CN215365929U - Processing system of smoke and dust is smelted to complicated tin - Google Patents
Processing system of smoke and dust is smelted to complicated tin Download PDFInfo
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- CN215365929U CN215365929U CN202121941340.6U CN202121941340U CN215365929U CN 215365929 U CN215365929 U CN 215365929U CN 202121941340 U CN202121941340 U CN 202121941340U CN 215365929 U CN215365929 U CN 215365929U
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- ATJFFYVFTNAWJD-UHFFFAOYSA-N Tin Chemical compound [Sn] ATJFFYVFTNAWJD-UHFFFAOYSA-N 0.000 title claims abstract description 104
- 239000000779 smoke Substances 0.000 title claims abstract description 77
- 239000000428 dust Substances 0.000 title claims abstract description 74
- 238000002386 leaching Methods 0.000 claims abstract description 126
- 238000005406 washing Methods 0.000 claims abstract description 121
- 229910052718 tin Inorganic materials 0.000 claims abstract description 104
- 239000007788 liquid Substances 0.000 claims abstract description 83
- 238000003723 Smelting Methods 0.000 claims abstract description 77
- 239000002893 slag Substances 0.000 claims abstract description 75
- 230000007246 mechanism Effects 0.000 claims abstract description 59
- 229910052793 cadmium Inorganic materials 0.000 claims abstract description 57
- BDOSMKKIYDKNTQ-UHFFFAOYSA-N cadmium atom Chemical compound [Cd] BDOSMKKIYDKNTQ-UHFFFAOYSA-N 0.000 claims abstract description 48
- HCHKCACWOHOZIP-UHFFFAOYSA-N Zinc Chemical compound [Zn] HCHKCACWOHOZIP-UHFFFAOYSA-N 0.000 claims abstract description 43
- 230000003647 oxidation Effects 0.000 claims abstract description 43
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 43
- 238000003756 stirring Methods 0.000 claims abstract description 38
- 239000012286 potassium permanganate Substances 0.000 claims abstract description 36
- 230000001376 precipitating effect Effects 0.000 claims abstract description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 53
- 239000000463 material Substances 0.000 claims description 45
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims description 40
- 239000011701 zinc Substances 0.000 claims description 31
- 229910052725 zinc Inorganic materials 0.000 claims description 27
- 239000010865 sewage Substances 0.000 claims description 26
- UOURRHZRLGCVDA-UHFFFAOYSA-D pentazinc;dicarbonate;hexahydroxide Chemical compound [OH-].[OH-].[OH-].[OH-].[OH-].[OH-].[Zn+2].[Zn+2].[Zn+2].[Zn+2].[Zn+2].[O-]C([O-])=O.[O-]C([O-])=O UOURRHZRLGCVDA-UHFFFAOYSA-D 0.000 claims description 24
- 229910000029 sodium carbonate Inorganic materials 0.000 claims description 20
- 239000008399 tap water Substances 0.000 claims description 20
- 235000020679 tap water Nutrition 0.000 claims description 20
- 238000001556 precipitation Methods 0.000 claims description 17
- 238000011144 upstream manufacturing Methods 0.000 claims description 11
- 239000002699 waste material Substances 0.000 claims description 8
- 238000010306 acid treatment Methods 0.000 claims description 3
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 abstract description 40
- 238000000034 method Methods 0.000 abstract description 35
- 238000001914 filtration Methods 0.000 abstract description 30
- 238000010438 heat treatment Methods 0.000 abstract description 19
- 239000000460 chlorine Substances 0.000 abstract description 18
- 239000000706 filtrate Substances 0.000 abstract description 17
- 229910052801 chlorine Inorganic materials 0.000 abstract description 14
- 238000001816 cooling Methods 0.000 abstract description 14
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 abstract description 13
- FMRLDPWIRHBCCC-UHFFFAOYSA-L Zinc carbonate Chemical compound [Zn+2].[O-]C([O-])=O FMRLDPWIRHBCCC-UHFFFAOYSA-L 0.000 abstract description 13
- 239000000047 product Substances 0.000 abstract description 13
- 239000011667 zinc carbonate Substances 0.000 abstract description 13
- 229910000010 zinc carbonate Inorganic materials 0.000 abstract description 13
- 235000004416 zinc carbonate Nutrition 0.000 abstract description 13
- 239000003513 alkali Substances 0.000 abstract description 10
- 238000006073 displacement reaction Methods 0.000 abstract description 8
- 229910052751 metal Inorganic materials 0.000 abstract description 8
- 239000002184 metal Substances 0.000 abstract description 8
- 238000002156 mixing Methods 0.000 abstract description 8
- 230000008901 benefit Effects 0.000 abstract description 4
- 150000002739 metals Chemical class 0.000 abstract description 3
- 239000012141 concentrate Substances 0.000 description 14
- 229910052745 lead Inorganic materials 0.000 description 13
- 230000008569 process Effects 0.000 description 13
- 239000000126 substance Substances 0.000 description 12
- 230000009286 beneficial effect Effects 0.000 description 10
- 230000001590 oxidative effect Effects 0.000 description 8
- 239000007800 oxidant agent Substances 0.000 description 7
- 238000007670 refining Methods 0.000 description 7
- 239000002253 acid Substances 0.000 description 5
- 229910052785 arsenic Inorganic materials 0.000 description 5
- XLOMVQKBTHCTTD-UHFFFAOYSA-N Zinc monoxide Chemical compound [Zn]=O XLOMVQKBTHCTTD-UHFFFAOYSA-N 0.000 description 4
- 238000002844 melting Methods 0.000 description 4
- 230000008018 melting Effects 0.000 description 4
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- 239000003517 fume Substances 0.000 description 3
- 238000011084 recovery Methods 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- 229910052787 antimony Inorganic materials 0.000 description 2
- 229910052797 bismuth Inorganic materials 0.000 description 2
- 230000007812 deficiency Effects 0.000 description 2
- 229910052500 inorganic mineral Inorganic materials 0.000 description 2
- 229910000765 intermetallic Inorganic materials 0.000 description 2
- 229910021645 metal ion Inorganic materials 0.000 description 2
- 235000010755 mineral Nutrition 0.000 description 2
- 239000011707 mineral Substances 0.000 description 2
- 238000003825 pressing Methods 0.000 description 2
- 239000011787 zinc oxide Substances 0.000 description 2
- CWYNVVGOOAEACU-UHFFFAOYSA-N Fe2+ Chemical compound [Fe+2] CWYNVVGOOAEACU-UHFFFAOYSA-N 0.000 description 1
- PTFCDOFLOPIGGS-UHFFFAOYSA-N Zinc dication Chemical compound [Zn+2] PTFCDOFLOPIGGS-UHFFFAOYSA-N 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- WATWJIUSRGPENY-UHFFFAOYSA-N antimony atom Chemical compound [Sb] WATWJIUSRGPENY-UHFFFAOYSA-N 0.000 description 1
- JCXGWMGPZLAOME-UHFFFAOYSA-N bismuth atom Chemical compound [Bi] JCXGWMGPZLAOME-UHFFFAOYSA-N 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 229910052802 copper Inorganic materials 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 230000007062 hydrolysis Effects 0.000 description 1
- 238000006460 hydrolysis reaction Methods 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 239000004973 liquid crystal related substance Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 230000000750 progressive effect Effects 0.000 description 1
- 230000001698 pyrogenic effect Effects 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000009628 steelmaking Methods 0.000 description 1
- 230000004083 survival effect Effects 0.000 description 1
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P10/00—Technologies related to metal processing
- Y02P10/20—Recycling
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- Manufacture And Refinement Of Metals (AREA)
Abstract
The utility model discloses a treatment system of complex tin smelting smoke dust, which comprises a feeding mechanism, a washing mechanism, a strong oxidation leaching mechanism, a replacing mechanism and a precipitating mechanism, wherein the feeding mechanism is used for feeding tin smelting smoke dust; the method for treating the complex tin smelting smoke dust is disclosed, valuable metals in the complex tin smelting smoke dust are comprehensively recovered, the resource utilization rate is improved, and the economic benefit is remarkable; the method specifically comprises the following steps: adding the complex tin smelting smoke dust into a washing liquid, stirring and filtering to obtain a washing liquid and washing slag; adding washing slag into a sulfuric acid solution for heating, and then adding a potassium permanganate solution for strong oxidation leaching to obtain a leaching product; heating the leaching product, stirring to remove chlorine, and filtering to obtain leaching solution and leaching residue respectively; mixing the leachate with a washing solution, adding alkali to adjust the pH value, standing, cooling and filtering to obtain a filtrate; adding zinc powder into the filtrate, performing a displacement reaction, and then filtering to respectively obtain sponge cadmium and a displaced solution; and adding alkali into the displaced liquid to adjust the pH value, standing, cooling and filtering to respectively obtain crude zinc carbonate and the precipitated liquid.
Description
Technical Field
The utility model relates to the technical field of comprehensive recovery of tin smelting, in particular to a treatment system for complex tin smelting smoke dust.
Background
Mineral resources belong to non-renewable resources and are the basis for human survival and development. At present, with the development of non-ferrous metal industry, natural mineral resources are continuously consumed, reserves are reduced step by step, and comprehensive recovery and secondary resource utilization are very important.
Dross is generated in the smelting and refining process of tin, and the dross is put into an electric furnace for smelting to generate crude tin, electric furnace slag and complex tin smelting smoke dust. Wherein, the crude tin can be directly returned to the tin refining process to produce refined tin; the electric furnace slag can be put into a rotary kiln for treatment; the complex tin smelting smoke dust contains higher elements such as tin, cadmium, zinc, chlorine and the like, has complex components and can cause resource waste when being directly treated as waste. Therefore, the comprehensive recovery of the complex tin smelting smoke dust has better practical significance.
In the traditional process, zinc oxide smoke dust is produced from a zinc-containing material by a pyrogenic process; or the zinc-containing material is leached by sulfuric acid, purified and electrodeposited by a wet process to produce cathode zinc; or the zinc-containing smoke dust produced in the steel-making process is leached by ammonia to prepare active zinc oxide. However, the complex tin smelting fumes contain high contents of tin, cadmium, chlorine and the like in addition to high contents of zinc, and the adoption of the above causes inadaptability, and other components in the complex tin smelting fumes cannot be fully recycled.
Therefore, a complex treatment system for tin smelting smoke dust to effectively recover tin, cadmium, zinc, chlorine and other elements contained in the treatment system is a problem to be solved by the technical personnel in the field.
SUMMERY OF THE UTILITY MODEL
In view of the above, the utility model provides a treatment system for complex tin smelting smoke, which is matched with a tin smelting main system to comprehensively recover valuable metals in the complex tin smelting smoke, so that the resource utilization rate is improved, and the economic benefit is obvious.
In order to achieve the purpose, the utility model adopts the following technical scheme:
the utility model provides a treatment system of complex tin smelting smoke dust, which comprises a feeding mechanism, a washing mechanism, a strong oxidation leaching mechanism, a replacing mechanism and a precipitating mechanism, wherein the feeding mechanism is used for feeding tin smelting smoke dust;
the feeding mechanism comprises a tap water pipe, a smoke dust material pile, a grab bucket crane and a hopper; the upstream of the tap water pipe is communicated with tap water, the downstream of the tap water pipe is respectively communicated with the washing mechanism and the strong oxidation leaching mechanism, the smoke dust material pile is communicated with the hopper through the grab bucket crane, and the downstream of the hopper is communicated with the washing mechanism;
the washing mechanism comprises a washing tank, a washing slag squeezing water pump, a washing slag plate-and-frame filter press, a washing liquid water pump and a washing liquid pool; the upstream of the washing tank is respectively connected with the tap water pipe and the discharge hole of the hopper, the downstream of the washing tank is connected with the washing slag plate-and-frame filter press through the squeezed washing slag water pump, and meanwhile, a first stirring paddle is arranged in the washing tank and driven by a motor; a liquid outlet of the washing slag plate frame filter press is connected with the washing liquid pool, and a slag outlet of the washing slag plate frame filter press is connected with the strong oxidation leaching mechanism; the lower stream of the washing liquid pool is respectively communicated with the washing tank and the replacing mechanism through the washing liquid pump;
the strong oxidation leaching mechanism comprises a potassium permanganate solution tank, a flowmeter, a strong oxidation leaching tank, a squeezed leaching residue water pump, a leaching residue plate-and-frame filter press, a leaching liquid tank, a leaching liquid water pump and a leaching residue material pile; the upstream of the potassium permanganate solution tank is connected with the tap water pipe, and the downstream of the potassium permanganate solution tank is connected with the strong oxidation leaching tank through the flowmeter; the upstream of the strong oxidation leaching tank is connected with a slag outlet of the washing slag plate-and-frame filter press and the tap water pipe, the downstream of the strong oxidation leaching tank is connected with the leaching slag plate-and-frame filter press through the squeezed leaching slag water pump, meanwhile, a second stirring paddle is arranged in the strong oxidation leaching tank, the second stirring paddle is driven by a motor, and a heater is arranged in the strong oxidation leaching tank; a liquid outlet of the leaching slag plate-and-frame filter press is connected with the leaching liquid pool, and a slag outlet of the leaching slag plate-and-frame filter press is communicated with the leaching slag pile; the leachate tank is connected with the replacement mechanism through the leachate water pump;
the replacement mechanism comprises a zinc powder material pile, a sodium carbonate material pile, a replacement tank, a sponge cadmium squeezing water pump, a sponge cadmium plate-and-frame filter press and a sponge cadmium material pile; the downstream of the zinc powder material pile and the sodium carbonate material pile is connected with the replacement tank; the upper stream of the replacement tank is connected with the washing liquid pool through the washing liquid water pump, and is simultaneously connected with the leaching liquid pool through the leaching liquid water pump, and the lower stream of the replacement tank is connected with the sponge cadmium plate-and-frame filter press through the sponge cadmium squeezing water pump; the slag outlet of the sponge cadmium plate-and-frame filter press is connected with the sponge cadmium material pile, and the liquid outlet of the sponge cadmium plate-and-frame filter press is connected with the precipitation mechanism;
the precipitation mechanism comprises a zinc precipitation tank, a squeezing basic zinc carbonate water pump, a basic zinc carbonate plate-and-frame filter press, a basic zinc carbonate material pile, a sewage pool and a sewage pump; the upper stream of the zinc precipitation tank is connected with a liquid outlet of the sponge cadmium plate-and-frame filter press and the sodium carbonate material pile, and the lower stream of the zinc precipitation tank is connected with the basic zinc carbonate plate-and-frame filter press through the pressed basic zinc carbonate water pump; the slag outlet of the basic zinc carbonate plate-and-frame filter press is connected with the basic zinc carbonate material pile, and the liquid outlet of the basic zinc carbonate plate-and-frame filter press is connected with the sewage pool; and the downstream of the sewage pool is communicated with a sewage and waste acid treatment system through the sewage pump.
The beneficial effects of the preferred technical scheme are as follows: the complex tin smelting smoke dust treatment system disclosed by the utility model is simple in equipment, compact in structure and small in occupied area.
The utility model provides a method for treating complex tin smelting smoke dust, which adopts the complex tin smelting smoke dust treatment system and specifically comprises the following steps:
(1) adding the complex tin smelting smoke dust into a washing liquid, stirring and filtering to respectively obtain a washing liquid and washing slag;
(2) adding the washing residue into a sulfuric acid solution for heating, and then adding a potassium permanganate solution for strong oxidation leaching to obtain a leaching product;
(3) heating the leaching product, stirring to remove chlorine, and filtering to obtain a leaching solution and leaching residues respectively;
(4) mixing the leachate with the washing solution in the step (1), adding alkali to adjust the pH value, standing, cooling and filtering to obtain a filtrate;
(5) adding zinc powder into the filtrate, performing a displacement reaction, and then filtering to respectively obtain sponge cadmium and a displaced solution;
(6) and adding alkali into the displaced liquid to adjust the pH value, standing, cooling and filtering to respectively obtain crude zinc carbonate and the precipitated liquid.
The beneficial effects of the preferred technical scheme are as follows: according to the utility model, the complex tin smelting smoke dust is washed firstly, and most of chlorine and cadmium can be washed into the solution, so that the components consuming the oxidant in the washing slag are reduced, and the consumption of the oxidant is reduced; potassium permanganate strong oxidant is added in the sulfuric acid leaching process to destroy the intermetallic compound structure in the complex tin smelting smoke dust, so that the leaching rate of zinc is improved; mixing the washing solution with the leachate, compensating for the acidity deficiency of the washing solution by the acidity of the leachate, and adding a low-valent metal ion such as Fe in the washing solution2+And a small amount of residual potassium permanganate in the leaching solution is consumed, so that the subsequent treatment is facilitated.
Preferably, the complex tin smelting smoke dust is electric furnace smoke dust produced in the process of refining dross by smelting tin at high temperature in an electric furnace, and the complex tin smelting smoke dust comprises the following components in percentage by weight: 33 to 42 percent of Sn, 1.3 to 3.1 percent of Pb, 4.5 to 13.5 percent of Zn, 0.3 to 2.0 percent of As, 0.5 to 2.4 percent of Fe, 0.05 to 0.25 percent of Cu, 0.12 to 0.25 percent of Bi, 0.1 to 0.3 percent of Sb, 1.5 to 4.5 percent of Cd and 8.5 to 16.0 percent of Cl.
Preferably, the volume mass ratio of the water to the complex tin smelting smoke dust in the step (1) is 3-5: 1L/kg; the stirring temperature is 15-35 ℃, the stirring time is 1-2 h, and the stirring speed is 80-100 rpm.
The beneficial effects of the preferred technical scheme are as follows: the method washes cadmium, zinc, chlorine and the like in the complex tin smelting smoke dust into the solution at the low temperature of 15-35 ℃, does not need heating and other operations, and is low in energy consumption.
Preferably, the concentration of the sulfuric acid solution in the step (2) is 200-250 g/L; the volume mass ratio of the sulfuric acid solution to the washing slag is (5-7) to 1; heating to 75-85 ℃; the concentration of the potassium permanganate solution is 50-60 g/L, and the mass ratio of potassium permanganate in the potassium permanganate solution to the washing slag is (0.9-1.2): 100; the strong oxidation leaching time is 2-3h, and the temperature is 75-85 ℃.
The beneficial effects of the preferred technical scheme are as follows: the washing slag is put into sulfuric acid solution, and then the potassium permanganate serving as a strong oxidant is added, so that zinc in the washing slag and other metal forming compounds can be subjected to strong oxidative leaching and then enter the solution.
Preferably, the heating in the step (3) is carried out to 90-95 ℃; the stirring time is 1-2 h, and the stirring speed is 80-100 rpm.
The beneficial effects of the preferred technical scheme are as follows: the utility model leads the chlorine dissolved in the solution to overflow from the solution in the high-temperature environment and be collected in the purifying tower for centralized treatment, thus improving the operating environment.
Preferably, the leaching slag obtained in the step (3) is tin concentrate, and is treated by a tin smelting procedure.
The tin concentrate produced in the leaching step is put into the tin smelting main system, the technological process of the tin smelting main system is fully utilized, the tin metal in the complex tin smelting smoke is recycled with low consumption and high efficiency, the comprehensive recycling of resources is realized, and the economic benefit is obvious.
Preferably, the alkali in the step (4) is sodium carbonate or sodium hydroxide, and the pH value is adjusted to be 2-3; the cooling temperature is 15-35 ℃.
The beneficial effects of the preferred technical scheme are as follows: and the subsequent zinc powder consumption can be reduced by adding alkali to adjust the acidity of the solution.
Preferably, in the step (4), the filter residue is hydrolysis residue of metal which is sold directly or is merged into zinc powder replacement residue for sale, and the metal comprises bismuth and antimony.
Preferably, the first and second liquid crystal materials are,the mass volume ratio of the zinc powder to the filtrate in the step (5) is (150-180) kg: 1/m3(ii) a The temperature of the displacement reaction is 50-55 ℃, and the pH value of the end point of the displacement reaction is 5-5.2.
The beneficial effects of the preferred technical scheme are as follows: the utility model uses zinc powder to replace cadmium in the solution, and can separate the cadmium.
Preferably, the alkali in the step (6) is sodium carbonate, the pH value is adjusted to be 6.5-7, and the cooling temperature is 15-35 ℃.
The beneficial effects of the preferred technical scheme are as follows: the zinc in the solution is extracted with low consumption and high efficiency to form valuable products, the resource utilization rate is improved, and the environmental protection is facilitated.
Further preferably, the liquid after precipitation in the step (6) is subjected to acid-contaminated water treatment, and the content of zinc ions is lower than 0.1 g/L.
The beneficial effects of the preferred technical scheme are as follows: the sewage for treating the complex tin smelting smoke dust is sent to the polluted acid sewage for unified treatment, so that the cost is saved, and the environment is not polluted.
According to the technical scheme, compared with the prior art, the utility model discloses a treatment method of complex tin smelting smoke dust, and the treatment method has the following beneficial effects:
(1) the method is matched with a tin smelting main system, valuable metals in complex tin smelting smoke dust are comprehensively recovered, the resource utilization rate is improved, and the economic benefit is obvious;
(2) the complex tin smelting smoke dust is washed firstly, most of chlorine and cadmium can be washed into solution, so that the components consuming the oxidant in the washing slag are reduced, and the consumption of the oxidant is reduced;
(3) potassium permanganate strong oxidant is added in the sulfuric acid leaching process to destroy the intermetallic compound structure in the complex tin smelting smoke dust, so that the leaching rate of zinc is improved;
(4) mixing the washing solution with the leachate, compensating for the acidity deficiency of the washing solution by the acidity of the leachate, and adding a low-valent metal ion such as Fe in the washing solution2+And a small amount of residual potassium permanganate in the leaching solution is consumed, so that the subsequent treatment is facilitated.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the embodiments or the prior art will be briefly described below, it is obvious that the drawings in the following description are only embodiments of the present invention, and for those skilled in the art, other drawings can be obtained according to the provided drawings without creative efforts.
FIG. 1 is a flow chart of examples 2 and 3 of the present invention.
FIG. 2 is a schematic structural diagram of a complex tin smelting fume treatment system provided in embodiment 1 of the present invention.
In the figure: 1 is water from a pipe network, 2 is a smoke dust material pile, 3 is a grab bucket crane, 4 is a hopper, 5 is a potassium permanganate solution tank, 6 is a flowmeter, 7 is a zinc powder material pile, 8 is a sodium carbonate material pile, 9 is an alkali zinc carbonate plate-and-frame filter press, 10 is a sewage pump, 11 is a sewage tank, 12 is an alkali zinc carbonate material pile, 13 is a pressing alkali zinc carbonate water pump, 14 is a zinc precipitation tank, 15 is a sponge cadmium plate-and-frame filter press, 16 is a sponge cadmium material pile, 17 is a pressing sponge cadmium water pump, 18 is a leaching residue pile, 19 is a replacement tank, 20 is a leaching solution water pump, 21 is a leaching solution tank, 22 is a leaching residue plate-and-frame filter press, 23 is a squeezing leaching residue water pump, 24 is a strong oxidation leaching tank, 25 is a washing solution tank, 26 is a washing solution water pump, 27 is a washing residue plate-and-frame filter press, 28 is a squeezing washing residue water pump, and 29 is a washing tank.
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
Example 1
The embodiment 1 of the utility model discloses a complex tin smelting smoke dust treatment system, which comprises a feeding mechanism, a washing mechanism, a strong oxidation leaching mechanism, a replacing mechanism and a precipitating mechanism, wherein the feeding mechanism is used for feeding tin smelting smoke dust;
the feeding mechanism comprises a tap water pipe, a smoke dust material pile, a grab bucket crane and a hopper; the upstream of the tap water pipe is communicated with tap water, the downstream is respectively communicated with the washing mechanism and the strong oxidation leaching mechanism, the smoke dust material pile is communicated with the hopper through the grab crane, and the downstream of the hopper is communicated with the washing mechanism;
the washing mechanism comprises a washing tank, a washing slag squeezing water pump, a washing slag plate-and-frame filter press, a washing liquid water pump and a washing liquid pool; the upstream of the washing tank is respectively connected with a tap water pipe and a discharge hole of the hopper, the downstream of the washing tank is connected with a washing slag plate frame filter press through a squeezing washing slag water pump, and meanwhile, a first stirring paddle is arranged in the washing tank and driven by a motor; the liquid outlet of the washing slag plate frame filter press is connected with a washing liquid pool, and the slag outlet of the washing slag plate frame filter press is connected with a strong oxidation leaching mechanism; the lower stream of the washing liquid pool is respectively communicated with the washing tank and the replacing mechanism through a washing liquid pump;
the strong oxidation leaching mechanism comprises a potassium permanganate solution tank, a flowmeter, a strong oxidation leaching tank, a squeezed leaching residue water pump, a leaching residue plate-and-frame filter press, a leaching liquid tank, a leaching liquid water pump and a leaching residue material pile; the upstream of the potassium permanganate solution tank is connected with a tap water pipe, and the downstream of the potassium permanganate solution tank is connected with a strong oxidation leaching tank through a flowmeter; the upper stream of the strong oxidation leaching tank is connected with a slag outlet and a tap water pipe of the washing slag plate-frame filter press, the lower stream of the strong oxidation leaching tank is connected with the leaching slag plate-frame filter press through a leaching slag squeezing water pump, meanwhile, a second stirring paddle is arranged in the strong oxidation leaching tank, the second stirring paddle is driven by a motor, and a heater is arranged in the strong oxidation leaching tank; a liquid outlet of the leaching residue plate-and-frame filter press is connected with a leaching liquid pool, and a residue outlet of the leaching residue plate-and-frame filter press is communicated with a leaching residue material pile; the leaching liquid pool is connected with a replacement mechanism through a leaching liquid water pump;
the replacement mechanism comprises a zinc powder material pile, a sodium carbonate material pile, a replacement tank, a sponge cadmium squeezing water pump, a sponge cadmium plate-and-frame filter press and a sponge cadmium material pile; the downstream of the zinc powder material pile and the sodium carbonate material pile is connected with a replacement tank; the upper stream of the replacement tank is connected with a washing liquid pool through a washing liquid pump, and is connected with a leaching liquid pool through a leaching liquid pump, and the lower stream of the replacement tank is connected with a sponge cadmium plate-and-frame filter press through a sponge cadmium squeezing pump; the slag outlet of the sponge cadmium plate-and-frame filter press is connected with a sponge cadmium material pile, and the liquid outlet of the sponge cadmium plate-and-frame filter press is connected with a precipitation mechanism;
the precipitation mechanism comprises a zinc precipitation tank, a squeezing basic zinc carbonate water pump, a basic zinc carbonate plate-and-frame filter press, a basic zinc carbonate material pile, a sewage pool and a sewage pump; the upper stream of the zinc precipitation tank is connected with a liquid outlet of the sponge cadmium plate-and-frame filter press and a sodium carbonate material pile, and the lower stream of the zinc precipitation tank is connected with the basic zinc carbonate plate-and-frame filter press through a basic zinc carbonate squeezing water pump; the slag outlet of the basic zinc carbonate plate-and-frame filter press is connected with a basic zinc carbonate material pile, and the liquid outlet of the basic zinc carbonate plate-and-frame filter press is connected with a sewage pool; the lower reaches of the sewage pool are communicated with a sewage and acid treatment system through a sewage pump.
Example 2
The embodiment 2 of the utility model discloses a method for treating complex tin smelting smoke dust, which adopts the treatment system of the complex tin smelting smoke dust disclosed in the embodiment 1, wherein the complex tin smelting smoke dust is electric furnace smoke dust produced in the process of refining dross by melting tin at high temperature in an electric furnace, and the complex tin smelting smoke dust comprises the following components in percentage by weight: 41.8% of Sn, 2.13% of Pb, 7.97% of Zn, 0.4% of As, 2.78% of Fe, 0.08% of Cu, 0.12% of Bi, 0.09% of Sb, 3.3% of Cd and 10.21% of Cl.
The method specifically comprises the following steps:
(1) adding the complex tin smelting smoke dust into water, stirring and filtering to respectively obtain washing liquid and washing slag;
wherein the volume mass ratio of the water to the complex tin smelting smoke dust is 3: 1L/kg; the stirring temperature is 15-35 ℃, the stirring time is 1-2 h, and the stirring speed is 80 rpm.
(2) Adding washing residues into a sulfuric acid solution for heating, and then adding a potassium permanganate solution for strong oxidation leaching to obtain a leaching product;
wherein the concentration of the sulfuric acid solution is 200 g/L; the volume mass ratio of the sulfuric acid solution to the washing slag is 5: 1; heating to 75-85 ℃; the concentration of the potassium permanganate solution is 60g/L, and the mass ratio of potassium permanganate in the potassium permanganate solution to washing slag is 1: 100; the strong oxidation leaching time is 3 hours, and the temperature is 75-85 ℃;
(3) heating the leaching product to 90-95 ℃, stirring at the rotating speed of 80rpm for 1h to remove chlorine, and filtering to respectively obtain leaching solution and leaching residues; the leaching slag is tin concentrate, and is treated by a tin smelting procedure;
wherein the yield of the tin concentrate is 75.2 percent of the input complex tin smelting smoke dust, and the tin concentrate comprises the following chemical components: sn: 52.31%, Zn: 4.12%, Cd: 0.13%, Pb: 2.54 percent of As and 1.95 percent of As;
(4) mixing the leachate with the washing liquid in the step (1), adding sodium carbonate to adjust the pH value to 2-3, standing, cooling to 15-35 ℃, and filtering to obtain a filtrate;
(5) according to the volume mass ratio of the filtrate to the zinc powder of 150kg/m3Adding zinc powder into the filtrate, performing a displacement reaction at 50-55 ℃ until the pH value is 5-5.2, and then filtering to respectively obtain sponge cadmium and a displaced solution;
the sponge cadmium comprises the following chemical components: zn: 1.43%, Pb: 1.57%, Cd: 75.31 percent;
(6) adding sodium carbonate into the displaced liquid to adjust the pH value to 6.5-7, standing and cooling to 15-35 ℃, filtering to respectively obtain crude zinc carbonate and the precipitated liquid, and sending the precipitated liquid to waste acid sewage treatment;
the chemical components of the crude zinc carbonate are as follows: zn: 47.21%, Pb: 1.69% and Sb2.93%.
Example 3
The embodiment 3 of the utility model discloses a method for treating complex tin smelting smoke dust, which adopts the treatment system of the complex tin smelting smoke dust disclosed in the embodiment 1, wherein the complex tin smelting smoke dust is electric furnace smoke dust produced in the process of refining dross by melting tin at high temperature in an electric furnace, and the complex tin smelting smoke dust comprises the following components in percentage by weight: 41.1% of Sn, 1.71% of Pb, 9.2% of Zn, 0.3% of As, 0.45% of Fe, 0.09% of Cu, 0.17% of Bi, 0.27% of Sb, 4.48% of Cd and 8.51% of Cl.
The method specifically comprises the following steps:
(1) adding the complex tin smelting smoke dust into water, stirring and filtering to respectively obtain washing liquid and washing slag;
wherein the volume mass ratio of the water to the complex tin smelting smoke dust is 4: 1L/kg; the stirring temperature is 15-35 ℃, the stirring time is 2h, and the stirring speed is 90 rpm.
(2) Adding washing residues into a sulfuric acid solution for heating, and then adding a potassium permanganate solution for strong oxidation leaching to obtain a leaching product;
wherein the concentration of the sulfuric acid solution is 250 g/L; the volume mass ratio of the sulfuric acid solution to the washing slag is 6: 1; heating to 75-85 ℃; the concentration of the potassium permanganate solution is 50g/L, and the mass ratio of potassium permanganate in the potassium permanganate solution to washing slag is 1.2: 100; the strong oxidation leaching time is 3 hours, and the temperature is 75-85 ℃;
(3) heating the leaching product to 90-95 ℃, stirring at the rotating speed of 100rpm for 2h to remove chlorine, and filtering to respectively obtain leaching solution and leaching residues; the leaching slag is tin concentrate, and is treated by a tin smelting procedure;
wherein the yield of the tin concentrate is 75.2 percent of the input complex tin smelting smoke dust, and the tin concentrate comprises the following chemical components: sn: 54.02%, Zn: 2.31%, Cd: 0.08%, Pb: 1.89 percent and As is 1.75 percent;
(4) mixing the leachate with the washing liquid in the step (1), adding sodium carbonate to adjust the pH value to 2-3, standing, cooling to 15-35 ℃, and filtering to obtain a filtrate;
(5) according to the volume mass ratio of the filtrate to the zinc powder of 180kg/m3Adding zinc powder into the filtrate, performing a displacement reaction at 50-55 ℃ until the pH value is 5-5.2, and then filtering to respectively obtain sponge cadmium and a displaced solution;
the sponge cadmium comprises the following chemical components: zn: 1.37%, Pb: 1.29%, Cd: 78.41 percent;
(6) adding sodium carbonate into the displaced liquid to adjust the pH value to 6.5-7, standing and cooling to 15-35 ℃, filtering to respectively obtain crude zinc carbonate and the precipitated liquid, and sending the precipitated liquid to waste acid sewage treatment;
the chemical components of the crude zinc carbonate are as follows: zn: 44.30%, Pb: 2.11 percent and Sb3.16 percent.
Example 4
The embodiment 4 of the utility model discloses a treatment method of complex tin smelting smoke dust, which adopts the treatment system of complex tin smelting smoke dust disclosed in the embodiment 1, wherein the complex tin smelting smoke dust is electric furnace smoke dust produced in the process of refining dross by melting tin at high temperature in an electric furnace, and the complex tin smelting smoke dust comprises the following components in percentage by weight: 34.3% of Sn, 2.90% of Pb, 4.50% of Zn, 1.66% of As, 2.39% of Fe, 0.15% of Cu, 0.15% of Bi, 0.13% of Sb, 1.57% of Cd and 15.56% of Cl.
The method specifically comprises the following steps:
(1) adding the complex tin smelting smoke dust into water, stirring and filtering to respectively obtain washing liquid and washing slag;
wherein the volume mass ratio of the water to the complex tin smelting smoke dust is 5: 1L/kg; the stirring temperature is 15-35 ℃, the stirring time is 1h, and the stirring speed is 100 rpm.
(2) Adding washing residues into a sulfuric acid solution for heating, and then adding a potassium permanganate solution for strong oxidation leaching to obtain a leaching product;
wherein the concentration of the sulfuric acid solution is 220 g/L; the volume mass ratio of the sulfuric acid solution to the washing slag is 7: 1; heating to 75-85 ℃; the concentration of the potassium permanganate solution is 55g/L, and the mass ratio of potassium permanganate in the potassium permanganate solution to washing slag is 0.9: 100; the strong oxidation leaching time is 2 hours, and the temperature is 75-85 ℃;
(3) heating the leaching product to 90-95 ℃, stirring at the rotating speed of 90rpm for 1h to remove chlorine, and filtering to respectively obtain leaching solution and leaching residues; the leaching slag is tin concentrate, and is treated by a tin smelting procedure;
wherein the yield of the tin concentrate is 78.6 percent of the input complex tin smelting smoke dust, and the tin concentrate comprises the following chemical components: sn: 55.53%, Zn: 3.75%, Cd: 0.09%, Pb: 2.15 percent of As and 2.03 percent of As;
(4) mixing the leachate with the washing liquid in the step (1), adding sodium carbonate to adjust the pH value to 2-3, standing, cooling to 15-35 ℃, and filtering to obtain a filtrate;
(5) according to the volume mass ratio of the filtrate to the zinc powder of 160kg/m3Adding zinc powder into the filtrate at 50-55 DEG CCarrying out a displacement reaction under the condition until the pH value is 5-5.2, and then filtering to respectively obtain sponge cadmium and a displaced liquid;
the sponge cadmium comprises the following chemical components: zn: 1.23%, Pb: 1.48%, Cd: 76.35 percent;
(6) adding sodium carbonate into the displaced liquid to adjust the pH value to 6.5-7, standing and cooling to 15-35 ℃, filtering to respectively obtain crude zinc carbonate and the precipitated liquid, and sending the precipitated liquid to waste acid sewage treatment;
the chemical components of the crude zinc carbonate are as follows: zn: 48.55%, Pb: 1.86% and Sb2.75%.
Example 5
The embodiment 5 of the utility model discloses a treatment method of complex tin smelting smoke dust, which adopts the treatment system of complex tin smelting smoke dust disclosed in the embodiment 1, wherein the complex tin smelting smoke dust is electric furnace smoke dust produced in the process of refining dross by melting tin at high temperature in an electric furnace, and the complex tin smelting smoke dust comprises the following components in percentage by weight: 41.8% of Sn, 2.13% of Pb, 7.97% of Zn, 0.4% of As, 2.78% of Fe, 0.08% of Cu, 0.12% of Bi, 0.09% of Sb, 3.3% of Cd and 10.21% of Cl.
The method specifically comprises the following steps:
(1) adding the complex tin smelting smoke dust into water, stirring and filtering to respectively obtain washing liquid and washing slag;
wherein the volume mass ratio of the water to the complex tin smelting smoke dust is 4: 1L/kg; the stirring temperature is 15-35 ℃, the stirring time is 1.5h, and the stirring speed is 80 rpm.
(2) Adding washing residues into a sulfuric acid solution for heating, and then adding a potassium permanganate solution for strong oxidation leaching to obtain a leaching product;
wherein the concentration of the sulfuric acid solution is 240 g/L; the volume mass ratio of the sulfuric acid solution to the washing slag is 5: 1; heating to 75-85 ℃; the concentration of the potassium permanganate solution is 58g/L, and the mass ratio of potassium permanganate in the potassium permanganate solution to washing slag is 0.9: 100; the strong oxidation leaching time is 3 hours, and the temperature is 75-85 ℃;
(3) heating the leaching product to 90-95 ℃, stirring at the rotating speed of 90rpm for 1h to remove chlorine, and filtering to respectively obtain leaching solution and leaching residues; the leaching slag is tin concentrate, and is treated by a tin smelting procedure;
wherein the yield of the tin concentrate is 80.5 percent of the input complex tin smelting smoke dust, and the tin concentrate comprises the following chemical components: sn: 49.78%, Zn: 3.8%, Cd: 0.06%, Pb: 2.38 percent and As is 1.87 percent;
(4) mixing the leachate with the washing liquid in the step (1), adding sodium carbonate to adjust the pH value to 2-3, standing, cooling to 15-35 ℃, and filtering to obtain a filtrate;
(5) according to the volume mass ratio of the filtrate to the zinc powder of 170kg/m3Adding zinc powder into the filtrate, performing a displacement reaction at 50-55 ℃ until the pH value is 5-5.2, and then filtering to respectively obtain sponge cadmium and a displaced solution;
the sponge cadmium comprises the following chemical components: zn: 1.25%, Pb: 1.44%, Cd: 77.57 percent;
(6) adding sodium carbonate into the displaced liquid to adjust the pH value to 6.5-7, standing and cooling to 15-35 ℃, filtering to respectively obtain crude zinc carbonate and the precipitated liquid, and sending the precipitated liquid to waste acid sewage treatment;
the chemical components of the crude zinc carbonate are as follows: zn: 46.93%, Pb: 1.52 percent and Sb3.65 percent.
The embodiments in the present description are described in a progressive manner, each embodiment focuses on differences from other embodiments, and the same and similar parts among the embodiments are referred to each other. The device disclosed by the embodiment corresponds to the method disclosed by the embodiment, so that the description is simple, and the relevant points can be referred to the method part for description.
The previous description of the disclosed embodiments is provided to enable any person skilled in the art to make or use the present invention. Various modifications to these embodiments will be readily apparent to those skilled in the art, and the generic principles defined herein may be applied to other embodiments without departing from the spirit or scope of the utility model. Thus, the present invention is not intended to be limited to the embodiments shown herein but is to be accorded the widest scope consistent with the principles and novel features disclosed herein.
Claims (1)
1. A treatment system for complex tin smelting smoke dust is characterized by comprising a feeding mechanism, a washing mechanism, a strong oxidation leaching mechanism, a replacing mechanism and a precipitating mechanism;
the feeding mechanism comprises a tap water pipe, a smoke dust material pile, a grab bucket crane and a hopper; the upstream of the tap water pipe is communicated with tap water, the downstream of the tap water pipe is respectively communicated with the washing mechanism and the strong oxidation leaching mechanism, the smoke dust material pile is communicated with the hopper through the grab bucket crane, and the downstream of the hopper is communicated with the washing mechanism;
the washing mechanism comprises a washing tank, a washing slag squeezing water pump, a washing slag plate-and-frame filter press, a washing liquid water pump and a washing liquid pool; the upstream of the washing tank is respectively connected with the tap water pipe and the discharge hole of the hopper, the downstream of the washing tank is connected with the washing slag plate-and-frame filter press through the squeezed washing slag water pump, and meanwhile, a first stirring paddle is arranged in the washing tank and driven by a motor; a liquid outlet of the washing slag plate frame filter press is connected with the washing liquid pool, and a slag outlet of the washing slag plate frame filter press is connected with the strong oxidation leaching mechanism; the lower stream of the washing liquid pool is respectively communicated with the washing tank and the replacing mechanism through the washing liquid pump;
the strong oxidation leaching mechanism comprises a potassium permanganate solution tank, a flowmeter, a strong oxidation leaching tank, a squeezed leaching residue water pump, a leaching residue plate-and-frame filter press, a leaching liquid tank, a leaching liquid water pump and a leaching residue material pile; the upstream of the potassium permanganate solution tank is connected with the tap water pipe, and the downstream of the potassium permanganate solution tank is connected with the strong oxidation leaching tank through the flowmeter; the upstream of the strong oxidation leaching tank is connected with a slag outlet of the washing slag plate-and-frame filter press and the tap water pipe, the downstream of the strong oxidation leaching tank is connected with the leaching slag plate-and-frame filter press through the squeezed leaching slag water pump, meanwhile, a second stirring paddle is arranged in the strong oxidation leaching tank, the second stirring paddle is driven by a motor, and a heater is arranged in the strong oxidation leaching tank; a liquid outlet of the leaching slag plate-and-frame filter press is connected with the leaching liquid pool, and a slag outlet of the leaching slag plate-and-frame filter press is communicated with the leaching slag pile; the leachate tank is connected with the replacement mechanism through the leachate water pump;
the replacement mechanism comprises a zinc powder material pile, a sodium carbonate material pile, a replacement tank, a sponge cadmium squeezing water pump, a sponge cadmium plate-and-frame filter press and a sponge cadmium material pile; the downstream of the zinc powder material pile and the sodium carbonate material pile is connected with the replacement tank; the upper stream of the replacement tank is connected with the washing liquid pool through the washing liquid water pump, and is simultaneously connected with the leaching liquid pool through the leaching liquid water pump, and the lower stream of the replacement tank is connected with the sponge cadmium plate-and-frame filter press through the sponge cadmium squeezing water pump; the slag outlet of the sponge cadmium plate-and-frame filter press is connected with the sponge cadmium material pile, and the liquid outlet of the sponge cadmium plate-and-frame filter press is connected with the precipitation mechanism;
the precipitation mechanism comprises a zinc precipitation tank, a squeezing basic zinc carbonate water pump, a basic zinc carbonate plate-and-frame filter press, a basic zinc carbonate material pile, a sewage pool and a sewage pump; the upper stream of the zinc precipitation tank is connected with a liquid outlet of the sponge cadmium plate-and-frame filter press and the sodium carbonate material pile, and the lower stream of the zinc precipitation tank is connected with the basic zinc carbonate plate-and-frame filter press through the pressed basic zinc carbonate water pump; the slag outlet of the basic zinc carbonate plate-and-frame filter press is connected with the basic zinc carbonate material pile, and the liquid outlet of the basic zinc carbonate plate-and-frame filter press is connected with the sewage pool; and the downstream of the sewage pool is communicated with a sewage and waste acid treatment system through the sewage pump.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN113564370A (en) * | 2021-08-18 | 2021-10-29 | 云南锡业股份有限公司锡业分公司 | Treatment system and method for complex tin smelting smoke dust |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN113564370A (en) * | 2021-08-18 | 2021-10-29 | 云南锡业股份有限公司锡业分公司 | Treatment system and method for complex tin smelting smoke dust |
| CN113564370B (en) * | 2021-08-18 | 2024-06-25 | 云南锡业股份有限公司锡业分公司 | Treatment system and method for complex tin smelting smoke dust |
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