CN215236722U - Aluminum cell waste cathode carbon block treatment system - Google Patents
Aluminum cell waste cathode carbon block treatment system Download PDFInfo
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- CN215236722U CN215236722U CN202121339911.9U CN202121339911U CN215236722U CN 215236722 U CN215236722 U CN 215236722U CN 202121339911 U CN202121339911 U CN 202121339911U CN 215236722 U CN215236722 U CN 215236722U
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Abstract
The utility model discloses an aluminium cell waste cathode carbon block processing system belongs to aluminium electroloysis overhaul sediment and handles the field. This processing system includes broken grinding module, pressure leaching filter module, heavy fluorine and alkali recovery module, the water logging filters the module, neutralization filter module, washing filter module and collection cigarette module, broken grinding module, pressure leaching filter module, heavy fluorine and alkali recovery module, water logging filters the module, neutralization filter module, washing filter module connects gradually, broken grinding module, pressure leaching filter module, heavy fluorine and alkali recovery module, water logging filter module, neutralization filter module, washing filter module all is connected with collection cigarette module. The utility model can not only avoid the harm of the waste cathode carbon blocks of the aluminum electrolytic cell to the environment, but also realize the resource utilization of the waste cathode carbon blocks.
Description
Technical Field
The utility model relates to the technical field of aluminum electrolysis overhaul slag treatment, in particular to an aluminum electrolysis cell waste cathode carbon block treatment system.
Background
The aluminum electrolytic cell is a main device for metal aluminum smelting, the lining needs to be removed by major repair every 5 to 8 years, major repair slag is produced, and 15 to 20kg of major repair slag is discharged per ton of electrolytic aluminum raw aluminum. The aluminum electrolysis overhaul slag is mainly divided into two categories of waste cathode carbon blocks and waste refractory materials, the main toxic and harmful components are cyanide and soluble fluoride, and the aluminum electrolysis overhaul slag is listed in the national hazardous waste record in 2016.
In the aluminum electrolysis overhaul slag, the waste cathode carbon blocks account for about 55 percent, the waste refractory material accounts for about 45 percent, and the research direction of the aluminum electrolysis overhaul slag treatment is classified treatment due to different components of the waste cathode carbon blocks and the waste refractory material. The treatment process of the aluminum electrolysis overhaul slag comprises solidification stabilization landfill, wet detoxification, traditional pyrogenic process, flotation, pyrogenic process volatilization and other processes. The most common wet detoxification process is classified into acid decomposition, alkali decomposition, water leaching and the like. The solidification and stabilization landfill not only can not fully utilize resources, but also occupies valuable hazardous and useless landfill resources; the traditional pyrogenic process is incomplete in detoxification and cannot fully recover resources; the detoxification products of the existing wet process are difficult to utilize, resources are difficult to recycle, and the salt content of the wastewater is high; large investment for pyrogenic volatilization, high treatment cost and immature technology. The current technology is difficult to meet the requirements of resource recovery and increasingly strict environmental protection.
SUMMERY OF THE UTILITY MODEL
Aiming at the defects existing in the prior art, the utility model aims to provide a treatment system for waste cathode carbon blocks of an aluminum electrolytic cell. According to the utility model discloses an aluminium cell cathode carbon piece processing system that gives up on carrying out decyanation and defluorination innocent treatment, the basis of retrieving the carbon resource to aluminium cell overhaul sediment, extract fluorine and sodium ion wherein and carry out recycle, realized the purpose of resourceization.
In order to realize the purpose of the utility model, the utility model discloses a technical scheme as follows:
the utility model provides an aluminium cell waste cathode carbon block processing system, includes that broken grinding module, pressure leach filter module, heavy fluorine and alkali recovery module, water logging filter module, neutralization filter module, washing filter module and collection cigarette module, broken grinding module, pressure leach filter module, heavy fluorine and alkali recovery module, water logging filter module, neutralization filter module, washing filter module connect gradually, and this broken grinding module, pressure leach filter module, heavy fluorine and alkali recovery module, water logging filter module, neutralization filter module, washing filter module are connected with collection cigarette module respectively.
Further, the crushing and grinding module comprises a crusher, a ball mill and a vibrating screen, a discharge port of the crusher is communicated with a feed port of the ball mill, a discharge port of the ball mill is communicated with a feed port of the vibrating screen, and a discharge port of the vibrating screen is connected with the water immersion filtering module.
Further, the pressure leaching and filtering module comprises a slurry preparation tank, a high-temperature high-pressure reaction kettle, a pressure leaching and pressure filtering pump, a pressure leaching and pressure filtering machine, a pressure leaching filtrate tank and a pressure leaching filtrate pump, wherein a feed inlet of the slurry preparation tank is communicated with a discharge outlet of the vibrating screen, a feed inlet of the high-temperature high-pressure reaction kettle is communicated with a discharge port of the slurry preparation tank, a discharge outlet of the high-temperature high-pressure reaction kettle is communicated with a feed inlet of the pressure leaching and pressure filtering machine through the pressure leaching and pressure filtering pump, a liquid outlet of the pressure leaching and pressure leaching filtrate tank is communicated with the pressure leaching filtrate tank, the pressure leaching filtrate tank is respectively communicated with the slurry preparation tank through the pressure leaching filtrate pump, and the pressure leaching filtrate tank is connected with the fluorine precipitation and alkali recovery module through the pressure leaching filtrate pump.
Further, the fluorine and alkali recovery module includes a fluorine reaction tank, a fluorine sloping plate settling tank, a fluorine centrifugal settling machine, a calcium fluoride filter pressing pump, a calcium fluoride filter press, a fluorine filtrate tank and a fluorine filtrate pump, the feed inlet and the pressure leaching pump of the fluorine reaction tank are communicated, the discharge outlet of the fluorine reaction tank is communicated with the feed inlet of the fluorine sloping plate settling tank, the discharge outlet of the fluorine sloping plate settling tank is communicated with the feed inlet of the fluorine centrifugal settling machine, the discharge outlet of the fluorine centrifugal settling machine is communicated with the feed inlet of the calcium fluoride filter press through the calcium fluoride filter pressing pump, the liquid outlets of the fluorine sloping plate settling tank, the fluorine centrifugal settling machine and the calcium fluoride filter press are communicated with the inlet of the fluorine filtrate tank, and the liquid outlet of the fluorine filtrate tank is connected with the slurry preparation tank and an external caustic soda evaporation recovery device through the fluorine filtrate pump.
Further, the water immersion filtering module comprises a water immersion reaction tank, a water immersion filter press pump, a water immersion filter press, a water immersion filtrate tank and a water immersion filtrate pump, a feed inlet of the water immersion reaction tank is communicated with a discharge outlet of the filter press, the discharge outlet of the water immersion reaction tank is communicated with the feed inlet of the water immersion filter press through the water immersion filter press pump, a liquid outlet of the water immersion filter press is communicated with a liquid inlet of the water immersion filtrate tank, the liquid outlet of the water immersion filtrate tank is communicated with the feed inlet of the filter press through the water immersion filtrate pump, and the water immersion filtrate tank is connected with the neutralization module through the water immersion filtrate pump.
Further, the neutralization filtering module comprises a neutralization reaction tank, a neutralization pressure filter pump, a neutralization filter press, a neutralization filtrate tank and a neutralization filtrate pump, wherein a feed inlet of the neutralization reaction tank is communicated with a discharge outlet of the water immersion pressure filter, a discharge outlet of the neutralization reaction tank is communicated with a feed inlet of the neutralization filter press through the neutralization pressure filter pump, a liquid outlet of the neutralization filter press is communicated with a liquid inlet of the neutralization filtrate tank, and a liquid outlet of the neutralization filtrate tank is respectively communicated with the feed inlet of the water immersion filtrate tank and the feed inlet of the neutralization reaction tank through the neutralization filtrate pump.
Furthermore, the washing and filtering module comprises a washing reaction tank, a washing filter-pressing pump, a washing filter press, a washing filtrate tank and a washing filtrate pump, wherein a feed inlet of the washing reaction tank is communicated with a discharge outlet of the neutralization filter press, a discharge outlet of the washing reaction tank is communicated with a feed inlet of the washing filter press through the washing filter-pressing pump, a liquid outlet of the washing filter press is communicated with a liquid inlet of the washing filtrate tank, and a liquid outlet of the washing filtrate tank is respectively communicated with the feed inlet of the neutralization filter-pressing tank and the feed inlet of the washing reaction tank through the washing filtrate pump.
Furthermore, the smoke collecting module comprises two environment smoke collecting hoods, a cloth bag dust remover and a smoke collecting pipeline, wherein the two environment smoke collecting hoods are respectively arranged above the crusher and the ball mill, the two environment smoke collecting hoods are both communicated with the cloth bag dust remover, and a discharge port of the cloth bag dust remover is communicated with an external smoke treatment system through an environment smoke collecting main pipe; the slurry preparation tank, the fluorine precipitation reaction tank, the water immersion reaction tank, the neutralization reaction tank and the washing reaction tank are provided with top covers and are communicated with an environmental smoke collection main pipe through smoke collection branch pipes; the high-temperature high-pressure reaction kettle is sealed, and the top of the high-temperature high-pressure reaction kettle is communicated with an environment smoke collection main pipe through a smoke discharge branch pipe.
To sum up, owing to adopted above-mentioned technical scheme, the beneficial effects of the utility model are that:
(1) the medicament consumption is less: the utility model adopts the high-temperature and high-pressure alkaline leaching process, can fully break cyanogen under the conditions of high temperature and high pressure, and greatly reduces the consumption of cyanogen breaking agents; the liquid-solid ratio of high-temperature and high-pressure alkaline leaching is low, and the conversion from the insoluble fluoride to the soluble fluoride can be realized by using lower sodium hydroxide;
(2) the product purity is high: the utility model has the advantages that the dosage of the medicament is less, the chemical medicament which is easy to dissolve is mainly used, the solubility of the reaction product is high, and the carbon material and the calcium fluoride can reach higher product purity through simple washing;
(3) use the utility model discloses a system resource recycle rate is high, and carbon, fluorine and sodium alkali resource in the useless negative pole carbon block obtain abundant recycle.
(4) Is beneficial to continuous production: the utility model treats the waste cathode carbon blocks of the aluminum electrolytic cell step by step, which is beneficial to controlling the process index and realizing continuous production.
Drawings
FIG. 1 is a schematic process flow diagram of the present invention;
fig. 2 is a schematic diagram of the processing system of the present invention.
1-a crusher, 2-a ball mill, 3-a vibrating screen, 4-an environmental smoke collecting hood, 5-a bag dust collector, 6-a slurry preparation tank, 7-a high-temperature high-pressure reaction kettle, 8-a pressure immersion pressure filtration pump, 9-a pressure immersion pressure filtration machine, 10-a pressure immersion filtration tank, 11-a pressure immersion filtrate pump, 12-a fluorine precipitation reaction tank, 13-a fluorine precipitation inclined plate settling tank, 14-a fluorine precipitation centrifugal settling machine, 15-a calcium fluoride pressure filtration pump, 16-a calcium fluoride pressure filtration machine, 17-a fluorine immersion filtration tank, 18-a fluorine immersion filtration pump, 19-a water immersion reaction tank, 20-a water immersion pressure filtration pump, 21-a water immersion pressure filtration machine, 22-a water immersion filtration tank, 23-a water immersion filtration pump, 24-a neutralization reaction tank, 25-a neutralization pressure filtration pump, 26-a neutralization pressure filtration machine, 27-a neutralization filtrate tank, 28-a neutralization filtrate pump, 29-a washing reaction tank, 30-a washing filter-pressing pump, 31-a washing filter press, 32-a washing filtrate tank and 33-a washing filtrate pump.
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention more apparent, the following description will be given of preferred embodiments and further detailed description of the present invention. It should be understood, however, that the numerous specific details set forth in the specification are merely set forth to provide a thorough understanding of one or more aspects of the present invention, which may be practiced without these specific details.
The utility model provides an aluminium cell waste cathode carbon block processing system, includes that broken grinding module, pressure leach filter module, heavy fluorine and alkali recovery module, water logging filter module, neutralization filter module, washing filter module and collection cigarette module, broken grinding module, pressure leach filter module, heavy fluorine and alkali recovery module, water logging filter module, neutralization filter module, washing filter module connect gradually, and this broken grinding module, pressure leach filter module, heavy fluorine and alkali recovery module, water logging filter module, neutralization filter module, washing filter module are connected with collection cigarette module respectively.
The crushing and grinding module comprises a crusher 1, a ball mill 2 and a vibrating screen 3, a discharge port of the crusher 1 is communicated with a feed port of the ball mill 2, a discharge port of the ball mill 2 is communicated with a feed port of the vibrating screen 3, and a discharge port of the vibrating screen 3 is connected with the water immersion filtering module.
The pressure leaching filter module comprises a slurry preparation tank 6, a high-temperature high-pressure reaction kettle 7, a pressure leaching pressure filter pump 8, a pressure leaching pressure filter 9, a pressure leaching filtrate tank 10 and a pressure leaching filtrate pump 11, wherein a feed inlet of the slurry preparation tank 6 is communicated with a discharge outlet of a vibrating screen 3, a feed inlet of the high-temperature high-pressure reaction kettle 7 is communicated with a discharge outlet of the slurry preparation tank 6, a discharge outlet of the high-temperature high-pressure reaction kettle 7 is communicated with a feed inlet of the pressure leaching pressure filter 9 through the pressure leaching pressure filter pump 8, a liquid outlet of the pressure leaching pressure filter 9 is communicated with the pressure leaching filtrate tank 10, the pressure leaching filtrate tank 10 is respectively communicated with the slurry preparation tank 6 through the pressure leaching filtrate pump 11, and the pressure leaching filtrate tank 10 is connected with a fluorine precipitation and alkali recovery module through the pressure leaching filtrate pump 11.
The fluorine and alkali precipitation recovery module comprises a fluorine precipitation reaction tank 12, a fluorine precipitation inclined plate settling tank 13, a fluorine precipitation centrifugal settling machine 14, a calcium fluoride filter press pump 15, a calcium fluoride filter press 16, a fluorine precipitation filtrate tank 17 and a fluorine precipitation filtrate pump 18, the feed inlet of the fluorine precipitation reaction tank 12 is communicated with a pressure leaching filtrate pump 11, the discharge outlet of the fluorine precipitation reaction tank 12 is communicated with the feed inlet of a fluorine precipitation inclined plate settling tank 13, the discharge hole of the fluorine-settling sloping plate settling tank 13 is communicated with the feed hole of a fluorine-settling centrifugal settling machine 14, the discharge hole of the fluorine-precipitating centrifugal settler 14 is communicated with the feed inlet of a calcium fluoride filter press 16 through a calcium fluoride filter press pump 15, the liquid outlets of the fluorine-settling inclined plate settling tank 13, the fluorine-settling centrifugal settling machine 14 and the calcium fluoride filter press 16 are all communicated with the liquid inlet of a fluorine-settling filtrate tank 17, the liquid outlet of the fluorine precipitation filtrate tank 17 is connected with the slurry preparation tank 6 and an external caustic soda evaporation recovery device through a fluorine precipitation filtrate pump 18.
The water leaching filter module comprises a water leaching reaction tank 19, a water leaching filter pressing pump 20, a water leaching filter pressing machine 21, a water leaching filtrate tank 22 and a water leaching filtrate pump 23, wherein a feed inlet of the water leaching reaction tank 19 is communicated with a discharge outlet of the pressure leaching filter pressing machine 9, the discharge outlet of the water leaching reaction tank 19 is communicated with the feed inlet of the water leaching filter pressing machine 21 through the water leaching filter pressing pump 20, a liquid outlet of the water leaching filter pressing machine 21 is communicated with a liquid inlet of the water leaching filtrate tank 22, a liquid outlet of the water leaching filtrate tank 22 is communicated with the feed inlet of the pressure leaching reaction tank through the water leaching filtrate pump 23, and the water leaching filtrate tank 22 is connected with the neutralization module through the water leaching filtrate pump 23.
The neutralization filtering module comprises a neutralization reaction tank 24, a neutralization filter press 25, a neutralization filter press 26, a neutralization filtrate tank 27 and a neutralization filtrate pump 28, wherein a feed inlet of the neutralization reaction tank 24 is communicated with a discharge outlet of the water immersion filter press 21, a discharge outlet of the neutralization reaction tank 24 is communicated with a feed inlet of the neutralization filter press 26 through the neutralization filter press 25, a liquid outlet of the neutralization filter press 26 is communicated with a liquid inlet of the neutralization filtrate tank 27, and a liquid outlet of the neutralization filtrate tank 27 is respectively communicated with a feed inlet of the water immersion filtrate tank 22 and a feed inlet of the neutralization reaction tank 24 through the neutralization filtrate pump 28.
The washing and filtering module comprises a washing reaction tank 29, a washing filter-pressing pump 30, a washing filter press 31, a washing filtrate tank 32 and a washing filtrate pump 33, wherein a feed inlet of the washing reaction tank 29 is communicated with a discharge outlet of the neutralization filter press 26, a discharge outlet of the washing reaction tank 29 is communicated with a feed inlet of the washing filter press 31 through the washing filter-pressing pump 30, a liquid outlet of the washing filter press 31 is communicated with a liquid inlet of the washing filtrate tank 32, and a liquid outlet of the washing filtrate tank 32 is respectively communicated with a feed inlet of the neutralization filtrate tank 27 and a feed inlet of the washing reaction tank 29 through the washing filtrate pump 33.
The smoke collecting module comprises two environment smoke collecting hoods 4, a bag-type dust collector 5 and smoke collecting pipelines, wherein the two environment smoke collecting hoods 4 are respectively arranged above the crusher 1 and the ball mill 2, the two environment smoke collecting hoods 4 are both communicated with the bag-type dust collector 5, and a discharge port of the bag-type dust collector 5 is communicated with an external smoke treatment system through an environment smoke collecting main pipe; the slurry preparation tank 6, the fluorine precipitation reaction tank 12, the water immersion reaction tank 19, the neutralization reaction tank 24 and the washing reaction tank 29 are provided with top covers and are communicated with an environmental smoke collection main pipe through smoke collection branch pipes; the high-temperature high-pressure reaction kettle 7 is operated in a sealing mode, and the top of the high-temperature high-pressure reaction kettle 7 is communicated with the environment smoke collection main pipe through a smoke discharge branch pipe.
Examples 1 to 3 are specific operations for carrying out the treatment by the above-mentioned aluminum electrolytic cell waste cathode carbon block treatment system.
Example 1
The aluminum electrolytic cell waste cathode carbon block treatment steps are as follows:
A. crushing, ball milling and screening: crushing the waste cathode carbon blocks by using a crusher 1, feeding the crushed waste cathode carbon blocks with the particle size less than 20mm into a ball mill 2, carrying out ball milling for 2 hours, feeding the ball-milled powder into a vibrating screen 3, sieving the powder by using a screen with the specification of 2mm, and feeding qualified undersize into a slurry preparation tank 6; returning the screened residues and the powder material unqualified in the spot check to the ball mill 2 for continuous ball milling; crushing, grinding and screening the waste cathode carbon blocks to obtain powder with the granularity requirement of 160-180 meshes;
B. slurry preparation: adding sodium hydroxide, process water, pressure immersion liquid conveyed by a pressure immersion liquid filter pump 11 and defluorination pressure immersion liquid conveyed by a defluorination liquid filter pump 18 into a slurry preparation tank, preparing liquid according to the concentration of NaOH of 35g/L, adding qualified waste cathode carbon block powder obtained by ball milling in the step A according to the liquid-solid ratio of 3:1, stirring and preparing slurry at normal temperature to produce waste cathode carbon block slurry;
C. pressure leaching and cyanogen breaking: the waste cathode carbon block slurry prepared by the slurry preparation tank 6 automatically flows into the high-temperature high-pressure reaction kettle 7, high-pressure oxygen is introduced, and leaching and cyanogen breaking are carried out for 2 hours at the temperature of 185 ℃ and the pressure of 1.12 MPa; sampling to test for CN in pressure immersion liquid-The concentration is less than 1.0mg/L, after the pressure leaching residue sample is fully washed by clear water and the fluorine concentration for toxicity leaching test is less than 100mg/L, high-temperature and high-pressure leaching slurry is conveyed to a pressure leaching filter press 9 through a pressure leaching filter pump 8 for filter pressing to obtain pressure leaching residue and pressure leaching liquid, the pressure leaching residue is conveyed to a water leaching reaction tank 19, the pressure leaching liquid automatically flows into a pressure leaching liquid tank 10 and then is conveyed to a fluorine precipitation reaction tank 12 through a pressure leaching liquid pump 11 for fluorine precipitation, or is conveyed to a slurry preparation tank 6 for recycling;
D. water leaching: putting the pressure leaching slag produced by the pressure leaching filter press 9 into a water leaching reaction tank 19, stirring and leaching, wherein the liquid-solid ratio of a water leaching solution to the pressure leaching slag is 6:1, the reaction time is 2 hours, sampling and detecting the toxicity of the leaching slag, and after the fluorine concentration of a leaching slag toxicity leaching test is lower than 100mg/L, performing pressure filtration on a water leaching slurry conveyer belt water leaching filter press 21 through a water leaching filter press pump 20 to produce a water leaching filtrate and water leaching slag, conveying the water leaching slag to a neutralization reaction tank 24, automatically leaching the water leaching filtrate into a water leaching filtrate tank 22, and conveying the water leaching filtrate to the pressure leaching filtrate tank 10 or the water leaching filtrate tank 19 for recycling through a water leaching filtrate pump 23;
E. neutralizing: conveying the water leaching slag produced by the water leaching filter press 21 to a neutralization reaction tank 24, adding hydrochloric acid for neutralization, stirring at normal temperature, conveying the neutralized slurry to a neutralization filter press 26 through a neutralization filter press pump 25 for filter pressing after the pH value of the slurry is stabilized at 7-9 for more than 1 hour, producing neutralized filtrate and neutralized slag, conveying the neutralized slag to a washing reaction tank 29, automatically flowing the neutralized filtrate into a neutralized filtrate tank 27, and conveying the neutralized filtrate to a water leaching filtrate tank 22 or a neutralized reaction tank 24 through a neutralized filtrate pump 28 for recycling;
F. washing: conveying neutralized slag produced by the water neutralization filter press 26 to a washing reaction tank 29, stirring and washing clean water at normal temperature, after sampling detection is performed on the content of soluble salts in the leached slag to be lower than a control index, conveying washing slurry to a washing filter press 31 through a washing filter press pump 30 for filter pressing to produce washing filtrate and washing slag, automatically flowing the washing filtrate into a washing filtrate tank 32, conveying the washing filtrate to the neutralized filtrate tank 27 or the washing reaction tank 29 through a washing filtrate pump 33 for recycling, and detecting the content of fluorine in a toxicity leaching test to be less than 100mg/L, wherein CN is CN-<5mg/L washing slag is a carbon material which is sold as a product;
G. and (3) recovering calcium fluoride: stirring the pressure leaching solution from a pressure leaching filtrate pump 11 in a fluorine precipitation reaction tank 12 at normal temperature, adding calcium chloride according to 1.05 times (calcium ion meter) of the theoretical dosage of the reaction of calcium ions and fluorine ions to carry out fluorine precipitation treatment on the pressure leaching solution, wherein the reaction time is 1h, the fluorine precipitation slurry automatically flows into a fluorine precipitation inclined plate settling tank 13 for settling, then the bottom slurry is put into a fluorine precipitation centrifugal settling machine 14 for centrifugal separation, the slurry produced by the centrifugal settling machine 14 is conveyed to a calcium fluoride filter press 16 by a calcium fluoride filter press pump 15 for filter pressing, the produced calcium fluoride (product), the fluorine precipitation filtrate generated by the fluorine precipitation inclined plate settling tank 13 and the centrifugal settling machine 14 automatically flows into a fluorine precipitation filtrate tank 17, and the fluorine precipitation filtrate is conveyed to a slurry preparation tank 6 for recycling by a fluorine precipitation filtrate pump 18 or conveyed to the outside by the fluorine precipitation filtrate pump 18 for evaporation and recovery of caustic soda;
H. collecting flue gas: after being collected by a smoke collecting hood 4, the dust-containing smoke generated by the crusher 1, the ball mill 2 and the vibrating screen 3 is sent to a bag-type dust remover 5 for dust removal treatment, and the smoke subjected to the dust removal treatment by the bag-type dust remover 5 is converged into a smoke main pipe; the equipment such as the slurry preparation tank 6, the high-temperature high-pressure reaction kettle 7, the fluorine precipitation reaction tank 12, the water immersion reaction tank 19, the neutralization reaction tank 24 and the washing reaction tank 29 introduces flue gas into a flue gas main pipe through a flue gas suction port at the top of each equipment, joins with flue gas subjected to dust removal treatment by the bag-type dust remover 5, and is discharged after reaching the standard after being sent to an external flue gas treatment system for treatment.
I. Treatment effect;
the components of the waste cathode carbon block of the aluminum electrolytic cell before treatment are as follows:
| composition (I) | C | NaF | CaF2 | Na3AlF6 | CaO |
| ％ | 69.35 | 15.55 | 0.54 | 2.94 | 1.55 |
| Composition (I) | MgO | SiO2 | Fe | Na2O | CN- |
| ％ | 0.87 | 4.96 | 1.18 | 2.372 | 0.08 |
The method is characterized in that leaching toxicity and corrosivity of carbon materials (main products) are identified, the carbon materials are judged to reach the standard, and detection data and judgment are shown in the following table:
in the above table, the leaching toxicity of the sample is detected according to the sulfuric acid-nitric acid method of the leaching toxicity leaching method of HJT 299-2007 solid waste, and in the leaching toxicity detection result, F-The concentration is identified according to the limit value of I-type industrial solid waste, and the cyanogen is identified according to the limit value specified in GB 5085.3-2007 identification standard leaching toxicity identification of hazardous waste; corrosivity leachate was prepared according to the "GB/T15555.12-1995 glass electrode method for identifying corrosivity of solid wastes", and identified according to the standard limits of the "GB 5085.1 Standard for identifying corrosivity of hazardous wastes".
According to the general rule of GB 5085.7-2019 hazardous waste identification Standard 6.2, the solid waste generated in the hazardous waste utilization process with the toxic hazardous characteristic is identified to be no longer hazardous and not to be hazardous waste, and the main product carbon material in the case is no longer hazardous and can be sold as a product. The byproduct saline-alkali solution containing fluorine and cyanogen has qualified indexes and no toxic and harmful components, and is reused for desulfurization.
The consumption of the refractory auxiliary material and the product yield per 100 tons of the waste refractory in this case are shown in the following table:
the cyanide breaking agent is not digested in the case.
Example 2
Example 2 aluminum cell waste cathode carbon block treatment steps are as follows:
A. crushing, ball milling and screening: crushing the waste cathode carbon blocks by using a crusher 1, feeding the crushed waste cathode carbon blocks with the particle size less than 20mm into a ball mill 2, carrying out ball milling for 2 hours, feeding the ball-milled powder into a vibrating screen 3, sieving the powder by using a screen with the specification of 2mm, and feeding qualified undersize into a slurry preparation tank 6; returning the screened residues and the powder material unqualified in the spot check to the ball mill 2 for continuous ball milling; crushing, grinding and screening the waste cathode carbon blocks to obtain powder with the granularity requirement of 160-180 meshes;
B. slurry preparation: adding sodium hydroxide, process water, pressure immersion liquid conveyed by a pressure immersion liquid filter pump 11 and defluorination pressure immersion liquid conveyed by a defluorination liquid filter pump 18 into a slurry preparation tank, preparing liquid according to the concentration of NaOH of 35g/L, adding qualified waste cathode carbon block powder obtained by ball milling in the step A according to the liquid-solid ratio of 3:1, stirring and preparing slurry at normal temperature to produce waste cathode carbon block slurry;
C. pressure leaching and cyanogen breaking: the waste cathode carbon block slurry prepared by the slurry preparation tank 6 automatically flows into a high-temperature high-pressure reaction kettle 7, sodium hypochlorite (with the effective chlorine content of 10%) is added according to 3.0 times of the theoretical amount, and leaching and cyanogen breaking are carried out for 2 hours at the temperature of 185 ℃ and the pressure of 1.12 MPa; sampling to test for CN in pressure immersion liquid-The concentration is less than 1.0mg/L, after the pressure leaching residue sample is fully washed by clear water and the fluorine concentration for toxicity leaching test is less than 100mg/L, high-temperature and high-pressure leaching slurry is conveyed to a pressure leaching filter press 9 through a pressure leaching filter pump 8 for filter pressing to obtain pressure leaching residue and pressure leaching liquid, the pressure leaching residue is conveyed to a water leaching reaction tank 19, the pressure leaching liquid automatically flows into a pressure leaching liquid tank 10 and then is conveyed to a fluorine precipitation reaction tank 12 through a pressure leaching liquid pump 11 for fluorine precipitation, or is conveyed to a slurry preparation tank 6 for recycling;
D. water leaching: putting the pressure leaching slag produced by the pressure leaching filter press 9 into a water leaching reaction tank 19, stirring and leaching, wherein the liquid-solid ratio of a water leaching solution to the pressure leaching slag is 6:1, the reaction time is 3 hours, sampling and detecting the toxicity of the leaching slag, and after the fluorine concentration of a leaching slag toxicity leaching test is lower than 100mg/L, performing pressure filtration on a water leaching slurry conveyer belt water leaching filter press 21 through a water leaching filter press pump 20 to produce a water leaching filtrate and water leaching slag, conveying the water leaching slag to a neutralization reaction tank 24, automatically leaching the water leaching filtrate into a water leaching filtrate tank 22, and conveying the water leaching filtrate to the pressure leaching filtrate tank 10 or the water leaching filtrate tank 19 for recycling through a water leaching filtrate pump 23;
E. neutralizing: conveying the water leaching slag produced by the water leaching filter press 21 to a neutralization reaction tank 24, adding hydrochloric acid for neutralization, stirring at normal temperature, conveying the neutralized slurry to a neutralization filter press 26 through a neutralization filter press pump 25 for filter pressing after the pH value of the slurry is stabilized at 7-9 for more than 1 hour, producing neutralized filtrate and neutralized slag, conveying the neutralized slag to a washing reaction tank 29, automatically flowing the neutralized filtrate into a neutralized filtrate tank 27, and conveying the neutralized filtrate to a water leaching filtrate tank 22 or a neutralized reaction tank 24 through a neutralized filtrate pump 28 for recycling;
F. washing: conveying neutralized slag produced by the water neutralization filter press 26 to a washing reaction tank 29, stirring and washing with clean water at normal temperature, after sampling detection that the content of soluble salts in the leached slag is lower than a control index, conveying washing slurry to a washing filter press 31 through a washing filter press pump 30 for filter pressing to produce washing filtrate and washing slag, automatically flowing the washing filtrate into a washing filtrate tank 32, conveying the washing filtrate to the neutralized filtrate tank 27 or the washing reaction tank 29 through a washing filtrate pump 33 for recycling, and detecting that the content of fluorine is less than 100mg/L in a toxicity leaching test, wherein CN-<5mg/L washing slag is a carbon material which is sold as a product;
G. and (3) recovering calcium fluoride: stirring the pressure leaching solution from a pressure leaching filtrate pump 11 in a fluorine precipitation reaction tank 12 at normal temperature, adding calcium chloride according to 1.05 times (calcium ion meter) of the theoretical dosage of the reaction of calcium ions and fluorine ions to carry out fluorine precipitation treatment on the pressure leaching solution, wherein the reaction time is 2h, the fluorine precipitation slurry automatically flows into a fluorine precipitation inclined plate settling tank 13 for settling, then the bottom slurry is put into a fluorine precipitation centrifugal settling machine 14 for centrifugal separation, the slurry produced by the centrifugal settling machine 14 is conveyed to a calcium fluoride filter press 16 by a calcium fluoride filter press pump 15 for filter pressing to produce calcium fluoride (product), the fluorine precipitation filtrate produced by the fluorine precipitation inclined plate settling tank 13 and the centrifugal settling machine 14 automatically flows into a fluorine precipitation filtrate tank 17, and the fluorine precipitation filtrate is conveyed to a slurry preparation tank 6 for recycling by a fluorine precipitation filtrate pump 18 or conveyed to the outside by the fluorine precipitation filtrate pump 18 for evaporation and recovery of caustic soda;
H. collecting flue gas: after being collected by a smoke collecting hood 4, the dust-containing smoke generated by the crusher 1, the ball mill 2 and the vibrating screen 3 is sent to a bag-type dust remover 5 for dust removal treatment, and the smoke subjected to the dust removal treatment by the bag-type dust remover 5 is converged into a smoke main pipe; the equipment such as the slurry preparation tank 6, the high-temperature high-pressure reaction kettle 7, the fluorine precipitation reaction tank 12, the water immersion reaction tank 19, the neutralization reaction tank 24 and the washing reaction tank 29 introduces flue gas into a flue gas main pipe through a flue gas suction port at the top of each equipment, joins with flue gas subjected to dust removal treatment by the bag-type dust remover 5, and is discharged after reaching the standard after being sent to an external flue gas treatment system for treatment.
I. Treatment effect;
the components of the waste cathode carbon block of the aluminum electrolytic cell before treatment are as follows:
| composition (I) | C | NaF | CaF2 | Na3AlF6 | CaO |
| ％ | 66.45 | 16.48 | 1.65 | 3.54 | 1.65 |
| Composition (I) | MgO | SiO2 | Fe | Na2O | CN- |
| ％ | 1.06 | 4.12 | 1.26 | 2.42 | 0.11 |
The leaching toxicity and corrosivity of the carbon material (main product) are identified, the carbon material is judged to reach the standard, and the detection data and the judgment result are shown in the following table:
in the above table, the leaching toxicity of the sample is detected according to the sulfuric acid-nitric acid method of the leaching toxicity leaching method of HJT 299-2007 solid waste, and in the leaching toxicity detection result, F-The concentration is identified according to the limit value of I-type industrial solid waste, and the cyanogen is identified according to the limit value specified in GB 5085.3-2007 identification standard leaching toxicity identification of hazardous waste; corrosivity leachate was prepared according to the "GB/T15555.12-1995 glass electrode method for identifying corrosivity of solid wastes", and identified according to the standard limits of the "GB 5085.1 Standard for identifying corrosivity of hazardous wastes".
According to the general rule of GB 5085.7-2019 hazardous waste identification Standard 6.2, the solid waste generated in the hazardous waste utilization process with toxic hazardous characteristics is identified to be no longer hazardous and not hazardous waste, the main product carbon material in the case is no longer hazardous waste and can be sold as a product, and the byproduct salt and alkali-containing liquid fluorine and cyanogen is qualified in index and free of toxic and harmful components and is reused for desulfurization.
The consumption of the refractory auxiliary material and the product yield per 100 tons of the waste refractory in this case are shown in the following table:
the utility model adopts the above process and processing system to process the waste cathode carbon blocks of the aluminum electrolytic cell, the carbon in the waste cathode carbon blocks can be ensured to be recycled, and the resources such as fluorine and Na in the waste cathode carbon blocks can be recycled, thereby realizing the comprehensive utilization of the resources.
Example 3
The treatment steps of the waste refractory materials of the aluminum electrolytic cell are as follows:
A. crushing, ball milling and screening: crushing the waste cathode carbon blocks by using a crusher 1, feeding the crushed waste cathode carbon blocks with the particle size less than 20mm into a ball mill 2, carrying out ball milling for 2 hours, feeding the ball-milled powder into a vibrating screen 3, sieving the powder by using a screen with the specification of 2mm, and feeding qualified undersize into a slurry preparation tank 6; returning the screened residues and the powder material unqualified in the spot check to the ball mill 2 for continuous ball milling; crushing, grinding and screening the waste cathode carbon blocks to obtain powder with the granularity requirement of 160-180 meshes;
B. slurry preparation: adding sodium hydroxide, process water, pressure immersion liquid conveyed by a pressure immersion liquid filter pump 11 and defluorination pressure immersion liquid conveyed by a defluorination liquid filter pump 18 into a slurry preparation tank, preparing liquid according to the concentration of NaOH of 35g/L, adding qualified waste cathode carbon block powder obtained by ball milling in the step A according to the liquid-solid ratio of 3:1, stirring and preparing slurry at normal temperature to produce waste cathode carbon block slurry;
C. pressure leaching and cyanogen breaking: the waste cathode carbon block slurry prepared by the slurry preparation tank 6 automatically flows into a high-temperature high-pressure reaction kettle 7, sodium hypochlorite (with the effective chlorine content of 10%) is added according to 3 times of the theoretical amount, and leaching and cyanogen breaking are carried out for 2 hours at the temperature of 185 ℃ and the pressure of 1.12 MPa; sampling to test for CN in pressure immersion liquid-The concentration is less than 1.0mg/L, the fluorine concentration of the pressure leaching residue sample is less than 100mg/L after being fully washed by clear water and subjected to toxicity leaching test, and the high temperature is carried out by a pressure leaching pressure filtration pump 8Conveying the high-pressure leaching slurry to a pressure leaching pressure filter 9 for pressure filtration to obtain pressure leaching residue and pressure leaching filtrate, conveying the pressure leaching residue to a water leaching reaction tank 19, automatically flowing the pressure leaching filtrate into a pressure leaching filtrate tank 10, conveying the pressure leaching filtrate to a fluorine precipitation reaction tank 12 for fluorine precipitation through a pressure leaching filtrate pump 11, or conveying the pressure leaching filtrate to a slurry preparation tank 6 for recycling;
D. water leaching: putting the pressure leaching slag produced by the pressure leaching filter press 9 into a water leaching reaction tank 19, stirring and leaching, wherein the liquid-solid ratio of a water leaching solution to the pressure leaching slag is 6:1, the reaction time is 3 hours, sampling and detecting the toxicity of the leaching slag, and after the fluorine concentration of a leaching slag toxicity leaching test is lower than 100mg/L, performing pressure filtration on a water leaching slurry conveyer belt water leaching filter press 21 through a water leaching filter press pump 20 to produce a water leaching filtrate and water leaching slag, conveying the water leaching slag to a neutralization reaction tank 24, automatically leaching the water leaching filtrate into a water leaching filtrate tank 22, and conveying the water leaching filtrate to the pressure leaching filtrate tank 10 or the water leaching filtrate tank 19 for recycling through a water leaching filtrate pump 23;
E. neutralizing: conveying the water leaching slag produced by the water leaching filter press 21 to a neutralization reaction tank 24, adding hydrochloric acid for neutralization, stirring at normal temperature, conveying the neutralized slurry to a neutralization filter press 26 through a neutralization filter press pump 25 for filter pressing after the pH value of the slurry is stabilized at 7-9 for more than 1 hour, producing neutralized filtrate and neutralized slag, conveying the neutralized slag to a washing reaction tank 29, automatically flowing the neutralized filtrate into a neutralized filtrate tank 27, and conveying the neutralized filtrate to a water leaching filtrate tank 22 or a neutralized reaction tank 24 through a neutralized filtrate pump 28 for recycling;
F. washing: conveying neutralized slag produced by the water neutralization filter press 26 to a washing reaction tank 29, stirring and washing with clean water at normal temperature, after sampling detection that the content of soluble salts in the leached slag is lower than a control index, conveying washing slurry to a washing filter press 31 through a washing filter press pump 30 for filter pressing to produce washing filtrate and washing slag, automatically flowing the washing filtrate into a washing filtrate tank 32, conveying the washing filtrate to the neutralized filtrate tank 27 or the washing reaction tank 29 through a washing filtrate pump 33 for recycling, and detecting that the content of fluorine is less than 100mg/L in a toxicity leaching test, wherein CN-<5mg/L washing slag is a carbon material which is sold as a product;
G. and (3) recovering calcium fluoride: stirring the pressure leaching solution from a pressure leaching filtrate pump 11 in a fluorine precipitation reaction tank 12 at normal temperature, adding calcium chloride according to 1.05 times (calcium ion meter) of the theoretical dosage of the reaction of calcium ions and fluorine ions to carry out fluorine precipitation treatment on the pressure leaching solution, wherein the reaction time is 2h, the fluorine precipitation slurry automatically flows into a fluorine precipitation inclined plate settling tank 13 for settling, then the bottom slurry is put into a fluorine precipitation centrifugal settling machine 14 for centrifugal separation, the slurry produced by the centrifugal settling machine 14 is conveyed to a calcium fluoride filter press 16 by a calcium fluoride filter press pump 15 for filter pressing to produce calcium fluoride (product), the fluorine precipitation filtrate produced by the fluorine precipitation inclined plate settling tank 13 and the centrifugal settling machine 14 automatically flows into a fluorine precipitation filtrate tank 17, and the fluorine precipitation filtrate is conveyed to a slurry preparation tank 6 for recycling by a fluorine precipitation filtrate pump 18 or conveyed to the outside by the fluorine precipitation filtrate pump 18 for evaporation and recovery of caustic soda;
H. collecting flue gas: after being collected by a smoke collecting hood 4, the dust-containing smoke generated by the crusher 1, the ball mill 2 and the vibrating screen 3 is sent to a bag-type dust remover 5 for dust removal treatment, and the smoke subjected to the dust removal treatment by the bag-type dust remover 5 is converged into a smoke main pipe; the equipment such as the slurry preparation tank 6, the high-temperature high-pressure reaction kettle 7, the fluorine precipitation reaction tank 12, the water immersion reaction tank 19, the neutralization reaction tank 24 and the washing reaction tank 29 introduces flue gas into a flue gas main pipe through a flue gas suction port at the top of each equipment, joins with flue gas subjected to dust removal treatment by the bag-type dust remover 5, and is discharged after reaching the standard after being sent to an external flue gas treatment system for treatment.
I. Treatment effect;
the components of the waste cathode carbon block of the aluminum electrolytic cell before treatment are as follows:
| composition (I) | C | NaF | CaF2 | Na3AlF6 | CaO |
| ％ | 66.12 | 16.02 | 1.65 | 3.62 | 1.66 |
| Composition (I) | MgO | SiO2 | Fe | Na2O | CN- |
| ％ | 1.06 | 4.81 | 1.26 | 2.49 | 0.09 |
The leaching toxicity and corrosivity of the carbon material (main product) are identified, the carbon material is judged to reach the standard, and the detection data and the judgment result are shown in the following table:
in the above table, the leaching toxicity of the sample is detected according to the sulfuric acid-nitric acid method of the leaching toxicity leaching method of HJT 299-2007 solid waste, and in the leaching toxicity detection result, F-The concentration is identified according to the limit value of I-type industrial solid waste, and the cyanogen is identified according to the limit value specified in GB 5085.3-2007 identification standard leaching toxicity identification of hazardous waste; corrosiveness leachate was prepared according to GB/T15555.12-1995 evaluation of corrosiveness of solid wastes on glass electrodesStandard limits of GB 5085.1 Standard for identifying hazardous waste corrosivity identification.
According to the general rule of GB 5085.7-2019 hazardous waste identification Standard 6.2, the solid waste generated in the hazardous waste utilization process with toxic hazardous characteristics is identified to be no longer hazardous and not hazardous waste, the main product carbon material in the case is no longer hazardous waste and can be sold as a product, and the byproduct salt and alkali-containing liquid fluorine and cyanogen is qualified in index and free of toxic and harmful components and is reused for desulfurization.
The consumption of the refractory auxiliary material and the product yield per 100 tons of the waste refractory in this case are shown in the following table:
the process and the treatment system are adopted to treat the waste cathode carbon blocks of the aluminum electrolytic cell, so that the carbon in the waste cathode carbon blocks can be recycled, the resources such as fluorine, Na and the like in the waste cathode carbon blocks can be recycled, and the comprehensive utilization of the resources is realized.
The foregoing is only a preferred embodiment of the present invention, and it should be noted that, for those skilled in the art, a plurality of modifications and decorations can be made without departing from the principle of the present invention, and these modifications and decorations should also be regarded as the protection scope of the present invention.
Claims (8)
1. The utility model provides an aluminium cell waste cathode carbon block processing system, its characterized in that, includes broken grinding module, pressure leaching filter module, sinks fluorine and alkali recovery module, water logging filter module, neutralization filter module, washing filter module and collection cigarette module, broken grinding module, pressure leaching filter module, heavy fluorine and alkali recovery module, water logging filter module, neutralization filter module, washing filter module connect gradually, and this broken grinding module, pressure leaching filter module, heavy fluorine and alkali recovery module, water logging filter module, neutralization filter module, washing filter module are connected with collection cigarette module respectively.
2. The aluminum electrolytic cell waste cathode carbon block processing system according to claim 1, wherein the crushing and grinding module comprises a crusher, a ball mill and a vibrating screen, a discharge port of the crusher is communicated with a feed port of the ball mill, a discharge port of the ball mill is communicated with a feed port of the vibrating screen, and a discharge port of the vibrating screen is connected with the water immersion filtering module.
3. The aluminum electrolysis cell waste cathode carbon block processing system according to claim 2, wherein the pressure leaching and filtering module comprises a slurry preparation tank, a high temperature and high pressure reaction kettle, a pressure leaching and pressure filtering pump, a pressure leaching press, a pressure leaching filtrate tank and a pressure leaching filtrate pump, wherein a feed inlet of the slurry preparation tank is communicated with a discharge outlet of the vibrating screen, a feed inlet of the high temperature and high pressure reaction kettle is communicated with a discharge outlet of the slurry preparation tank, a discharge outlet of the high temperature and high pressure reaction kettle is communicated with a feed inlet of the pressure leaching press through the pressure leaching and pressure filtering pump, a liquid outlet of the pressure leaching press is communicated with the pressure leaching filtrate tank, the pressure leaching filtrate tanks are respectively communicated with the slurry preparation tank through the pressure leaching filtrate pump, and the pressure leaching filtrate tank is connected with the fluorine precipitation and alkali recovery module through the pressure leaching filtrate pump.
4. The aluminum electrolysis cell waste cathode carbon block processing system according to claim 3, the fluorine and alkali precipitation recovery module comprises a fluorine precipitation reaction tank, a fluorine precipitation inclined plate settling tank, a fluorine precipitation centrifugal settling machine, a calcium fluoride filter press pump, a calcium fluoride filter press, a fluorine precipitation filtrate tank and a fluorine precipitation filtrate pump, the feed inlet of the fluorine-precipitating reaction tank is communicated with a pressure leaching filtrate pump, the discharge outlet of the fluorine-precipitating reaction tank is communicated with the feed inlet of a fluorine-precipitating inclined plate settling tank, the discharge hole of the fluorine-precipitating inclined plate settling tank is communicated with the feed inlet of a fluorine-precipitating centrifugal settling machine, the discharge hole of the fluorine-precipitating centrifugal settling machine is communicated with the feed inlet of a calcium fluoride filter press through a calcium fluoride filter press pump, the liquid outlets of the fluorine-settling inclined plate settling tank, the fluorine-settling centrifugal settling machine and the calcium fluoride filter press are all communicated with the liquid inlet of the fluorine-settling filtrate tank, and the liquid outlet of the fluorine precipitation filtrate tank is connected with the slurry preparation tank and the external caustic soda evaporation and recovery device through a fluorine precipitation filtrate pump.
5. The aluminum electrolysis cell waste cathode carbon block processing system according to claim 4, wherein the water leaching and filtering module comprises a water leaching reaction tank, a water leaching filter press, a water leaching filtrate tank and a water leaching filtrate pump, a feed inlet of the water leaching reaction tank is communicated with a discharge outlet of the pressure leaching filter, a discharge outlet of the water leaching reaction tank is communicated with a feed inlet of the water leaching filter press through the water leaching filter press, a liquid outlet of the water leaching filter press is communicated with a liquid inlet of the water leaching filtrate tank, a liquid outlet of the water leaching filtrate tank is communicated with a feed inlet of the pressure leaching reaction tank through the water leaching filtrate pump, and the water leaching filtrate tank is connected with the neutralization module through the water leaching filtrate pump.
6. The aluminum electrolysis cell waste cathode carbon block processing system according to claim 5, wherein the neutralization filtration module comprises a neutralization reaction cell, a neutralization filter press pump, a neutralization filter press, a neutralization filtrate tank and a neutralization filtrate pump, wherein a feed inlet of the neutralization reaction cell is communicated with a discharge outlet of the water immersion filter press, a discharge outlet of the neutralization reaction cell is communicated with a feed inlet of the neutralization filter press through the neutralization filter press pump, a liquid outlet of the neutralization filter press is communicated with a liquid inlet of the neutralization filtrate tank, and a liquid outlet of the neutralization filtrate tank is respectively communicated with a feed inlet of the water immersion filtrate tank and a feed inlet of the neutralization reaction cell through the neutralization filtrate pump.
7. The aluminum electrolysis cell waste cathode carbon block processing system according to claim 6, wherein the washing and filtering module comprises a washing reaction cell, a washing filter press pump, a washing filter press, a washing filtrate tank and a washing filtrate pump, wherein a feed inlet of the washing reaction cell is communicated with a discharge outlet of the neutralization filter press, a discharge outlet of the washing reaction cell is communicated with a feed inlet of the washing filter press through the washing filter press pump, a liquid outlet of the washing filter press is communicated with a liquid inlet of the washing filtrate tank, and a liquid outlet of the washing filtrate tank is respectively communicated with a feed inlet of the neutralization filtrate tank and a feed inlet of the washing reaction cell through the washing filtrate pump.
8. The aluminum electrolytic cell waste cathode carbon block processing system according to claim 7, wherein the fume collecting module comprises two environmental fume collecting hoods, a cloth bag dust remover and a fume collecting pipeline, the two environmental fume collecting hoods are respectively arranged above the crusher and the ball mill, the two environmental fume collecting hoods are both communicated with the cloth bag dust remover, and a discharge port of the cloth bag dust remover is communicated with an external fume processing system through an environmental fume collecting main pipe; the slurry preparation tank, the fluorine precipitation reaction tank, the water immersion reaction tank, the neutralization reaction tank and the washing reaction tank are provided with top covers and are communicated with an environmental smoke collection main pipe through smoke collection branch pipes; the high-temperature high-pressure reaction kettle is sealed, and the top of the high-temperature high-pressure reaction kettle is communicated with an environment smoke collection main pipe through a smoke discharge branch pipe.
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