pressurizing dewatering tank 6, and controlling the slurry temperature to be 110-150 ℃ to separate crystal water in the sodium carbonate monohydrate, so as to obtain sodium carbonate without crystal water. The overflow liquid discharged from the thickener 13 is collected in a mother liquor tank 14, and then returned to the MVR evaporator 5 to recover sodium carbonate.
(7) The high-temperature sodium carbonate slurry discharged from the heating and pressurizing dewatering tank 6 is sent into a centrifugal machine 7, sodium carbonate without crystal water containing free water is separated to obtain a crystallization mother liquor, the crystallization mother liquor is sent into a mother liquor tank 14, and then the mother liquor is returned to the MVR evaporator 5 to recover sodium carbonate.
(8) And (3) conveying the sodium carbonate without crystal water separated by the centrifugal machine 7 into a flash evaporation dryer 8, wherein the flash evaporation air inlet temperature is 160-300 ℃, and drying to obtain a heavy sodium carbonate product which is discharged out of the system through a heavy sodium carbonate discharging pipe.
Finally, it should be noted that: the above embodiments are only for illustrating the technical solution of the present utility model, and not for limiting the same; although the utility model has been described in detail with reference to the foregoing embodiments, it will be understood by those of ordinary skill in the art that: the technical scheme described in the foregoing embodiments can be modified or some or all of the technical features thereof can be replaced by equivalents; such modifications and substitutions do not depart from the spirit of the utility model.
Claims (4)
1. The system for recycling sodium carbonate and aluminum hydroxide from solid waste alkaline calcium leaching solution of an electrolytic aluminum factory is characterized by comprising a heat exchanger, an extraction tank, a carbonizer, a filter press, an MVR evaporator, a heating and pressurizing dewatering tank, a centrifuge and a flash dryer, wherein a leaching solution feeding pipe is communicated with a high-temperature inlet of the heat exchanger, a high-temperature outlet of the heat exchanger is communicated with an inlet of the extraction tank, a first outlet of the extraction tank is communicated with a lithium salt discharge pipe, a second outlet of the extraction tank is communicated with an inlet of the carbonizer, an outlet of the carbonizer is communicated with an inlet of the filter press, and a filter cake outlet of the filter press is communicated with an aluminum hydroxide discharge pipe; the filter liquor outlet of the filter press is communicated with the inlet of the MVR evaporator, the outlet of the MVR evaporator is communicated with the inlet of the heating and pressurizing dewatering tank, the slurry outlet of the heating and pressurizing dewatering tank is communicated with the inlet of the centrifugal machine, the slurry outlet of the centrifugal machine is communicated with the inlet of the flash dryer, and the outlet of the flash dryer is communicated with a sodium carbonate discharging pipe.
2. The system for recycling sodium carbonate and aluminum hydroxide from solid waste alkaline calcium leaching solution of an electrolytic aluminum plant according to claim 1, wherein a thickener is arranged between the MVR evaporator and the heating and pressurizing dewatering tank, an outlet of the MVR evaporator is communicated with an inlet of the thickener, and a slurry outlet of the thickener is communicated with an inlet of the heating and pressurizing dewatering tank.
3. The system for recycling sodium carbonate and aluminum hydroxide from solid waste alkaline calcium leaching solution of electrolytic aluminum factory according to claim 2, wherein an overflow port of the thickener is communicated with an inlet of a mother liquor tank, and an outlet of the mother liquor tank is communicated with an inlet of the MVR evaporator.
4. The system for recovering sodium carbonate and aluminum hydroxide from solid waste alkaline calcium leachate of an electrolytic aluminum plant according to claim 1, wherein a liquid outlet of the centrifuge is communicated with an inlet of a mother liquor tank, and an outlet of the mother liquor tank is communicated with an inlet of the MVR evaporator.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202422416753.2U CN221933134U (en) | 2024-10-08 | 2024-10-08 | System for recycling sodium carbonate and aluminum hydroxide from solid waste alkaline calcium leaching solution of electrolytic aluminum factory |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202422416753.2U CN221933134U (en) | 2024-10-08 | 2024-10-08 | System for recycling sodium carbonate and aluminum hydroxide from solid waste alkaline calcium leaching solution of electrolytic aluminum factory |
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| Publication Number | Publication Date |
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| CN221933134U true CN221933134U (en) | 2024-11-01 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN202422416753.2U Active CN221933134U (en) | 2024-10-08 | 2024-10-08 | System for recycling sodium carbonate and aluminum hydroxide from solid waste alkaline calcium leaching solution of electrolytic aluminum factory |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN221933134U (en) |
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