CN116043276B - Vertical structure inert anode aluminum electrolysis cell - Google Patents
Vertical structure inert anode aluminum electrolysis cell Download PDFInfo
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- CN116043276B CN116043276B CN202310009797.0A CN202310009797A CN116043276B CN 116043276 B CN116043276 B CN 116043276B CN 202310009797 A CN202310009797 A CN 202310009797A CN 116043276 B CN116043276 B CN 116043276B
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- 238000005868 electrolysis reaction Methods 0.000 title claims abstract description 70
- 229910052782 aluminium Inorganic materials 0.000 title claims abstract description 65
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 title claims abstract description 65
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 122
- 238000010438 heat treatment Methods 0.000 claims abstract description 114
- 229910002804 graphite Inorganic materials 0.000 claims abstract description 109
- 239000010439 graphite Substances 0.000 claims abstract description 109
- 229910052751 metal Inorganic materials 0.000 claims abstract description 77
- 239000002184 metal Substances 0.000 claims abstract description 77
- 239000002245 particle Substances 0.000 claims description 68
- 229910052593 corundum Inorganic materials 0.000 claims description 59
- 239000010431 corundum Substances 0.000 claims description 59
- 239000000571 coke Substances 0.000 claims description 53
- 239000000463 material Substances 0.000 claims description 50
- 239000003792 electrolyte Substances 0.000 claims description 40
- 239000000919 ceramic Substances 0.000 claims description 38
- 230000007797 corrosion Effects 0.000 claims description 16
- 238000005260 corrosion Methods 0.000 claims description 16
- 230000003647 oxidation Effects 0.000 claims description 16
- 238000007254 oxidation reaction Methods 0.000 claims description 16
- 239000007788 liquid Substances 0.000 claims description 13
- 239000010935 stainless steel Substances 0.000 claims description 13
- 229910001220 stainless steel Inorganic materials 0.000 claims description 13
- 229910000831 Steel Inorganic materials 0.000 claims description 10
- 239000011094 fiberboard Substances 0.000 claims description 10
- 239000010959 steel Substances 0.000 claims description 10
- 229910052581 Si3N4 Inorganic materials 0.000 claims description 9
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims description 8
- 239000002131 composite material Substances 0.000 claims description 8
- 238000004321 preservation Methods 0.000 claims description 8
- HQVNEWCFYHHQES-UHFFFAOYSA-N silicon nitride Chemical compound N12[Si]34N5[Si]62N3[Si]51N64 HQVNEWCFYHHQES-UHFFFAOYSA-N 0.000 claims description 8
- 229910045601 alloy Inorganic materials 0.000 claims description 6
- 239000000956 alloy Substances 0.000 claims description 6
- 239000002006 petroleum coke Substances 0.000 claims description 6
- 229910001030 Iron–nickel alloy Inorganic materials 0.000 claims description 5
- XUIMIQQOPSSXEZ-UHFFFAOYSA-N Silicon Chemical compound [Si] XUIMIQQOPSSXEZ-UHFFFAOYSA-N 0.000 claims description 5
- 238000002156 mixing Methods 0.000 claims description 5
- 229910052710 silicon Inorganic materials 0.000 claims description 5
- 239000010703 silicon Substances 0.000 claims description 5
- 229910000838 Al alloy Inorganic materials 0.000 claims description 3
- 229910052582 BN Inorganic materials 0.000 claims description 3
- PZNSFCLAULLKQX-UHFFFAOYSA-N Boron nitride Chemical compound N#B PZNSFCLAULLKQX-UHFFFAOYSA-N 0.000 claims description 3
- 229910000792 Monel Inorganic materials 0.000 claims description 3
- PMHQVHHXPFUNSP-UHFFFAOYSA-M copper(1+);methylsulfanylmethane;bromide Chemical compound Br[Cu].CSC PMHQVHHXPFUNSP-UHFFFAOYSA-M 0.000 claims description 3
- 229910001026 inconel Inorganic materials 0.000 claims description 3
- -1 iron-chromium-aluminum Chemical compound 0.000 claims description 3
- 239000004576 sand Substances 0.000 claims description 3
- SEPPVOUBHWNCAW-FNORWQNLSA-N (E)-4-oxonon-2-enal Chemical compound CCCCCC(=O)\C=C\C=O SEPPVOUBHWNCAW-FNORWQNLSA-N 0.000 claims description 2
- 241000276425 Xiphophorus maculatus Species 0.000 claims description 2
- 239000004411 aluminium Substances 0.000 claims 1
- 238000009434 installation Methods 0.000 abstract description 6
- 238000003723 Smelting Methods 0.000 abstract description 3
- 238000012360 testing method Methods 0.000 description 19
- 238000000034 method Methods 0.000 description 17
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 9
- 229910052799 carbon Inorganic materials 0.000 description 7
- 238000009413 insulation Methods 0.000 description 7
- 230000001681 protective effect Effects 0.000 description 6
- 238000007789 sealing Methods 0.000 description 6
- 238000001514 detection method Methods 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- 238000007731 hot pressing Methods 0.000 description 4
- 230000002093 peripheral effect Effects 0.000 description 4
- 230000002265 prevention Effects 0.000 description 4
- HBMJWWWQQXIZIP-UHFFFAOYSA-N silicon carbide Chemical compound [Si+]#[C-] HBMJWWWQQXIZIP-UHFFFAOYSA-N 0.000 description 4
- 229910010271 silicon carbide Inorganic materials 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 3
- QYEXBYZXHDUPRC-UHFFFAOYSA-N B#[Ti]#B Chemical compound B#[Ti]#B QYEXBYZXHDUPRC-UHFFFAOYSA-N 0.000 description 2
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- 229910033181 TiB2 Inorganic materials 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 229910010293 ceramic material Inorganic materials 0.000 description 2
- 238000005520 cutting process Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 230000002035 prolonged effect Effects 0.000 description 2
- 238000011160 research Methods 0.000 description 2
- 229910003264 NiFe2O4 Inorganic materials 0.000 description 1
- 229920006926 PFC Polymers 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 239000010406 cathode material Substances 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000004891 communication Methods 0.000 description 1
- 230000008094 contradictory effect Effects 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 238000005485 electric heating Methods 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 239000000835 fiber Substances 0.000 description 1
- 230000017525 heat dissipation Effects 0.000 description 1
- 230000020169 heat generation Effects 0.000 description 1
- 230000003993 interaction Effects 0.000 description 1
- 210000001503 joint Anatomy 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000155 melt Substances 0.000 description 1
- 238000006386 neutralization reaction Methods 0.000 description 1
- NQNBVCBUOCNRFZ-UHFFFAOYSA-N nickel ferrite Chemical compound [Ni]=O.O=[Fe]O[Fe]=O NQNBVCBUOCNRFZ-UHFFFAOYSA-N 0.000 description 1
- 230000000737 periodic effect Effects 0.000 description 1
- 230000035699 permeability Effects 0.000 description 1
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Classifications
-
- C—CHEMISTRY; METALLURGY
- C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
- C25C—PROCESSES FOR THE ELECTROLYTIC PRODUCTION, RECOVERY OR REFINING OF METALS; APPARATUS THEREFOR
- C25C3/00—Electrolytic production, recovery or refining of metals by electrolysis of melts
- C25C3/06—Electrolytic production, recovery or refining of metals by electrolysis of melts of aluminium
- C25C3/08—Cell construction, e.g. bottoms, walls, cathodes
-
- C—CHEMISTRY; METALLURGY
- C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
- C25C—PROCESSES FOR THE ELECTROLYTIC PRODUCTION, RECOVERY OR REFINING OF METALS; APPARATUS THEREFOR
- C25C3/00—Electrolytic production, recovery or refining of metals by electrolysis of melts
- C25C3/06—Electrolytic production, recovery or refining of metals by electrolysis of melts of aluminium
- C25C3/08—Cell construction, e.g. bottoms, walls, cathodes
- C25C3/085—Cell construction, e.g. bottoms, walls, cathodes characterised by its non electrically conducting heat insulating parts
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Electrochemistry (AREA)
- Materials Engineering (AREA)
- Metallurgy (AREA)
- Organic Chemistry (AREA)
- Electrolytic Production Of Metals (AREA)
Abstract
The application relates to the field of aluminum smelting, in particular to an inert anode aluminum electrolysis cell with a vertical structure, which comprises the following components: the application relates to an electrolytic tank shell, a heating device and a graphite base, wherein three insulating layers are arranged in the electrolytic tank shell, the heating device is arranged in a groove on a first insulating layer, the graphite base is arranged at the bottom of an inner cavity of the electrolytic tank shell, an installation groove is arranged at the bottom of the graphite base, a cathode is vertically arranged in the installation groove, anodes and cathodes are staggered, and are suspended above the electrolytic tank shell through a connecting guide rod, anode current enters the inside of the electrolytic tank shell from the top of the electrolytic tank through the guide rod, and cathode current is led out of the electrolytic tank shell through a metal electric rod.
Description
Technical Field
The application relates to the technical field of aluminum smelting, in particular to an inert anode aluminum electrolysis cell with a vertical structure.
Background
Under the current background of carbon peak and carbon neutralization, the problems of high carbon emission intensity and large carbon emission amount caused by carbon anode consumption and anode effect in the traditional prebaked carbon anode aluminum electrolysis production process are increasingly highlighted. The inert anode aluminum electrolysis technology has no emission of carbon dioxide and PFCs in the electrolysis process, and the electrolysis process generates about 0.88 ton of oxygen per ton of aluminum, so that the technology becomes an important research direction for the technical development of the aluminum smelting industry.
Currently, an inert anode aluminum electrolysis cell with a vertical electrode structure has become a mainstream research direction. The electrode area of the inert anode aluminum electrolysis cell adopting vertical electrode arrangement can be greatly increased, thereby reducing the volume of the electrolysis cell, increasing the yield and reducing the heat dissipation, and further overcoming the defect that the theoretical decomposition voltage of the inert anode is higher than that of the carbon anode. The inert anode aluminum electrolysis cell with vertical electrode arrangement needs to adopt cathode materials which can be well wetted with aluminum water, and aluminum can be smoothly separated out and converged on an aluminum liquid film formed on the surface of the cathode.
At present, the common materials are TiB2 ceramics or TiB2-C composite ceramics with high TiB2 content, and the like, and the size of the materials is not easy to be large due to the limitation of the current preparation technology. Multiple tiles are typically required for use as wettable cathodes. At present, two common splicing schemes are adopted, one scheme is that a cathode is firstly connected with a graphite base through ramming of cathode paste, and then a metal collector bar is connected with the graphite base; the other is to connect the monolithic cathode with the metal guide rod and then combine it together with the cathode paste or corundum castable.
Both of the above solutions have some drawbacks. First, if the cathode is connected to the graphite base by ramming only the cathode paste, the uniformity of conduction is poor, and the conductivity of the cathode paste is greatly changed after the cathode paste is permeated by the electrolyte melt, so that the cathode current distribution is uneven, and the cathode is broken and damaged when the current is severely biased. The second is that the corrosion resistance and protection of the metal guide rod are difficult. The metal guide rod is too close to the electrolytic reaction area of the cathode, and the metal guide rod is easily corroded by the permeated electrolyte melt or molten aluminum directly and electrochemically, so that the guide rod is damaged, expanded and broken.
In order to reduce the corrosion rate of the inert anode, the aluminum electrolysis of the inert anode generally adopts a low-temperature electrolyte system, KF or LiF is usually contained in the low-temperature electrolyte system, the operation superheat degree of the low-temperature electrolyte is higher, furnace side crust is not easy to form at the side part of the electrolytic tank, and the permeability of the low-temperature electrolyte melt is strong. Conventional electrolyzer sidewall materials and structures are easily corroded by electrolyte melts, and even directly infiltrate into the heat insulation layer from the splicing gaps of the hearth to damage the heat insulation layer materials, thereby affecting the service life of the electrolyzer. In addition, small-scale electrolysis experiments often require external heating because the amount of heat generated by the electrolysis process does not maintain the electrolyte melt at a constant target temperature. If a heating furnace is used for external heating, the size and scale of the electrolytic cell are limited, and the operation time is relatively short. If the heating element is arranged inside the hearth, the heating element needs to be replaced repeatedly, even frequently, which can affect the normal operation of the electrolytic cell.
If the application number is 201710678953.7, the heating device is attached to the inner wall of the electrolytic tank, and the 100A-1000A electrolysis test can be carried out, but the heating device still needs to be replaced periodically. In the scheme, the heating element is a single-end electric heating tube and the protective material is graphite. Graphite is susceptible to oxidation despite being subject to long-term corrosion by the electrolyte melt and the aluminum water. In actual use, graphite near the interface of electrolyte melt has high oxidation speed, is easy to punch, and the heating pipe is easy to damage, especially oxygen is released in the process of inert anode aluminum electrolysis test, so that the graphite oxidation is accelerated, the heating device is frequently replaced, the fluctuation range of the electrolyte temperature is large, and the electrolysis test can not be performed normally sometimes. Even after the heating device is damaged, the temperature is reduced, the electrolyte is solidified, and the damaged heating device is tied on the side wall of the electrolytic tank, so that the heating device cannot be replaced and is forced to stop.
The existing technical proposal can not well solve the problem of the inert anode aluminum electrolysis cell with a vertical structure, and therefore, a simple, stable and reliable inert anode aluminum electrolysis cell with a vertical structure is still needed.
Disclosure of Invention
The application mainly aims to provide an inert anode aluminum electrolysis cell with a vertical structure, which aims to solve the technical problems.
To achieve the above object, the present application provides an inert anode aluminum electrolysis cell of vertical structure, comprising:
the electrolytic cell comprises an electrolytic cell shell, wherein three layers of insulating layers are arranged inside the electrolytic cell shell, each three layers of insulating layers comprises a first insulating layer, a second insulating layer and a third insulating layer, the first insulating layer and the second insulating layer are of fixed structures, a groove is formed in the first insulating layer, the opening of the groove is upward, and the third insulating layer is of a replaceable movable structure;
the heating device is arranged in the groove on the first insulating layer and is used for adjusting the temperature of the electrolytic tank;
the graphite base is arranged at the bottom of the inner cavity of the electrolytic cell shell, the bottom of the graphite base is provided with a mounting groove, the side wall of the second insulating layer and the bottom of the graphite base are attached to the third insulating layer, and an electrolytic cell hearth is formed and is used for containing electrolyte melt and aluminum liquid;
the cathode is in a vertical plate shape, the cathode is vertically arranged in the mounting groove and is in threaded connection with the graphite base through a graphite bolt, the contact surfaces among the graphite base, the graphite bolt and the cathode are all covered with cathode paste, one side of the cathode is provided with anodes, the anodes and the cathodes are arranged in a staggered mode and are suspended above the electrolytic tank shell through connecting guide rods, anode current enters the electrolytic tank shell from the top of the electrolytic tank through the guide rods, and the cathode current is led out of the electrolytic tank shell through the graphite base and a metal electric rod connected with the graphite base.
Optionally, the heating device adopts direct current to heat, be equipped with heating element in the heating device, heating element is burnt grain or first metal hot plate or second metal hot plate.
Optionally, the coke particles are mixed by one or more of petroleum coke particles, graphite particles and graphite powder, a negative electrode graphite rod and a positive electrode graphite rod are inserted in the coke particles, the negative electrode graphite rod is used for exporting direct current, and the positive electrode graphite rod is used for importing direct current.
Optionally, a heat-insulating cover is arranged at the groove of the first insulating layer, and the heat-insulating cover is used for reducing burning loss caused by coke particle oxidation.
Optionally, the first metal heating plate or the second metal heating plate is made of one of 310S stainless steel, iron-chromium-aluminum alloy, monel alloy and Inconel alloy, and industrial alumina or corundum sand is filled in the first metal heating plate or the second metal heating plate so as to reduce oxidation of the first metal heating plate or the second metal heating plate in the direct current heating process.
Alternatively, the cathode employs TiB 2 -C composite hot-pressed ceramic, tiB 2 The mass percentage content is more than or equal to 60 percent.
Optionally, the first insulating layer is integrally cast by corundum castable, the second insulating layer is made of oxidation-resistant and electrolyte corrosion-resistant materials, and the second insulating layer is made of NiFe2O4 ceramic or NiFe 2 O 4 -one of NiO ceramic, dense corundum, boron nitride ceramic, aluminum nitride ceramic, silicon carbide-bonded silicon nitride ceramic, and the third insulating layer is made of dense corundum material.
Optionally, the shape of the interior of the electrolytic tank furnace chamber is round or square.
Optionally, the inside three-layer insulating layer of electrolysis trough casing is outside first prevention of seepage heat preservation, prevention of seepage heat preservation includes from inside to outside in proper order: dry type anti-seepage material, ceramic fiber board and steel tank shell.
Optionally be equipped with the second prevention of seepage heat preservation below the graphite base of the interior bottom of electrolysis trough casing, the second prevention of seepage heat preservation includes from inside to outside in proper order: corundum castable, dry type anti-seepage material, ceramic fiber board and steel tank shell.
Compared with the prior art, the application has the beneficial technical effects that:
(1) The direct current heating device is arranged in the groove on the first insulating layer, and adopts coke particles or the first metal heating plate or the second metal heating plate as a heating element, so that the direct current heating device is stable, not easy to damage, long in service life, low in direct current heating voltage and safe to operate.
(2) The first insulating layer adopts corundum castable, so that the electrolytic tank is not limited by size and scale, and different scale electrolytic tests can be satisfied.
(3) The three-layer insulating layer structure is adopted inside the electrolytic tank shell, the third insulating layer is a replaceable buffer layer, the second insulating layer is a corrosion-resistant layer, and the first insulating layer is a heating insulating layer, so that the problems that the electrolytic tank is required to be heated and insulated in a small scale, the side wall in the electrolytic tank shell is easy to corrode due to no furnace wall protection, the electrolyte melt is easy to permeate from a splicing gap of a hearth to damage the insulating layer and the like are solved.
(4) The graphite bolt is matched with the cathode paste by ramming, so that the effective conductive connection of the cathode and the graphite base is realized, and the problem that failure is easy to occur only by ramming the cathode paste or directly connecting the cathode with a metal guide rod is solved.
Drawings
In order to more clearly illustrate the embodiments of the present application or the technical solutions in the prior art, the drawings that are required in the embodiments or the description of the prior art will be briefly described, and it is obvious that the drawings in the following description are only some embodiments of the present application, and other drawings may be obtained according to the structures shown in these drawings without inventive effort for a person skilled in the art.
FIG. 1 is a schematic cross-sectional view of an inert anode aluminum electrolysis cell of vertical electrode structure employing coke grain heating in accordance with the present application.
FIG. 2 is a schematic diagram of the overall morphology of coke particles when the interior of the electrolytic tank furnace chamber is circular.
FIG. 3 is a schematic diagram of the overall morphology of coke particles when the interior of the electrolytic tank furnace chamber is square.
FIG. 4 is a schematic cross-sectional view of an inert anode aluminum electrolysis cell of 200A vertical electrode configuration heated by a first metal heating plate according to the application.
FIG. 5 is a schematic view of the overall morphology of the first metal heating plate of the present application after being unfolded.
FIG. 6 is a schematic cross-sectional view of an inert anode aluminum electrolysis cell of 1000A vertical electrode configuration heated by a second metal heating plate according to the application.
FIG. 7 is a schematic view of the overall morphology of the second metal heater plate of the present application after being unfolded.
The meaning of the mark is as follows: 1. an electrolyzer housing; 2. ceramic fiber board; 3. dry type anti-seepage material; 4. a first insulating layer; 5. a heating device; 6. a second insulating layer; 7. a third insulating layer; 8. a negative electrode graphite rod; 9. a thermal insulation cover; 10. a heat preservation sealing layer; 11. a guide rod; 12. a metal electric rod; 13. a graphite base; 14. graphite bolts; 15. cathode paste; 16. a cathode; 17. an anode; 18. a positive electrode graphite rod; 19. an anode bus; 20. coke particles; 21. a first metal heating plate; 22. a first stainless steel rod; 23. a second stainless steel rod; 24. a second metal heating plate; 25. a third stainless steel rod; 26. and a fourth stainless steel rod.
Detailed Description
The following description of the embodiments of the present application will be made clearly and fully with reference to the accompanying drawings, in which it is evident that the embodiments described are only some, but not all embodiments of the application. All other embodiments, which can be made by those skilled in the art based on the embodiments of the application without making any inventive effort, are intended to be within the scope of the application.
It should be noted that all directional indicators (such as up, down, left, right, front, and rear … …) in the embodiments of the present application are merely used to explain the relative positional relationship, movement, etc. between the components in a particular posture (as shown in the drawings), and if the particular posture is changed, the directional indicator is changed accordingly.
In the present application, unless specifically stated and limited otherwise, the terms "connected," "affixed," and the like are to be construed broadly, and for example, "affixed" may be a fixed connection, a removable connection, or an integral body; can be mechanically or electrically connected; either directly or indirectly, through intermediaries, or both, may be in communication with each other or in interaction with each other, unless expressly defined otherwise. The specific meaning of the above terms in the present application can be understood by those of ordinary skill in the art according to the specific circumstances.
In addition, if there is a description of "first", "second", etc. in the embodiments of the present application, the description of "first", "second", etc. is for descriptive purposes only and is not to be construed as indicating or implying a relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defining "a first" or "a second" may explicitly or implicitly include at least one such feature. In addition, the meaning of "and/or" as it appears throughout includes three parallel schemes, for example "A and/or B", including the A scheme, or the B scheme, or the scheme where A and B are satisfied simultaneously. In addition, the technical solutions of the embodiments may be combined with each other, but it is necessary to base that the technical solutions can be realized by those skilled in the art, and when the technical solutions are contradictory or cannot be realized, the combination of the technical solutions should be considered to be absent and not within the scope of protection claimed in the present application.
As shown in fig. 1 and 2, the present embodiment provides an inert anode aluminum electrolysis cell of vertical structure, comprising:
the electrolytic tank comprises an electrolytic tank shell 1, wherein three layers of insulating layers are arranged in the electrolytic tank shell 1, each three layers of insulating layers comprise a first insulating layer 4, a second insulating layer 6 and a third insulating layer 7, the first insulating layer 4 and the second insulating layer 6 are of fixed structures, a groove is formed in the first insulating layer 4, an opening of the groove is upward, and the third insulating layer 7 is of a replaceable movable structure;
the heating device 5 is arranged in the groove on the first insulating layer 4, and the heating device 5 is used for adjusting the temperature of the electrolytic tank;
the graphite base 13 is arranged at the bottom of the inner cavity of the electrolytic cell shell 1, the bottom of the graphite base 13 is provided with a mounting groove, the side wall of the second insulating layer 6 and the bottom of the graphite base 13 are attached to the third insulating layer 7, and an electrolytic cell hearth is formed and used for containing electrolyte melt and aluminum liquid;
the cathode 16, the cathode 16 is vertical platy, the cathode 16 is vertical to be located in the mounting groove, and cathode 16 passes through graphite bolt 14 and graphite base 13 threaded connection, the contact surface between graphite base 13, graphite bolt 14 and the cathode 16 all covers and has cathode paste 15, one side of cathode 16 is equipped with positive pole 17, positive pole 17 and cathode 16 staggered arrangement, and hang in the top of electrolysis trough casing 1 through connecting guide arm 11, and positive pole 17 electric current gets into the inside of electrolysis trough casing 1 from the electrolysis trough top through guide arm 11, and the cathode 16 electric current is outside through graphite base 13, with the metal electric rod 12 that is connected on the graphite base 13 draws electrolysis trough casing 1.
Wherein, the inside three-layer insulating layer that is provided with of electrolysis trough casing 1, three-layer insulating layer is from interior to exterior in proper order: a third insulating layer 7 of a replaceable dense corundum material; a second insulating layer 6 of dense corundum material; a first insulating layer 4 of corundum castable material. The first insulating layer 4 is provided with a groove which is opened upwards, and a heating device 5 is arranged in the groove to adjust the temperature in the electrolytic tank. The third insulating layer 7 is composed of two circular arc-shaped compact corundum sheets, and can be replaced at any time. The second insulating layer 6 is a complete compact corundum crucible, the graphite base 13 is placed at the bottom of the corundum crucible, and the metal electric rod 12 penetrates through a reserved hole on the corundum crucible and is connected with the graphite base 13 through threads. The second insulating layer 6 made of dense corundum is wrapped by the first insulating layer 4 cast by corundum castable, forms a circular electrolytic tank hearth without a splicing gap, is used for containing electrolyte melt and aluminum liquid, and is used as a working area of the inert anode 17 and the wettable cathode 16. The net dimensions inside the furnace are: 300mm in diameter and 500mm in depth. The cathode 16 is a wettable cathode, a vertical plate-shaped structure is adopted, the cathode 16 is embedded into a groove of a graphite base 13 at the bottom of the electrolytic tank shell 1, the cathode 16 and the graphite base 13 are connected together by a graphite bolt 14, and surrounding gaps and pits are filled by ramming cathode paste 15. The cathode 16 current is led out of the tank through the graphite base 13 and the metal electric rod 12 connected with the graphite base 13. Inert anodes 17 are arranged in a vertical plate shape in a staggered manner with cathodes 16 and are suspended above the electrolytic cell by guide rods 11, and current of the anodes 17 enters the cell from the top of the electrolytic cell through anode bus bars 19 and the guide rods 11. The heat-insulating sealing layer 10 at the furnace mouth of the electrolytic bath is also a protective material of the anode rod and is made of corundum castable.
In this embodiment, the heating device 5 is heated by direct current, and a heating element is disposed in the heating device 5, and the heating element is a coke grain 2020 or a first metal heating plate 21 or a second metal heating plate 24.
In this embodiment, the coke particles 20 are formed by mixing one or more of petroleum coke particles, graphite particles and graphite powder, and the anode graphite rod 8 and the cathode graphite rod 18 are inserted into the coke particles 20, wherein the anode graphite rod 8 is used for exporting direct current, and the cathode graphite rod 18 is used for importing direct current.
The grooves in the first insulating layer 4 are filled with coke particles 20, the negative electrode graphite rod 8 and the positive electrode graphite rod 18 are respectively used as a negative electrode and a positive electrode for enabling direct current to flow through the coke particles 20, the negative electrode graphite rod 8 and the positive electrode graphite rod 18 are inserted into the coke particles 20, and the coke particles 20 are formed by mixing 50% of petroleum coke particles with the particle size of 1-3mm, 45% of graphite particles with the particle size of 1-3 and 5% of graphite powder. The heating element is the coke particles 20 or the first metal heating plate 21 or the second metal heating plate 24, and adopts direct current to heat, so that the structure is simple and the performance is stable. The insulating side walls are not easily damaged by the heating element even if they penetrate into a small amount of electrolyte melt. When the coke particles 20 are adopted, the electrolyte has no corrosion effect on the coke particles 20, and basically does not influence the conduction and heating of the coke particles 20; when the first metal heating plate 21 or the second metal heating plate 24 is used, the filled alumina may bring the infiltrated small amount of electrolyte melt into a semi-solidified state without affecting the conduction and heat generation of the first metal heating plate 21 or the second metal heating plate 24. In addition, the direct current heating is characterized by low voltage and high current, and the heating element is required to have small resistance, so that the first metal heating plate 21 or the second metal heating plate 24 can be made to be thicker, and the oxidation and corrosion resistance is also higher. Therefore, the application can ensure that the temperature of the electrolytic tank is stable, electrolyte can not be solidified, the side wall of the third insulating layer 7 can not be dead, and the replacement is convenient. The stability and the operability of the electrolytic tank are improved greatly, and the service life of the electrolytic tank is prolonged greatly.
In this embodiment, a heat insulation cover 9 is disposed at the groove of the first insulating layer 4, and the heat insulation cover 9 is used to reduce oxidation burning loss of the coke particles 20.
When the electrolytic bath reaches the target temperature and keeps stable, the direct current of the coke particles 20 layer is 1.2kA, the voltage is 4-5V, when the voltage of the coke particles 20 layer is more than 5V, the coke particles 20 are burnt, the heat-insulating cover 9 is opened, the coke particles 20 are supplemented and pressed by a tool, and the voltage of the coke particles 20 layer is recovered to be below 5V. When the heating power needs to be changed, the heating power can be realized by adjusting the direct current.
In this embodiment, the first metal heating plate 21 or the second metal heating plate 24 is made of one of 310S stainless steel, iron-chromium-aluminum alloy, monel alloy and Inconel alloy, and industrial alumina or corundum sand is filled in the first metal heating plate 21 or the second metal heating plate 24 to reduce oxidation of the first metal heating plate 21 or the second metal heating plate 24 in the direct current heating process.
In this embodiment, the cathode 16 is TiB 2 -C composite hot-pressed ceramic, tiB 2 The mass percentage content is more than or equal to 60 percent.
In this embodiment, the first insulating layer 4 is integrally cast with corundum castable, the second insulating layer 6 is made of an oxidation-resistant and electrolyte corrosion-resistant material, and the second insulating layer 6 is made of NiFe 2 O 4 Ceramic, niFe 2 O 4 One of NiO ceramic, dense corundum, boron nitride ceramic, aluminum nitride ceramic, silicon carbide-silicon nitride ceramic, and the third insulating layer 7 is made of dense corundum material.
In this embodiment, referring to fig. 2 and 3, the shape of the interior of the electrolytic cell furnace is circular or square.
In this embodiment, the first impermeable insulating layer is arranged outside the three insulating layers inside the electrolytic tank shell 1, and the impermeable insulating layer sequentially comprises from inside to outside: dry type anti-seepage material 3, ceramic fiber board 2 and steel tank shell.
In this embodiment, a second impermeable insulating layer is arranged below the graphite base 13 at the bottom in the electrolytic tank shell 1, and the second impermeable insulating layer sequentially comprises from inside to outside: corundum castable, dry type anti-seepage material 3, ceramic fiber plate 2 and steel tank shell.
The insulating side wall of the electrolytic tank is three layers, the side wall of the third insulating layer 7 is made of compact corundum material, does not pollute electrolyte and is a replaceable buffer layer, and the side wall of the second insulating layer 6 is protected physically in the first step, so that the electrolyte melt is prevented from directly scouring the side wall of the second insulating layer 6. The side wall of the second insulating layer 6 is made of a material which can resist oxidation and electrolyte melt corrosion. The first insulating layer 4 is integrally poured by corundum castable, and the side wall of the second insulating layer 6 and the graphite base 13 at the bottom of the electrolytic tank shell 1 are wrapped into a whole without a splicing gap. The temperature of the outer layer of the insulating side wall is gradually reduced, and the leakage of electrolyte melt to the external heat insulation layer can be effectively avoided by matching with the dry anti-seepage material 3, so that the service life of the electrolytic tank is greatly prolonged.
In addition, the side wall of the first insulating layer 4 is made of corundum castable, so that the electrolytic tank is not limited in size, can be suitable for electrolytic tanks of different scales, and can be realized by tens of amperes to thousands of amperes in a laboratory and tens of amperes to hundreds of amperes in industrial tests.
According to an inert anode aluminum electrolysis cell with a vertical structure, the application performs relevant electrolysis tests, and the relevant processes and the effects obtained by the tests are as follows.
First kind: referring to fig. 1 and 2, a 100A inert anode aluminum electrolysis cell with vertically arranged electrodes, cathodes connected to the bottom of the cell, and heating elements using coke particles 20.
The three-layer insulating side wall of the electrolytic tank is sequentially provided with the following components from inside to outside: an inner third insulation layer 7 of replaceable compact corundum material; a second insulating layer 6 of dense corundum material; a first insulating layer 4 of corundum castable material. The first insulating layer 4 is provided with a groove which is opened upwards, coke particles 20 are contained in the groove, and the negative electrode graphite rod 8 and the positive electrode graphite rod 18 are respectively used as a negative electrode and a positive electrode of the coke particles 20 which are electrified with direct current and are inserted into the coke particles 20. The third insulating layer 7 is composed of two circular arc-shaped compact corundum sheets, and can be replaced at any time. The second insulating layer 6 is a complete compact corundum crucible, the graphite base 13 is placed at the bottom of the corundum crucible, and the metal electric rod 12 penetrates through a reserved hole on the corundum crucible and is connected with the graphite base 13 through threads. The second insulating layer 6 made of dense corundum is wrapped by the first insulating layer 4 cast by corundum castable, forms a circular electrolytic tank hearth without a splicing gap, is used for containing electrolyte melt and aluminum liquid, and is used as a working area of the inert anode 17 and the wettable cathode 16. The net dimensions inside the furnace are: 300mm in diameter and 500mm in depth. The impermeable heat-insulating layer outside the first insulating layer 4 is sequentially provided with a dry impermeable material layer 3, a ceramic fiber board 2 and a steel tank shell from inside to outside.
Wettable cathode 16 is of TiB 2 TiB content of more than 60% 2 C hot pressing the composite ceramic, embedding the vertical plate structure into the installation groove of the graphite base 13 at the bottom of the electrolytic tank, connecting the cathode 16 and the graphite base 13 together by using graphite bolts 14, and tamping and filling peripheral gaps and pits by using cathode paste 15. The cathode 16 current is led out of the tank through the graphite base 13 and the metal electric rod 12 connected with the graphite base 13. Inert anodes 17 are arranged in a vertical plate shape in a staggered manner with cathodes 16 and are suspended above the electrolytic cell by guide rods 11, and anode current enters the cell from the top of the electrolytic cell through anode bus bars 19 and guide rods 11. The heat-insulating sealing layer 10 at the furnace mouth of the electrolytic bath is also a protective material of the anode rod and is made of corundum castable.
The coke particles 20 filled in the grooves of the first insulating layer 4 are formed by mixing 50% of petroleum coke particles with the particle size of 1-3mm, 45% of graphite particles with the particle size of 1-3 and 5% of graphite powder. The negative electrode graphite rod 8 and the positive electrode graphite rod 18 serve as a negative electrode and a positive electrode, respectively, for applying direct current to the coke particles 20. When the electrolytic bath reaches the target temperature and keeps stable, the direct current of the coke particles 20 layer is 1.2kA, the voltage is 4-5V, when the voltage of the coke particles 20 layer is more than 5V, the coke particles 20 are burnt, the heat preservation cover 9 is opened, the coke particles 20 are supplemented and pressed by a tool, and the voltage of the coke particles 20 layer is recovered to be below 5V. When the heating power needs to be changed, the heating power can be realized by adjusting the direct current.
In the electrolytic test process, KF-NaF-AlF is adopted 3 The low-temperature electrolyte system has an electrolysis temperature of 800-850 ℃, the direct current in the electrolysis process is 100A, two wettable cathodes and one inert anode. The electrolysis process requires continuous alumina feed and periodic removal of the bottom produced aluminum water. The third insulating layer 7 is made of dense corundum material and is replaced about every 10 days; the coke particles 20 were replenished in small amounts every 2 days. The electrolysis test progresses for about 1000 hours, and the test is stopped and the heating is stopped due to the detection requirement of the inert anode. And taking out the inert anode, the electrolyte and the aluminum liquid completely, and observing that the electrolytic bath is still intact.
Second kind: referring to FIG. 3, a 200A inert anode aluminum electrolysis cell with vertically arranged electrodes and cathodes connected to the bottom of the cell, the heating element being coke particles 20.
The three-layer insulating side wall of the electrolytic tank is sequentially provided with the following components from inside to outside: a third insulating layer 7 of a replaceable dense corundum material; niFe 2 O 4 A second insulating layer 6 made of a base ceramic material; a first insulating layer 4 of corundum castable material. The first insulating layer 4 is provided with a groove which is opened upwards, coke particles 20 are contained in the groove, and the negative electrode graphite rod 8 and the positive electrode graphite rod 18 are respectively used as a negative electrode and a positive electrode of the coke particles 20 which are electrified with direct current and are inserted into the coke particles 20. The third insulating layer 7 is composed of four rectangular compact corundum sheets, and can be replaced at any time. The second insulating layer 6 is also made of four rectangular NiFe 2 O 4 The base ceramic block is formed and is in butt joint with the edge of the graphite base 13, and is wrapped by the first insulating layer 4 cast by corundum castable, so that a square electrolytic tank hearth without a splicing gap is formed, is used for containing electrolyte melt and aluminum liquid, and is used as a working area of the inert anode 17 and the wettable cathode 16. The net dimensions inside the furnace are: 320mm long, 270mm wide and 500mm deep. The impermeable heat-insulating layer outside the first insulating layer 4 is sequentially provided with a dry impermeable material layer 3, a ceramic fiber board 2 and a steel tank shell from inside to outside.
Wettable cathode 16 is of TiB 2 TiB content of more than 60% 2 C hot pressing the composite ceramic, embedding the vertical plate structure into the installation groove of the graphite base 13 at the bottom of the electrolytic tank, connecting the cathode 16 and the graphite base 13 together by using graphite bolts 14, and tamping and filling peripheral gaps and pits by using cathode paste 15. The cathode current is led out of the tank through the graphite base 13 and the metal electric rod 12 connected with the graphite base 13. Inert anodes 17 are arranged in a vertical plate shape in a staggered manner with cathodes 16 and are suspended above the electrolytic cell by guide rods 11, and anode current enters the cell from the top of the electrolytic cell through anode bus bars 19 and guide rods 11. The heat-insulating sealing layer 10 at the furnace mouth of the electrolytic bath is also a protective material of the anode rod and is made of corundum castable.
The coke particles 20 filled in the grooves of the first insulating layer 4 are formed by mixing 50% of petroleum coke particles with the particle size of 1-3mm, 45% of graphite particles with the particle size of 1-3 and 5% of graphite powder. The negative electrode graphite rod 8 and the positive electrode graphite rod 18 serve as a negative electrode and a positive electrode, respectively, for applying direct current to the coke particles 20. When the electrolyzer reaches the target temperature and keeps stable, the direct current of the coke particles 20 layers is 1.5kA, and the voltage is 4-5V. When the voltage of the coke particles 20 layer is more than 5V, the burning loss of the coke particles 20 is indicated, the heat-insulating cover 9 is opened, the coke particles 20 are supplemented and pressed by a tool, and the voltage of the coke particles 20 layer is restored to below 5V. When the heating power needs to be changed, the heating power can be realized by adjusting the direct current.
In the electrolytic test process, KF-NaF-AlF is adopted 3 The low-temperature electrolyte system has an electrolysis temperature of 800-850 ℃, the direct current in the electrolysis process is 200A, two wettable cathodes and one inert anode. The electrolysis process needs to continuously provide alumina blanking, and aluminum water generated at the bottom needs to be taken out periodically, so that the aluminum level is always kept lower than that of the middle corrosion-resistant insulating side wall, and NiFe is prevented from being caused by the aluminum water 2 O 4 And (3) corrosion of the base ceramic material. The third insulating layer 7 is made of dense corundum material and is replaced about every 10 days; the coke particles 20 were replenished in small amounts every 2 days. The electrolysis test progresses for about 1000 hours, and the test is stopped and the heating is stopped due to the detection requirement of the inert anode. And taking out the inert anode, the electrolyte and the aluminum liquid completely, and observing that the electrolytic bath is still intact.
Third kind: referring to fig. 4 and 5, a 200A inert anode aluminum electrolysis cell with vertically arranged electrodes and cathodes connected to the bottom of the cell, the heating element using a first metal heating plate 21.
The three-layer insulating side wall of the electrolytic tank is sequentially provided with the following components from inside to outside: a third insulating layer 7 of a replaceable dense corundum material; a second insulating layer 6 of silicon carbide combined with silicon nitride material; a first insulating layer 4 of corundum castable material. The first insulating layer 4 is provided with a groove which is opened upwards, and two first metal heating plates 21 are arranged in the groove. The first stainless steel rod 22 and the second stainless steel rod 23 are welded to the first metal heater plate 21 as a negative electrode and a positive electrode, respectively, to which the first metal heater plate 21 is energized with direct current. The third insulating layer 7 is composed of four rectangular compact corundum sheets, and can be replaced at any time. The second insulating layer 6 is also formed by combining four rectangular silicon carbide with silicon nitride ceramic blocks, is butted with the edge of the graphite base 13, is wrapped by the first insulating layer 4 cast by corundum castable, forms a square electrolytic tank hearth without splicing gaps, is used for containing electrolyte melt and aluminum liquid, and is used as a working area of the inert anode 16 and the wettable cathode 17. The net dimensions inside the furnace are: 320mm long, 270mm wide and 500mm deep. The impermeable heat-insulating layer outside the first insulating layer 4 is sequentially provided with a dry impermeable material 3, a ceramic fiber board 2 and a steel tank shell from inside to outside.
Wettable cathode 16 is of TiB 2 TiB content of more than 60% 2 C hot pressing the composite ceramic, embedding the vertical plate structure into the installation groove of the graphite base 13 at the bottom of the electrolytic tank, connecting the cathode 16 and the graphite base 13 together by using graphite bolts 14, and tamping and filling peripheral gaps and pits by using cathode paste 15. The cathode current is led out of the tank through the graphite base 13 and the metal electric rod 12 connected with the graphite base 13. Inert anodes 17 are arranged in a vertical plate shape in a staggered manner with cathodes 16 and are suspended above the electrolytic cell by guide rods 11, and anode current enters the cell from the top of the electrolytic cell through anode bus bars 19 and guide rods 11. The heat-insulating sealing layer 10 at the furnace mouth of the electrolytic bath is also a protective material of the anode rod and is made of corundum castable.
The first metal heating plates 21 arranged in the grooves of the first insulating layer 4 are made of 310s stainless steel, are formed by cutting a whole plate, have the same appearance, and are connected in parallel. Each first metal heating plate 21 has a thickness of 10mm, a width of 40mm of the cut strip and a total length of about 4000mm of the cut strip, and heats both side walls of the hearth. After the parallel connection, the parallel resistance of the two first metal heating plates 21 at 800 ℃ is 0.0068 ohm, and the direct current is conducted for 1kA, and the voltage is 6.8V. The gap between the first metal heating plate 21 and the groove is filled with industrial oxidation.
In the electrolytic test process, KF-NaF-AlF is adopted 3 The low-temperature electrolyte system has an electrolysis temperature of 800-850 ℃, the direct current in the electrolysis process is 200A, two wettable cathodes and one inert anode. The electrolysis process needs to continuously provide alumina blanking, and aluminum water generated at the bottom needs to be taken out periodically, so that the aluminum level is always kept lower than that of the middle corrosion-resistant insulating side wall, and the corrosion of the aluminum water to silicon carbide-bonded silicon nitride materials is avoided. Dense corundum material with third insulating layer 7Quality, about once every 10 days; the electrolysis test progresses for about 1000 hours, and the test is stopped and the heating is stopped due to the detection requirement of the inert anode. After taking out the inert anode, the electrolyte and the aluminum liquid, the electrolytic bath is still intact, and the surface of the first metal heating plate 21 is only slightly oxidized.
Fourth kind: referring to fig. 6 and 7, a 1000A inert anode aluminum electrolysis cell with vertically arranged electrodes and cathodes connected to the bottom of the cell, the heating element using a second metal heater plate 24.
The three-layer insulating side wall of the electrolytic tank is sequentially provided with the following components from inside to outside: a third insulating layer 7 of a replaceable dense corundum material; a second insulating layer 6 of silicon carbide combined with silicon nitride material; a first insulating layer 4 of corundum castable material. The first insulating layer 4 is provided with a groove which is opened upwards, and two second metal heating plates 24 are arranged in the groove. The third stainless steel rod 25 and the fourth stainless steel rod 26 are respectively used as a negative electrode and a positive electrode of the second metal heating plate 24 which are electrified with direct current, and are welded on the second metal heating plate 24. The third insulating layer 7 is composed of four rectangular compact corundum sheets, and can be replaced at any time. The second insulating layer 6 is also composed of eight rectangular silicon carbide combined with silicon nitride ceramic blocks, is butted with the edge of the graphite base 13, is wrapped by the first insulating layer 4 cast by corundum castable, forms a square electrolytic tank hearth without a splicing gap, is used for containing electrolyte melt and aluminum liquid, and is used as a working area of the inert anode 17 and the wettable cathode 16. The net dimensions inside the furnace are: 960mm long, 270mm wide and 500mm deep. The impermeable insulating layer outside the outer insulating side wall 64 is sequentially provided with a dry impermeable material 3, a ceramic fiber board 2 and a steel tank shell from inside to outside.
Wettable cathode 16 is of TiB 2 TiB content of more than 60% 2 C hot pressing the composite ceramic, embedding the vertical plate structure into the installation groove of the graphite base 13 at the bottom of the electrolytic tank, connecting the cathode 16 and the graphite base 13 together by using graphite bolts 14, and tamping and filling peripheral gaps and pits by using cathode paste 15. The cathode current is led out of the tank through the graphite base 13 and the metal electric rod 12 connected with the graphite base 13. Inert anodes 17 are arranged in a vertical plate shape and staggered with cathodes 16 and are suspended above the electrolytic tank by guide rods 11, and the anodes are arranged in a staggered mannerCurrent enters the cell from the top of the cell via anode bus bar 19 and guide bar 11. The heat-insulating sealing layer 10 at the furnace mouth of the electrolytic bath is also a protective material of the anode rod and is made of corundum castable.
The second metal heating plates 24 arranged in the grooves of the first insulating layer 4 are made of 310s stainless steel, are formed by cutting a whole plate, have the same appearance, and are connected in parallel. Each second metal heater plate 24 has a thickness of 12mm, a slat width of 80mm and a total length of about 8000mm, each for two side wall heats. After the parallel connection, the parallel resistance of the two second metal heating plates 24 at 800 ℃ was 0.0057 ohm, the direct current was 1.6kA, and the voltage was 9.12V. The gap between the second metal heating plate 24 and the groove is filled with industrial oxidation and covers the second metal heating plate 24.
In the electrolytic test process, KF-NaF-AlF is adopted 3 The low-temperature electrolyte system has the electrolysis temperature of 800-850 ℃, the direct current in the electrolysis process of 1000A, six wettable cathodes 16 and five inert anodes 17. The electrolysis process needs to continuously provide alumina blanking, and aluminum water generated at the bottom needs to be taken out periodically, so that the aluminum level is always kept lower than that of the middle corrosion-resistant insulating side wall, and the corrosion of the aluminum water to silicon carbide-bonded silicon nitride materials is avoided. The third insulating layer 7 is made of dense corundum material and is replaced about every 10 days; the electrolysis test progresses for about 2000 hours, and the test is stopped and the heating is stopped due to the detection requirement of the inert anode. After taking out the inert anode, the electrolyte and the aluminum liquid, the electrolytic cell is still intact, and the surface of the second metal heating plate 24 is only slightly oxidized.
The foregoing description is only of the optional embodiments of the present application, and is not intended to limit the scope of the application, and all the equivalent structural changes made by the description of the present application and the accompanying drawings or the direct/indirect application in other related technical fields are included in the scope of the application.
Claims (10)
1. An inert anode aluminum electrolysis cell of vertical structure, comprising:
the electrolytic cell comprises an electrolytic cell shell (1), wherein three layers of insulating layers are arranged inside the electrolytic cell shell (1), each three layers of insulating layers comprise a first insulating layer (4), a second insulating layer (6) and a third insulating layer (7), the first insulating layer (4) and the second insulating layer (6) are of fixed structures, a groove is formed in the first insulating layer (4), an opening of the groove is upward, and the third insulating layer (7) is of a replaceable movable structure;
the heating device (5) is arranged in the groove on the first insulating layer (4), and the heating device (5) is used for adjusting the temperature of the electrolytic tank;
the graphite base (13), the bottom of the inner cavity of the electrolytic tank shell (1) is arranged on the graphite base (13), the bottom of the graphite base (13) is provided with a mounting groove, the side wall of the second insulating layer (6) is attached to the bottom of the graphite base (13) and the third insulating layer (7), and an electrolytic tank hearth is formed, and the electrolytic tank hearth is used for containing electrolyte melt and aluminum liquid;
cathode (16), cathode (16) are vertical platy, cathode (16) are vertical locate in the mounting groove, and cathode (16) pass through graphite bolt (14) and graphite base (13) threaded connection, contact surface between graphite base (13), graphite bolt (14) and cathode (16) all is covered with negative pole paste (15), one side of cathode (16) is equipped with positive pole (17), positive pole (17) and cathode (16) staggered arrangement, and hang the top at electrolysis trough casing (1) through connecting guide arm (11), and positive pole (17) electric current gets into the inside of electrolysis trough casing (1) from electrolysis trough top through guide arm (11), and outside electrolysis trough casing (1) are drawn forth to metal electric rod (12) that are connected on negative pole base (13) through graphite base (13) electric current.
2. The vertical inert anode aluminum electrolysis cell according to claim 1, wherein the heating device (5) is heated by direct current, a heating element is arranged in the heating device (5), and the heating element is a coke grain (20) or a first metal heating plate (21) or a second metal heating plate (24).
3. The vertical inert anode aluminum electrolysis cell according to claim 2, wherein the coke particles (20) are formed by mixing one or more of petroleum coke particles, graphite particles and graphite powder, a negative electrode graphite rod (8) and a positive electrode graphite rod (18) are inserted into the coke particles (20), the negative electrode graphite rod (8) is used for exporting direct current, and the positive electrode graphite rod (18) is used for importing direct current.
4. The vertical inert anode aluminum electrolysis cell according to claim 1, wherein a heat preservation cover (9) is arranged at the groove of the first insulating layer (4), and the heat preservation cover (9) is used for reducing oxidation burning loss of coke particles (20).
5. The vertical inert anode aluminum reduction cell according to claim 2, wherein the first metal heating plate (21) or the second metal heating plate (24) is made of one of 310S stainless steel, iron-chromium-aluminum alloy, monel alloy and Inconel alloy, and industrial alumina or corundum sand is filled in the first metal heating plate (21) or the second metal heating plate (24) to reduce oxidation of the first metal heating plate (21) or the second metal heating plate (24) in the direct current heating process.
6. A vertical inert anode aluminium electrolysis cell according to claim 2, wherein the cathode (16) is of TiB 2 -C composite hot-pressed ceramic, tiB 2 The mass percentage content is more than or equal to 60 percent.
7. The vertical inert anode aluminum electrolysis cell according to claim 1, wherein the first insulating layer (4) is integrally cast by corundum castable, the second insulating layer (6) is made of oxidation-resistant and electrolyte corrosion-resistant materials, and the second insulating layer (6) is made of NiFe 2 O 4 Ceramic, niFe 2 O 4 -one of NiO ceramic, dense corundum, boron nitride ceramic, aluminum nitride ceramic, silicon carbide-bonded silicon nitride ceramic, the third insulating layer (7) being of dense corundum material.
8. The inert anode aluminum electrolysis cell of claim 1, wherein the shape of the interior of the cell hearth is circular or square.
9. The vertical inert anode aluminum electrolysis cell according to claim 1, wherein a first impermeable heat-insulating layer is arranged outside three insulating layers inside the electrolysis cell shell (1), and the impermeable heat-insulating layer sequentially comprises from inside to outside: dry type anti-seepage material (3), ceramic fiber board (2) and steel tank shell.
10. The vertical inert anode aluminum electrolysis cell according to claim 1, wherein a second impermeable heat-insulating layer is arranged below a graphite base (13) at the inner bottom of the electrolysis cell shell (1), and the second impermeable heat-insulating layer sequentially comprises from inside to outside: corundum castable, dry type anti-seepage material (3), ceramic fiber board (2) and steel tank shell.
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| CN105297075A (en) * | 2015-10-28 | 2016-02-03 | 兰州资源环境职业技术学院 | Aluminum electrolytic graphite crucible experimental device and experimental method |
| CN107541755A (en) * | 2017-08-10 | 2018-01-05 | 中国铝业股份有限公司 | A kind of internal heating type fused-salt bath |
| CN111172562A (en) * | 2020-01-20 | 2020-05-19 | 镇江慧诚新材料科技有限公司 | Preparation method of fuel aluminum for aluminum-air battery |
| CN210683970U (en) * | 2019-07-08 | 2020-06-05 | 四川江铜稀土有限责任公司 | Double-graphite-groove rare earth electrolytic cell |
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| US6866768B2 (en) * | 2002-07-16 | 2005-03-15 | Donald R Bradford | Electrolytic cell for production of aluminum from alumina |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN105297075A (en) * | 2015-10-28 | 2016-02-03 | 兰州资源环境职业技术学院 | Aluminum electrolytic graphite crucible experimental device and experimental method |
| CN107541755A (en) * | 2017-08-10 | 2018-01-05 | 中国铝业股份有限公司 | A kind of internal heating type fused-salt bath |
| CN210683970U (en) * | 2019-07-08 | 2020-06-05 | 四川江铜稀土有限责任公司 | Double-graphite-groove rare earth electrolytic cell |
| CN111172562A (en) * | 2020-01-20 | 2020-05-19 | 镇江慧诚新材料科技有限公司 | Preparation method of fuel aluminum for aluminum-air battery |
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