CN203403143U - Deironing device used in zinc hydrometallurgy production - Google Patents
Deironing device used in zinc hydrometallurgy production Download PDFInfo
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- CN203403143U CN203403143U CN201320525041.3U CN201320525041U CN203403143U CN 203403143 U CN203403143 U CN 203403143U CN 201320525041 U CN201320525041 U CN 201320525041U CN 203403143 U CN203403143 U CN 203403143U
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Abstract
The utility model discloses a deironing device used in zinc hydrometallurgy production. The deironing device comprises a fluidized bed roaster. An output port of the fluidized bed roaster is communicated with an input port of a first solid-liquid separation device through a neutral leaching tank, an output port of the first solid-liquid separation device is communicated with an input port of a second solid-liquid separation tank through a hot acid reduction cell, an output port in the bottom end of the second solid-liquid separation device is communicated with an input port of a flotation machine, a first output port of the flotation machine is communicated with a zinc concentrate input port of the fluidized bed roaster, a second output port of the flotation machine is communicated with an input port of a fuming furnace, an output port in the side face of the second solid-liquid separation device is communicated with an input port of a pressure filter through a preneutralization tank, a first output port of the pressure filter is communicated with an input port of a reaction still, an output port of the reaction still is communicated with an input port of a third solid-liquid separation device through a flash drum, and an output port of the fuming furnace is communicated with the inlet end of the preneutralization tank. The deironing device used in the zinc hydrometallurgy production is high in deironing rate, small in zinc loss and high in zinc recovery rate, and reduces production cost.
Description
Technical field
The utility model relates to technical field of wet metallurgy, particularly the deironing apparatus in a kind of zinc hydrometallurgy production.
Background technology
Deironing is the important topic that wet method zinc is smelted, roasting in the smelting of wet method zinc, leach, purify, the technique of electrodeposition and founding is basic identical, the key distinction has been to adopt different method for removing iron, thereby produced different wet method zinc smelting technologyes: 1, conventional method, zinc ore concentrate is after roasting, adopt neutral leaching and low Ore Leaching, zinc leaching rate about 70%, slag rate approximately 60%, iron is stayed in leached mud, this method is because Zinc in Leaching Residue is high, the general rotary kiln evaporation that adopts reclaims zinc oxide, iron is walked kiln slag and is removed, kiln slag is containing zinc approximately 1～2%, iron content approximately 25～30%, the curing slag that this method output scum is pyrogenic attack, heavy metal ion is well solidified, being convenient to slag muck deposits and sells, but this method exists energy consumption large, large and the low concentration SO2 fume of refractory wear such as need process at the problem, cause production cost high, 2, the high acid system of high temperature, zinc ore concentrate is after roasting, adopt the high Ore Leaching of high temperature, zinc leaching rate about 96～98%, most of zinc is entered solution by leaching, and a large amount of iron is also entered solution by leaching simultaneously, general infusion solution iron content 20～30g/l, need carry out independent deironing processing to meet purification requirement to the iron entering in infusion solution, produce three kinds of method for removing iron for this reason.Specific as follows: (1) jarosite process, adopt sylvite, sodium salt or ammonia salt that ferric ion in infusion solution is formed to Jarosite Residues and deironing, slag rate approximately 50%, slag is containing zinc approximately 4～6%, iron content approximately 25～30%, the vanadium slag of this method output is the sticky shape slag of wet method, belongs to dangerous solid waste, store up the special slag field that need be placed on antiseep, environment is had to disadvantageous effect; (2) goethite process, adopt air or oxygen that oxidation of divalent iron ion in infusion solution is become to ferric ion, then adopt Wingdale neutralization, form pyrrhosiderite slag, except de-iron, slag rate approximately 40%, slag is containing zinc approximately 8%, iron content approximately 35～40%, the scum of this method output is wet method gypsum tailings, store up and need be placed on antiseep slag field, top layer vegetation is reclaimed, and could meet environmental requirement; (3) hematite process, under high-temperature and high-pressure conditions, forms rhombohedral iron ore slag and deironing by oxidation of divalent iron ion in infusion solution, slag rate approximately 20%, slag is containing zinc approximately 1%, iron content approximately 50～60%, the scum of this method output is wet method powdery slag, can direct marketing cement mill and Steel Plant.
The zinc factory of current unique employing hematite process deferrization process is Japanese Iijima smeltery, this factory's zinc ore concentrate is through roasting, adopt neutral leaching and low Ore Leaching, in being isolated to, soaking supernatant liquor leaches solution of zinc sulfate and send purification, electrodeposition and founding output zinc ingot metal again, low acid sludge is through SO2 pressure leaching, in the leached mud of output, reclaim out Pb, Ag, Cu etc., leach supernatant liquor through in two sections of Wingdales and after, under high-temperature and high-pressure conditions, oxidation of divalent iron ion in infusion solution is formed to rhombohedral iron ore slag, thereby except de-iron.
Above-mentioned various wet method zinc is smelted deferrization process can be summarized as two large classes: a class is to take the pyrogenic attack leached mud technique that conventional method is representative, the feature of this method is a kind of waste (iron content), with pyrogenic process, solidify slag venting, waste is convenient to store up and sell, favourable to environmental protection, but exist zinc leaching rate low, need to adopt rotary kiln to process leached mud and reclaim zinc oxide, energy consumption is large, and low concentration SO2 fume such as need process at the problem, cause the wasting of resources, and production cost is high; Another kind ofly take the wet processing leached mud technique that the high acid system of high temperature is representative, the feature of this method is to produce two kinds of wastes, a kind of is to leach the high slag that soaks of underflow output, another kind is deironing output scum from supernatant liquor, and this method adopts the high Ore Leaching of high temperature, and zinc leaching rate is high, technological process is simple, but owing to being wet method slag, need special slag field to store up, be unfavorable for environmental protection.The wet method powdery slag that hematite process obtains can direct marketing cement mill and Steel Plant, the still current complete deironing apparatus that is not also applicable to hematite process.
Utility model content
Technical problem to be solved in the utility model is, not enough for prior art, and the deironing apparatus of a kind of zinc hydrometallurgy in producing is provided, and improves deironing rate and zinc recovery, reduces production costs, and meets the requirement of environmental protection and comprehensive utilization of resources, saves Mineral resources.
For solving the problems of the technologies described above, the technical scheme that the utility model adopts is: the deironing apparatus in a kind of zinc hydrometallurgy production, comprise the fluidizing reactor for roasting zinc ore concentrate, the delivery port of fluidizing reactor is communicated with the first solid-liquid separating equipment input aperture through neutral leaching vat, described the first solid-liquid separating equipment bottom delivery port is communicated with the second solid-liquid separating equipment input aperture through hot acid reducing bath, described the second solid-liquid separating equipment bottom delivery port is communicated with flotation machine input aperture, the first delivery port of described flotation machine is communicated with the zinc ore concentrate input aperture of described fluidizing reactor, the second delivery port of described flotation machine is communicated with fuming furnace input aperture, described the second solid-liquid separating equipment side delivery port is communicated with pressure filter input aperture through pre-neutralization groove, and the first delivery port of described pressure filter is communicated with reactor input aperture, and described reactor delivery port is communicated with the 3rd solid-liquid separating equipment input aperture by flash drum, a delivery port of described the 3rd solid-liquid separating equipment is communicated with described neutral leaching vat, a delivery port of described fuming furnace is communicated with described pre-neutralization groove inlet end.
The first solid-liquid separating equipment, the second solid-liquid separating equipment, the 3rd solid-liquid separating equipment all can adopt thickener.
The second delivery port of described pressure filter is communicated with indium recovery system, is conducive to the comprehensive utilization of resource, saves Mineral resources.
Zinc ore concentrate obtains calcining through fluidizing reactor roasting, and neutral leaching vat carry out neutrality by calcining and leach, then in being isolated to, soak supernatant liquor and in soak underflow, in soak supernatant liquor and leach solution of zinc sulfate, hot acid reduction leaching vat soak underflow in inciting somebody to action and carry out hot acid leaching, add waste electrolyte, make to take the indissoluble zinc that zinc ferrite is main existence form further to leach under high temperature peracid, reduce leaching simultaneously, add excessive zinc sulfide concentrates to make Fe3+ in solution be reduced into Fe2+, after separation, obtain reduction and leach supernatant liquor and underflow slag, reduction is leached supernatant liquor and is sent in pre-neutralization groove, underflow slag obtains sulphur concentrate and tailings through flotation machine flotation, sulphur concentrate obtains calcining through roasting together with zinc ore concentrate, calcining leaches for neutral, mine tailing obtains zinc oxide and waste residue through blast furnace fuming, add reduction to leach in supernatant liquor in zinc oxide, in pre-neutralization groove, carry out pre-neutralization, add again zinc dust precipitation to obtain indium precipitation, after thickener separation, obtain liquid and indium slag after heavy indium, after heavy indium, in liquid, pass into oxygen, control the temperature and pressure of reactor, iron precipitation in liquid after heavy indium is entered in slag, after flash drum decrease temperature and pressure, again through thickener separated dense supernatant liquor and thickened underflow (dense supernatant liquor comprise deironing after liquid and the calcining obtaining with sulfuric acid), then carry out neutrality leaching, thickened underflow is through press filtration, washing, obtain scum, indium slag send indium recovery system to reclaim, in soak supernatant liquor through purification, electrodeposition, founding, obtain zinc ingot metal, the waste electrolyte that wherein electrodeposition produces leaches for hot acid reduction.
Compared with prior art, the beneficial effect that the utility model has is: device of the present utility model is applicable to hematite process, deironing rate is high, and zinc loss is little, and the rate of recovery of zinc is high, scum can directly sell to cement mill outward or Steel Plant are used as raw material, without slag field, store up, thereby reduce production costs, and be conducive to the comprehensive utilization of environmental protection and resource, save Mineral resources, be conducive to economic Sustainable development.
Accompanying drawing explanation
Fig. 1 is the utility model one example structure schematic diagram.
Embodiment
As shown in Figure 1, the utility model one embodiment comprises the fluidizing reactor 1 for roasting zinc ore concentrate, the delivery port of fluidizing reactor 1 is communicated with the first thickener 12 input apertures through neutral leaching vat 11, described the first thickener 12 delivery ports are communicated with the second thickener 21 input apertures through hot acid reducing bath 2, described the second thickener 21 bottom delivery ports are communicated with flotation machine 3 input apertures, the first delivery port of described flotation machine 3 is communicated with the zinc ore concentrate input aperture of described fluidizing reactor 1, and the second delivery port of described flotation machine 3 is communicated with fuming furnace 31 input apertures; Described the second thickener 21 side delivery ports are communicated with pressure filter 23 input apertures through pre-neutralization groove 22, the first delivery port of described pressure filter 23 is communicated with reactor 4 input apertures, the second delivery port of pressure filter 23 is communicated with indium recovery system, and described reactor 4 delivery ports are communicated with the 3rd thickener 42 input apertures by flash drum 41; Described the 3rd thickener 42 side delivery ports are communicated with described neutral leaching vat inlet end; A delivery port of described fuming furnace 31 is communicated with described pre-neutralization groove 22 inlet ends.
In Fig. 1, A is zinc ore concentrate input aperture; B is flue gas delivery port, and flue gas is sent into the sulphuric acid plant that gathers dust; C is the first thickener 12 side delivery ports, soaks supernatant liquor in output; D is the first thickener 12 delivery ports, soaks underflow in output; E mouth input waste electrolyte, F mouth input zinc ore concentrate; G is the second thickener 22 bottom delivery ports, output underflow slag; H is the second thickener 22 side delivery ports, and output reduction is leached supernatant liquor to pre-neutralization groove 22 first input aperture N; I is the first delivery port of flotation machine 3, output sulphur concentrate; J is the second delivery port of flotation machine 3, and output mine tailing is to fuming furnace 31 input aperture K; L is fuming furnace 31 side delivery ports, and output zinc oxide is to pre-neutralization groove 22 second input aperture P; Fuming furnace 31 delivery port M output waste residues; Q is pre-neutralization groove 22 delivery ports; R is the second delivery port of pressure filter 23, exports rich indium liquid to indium recovery system; S is the first delivery port of pressure filter 23, and after the heavy indium of output, liquid is to reactor 4 input aperture T; U is reactor 4 delivery ports, and 41 input aperture V are connected with flash drum; W is flash drum 41 delivery ports; X is the 3rd thickener 42 side delivery ports, exports dense supernatant liquor, and dense supernatant liquor is delivered to neutral leaching vat; Y is the 3rd thickener 42 bottom delivery ports, and output thickened underflow send after press filtration washing, and output scum is sold outward.
The utility model equipment selects parameter as follows:
Flotation machine: volume V=60～130m
3; Thickener: cross-sectional area S=113～453m
2; Reactor: volume V=160～340m
3; Fluidizing reactor: cross-sectional area S=75～155m
2; Pressure filter: filtration area S=160～300m
2; Fuming furnace: cross-sectional area S=8～18m
2; Flash drum: volume V=15～40m
3.
The workflow of the utility model device is as follows:
Zinc ore concentrate obtains calcining and flue gas through fluidizing reactor 1 roasting, control 950～980 ℃ of calcining temperature, calcining is sent into neutral leaching vat 11 and carry out neutrality leaching, control 40～60 ℃ of temperature, terminal pH4.8～5.2, in the first thickener 12 separation obtain, soak again supernatant liquor and in soak underflow, in soak supernatant liquor and leach solution of zinc sulfate.Will in soak underflow and send into hot acid reducing bath 2 and carry out hot acid leaching, add waste electrolyte, make to take the indissoluble zinc that zinc ferrite is main existence form further to leach under high temperature peracid, reduce leaching simultaneously, add excessive zinc sulfide concentrates to make Fe3+ in solution be reduced into Fe2+, control 85～95 ℃ of temperature, eventually sour 45～55g/l, after the second thickener 21 separation, obtain reduction and leach supernatant liquor and underflow slag, wherein underflow slag send flotation machine 3 to obtain sulphur concentrate and tailings, sulphur concentrate obtains calcining through roasting together with zinc ore concentrate, calcining leaches for neutral, mine tailing obtains zinc oxide and waste residue through fuming furnace 31, wherein zinc oxide adds pre-neutralization groove 22, above-mentioned reduction is leached in supernatant liquor and carried out pre-neutralization, add again zinc dust precipitation to obtain indium precipitation, wherein 50～60 ℃ of temperature are controlled in pre-neutralization, terminal pH1.2～1.8, during zinc dust precipitation indium, control 55～65 ℃ of temperature, terminal pH3.5～4.5, after pressure filter 23 separation, obtain liquid and indium slag after heavy indium, indium slag send indium recovery system to reclaim.After heavy indium, liquid enters reactor 4, pass into the oxygen of concentration 98%, control 170～185 ℃ of temperature, pressure 1100～1300kPa, enters in slag the iron precipitation in liquid after heavy indium, after flash drum 41 decrease temperature and pressure, again through separated dense supernatant liquor and the thickened underflow of obtaining of the 3rd thickener 42, carry out neutrality again and leach, thickened underflow, through press filtration, washing, obtains scum.In above-mentioned, soak supernatant liquor through purification, electrodeposition, founding, obtain zinc ingot metal, the waste electrolyte that wherein electrodeposition produces leaches for hot acid.
Claims (3)
1. the zinc hydrometallurgy deironing apparatus in producing, comprise the fluidizing reactor (1) for roasting zinc ore concentrate, it is characterized in that, the delivery port of fluidizing reactor (1) is communicated with the first solid-liquid separating equipment input aperture through neutral leaching vat (11), described the first solid-liquid separating equipment bottom delivery port is communicated with the second solid-liquid separating equipment input aperture through hot acid reducing bath (2), described the second solid-liquid separating equipment bottom delivery port is communicated with flotation machine (3) input aperture, the first delivery port of described flotation machine (3) is communicated with the zinc ore concentrate input aperture of described fluidizing reactor (1), the second delivery port of described flotation machine (3) is communicated with fuming furnace (31) input aperture, described the second solid-liquid separating equipment side delivery port is communicated with pressure filter (23) input aperture through pre-neutralization groove (22), the first delivery port of described pressure filter (23) is communicated with reactor (4) input aperture, and described reactor (4) delivery port is communicated with the 3rd solid-liquid separating equipment input aperture by flash drum (41), a delivery port of described the 3rd solid-liquid separating equipment is communicated with described neutral leaching vat (11), a delivery port of described fuming furnace (31) is communicated with described pre-neutralization groove (22) inlet end.
2. the deironing apparatus in zinc hydrometallurgy production according to claim 1, is characterized in that, described the first solid-liquid separating equipment, the second solid-liquid separating equipment, the 3rd solid-liquid separating equipment are thickener.
3. the deironing apparatus in zinc hydrometallurgy production according to claim 1 and 2, is characterized in that, the second delivery port of described pressure filter (23) is communicated with indium recovery system.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201320525041.3U CN203403143U (en) | 2013-08-27 | 2013-08-27 | Deironing device used in zinc hydrometallurgy production |
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| Application Number | Priority Date | Filing Date | Title |
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| CN201320525041.3U CN203403143U (en) | 2013-08-27 | 2013-08-27 | Deironing device used in zinc hydrometallurgy production |
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| CN201320525041.3U Expired - Lifetime CN203403143U (en) | 2013-08-27 | 2013-08-27 | Deironing device used in zinc hydrometallurgy production |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104120252A (en) * | 2014-07-25 | 2014-10-29 | 长沙有色冶金设计研究院有限公司 | Ore pulp cooling method and device for pressurized oxygen leaching of zinc sulfide concentrate |
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2013
- 2013-08-27 CN CN201320525041.3U patent/CN203403143U/en not_active Expired - Lifetime
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104120252A (en) * | 2014-07-25 | 2014-10-29 | 长沙有色冶金设计研究院有限公司 | Ore pulp cooling method and device for pressurized oxygen leaching of zinc sulfide concentrate |
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Granted publication date: 20140122 |
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