CN103966422B - Calcining, alkali leaching, pickling and gravity treatment is utilized to select the method for v-ti magnetite concentrate again - Google Patents
Calcining, alkali leaching, pickling and gravity treatment is utilized to select the method for v-ti magnetite concentrate again Download PDFInfo
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Abstract
The method that the present invention discloses and a kind ofly utilizes calcining, v-ti magnetite concentrate is selected in alkali leaching, pickling and gravity treatment again, comprise the steps: by v-ti magnetite concentrate by weight the ratio of 1:0.1 ~ 0.2 add CaO and calcine, form calcination product A; Product A is placed in the alkaline solution alkali leaching reaction 0.5 ~ 5 hour that mass concentration is 5% ~ 52%, filters, obtain filtrate and alkali leaching cake B, B to be placed under H2SO4 solution 50 ~ 90 DEG C of conditions pickling 5 ~ 60 minutes, to filter, obtain filtrate and acidleach filter cake C; Again C is carried out gravity treatment, obtaining TFe content range is respectively 65% ~ 68% iron ore concentrate and TiO
2content range is 60% ~ 80% ilmenite concentrate.Advantage of the present invention is: reduce NaOH or KOH consumption, achieve and v-ti magnetite concentrate is efficiently sorted, alkaline consumption is low, reduce and enter the foreign matter contents such as blast furnace Al and Si, improve the capacity factor of a blast furnace, reduce the quantity discharged of blast furnace slag, reduce ironmaking cost, solve with serious pollution problem, improve titanium resource comprehensive utilization ratio simultaneously.
Description
Technical field
The present invention relates to a kind of ore-dressing technique of v-ti magnetite concentrate, particularly relate to a kind of method utilizing calcining, alkali leaching, pickling and gravity treatment to select v-ti magnetite concentrate again.
Background technology
Vanadium titano-magnetite is a kind of complex ore of multiple metallic element, is based on the magnetite 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 body 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 | Fe2O3 | TiO2 | V2O5 |
| Raw ore | 29.53 | 21.36 | 20.20 | 0.631 | 17.70 | 10.54 | 0.278 |
| Concentrate | 54.01 | 32.42 | 51.16 | 0.574 | 40.97 | 12.67 | 0.61 |
| Element | SiO2 | Al2O3 | 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 concentration method cannot realize titanium, iron from the source of ore, cause v-ti magnetite ore after physical concentration, iron concentrate grade low (TFe<55%), the titanium in iron ore concentrate enters blast furnace slag (TiO completely at iron manufacturing process
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 technical 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 concentration methods such as common gravity separation method, magnetic method, flotation process 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 smelting, almost all enter slag phase, form TiO
2the blast furnace slag of content 20 ~ 24%; In addition, because the foreign matter contents such as S, Si, the Al in iron ore concentrate are also too high, above-mentioned reason not only causes that steelmaking furnace utilization coefficient 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 surface physicochemical property, adds complexity and the process cost of the method.In a word, by this kind of procedure complexity, and in treating processes, 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 processing sefstromite concentrate prepares the method for titanium liquid ", proposes the method with salt pickling separating titanium iron.This invention is the method that wet processing 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.
During Chinese patent 201210137458.2 discloses " reclaiming the method for vanadium in vanadium titano-magnetite ", adopt calcification baking-carbonating to leach the vanadium reclaimed in vanadium titano-magnetite, the agglomerates of sintered pellets of the calcic Iron-ore Slag obtained can directly apply to blast-furnace smelting; Thus efficiently solve the recovery of vanadium in vanadium titano-magnetite, can't follow-up blast-furnace smelting be impacted; The recyclable chromium of crystalline mother solution obtained after reclaiming vanadium, thus more effectively realize the comprehensive utilization of vanadium titano-magnetite.Although the method applies the method for calcification baking, alkali-free leaching, magnetic separation process, pickling is weakly acidic carbonating, obviously different from the mechanism of action of sulfuric acid strong acid.
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 the method that v-ti magnetite concentrate is selected in quality and the high and utilization calcining of good operability of efficiency, alkali leaching, pickling and gravity treatment again, achieve and high efficiency separation is carried out to titanium, iron in v-ti magnetite concentrate, 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 quantity discharged of blast furnace slag, reduce ironmaking cost, improve TiO
2comprehensive resource utilization rate, reduces NaOH or KOH consumption simultaneously, decreases environmental pollution.
In order to realize object of the present invention, technical scheme of the present invention is achieved in that
A kind of method utilizing calcining, alkali leaching, pickling and gravity treatment to select v-ti magnetite concentrate more of the present invention, is characterized in that comprising the steps:
1) calcine
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 ratio of the v-ti magnetite concentrate of S content >0.5% 1:0.1 ~ 0.2 by weight adds CaO, at the temperature of 800 DEG C ~ 1400 DEG C, carry out calcining 20 ~ 60 minutes, forms calcination product A;
2) alkali leaching
By step 1) in calcination product A be placed in the alkaline solution that mass concentration is 5% ~ 52%, alkali leaching reaction 0.5 ~ 5 hour at the temperature of 300 DEG C ~ 370 DEG C, filtered by reactant, obtain filtrate and alkali leaching cake B, described filtrate feeds recovery and processing system;
3) pickling
By step 2) in alkali leaching cake B add water and make 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 C, described filtrate feeds recovery and processing system;
4) gravity treatment
By step 3) in the acidleach filter cake C ore pulp making mass concentration 35% ~ 40% that adds water carry out gravity treatment, obtain gravity concentrate D, gravity tailings E and gravity treatment chats F respectively, described gravity concentrate D to be TFe content range be 65% ~ 68% iron ore concentrate, described gravity treatment chats F to be TiO2 content range be 60% ~ 80% ilmenite concentrate, described gravity tailings E is SiO
2content range is the true tailings of 58% ~ 62%.
Described alkaline solution is any one in NaOH or the KOH aqueous solution, NaOH and KOH mixed aqueous solution.
Described gravity treatment adopts the spiral chute of ￠ 0.6 ~ ￠ 1.2 meters to carry out gravity treatment.
Advantage of the present invention is:
Method synthesis of the present invention uses calcining, alkali leaching, pickling and gravity treatment to select the method for v-ti magnetite concentrate again, achieves titanium in v-ti magnetite concentrate, iron high efficiency separation; 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 3%, Al by 3% ~ 6%
2o
3content is down to less than 3% by 3% ~ 6%, for subsequent smelting creates better condition.
Calcination utilizes CaO part to replace alkali lye consumption in the dipped journey of alkali, decreases the consumption 20% ~ 30% of NaOH or KOH in follow-up alkali leaching operation; Because CaO price is NaOH price 1/5 ~ 1/6, be 1/20 of KOH price, therefore greatly can reduce production cost.
The process of alkali leaching has carried out chemical reaction to elements such as Ti, S, Si, Al in v-ti magnetite concentrate, defines corresponding salt.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 SiO2, Al
2o
3deng on mineral, alkali is made to soak v-ti magnetite concentrate more less than alkali leaching ferrotianium raw ore alkali consumption, better effects if.Such as, after calcining, when soaking with NaOH alkali, the alkali number that the present invention consumes is less than 60kg/t concentrate, reduces more than 7 times than the alkali number 469kg/t raw ore of alkali leaching raw ore consumption.
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 conditions is gentle, and little to equipment corrosion, cost is low, is more conducive to suitability for industrialized production.
Add gravity treatment, make iron concentrate grade bring up to 65% ~ 68% by 50% ~ 55%, be less than 0.1%, SiO containing S amount in iron ore concentrate simultaneously
2and Al
2o
3content is all less than 3%, TiO
2content is down to less than 6% by 12.91%; Meanwhile, TiO can also be obtained
2content is the ilmenite concentrate of 60% ~ 80%.Employing the method achieves and is effectively separated titanium, iron, reduces and enters blast furnace TiO
2, the impurity such as S, Si, Al content, improve the capacity factor of a blast furnace, reduce the quantity discharged of blast furnace slag, reduce ironmaking cost, improve titanium resource comprehensive utilization ratio simultaneously.
Accompanying drawing explanation
Fig. 1 is present invention process schema.
Fig. 2 is that the present invention adopts two sections of gravity separation technology schemas.
Embodiment
Below in conjunction with accompanying drawing, the specific embodiment of the present invention is described further:
As shown in Figure 1.
Embodiment 1
1) calcine
Be 50.2%, TiO by TFe content
2content is 14.5%, SiO
2content is 3.60%, Al
2o
3content is 4.45%, the v-ti magnetite concentrate of S content 0.56%, and the ratio of 1:0.1 adds CaO by weight, at the temperature of 800 DEG C, carry out calcining 60 minutes, and form calcination product A, its chemical equation is:
2) alkali leaching
By step 1) in calcination product A be placed in the NaOH alkaline solution that mass concentration is 30%, alkali leaching reaction 4.5 hours at the temperature of 300 DEG C, reactant is filtered, obtain filtrate and alkali leaching cake B, NaOH consumption 48kg/t is to ore deposit, described filtrate feeds recovery and processing system, and its chemical equation is:
3) pickling
By step 2) in alkali leaching cake B add water and make the ore pulp that solid-liquid mass ratio is 1:9, then be placed in the H that mass concentration is 7%
2sO
4in solution, under the condition of 65 DEG C, pickling 55 minutes, filters pickling reactant, and obtain filtrate and acidleach filter cake C, described filtrate feeds recovery and processing system, and its chemical equation is:
Na
2o (TiO
2)
x+ H
+ heating(H
2o) (TiO
2)
x↓+Na
+
Na
2o (SiO
2)
t+ H
+ heating(H
2o) (SiO
2)
t↓+Na
+
4) gravity treatment
By step 3) in the add water spiral chute of the ore pulp ￠ 1.2 meters making mass concentration 40% of acidleach filter cake C carry out gravity treatment, respectively gravity concentrate D, gravity tailings E and gravity treatment chats F, gravity concentrate D to be TFe content be 65.9% final iron ore concentrate (SiO
2content is 0.68%, Al
2o
3content is 1.38%, S content is 0.02%), described gravity tailings E is SiO
2content is the true tailings of 60.9%, and gravity treatment chats F is TiO
2content is the final ilmenite concentrate of 61.0%.
Embodiment 2
1) calcine
Be 54.1%, TiO by TFe content
2content is 11.0%, SiO
2content is 3.52%, Al
2o
3content is 5.48%, the v-ti magnetite concentrate of S content 0.71%, and the ratio of 1:0.1 adds CaO by weight, at the temperature of 900 DEG C, carry out calcining 50 minutes, and form calcination product A, its chemical equation is with embodiment 1.
2) alkali leaching
By step 1) calcination product A is placed in the NaOH alkaline solution that mass concentration is 20%, alkali leaching reaction 2 hours at the temperature of 350 DEG C, reactant is filtered, obtain filtrate and alkali leaching cake B, NaOH consumption 42kg/t is to ore deposit, described filtrate feeds recovery and processing system, and its chemical equation is with embodiment 1.
3) pickling
By step 2) in alkali leaching cake B add water and make the ore pulp that solid-liquid mass ratio is 1:7, then be placed in the H that mass concentration is 7%
2sO
4in solution, under the condition of 50 DEG C, pickling 20 minutes, filters pickling reactant, and obtain filtrate and acidleach filter cake C, described filtrate feeds recovery and processing system, and its chemical equation is with embodiment 1.
4) gravity treatment
By step 3) in the add water spiral chute of the ore pulp ￠ 0.9 meter making mass concentration 36% of acidleach filter cake C carry out gravity treatment, respectively gravity concentrate D, gravity tailings E and gravity treatment chats F, gravity concentrate D to be TFe content be 66.0% final iron ore concentrate (SiO
2content is 0.68%, Al
2o
3content is 1.38%, S content is 0.02%), described gravity tailings E is SiO
2content is the true tailings of 59.1%, and gravity treatment chats F is TiO
2content is the final ilmenite concentrate of 76.3%.
Embodiment 3
1) calcine
Be 53.5%, TiO by TFe content
2content is 12.9%, SiO
2content is 3.70%, Al
2o
3content is 5.46%, the v-ti magnetite concentrate of S content 0.84%, and the ratio of 1:0.1 adds CaO by weight, at the temperature of 1000 DEG C, carry out calcining 40 minutes, and form calcination product A, its chemical equation is with embodiment 1.
2) alkali leaching
By step 1) calcination product A is placed in the NaOH alkaline solution that mass concentration is 15%, alkali leaching reaction 2.5 hours at the temperature of 310 DEG C, reactant is filtered, obtain filtrate and alkali leaching cake B, NaOH consumption 43kg/t is to ore deposit, described filtrate feeds recovery and processing system, and its chemical equation is with embodiment 1.
3) pickling
By step 2) in alkali leaching cake B add water and make the ore pulp that solid-liquid mass ratio is 1:5, then be placed in the H that mass concentration is 6%
2sO
4in solution, under the condition of 60 DEG C, pickling 10 minutes, filters pickling reactant, and obtain filtrate and acidleach filter cake C, described filtrate feeds recovery and processing system, and its chemical equation is with embodiment 1.
4) gravity treatment
By step 3) in the add water spiral chute of the ore pulp ￠ 1.2 meters making mass concentration 40% of acidleach filter cake C carry out gravity treatment, respectively gravity concentrate D, gravity tailings E and gravity treatment chats F, gravity concentrate D to be TFe content be 65.8% final iron ore concentrate (SiO
2content is 0.48%, Al
2o
3content is 1.88%, S content is 0.02%), described gravity tailings E is SiO
2content is the true tailings of 59.6%, and gravity treatment chats F is TiO
2content is the final ilmenite concentrate of 72.8%.
Embodiment 4
1) calcine
Be 52.0%, TiO by TFe content
2content is 13.5%, SiO
2content is 3.90%, Al
2o
3content is 5.60%, the v-ti magnetite concentrate of S content 0.59%, and the ratio of 1:0.15 adds CaO by weight, at the temperature of 1100 DEG C, carry out calcining 40 minutes, and form calcination product A, its chemical equation is with embodiment 1.
2) alkali leaching
By step 1) calcination product A is placed in the NaOH alkaline solution that mass concentration is 10%, alkali leaching reaction 0.5 hour at the temperature of 365 DEG C, reactant is filtered, obtain filtrate and alkali leaching cake B, NaOH consumption 40kg/t is to ore deposit, described filtrate feeds recovery and processing system, and its chemical equation is with embodiment 1.
3) pickling
By step 2) in alkali leaching cake B add water and make the ore pulp that solid-liquid mass ratio is 1:1.5, then be placed in the H that mass concentration is 3%
2sO
4in solution, under the condition of 65 DEG C, pickling 40 minutes, filters pickling reactant, and obtain filtrate and acidleach filter cake C, described filtrate feeds recovery and processing system, and its chemical equation is with embodiment 1.
4) gravity treatment
By step 3) in the add water spiral chute of the ore pulp ￠ 0.9 meter making mass concentration 40% of acidleach filter cake C carry out gravity treatment, respectively gravity concentrate D, gravity tailings E and gravity treatment chats F, gravity concentrate D to be TFe content be 67.5% final iron ore concentrate (SiO
2content is 0.48%, Al
2o
3content is 1.88%, S content is 0.02%), described gravity tailings E is SiO
2content is the true tailings of 58.2%, and gravity treatment chats F is TiO
2content is the final ilmenite concentrate of 72.5%.
Embodiment 5
As shown in Figure 2.
1) calcine
Be 52.3%, TiO by TFe content
2content is 12.5%, SiO
2content is 3.89%, Al
2o
3content is 4.62%, the v-ti magnetite concentrate of S content 0.57%, and the ratio of 1:0.15 adds CaO by weight, at the temperature of 1200 DEG C, carry out calcining 30 minutes, and form calcination product A, its chemical equation is with embodiment 1.
2) alkali leaching
By step 1) calcination product A is placed in the KOH alkaline solution that mass concentration is 38%, alkali leaching reaction 4.0 hours at the temperature of 300 DEG C, reactant is filtered, obtain filtrate and alkali leaching cake B, KOH consumption 65kg/t is to ore deposit, described filtrate feeds recovery and processing system, and its chemical equation is:
3) pickling
By step 2) in alkali leaching cake B add water and make the ore pulp that solid-liquid mass ratio is 1:3.5, then be placed in the H that mass concentration is 9%
2sO
4in solution, under the condition of 60 DEG C of pickling 20 minutes, filtered by pickling reactant, obtain filtrate and acidleach filter cake C, described filtrate fed recovery and processing system, and its chemical equation is:
K
2o (TiO
2) x+H
+ heating(H
2o) (TiO
2)
x↓+K
+
K
2o (SiO
2)
t+ H
+ heating(H
2o) (SiO
2)
t↓+K
+
4) gravity treatment
By step 3) in add water spiral chute that the ore pulp of making mass concentration 36% feeds ￠ 0.6 meter of acidleach filter cake C carry out one section and roughly select, obtain one section of rougher concentration D1, an one section of rougher tailings E1 and section respectively and roughly select chats F, the spiral chute that the ore pulp of making mass concentration 41% of being added water by one section of rougher concentration D1 feeds ￠ 0.6 meter carry out two sections selected, obtain two sections of selected concentrate D2 and two section cleaner tailings E2 respectively, two sections of cleaner tailings E2 return one section of spiral chute roughly selected, two sections of selected concentrate D2 to be TFe content be 66.1% final iron ore concentrate (SiO
2content is 0.43%, Al
2o
3content is 1.65%, S content is 0.02%), one section of described rougher tailings E1 is SiO
2content is the true tailings of 59.9%, and one section is roughly selected chats F is TiO
2content is the final ilmenite concentrate of 71.3%.
Embodiment 6
1) calcine
Be 53.5%, TiO by TFe content
2content is 11.8%, SiO
2content is 3.90%, Al
2o
3content is 4.70%, the v-ti magnetite concentrate of S content 0.55%, and the ratio of 1:0.2 adds CaO by weight, at the temperature of 1300 DEG C, carry out calcining 20 minutes, and form calcination product A, its chemical equation is with embodiment 1.
2) alkali leaching
By step 1) calcination product A is placed in the KOH alkaline solution that mass concentration is 48%, alkali leaching reaction 3.5 hours at the temperature of 310 DEG C, reactant is filtered, obtain filtrate and alkali leaching cake B, KOH consumption 46kg/t is to ore deposit, described filtrate feeds recovery and processing system, and its chemical equation is with embodiment 5.
3) pickling
By step 2) in alkali leaching cake B add water and make the ore pulp that solid-liquid mass ratio is 1:2, then be placed in the H that mass concentration is 2%
2sO
4in solution, under the condition of 90 DEG C, pickling 50 minutes, filters pickling reactant, and obtain filtrate and acidleach filter cake C, described filtrate feeds recovery and processing system, and its chemical equation is with embodiment 5.
4) gravity treatment
By step 3) in add water spiral chute that the ore pulp of making mass concentration 37% feeds ￠ 0.9 meter of acidleach filter cake C carry out one section and roughly select, obtain one section of rougher concentration D1, an one section of rougher tailings E1 and section respectively and roughly select chats F, the spiral chute that the ore pulp of making mass concentration 40% of being added water by one section of rougher concentration D1 feeds ￠ 0.6 meter carry out two sections selected, obtain two sections of selected concentrate D2 and two section cleaner tailings E2 respectively, two sections of cleaner tailings E2 return one section of spiral chute roughly selected, two sections of selected concentrate D2 to be TFe content be 66.3% final iron ore concentrate (SiO
2content is 0.49%, Al
2o
3content is 1.85%, S content is 0.02%), one section of described rougher tailings E1 is SiO
2content is the true tailings of 58.0%, and one section is roughly selected chats F is TiO
2content is the final ilmenite concentrate of 72.8%.
Embodiment 7:
1) calcine
Be 52.3%, TiO by TFe content
2content is 11.1%, SiO
2content is 4.00%, Al
2o
3content is 4.62%, the v-ti magnetite concentrate of S content 0.68%, and the ratio of 1:0.2 adds CaO by weight, at the temperature of 1400 DEG C, carry out calcining 15 minutes, and form calcination product A, its chemical equation is with embodiment 1.
2) alkali leaching
By step 1) calcination product A is placed in that NaOH mass concentration is 20%, KOH mass concentration is the alkaline solution of 6%, alkali leaching reaction 2.0 hours at the temperature of 300 DEG C, reactant is filtered, obtain filtrate and alkali leaching cake B, NaOH consumption 30kg/t is to ore deposit, KOH consumption 10kg/t is to ore deposit, and described filtrate feeds recovery and processing system, and its chemical equation is with embodiment 1 and embodiment 5.
3) pickling
By step 2) in alkali leaching cake B add water and make the ore pulp that solid-liquid mass ratio is 1:2, then be placed in the H that mass concentration is 2%
2sO
4in solution, 80 DEG C of pickling 45 minutes, filtered by pickling reactant, obtain filtrate and acidleach filter cake C, described filtrate feeds recovery and processing system, and its chemical equation is with embodiment 1 and embodiment 5.
4) gravity treatment
By step 3) in add water one section of spiral chute that the ore pulp of making mass concentration 37% feeds ￠ 0.9 meter of acidleach filter cake C carry out one section and roughly select, obtain one section of rougher concentration D1, an one section of rougher tailings E1 and section respectively and roughly select chats F, the spiral chute that the ore pulp of making mass concentration 40% of being added water by one section of rougher concentration D1 feeds ￠ 0.6 meter carry out two sections selected, obtain two sections of selected concentrate D2 and two section cleaner tailings E2 respectively, two sections of cleaner tailings E2 return one section of spiral chute, two sections of selected concentrate D2 to be TFe content be 67.3% final iron ore concentrate (SiO
2content is 0.33%, Al
2o
3content is 1.33%, S content is 0.01%), one section of described rougher tailings E1 is SiO
2content is the true tailings of 58.5%, and one section is roughly selected chats F is TiO
2content is the final ilmenite concentrate of 73.0%.
Claims (2)
1. utilize calcining, alkali leaching, pickling and gravity treatment to select a method for v-ti magnetite concentrate again, it is characterized in that comprising the steps:
1) calcine
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 ratio of the v-ti magnetite concentrate of S content >0.5% 1:0.1 ~ 0.2 by weight adds CaO, at the temperature of 800 DEG C ~ 1400 DEG C, carry out calcining 20 ~ 60 minutes, forms calcination product A;
2) alkali leaching
Calcination product A in step 1) is placed in the alkaline solution that mass concentration is 5% ~ 52%, alkali leaching reaction 0.5 ~ 5 hour at the temperature of 300 DEG C ~ 370 DEG C, filtered by reactant, obtain filtrate and alkali leaching cake B, described filtrate feeds recovery and processing system;
3) pickling
By step 2) in alkali leaching cake B add water and make 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 C, described filtrate feeds recovery and processing system;
4) gravity treatment
The ore pulp making mass concentration 35% ~ 40% that added water by acidleach filter cake C in step 3) carries out gravity treatment, obtain gravity concentrate D, gravity tailings E and gravity treatment chats F respectively, described gravity concentrate D to be TFe content range be 65% ~ 68% iron ore concentrate, described gravity treatment chats F to be TiO2 content range be 60% ~ 80% ilmenite concentrate, described gravity tailings E is SiO
2content range is the true tailings of 58% ~ 62%,
Described alkaline solution is any one in NaOH or the KOH aqueous solution, NaOH and KOH mixed aqueous solution.
2. the method utilizing calcining, alkali leaching, pickling and gravity treatment to select v-ti magnetite concentrate more according to claim 1, is characterized in that described gravity treatment adopts the spiral chute of ￠ 0.6 ~ ￠ 1.2 meters to carry out gravity treatment.
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| CN104894365A (en) * | 2015-06-12 | 2015-09-09 | 鞍钢集团矿业公司 | Method for recleaning of vanadium-titanium magnetite concentrate through calcination, oxidation alkaline leaching, acid pickling and reselection |
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| US4567026A (en) * | 1984-10-24 | 1986-01-28 | Internorth, Inc. | Method for extraction of iron aluminum and titanium from coal ash |
| CN101037722A (en) * | 2007-04-28 | 2007-09-19 | 中南大学 | Method for preparing puddling iron concentrate by high-alumina iron ore |
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| BR9704435A (en) * | 1997-10-17 | 2000-06-06 | Vale Do Rio Doce Co | Process for the production of titanium concentrate with a chemical composition similar to ilmenite from anatase ores with high content of impurities |
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| US4567026A (en) * | 1984-10-24 | 1986-01-28 | Internorth, Inc. | Method for extraction of iron aluminum and titanium from coal ash |
| CN101037722A (en) * | 2007-04-28 | 2007-09-19 | 中南大学 | Method for preparing puddling iron concentrate by high-alumina iron ore |
| CN102181626A (en) * | 2011-04-08 | 2011-09-14 | 北京矿冶研究总院 | Beneficiation method of ilmenite |
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