CN206635376U - A kind of Tin concentrate ore-sorting system for removing arsenic removal and sulphur - Google Patents
A kind of Tin concentrate ore-sorting system for removing arsenic removal and sulphur Download PDFInfo
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- CN206635376U CN206635376U CN201720295875.8U CN201720295875U CN206635376U CN 206635376 U CN206635376 U CN 206635376U CN 201720295875 U CN201720295875 U CN 201720295875U CN 206635376 U CN206635376 U CN 206635376U
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- ore
- tin
- sulphur
- tin concentrate
- concentrate
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- ATJFFYVFTNAWJD-UHFFFAOYSA-N Tin Chemical compound [Sn] ATJFFYVFTNAWJD-UHFFFAOYSA-N 0.000 title claims abstract description 131
- 239000012141 concentrate Substances 0.000 title claims abstract description 121
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 title claims abstract description 63
- 229910052785 arsenic Inorganic materials 0.000 title claims abstract description 59
- RQNWIZPPADIBDY-UHFFFAOYSA-N arsenic atom Chemical compound [As] RQNWIZPPADIBDY-UHFFFAOYSA-N 0.000 title claims abstract description 59
- 239000005864 Sulphur Substances 0.000 title claims abstract description 52
- 239000000463 material Substances 0.000 claims abstract description 68
- 238000005188 flotation Methods 0.000 claims abstract description 47
- 239000000203 mixture Substances 0.000 claims abstract description 37
- 230000008676 import Effects 0.000 claims abstract description 31
- 238000002156 mixing Methods 0.000 claims abstract description 31
- 239000002253 acid Substances 0.000 claims abstract description 21
- TUZCOAQWCRRVIP-UHFFFAOYSA-N butoxymethanedithioic acid Chemical compound CCCCOC(S)=S TUZCOAQWCRRVIP-UHFFFAOYSA-N 0.000 claims abstract description 21
- 239000004088 foaming agent Substances 0.000 claims abstract description 21
- VAJVDSVGBWFCLW-UHFFFAOYSA-N 3-Phenyl-1-propanol Chemical compound OCCCC1=CC=CC=C1 VAJVDSVGBWFCLW-UHFFFAOYSA-N 0.000 claims abstract description 9
- DYUQAZSOFZSPHD-UHFFFAOYSA-N Phenylpropyl alcohol Natural products CCC(O)C1=CC=CC=C1 DYUQAZSOFZSPHD-UHFFFAOYSA-N 0.000 claims abstract description 9
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims description 36
- -1 floation tank Chemical compound 0.000 claims description 19
- 229910000029 sodium carbonate Inorganic materials 0.000 claims description 18
- GCLGEJMYGQKIIW-UHFFFAOYSA-H sodium hexametaphosphate Chemical compound [Na]OP1(=O)OP(=O)(O[Na])OP(=O)(O[Na])OP(=O)(O[Na])OP(=O)(O[Na])OP(=O)(O[Na])O1 GCLGEJMYGQKIIW-UHFFFAOYSA-H 0.000 claims description 15
- 238000000034 method Methods 0.000 abstract description 9
- 238000010276 construction Methods 0.000 abstract description 2
- 230000008569 process Effects 0.000 abstract description 2
- 239000002893 slag Substances 0.000 description 25
- 239000013067 intermediate product Substances 0.000 description 19
- 239000003638 chemical reducing agent Substances 0.000 description 18
- 230000004907 flux Effects 0.000 description 18
- 238000004519 manufacturing process Methods 0.000 description 18
- 238000003723 Smelting Methods 0.000 description 13
- 125000001797 benzyl group Chemical group [H]C1=C([H])C([H])=C(C([H])=C1[H])C([H])([H])* 0.000 description 11
- 150000001875 compounds Chemical class 0.000 description 11
- 229910052717 sulfur Inorganic materials 0.000 description 11
- 239000011593 sulfur Substances 0.000 description 11
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical group O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 8
- XOLBLPGZBRYERU-UHFFFAOYSA-N tin dioxide Chemical compound O=[Sn]=O XOLBLPGZBRYERU-UHFFFAOYSA-N 0.000 description 8
- 229910001887 tin oxide Inorganic materials 0.000 description 8
- 238000006477 desulfuration reaction Methods 0.000 description 7
- 230000023556 desulfurization Effects 0.000 description 7
- 241000876852 Scorias Species 0.000 description 6
- 241001062472 Stokellia anisodon Species 0.000 description 6
- IQUSIJUQYSBUAC-UHFFFAOYSA-N [Sn].[As].[S] Chemical compound [Sn].[As].[S] IQUSIJUQYSBUAC-UHFFFAOYSA-N 0.000 description 6
- 238000004458 analytical method Methods 0.000 description 6
- 238000000227 grinding Methods 0.000 description 6
- 238000005245 sintering Methods 0.000 description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 6
- MOMKYJPSVWEWPM-UHFFFAOYSA-N 4-(chloromethyl)-2-(4-methylphenyl)-1,3-thiazole Chemical compound C1=CC(C)=CC=C1C1=NC(CCl)=CS1 MOMKYJPSVWEWPM-UHFFFAOYSA-N 0.000 description 5
- 230000009429 distress Effects 0.000 description 5
- 235000019983 sodium metaphosphate Nutrition 0.000 description 5
- 239000000571 coke Substances 0.000 description 4
- 239000003500 flue dust Substances 0.000 description 4
- 239000000377 silicon dioxide Substances 0.000 description 4
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 3
- 235000019738 Limestone Nutrition 0.000 description 3
- RHZUVFJBSILHOK-UHFFFAOYSA-N anthracen-1-ylmethanolate Chemical compound C1=CC=C2C=C3C(C[O-])=CC=CC3=CC2=C1 RHZUVFJBSILHOK-UHFFFAOYSA-N 0.000 description 3
- 239000003830 anthracite Substances 0.000 description 3
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 3
- 239000006028 limestone Substances 0.000 description 3
- 229910052760 oxygen Inorganic materials 0.000 description 3
- 239000001301 oxygen Substances 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- CWYNVVGOOAEACU-UHFFFAOYSA-N Fe2+ Chemical compound [Fe+2] CWYNVVGOOAEACU-UHFFFAOYSA-N 0.000 description 2
- 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 2
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 238000002485 combustion reaction Methods 0.000 description 2
- 230000007812 deficiency Effects 0.000 description 2
- 229910052751 metal Inorganic materials 0.000 description 2
- 239000002184 metal Substances 0.000 description 2
- 229910052708 sodium Inorganic materials 0.000 description 2
- 239000011734 sodium Substances 0.000 description 2
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- SSISHJJTAXXQAX-ZETCQYMHSA-N L-ergothioneine Chemical compound C[N+](C)(C)[C@H](C([O-])=O)CC1=CNC(=S)N1 SSISHJJTAXXQAX-ZETCQYMHSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 239000002802 bituminous coal Substances 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000003546 flue gas Substances 0.000 description 1
- PCHJSUWPFVWCPO-UHFFFAOYSA-N gold Chemical compound [Au] PCHJSUWPFVWCPO-UHFFFAOYSA-N 0.000 description 1
- 239000010931 gold Substances 0.000 description 1
- 229910052737 gold Inorganic materials 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 239000000155 melt Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000002269 spontaneous effect Effects 0.000 description 1
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- Manufacture And Refinement Of Metals (AREA)
Abstract
The utility model discloses a kind of Tin concentrate ore-sorting system for removing arsenic removal and sulphur, the ore-sorting system includes floation tank, rotary kiln and electric furnace, and electric furnace is provided with mixtures of materials import, and mixtures of materials import is connected with material mixing pit；Floation tank is provided with high pozzuolite Tin concentrate ore pulp import and No. two phenylpropyl alcohol hydroximic acid, butyl xanthate and foaming agent oil inlets, and floation tank is additionally provided with flotation concentrate outlet and flotation tailing outlet, and both are respectively connecting to rotary kiln and material mixing pit.Ore-sorting system of the present utility model is simple in construction, and arsenic removal and sulphur can be effectively gone using the ore-sorting system, and reduces the loss of the tin in ore dressing process, high financial profit.
Description
Technical field
It the utility model is related to a kind of ore-sorting system, and in particular to a kind of Tin concentrate ore-sorting system for removing arsenic removal and sulphur.Category
In non-ferrous metal ore technical field.
Background technology
The smelting and its efforts at environmental protection of arsenic, sulfur content to tin in Tin concentrate has a great influence, therefore to arsenic, sulphur in Tin concentrate
Content requirement it is tighter.It is the method generally used at present using rotary kiln dearsenification desulfurization, high pozzuolite ore deposit in production process with producing
Through rotary kiln high temperature dearsenification sulphur after raw intermediate products scoria mixing, still, tin ferrous metal fusing point in part is low in scoria, thing
Material melts conglomeration in kiln internal cause scoria, and after conglomeration, heat does not distribute in time, sulphur spontaneous combustion at high temperature, temperature more and more higher, temperature
Degree exceedes the fusing point of material, and partial material starts to melt, and material conglomeration by becomes to tie kiln, when knot kiln is too thick, the inside part
Thioneine does not have enough oxygen to participate in reaction, and at high temperature, sulphur reacts generation artificial gold formation gaseous state with tin and taken away with flue gas, sulphur
Change reaction generation sulfur dioxide and tin oxide, tin oxide when tin runs into the oxygen in air to collect in bagroom, therefore,
The stanniferous height of flue dust, it is general up to 8~12%, sometimes up to more than 20%, roasted ore arsenic+sulphur≤0.8%.Mode of heating is using combustion
Burn bituminous coal to directly heat, oxygen enters kiln body deficiency.
The content of the invention
The purpose of this utility model is to overcome above-mentioned the deficiencies in the prior art, there is provided a kind of Tin concentrate for removing arsenic removal and sulphur
Ore-sorting system.
To achieve the above object, the utility model uses following technical proposals：
A kind of Tin concentrate ore-sorting system for removing arsenic removal and sulphur, including floation tank, rotary kiln and electric furnace, the electric furnace are provided with thing
Expect mixture intake, mixtures of materials import is connected with material mixing pit；The floation tank enters provided with high pozzuolite Tin concentrate ore pulp
Mouth and No. two phenylpropyl alcohol hydroximic acid, butyl xanthate and foaming agent oil inlets, the floation tank are additionally provided with flotation concentrate outlet and floated
Mine tailing is selected to export, both are respectively connecting to rotary kiln and material mixing pit.
Preferably, the rotary kiln exports provided with roasted ore, and it is connected to material mixing pit.
Preferably, the electric furnace is additionally provided with sodium carbonate and calgon import.
A kind of Tin concentrate ore-dressing technique for removing arsenic removal and sulphur, is comprised the following steps that corresponding to above-mentioned ore-sorting system：
(1) Tin concentrate is taken, picks out high pozzuolite Tin concentrate and low pozzuolite Tin concentrate, low pozzuolite Tin concentrate is standby, by high arsenic
Sulphur Tin concentrate ore grinding accounts for 90~95% to -0.074mm, and it is 25~30% to add water to size mixing to ore pulp mass concentration, sequentially adds benzene
No. two first hydroximic acid, butyl xanthate and foaming agent oil, flotation is carried out, obtain flotation concentrate and flotation tailing；
(2) flotation concentrate is sent into rotary kiln, high-temperature roasting dearsenification desulfurization, during roasting control do not lump, be calcined
Ore deposit；
(3) low pozzuolite Tin concentrate, roasted ore, reducing agent, flux and production intermediate products are well mixed, obtain material and mix
Compound, first take the mixtures of materials of quality accounting 50% to be sent into 1100~1250 DEG C of smeltings in electric furnace, after 1~3 hour, add carbon
Sour sodium and calgon, then take remaining mixtures of materials to be sent into electric furnace and smelt, after smelting 5~8 hours, put for the first time
Tin, after mixtures of materials has all melted, tin is put for the second time, slag making is carried out, then adds flotation tailing, furnace temperature is increased to 1400
~1500 DEG C, the tin gangue for making all infusibilities is in molten condition, and tin oxide is fully reduced into metallic tin, tin is separated with slag, takes
Slag sample analysis, when stanniferous amount is less than 5% in slag specimen, slagging, terminate.
Preferably, in step (1), quality accounting >=3% of arsenic and sulphur in the high pozzuolite Tin concentrate, low pozzuolite Tin concentrate
The quality accounting ＜ 3% of middle arsenic and sulphur.
Preferably, in step (1), No. two high pozzuolite Tin concentrate, benzyl hydroximic acid, butyl xanthate and foaming agent oily quality
Than for 1：0.1~0.2：0.01~0.03：0.01~0.02.
Preferably, in step (2), sintering temperature is 800~900 DEG C, and roasting time is 1~3 hour.
Preferably, after step (2) terminates, the total amount that the content summation of arsenic and sulphur accounts for roasted ore is not higher than 0.5%, arsenic and sulphur
Removal efficiency be not less than 85%.
Preferably, in step (3), the reducing agent is coke or anthracite；The flux is silica or lime stone；It is described
Production intermediate products are the mixture of one or both of flue dust, scoria.
Preferably, in step (3), the low pozzuolite Tin concentrate, roasted ore, reducing agent, flux, production intermediate products, carbon
The mass ratio of sour sodium and calgon is 1：1~3：0.1~0.3：0.1~0.3：1~3：0.1~0.2：0.5~0.8.
The beneficial effects of the utility model：
Ore-sorting system of the present utility model is simple in construction, can effectively go arsenic removal and sulphur using the ore-sorting system, and drop
Tin loss in low ore dressing process, high financial profit.
Brief description of the drawings
Fig. 1 is ore-sorting system structural representation of the present utility model；
Wherein, 1 is floation tank, and 2 be rotary kiln, and 3 be electric furnace, and 4 be material mixing pit, and 11 be that high pozzuolite Tin concentrate ore pulp enters
Mouthful, 12 be No. two phenylpropyl alcohol hydroximic acid, butyl xanthate and foaming agent oil inlets, and 13 be that flotation concentrate exports, and 14 go out for flotation tailing
Mouthful, 21 be that roasted ore exports, and 31 be mixtures of materials import, and 32 be sodium carbonate and calgon import.
Embodiment
The utility model is further elaborated with reference to the accompanying drawings and examples, it should explanation, under state
It is bright merely to explain the utility model, its content is not defined.
Embodiment 1：
As shown in figure 1, a kind of Tin concentrate ore-sorting system for removing arsenic removal and sulphur, including floation tank 1, rotary kiln 2 and electric furnace 3,
Electric furnace 3 is provided with mixtures of materials import 31, and mixtures of materials import 31 is connected with material mixing pit 4；Floation tank 1 is provided with high pozzuolite
Tin concentrate ore pulp import 11 and No. two phenylpropyl alcohol hydroximic acid, butyl xanthate and foaming agent oil inlets 12, floation tank 1 are additionally provided with flotation
Concentrate outlet 13 and flotation tailing outlet 14, both are respectively connecting to rotary kiln 2 and material mixing pit 4.
Rotary kiln 2 is provided with roasted ore outlet 21, and it is connected to material mixing pit 4.
Electric furnace 3 is additionally provided with sodium carbonate and calgon import 32.
A kind of Tin concentrate ore-dressing technique for removing arsenic removal and sulphur, is comprised the following steps that corresponding to above-mentioned ore-sorting system：
(1) Tin concentrate is taken, picks out high pozzuolite Tin concentrate and low pozzuolite Tin concentrate, low pozzuolite Tin concentrate is standby, by high arsenic
Sulphur Tin concentrate ore grinding accounts for 90% to -0.074mm, and it is 25% to add water to size mixing to ore pulp mass concentration, sequentially add benzyl hydroximic acid,
No. two oil of butyl xanthate and foaming agent, flotation is carried out, obtain flotation concentrate and flotation tailing；
(2) flotation concentrate is sent into rotary kiln 2, high-temperature roasting dearsenification desulfurization, during roasting control do not lump, be calcined
Ore deposit；
(3) low pozzuolite Tin concentrate, roasted ore, reducing agent, flux and production intermediate products are well mixed, obtain material and mix
Compound, first take the mixtures of materials of quality accounting 50% to be sent into 1100 DEG C of smeltings in electric furnace 3, after 1 hour, add sodium carbonate and six
Sodium metaphosphate, then take remaining mixtures of materials to be sent into electric furnace 3 and smelt, after smelting 5 hours, tin is put for the first time, treats that material mixes
After compound has all melted, tin is put for the second time, slag making is carried out, then adds flotation tailing, and furnace temperature is increased to 1400 DEG C, makes institute in distress
Molten tin gangue is in molten condition, and tin oxide is fully reduced into metallic tin, tin is separated with slag, slag sample analysis is taken, when in slag specimen
When stanniferous amount is less than 5%, slagging, terminate.
In step (1), quality accounting >=3% of arsenic and sulphur in the high pozzuolite Tin concentrate, in low pozzuolite Tin concentrate arsenic and
The quality accounting ＜ 3% of sulphur；No. two high pozzuolite Tin concentrate, benzyl hydroximic acid, butyl xanthate and foaming agent oily mass ratioes are 1：
0.1：0.01：0.01.
In step (2), sintering temperature is 800 DEG C, and roasting time is 1 hour；After step (2) terminates, the content of arsenic and sulphur
Summation accounts for the total amount of roasted ore not higher than 0.5%, and the removal efficiency of arsenic and sulphur is not less than 85%.
In step (3), the reducing agent is coke；The flux is silica；The production intermediate products are flue dust；It is described
Low pozzuolite Tin concentrate, roasted ore, reducing agent, flux, production intermediate products, the mass ratio of sodium carbonate and calgon are 1：1：
0.1：0.1：1：0.1：0.5.
The batch Tin concentrate stanniferous 43.22%, containing arsenic 6.45%, sulfur-bearing 8.98%, after being handled using embodiment 1, obtain
The Tin concentrate of yield 85.2%, its stanniferous 57.12%, containing arsenic 0.53%, sulfur-bearing 0.57%.
Embodiment 2：
As shown in figure 1, a kind of Tin concentrate ore-sorting system for removing arsenic removal and sulphur, including floation tank 1, rotary kiln 2 and electric furnace 3,
Electric furnace 3 is provided with mixtures of materials import 31, and mixtures of materials import 31 is connected with material mixing pit 4；Floation tank 1 is provided with high pozzuolite
Tin concentrate ore pulp import 11 and No. two phenylpropyl alcohol hydroximic acid, butyl xanthate and foaming agent oil inlets 12, floation tank 1 are additionally provided with flotation
Concentrate outlet 13 and flotation tailing outlet 14, both are respectively connecting to rotary kiln 2 and material mixing pit 4.
Rotary kiln 2 is provided with roasted ore outlet 21, and it is connected to material mixing pit 4.
Electric furnace 3 is additionally provided with sodium carbonate and calgon import 32.
A kind of Tin concentrate ore-dressing technique for removing arsenic removal and sulphur, is comprised the following steps that corresponding to above-mentioned ore-sorting system：
(1) Tin concentrate is taken, picks out high pozzuolite Tin concentrate and low pozzuolite Tin concentrate, low pozzuolite Tin concentrate is standby, by high arsenic
Sulphur Tin concentrate ore grinding accounts for 95% to -0.074mm, and it is 30% to add water to size mixing to ore pulp mass concentration, sequentially add benzyl hydroximic acid,
No. two oil of butyl xanthate and foaming agent, flotation is carried out, obtain flotation concentrate and flotation tailing；
(2) flotation concentrate is sent into rotary kiln 2, high-temperature roasting dearsenification desulfurization, during roasting control do not lump, be calcined
Ore deposit；
(3) low pozzuolite Tin concentrate, roasted ore, reducing agent, flux and production intermediate products are well mixed, obtain material and mix
Compound, first take the mixtures of materials of quality accounting 50% to be sent into 1250 DEG C of smeltings in electric furnace 3, after 3 hours, add sodium carbonate and six
Sodium metaphosphate, then take remaining mixtures of materials to be sent into electric furnace 3 and smelt, after smelting 8 hours, tin is put for the first time, treats that material mixes
After compound has all melted, tin is put for the second time, slag making is carried out, then adds flotation tailing, and furnace temperature is increased to 1500 DEG C, makes institute in distress
Molten tin gangue is in molten condition, and tin oxide is fully reduced into metallic tin, tin is separated with slag, slag sample analysis is taken, when in slag specimen
When stanniferous amount is less than 5%, slagging, terminate.
In step (1), quality accounting >=3% of arsenic and sulphur in the high pozzuolite Tin concentrate, in low pozzuolite Tin concentrate arsenic and
The quality accounting ＜ 3% of sulphur；No. two high pozzuolite Tin concentrate, benzyl hydroximic acid, butyl xanthate and foaming agent oily mass ratioes are 1：
0.2：0.03：0.02.
In step (2), sintering temperature is 900 DEG C, and roasting time is 3 hours；After step (2) terminates, the content of arsenic and sulphur
Summation accounts for the total amount of roasted ore not higher than 0.5%, and the removal efficiency of arsenic and sulphur is not less than 85%.
In step (3), the reducing agent is anthracite；The flux is lime stone；The production intermediate products are liquate
Slag；The low pozzuolite Tin concentrate, roasted ore, reducing agent, flux, the quality for producing intermediate products, sodium carbonate and calgon
Than for 1：3：0.3：0.3：3：0.2：0.8.
The batch Tin concentrate stanniferous 42.15%, containing arsenic 5.45%, sulfur-bearing 7.98%, after being handled using embodiment 2, obtain
The Tin concentrate of yield 86.2%, its stanniferous 54.33%, containing arsenic 0.43%, sulfur-bearing 0.51%.
Embodiment 3：
As shown in figure 1, a kind of Tin concentrate ore-sorting system for removing arsenic removal and sulphur, including floation tank 1, rotary kiln 2 and electric furnace 3,
Electric furnace 3 is provided with mixtures of materials import 31, and mixtures of materials import 31 is connected with material mixing pit 4；Floation tank 1 is provided with high pozzuolite
Tin concentrate ore pulp import 11 and No. two phenylpropyl alcohol hydroximic acid, butyl xanthate and foaming agent oil inlets 12, floation tank 1 are additionally provided with flotation
Concentrate outlet 13 and flotation tailing outlet 14, both are respectively connecting to rotary kiln 2 and material mixing pit 4.
Rotary kiln 2 is provided with roasted ore outlet 21, and it is connected to material mixing pit 4.
Electric furnace 3 is additionally provided with sodium carbonate and calgon import 32.
A kind of Tin concentrate ore-dressing technique for removing arsenic removal and sulphur, is comprised the following steps that corresponding to above-mentioned ore-sorting system：
(1) Tin concentrate is taken, picks out high pozzuolite Tin concentrate and low pozzuolite Tin concentrate, low pozzuolite Tin concentrate is standby, by high arsenic
Sulphur Tin concentrate ore grinding accounts for 90% to -0.074mm, and it is 30% to add water to size mixing to ore pulp mass concentration, sequentially add benzyl hydroximic acid,
No. two oil of butyl xanthate and foaming agent, flotation is carried out, obtain flotation concentrate and flotation tailing；
(2) flotation concentrate is sent into rotary kiln 2, high-temperature roasting dearsenification desulfurization, during roasting control do not lump, be calcined
Ore deposit；
(3) low pozzuolite Tin concentrate, roasted ore, reducing agent, flux and production intermediate products are well mixed, obtain material and mix
Compound, first take the mixtures of materials of quality accounting 50% to be sent into 1100 DEG C of smeltings in electric furnace 3, after 3 hours, add sodium carbonate and six
Sodium metaphosphate, then take remaining mixtures of materials to be sent into electric furnace 3 and smelt, after smelting 5 hours, tin is put for the first time, treats that material mixes
After compound has all melted, tin is put for the second time, slag making is carried out, then adds flotation tailing, and furnace temperature is increased to 1500 DEG C, makes institute in distress
Molten tin gangue is in molten condition, and tin oxide is fully reduced into metallic tin, tin is separated with slag, slag sample analysis is taken, when in slag specimen
When stanniferous amount is less than 5%, slagging, terminate.
In step (1), quality accounting >=3% of arsenic and sulphur in the high pozzuolite Tin concentrate, in low pozzuolite Tin concentrate arsenic and
The quality accounting ＜ 3% of sulphur；No. two high pozzuolite Tin concentrate, benzyl hydroximic acid, butyl xanthate and foaming agent oily mass ratioes are 1：
0.1：0.03：0.01.
In step (2), sintering temperature is 900 DEG C, and roasting time is 1 hour；After step (2) terminates, the content of arsenic and sulphur
Summation accounts for the total amount of roasted ore not higher than 0.5%, and the removal efficiency of arsenic and sulphur is not less than 85%.
In step (3), the reducing agent is coke；The flux is lime stone；The production intermediate products are flue dust；Institute
The mass ratio for stating low pozzuolite Tin concentrate, roasted ore, reducing agent, flux, production intermediate products, sodium carbonate and calgon is 1：
3：0.1：0.3：1：0.2：0.5.
The batch Tin concentrate stanniferous 45.01%, containing arsenic 6.23%, sulfur-bearing 8.65%, after being handled using embodiment 3, obtain
The Tin concentrate of yield 85.5%, its stanniferous 59.02%, containing arsenic 0.45%, sulfur-bearing 0.41%.
Embodiment 4：
As shown in figure 1, a kind of Tin concentrate ore-sorting system for removing arsenic removal and sulphur, including floation tank 1, rotary kiln 2 and electric furnace 3,
Electric furnace 3 is provided with mixtures of materials import 31, and mixtures of materials import 31 is connected with material mixing pit 4；Floation tank 1 is provided with high pozzuolite
Tin concentrate ore pulp import 11 and No. two phenylpropyl alcohol hydroximic acid, butyl xanthate and foaming agent oil inlets 12, floation tank 1 are additionally provided with flotation
Concentrate outlet 13 and flotation tailing outlet 14, both are respectively connecting to rotary kiln 2 and material mixing pit 4.
Rotary kiln 2 is provided with roasted ore outlet 21, and it is connected to material mixing pit 4.
Electric furnace 3 is additionally provided with sodium carbonate and calgon import 32.
A kind of Tin concentrate ore-dressing technique for removing arsenic removal and sulphur, is comprised the following steps that corresponding to above-mentioned ore-sorting system：
(1) Tin concentrate is taken, picks out high pozzuolite Tin concentrate and low pozzuolite Tin concentrate, low pozzuolite Tin concentrate is standby, by high arsenic
Sulphur Tin concentrate ore grinding accounts for 95% to -0.074mm, and it is 25% to add water to size mixing to ore pulp mass concentration, sequentially add benzyl hydroximic acid,
No. two oil of butyl xanthate and foaming agent, flotation is carried out, obtain flotation concentrate and flotation tailing；
(2) flotation concentrate is sent into rotary kiln 2, high-temperature roasting dearsenification desulfurization, during roasting control do not lump, be calcined
Ore deposit；
(3) low pozzuolite Tin concentrate, roasted ore, reducing agent, flux and production intermediate products are well mixed, obtain material and mix
Compound, first take the mixtures of materials of quality accounting 50% to be sent into 1250 DEG C of smeltings in electric furnace 3, after 1 hour, add sodium carbonate and six
Sodium metaphosphate, then take remaining mixtures of materials to be sent into electric furnace 3 and smelt, after smelting 8 hours, tin is put for the first time, treats that material mixes
After compound has all melted, tin is put for the second time, slag making is carried out, then adds flotation tailing, and furnace temperature is increased to 1400 DEG C, makes institute in distress
Molten tin gangue is in molten condition, and tin oxide is fully reduced into metallic tin, tin is separated with slag, slag sample analysis is taken, when in slag specimen
When stanniferous amount is less than 5%, slagging, terminate.
In step (1), quality accounting >=3% of arsenic and sulphur in the high pozzuolite Tin concentrate, in low pozzuolite Tin concentrate arsenic and
The quality accounting ＜ 3% of sulphur；No. two high pozzuolite Tin concentrate, benzyl hydroximic acid, butyl xanthate and foaming agent oily mass ratioes are 1：
0.2：0.01：0.02.
In step (2), sintering temperature is 800 DEG C, and roasting time is 1~3 hour；After step (2) terminates, arsenic and sulphur contain
Amount summation accounts for the total amount of roasted ore not higher than 0.5%, and the removal efficiency of arsenic and sulphur is not less than 85%.
In step (3), the reducing agent is anthracite；The flux is silica；The production intermediate products are scoria；
The low pozzuolite Tin concentrate, roasted ore, reducing agent, flux, production intermediate products, the mass ratio of sodium carbonate and calgon are
1：1：0.3：0.1：3：0.1：0.8.
The batch Tin concentrate stanniferous 43.12%, containing arsenic 6.43%, sulfur-bearing 8.87%, after being handled using embodiment 4, obtain
The Tin concentrate of yield 85.2%, its stanniferous 57.78%, containing arsenic 0.43%, sulfur-bearing 0.47%.
Embodiment 5：
As shown in figure 1, a kind of Tin concentrate ore-sorting system for removing arsenic removal and sulphur, including floation tank 1, rotary kiln 2 and electric furnace 3,
Electric furnace 3 is provided with mixtures of materials import 31, and mixtures of materials import 31 is connected with material mixing pit 4；Floation tank 1 is provided with high pozzuolite
Tin concentrate ore pulp import 11 and No. two phenylpropyl alcohol hydroximic acid, butyl xanthate and foaming agent oil inlets 12, floation tank 1 are additionally provided with flotation
Concentrate outlet 13 and flotation tailing outlet 14, both are respectively connecting to rotary kiln 2 and material mixing pit 4.
Rotary kiln 2 is provided with roasted ore outlet 21, and it is connected to material mixing pit 4.
Electric furnace 3 is additionally provided with sodium carbonate and calgon import 32.
A kind of Tin concentrate ore-dressing technique for removing arsenic removal and sulphur, is comprised the following steps that corresponding to above-mentioned ore-sorting system：
(1) Tin concentrate is taken, picks out high pozzuolite Tin concentrate and low pozzuolite Tin concentrate, low pozzuolite Tin concentrate is standby, by high arsenic
Sulphur Tin concentrate ore grinding accounts for 93% to -0.074mm, and it is 27% to add water to size mixing to ore pulp mass concentration, sequentially add benzyl hydroximic acid,
No. two oil of butyl xanthate and foaming agent, flotation is carried out, obtain flotation concentrate and flotation tailing；
(2) flotation concentrate is sent into rotary kiln 2, high-temperature roasting dearsenification desulfurization, during roasting control do not lump, be calcined
Ore deposit；
(3) low pozzuolite Tin concentrate, roasted ore, reducing agent, flux and production intermediate products are well mixed, obtain material and mix
Compound, first take the mixtures of materials of quality accounting 50% to be sent into 1200 DEG C of smeltings in electric furnace 3, after 2 hours, add sodium carbonate and six
Sodium metaphosphate, then take remaining mixtures of materials to be sent into electric furnace 3 and smelt, after smelting 6 hours, tin is put for the first time, treats that material mixes
After compound has all melted, tin is put for the second time, slag making is carried out, then adds flotation tailing, and furnace temperature is increased to 1450 DEG C, makes institute in distress
Molten tin gangue is in molten condition, and tin oxide is fully reduced into metallic tin, tin is separated with slag, slag sample analysis is taken, when in slag specimen
When stanniferous amount is less than 5%, slagging, terminate.
In step (1), quality accounting >=3% of arsenic and sulphur in the high pozzuolite Tin concentrate, in low pozzuolite Tin concentrate arsenic and
The quality accounting ＜ 3% of sulphur；No. two high pozzuolite Tin concentrate, benzyl hydroximic acid, butyl xanthate and foaming agent oily mass ratioes are 1：
0.15：0.02：0.01.
In step (2), sintering temperature is 850 DEG C, and roasting time is 2 hours；After step (2) terminates, the content of arsenic and sulphur
Summation accounts for the total amount of roasted ore not higher than 0.5%, and the removal efficiency of arsenic and sulphur is not less than 85%.
In step (3), the reducing agent is coke；The flux is silica；The production intermediate products are scoria；Institute
The mass ratio for stating low pozzuolite Tin concentrate, roasted ore, reducing agent, flux, production intermediate products, sodium carbonate and calgon is 1：
2：0.2：0.2：2：0.1：0.7.
The batch Tin concentrate stanniferous 45.23%, containing arsenic 6.58%, sulfur-bearing 8.68%, after being handled using embodiment 5, obtain
The Tin concentrate of yield 85.8%, its stanniferous 59.25%, containing arsenic 0.41%, sulfur-bearing 0.38%.
It is not new to this practicality although above-mentioned specific embodiment of the present utility model is described with reference to accompanying drawing
The limitation of type protection domain, on the basis of the technical solution of the utility model, those skilled in the art need not pay creation
Property the various modifications that can make of work or deformation still within the scope of protection of the utility model.
Claims (3)
1. a kind of Tin concentrate ore-sorting system for removing arsenic removal and sulphur, including floation tank, rotary kiln and electric furnace, it is characterised in that described
Electric furnace is provided with mixtures of materials import, and mixtures of materials import is connected with material mixing pit；The floation tank is provided with high pozzuolite tin
Concentrate pulp import and No. two phenylpropyl alcohol hydroximic acid, butyl xanthate and foaming agent oil inlets, the floation tank are additionally provided with flotation essence
Ore deposit exports and flotation tailing outlet, and both are respectively connecting to rotary kiln and material mixing pit.
A kind of 2. Tin concentrate ore-sorting system for removing arsenic removal and sulphur according to claim 1, it is characterised in that the rotary kiln
Exported provided with roasted ore, it is connected to material mixing pit.
3. a kind of Tin concentrate ore-sorting system for removing arsenic removal and sulphur according to claim 1, it is characterised in that the electric furnace is also
Provided with sodium carbonate and calgon import.
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Effective date of registration: 20191114 Address after: 341400 Longhua Industrial Park, Nankang Economic Development Zone, Ganzhou City, Jiangxi Province Patentee after: Jiangxi new South Mountain Technologies Ltd Address before: 330096 Jiangxi high tech Industrial Development Zone, Nanchang Province, Nanchang University, science and Technology Park,, No. 589 high tech building, room No. 1, room 223 Patentee before: Nanchang special technology Co., Ltd. |
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