CN203530398U - Laterite-nickel ore jointly leaches system - Google Patents
Laterite-nickel ore jointly leaches system Download PDFInfo
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- CN203530398U CN203530398U CN201320621020.1U CN201320621020U CN203530398U CN 203530398 U CN203530398 U CN 203530398U CN 201320621020 U CN201320621020 U CN 201320621020U CN 203530398 U CN203530398 U CN 203530398U
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- PXHVJJICTQNCMI-UHFFFAOYSA-N nickel Substances [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 title claims abstract description 216
- 229910052759 nickel Inorganic materials 0.000 title claims abstract description 113
- 238000002386 leaching Methods 0.000 claims abstract description 141
- CWYNVVGOOAEACU-UHFFFAOYSA-N Fe2+ Chemical compound [Fe+2] CWYNVVGOOAEACU-UHFFFAOYSA-N 0.000 claims abstract description 24
- WYTGDNHDOZPMIW-RCBQFDQVSA-N alstonine Natural products C1=CC2=C3C=CC=CC3=NC2=C2N1C[C@H]1[C@H](C)OC=C(C(=O)OC)[C@H]1C2 WYTGDNHDOZPMIW-RCBQFDQVSA-N 0.000 claims abstract description 22
- 239000007788 liquid Substances 0.000 claims abstract description 22
- 230000003472 neutralizing effect Effects 0.000 claims abstract description 21
- QXZUUHYBWMWJHK-UHFFFAOYSA-N [Co].[Ni] Chemical compound [Co].[Ni] QXZUUHYBWMWJHK-UHFFFAOYSA-N 0.000 claims abstract description 20
- 238000001556 precipitation Methods 0.000 claims abstract description 18
- 239000002562 thickening agent Substances 0.000 claims abstract description 14
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 12
- 239000006228 supernatant Substances 0.000 claims abstract description 8
- 238000009423 ventilation Methods 0.000 claims abstract description 4
- ZGDWHDKHJKZZIQ-UHFFFAOYSA-N cobalt nickel Chemical compound [Co].[Ni].[Ni].[Ni] ZGDWHDKHJKZZIQ-UHFFFAOYSA-N 0.000 claims abstract 5
- 239000002689 soil Substances 0.000 claims description 64
- 239000000126 substance Substances 0.000 claims description 12
- 238000005496 tempering Methods 0.000 claims description 12
- 238000005406 washing Methods 0.000 claims description 12
- 239000003795 chemical substances by application Substances 0.000 claims description 9
- 230000004888 barrier function Effects 0.000 claims description 3
- 239000000945 filler Substances 0.000 claims description 3
- 239000006260 foam Substances 0.000 claims description 3
- 239000002245 particle Substances 0.000 claims description 3
- 238000007873 sieving Methods 0.000 claims description 3
- 238000011144 upstream manufacturing Methods 0.000 claims description 3
- 238000000034 method Methods 0.000 abstract description 50
- 239000002253 acid Substances 0.000 abstract description 22
- QAOWNCQODCNURD-UHFFFAOYSA-N sulfuric acid Substances OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 abstract description 17
- 238000011084 recovery Methods 0.000 abstract description 12
- 238000004519 manufacturing process Methods 0.000 abstract description 9
- 238000002156 mixing Methods 0.000 abstract description 8
- 238000005265 energy consumption Methods 0.000 abstract description 6
- 239000002994 raw material Substances 0.000 abstract description 5
- 239000002002 slurry Substances 0.000 abstract description 4
- 230000007704 transition Effects 0.000 abstract 2
- 239000012141 concentrate Substances 0.000 abstract 1
- 238000003672 processing method Methods 0.000 abstract 1
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 38
- 238000000605 extraction Methods 0.000 description 17
- 229910017052 cobalt Inorganic materials 0.000 description 15
- 239000010941 cobalt Substances 0.000 description 15
- GUTLYIVDDKVIGB-UHFFFAOYSA-N cobalt atom Chemical compound [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 description 15
- 238000005516 engineering process Methods 0.000 description 15
- 238000006243 chemical reaction Methods 0.000 description 13
- 239000000284 extract Substances 0.000 description 13
- 229910052742 iron Inorganic materials 0.000 description 13
- 238000000227 grinding Methods 0.000 description 12
- 239000012535 impurity Substances 0.000 description 12
- 238000013019 agitation Methods 0.000 description 11
- 238000006386 neutralization reaction Methods 0.000 description 11
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 9
- 238000010438 heat treatment Methods 0.000 description 9
- 229910052739 hydrogen Inorganic materials 0.000 description 9
- CPLXHLVBOLITMK-UHFFFAOYSA-N Magnesium oxide Chemical compound [Mg]=O CPLXHLVBOLITMK-UHFFFAOYSA-N 0.000 description 7
- NVIVJPRCKQTWLY-UHFFFAOYSA-N cobalt nickel Chemical compound [Co][Ni][Co] NVIVJPRCKQTWLY-UHFFFAOYSA-N 0.000 description 7
- 229910052751 metal Inorganic materials 0.000 description 6
- 239000002184 metal Substances 0.000 description 6
- 239000000203 mixture Substances 0.000 description 6
- 239000011504 laterite Substances 0.000 description 5
- 229910001710 laterite Inorganic materials 0.000 description 5
- 150000001875 compounds Chemical class 0.000 description 4
- 239000000395 magnesium oxide Substances 0.000 description 4
- 241000080590 Niso Species 0.000 description 3
- 230000002411 adverse Effects 0.000 description 3
- 229910052782 aluminium Inorganic materials 0.000 description 3
- 229910021529 ammonia Inorganic materials 0.000 description 3
- 230000007613 environmental effect Effects 0.000 description 3
- 239000007789 gas Substances 0.000 description 3
- 239000011777 magnesium Substances 0.000 description 3
- 229910052748 manganese Inorganic materials 0.000 description 3
- 230000035484 reaction time Effects 0.000 description 3
- 230000000630 rising effect Effects 0.000 description 3
- 238000003756 stirring Methods 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 2
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 description 2
- 235000019738 Limestone Nutrition 0.000 description 2
- 238000003723 Smelting Methods 0.000 description 2
- 229910000831 Steel Inorganic materials 0.000 description 2
- 235000011941 Tilia x europaea Nutrition 0.000 description 2
- 229910052791 calcium Inorganic materials 0.000 description 2
- 229910052804 chromium Inorganic materials 0.000 description 2
- 238000005352 clarification Methods 0.000 description 2
- 229910052802 copper Inorganic materials 0.000 description 2
- 230000007423 decrease Effects 0.000 description 2
- 230000003247 decreasing effect Effects 0.000 description 2
- 230000003301 hydrolyzing effect Effects 0.000 description 2
- 239000000543 intermediate Substances 0.000 description 2
- 239000004571 lime Substances 0.000 description 2
- 239000006028 limestone Substances 0.000 description 2
- 229910052749 magnesium Inorganic materials 0.000 description 2
- 239000002244 precipitate Substances 0.000 description 2
- 238000012216 screening Methods 0.000 description 2
- 239000002893 slag Substances 0.000 description 2
- 239000010959 steel Substances 0.000 description 2
- 229910052725 zinc Inorganic materials 0.000 description 2
- -1 Al<0.1g/L Substances 0.000 description 1
- 229910000863 Ferronickel Inorganic materials 0.000 description 1
- 229910018661 Ni(OH) Inorganic materials 0.000 description 1
- 229910000805 Pig iron Inorganic materials 0.000 description 1
- 238000007792 addition Methods 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 230000008021 deposition Effects 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 150000002500 ions Chemical class 0.000 description 1
- AXZKOIWUVFPNLO-UHFFFAOYSA-N magnesium;oxygen(2-) Chemical compound [O-2].[Mg+2] AXZKOIWUVFPNLO-UHFFFAOYSA-N 0.000 description 1
- 238000002844 melting Methods 0.000 description 1
- 230000008018 melting Effects 0.000 description 1
- 150000001455 metallic ions Chemical class 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 230000001698 pyrogenic effect Effects 0.000 description 1
- 238000002791 soaking Methods 0.000 description 1
- WWNBZGLDODTKEM-UHFFFAOYSA-N sulfanylidenenickel Chemical compound [Ni]=S WWNBZGLDODTKEM-UHFFFAOYSA-N 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
Images
Classifications
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P10/00—Technologies related to metal processing
- Y02P10/20—Recycling
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- Manufacture And Refinement Of Metals (AREA)
Abstract
A system for jointly leaching laterite-nickel ore is characterized in that a limonite type laterite-nickel ore primary atmospheric pressure leaching tank and a serpentine ore pulp transition tank are communicated with a mixing tank in parallel, and the mixing tank, a secondary pressurized leaching tank and a leached ore pulp neutralizing tank are communicated in sequence; the first-stage normal-pressure leaching tank is provided with a limonite type laterite-nickel ore feed inlet and a concentrated sulfuric acid inlet; the serpentine slurry transition groove is provided with a serpentine slurry feeding port and a water filling port; the two-stage pressure leaching tank is communicated with a ventilation source; the ore pulp neutralizing tank is communicated with a tailing pond through an underflow thickener; the ore pulp neutralizing tank is also communicated with the cobalt-nickel settling tank through a supernatant liquid pool; the cobalt-nickel precipitation tank is communicated with the tail liquid treatment device through a tail liquid thickener and is communicated with the nickel-cobalt concentrate container through a filter press. The utility model discloses do not have special requirement to ore type and grade, raw materials adaptability is wide, reduces investment, energy consumption and manufacturing cost, and the flow is simple, and the full flow Ni, Co rate of recovery are >90% respectively, >88%, are higher than the processing method in the current non-high pressure acid leaching technique.
Description
Technical field
The utility model relates to the system that a kind of red soil nickel ore is combined leaching, from red soil nickel ore, extracts the system of nickel cobalt, and particularly a kind of nickel laterite extracts the system of nickel cobalt enriched substance intermediates.
Technical background
The development of global economy makes the demand steady-state growth of nickel, and along with the exhaustion day by day of nickel sulfide ore resource, the red soil nickel ore that accounts for global 70% nickel resources has become main nickel source.
Red soil nickel ore is the oxidized ore that richness is deposited nickel, and its nickel reserves take up an area approximately 70% of continental rise nickel total stocks on ball.At present, Proress Technolgies of Laterite-nickel Ore is mainly divided into thermal process and wet processing both at home and abroad.Thermal process mainly comprises four kinds: (1) RKEF technique melting ferronickel; (2) blast furnace smelting nickel-contained pig iron; (3) blast furnace smelting ice nickel; (4) rotary kiln reduction-ore-dressing technique.Thermal process is because energy consumption is higher, be only suitable for processing the laterite that nickel content is higher (nickeliferous be more than or equal to 1.5%), and the valuable metal cobalt of association can not reclaim.Wet processing mainly comprises three kinds: (1) reducing roasting-ammonia soaks; (2) high pressure acidleach; (3) normal pressure acidleach.
Ammonia soaks and is applicable to the ore that content of magnesia is high, and whole flow process nickel recovery is 70%～80%, and the cobalt rate of recovery is 40%～50%.The ore that iron content is high, magnesium oxide is low adopts the method for high pressure acidleach, the rate of recovery 90%～92% of this method nickel, the rate of recovery 88%～90% of cobalt.Reducing roasting-ammonia soaking technology is because energy consumption is high, and it is not enough that the low and environmental protection pressure of the rate of recovery is larger etc., has been eliminated gradually in the world, in newly-built nickel laterite project, seldom uses this technique.
In recent years, the hydrometallurgical technology development of whole world nickel laterite rapidly, high pressure acid leaching process particularly, this technique has nickel cobalt leaching yield high (nickel cobalt leaching yield is up to more than 97% and 95%), after leaching, liquid foreign matter content is low, subsequent disposal operation is relatively simple, can obtain the high-quality advantages such as nickel cobalt enriched substance, has become the topmost treatment process of nickel laterite in recent years.
But there is the deficiencies such as equipment requirements is high, production and operation cost is higher, project investment is large in high pressure acid leaching process.
Utility model content
The purpose of this utility model is to provide the system that a kind of red soil nickel ore is combined leaching, and its ore wide adaptability, production cost is low, system flow is simple, reclaim high rate, can from red soil nickel ore, extract to environmental friendliness nickel cobalt.
Another one object of the present utility model is to provide the system that a kind of red soil nickel ore is combined leaching, and its applicable grade wide ranges, flow process are simple, energy consumption and cost is low, the rate of recovery is high.
For this reason, the utility model provides a kind of red soil nickel ore to combine the system of leaching, it is characterized in that, one section of normal pressure leaching vat of limonite type red soil nickel ore and serpentine ore pulp ramp pan are communicated with tempering tank in parallel, this tempering tank, two sections of pressure leaching grooves and leach after ore pulp neutralizing well be communicated with successively; One section of normal pressure leaching vat is provided with limonite type red soil nickel ore opening for feed and vitriol oil entrance; Serpentine ore pulp ramp pan is provided with serpentine ore pulp opening for feed and filler; Two sections of pressure leaching grooves are communicated with ventilation source; Ore pulp neutralizing well is communicated with Tailings Dam by underflow thickener; Ore pulp neutralizing well is also communicated with cobalt nickel settling bath by supernatant liquid pool; Cobalt nickel settling bath is communicated with tail washings treatment unit by tail washings thickener, and is communicated with nickel cobalt enriched substance container by pressure filter.
Preferably, in the upstream of one section of normal pressure leaching vat of limonite type red soil nickel ore, be provided with crusher, ball mill, grain sieving machine, particle thickener and/or limonite type red soil nickel ore ramp pan.
Preferably, between one section of normal pressure leaching vat of limonite type red soil nickel ore and tempering tank, be provided with one section of ore pulp ramp pan.
Preferably, between tempering tank and two sections of pressure leaching grooves, be provided with barrier film force (forcing) pump.
Preferably, at two sections of pressure leaching grooves with after leaching, between ore pulp neutralizing well, be provided with flash drum, foam removal groove and two sections of leaching ore pulp storage tanks.
Preferably, leach rear ore pulp neutralizing well and be provided with neutralizing agent entrance and two sections of leaching ore pulp opening for feeds.
Preferably, underflow thickener is provided with solidifying wadding agent entrance and wash water entrance.
Preferably, cobalt nickel settling bath is provided with supernatant liquor entrance and precipitation agent entrance.
The utility model is realized by following technical proposal: red soil nickel ore is through the method process for producing nickel cobalt enriched substance of " after normal pressure leaching-pressure leaching-leaching in ore pulp and removal of impurities-nickel cobalt precipitation ".Comprise the following steps:
(1) normal pressure leaches: limonite type red soil nickel ore after broken ore grinding or fine fraction mixed type red soil nickel ore add the vitriol oil to carry out normal pressure to stir self-heating and leach;
(2) pressure leaching: serpentine type red soil nickel ore or coarse fraction mixed type red soil nickel ore are sent into autoclave after mixing with ore pulp after the leaching of first paragraph normal pressure after broken ore grinding and carried out two sections of pressure leachings;
(3) leach in rear ore pulp and removal of impurities: after pressure leaching, ore pulp adds Wingdale, passes into SO simultaneously
2with air gas mixture or add hydrogen peroxide carry out in and removal of impurities;
(4) cobalt nickel precipitation: after neutralization, ore pulp carries out after the dense washing of CCD adverse current, and after washing, liquid adds NaOH neutralization precipitation to obtain nickel cobalt enriched substance.
In step (1), limonite type red soil nickel ore directly adds sulfuric acid to carry out normal pressure agitation leach after broken ore grinding, or the broken classification of mixed type red soil nickel ore process, and fine fraction ore adds sulfuric acid to carry out normal pressure agitation leach.According to the difference of feedstock property, can be used for processing limonite type red soil nickel ore and serpentine type red soil nickel ore, also can process mixed type red soil nickel ore, extensive to adaptability to raw material.Vitriol oil consumption 0.5～1.5t/t ore deposit is controlled in normal pressure agitation leach, leaching cycle 1～8h, 70～120 ℃ of extraction temperatures, initial pulp density 20～50%.Ni leaching yield >97% with this understanding, Co leaching yield >95%; In normal pressure agitation leach process, valuable metal Ni, the oxide compound of Co and sulfuric acid generation neutralization reaction enter solution, simultaneously, other impurity element enters solution as neutralization reaction occurs the oxide compound of Fe, Mg, Al, Ni, Co, Mn, Zn, Cu, Ca, Cr etc. also part, and main chemical reactions equation is as follows:
NiO+H
2SO
4=NiSO
4+H
2O (1)
CoO+H
2SO
4=CoSO
4+H
2O (2)
2FeOOH+3H
2SO
4=Fe
2(SO
4)
3+4H
2O (3)
FeO+H
2SO
4=FeSO
4+H
2O (4)
Al
2O
3+3H
2SO
4=Al
2(SO
4)
3+3H
2O (5)
MgO+H
2SO
4=MgSO
4+H
2O (6)
MnO+H
2SO
4=MnSO
4+H
2O (7)
ZnO+H
2SO
4=ZnSO
4+H
2O (8)
CuO+H
2SO
4=CuSO
4+H
2O (9)
Cr
2O
3+3H
2SO
4=Cr
2(SO
4)
3+3H
2O (10)
In step (2), after serpentine type red soil nickel ore or mixed type red soil nickel ore coarse fraction ore leach with normal pressure after broken ore grinding, ore pulp adds in autoclave after mixing, after utilizing first paragraph normal pressure to leach, in ore pulp, in remaining sulfuric acid and autoclave pressure, iron precipitates the leaching that serpentine or mixed type red soil nickel ore coarse fraction ore are carried out in newly-generated acid, the object that simultaneously reaches red soil nickel ore leaching and neutralized ex iron, reduces sulfuric acid consumption to greatest extent; According to the difference of feedstock property, the ore that pressure leaching Duan Xin adds can serpentine type red soil nickel ore, can be also coarsely graded mixed type red soil nickel ore.Pressure leaching controls two sections of pressure leaching ore deposit additions and one section of normal pressure leaching ore deposit usage ratio is 1:0.25～1:4, leaching cycle 1～8h, and 120～180 ℃ of extraction temperatures, leach pressure 3～8atm, newly add the initial pulp density 20～50% of ore.Ni leaching yield >93% with this understanding, Co leaching yield >90%, Fe concentration <4g/L in solution.In pressure leaching process, after one section of leaching, ore pulp Fe3+ hydrolytic precipitation enters in slag, two sections add valuable metal Ni in ore deposit, the oxide compound of Co and sulfuric acid generation neutralization reaction enter solution, other impurity element enters solution as neutralization reaction occurs the oxide compound of Mg, Al, Ni, Co, Mn, Zn, Cu, Ca, Cr etc. also part simultaneously, and main chemical reactions equation is as follows:
NiO+H
2SO
4=NiSO
4+H
2O (11)
CoO+H
2SO
4=CoSO
4+H
2O (12)
Fe
2(SO
4)
3+4H
2O=2FeOOH↓+3H
2SO
4 (13)
Fe
2(SO
4)
3+3H
2O=Fe
2O
3↓+3H
2SO
4 (14)
Al
2O
3+3H
2SO
4=Al
2(SO
4)
3+3H
2O (15)
MgO+H
2SO
4=MgSO
4+H
2O (16)
MnO+H
2SO
4=MnSO
4+H
2O (17)
ZnO+H
2SO
4=ZnSO
4+H
2O (18)
CuO+H
2SO
4=CuSO
4+H
2O (19)
Cr
2O
3+3H
2SO
4=Cr
2(SO
4)
3+3H
2O (20)
In step (3), after pressure leaching, ore pulp adds limestone slurry, and passes into SO
2with air gas mixture or H
2o
2in carrying out and removal of impurities.By in oxidation and removal of impurities, iron concentration <0.1g/L in ore pulp after neutralization.In pressure leaching ore pulp, with removal of impurities reaction conditions be: 50～100 ℃ of temperature of reaction, reaction times 0.5～6h, controls solution terminal pH2～5, liquid Fe<0.1g/L after removal of impurities, Ni, Co rate of loss <2%, main chemical reactions equation is as follows:
CaCO
3+H
2SO
4=CaSO
4↓+H
2O+CO
2↑ (21)
Along with reaction is carried out rising with pH value, part Fe, Al, the reaction of Cr ion generation hydrolytic precipitation.Main chemical reactions equation is as follows:
Fe
2(SO
4)
3+3H
2O=Fe
2O
3↓+3H
2SO
4 (22)
Al
2(SO
4)
3+6H
2O=2Al
2O
3↓+3H
2SO
4 (23)
Cr
2(SO
4)
3+3H
2O=Cr
2O
3↓+3H
2SO
4 (24)
In step (3), in and after removal of impurities ore pulp enter the dense washing of CCD adverse current, Ni, Co rate of recovery >98%, after washing, supernatant liquor adopts NaOH neutralization precipitation to obtain nickel cobalt enriched substance, Ni, Co rate of recovery >99.5%.Main chemical reactions equation is as follows:
(1+a)NiSO
4+2NaOH=Na
2SO
4+Ni(OH)
2·aNiSO
4↓ (25)
(1+b)CoSO
4+2NaOH=Na
2SO
4+Co(OH)
2·bCoSO
4↓ (26)
After nickel cobalt precipitation, the dense washing underflow of solution and CCD adverse current carries out neutralization precipitation with lime white after mixing, and makes the precipitations such as Mg and a small amount of residual Fe in solution, Mn, Ni, Co, then sends into Tailings Dam clarification, and after clarification, liquid returns to main production system and recycles.
The utility model method is compared with wet method system with pyrogenic process system of the prior art, can process limonite type red soil nickel ore and serpentine type red soil nickel ore according to the difference of feedstock property simultaneously, also can process mixed type red soil nickel ore.
Therefore, the utility model to ore type and grade without particular requirement, adaptability to raw material is wide, the utility model method leaches phase specific energy with traditional normal pressure and greatly improves valuable metal leaching yield, reduces sulfuric acid consumption and leach foreign matter content in rear ore pulp, leach with conventional press temperature of reaction and the pressure that phase specific energy greatly reduces pressure leaching section, reduce investment, energy consumption and production cost.
In addition, after the neutralization of the utility model method, slag can be afforested and reclaim on the spot, has greatly reduced the discharge of tailings, waste gas and waste water, environmental friendliness.
Whole process Ni of the present utility model, the Co rate of recovery be >90%, >88% respectively, and metal recovery rate is high.
Accompanying drawing explanation
Fig. 1 is according to the overview flow chart of red soil nickel ore associating leaching system of the present utility model;
Fig. 2 is according to the structure principle chart of red soil nickel ore associating leaching system of the present utility model.
Embodiment
Below in conjunction with embodiment, the utility model is described further.
As shown in Figure 1-2, according to a kind of red soil nickel ore associating leaching system of the present utility model, one section of normal pressure leaching vat 10 of limonite type red soil nickel ore and serpentine ore pulp ramp pan 20 are communicated with tempering tank 30 in parallel, this tempering tank 30, two sections of pressure leaching grooves 40 and leach after ore pulp neutralizing well 50 be communicated with successively; One section of normal pressure leaching vat 10 is provided with limonite type red soil nickel ore opening for feed 11 and vitriol oil entrance 12; Serpentine ore pulp ramp pan 20 is provided with serpentine ore pulp opening for feed 21 and filler 22; Two sections of pressure leaching grooves 40 are communicated with ventilation source 41; Ore pulp neutralizing well 50 is communicated with Tailings Dam 60 by underflow thickener 55; Ore pulp neutralizing well 50 is also communicated with cobalt nickel settling bath 80 by supernatant liquid pool 70; Cobalt nickel settling bath 80 is communicated with tail washings treatment unit 100 by tail washings thickener 90, and is communicated with nickel cobalt enriched substance container 99 by pressure filter 91.
In the upstream of one section of normal pressure leaching vat 10 of limonite type red soil nickel ore, be provided with in crusher, ball mill, grain sieving machine, particle thickener and limonite type red soil nickel ore ramp pan one, several or whole (seeing Reference numeral 13).
Between one section of normal pressure leaching vat 10 of limonite type red soil nickel ore and tempering tank 30, be provided with one section of ore pulp ramp pan 14.
Between tempering tank 30 and two sections of pressure leaching grooves 40, be provided with barrier film force (forcing) pump 35.
At two sections of pressure leaching grooves 40 with after leaching, between ore pulp neutralizing well 50, be provided with flash drum, foam removal groove and two sections of leaching ore pulp storage tanks (seeing Reference numeral 45).
After leaching, ore pulp neutralizing well 50 is provided with neutralizing agent entrance 51 and two sections of leaching ore pulp opening for feeds 52.
Cobalt nickel settling bath 80 is provided with supernatant liquor entrance 81 and precipitation agent entrance 82.
embodiment 1
Get 200g (dry meter) limonite type red soil nickel ore (Ni1.17%, Co0.10%, Fe43.05%, MgO1.43%), add water furnishing pulp density 33%, adopt 98%H
2sO
4solution carries out self-heating agitation leach under normal pressure, and 95 ℃ of extraction temperatures leach through 6h, and nickel, cobalt leaching yield reach respectively 98.11% and 96.48%, altogether consume sour 224.48g, close 1.1t acid/t ore deposit.
Get 200g (dry meter) serpentine type red soil nickel ore (Ni1.54%, Co0.02%, Fe5.53%, MgO32.0%), furnishing pulp density is 33%, sends in autoclave, carry out two sections of pressure leachings with ore pulp after normal pressure leaches after mixing, at 150 ℃ of extraction temperatures, leach 2h, leach pressure 0.45MPa, nickel, the total leaching yield of cobalt reach respectively 93.61% and 91.39%, total acid consumption 550kg/t ore deposit.Liquid Fe content 4.01g/L after leaching.
Contrast with traditional technology:
(1) one section of normal pressure extract technology
Get 400g mixed type red soil nickel ore (Ni1.36%, Co0.06%, Fe24.29%, MgO16.72%), add water furnishing pulp density 33%, adopt 98%H
2sO
4solution carries out self-heating agitation leach under normal pressure, and 95 ℃ of extraction temperatures leach through 6h, and it is 83.11% and 80.79% that nickel, cobalt leaching yield reach respectively, consumes sour 220g, closes 550kg acid/t ore deposit.Liquid Fe content 113.55g/L after leaching.
Compare traditional normal pressure extract technology, under identical acid consumption condition, associating leaching novel technique improves respectively 10.50% and 10.60% than tradition one section of normal pressure extract technology nickel, cobalt leaching yield, liquid concentration of iron decline 109.54g/L after simultaneously leaching, and novel process has alleviated follow-up deferrization process burden greatly.
(2) one sections of pressure leaching process
Get 400g mixed type red soil nickel ore (Ni1.36%, Co0.06%, Fe24.29%, MgO16.72%), add water furnishing pulp density 33%, add water furnishing pulp density 33%, adopt 98%H
2sO
4solution carries out pressure leaching in autoclave, and 250 ℃ of extraction temperatures leach pressure 4.5MPa, through 1h, leach, and it is 97.35% and 96.01% that nickel, cobalt leaching yield reach respectively, consumes sour 210g, closes 525kg acid/t ore deposit.Liquid Fe content 1.55g/L after leaching.
Compare conventional press extract technology, under slightly high acid consumption condition, associating leaching novel technique reduces respectively 3.74% and 4.62% than tradition one section of normal pressure extract technology nickel, cobalt leaching yield, liquid concentration of iron rising 2.46g/L after simultaneously leaching, but extraction temperature has reduced by 100 ℃, leach pressure decreased 4.05MPa novel process and take less nickel cobalt leaching yield as cost greatly reduces extraction temperature and pressure, reduced production and operation cost and reduced facility investment.
embodiment 2
Get 800g mixed type red soil nickel ore (Ni1.52%, Fe16.32%, MgO23.49%, Si16.09%), by 1mm, sieve the lower ore deposit (Ni1.54% of obtain-1mm sieve, Fe18.68%, MgO21.05%, Si15.19%) 512g, ore deposit (Ni1.47% on+1mm sieve, Fe11.95%, MgO28.03%, Si17.76%) 288g, add water furnishing pulp density 35%, adopt 98%H
2sO
4solution carries out self-heating agitation leach under normal pressure, and 100 ℃ of extraction temperatures leach through 5h, and nickel leaching yield reaches 98.45%, altogether consumes sour 512g, closes 1t acid/t ore deposit.
Get that on 288g+1mm sieve, to add water furnishing pulp density after the ore grinding of ore deposit be 35%, after leaching with the lower ore deposit of one section-1mm sieve normal pressure, ore pulp adds after mixing and in autoclave, carries out two sections of pressure leachings, at 160 ℃ of extraction temperatures, leach 1.5h, leach pressure 0.48MPa, the total leaching yield of nickel reaches 94.05%, total acid consumption 640kg/t ore deposit.Liquid Fe content 2.47g/L after leaching.
Contrast with traditional technology:
(1) one section of normal pressure extract technology
The mixed type red soil nickel ore 800g (Ni1.52%, Fe16.32%, MgO23.49%, Si16.09%) that gets equal in quality and composition, adds water furnishing pulp density 35% after ore grinding, adopt 98%H
2sO
4solution carries out self-heating agitation leach under normal pressure, and 100 ℃ of extraction temperatures leach through 5h, and nickel leaching yield is 81.64%, consumes sour 512g, closes 640kg acid/t ore deposit.Liquid Fe content 34.27g/L after leaching.
Compare traditional normal pressure extract technology, under identical acid consumption condition, associating leaching novel technique improves 12.41% than one section of normal pressure extract technology nickel leaching yield of tradition, liquid concentration of iron decline 31.80g/L after simultaneously leaching, and novel process has alleviated follow-up deferrization process burden greatly.
(2) one sections of pressure leaching process
The mixed type red soil nickel ore 800g (Ni1.52%, Fe16.32%, MgO23.49%, Si16.09%) that gets equal in quality and composition, adds water furnishing pulp density 35% after ore grinding, adopt 98%H
2sO
4in autoclave, carry out pressure leaching, 250 ℃ of extraction temperatures, leach pressure 4.5MPa, through 1h, leach, and nickel leaching yield reaches 98.83%, consumes sour 512g, closes 640kg acid/t ore deposit.Liquid Fe content 1.03g/L after leaching.
Compare conventional press extract technology, under identical acid consumption condition, associating leaching novel technique reduces by 4.78% than one section of normal pressure extract technology nickel leaching yield of tradition, liquid concentration of iron rising 1.44g/L after simultaneously leaching, but extraction temperature has reduced by 90 ℃, leach pressure decreased 4.02MPa, novel process is with less nickel, leaching yield is that cost greatly reduces extraction temperature and pressure, has reduced production and operation cost and has reduced facility investment.
embodiment 3
420.5kg (dry meter) limonite type red soil nickel ore (Ni1.18%, Co0.10%, Fe41.15%, MgO2.45%), through broken ore grinding, is adopted to 98%H
2sO
4solution carries out self-heating agitation leach under normal pressure, through 4h, leaches, and nickel, cobalt leaching yield reach respectively 97.55% and 95.37%, altogether consume sour 462.55kg, close 1.1t acid/t ore deposit.
Get 420.5kg (dry meter) serpentine type red soil nickel ore (Ni1.55%, Co0.07%, Fe5.43%, MgO28.95%), furnishing pulp density is 33%-35%, sends in autoclave, carry out two sections of pressure leachings with ore pulp after normal pressure leaches after mixing, and at 140～160 ℃ of extraction temperatures, 2h is soaked in normal pressure stirring, nickel, cobalt leaching yield reach respectively 94.14% and 92.58%, obtain ore pulp 1298.33kg after pressure leaching.
After pressure leaching, ore pulp adds limestone slurry, and passes into SO
2in carrying out at 90～100 ℃ with air gas mixture and removal of impurities, reaction times 3～4h, control endpoint pH 3～4, liquid Fe<0.1g/L after removal of impurities, Al<0.1g/L, Mn<0.12g/L, Ni, Co rate of loss <1.5%.
After removal of impurities ore pulp after filtration, washing, obtain containing Ni4.05g/L solution 1862.62L, add 50-100g/L NaOH solution at 40～60 ℃, to carry out nickel cobalt precipitation, reaction times 2～3h, Ni, Co deposition rate >99.5%, obtains nickel cobalt enriched substance 19.13kg (dry meter), in enriched substance, Ni, Co content are respectively 39.23%, 2.85%.
After precipitation, liquid adopts lime white neutralization, makes most precipitation by metallic ion in solution, reaches environment protection emission requirement.
embodiment 4
Mixed type red soil nickel ore 2248.7kg (dry meter) is carried out to 1mm screening, obtain-1mm fine fraction ore 1506.6 (Ni1.52%, Co0.072%, Fe20.86%, Mg11.75%) ,+1mm coarse fraction ore 741.2kg (Ni1.46%, Co0.043%, Fe9.06%, Mg18.19%) ,-1mm fine fraction ore adopts 98%H in 5 30L leach steel basin continuously
2sO
4under normal pressure, carry out self-heating leaching, leaching cycle 5h, 95～105 ℃ of extraction temperatures, initial pulp density 33%, normal pressure leaches and carries out continuously altogether 210h, co-processing ore 1506.6kg, nickel, cobalt leaching yield reach respectively 98.46% and 96.37%, altogether consume sour 1506.5kg, meter 1.0t acid/t ore deposit.
After+1mm coarse fraction ore reduction ore grinding, mix by surge pump and send into continuously in the horizontal 5 compartment autoclaves of 68L and carry out two sections of leachings with ore pulp after normal pressure leaching, 150 ℃ of temperature of reaction, pressure 4.5atm, leaching cycle 2h, pressure leaching carries out 210h altogether continuously, co-processing coarse fraction ore 741.2kg, nickel, the total leaching yield of cobalt reach respectively 94.33% and 92.17%.
embodiment 5
Mixed type red soil nickel ore 1135.9kg (dry meter) is carried out to 1mm screening, obtain-1mm fine fraction ore 728.1 (Ni1.30%, Co0.062%, Fe21.92%, Mg12.75%) ,+1mm coarse fraction ore 408.1kg (Ni1.27%, Co0.047%, Fe10.26%, Mg19.01%) ,-1mm fine fraction ore adopts 98%H in 5 30L leach steel basin continuously
2sO
4under normal pressure, carry out self-heating leaching, leaching cycle 4h, 90～110 ℃ of extraction temperatures, initial pulp density 33%, normal pressure leaches and carries out continuously altogether 90h, co-processing ore 728.1kg, nickel, cobalt leaching yield reach respectively 98.59% and 96.05%, altogether consume sour 728.3kg, meter 1.0t acid/t ore deposit.
After+1mm coarse fraction ore reduction ore grinding, sending into continuously horizontal 5 compartments of 68L with ore pulp after normal pressure leaches by surge pump mixes to send into and in autoclave, carries out two sections of leachings, 150 ℃ of temperature of reaction, pressure 4.5atm, leaching cycle 90min, pressure leaching carries out 90h altogether continuously, and co-processing coarse fraction ore 408.1kg nickel, the total leaching yield of cobalt reach respectively 94.19% and 92.25%.
The utility model provides a kind of system of extracting nickel cobalt from red soil nickel ore, particularly the system of dissimilar nickel cobalt extracted from laterite-nickel ore enriched substance intermediates.Be characterized in, red soil nickel ore adopts " after pressure leaching-leachings of normal pressure agitation leach-low temperature in ore pulp and removal of impurities-nickel cobalt precipitate " flow process to process, and final production goes out nickel cobalt enriched substance.
Implement technique of the present utility model and thermal process of the prior art and wet processing comparison: limonite type red soil nickel ore adds the vitriol oil to carry out the leaching of one section of normal pressure stirring self-heating after broken classification, after serpentine type red soil nickel ore leaches with first paragraph after broken ore grinding, ore pulp is sent in autoclave pressure simultaneously, utilizes first paragraph normal pressure to leach the Ore Leaching serpentine that in residual acid and autoclave pressure, iron precipitation generates.
According to the difference of raw material, also can process same mixed type red soil nickel ore, be that mixed type red soil nickel ore fine fraction ore after classification adds the vitriol oil to carry out one section of normal pressure agitation leach, on sieve ore deposit after broken ore grinding, leach with first paragraph after ore pulp send in autoclave pressure simultaneously, utilize first paragraph normal pressure to leach the acid that in residual acid and autoclave pressure, iron precipitation generates and carry out the leaching of coarse fraction ore.
Therefore, the utility model to ore type and grade without particular requirement, adaptability to raw material is wide, leaching phase specific energy with traditional normal pressure greatly improves valuable metal leaching yield, reduces sulfuric acid consumption and leaches foreign matter content in rear ore pulp, leach with conventional press temperature of reaction and the pressure that phase specific energy greatly reduces pressure leaching section, reduce investment, energy consumption and production cost.
The utility model adopts the method for normal pressure-pressurization associating leaching, and flow process is simple, cost-saving.
In addition, whole process Ni of the present utility model, the Co rate of recovery be >90%, >88% respectively, higher than the treatment process in existing non-high pressure acidleach technology.
Claims (8)
1. a red soil nickel ore is combined the system of leaching, it is characterized in that, one section of normal pressure leaching vat of limonite type red soil nickel ore and serpentine ore pulp ramp pan are communicated with tempering tank in parallel, this tempering tank, two sections of pressure leaching grooves and leach after ore pulp neutralizing well be communicated with successively; One section of normal pressure leaching vat is provided with limonite type red soil nickel ore opening for feed and vitriol oil entrance; Serpentine ore pulp ramp pan is provided with serpentine ore pulp opening for feed and filler; Two sections of pressure leaching grooves are communicated with ventilation source; Ore pulp neutralizing well is communicated with Tailings Dam by underflow thickener; Ore pulp neutralizing well is also communicated with cobalt nickel settling bath by supernatant liquid pool; Cobalt nickel settling bath is communicated with tail washings treatment unit by tail washings thickener, and is communicated with nickel cobalt enriched substance container by pressure filter.
2. the system as claimed in claim 1, is characterized in that: in the upstream of one section of normal pressure leaching vat of limonite type red soil nickel ore, be provided with crusher, ball mill, grain sieving machine, particle thickener and/or limonite type red soil nickel ore ramp pan.
3. the system as claimed in claim 1, is characterized in that: between one section of normal pressure leaching vat of limonite type red soil nickel ore and tempering tank, be provided with one section of ore pulp ramp pan.
4. the system as claimed in claim 1, is characterized in that: between tempering tank and two sections of pressure leaching grooves, be provided with barrier film force (forcing) pump.
5. the system as claimed in claim 1, is characterized in that: at two sections of pressure leaching grooves with after leaching, between ore pulp neutralizing well, be provided with flash drum, foam removal groove and two sections of leaching ore pulp storage tanks.
6. the system as claimed in claim 1, is characterized in that: after leaching, ore pulp neutralizing well is provided with neutralizing agent entrance and two sections of leaching ore pulp opening for feeds.
7. the system as claimed in claim 1, is characterized in that: underflow thickener is provided with solidifying wadding agent entrance and wash water entrance.
8. the system as claimed in claim 1, is characterized in that: cobalt nickel settling bath is provided with supernatant liquor entrance and precipitation agent entrance.
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104178627A (en) * | 2014-08-21 | 2014-12-03 | 江苏申港锅炉有限公司 | High-pressure pretreatment system for gold ores |
| CN105779759A (en) * | 2016-04-10 | 2016-07-20 | 安徽众尚微波科技有限公司 | Continuous production device for microwave heating catalyzing nickel-cobalt leaching reaction |
| CN108950243A (en) * | 2018-05-22 | 2018-12-07 | 广西银亿新材料有限公司 | A kind of processing method of red soil nickel ore leaching liquid spent acid |
| CN110669934A (en) * | 2019-10-23 | 2020-01-10 | 金川集团股份有限公司 | Nickel hydroxide cobalt slag leaching device and method |
| CN110699557A (en) * | 2019-10-23 | 2020-01-17 | 金川集团股份有限公司 | Low-cost treatment device and method for nickel hydroxide cobalt slag |
| CN113564383A (en) * | 2021-09-23 | 2021-10-29 | 矿冶科技集团有限公司 | System and process for extracting nickel and cobalt from laterite-nickel ore by two-stage pressurization |
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2013
- 2013-10-09 CN CN201320621020.1U patent/CN203530398U/en not_active Expired - Lifetime
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104178627A (en) * | 2014-08-21 | 2014-12-03 | 江苏申港锅炉有限公司 | High-pressure pretreatment system for gold ores |
| CN105779759A (en) * | 2016-04-10 | 2016-07-20 | 安徽众尚微波科技有限公司 | Continuous production device for microwave heating catalyzing nickel-cobalt leaching reaction |
| CN108950243A (en) * | 2018-05-22 | 2018-12-07 | 广西银亿新材料有限公司 | A kind of processing method of red soil nickel ore leaching liquid spent acid |
| CN110669934A (en) * | 2019-10-23 | 2020-01-10 | 金川集团股份有限公司 | Nickel hydroxide cobalt slag leaching device and method |
| CN110699557A (en) * | 2019-10-23 | 2020-01-17 | 金川集团股份有限公司 | Low-cost treatment device and method for nickel hydroxide cobalt slag |
| CN110699557B (en) * | 2019-10-23 | 2023-06-27 | 金川集团股份有限公司 | Low-cost treatment device and method for cobalt nickel hydroxide slag |
| CN110669934B (en) * | 2019-10-23 | 2024-01-16 | 金川集团股份有限公司 | Nickel cobalt hydroxide slag leaching device and method |
| CN113564383A (en) * | 2021-09-23 | 2021-10-29 | 矿冶科技集团有限公司 | System and process for extracting nickel and cobalt from laterite-nickel ore by two-stage pressurization |
| CN113564383B (en) * | 2021-09-23 | 2022-02-01 | 矿冶科技集团有限公司 | System and process for extracting nickel and cobalt from laterite-nickel ore by two-stage pressurization |
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Effective date of registration: 20170712 Address after: 100160 Beijing City, South West Fourth Ring Road, Fengtai District, No. 188 headquarters base area, building eighteen, No. 23 Co-patentee after: XUZHOU BGRIMM METAL RECYCLING INSTITUTE Patentee after: BEIJING GENERAL Research Institute OF MINING AND METALLURGY Address before: 100160, Beijing, Fengtai District, Fengtai District, South Fourth Ring Road West, No. 188 headquarters base, No. twenty-three, building eighteen Patentee before: BEIJING GENERAL Research Institute OF MINING AND METALLURGY |
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