CN105013608A - Vanadium-titanium magnetite concentrate re-concentration method achieved through oxidation alkaline leaching, acid pickling, desliming and gravity and magnetism - Google Patents
Vanadium-titanium magnetite concentrate re-concentration method achieved through oxidation alkaline leaching, acid pickling, desliming and gravity and magnetism Download PDFInfo
- Publication number
- CN105013608A CN105013608A CN201510320560.XA CN201510320560A CN105013608A CN 105013608 A CN105013608 A CN 105013608A CN 201510320560 A CN201510320560 A CN 201510320560A CN 105013608 A CN105013608 A CN 105013608A
- Authority
- CN
- China
- Prior art keywords
- concentrate
- magnetic
- desliming
- content
- pickling
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Landscapes
- Manufacture And Refinement Of Metals (AREA)
Abstract
The invention relates to a vanadium-titanium magnetite concentrate re-concentration method achieved through oxidation alkaline leaching, acid pickling, desliming and gravity and magnetism. The method is characterized by including the following steps that oxidation alkaline leaching is performed on vanadium-titanium magnetite concentrate, and the vanadium-titanium magnetite concentrate is placed in an alkaline solution; oxidization agents are added; then, an alkaline leaching reaction lasts for 0.5-2 h at the temperature of 220-330 DEG C; filtration is performed, and then filter liquor and alkaline leached filter cakes A are obtained; water is added in the alkaline leached filter cakes A, and ore pulp is prepared; then, the ore pulp is placed in a H2SO4 solution, and acid pickling is performed for 5-60 min at the temperature of 50-90 DEG C; filtration is performed, and filter liquor and acid leached filter cakes B are obtained; water is added into B, and ore pulp with the mass concentration being 30-35% can be prepared; and desliming and gravity and magnetism combined re-concentration is performed, and iron concentrate with the TFe content being 64-70% and titanium concentrate with the TiO2 content being 60-82% can be obtained respectively. The method has the beneficial effects that due to introduction of O2 or H2O2 during oxidation alkaline leaching, S compounds can be oxidized, the reaction is accelerated, the reaction temperature is lowered, the reaction time is shortened, and energy consumption and equipment investment are greatly reduced.
Description
Technical field
The present invention relates to a kind of ore-dressing technique of v-ti magnetite concentrate, particularly relate to one and utilize alkali oxide leaching, pickling, desliming and heavy magnetic to select v-ti magnetite concentrate method again.
Background technology
Vanadium titano-magnetite is a kind of grandidierite of multiple metallic element, is based on the magnetic iron ore of the symbiosis of iron content, vanadium, titanium.And one of v-ti magnetite concentrate product that to be vanadium titano-magnetite obtain through ore dressing, wherein vanadium is composed with isomorph and is stored in titanomagnetite, displacement ferric ion.Titanomagnetite is oikocryst mineral (Fe
3o
4) and chadacryst ore deposit [ulvite 2FeOTiO
2, ilmenite FeOTiO
2, aluminum-spinel (Mg, Fe) (Al, Fe)
2o
4] complex that formed.Such as, Chinese Panzhihua Region Midi Concentrator v-ti magnetite green ore and the chemistry of the v-ti magnetite concentrate after selecting iron multielement analysis the results are shown in Table 1, and v-ti magnetite green ore and vanadium titano-magnetite concentrate material phase analysis result are respectively in table 2 and table 3.
Table 1 Chinese Panzhihua Region Midi Concentrator raw ore and v-ti magnetite concentrate chemistry multielement analysis result
| Element | TFe | FeO | mFe | S | Fe 2O 3 | TiO 2 | V 2O 5 |
| Raw ore | 29.53 | 21.36 | 20.20 | 0.631 | 17.70 | 10.54 | 0.27 8 |
| Concentrate | 54.01 | 32.42 | 51.16 | 0.574 | 40.97 | 12.67 | 0.61 |
| Element | SiO 2 | Al 2O 3 | CaO | MgO | Co | P | As |
| Raw ore | 22.80 | 7.65 | 6.36 | 7.23 | 0.02 | 0.015 | <0.01 |
| Concentrate | 3.21 | 3.30 | 0.98 | 2.90 | 0.02 | 0.008 | <0.010 |
Table 2 Chinese Panzhihua Region Midi Concentrator v-ti magnetite green ore titanium, iron chemical phase analysis result
Table 3 Chinese Panzhihua Region Midi Concentrator vanadium titano-magnetite concentrate titanium, iron chemical phase analysis result
Vanadium titano-magnetite aboundresources in the world, whole world reserves reach more than 40,000,000,000 tons, and reserves in China reaches 98.3 hundred million tons.In v-ti magnetite ore, iron is mainly composed and is stored in titanomagnetite, the TiO in ore
2main tax is stored in granular ilmenite and titanomagnetite.Generally, the titanium of about 57% is composed and is stored in titanomagnetite (mFeTiO
3nFe
3o
4) in, the titanium of about 40% is composed and is stored in ilmenite (FeTiO
3) in, because vanadium titano-magnetite ore composition is complicated, character is special, and thus the comprehensive utilization of this kind of ore is the international a great problem always thoroughly do not solved.This occurrence characteristics of vanadium titano-magnetite mineral determines the effective separation adopting physical upgrading method cannot realize titanium, iron from the source of ore, cause v-ti magnetite ore after physical upgrading, iron concentrate grade low (TFe<55%), the titanium in iron ore concentrate enters blast furnace slag (TiO completely at ironmaking processes
2content reaches more than 22%) form vitreum, TiO
2lose activity and cannot economic recovery, meanwhile, titanium recovery rate is low only has 18%.Therefore sort titanium iron ore by the beneficiation method of physics and greatly reduce the value that titanium and iron utilizes separately.
China is first country comprehensively extracting iron, vanadium, titanium with commercial scale from complicated vanadium titano-magnetite in the world, but due to general physical method fundamentally can not change iron, the tax of the fine and close symbiosis of titanium deposits characteristic, therefore, adopt the physical upgrading methods such as common gravity separation method, magnetic method, floatation to carry out titanium, iron is separated, efficiency is low, is difficult to select of high grade and the ilmenite concentrate that impurity is few or iron ore concentrate; Meanwhile, TiO
2organic efficiency is not high, v-ti magnetite green ore after Mineral separation, the TiO of about 54%
2enter iron ore concentrate, these TiO
2after blast furnace process, almost all enter slag phase, form TiO
2the blast furnace slag of content 20 ~ 24%; In addition, because the impurity contents such as S, Si, the Al in iron ore concentrate are also too high, above-mentioned reason not only causes that steelmaking furnace usage factor is low, energy consumption is large, titanium resource waste, and amount of slag is large, environmental pollution is serious.
CN2011100879566 discloses " a kind of beneficiation method of ilmenite ", is the magnetic separation after ore grinding, alkaline pretreatment, filtration, again ore grinding of v-ti magnetite green ore is obtained the method for ilmenite concentrate and iron ore concentrate.The method is by iron content 32.16% with containing TiO
2the v-ti magnetite green ore of 12.11%, by magnetic separation process after ore grinding, alkaline pretreatment, filtration, again ore grinding, defines iron content 59.30% iron ore concentrate and contains TiO
2the ilmenite concentrate of 20.15%.Because the method is for ilmenite raw ore, raw ore SiO
2, Al
2o
3, the gangue mineral content such as CaO, MgO is high, the process of alkali leaching preferentially will occur in SiO
2, Al
2o
3with it mineral, define the alkali leaching rear compound similar to titanium in the dipped journey of alkali, the NaOH alkali number of alkali leaching ferrotianium raw ore consumption is 469Kg/t raw ore, and cost is high; And the titanium compound formed after the leaching of ferrotianium raw ore alkali, the compound of the silicon formed after soaking with the gangue mineral alkali such as quartz, it is very difficult for wanting to realize effectively being separated in follow-up magnetic separation, and this also constrains the raising of the rear iron concentrate grade of ferrotianium raw ore alkali leaching and ilmenite concentrate grade.Meanwhile, the method adopts twice grinding process to change mineral surfaces physicochemical properties, adds complexity and the process cost of the method.In a word, by this kind of procedure complexity, and in processing procedure, quantity of alkali consumption is large, cost is high; Meanwhile, more high-grade iron ore concentrate and ilmenite concentrate cannot be obtained.
CN201310183580.8 discloses " a kind of wet-treating sefstromite concentrate prepares the method for titanium liquid ", proposes the method with salt pickling separating titanium iron.This invention is the method that wet-treating v-ti magnetite concentrate prepares titanium liquid, comprise v-ti magnetite concentrate hydrochloric acid leaching, molten salt react ion, again pickling, sulfuric acid solution, filtration etc. and obtain the processes such as titanium liquid, the method is mainly for extraction ilmenite concentrate, its complex technical process, need in hydrochloric acid leaching process to react with hydrochloric acid and iron and vanadium to dissolve in filtrate, consume a large amount of hydrochloric acid, cost is high; Meanwhile, NaOH and titanium and pasc reaction is used to consume alkali in fused salt process.In addition, owing to employing hydrochloric acid in the method leaching process, in hydrochloric acid, chlorion is large to equipment corrosion, not easily suitability for industrialized production.The method is mainly applicable to the recycling of titanium in the low poor v-ti magnetite concentrate of high vanadium low iron content.
CN201410164253.2 discloses one and " utilizes alkali leaching, pickling, desliming and heavy magnetic associating to select v-ti magnetite concentrate method again ", and v-ti magnetite concentrate is placed in soda ash solution by this invention, and alkali leaching reaction 0.5 ~ 5 hour, in H after filtration
2sO
4pickling in solution, then acidleach filter cake is carried out desliming, being added water by the sand setting that desliming operation obtains is mixed with ore pulp and carries out gravity treatment, then gravity tailings is carried out magnetic separation, and obtaining TFe content is respectively 63% ~ 69% iron ore concentrate, TiO
2content is 60% ~ 82% ilmenite concentrate.The method achieve and efficiently sort v-ti magnetite concentrate, but adopt alkali leaching due to simple in reaction, react 0.5 ~ 5 hour at 280 ~ 370 DEG C of temperature, chemical reaction temperature is higher, and the time is longer, and SiO after reaction
2and TiO
2content is up to 3%, and impurity content is higher, causes the capacity factor of a blast furnace to reduce, adds ironmaking cost; Meanwhile, the alkali number consumed in this inventive method is up to 100kg/t concentrate, and alkaline consumption is higher, and titanium resource utilization rate is not high.
Summary of the invention
In order to overcome the deficiency of above-mentioned beneficiation method, technical problem to be solved by this invention is on the basis that physics and chemistry beneficiation method effectively combines, there is provided a kind of cost low, reclaim quality and efficiency is high, technique is simple, and utilize alkali oxide leaching, pickling, desliming and the heavy magnetic of good operability select v-ti magnetite concentrate method again, achieve and titanium, iron in v-ti magnetite concentrate are efficiently separated, improve into stokehold Iron grade, reduce and enter blast furnace TiO
2, the impurity such as S, Si, Al content, improve the capacity factor of a blast furnace, reduce the discharge capacity of blast furnace slag, reduce ironmaking cost, improve TiO simultaneously
2comprehensive resource utilization rate, reduces environmental pollution.
In order to realize object of the present invention, technical scheme of the present invention is achieved in that
One of the present invention utilizes alkali oxide leaching, pickling, desliming and heavy magnetic to select v-ti magnetite concentrate method again, it is characterized in that comprising the steps:
1) alkali oxide leaching
Be 50% ~ 55%, TiO by TFe content range
2content range is 10% ~ 15%, SiO
2content is 3% ~ 6%, Al
2o
3content is 3% ~ 6%, the v-ti magnetite concentrate of S content >0.5%, be placed in the aqueous slkali that mass concentration is 5% ~ 52%, add oxidant, then at the temperature of 220 DEG C ~ 330 DEG C, alkali soaks reaction 0.5 ~ 2 hour, reactant is filtered, obtain filtrate and alkali leaching cake A, described filtrate feeds recovery and processing system;
2) pickling
Alkali leaching cake A in step 1) is added water and makes the ore pulp that solid-liquid mass ratio is 1:1 ~ 10, then be placed in the H that mass concentration is 1% ~ 10%
2sO
4in solution, under 50 ~ 90 DEG C of conditions, pickling 5 ~ 60 minutes, filters pickling reactant, and obtain filtrate and acidleach filter cake B, described filtrate feeds recovery and processing system;
3) desliming
By step 2) in acidleach filter cake B add water and be mixed with the ore pulp that mass concentration is 21% ~ 25%, carry out desliming operation with the desliming bucket of ∮ 3.0 ~ 5.0 meters, obtain sand setting C and overflow D;
4) heavy magnetic selects again
The ore pulp being made into mass concentration 36% ~ 41% that added water by sand setting C in step 3) carries out gravity treatment, obtains gravity concentrate E and gravity tailings F; The ore pulp being mixed with mass concentration 30% ~ 34% that added water by gravity tailings F again carries out magnetic separation, obtains magnetic concentrate G and magnetic tailing H;
Described gravity concentrate E and magnetic concentrate G merges into the final iron ore concentrate that TFe content range is 64% ~ 70%, and described magnetic tailing H and overflow D merges into TiO
2content range is the final ilmenite concentrate of 60% ~ 82%.
Described aqueous slkali is any one in the NaOH aqueous solution, the KOH aqueous solution or NaOH and KOH mixed aqueous solution.
Described oxidant is oxygen or H
2o
2, oxygen addition is 20 ~ 120psi, H
2o
2addition is 50 ~ 200kg/t
to ore deposit.
Described gravity treatment adopts the spiral chute of ￠ 0.6 ~ ￠ 1.2 meters to carry out gravity treatment.
Described magnetic separation adopts the drum magnetic separator of 0.12T ~ 0.15T to carry out magnetic separation.
Described magnetic separation adopts the magnetic dewater cone of 0.03T ~ 0.05T to carry out magnetic separation.
Described magnetic separation adopts the drum magnetic separator of 0.12T ~ 0.15T and 0.03T ~ 0.05T magnetic dewater cone to carry out two stages of magnetic separation respectively.
Advantage of the present invention is:
The process of alkali oxide leaching has carried out chemical reaction to elements such as Ti, S, Si, Al in v-ti magnetite concentrate, defines corresponding salt, makes the iron in v-ti magnetite concentrate change the form of iron oxide into.With v-ti magnetite concentrate unlike, SiO in ilmenite raw ore
2content >20% and Al
2o
3content >7% is far away higher than SiO in v-ti magnetite concentrate
2content <6% and Al
2o
3content <6%, in alkali leaching ilmenite raw ore process, because the process of alkali leaching preferentially will occur in SiO
2, Al
2o
3deng on mineral, alkali is made to soak v-ti magnetite concentrate more less than alkali leaching ilmenite raw ore alkali consumption, simultaneously O
2introducing make containing S compound oxidation, oxidized FeTiO
3, accelerate reaction, reduce reaction temperature, shorten the reaction time, better effects if, greatly reduce energy consumption and equipment investment.Such as, when soaking with NaOH alkali oxide, the alkali number that the present invention consumes is less than 90kg/t concentrate, than the alkali number 469kg/t that alkali leaching raw ore consumes
raw orereduce more than 5.2 times, the alkali number consumed than the alkali leaching not passing into oxygen reduces 10kg/t concentrate; O
2introducing alkali is soaked reaction temperature is minimum is down to 220 DEG C, the reaction time is less than 2 hours.
Acid cleaning process has dissolved oxysalt and the sulfide such as Ti, Si, Al after alkali leaching effectively, makes it to dissociate with iron ore concentrate.In addition because the present invention adopts sulfuric acid to carry out pickling, reaction condition is gentle, and little to equipment corrosion, cost is low, is more conducive to suitability for industrialized production.
Desliming process presses granularity and the gravity grading of mineral, and the titanium compound generated after alkali leaching is than the fine size of magnet mineral, and proportion is little, and the difference of specific gravity of titanium, iron is comparatively large, achieves effective separation of titanium, iron.
Add heavy magnetic beneficiation combined method, make iron concentrate grade bring up to 64% ~ 70% by 50% ~ 55%, in isolated iron ore concentrate, S content significantly reduces simultaneously, is down to is less than 0.10%, SiO by more than 0.50%
2content is down to less than 1%, Al by 3% ~ 6%
2o
3content is down to less than 1.8%, TiO by 3% ~ 6%
2content is down to less than 6% by more than 12%; Meanwhile, TiO can also be obtained
2content is the ilmenite concentrate of 60% ~ 82%.
Integrated use alkali oxide leaching of the present invention, pickling, desliming and the associating of heavy magnetic select v-ti magnetite concentrate again, achieve titanium in v-ti magnetite concentrate, iron is efficiently separated, reduce and enter blast furnace TiO
2, the impurity such as S, Si, Al content, improve the capacity factor of a blast furnace, reduce the discharge capacity of blast furnace slag, reduce ironmaking cost, for subsequent smelting creates better condition, improve the comprehensive utilization ratio of titanium resource simultaneously.
Accompanying drawing explanation
Fig. 1 is present invention process flow chart.
Fig. 2 is the process chart that the present invention adopts two stages of magnetic separation.
Fig. 3 is the process chart that the present invention adopts another embodiment of two stages of magnetic separation.
Detailed description of the invention
Below in conjunction with accompanying drawing, the specific embodiment of the present invention is described further:
Embodiment 1:
As shown in Figure 1.
1) alkali oxide leaching
Be 51.0%, TiO by TFe content
2content is 14.1%, SiO
2content is 4.57%, Al
2o
3content is 4.79%, the v-ti magnetite concentrate of S content 0.77%, is placed in the NaOH aqueous slkali that mass concentration is 20%, passes into the O of 22psi
2, then at the temperature of 230 DEG C, alkali soaks reaction 45 minutes, and filtered by reactant, obtain filtrate and alkali leaching cake A, NaOH consumption 53.1 kg/t is to ore deposit, and described filtrate feeds recovery and processing system, and its chemical equation is:
4mFeTiO
3+8NaOH +mO
2 2mFe
2O
3↓+4Na
2O·(TiO
2)
m↓+4H
2O m≥1
pFe
3O
4·q（FeO·TiO
2) +2rNaOH
pFe
3O
4↓+qFeO↓+ (Na
2O)
r·(TiO
2)
q↓+rH
2O
Al
2O
3+2NaOH
2NaAlO
2+ H
2O
tSiO
2+2NaOH
Na
2O·(SiO
2)
t↓+ H
2O
3FeS
2+6NaOH
3FeS↓+Na
2SO
3+2Na
2S+3H
2O
4FeS
2+ 11O
2 2Fe
2O
3 + 8SO
2
4FeO+O
2 2Fe
2O
3
2SO
2+O
2+4NaOH
2Na
2SO
4+ 2H
2O
2) pickling
Alkali leaching cake A in step 1) is added water and makes the ore pulp that quality solid-to-liquid ratio is 1: 2, then be placed in the H that mass concentration is 3%
2sO
4in solution, 75 DEG C of pickling 10 minutes, filtered by pickling reactant, obtain filtrate and acidleach filter cake B, described filtrate feeds recovery and processing system, and its chemical equation is:
Na
2O·(TiO
2)
x +H
+ (H
2O)·（TiO
2)
x↓+Na
+
Na
2O·（SiO
2）
t+H
+ (H
2O)·（SiO
2)
t↓+Na
+
NaAlO
2+4H
+ Al
3++Na
++2H
2O
3) desliming
By step 2) in acidleach filter cake B add water and be mixed with the ore pulp that mass concentration is 22%, carry out desliming operation with the desliming bucket of ∮ 3.0 meters, obtain sand setting C and overflow D;
4) heavy magnetic selects again
The spiral chute that the ore pulp that is made into mass concentration 37% of being added water by sand setting C in step 3) feeds ￠ 1.2 meters carries out gravity treatment, obtains gravity concentrate E and gravity tailings F;
The drum magnetic separator that the ore pulp that is mixed with mass concentration 32% of being added water by gravity tailings F again carries out feeding 0.15T carries out magnetic separation, obtains magnetic concentrate G and magnetic tailing H;
It is the final iron ore concentrate of 64.1% that described gravity concentrate E and magnetic concentrate G merges into TFe content, wherein SiO
2content is 0.94%, Al
2o
3content is 1.27%, S content is 0.02%; Described magnetic tailing H and overflow D merges into TiO
2content is the ilmenite concentrate of 61.8%.
Embodiment 2:
As shown in Figure 1.
1) alkali oxide leaching
Be 51.6%, TiO by TFe content
2content is 13.9%, SiO
2content is 4.35%, Al
2o
3content is 4.33%, the v-ti magnetite concentrate of S content 0.57%, is placed in the NaOH aqueous slkali that mass concentration is 27%, passes into the O of 75psi
2, then at the temperature of 315 DEG C, alkali soaks reaction 1.0 hours, and filtered by reactant, obtain filtrate and alkali leaching cake A, NaOH consumption 83.4 kg/t is to ore deposit, and described filtrate feeds recovery and processing system, and its chemical equation is with embodiment 1;
2) pickling
Alkali leaching cake A in step 1) is added water and makes the ore pulp that quality solid-to-liquid ratio is 1:4, then be placed in the H that mass concentration is 5%
2sO
4in solution, 80 DEG C of pickling 60 minutes, filtered by pickling reactant, obtain filtrate and acidleach filter cake B, described filtrate feeds recovery and processing system, and its chemical equation is with embodiment 1;
3) desliming
By step 2) in filtration after concentrated ilmenite B add water and be mixed with the ore pulp that mass concentration is 21%, carry out desliming operation with the desliming bucket of ∮ 5.0 meters, obtain sand setting C and overflow D;
4) heavy magnetic selects again
The spiral chute that the ore pulp that is made into mass concentration 36% of being added water by sand setting C in step 3) feeds ￠ 0.6 meter carries out gravity treatment, obtains gravity concentrate E and gravity tailings F;
The drum magnetic separator that the ore pulp that is mixed with mass concentration 33% of being added water by gravity tailings F again carries out feeding 0.12T carries out magnetic separation, obtains magnetic concentrate G and magnetic tailing H;
Described gravity concentrate E and magnetic concentrate G merges into the final iron ore concentrate that TFe content is 69.9%, wherein SiO
2content is 0.31%, Al
2o
3content is 0.27%, S content is 0.01%; Described magnetic tailing H and overflow D merges into TiO
2content is the ilmenite concentrate of 65.2%.
Embodiment 3:
As shown in Figure 1.
1) alkali oxide leaching
Be 52.6%, TiO by TFe content
2content is 12.2%, SiO
2content is 3.35%, Al
2o
3content is 5.37%, the v-ti magnetite concentrate of S content 0.71%, is placed in the NaOH aqueous slkali that mass concentration is 33%, adds 59kg/t
to ore deposith
2o
2, then at the temperature of 255 DEG C, alkali soaks reaction 1.5 hours, and filtered by reactant, obtain filtrate and alkali leaching cake A, NaOH consumption 85.5 kg/t is to ore deposit, and described filtrate feeds recovery and processing system, and its chemical equation is:
2mFeTiO
3+4NaOH+mH
2O
2 mFe
2O
3↓+2Na
2O·(TiO
2)
m↓+(m+2)H
2O m≥1
pFe
3O
4·q（FeO·TiO
2) +2rNaOH
pFe
3O
4↓+qFeO↓+ (Na
2O)
r·(TiO
2)
q↓+rH
2O
Al
2O
3+2NaOH
2NaAlO
2+ H
2O
tSiO
2+2NaOH
Na
2O·(SiO
2)
t↓+ H
2O
3FeS
2+6NaOH
3FeS↓+Na
2SO
3+2Na
2S+3H
2O
2FeS
2+ 11H
2O
2 Fe
2O
3 +4SO
2+ 11H
2O
2FeO+H
2O
2 Fe
2O
3+ H
2O
SO
2+H
2O
2+2NaOH
Na
2SO
4+ 2H
2O
2) pickling
Alkali leaching cake A in step 1) is added water and makes the ore pulp that quality solid-to-liquid ratio is 1:3.2, then be placed in the H that mass concentration is 7.5%
2sO
4in solution, 50 DEG C of pickling 55 minutes, filtered by pickling reactant, obtain filtrate and acidleach filter cake B, described filtrate feeds recovery and processing system, and its chemical equation is with embodiment 1;
3) desliming
By step 2) in filtration after concentrated ilmenite B add water and be mixed with the ore pulp that mass concentration is 24%, carry out desliming operation with the desliming bucket of ∮ 5.0 meters, obtain sand setting C and overflow D;
4) heavy magnetic selects again
The spiral chute that the ore pulp that is made into mass concentration 41% of being added water by sand setting C in step 3) feeds ￠ 0.9 meter carries out gravity treatment, obtains gravity concentrate E and gravity tailings F;
It is that the magnetic dewater cone of 0.03T carries out magnetic separation that the ore pulp that is mixed with mass concentration 31% of being added water by gravity tailings F again feeds field intensity, obtains magnetic concentrate G and magnetic tailing H;
Described gravity concentrate E and magnetic concentrate G merges into the final iron ore concentrate that TFe content is 66.2%, wherein SiO
2content is 0.55%, Al
2o
3content is 0.91%, S content is 0.02%, and described magnetic tailing H and overflow D merges into TiO
2content is the ilmenite concentrate of 63.2%.
Embodiment 4:
As shown in Figure 1.
1) alkali oxide leaching
Be 53.7%, TiO by TFe content
2content is 11.8%, SiO
2content is 4.15%, Al
2o
3content is 4.98%, the v-ti magnetite concentrate of S content 0.69%, is placed in the NaOH aqueous slkali that mass concentration is 40%, passes into the O of 105psi
2, then at the temperature of 280 DEG C, alkali soaks reaction 2.0 hours, and filtered by reactant, obtain filtrate and alkali leaching cake A, NaOH consumption 88.6 kg/t is to ore deposit, and described filtrate feeds recovery and processing system, and its chemical equation is with embodiment 1;
2) pickling
Alkali leaching cake A in step 1) is added water and makes the ore pulp that quality solid-to-liquid ratio is 1:6, then be placed in the H that mass concentration is 6.5%
2sO
4in solution, 70 DEG C of pickling 25 minutes, filtered by pickling reactant, obtain filtrate and acidleach filter cake B, described filtrate feeds recovery and processing system, and its chemical equation is with embodiment 1;
3) desliming
By step 2) in filtration after concentrated ilmenite B add water and be mixed with the ore pulp that mass concentration is 24%, carry out desliming operation with the desliming bucket of ∮ 3.0 meters, obtain sand setting C and overflow D;
4) heavy magnetic selects again
The spiral chute that the ore pulp that is made into mass concentration 40% of being added water by sand setting C in step 3) feeds ￠ 1.2 meters carries out gravity treatment, obtains gravity concentrate E and gravity tailings F; Gravity tailings F is added water and forms the ore pulp of mass concentration 30% to feed field intensity be that the magnetic dewater cone of 0.05T carries out magnetic separation, obtain magnetic concentrate G and magnetic tailing H;
Described gravity concentrate E and magnetic concentrate G merges into the final iron ore concentrate that TFe content is 67.0%, wherein SiO
2content is 0.62%, Al
2o
3content is 0.71%, S content is 0.01%; Described magnetic tailing H and overflow D merges into TiO
2content is the ilmenite concentrate of 71.3%.
Embodiment 5:
As shown in Figure 2.
1) alkali oxide leaching
Be 54.1%, TiO by TFe content
2content is 11.2%, SiO
2content is 3.89%, Al
2o
3content is 5.05%, the v-ti magnetite concentrate of S content 0.72%, is placed in the KOH aqueous slkali that mass concentration is 25%, passes into the O of 120psi
2, then at the temperature of 220 DEG C, alkali soaks reaction 2.0 hours, and filtered by reactant, obtain filtrate and alkali leaching cake A, KOH consumption 87.8 kg/t is to ore deposit, and described filtrate feeds recovery and processing system, and its chemical equation is:
4mFeTiO
3+8KOH+mO
2 2mFe
2O
3↓+4K
2O·(TiO
2)
m↓+4H
2O m≥1
pFe
3O
4·q（FeO·TiO
2) +2rKOH
pFe
3O
4↓+qFeO↓+ (K
2O)
r·(TiO
2)
q↓+rH
2O
Al
2O
3+2KOH
2KAlO
2+ H
2O
tSiO
2+2KOH
K
2O·（SiO
2）
t↓+ H
2O
3FeS
2+6KOH
3FeS↓+K
2SO
3+2K
2S+3H
2O
4FeS
2+ 11O
2 2Fe
2O
3 + 8SO
2
4FeO+O
2 2Fe
2O
3
2SO
2+O
2+4KOH
2K
2SO
4+ 2H
2O
2) pickling
Alkali leaching cake A in step 1) is added water and makes the ore pulp that quality solid-to-liquid ratio is 1:8.3, then be placed in the H that mass concentration is 5%
2sO
4in solution, 85 DEG C of pickling 30 minutes, filtered by pickling reactant, obtain filtrate and acidleach filter cake B, described filtrate feeds recovery and processing system, and its chemical equation is:
K
2O·(TiO
2)
x +H
+ (H
2O)·（TiO
2)
x↓+ K
+
K
2O·（SiO
2）t+H+
(H
2O)·（SiO
2) t↓+ K +
KAlO
2+4H+
Al3+ +K++2H
2O
3) desliming
By step 2) in filtration after concentrated ilmenite B add water and be mixed with the ore pulp that mass concentration is 23%, carry out desliming operation with the desliming bucket of ∮ 5.0 meters, obtain sand setting C and overflow D;
4) heavy magnetic selects again
The spiral chute that the ore pulp that is made into mass concentration 41% of being added water by sand setting C in step 3) feeds ￠ 0.6 meter carries out gravity treatment, obtains gravity concentrate E and gravity tailings F; Gravity tailings F is added water and forms the ore pulp of mass concentration 33% to feed field intensity be that the drum magnetic separator of 0.12T carries out a stages of magnetic separation, obtain an a stages of magnetic separation concentrate G1 and stages of magnetic separation mine tailing H1; By concentration be again 32% a stages of magnetic separation concentrate G1 field intensity be that the magnetic dewater cone of 0.03T carries out two stages of magnetic separation, respectively two stages of magnetic separation concentrate G2 and two stages of magnetic separation mine tailing H2;
Described gravity concentrate E and magnetic concentrate G2 merges into the final iron ore concentrate that TFe content is 68.7%, wherein SiO
2content is 0.30%, Al
2o
3content is 0.34%, S content is 0.01%; Described magnetic tailing H1 and H2 merges into final mine tailing, and overflow D is TiO
2content is the final ilmenite concentrate of 81.8%.
Embodiment 6:
As shown in Figure 3.
1) alkali oxide leaching
Be 50.7%, TiO by TFe content
2content is 14.5%, SiO
2content is 4.38%, Al
2o
3content is 4.96%, the v-ti magnetite concentrate of S content 0.81%, is placed in the KOH aqueous slkali that mass concentration is 10%, adds 102kg/t
to ore deposith
2o
2, then at the temperature of 295 DEG C, alkali soaks reaction 1.0 hours, and filtered by reactant, obtain filtrate and alkali leaching cake A, KOH consumption 78.6kg/t is to ore deposit, and described filtrate feeds recovery and processing system, and its chemical equation is:
2mFeTiO
3+4KOH+mH
2O
2 mFe
2O
3↓+2K
2O·(TiO
2)
m↓+(m+2)H
2O m≥1
pFe
3O
4·q（FeO·TiO
2) +2rKOH
pFe
3O
4↓+qFeO↓+ (K
2O)
r·(TiO
2)
q↓+rH
2O
Al
2O
3+2KOH
2KAlO
2+ H
2O
tSiO
2+2KOH
K
2O·(SiO
2)
t↓+ H
2O
3FeS
2+6KOH
3FeS↓+K
2SO
3+2K
2S+3H
2O
2FeS
2+ 11H
2O
2 Fe
2O
3 +4SO
2+ 11H
2O
2FeO+H
2O
2 Fe
2O
3+ H
2O
SO
2+H
2O
2+2KOH
K
2SO
4+ 2H
2O
2) pickling
Alkali leaching cake A in step 1) is added water and makes the ore pulp that quality solid-to-liquid ratio is 1:9, then be placed in the H that mass concentration is 8%
2sO
4in solution, 60 DEG C of pickling 35 minutes, filtered by pickling reactant, obtain filtrate and acidleach filter cake B, described filtrate feeds recovery and processing system, and its chemical equation is with embodiment 5;
3) desliming
By step 2) in filtration after concentrated ilmenite B add water and be mixed with the ore pulp that mass concentration is 23%, carry out desliming operation with the desliming bucket of ∮ 3.0 meters, obtain sand setting C and overflow D;
4) heavy magnetic selects again
The spiral chute that the ore pulp that is made into mass concentration 37% of being added water by sand setting C in step 3) feeds ￠ 0.9 meter carries out gravity treatment, obtains gravity concentrate E and gravity tailings F; Being added water by gravity tailings F and forming the ore pulp field intensity of mass concentration 32% is that the magnetic dewater cone of 0.05T carries out a stages of magnetic separation, obtains an a stages of magnetic separation concentrate G1 and stages of magnetic separation mine tailing H1; By concentration be again 34% a stages of magnetic separation concentrate G1 to feed field intensity be that 0.15T drum magnetic separator carries out two stages of magnetic separation, respectively two stages of magnetic separation concentrate G2 and two stages of magnetic separation mine tailing H2;
Described gravity concentrate E and magnetic concentrate G2 merges into the final iron ore concentrate that TFe content is 65.5%, wherein SiO
2content is 0.42%, Al
2o
3content is 0.27%, S content is 0.01%; Described magnetic tailing H1 and H2 merges into final mine tailing, and overflow D is TiO
2content is the final ilmenite concentrate of 67.1%.
Embodiment 7:
As shown in Figure 3.
1) alkali oxide leaching
Be 52.1%, TiO by TFe content
2content is 13.0%, SiO
2content is 4.26%, Al
2o
3content is 4.85%, the v-ti magnetite concentrate of S content 0.84%, be placed in NaOH mass concentration be 22% and KOH mass concentration be the mixed ammonium/alkali solutions of 5%, pass into the O of 89psi
2, then at the temperature of 260 DEG C, alkali soaks reaction 75 minutes, is filtered by reactant, obtain filtrate and alkali leaching cake A, NaOH consumption 32.6kg/t is to ore deposit, KOH consumption 49.3 kg/t to ore deposit, and described filtrate feeds recovery and processing system, and its chemical equation is with embodiment 1 and embodiment 5;
2) pickling
Alkali leaching cake A in step 1) is added water and makes the ore pulp that quality solid-to-liquid ratio is 1:9, then be placed in the H that mass concentration is 9%
2sO
4in solution, 90 DEG C of pickling 20 minutes, filtered by pickling reactant, obtain filtrate and acidleach filter cake B, described filtrate feeds recovery and processing system, and its chemical equation is with embodiment 1 and embodiment 5;
3) desliming
By step 2) in filtration after concentrated ilmenite B add water and be mixed with the ore pulp that mass concentration is 22%, carry out desliming operation with the desliming bucket of ∮ 3.0 meters, obtain sand setting C and overflow D;
4) heavy magnetic selects again
The spiral chute that the ore pulp that is made into mass concentration 40% of being added water by sand setting C in step 3) feeds ￠ 0.9 meter carries out gravity treatment, obtains gravity concentrate E and gravity tailings F; Being added water by gravity tailings F and forming the ore pulp field intensity of mass concentration 31% is that the magnetic dewater cone of 0.05T carries out a stages of magnetic separation, obtains an a stages of magnetic separation concentrate G1 and stages of magnetic separation mine tailing H1; By concentration be again 31% a stages of magnetic separation concentrate G1 to feed field intensity be that 0.15T drum magnetic separator carries out two stages of magnetic separation, respectively two stages of magnetic separation concentrate G2 and two stages of magnetic separation mine tailing H2;
Described gravity concentrate E and magnetic concentrate G2 merges into the final iron ore concentrate that TFe content is 66.4%, wherein SiO
2content is 0.45%, Al
2o
3content is 0.29%, S content is 0.01%; Described magnetic tailing H1 and H2 merges into final mine tailing, and overflow D is TiO
2content is the final ilmenite concentrate of 68.2%.
Embodiment 8:
As shown in Figure 3.
1) alkali oxide leaching
Be 52.6%, TiO by TFe content
2content is 12.7%, SiO
2content is 4.46%, Al
2o
3content is 5.05%, the v-ti magnetite concentrate of S content 0.74%, be placed in NaOH mass concentration be 20% and KOH mass concentration be the mixed ammonium/alkali solutions of 6%, add 192kg/t
to ore deposith
2o
2, then at the temperature of 265 DEG C, alkali soaks reaction 70 minutes, is filtered by reactant, filtrate and alkali leaching cake A, NaOH consumption 30.6kg/t to ore deposit, KOH consumption 46.8kg/t is to ore deposit, described filtrate feeds recovery and processing system, and its chemical equation is with embodiment 3 and embodiment 6;
2) pickling
Alkali leaching cake A in step 1) is added water and makes the ore pulp that quality solid-to-liquid ratio is 1:8.5, then be placed in the H that mass concentration is 9.5%
2sO
4in solution, 80 DEG C of pickling 30 minutes, filtered by pickling reactant, obtain filtrate and acidleach filter cake B, described filtrate feeds recovery and processing system, and its chemical equation is with embodiment 1 and embodiment 5;
3) desliming
By step 2) in filtration after concentrated ilmenite B add water and be mixed with the ore pulp that mass concentration is 22%, carry out desliming operation with the desliming bucket of ∮ 3.0 meters, obtain sand setting C and overflow D;
4) heavily magnetic separation is again
The spiral chute that the ore pulp that is made into mass concentration 40% of being added water by sand setting C in step 3) feeds ￠ 0.9 meter carries out gravity treatment, obtains gravity concentrate E and gravity tailings F; Being added water by gravity tailings F and forming the ore pulp field intensity of mass concentration 31% is that the magnetic dewater cone of 0.05T carries out a stages of magnetic separation, obtains an a stages of magnetic separation concentrate G1 and stages of magnetic separation mine tailing H1; By concentration be again 31% a stages of magnetic separation concentrate G1 to feed field intensity be that 0.15T drum magnetic separator carries out two stages of magnetic separation, respectively two stages of magnetic separation concentrate G2 and two stages of magnetic separation mine tailing H2;
Described gravity concentrate E and magnetic concentrate G2 merges into the final iron ore concentrate that TFe content is 67.2%, wherein SiO
2content is 0.47%, Al
2o
3content is 0.89%, S content is 0.01%; Described magnetic tailing H1 and H2 merges into final mine tailing, and overflow D is TiO
2content is the final ilmenite concentrate of 60.8%.
Claims (7)
1. utilize alkali oxide leaching, pickling, desliming and heavy magnetic to select a v-ti magnetite concentrate method again, it is characterized in that comprising the steps:
1) alkali oxide leaching
Be 50% ~ 55%, TiO by TFe content range
2content range is 10% ~ 15%, SiO
2content is 3% ~ 6%, Al
2o
3content is 3% ~ 6%, the v-ti magnetite concentrate of S content >0.5%, be placed in the aqueous slkali that mass concentration is 5% ~ 52%, add oxidant, then at the temperature of 220 DEG C ~ 330 DEG C, alkali soaks reaction 0.5 ~ 2 hour, reactant is filtered, obtain filtrate and alkali leaching cake A, described filtrate feeds recovery and processing system;
2) pickling
Alkali leaching cake A in step 1) is added water and makes the ore pulp that solid-liquid mass ratio is 1:1 ~ 10, then be placed in the H that mass concentration is 1% ~ 10%
2sO
4in solution, under 50 ~ 90 DEG C of conditions, pickling 5 ~ 60 minutes, filters pickling reactant, and obtain filtrate and acidleach filter cake B, described filtrate feeds recovery and processing system;
3) desliming
By step 2) in acidleach filter cake B add water and be mixed with the ore pulp that mass concentration is 21% ~ 25%, carry out desliming operation with the desliming bucket of ∮ 3.0 ~ 5.0 meters, obtain sand setting C and overflow D;
4) heavy magnetic selects again
The ore pulp being made into mass concentration 36% ~ 41% that added water by sand setting C in step 3) carries out gravity treatment, obtains gravity concentrate E and gravity tailings F; The ore pulp being mixed with mass concentration 30% ~ 34% that added water by gravity tailings F again carries out magnetic separation, obtains magnetic concentrate G and magnetic tailing H;
Described gravity concentrate E and magnetic concentrate G merges into the final iron ore concentrate that TFe content range is 64% ~ 70%, and described magnetic tailing H and overflow D merges into TiO
2content range is the final ilmenite concentrate of 60% ~ 82%.
2. alkali oxide leaching, pickling, desliming and the heavy magnetic of utilizing according to claim 1 selects v-ti magnetite concentrate method again, it is characterized in that described aqueous slkali is any one in the NaOH aqueous solution, the KOH aqueous solution or NaOH and KOH mixed aqueous solution.
3. alkali oxide leaching, pickling, desliming and the heavy magnetic of utilizing according to claim 1 selects v-ti magnetite concentrate method again, it is characterized in that described oxidant is O
2or H
2o
2, described O
2addition is 20 ~ 120psi, H
2o
2addition is 50 ~ 200kg/t
to ore deposit.
4. alkali oxide leaching, pickling, desliming and the heavy magnetic of utilizing according to claim 1 selects v-ti magnetite concentrate method again, it is characterized in that described gravity treatment adopts the spiral chute of ￠ 0.6 ~ ￠ 1.2 meters to carry out gravity treatment.
5. alkali oxide leaching, pickling, desliming and the heavy magnetic of utilizing according to claim 1 selects v-ti magnetite concentrate method again, it is characterized in that described magnetic separation adopts the drum magnetic separator of 0.12T ~ 0.15T to carry out magnetic separation.
6. alkali oxide leaching, pickling, desliming and the heavy magnetic of utilizing according to claim 1 selects v-ti magnetite concentrate method again, it is characterized in that described magnetic separation adopts the magnetic dewater cone of 0.03T ~ 0.05T to carry out magnetic separation.
7. alkali oxide leaching, pickling, desliming and the heavy magnetic of utilizing according to claim 1 selects v-ti magnetite concentrate method again, it is characterized in that described magnetic separation adopts the drum magnetic separator of 0.12T ~ 0.15T and 0.03T ~ 0.05T magnetic dewater cone to carry out two stages of magnetic separation respectively.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510320560.XA CN105013608A (en) | 2015-06-12 | 2015-06-12 | Vanadium-titanium magnetite concentrate re-concentration method achieved through oxidation alkaline leaching, acid pickling, desliming and gravity and magnetism |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510320560.XA CN105013608A (en) | 2015-06-12 | 2015-06-12 | Vanadium-titanium magnetite concentrate re-concentration method achieved through oxidation alkaline leaching, acid pickling, desliming and gravity and magnetism |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN105013608A true CN105013608A (en) | 2015-11-04 |
Family
ID=54404115
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201510320560.XA Pending CN105013608A (en) | 2015-06-12 | 2015-06-12 | Vanadium-titanium magnetite concentrate re-concentration method achieved through oxidation alkaline leaching, acid pickling, desliming and gravity and magnetism |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN105013608A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109174398A (en) * | 2018-08-02 | 2019-01-11 | 汤铁 | A kind of comprehensive utilization process of vanadium titano-magnetite |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO1995028503A1 (en) * | 1994-04-15 | 1995-10-26 | Technological Resources Pty Ltd | Treatment of leach liquors for upgrading a titaniferous material |
| CN102181626A (en) * | 2011-04-08 | 2011-09-14 | 北京矿冶研究总院 | Beneficiation method of ilmenite |
| CN102417978A (en) * | 2011-12-14 | 2012-04-18 | 昆明理工大学 | Method for enriching titanium in coal gangue |
| CN103691550A (en) * | 2013-12-18 | 2014-04-02 | 广西科晟达机械制造有限公司 | Beneficiation method of ilmenite |
| CN103962220A (en) * | 2014-04-23 | 2014-08-06 | 鞍钢集团矿业公司 | Vanadium-titanium magnetite concentrate recleaning method realized through alkaline leaching, acid pickling, desliming and combined gravity-magnetic separation |
| CN103962219A (en) * | 2014-04-23 | 2014-08-06 | 鞍钢集团矿业公司 | Vanadium-titanium magnetite concentrate recleaning method realized through alkaline leaching, classification and combined magnetic-gravity separation |
-
2015
- 2015-06-12 CN CN201510320560.XA patent/CN105013608A/en active Pending
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO1995028503A1 (en) * | 1994-04-15 | 1995-10-26 | Technological Resources Pty Ltd | Treatment of leach liquors for upgrading a titaniferous material |
| CN102181626A (en) * | 2011-04-08 | 2011-09-14 | 北京矿冶研究总院 | Beneficiation method of ilmenite |
| CN102417978A (en) * | 2011-12-14 | 2012-04-18 | 昆明理工大学 | Method for enriching titanium in coal gangue |
| CN103691550A (en) * | 2013-12-18 | 2014-04-02 | 广西科晟达机械制造有限公司 | Beneficiation method of ilmenite |
| CN103962220A (en) * | 2014-04-23 | 2014-08-06 | 鞍钢集团矿业公司 | Vanadium-titanium magnetite concentrate recleaning method realized through alkaline leaching, acid pickling, desliming and combined gravity-magnetic separation |
| CN103962219A (en) * | 2014-04-23 | 2014-08-06 | 鞍钢集团矿业公司 | Vanadium-titanium magnetite concentrate recleaning method realized through alkaline leaching, classification and combined magnetic-gravity separation |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109174398A (en) * | 2018-08-02 | 2019-01-11 | 汤铁 | A kind of comprehensive utilization process of vanadium titano-magnetite |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN103966435B (en) | Alkali leaching, pickling and magnetic separation is utilized to select the method for v-ti magnetite concentrate again | |
| CN103952533B (en) | Calcining, alkali leaching and desliming is utilized to select the method for v-ti magnetite concentrate again | |
| CN103977880B (en) | Method for recleaning of vanadium-titanium magnetite concentrates by utilizing alkaline leaching, desliming and magnetic-gravity combined separation | |
| CN104962735A (en) | Method for recleaning vanadium-titanium magnetite concentrates through oxidation alkaline leaching, acid pickling and magnetic separation | |
| CN103966423B (en) | Alkali leaching, pickling and gravity treatment is utilized to select the method for v-ti magnetite concentrate again | |
| CN103952532B (en) | Utilize the method that alkali soaks, v-ti magnetite concentrate is selected in classification again | |
| CN103966436B (en) | Utilize the method that alkali soaks, v-ti magnetite concentrate is selected in desliming again | |
| CN103962226B (en) | Calcining, alkali leaching, pickling and magnetic reconnection is utilized to close and select v-ti magnetite concentrate method again | |
| CN103966422B (en) | Calcining, alkali leaching, pickling and gravity treatment is utilized to select the method for v-ti magnetite concentrate again | |
| CN105013608A (en) | Vanadium-titanium magnetite concentrate re-concentration method achieved through oxidation alkaline leaching, acid pickling, desliming and gravity and magnetism | |
| CN103962220B (en) | Alkali leaching, pickling, desliming and heavy magnetic associating is utilized to select v-ti magnetite concentrate method again | |
| CN104689902A (en) | Method for recleaning vanadium-titanium magnetite concentrates by utilizing alkaline leaching, acid pickling, desliming and reverse flotation | |
| CN103962224B (en) | Alkali leaching, pickling and magnetic reconnection is utilized to close the method selecting v-ti magnetite concentrate again | |
| CN103962225B (en) | The method of utilize that alkali soaks, v-ti magnetite concentrate being selected in classification and gravity treatment again | |
| CN103962227B (en) | Utilize the method that v-ti magnetite concentrate is selected in alkali leaching, desliming and gravity treatment again | |
| CN103952549B (en) | Alkali leaching, pickling and reverse flotation is utilized to select the method for v-ti magnetite concentrate again | |
| CN105296752A (en) | Method for recleaning vanadium-titanium magnetite concentrates by using oxidation and alkaline leaching, desliming and combined magneto-gravity separation | |
| CN104878221A (en) | Method for utilizing oxidation alkaline leaching and desliming to re-concentrate vanadium-titanium magnetite concentrates | |
| CN103962218B (en) | Utilize calcining, alkali leaching, desliming and heavily select the method selecting v-ti magnetite concentrate again | |
| CN103962223B (en) | Utilize the method that v-ti magnetite concentrate is selected in calcining, alkali leaching, classification again | |
| CN103962228B (en) | Utilize calcining, alkali leaching, classification and heavily select the method selecting v-ti magnetite concentrate again | |
| CN104962730A (en) | Method for magnetic separation of vanadium-titanium magnetite concentrate through forging, oxidative alkaline leaching and de-sliming | |
| CN104959215A (en) | Method for reselecting vanadium-titanium magnetite concentrate by using oxidization alkaline leaching, acid washing and magnetic gravitational combination | |
| CN104888937A (en) | Vanadium-titanium magnetite concentrate method by using calcinations, oxidation by alkaline leaching, grading and magnetic gravitational reselection | |
| CN104911331A (en) | Method for separating vanadium-titanium magnetite concentrate by calcining, oxidation alkali leaching, pickling and magnetic reseparation |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| CB02 | Change of applicant information |
Address after: 114001 Anshan District, Liaoning, No. 219 Road, No. 39, Tiedong Applicant after: Anshan Iron and Steel Group Mining Co., Ltd. Address before: 114001 Anshan District, Liaoning, No. 219 Road, No. 39, Tiedong Applicant before: Angang Group Mine Company |
|
| COR | Change of bibliographic data | ||
| RJ01 | Rejection of invention patent application after publication | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20151104 |