CN220366711U - Sulfuric acid process draws lithium acidizing tail gas processing system - Google Patents
Sulfuric acid process draws lithium acidizing tail gas processing system Download PDFInfo
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- CN220366711U CN220366711U CN202321871688.1U CN202321871688U CN220366711U CN 220366711 U CN220366711 U CN 220366711U CN 202321871688 U CN202321871688 U CN 202321871688U CN 220366711 U CN220366711 U CN 220366711U
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- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 title claims abstract description 88
- 238000000034 method Methods 0.000 title claims abstract description 65
- WHXSMMKQMYFTQS-UHFFFAOYSA-N Lithium Chemical compound [Li] WHXSMMKQMYFTQS-UHFFFAOYSA-N 0.000 title claims abstract description 60
- 229910052744 lithium Inorganic materials 0.000 title claims abstract description 60
- 238000002156 mixing Methods 0.000 claims abstract description 83
- 239000002002 slurry Substances 0.000 claims abstract description 78
- 239000007788 liquid Substances 0.000 claims abstract description 63
- 230000020477 pH reduction Effects 0.000 claims abstract description 52
- 238000010521 absorption reaction Methods 0.000 claims abstract description 51
- 239000000428 dust Substances 0.000 claims abstract description 50
- WMFOQBRAJBCJND-UHFFFAOYSA-M Lithium hydroxide Chemical compound [Li+].[OH-] WMFOQBRAJBCJND-UHFFFAOYSA-M 0.000 claims abstract description 30
- 239000007791 liquid phase Substances 0.000 claims abstract description 23
- XGZVUEUWXADBQD-UHFFFAOYSA-L lithium carbonate Chemical compound [Li+].[Li+].[O-]C([O-])=O XGZVUEUWXADBQD-UHFFFAOYSA-L 0.000 claims abstract description 12
- 229910052808 lithium carbonate Inorganic materials 0.000 claims abstract description 12
- 238000000605 extraction Methods 0.000 claims description 21
- 238000001816 cooling Methods 0.000 claims description 13
- 239000002253 acid Substances 0.000 abstract description 8
- 239000002351 wastewater Substances 0.000 abstract description 5
- 239000007789 gas Substances 0.000 description 64
- 239000000243 solution Substances 0.000 description 12
- INHCSSUBVCNVSK-UHFFFAOYSA-L lithium sulfate Inorganic materials [Li+].[Li+].[O-]S([O-])(=O)=O INHCSSUBVCNVSK-UHFFFAOYSA-L 0.000 description 8
- RBTVSNLYYIMMKS-UHFFFAOYSA-N tert-butyl 3-aminoazetidine-1-carboxylate;hydrochloride Chemical compound Cl.CC(C)(C)OC(=O)N1CC(N)C1 RBTVSNLYYIMMKS-UHFFFAOYSA-N 0.000 description 8
- 239000012717 electrostatic precipitator Substances 0.000 description 7
- 238000011010 flushing procedure Methods 0.000 description 7
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 6
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 6
- 230000002378 acidificating effect Effects 0.000 description 6
- 239000003546 flue gas Substances 0.000 description 6
- 239000012530 fluid Substances 0.000 description 5
- 239000007921 spray Substances 0.000 description 5
- CNLWCVNCHLKFHK-UHFFFAOYSA-N aluminum;lithium;dioxido(oxo)silane Chemical compound [Li+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O CNLWCVNCHLKFHK-UHFFFAOYSA-N 0.000 description 4
- 229910052642 spodumene Inorganic materials 0.000 description 4
- 238000005406 washing Methods 0.000 description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 4
- 238000006243 chemical reaction Methods 0.000 description 3
- 230000001143 conditioned effect Effects 0.000 description 3
- 239000012452 mother liquor Substances 0.000 description 3
- 238000004064 recycling Methods 0.000 description 3
- 229910000029 sodium carbonate Inorganic materials 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- 229910018072 Al 2 O 3 Inorganic materials 0.000 description 2
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 description 2
- 239000006096 absorbing agent Substances 0.000 description 2
- 239000006227 byproduct Substances 0.000 description 2
- 230000003750 conditioning effect Effects 0.000 description 2
- 239000000110 cooling liquid Substances 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000002386 leaching Methods 0.000 description 2
- 229910003002 lithium salt Inorganic materials 0.000 description 2
- 159000000002 lithium salts Chemical class 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000012071 phase Substances 0.000 description 2
- 238000001556 precipitation Methods 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 229910052938 sodium sulfate Inorganic materials 0.000 description 2
- 235000011152 sodium sulphate Nutrition 0.000 description 2
- 238000001179 sorption measurement Methods 0.000 description 2
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 description 1
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 description 1
- 229910018068 Li 2 O Inorganic materials 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 1
- 239000000920 calcium hydroxide Substances 0.000 description 1
- 229910001861 calcium hydroxide Inorganic materials 0.000 description 1
- 238000002425 crystallisation Methods 0.000 description 1
- 230000008025 crystallization Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000001419 dependent effect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000006073 displacement reaction Methods 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- PQVSTLUFSYVLTO-UHFFFAOYSA-N ethyl n-ethoxycarbonylcarbamate Chemical compound CCOC(=O)NC(=O)OCC PQVSTLUFSYVLTO-UHFFFAOYSA-N 0.000 description 1
- 239000013505 freshwater Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- 125000003010 ionic group Chemical group 0.000 description 1
- GLXDVVHUTZTUQK-UHFFFAOYSA-M lithium hydroxide monohydrate Substances [Li+].O.[OH-] GLXDVVHUTZTUQK-UHFFFAOYSA-M 0.000 description 1
- 229940040692 lithium hydroxide monohydrate Drugs 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000012544 monitoring process Methods 0.000 description 1
- 238000006386 neutralization reaction Methods 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000000779 smoke Substances 0.000 description 1
- 229910052708 sodium Inorganic materials 0.000 description 1
- 239000011734 sodium Substances 0.000 description 1
- 230000003068 static effect Effects 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
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- Treating Waste Gases (AREA)
Abstract
The utility model belongs to the technical field of tail gas treatment of acidification roasting, and particularly relates to a tail gas treatment system for extracting lithium by a sulfuric acid method. The tail gas treatment system for extracting lithium by the sulfuric acid method comprises an acidification kiln, a slurry mixing tank, a wet venturi dust remover and an absorption tower; the exhaust port of the acidification kiln is connected with the tail gas inlet of the wet venturi dust collector through a first pipeline; the liquid outlet of the slurry mixing tank is connected with the liquid phase inlet of the wet venturi dust collector through a second pipeline; the exhaust port of the wet venturi dust collector is connected with the tail gas inlet of the absorption tower through a third pipeline, and lithium hydroxide and/or lithium carbonate absorption liquid is arranged in the absorption tower. The utility model carries out dust removal and acid removal treatment on the acidified tail gas, the adopted slurry mixing liquid and absorption liquid are both from the technological process of extracting lithium by the sulfuric acid method, and the used slurry mixing liquid and absorption liquid are used for mixing slurry, so that the loss of lithium resources in the process of extracting lithium by the sulfuric acid method can be reduced to the greatest extent, and no waste water is generated in the treatment process.
Description
Technical Field
The utility model belongs to the technical field of tail gas treatment of acidification roasting, and particularly relates to a tail gas treatment system for extracting lithium by a sulfuric acid method.
Background
The sulfuric acid method is the main flow process for extracting lithium from the current ore, namely spodumene is firstly baked and transformed and then reacts with sulfuric acid at high temperature (250 ℃) to leach lithium sulfate solution; then lithium sulfate reacts with excessive sodium carbonate to generate lithium carbonate, sodium sulfate mother liquor containing lithium and excessive sodium carbonate is subjected to neutralization and carbonate removal, and then evaporated and crystallized to obtain sodium sulfate byproducts, and secondary lithium-containing mother liquor (sodium precipitation mother liquor) is subjected to secondary lithium precipitation (reaction with sodium carbonate) to obtain lower-grade lithium carbonate; lithium carbonate and calcium hydroxide are subjected to causticization reaction to generate a lithium hydroxide solution with lower concentration, and the lithium hydroxide monohydrate product is obtained through secondary crystallization of the solution. The core of the process is the process of preparing spodumene clinker by acidification and roasting. The process has the advantages of high production efficiency, high lithium recovery rate and the like. Take spodumene as an example, wherein alpha-Li is mainly used 2 O·Al 2 O 3 ·4SiO 2 In the form of insoluble acid and alkali, and is subjected to 1100 ℃ high temperatureTransformation to beta-Li 2 O·Al 2 O 3 ·4SiO 2 The soluble sulfate is generated by displacement reaction with sulfuric acid, and further purified and converted into a lithium salt product. In the acidification roasting process, an external heating rotary kiln is generally used by lithium salt production enterprises, a large amount of acid tail gas is generated, and the main components are as follows: vapor, SO 2 、SO 3 And a small amount of spodumene dust, and the tail gas needs to be treated to reach the emission standard.
As for the generated acidified roasting tail gas, alkaline liquid is mostly adopted for spray treatment at present, and although the method can reduce the acid and dust content of the tail gas to a certain extent, the operation load of a washing tower can be increased, and other byproducts or waste water are also generated.
Chinese patent CN115282759a discloses an acidified roasting flue gas treatment method and system, the method mainly comprising: firstly, adopting a heat exchanger to cool the acidified roasting flue gas; then a dust remover is adopted to remove dust from the cooled flue gas through cooling liquid; then the first-stage absorption device is adopted to absorb and treat acidic substances in the dust-removed flue gas through the spray liquid, so as to obtain the first-stage absorbed flue gas, and the spray liquid after absorption treatment is recycled; and finally, a secondary absorption device is adopted to wash and secondarily absorb the smoke after primary absorption through washing water, and the cooling liquid and the washing water adopted in the patent are industrial fresh water or washing water of other working procedures, but the water is not mentioned, and if the waste water is removed, the cost of waste water treatment can be obviously increased.
Disclosure of Invention
Aiming at the defects, the utility model provides a sulfuric acid method lithium extraction acidification tail gas treatment system, which realizes the purposes of low cost and high-efficiency dust removal and acid removal of sulfuric acid method lithium extraction acidification tail gas.
The utility model relates to a sulfuric acid method lithium extraction acidification tail gas treatment system, which comprises an acidification kiln, a slurry mixing tank, a wet venturi dust remover and an absorption tower, wherein the acidification kiln comprises a kiln body and a liquid inlet pipe;
the exhaust port of the acidification kiln is connected with the tail gas inlet of the wet venturi dust collector through a first pipeline, and the first pipeline is used for conveying the acidification tail gas;
the liquid outlet of the slurry mixing tank is connected with the liquid phase inlet of the wet venturi dust collector through a second pipeline, and the second pipeline is used for conveying slurry mixing;
the exhaust port of the wet venturi dust collector is connected with the tail gas inlet of the absorption tower through a third pipeline, the third pipeline is used for conveying the acidified tail gas after dust removal, and lithium hydroxide and/or lithium carbonate absorption liquid is arranged inside the absorption tower.
In one embodiment of the present utility model, the second pipe includes a second input pipe and a second output pipe;
one end of the second input pipeline is connected with a liquid outlet of the slurry mixing tank, and the other end of the second input pipeline is connected with an inlet of the heat exchanger;
one end of the second output pipeline is connected with the outlet of the heat exchanger, and the other end of the second output pipeline is connected with the liquid phase inlet of the dust remover.
In a specific embodiment of the utility model, a liquid outlet of the slurry mixing tank is connected with a slurry mixing pump, and an output port of the slurry mixing pump is connected with the second input pipeline.
In a specific embodiment of the utility model, the discharge port of the acidification kiln is connected with the feed port of the acidification cooling kiln through a fourth pipeline, and the discharge port of the acidification cooling kiln is connected with the pulp mixing tank through a fifth pipeline.
In one embodiment of the present utility model, the liquid phase outlet of the wet venturi scrubber is connected to the surge tank through a sixth pipe.
In one specific embodiment of the utility model, the liquid phase outlet of the wet venturi scrubber is connected with a liquid phase output pump, and the output end of the liquid phase output pump is connected with the sixth pipeline.
In one specific embodiment of the utility model, the liquid outlet of the absorption tower is connected with the size mixing tank through a seventh pipeline.
In one specific embodiment of the utility model, the liquid outlet of the size mixing tank is connected with the size mixing tank through an eighth pipeline.
In a specific embodiment of the utility model, the tail gas outlet of the absorption tower is connected with a chimney through a ninth pipeline.
In one embodiment of the present utility model, the ninth conduit includes a ninth input conduit and a ninth output conduit;
one end of the ninth input pipeline is connected with a tail gas outlet of the absorption tower, and the other end of the ninth input pipeline is connected with an input port of a fan;
one end of the ninth output pipeline is connected with the output port of the fan, and the other end of the ninth output pipeline is connected with the chimney.
Compared with the prior art, the utility model has the beneficial effects that:
1. the sulfuric acid method lithium extraction acidification tail gas treatment system can treat the acidic tail gas generated based on the sulfuric acid method lithium extraction acidification kiln with low cost and high efficiency, the wet venturi dust remover uses the slurry mixing liquid, lithium-containing dust in the acidic tail gas can be removed, the absorption tower uses lithium hydroxide and/or lithium carbonate absorption liquid, and SO in the acidification tail gas can be further removed 2 、SO 3 And acid gases are reacted to generate lithium sulfate, so that the recycling of lithium elements in the process of extracting lithium by a sulfuric acid method is realized.
2. The heat exchanger is arranged in the sulfuric acid method lithium extraction and acidification tail gas treatment system, so that the heat exchange can be carried out on the pulp, and the pulp subjected to the heat exchange is conveyed to the wet venturi dust remover, so that lithium-containing dust in the acidification tail gas can be removed, and the acidification tail gas can be cooled, and the post-treatment of the acidification tail gas is safer and more convenient.
3. The slurry mixing pump is arranged in the tail gas treatment system for extracting lithium by the sulfuric acid method, so that the slurry mixing pump can be used for pressurizing the slurry, and the conveying of the slurry mixing is facilitated.
4. According to the utility model, the acidification cooling kiln and the slurry mixing tank are arranged in the tail gas treatment system for extracting lithium by the sulfuric acid method, so that clinker extracted by the sulfuric acid method can be cooled and subjected to slurry mixing treatment, and the clinker can be more conveniently subjected to the next leaching process.
5. The sixth pipeline, the seventh pipeline and the eighth pipeline are connected with the slurry mixing tank, so that slurry mixing liquid, slurry mixing liquid absorbing lithium-containing dust and absorption liquid treating acidified tail gas can be input into the slurry mixing tank and mixed with clinker extracted by the sulfuric acid method, lithium loss can be reduced, and utilization of lithium resources is improved.
Drawings
FIG. 1 is a schematic diagram of the sulfuric acid process lithium extraction acidification tail gas treatment system.
In the drawings, the list of components represented by the various numbers is as follows:
1. acidifying kiln; 2. a wet venturi scrubber; 3. a slurry mixing tank; 4. an absorption tower; 5. a first pipe; 6. a second pipe; 61. a second input conduit; 62. a second output conduit; 7. a third conduit; 8. a heat exchanger; 9. a slurry pump; 10. a fourth conduit; 11. acidifying and cooling the kiln; 12. a fifth pipe; 13. a size mixing tank; 14. a sixth conduit; 15. a liquid phase output pump; 16. a seventh pipe; 17. an eighth conduit; 18. a ninth conduit; 181. a ninth input conduit; 182. a ninth output duct; 19. a chimney; 20. a blower.
Detailed Description
In order to make the objects, technical solutions and advantages of the present utility model more apparent, the technical solutions of the present utility model will be described in detail below. It will be apparent that the described embodiments are only some, but not all, embodiments of the utility model. All other embodiments, based on the examples herein, which are within the scope of the utility model as defined by the claims, will be within the scope of the utility model as defined by the claims.
Examples
Based on the attached figure 1, the system for treating tail gas of lithium extraction and acidification by the sulfuric acid method comprises an acidification kiln 1, a slurry mixing tank 3, a wet venturi dust collector 2 and an absorption tower 4;
the exhaust port of the acidification kiln 1 is connected with the tail gas inlet of the wet venturi dust collector 2 through a first pipeline 5, and the first pipeline 5 is used for conveying the acidification tail gas;
the liquid outlet of the slurry mixing tank 3 is connected with the liquid phase inlet of the wet venturi dust collector 2 through a second pipeline 6, and the second pipeline 6 is used for conveying slurry mixing which is lithium-containing solution generated or recovered in the process of extracting lithium by a sulfuric acid method;
the exhaust port of the wet venturi dust collector 2 is connected with the tail gas inlet of the absorption tower 4 through a third pipeline 7, the third pipeline 7 is used for conveying the acidified tail gas after dust removal, and lithium hydroxide and/or lithium carbonate absorption liquid is arranged inside the absorption tower 4.
In some examples, when the temperature of the lithium-containing solution produced or recovered by the lithium extraction process by the sulfuric acid method is higher as the slurry adjustment liquid, the heat exchanger 8 needs to be arranged to cool, and the second pipeline 6 comprises a second input pipeline 61 and a second output pipeline 62; one end of the second input pipeline 61 is connected with a liquid outlet of the slurry mixing tank 3, and the other end of the second input pipeline 61 is connected with an inlet of the heat exchanger 8; one end of the second output pipeline 62 is connected with the outlet of the heat exchanger 8, and the other end of the second output pipeline 62 is connected with the liquid phase inlet of the wet venturi dust collector 2.
In some examples, the acidified tail gas and the slurry are input into the wet venturi dust collector 2, and the slurry can absorb the acidified dust in the acidified tail gas on one hand and exchange heat with the gas phase of the acidified tail gas on the other hand; because the temperature of the tail gas after acidification and roasting is up to 200-250 ℃, and a large amount of thermal mass is carried, the subsequent treatment is not facilitated, the temperature of the tail gas can be reduced to be less than or equal to 70 ℃ by adjusting the heat exchange between the slurry and the acidified tail gas, the post-treatment process is safer, and the heat-resistant requirements of post-treatment equipment and devices are reduced; in addition, the specific heat capacity of the liquid is generally larger than that of the gas, and the liquid is used as a medium for absorbing the acidified tail gas, so that the heat exchange effect is good.
In some examples, a heat exchanger 8 or a heat recoverer may also be provided on the first conduit 5 to cool the acidified tail gas while recovering the heat energy of the acidified tail gas.
In some examples, heat exchange by heat exchanger 8 is not required when the temperature of the conditioned slurry used is below 70 ℃, particularly when the temperature of the conditioned slurry is at ambient temperature of 25-30 ℃; in order to realize the switching between no heat exchange and heat exchange so as to adapt to different temperatures of slurry adjustment, a connecting pipe is arranged between the second input pipeline 61 and the second output pipeline 62, is connected with the heat exchanger 8 in parallel, and is provided with valves which can be opened/closed at the inlet and the outlet of the connecting pipe and the heat exchanger 8; when the slurry is mixed at normal temperature, the valve of the inlet and outlet of the heat exchanger 8 is closed; when the temperature of the slurry is higher than 70 ℃, the valve on the connecting pipe is closed, and a heat exchange medium is introduced into the heat exchanger 8 so as to cool the slurry.
In some examples, the flow rate of the conditioning fluid into the wet venturi scrubber 2 is dependent on the heat exchange amount of the acidified tail gas and the conditioning fluid to ensure that the temperature of the acidified tail gas phase passing through the wet venturi scrubber 2 is below 70 ℃.
In some examples, the liquid outlet of the slurry mixing tank 3 is connected with the slurry mixing pump 9, and the output port of the slurry mixing pump 9 is connected with the second input pipeline 61; the slurry mixing pump 9 can boost the pressure of the slurry to facilitate the transportation of the slurry.
In some examples, the slurry mixing pump 9 is preferably a variable frequency pump, and can adjust the flow rate of the slurry mixing liquid conveyed by the second pipeline 6, and can be used as an alternative to arranging a flowmeter on the second pipeline 6; of course, when the size mixing pump 9 is selected as a non-variable frequency pump, a flow meter may be provided on the second pipe 6 in order to determine the size of the size mixing liquid to be fed into the wet venturi scrubber 2.
In some examples, a thermometer is provided on the second conduit 6, in particular at the inlet and/or at the outlet of the heat exchanger 8, to adjust the delivery of the heat exchange medium, monitoring the temperature of the conditioned slurry entering the wet venturi scrubber 2.
In some examples, the discharge port of the acidification kiln 1 is connected to the feed port of the acidification cooling kiln 11 through a fourth pipeline 10, and the discharge port of the acidification cooling kiln 11 is connected to the size mixing tank 13 through a fifth pipeline 12; the lithium-containing material based on the sulfuric acid method for extracting lithium in the acidification kiln 1 is input into an acidification cooling kiln 11 through a fourth pipeline 10 for cooling so as to obtain clinker.
In some examples, to achieve size mixing, a stirrer is provided inside the size mixing tank 13.
In some examples, in order to transfer the clinker extracted by the sulfuric acid process in the acidification kiln 1 into the acidification cooling kiln 11, a screw conveyor may be provided on the fourth conduit 10 to transfer the clinker from low to high.
In some examples, in order to transfer the clinker in the acidification cooling kiln 11 into the surge tank 13, a screw conveyor may be provided on the fifth conduit 12 to transfer the clinker from low to high.
In some examples, the liquid phase outlet of the wet venturi scrubber 2 is connected to the surge tank 13 by a sixth conduit 14; the dust in the acidified tail gas is taken out from the wet venturi dust remover 2 by the slurry mixing liquid, heat exchange and gas-liquid separation of the acidified tail gas are carried out, and the slurry mixing liquid is lithium-containing solution, so that the dust in the acidified tail gas also contains lithium dust, and the slurry mixing liquid is conveyed to the slurry mixing tank 13, so that the clinker can be mixed, the loss of lithium resources can be reduced, and waste water is not generated in the processes of dust removal and cooling by adopting the slurry mixing liquid.
In some examples, the liquid phase outlet of the wet venturi scrubber 2 is connected to a liquid phase output pump 15, and the output of the liquid phase output pump 15 is connected to a sixth conduit 14.
In some examples, the sixth conduit 14 includes a sixth input conduit and a sixth output conduit, one end of the sixth input conduit being connected to the liquid phase outlet of the wet venturi scrubber 2, the other end of the sixth input conduit being connected to the inlet of the liquid phase output pump 15; one end of the sixth output pipe is connected with the outlet of the liquid phase output pump 15, and the other end of the sixth output pipe is connected with the slurry mixing tank 13.
In some examples, a slurry mixing and returning pipeline (not shown in fig. 1) is arranged between the sixth pipeline 14 and the second input pipeline 61 or the second output pipeline 62, so as to return the slurry mixing liquid discharged by the wet venturi dust collector 2, and improve the dust removing adsorption and heat exchanging effects of the slurry mixing liquid; when the heat exchange amount of the slurry discharged by the wet venturi dust collector 2 is small, the discharged slurry is circularly used in the wet venturi dust collector 2 through the slurry-mixing feedback pipeline and the second output pipeline 62; when the dust removal adsorption amount of the slurry discharged by the wet venturi dust collector 2 is low, the discharged slurry is conveyed back to the wet venturi dust collector 2 for recycling through the slurry return conveying pipeline, the second input pipeline 61, the heat exchanger 8 and the second output pipeline 62.
In some examples, the drain of the absorber tower 4 is connected to the surge tank 13 via a seventh conduit 16.
In this embodiment, the absorption solution adopts lithium hydroxide and/or lithium carbonate solution, and can react with the acidified tail gas of the lithium extraction by the sulfuric acid method to generate lithium sulfate, and the solution containing lithium sulfate is input into the slurry mixing tank 13, mixed with clinker for slurry mixing, and then can be used as a raw material in the next leaching process.
In some examples, the absorption tower 4 is a spray tower, a packed tower, a liquid injection tower, or the like, preferably a spray tower, provided with a circulation pump to allow lithium hydroxide and/or lithium carbonate to sufficiently absorb the acidified tail gas, converting to lithium sulfate; no waste water is generated in the process of treating the acidified tail gas by adopting the absorption tower 4; lithium hydroxide and/or lithium carbonate are produced or recovered from the sulfuric acid process lithium extraction process.
In some examples, to buffer the absorption liquid containing lithium sulfate, the seventh pipe 16 includes a seventh input pipe and a seventh output pipe, one end of the seventh input pipe is connected to the absorption tower 4, the other end of the seventh input pipe is connected to the inlet of the absorption liquid buffer tank, one end of the seventh output pipe is connected to the outlet of the absorption liquid buffer tank, and the other end of the seventh output pipe is connected to the slurry mixing tank 13.
In some examples, the drain port of the size mixing tank 3 is connected to the size mixing tank 13 via an eighth conduit 17.
In some examples, the size mixing tank 3 is provided with an overflow port to prevent excessive size mixing liquid stored in the size mixing tank 3, and the overflow port of the size mixing tank 3 is connected with an eighth pipeline 17 to convey the overflowed size mixing liquid into the size mixing tank 13 for size mixing.
In some examples, the tail gas outlet of absorber 4 is connected to stack 19 by a ninth conduit 18; the acidified tail gas is treated by the absorption liquid in the absorption tower 4, so that not only acidic substances in the acidified tail gas are removed through reaction, but also the absorption liquid can play a certain role in dedusting the acidified tail gas.
In some examples, the ninth conduit 18 includes a ninth input conduit 181 and a ninth output conduit 182; one end of a ninth input pipeline 181 is connected with a tail gas outlet of the absorption tower 4, and the other end of the ninth input pipeline 181 is connected with an input port of the fan 20; one end of the ninth output pipe 182 is connected to the output port of the blower 20, and the other end of the ninth output pipe 182 is connected to the chimney 19.
In some examples, the ninth output duct 182 includes a ninth output duct a and a ninth output duct B, one end of the ninth output duct a being connected to the input port of the blower 20, the other end of the ninth output duct a being connected to the electrostatic precipitator, one end of the ninth output duct B being connected to the outlet of the electrostatic precipitator, the other end of the ninth output duct B being connected to the inlet of the chimney 19; the electrostatic precipitator is arranged, so that substances such as ionic groups, particles and the like with static electricity in the flue gas discharged from the absorption tower 4 can be removed.
In some examples, a plurality of absorption towers 4 are serially connected in series, each absorption tower 4 is internally provided with absorption liquid,
in some examples, the electrostatic precipitator is provided with a flushing liquid input pipeline and a flushing liquid output pipeline, and the flushing liquid input pipeline conveys flushing liquid into the electrostatic precipitator so as to clean the electrostatic precipitator; one end of the flushing fluid output pipeline is connected with a liquid outlet of the electrostatic precipitator, and the other end of the flushing fluid output pipeline is connected with the slurry mixing tank 13 so as to convey flushing fluid into the slurry mixing tank 13 and participate in the slurry mixing process.
The sulfuric acid method lithium extraction acidification tail gas treatment system can treat the acidic tail gas generated by the sulfuric acid method lithium extraction acidification kiln 1 at low cost and high efficiency, the wet venturi dust remover 2 uses the slurry, lithium-containing dust in the acidic tail gas can be removed, the absorption tower 4 uses lithium hydroxide and/or lithium carbonate absorption liquid, and SO in the acidification tail gas can be further removed 2 、SO 3 And acid gases are reacted to generate lithium sulfate, so that the recycling of lithium elements in the process of extracting lithium by a sulfuric acid method is realized.
The utility model carries out dust removal and acid removal treatment on the acidified tail gas, the adopted size mixing liquid and absorption liquid are both from lithium-containing solution produced or recovered in the process of extracting lithium by the sulfuric acid method, and the used size mixing liquid and absorption liquid are used for size mixing, so that the loss of lithium resources in the process of extracting lithium by the sulfuric acid method can be reduced to the greatest extent.
Claims (10)
1. The tail gas treatment system for extracting lithium by a sulfuric acid method comprises an acidification kiln and is characterized by also comprising a slurry mixing liquid tank, a wet venturi dust remover and an absorption tower;
the exhaust port of the acidification kiln is connected with the tail gas inlet of the wet venturi dust collector through a first pipeline, and the first pipeline is used for conveying the acidification tail gas;
the liquid outlet of the slurry mixing tank is connected with the liquid phase inlet of the wet venturi dust collector through a second pipeline, and the second pipeline is used for conveying slurry mixing;
the exhaust port of the wet venturi dust collector is connected with the tail gas inlet of the absorption tower through a third pipeline, the third pipeline is used for conveying the acidified tail gas after dust removal, and lithium hydroxide and/or lithium carbonate absorption liquid is arranged inside the absorption tower.
2. The sulfuric acid process lithium extraction acidification tail gas treatment system according to claim 1, wherein said second conduit comprises a second input conduit and a second output conduit;
one end of the second input pipeline is connected with a liquid outlet of the slurry mixing tank, and the other end of the second input pipeline is connected with an inlet of the heat exchanger;
one end of the second output pipeline is connected with the outlet of the heat exchanger, and the other end of the second output pipeline is connected with the liquid phase inlet of the dust remover.
3. The tail gas treatment system for lithium extraction and acidification by sulfuric acid process according to claim 2, wherein a liquid outlet of the slurry mixing tank is connected with a slurry mixing pump, and an output port of the slurry mixing pump is connected with the second input pipeline.
4. The tail gas treatment system for extracting lithium and acidizing by a sulfuric acid process according to claim 1, wherein the discharge port of the acidizing kiln is connected with the feed port of the acidizing cooling kiln through a fourth pipeline, and the discharge port of the acidizing cooling kiln is connected with the size mixing tank through a fifth pipeline.
5. The sulfuric acid process lithium extraction acidification tail gas treatment system according to claim 4, wherein a liquid phase outlet of the wet venturi scrubber is connected with the size mixing tank through a sixth pipeline.
6. The sulfuric acid process lithium extraction acidification tail gas treatment system according to claim 5, wherein a liquid phase outlet of the wet venturi scrubber is connected with a liquid phase output pump, and an output end of the liquid phase output pump is connected with the sixth pipeline.
7. The sulfuric acid process lithium extraction acidification tail gas treatment system according to claim 4, wherein a liquid outlet of the absorption tower is connected with the size mixing tank through a seventh pipeline.
8. The sulfuric acid process lithium extraction acidification tail gas treatment system according to claim 4, wherein a liquid outlet of the slurry mixing tank is connected with the slurry mixing tank through an eighth pipeline.
9. The system for treating tail gas of lithium extraction acidification by sulfuric acid process according to any one of claims 1 to 8, wherein the tail gas outlet of the absorption tower is connected with a chimney through a ninth pipeline.
10. The sulfuric acid process lithium extraction acidification tail gas treatment system according to claim 9, wherein said ninth conduit comprises a ninth input conduit and a ninth output conduit;
one end of the ninth input pipeline is connected with a tail gas outlet of the absorption tower, and the other end of the ninth input pipeline is connected with an input port of a fan;
one end of the ninth output pipeline is connected with the output port of the fan, and the other end of the ninth output pipeline is connected with the chimney.
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