CN216824632U - Treatment system for detoxifying overhaul slag of aluminum electrolysis cell - Google Patents
Treatment system for detoxifying overhaul slag of aluminum electrolysis cell Download PDFInfo
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- CN216824632U CN216824632U CN202123332822.4U CN202123332822U CN216824632U CN 216824632 U CN216824632 U CN 216824632U CN 202123332822 U CN202123332822 U CN 202123332822U CN 216824632 U CN216824632 U CN 216824632U
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- 229910052782 aluminium Inorganic materials 0.000 title claims abstract description 27
- 239000002893 slag Substances 0.000 title claims abstract description 22
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 title claims abstract description 21
- 238000005868 electrolysis reaction Methods 0.000 title claims description 10
- 238000010438 heat treatment Methods 0.000 claims abstract description 49
- 238000001704 evaporation Methods 0.000 claims abstract description 39
- 238000002156 mixing Methods 0.000 claims abstract description 28
- 239000007788 liquid Substances 0.000 claims abstract description 24
- 238000000926 separation method Methods 0.000 claims abstract description 23
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 35
- 230000014759 maintenance of location Effects 0.000 claims description 12
- 239000002002 slurry Substances 0.000 abstract description 42
- XFXPMWWXUTWYJX-UHFFFAOYSA-N Cyanide Chemical compound N#[C-] XFXPMWWXUTWYJX-UHFFFAOYSA-N 0.000 abstract description 13
- 238000001784 detoxification Methods 0.000 abstract description 9
- KRHYYFGTRYWZRS-UHFFFAOYSA-M Fluoride anion Chemical compound [F-] KRHYYFGTRYWZRS-UHFFFAOYSA-M 0.000 abstract description 8
- AZDRQVAHHNSJOQ-UHFFFAOYSA-N alumane Chemical compound [AlH3] AZDRQVAHHNSJOQ-UHFFFAOYSA-N 0.000 abstract description 7
- 239000004411 aluminium Substances 0.000 abstract description 4
- 239000013049 sediment Substances 0.000 abstract description 4
- 238000007255 decyanation reaction Methods 0.000 abstract description 3
- 238000006115 defluorination reaction Methods 0.000 abstract description 3
- 239000012065 filter cake Substances 0.000 abstract description 3
- 239000002699 waste material Substances 0.000 abstract description 3
- 239000003795 chemical substances by application Substances 0.000 abstract 1
- 150000003841 chloride salts Chemical class 0.000 abstract 1
- 238000002386 leaching Methods 0.000 description 21
- PUZPDOWCWNUUKD-UHFFFAOYSA-M sodium fluoride Chemical compound [F-].[Na+] PUZPDOWCWNUUKD-UHFFFAOYSA-M 0.000 description 16
- 238000000034 method Methods 0.000 description 13
- JMANVNJQNLATNU-UHFFFAOYSA-N oxalonitrile Chemical compound N#CC#N JMANVNJQNLATNU-UHFFFAOYSA-N 0.000 description 12
- 239000000843 powder Substances 0.000 description 11
- 238000000227 grinding Methods 0.000 description 10
- 239000007787 solid Substances 0.000 description 10
- 238000004537 pulping Methods 0.000 description 8
- 235000013024 sodium fluoride Nutrition 0.000 description 8
- 239000011775 sodium fluoride Substances 0.000 description 8
- 239000007791 liquid phase Substances 0.000 description 6
- 238000003756 stirring Methods 0.000 description 6
- 238000006243 chemical reaction Methods 0.000 description 5
- 238000009833 condensation Methods 0.000 description 5
- 230000005494 condensation Effects 0.000 description 5
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 4
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 4
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 4
- 239000011575 calcium Substances 0.000 description 4
- 229910052791 calcium Inorganic materials 0.000 description 4
- 238000005265 energy consumption Methods 0.000 description 4
- 239000011777 magnesium Substances 0.000 description 4
- 229910052749 magnesium Inorganic materials 0.000 description 4
- 239000000463 material Substances 0.000 description 4
- 238000005086 pumping Methods 0.000 description 4
- 150000003839 salts Chemical class 0.000 description 4
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 3
- 230000003139 buffering effect Effects 0.000 description 3
- 239000002244 precipitate Substances 0.000 description 3
- XTEGARKTQYYJKE-UHFFFAOYSA-M Chlorate Chemical compound [O-]Cl(=O)=O XTEGARKTQYYJKE-UHFFFAOYSA-M 0.000 description 2
- KXZJHVJKXJLBKO-UHFFFAOYSA-N chembl1408157 Chemical compound N=1C2=CC=CC=C2C(C(=O)O)=CC=1C1=CC=C(O)C=C1 KXZJHVJKXJLBKO-UHFFFAOYSA-N 0.000 description 2
- 125000001309 chloro group Chemical class Cl* 0.000 description 2
- 230000008020 evaporation Effects 0.000 description 2
- 150000002500 ions Chemical class 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000011780 sodium chloride Substances 0.000 description 2
- IRPGOXJVTQTAAN-UHFFFAOYSA-N 2,2,3,3,3-pentafluoropropanal Chemical compound FC(F)(F)C(F)(F)C=O IRPGOXJVTQTAAN-UHFFFAOYSA-N 0.000 description 1
- KLZUFWVZNOTSEM-UHFFFAOYSA-K Aluminum fluoride Inorganic materials F[Al](F)F KLZUFWVZNOTSEM-UHFFFAOYSA-K 0.000 description 1
- BDAGIHXWWSANSR-UHFFFAOYSA-M Formate Chemical compound [O-]C=O BDAGIHXWWSANSR-UHFFFAOYSA-M 0.000 description 1
- -1 aluminum ions Chemical class 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 238000000498 ball milling Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- WUKWITHWXAAZEY-UHFFFAOYSA-L calcium difluoride Chemical compound [F-].[F-].[Ca+2] WUKWITHWXAAZEY-UHFFFAOYSA-L 0.000 description 1
- 229910001634 calcium fluoride Inorganic materials 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 150000004673 fluoride salts Chemical class 0.000 description 1
- 239000002920 hazardous waste Substances 0.000 description 1
- XLYOFNOQVPJJNP-ZSJDYOACSA-N heavy water Substances [2H]O[2H] XLYOFNOQVPJJNP-ZSJDYOACSA-N 0.000 description 1
- 230000007062 hydrolysis Effects 0.000 description 1
- 238000006460 hydrolysis reaction Methods 0.000 description 1
- QWPPOHNGKGFGJK-UHFFFAOYSA-N hypochlorous acid Chemical compound ClO QWPPOHNGKGFGJK-UHFFFAOYSA-N 0.000 description 1
- ORUIBWPALBXDOA-UHFFFAOYSA-L magnesium fluoride Chemical compound [F-].[F-].[Mg+2] ORUIBWPALBXDOA-UHFFFAOYSA-L 0.000 description 1
- 229910001635 magnesium fluoride Inorganic materials 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 230000007935 neutral effect Effects 0.000 description 1
- 150000002825 nitriles Chemical class 0.000 description 1
- 229910000069 nitrogen hydride Inorganic materials 0.000 description 1
- 231100000252 nontoxic Toxicity 0.000 description 1
- 230000003000 nontoxic effect Effects 0.000 description 1
- 239000007800 oxidant agent Substances 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 150000003388 sodium compounds Chemical class 0.000 description 1
- 159000000000 sodium salts Chemical class 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
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Abstract
The utility model belongs to the technical field of electrolytic aluminum waste treatment, concretely relates to carry out processing system of detoxification to aluminium cell overhaul sediment. The treatment system comprises a mixing tank, a preheating device, a high-temperature heating section, a self-evaporation device and a solid-liquid separation device; the discharge port of the mixing tank is connected with the inlet of a preheating device, and the preheating device comprises a multistage preheating section; the tail end of the preheating device is connected with a high-temperature heating device; the tail end of the high-temperature heating device is connected with a self-evaporation device, the self-evaporation device comprises a multi-stage self-evaporator, and the tail end of the self-evaporation device is connected with a solid-liquid separation device. The fluoride in the overhaul slag of the aluminum electrolytic cell is leached under the conditions of high temperature and high pressure, and the cyanide is decomposed at the same time, so that the aims of removing the cyanide and defluorination are realized in one step, other agents are not needed, only heat energy needs to be consumed, and secondary steam generated by self-evaporation can also be used for preheating slurry; the filter cake after decyanation and defluorination does not contain chloride salt, thus being convenient for further comprehensive utilization.
Description
Technical Field
The utility model belongs to the technical field of electrolytic aluminum waste treatment, concretely relates to carry out processing system of detoxification to aluminium cell overhaul sediment.
Background
Aluminum cell overhaul residues are linings removed after cell breakage, which are listed as hazardous wastes due to fluoride/cyanide content. The existing overhaul slag treatment process comprises a fire method and a wet method, wherein the fire method cannot be popularized and applied due to high energy consumption, and the wet method treatment is the mainstream technology of the existing overhaul slag treatment. The wet processing line is to add oxidant into the overhaul slag to decompose and detoxify cyanide ions and add Ca2+/Mg2+/Al3+Corresponding fluoride salt precipitation detoxification is formed. The method has high efficiency and stable detoxification effect. However, this process simultaneously decomposes the cyanide and removes the precipitate of F ions, producing a soluble sodium salt, usually sodium chloride. Along with the repeated reaction, the concentration of sodium chloride is higher in the circulating water, and the waste liquid in the tailings after solid-liquid separation also brings more soluble salt into the tailings. The high content of soluble salts causes great difficulty in recycling the tailings.
The invention discloses a harmless treatment and recovery process of electrolytic bath overhaul residues or solid cyanide and fluoride-containing materials at normal temperature, which is characterized in that the electrolytic bath overhaul residues containing cyanide and fluoride are mixed with calcium, magnesium and sodium compounds which can be decomposed into hypochlorous acid in water and water-soluble calcium, magnesium and aluminum salts in a weight ratio of 1: 1 to be ground into pulp by water balls, cyanide is decomposed and reduced in a liquid phase of ball-milling pulp, and simultaneously water-soluble calcium, magnesium and aluminum salts release calcium, magnesium and aluminum ions to generate water-insoluble calcium fluoride, magnesium fluoride and harmless precipitates of aluminum fluoride in the liquid phase, and neutral water is separated from slurry after solid-liquid separation, so that the aim of harmless and non-discharge is achieved. The invention patent application generates soluble chlorine salt while decomposing cyanide and removing F ion precipitate.
Disclosure of Invention
The utility model discloses a do not contain the chlorine salt in making the tailings filter cake when optimizing resource utilization, low energy consumption remove cyanogen defluorination, adopt the highly compressed system of leaching of high temperature, leach the fluoride in the aluminium cell overhaul sediment under the highly compressed condition of high temperature, decompose the cyanide simultaneously, the high temperature ground paste will leach the thick liquid through multistage self-evaporation and fall to the ordinary pressure, the flash steam that the self-evaporation produced is used for preheating the ground paste. The utility model discloses but make full use of system's heat falls to the minimum with the energy consumption.
The overhaul slag of the aluminum electrolytic cell contains hypertoxic sodium cyanide, and the sodium cyanide is easy to dissolve in water. The utility model adopts a pressurization cyanogen removal method to remove the virulent cyanides in the overhaul residues, and simultaneously dissolve and recycle the soluble sodium fluoride in the overhaul residues.
The basic principle of the pressurized hydrolysis decyanation of the utility model is that cyanide aqueous solution is placed in a closed container, and under certain pressure and temperature conditions, the cyanide is decomposed into non-toxic or slightly-toxic compounds such as formate, ammonia and the like through certain reaction time. When cyanide in wastewater exists in a free state, the reaction equation is as follows: CN-+2H2O=HCOO-+NH3。
The utility model discloses a carry out the processing system of detoxification to aluminium cell overhaul sediment that adopts, include: the device comprises a mixing tank, a preheating device, a high-temperature heating device, a self-evaporation device and a solid-liquid separation device;
the mixing tank is used for mixing, stirring and pulping the overhaul slag grinding powder material of the aluminum electrolytic tank and clear water;
the preheating device comprises a plurality of stages of preheating sections, each stage of preheating section is of a sleeve structure, a discharge port of the mixing tank is connected with a tube pass inlet of the preheating device, and steam is introduced into a shell pass of the preheating device to preheat slurry in the tube pass;
the high-temperature heating device comprises a plurality of stages of high-temperature heating sections, each stage of high-temperature heating section is of a sleeve structure, the tail end of the preheating device is connected with a tube pass inlet of the high-temperature heating device, a shell pass of the high-temperature heating device is connected with a heat source, and the heat source adopts heat conduction oil or other heat sources such as high-temperature steam, molten salt and the like. After being treated by a high-temperature heating device, the leaching and cyanogen removal reaction of soluble fluoride in the slurry is completed in a retention tank.
The high-temperature heating device is characterized in that the end of the tube pass is connected with a self-evaporation device, the self-evaporation device is mainly used for reducing the pressure of the leached slurry to normal pressure from high pressure so as to be beneficial to liquid-solid separation under the normal pressure, secondary steam is released during self-evaporation, the secondary steam can be used for preheating the slurry, heat energy is utilized to the maximum extent, energy consumption in the overhaul slag detoxification treatment process is reduced, and resource utilization is optimized. The self-evaporation device comprises a multi-stage self-evaporator, the stage number of the self-evaporation device is one stage more than that of the preheating device, and except the final stage self-evaporator, the steam outlets of other self-evaporators are connected with the shell pass of the preheating device. The secondary steam generated by the evaporator is used for carrying out multi-stage preheating on the slurry in the tube pass of the preheating device.
The tail end of the self-evaporation device is connected with a solid-liquid separation device for separating the residue and liquid after self-evaporation.
In addition, the shell pass of each stage of preheating section of the preheating device is connected with a condensate water tank, the steam outlet of the self-evaporator is connected with the shell pass of each stage of preheating section through a pipeline, and a condensate water pipe connected with the condensate water tank is further arranged on the pipeline between the self-evaporator and the shell pass of each stage of preheating section. The condensate tank is used for receiving the shell side of the preheating device and condensate water generated by the evaporator.
Preferably, a retention tank is arranged between the high-temperature heating device and the self-evaporation device to ensure the leaching time of slurry reaction.
Preferably, a buffer tank is arranged between the end of the evaporator and the solid-liquid separation device for buffering the material, because the feed from the evaporator is continuous, while the solid-liquid separation device may be operated discontinuously, such as a filter press.
Preferably, the solid-liquid separation device is a filter press, or other solid-liquid separation devices can be adopted, and the leaching liquid tank is arranged below the filter press.
Preferably, the preheating device comprises two-stage to eight-stage preheating sections, the high-temperature heating device comprises two-stage high-temperature heating sections, and the self-evaporation device comprises three-stage to nine-stage self-evaporators.
The utility model discloses specific operation flow is as follows:
(1) grinding: grinding the overhaul slag of the aluminum electrolytic cell into powder to obtain overhaul slag fine powder with the granularity of less than 100 meshes, and then sending the powder into a mixing tank.
(2) Pulping: and adding clear water into the mixing tank according to the liquid-solid ratio of 3: 1-10: 1, and mixing and stirring to prepare the pulp.
(3) Leaching: pumping the slurry to a tube pass of a preheating device by using a pump, sequentially carrying out multistage preheating, and raising the temperature of the slurry to 140-180 ℃;
then heating to 200-300 ℃ by a high-temperature heating device, wherein the heat source of the high-temperature heating device adopts heat conduction oil or other heat sources such as high-temperature steam, molten salt and the like; after being treated by the preheating device and the high-temperature heating device, the leaching of the soluble fluoride and the decyanation reaction are completed.
Before entering a self-evaporation device, slurry enters a retention tank; the time of the slurry in the retention tank is set to be 40-100 min. Then the slurry is sequentially passed through a multi-stage self-evaporation device, the temperature is reduced to 105 ℃, self-evaporated secondary steam is used for preheating the slurry, and the generated condensed water can be returned to the mixing tank for pulping.
The preheating is performed before the high-temperature heating of the slurry, in order to utilize the secondary steam generated from the evaporator. The slurry is heated to a certain temperature and then heated to 200-300 ℃, so that the consumption of a heat source of a high-temperature heating device can be reduced.
When the slurry is heated in the tube pass of the high-temperature heating device, the temperature is 200-300 ℃, and the pressure is 1.5-8.5 MPa.
(4) And (3) performing liquid-solid separation on the slurry after temperature reduction, wherein most of NaF enters a liquid phase, and compared with the NaF leached at normal temperature, the leaching rate can be improved by more than 50%. Before solid-liquid separation, the slurry enters a buffer tank for buffering.
The utility model has the advantages that:
the utility model discloses the method has just realized removing cyanogen and the target of defluorinating on one step under the highly compressed condition of high temperature, and does not need other medicaments, only needs to consume heat energy, and removes the filter cake after cyanogen defluorinating and does not contain the chlorate, is convenient for further comprehensive utilization.
The utility model discloses a processing system reheats to the temperature of leaching after multistage preheating, and the flash steam that leaches the ground paste self-evaporation production is used for carrying out multistage preheating to the ground paste, has accomplished the maximize with the utilization of heat energy, and production operation consumption and cost have also fallen to minimumly.
Drawings
FIG. 1 is a schematic structural diagram of a treatment system for detoxifying overhaul residues of an aluminum electrolysis cell.
In the drawing, 1 is a mixing tank, 2 is a preheating device, 21 is a first-stage preheating section, 22 is a second-stage preheating section, 23 is a third-stage preheating section, 24 is a fourth-stage preheating section, 25 is a fifth-stage preheating section, 3 is a high-temperature heating device, 31 is a heat conducting oil heating section, 32 is a heat conducting oil furnace, 4 is a self-evaporation device, 41 is a first-stage self-evaporator, 42 is a second-stage self-evaporator, 43 is a third-stage self-evaporator, 44 is a fourth-stage self-evaporator, 45 is a fifth-stage self-evaporator, 46 is a sixth-stage self-evaporator, 5 is a filter press, 6 is a leaching liquid tank, 7 is a retention tank, 8 is a buffer tank, 91 is a first condensation water tank, 92 is a second condensation water tank, 93 is a third condensation water tank, 94 is a fourth condensation water tank, and 95 is a fifth condensation water tank.
Detailed Description
The present invention will be described in more detail with reference to the following embodiments, so as to facilitate the understanding of the technical solutions of the present invention, but the present invention is not limited to the scope of the present invention.
Example 1
As shown in fig. 1, the system for detoxifying overhaul slag of an aluminum electrolysis cell of the present embodiment includes: a mixing tank 1, a preheating device 2, a high-temperature heating device 3, a self-evaporation device 4 and a solid-liquid separation device;
the mixing tank 1 is used for mixing, stirring and pulping the overhaul slag grinding powder material of the aluminum electrolytic tank and clear water;
the preheating device 2 comprises five-stage preheating sections, each stage of preheating section is of a sleeve structure, a discharge port of the mixing tank 1 is connected with a tube side inlet of the preheating device 2, specifically, the five-stage sleeve structure comprises a first-stage preheating section 21, a second-stage preheating section 22, a third-stage preheating section 23, a fourth-stage preheating section 24 and a fifth-stage preheating section 25, and a discharge port of the mixing tank 1 is sequentially connected with the fifth-stage preheating section 25, the fourth-stage preheating section 24, the third-stage preheating section 23, the second-stage preheating section 22 and the first-stage preheating section 21;
the high-temperature heating device (3) comprises two-stage high-temperature heating sections, each stage of high-temperature heating section is of a sleeve structure, the tube pass end of the first-stage preheating section 21 is connected with the tube pass inlet of the high-temperature heating device 3, the shell pass of the high-temperature heating device 3 is connected with a heat source, and after the high-temperature heating device is used for processing, soluble fluoride in slurry is leached and cyanogen removal reaction is completed. The heat source of the embodiment adopts heat conduction oil, and specifically, the embodiment can adopt a heat conduction oil heating furnace 32 to provide heat conduction oil for the shell pass of the secondary heat conduction oil heating section 31.
The end-to-end connection of high temperature heating device 3 has and stops jar 7, and the discharge gate that stops jar 7 is connected from evaporation plant 4, and from evaporation plant 4 includes six grades of self evaporators: the steam outlets of the first-stage self-evaporator 41, the second-stage self-evaporator 42, the third-stage self-evaporator 43, the fourth-stage self-evaporator 44, the fifth-stage self-evaporator 45 and the sixth-stage self-evaporator 46 are respectively connected with the shell passes of the first-stage preheating section 21, the second-stage preheating section 22, the third-stage preheating section 23, the fourth-stage preheating section 24 and the fifth-stage preheating section 25 through pipelines. The six stages of vapor from evaporator 26 are vented to the atmosphere.
The tail end of the self-evaporation device 4 is connected with a buffer tank 8, and a discharge port of the buffer tank 8 is connected with a solid-liquid separation device for separating the residue and liquid after self-evaporation. The solid-liquid separation device of the embodiment is a filter press 5, and a leachate tank 6 is arranged below the filter press 5.
In addition, the shell pass of each stage of preheating section of the preheating device 2 is connected with a condensate water tank, specifically, the first stage preheating section 21, the second stage preheating section 22, the third stage preheating section 23, the fourth stage preheating section 24 and the fifth stage preheating section 25 are respectively connected with a first condensate water tank 91, a second condensate water tank 92, a third condensate water tank 93, a fourth condensate water tank 94 and a fifth condensate water tank 95, the condensate water tanks are communicated with one another, only the condensate water of the final fifth condensate water tank 95 is recovered, or the condensate water of the fifth condensate water tank 95 is returned to the mixing tank 1 for pulping. A condensate pipe connected with a condensate water tank is also arranged on a pipeline between the self-evaporator and the preheating section shell pass.
Example 2
The method for carrying out the aluminum electrolysis cell overhaul slag detoxification treatment by adopting the treatment system of the embodiment 1 comprises the following steps:
(1) grinding: grinding the overhaul slag of the aluminum electrolytic cell into fine powder (the granularity is less than 100 meshes), and detecting the F-leaching concentration at normal temperature to be 2410mg/L and the CN-concentration to be 7 mg/L; the powder is fed to a mixing tank.
(2) Pulping: adding clear water into the mixing tank according to the liquid-solid ratio of 10:1, and mixing and stirring to prepare the pulp.
(3) Leaching: pumping the slurry to a preheating device, sequentially carrying out five-stage preheating to increase the temperature of the slurry to 160 ℃, and then heating the slurry to 220 ℃ through a second-stage high-temperature heating section;
before entering the self-evaporation device, the slurry enters a retention tank, and the slurry stays in the retention tank for 40 min;
and then the slurry is sequentially subjected to six-stage self-evaporation, the temperature is reduced to 105 ℃, and the self-evaporated secondary steam is used for preheating the slurry in the preheating device.
(4) And (3) carrying out liquid-solid separation after the slurry after temperature reduction is buffered by a buffer tank, allowing most of NaF to enter a liquid phase, and detecting that the F-leaching concentration is 4761mg/L and the CN-concentration is 1mg/L, so that the leaching rate of sodium fluoride is improved by 97%.
Example 3
The method for carrying out the aluminum electrolysis cell overhaul slag detoxification treatment by adopting the treatment system of the embodiment 1 comprises the following steps:
(1) grinding: grinding the overhaul residues into fine powder (the granularity is less than 100 meshes), and detecting the F-leaching concentration to be 5855mg/L and the CN-concentration to be 12mg/L at normal temperature; the powder was fed to a mixing tank.
(2) Pulping: adding clear water according to the liquid-solid ratio of 5:1, mixing and stirring to prepare the pulp.
(3) Leaching: pumping the slurry to a preheating device in a mixing tank, sequentially carrying out five-stage preheating to increase the temperature of the slurry to 150 ℃, then heating to 200 ℃ through a two-stage high-temperature heating section, before entering a self-evaporation device, enabling the slurry to enter a retention tank, enabling the slurry to stay in the retention tank for 60min, sequentially carrying out six-stage self-evaporation on the slurry, reducing the temperature to 105 ℃, and preheating the slurry by using self-evaporated secondary steam.
(4) And (3) carrying out liquid-solid separation after the slurry after temperature reduction is buffered by a buffer tank, allowing most of NaF to enter a liquid phase, and detecting that the F-leaching concentration is 9744mg/L and the CN-concentration is 2mg/L, so that the leaching rate of sodium fluoride is improved by 66%.
Example 4
The method for carrying out the aluminum electrolysis cell overhaul slag detoxification treatment by adopting the treatment system of the embodiment 1 comprises the following steps:
(1) grinding: grinding the overhaul residues into fine powder (the granularity is less than 100 meshes), and detecting the F-leaching concentration to be 4335mg/L and the CN-concentration to be 20mg/L at normal temperature; the powder was fed to a mixing tank.
(2) Pulping: adding clear water into the mixing tank according to the liquid-solid ratio of 8:1, and mixing and stirring to prepare the pulp.
(3) Leaching: pumping the slurry to a preheating device, sequentially carrying out five-stage preheating to increase the temperature of the slurry to 180 ℃, then heating to 260 ℃ through a high-temperature heating section, before entering a self-evaporation device, enabling the slurry to enter a retention tank, enabling the slurry to stay in the retention tank for 90min, sequentially carrying out six-stage self-evaporation on the slurry, reducing the temperature to 105 ℃, and preheating the slurry by using self-evaporated secondary steam.
(4) And (3) buffering the slurry after cooling by a buffer tank, performing liquid-solid separation, and detecting a liquid phase, wherein the detected F-leaching concentration is 7266mg/L, the detected CN-concentration is 0.5mg/L, and the leaching rate of the sodium fluoride is improved by 67%.
The above-mentioned embodiments are merely preferred embodiments of the present invention, and not intended to limit the scope of the present invention, so that equivalent changes or modifications made by the structure, features and principles of the present invention should be included in the claims of the present invention.
Claims (6)
1. A treatment system for detoxifying overhaul slag of an aluminum electrolysis cell is characterized by comprising a mixing tank (1), a preheating device (2), a high-temperature heating device (3), a self-evaporation device (4) and a solid-liquid separation device;
the preheating device (2) comprises a plurality of stages of preheating sections, each stage of preheating section is of a sleeve structure, and a discharge port of the mixing tank (1) is connected with a tube pass inlet of the preheating device (2);
the high-temperature heating device (3) comprises a plurality of stages of high-temperature heating sections, each stage of high-temperature heating section is of a sleeve structure, the tail end of a tube side of the preheating device (2) is connected with a tube side inlet of the high-temperature heating device (3), and a shell side of the high-temperature heating device (3) is connected with a heat source;
the tail end of the tube pass of the high-temperature heating device (3) is connected with a self-evaporation device (4), the self-evaporation device (4) comprises a multi-stage self-evaporator, the stage number of the self-evaporation device (4) is one more stage than that of the preheating device (2), and except for a final stage self-evaporator, the steam outlets of other self-evaporators are connected with the shell pass of the preheating device (2);
the tail end of the self-evaporation device (4) is connected with a solid-liquid separation device.
2. The system for detoxifying the aluminum reduction cell overhaul slag according to claim 1,
the shell side of each stage of preheating section of the preheating device (2) is connected with a condensate water tank, the steam outlet of the self-evaporator is connected with the shell side of each stage of preheating section through a pipeline, and a condensate pipe connected with the condensate water tank is further arranged on the pipeline between the self-evaporator and the shell side of each stage of preheating section.
3. The treatment system for detoxifying the overhaul slag of the aluminum electrolysis cell according to claim 1, wherein a retention tank (7) is further arranged between the high temperature heating device (3) and the self-evaporation device (4).
4. The treatment system for detoxifying the overhaul slag of aluminum electrolytic cell according to claim 1, wherein a buffer tank (8) is provided between the tail end self-evaporator and the solid-liquid separation device.
5. The treatment system for detoxifying the overhaul residues of the aluminum electrolysis cell according to claim 1, wherein the solid-liquid separation device is a filter press (5), and a leachate tank (6) is arranged below the filter press (5).
6. The treatment system for detoxifying the aluminum reduction cell overhaul slag according to claim 1, wherein the preheating device (2) comprises two-eight stage preheating section, the high temperature heating device (3) comprises two-stage high temperature heating section, and the self-evaporation device (4) comprises three-nine stage self-evaporator.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN114377338A (en) * | 2021-12-28 | 2022-04-22 | 郑州鸿跃环保科技有限公司 | Treatment system and treatment method for detoxifying overhaul residues of aluminum electrolysis cell |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114377338A (en) * | 2021-12-28 | 2022-04-22 | 郑州鸿跃环保科技有限公司 | Treatment system and treatment method for detoxifying overhaul residues of aluminum electrolysis cell |
| CN114377338B (en) * | 2021-12-28 | 2024-07-30 | 郑州鸿跃环保科技有限公司 | Treatment system and treatment method for detoxification of aluminum electrolysis cell overhaul slag |
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