CN105013608A - Vanadium-titanium magnetite concentrate re-concentration method achieved through oxidation alkaline leaching, acid pickling, desliming and gravity and magnetism - Google Patents

Abstract

The invention relates to a method for re-selecting vanadium-titanium magnetite concentrate by oxidizing alkali leaching, pickling, desliming and remagnetization, which is characterized in that it comprises the following steps: the vanadium-titanium magnetite concentrate is placed in an alkaline solution by oxidizing alkali leaching, Add an oxidizing agent, then react with alkali leaching at a temperature of 220°C to 330°C for 0.5 to 2 hours, filter to obtain the filtrate and alkali leaching filter cake A, add water to the alkali leaching filter cake A to make a slurry, and then place it in H ₂ SO ₄ In the solution, acid wash at 50-90°C for 5-60 minutes, filter to obtain the filtrate and acid leaching filter cake B; then add water to B to make a pulp with a mass concentration of 30-35% for desliming and gravity-magnetic re-election. Iron concentrates with TFe content of 64-70% and titanium concentrates with TiO ₂ content of 60-82% were obtained respectively. Its advantages are: the introduction of O ₂ or H ₂ O ₂ in the oxidative alkali leaching oxidizes the S-containing compound, accelerates the reaction, reduces the reaction temperature, shortens the reaction time, and greatly reduces energy consumption and equipment investment.

Description

The method of re-selecting vanadium-titanium magnetite concentrate by oxidizing alkali leaching, pickling, desliming and re-magnetism

technical field

The invention relates to a beneficiation process of a vanadium-titanium magnetite concentrate, in particular to a method for re-selecting a vanadium-titanium magnetite concentrate by using oxidative alkali leaching, pickling, desliming and gravity magnetism.

Background technique

Vanadium-titanium magnetite is a compound ore of multi-metal elements, which is a symbiotic magnetite mainly containing iron, vanadium and titanium. The vanadium-titanium magnetite concentrate is one of the products obtained from vanadium-titanium magnetite through ore dressing, in which vanadium exists in the titanium magnetite in the same quality and isomorphism to replace high-valent iron ions. Titanomagnetite is the main crystal mineral (Fe ₃ O ₄ ) and guest crystal ore [ilmenite spar 2FeO·TiO ₂ , ilmenite FeO·TiO ₂ , aluminum magnesium spinel (Mg,Fe) (Al,Fe ) ₂ O ₄ ] complexes formed. For example, the chemical multi-element analysis results of vanadium-titanium magnetite raw ore and vanadium-titanium magnetite concentrate after iron selection in Midi Concentrator in Panzhihua, China are shown in Table 1. The vanadium-titanium magnetite raw ore and vanadium-titanium magnetite concentrate The analysis results are shown in Table 2 and Table 3, respectively.

Table 1 Chemical multi-element analysis results of raw ore and vanadium-titanium magnetite concentrate of Midi concentrator in Panzhihua, China

element TF FeO mFe S _{Fe2O3 _} TiO ₂ V ₂ O 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 ₂ O 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 The chemical phase analysis results of titanium and iron in the vanadium-titanium magnetite raw ore of Midi concentrator in Panzhihua, China

Table 3 Chemical phase analysis results of titanium and iron in the vanadium-titanium magnetite concentrate of Midi concentrator in Panzhihua, China

The vanadium-titanium magnetite resources are abundant in the world, with reserves of more than 40 billion tons in the world and 9.83 billion tons in China. Iron in vanadium-titanium magnetite ore mainly occurs in titanomagnetite, and TiO ₂ in the ore mainly occurs in granular ilmenite and titanomagnetite. Generally, about 57% of titanium occurs in titanomagnetite (mFeTiO ₃ ·nFe ₃ O ₄ ), and about 40% of titanium occurs in ilmenite (FeTiO ₃ ). The ore has complex composition and special properties, so the comprehensive utilization of this kind of ore is a major problem that has not been completely solved in the world. The occurrence characteristics of vanadium-titanium magnetite minerals determine that the effective separation of titanium and iron from the source of the ore cannot be achieved by physical beneficiation methods, resulting in low grade iron concentrates (TFe<55 %), the titanium in the iron concentrate completely enters the blast furnace slag (TiO ₂ content is more than 22%) to form a glass body during the ironmaking process, and the TiO ₂ loses its activity and cannot be economically recovered. At the same time, the titanium recovery rate is as low as 18%. Therefore, the use of physical beneficiation methods to separate ilmenite ore greatly reduces the value of titanium and iron alone.

China is the first country in the world to comprehensively extract iron, vanadium and titanium from complex vanadium-titanium magnetite on an industrial scale. , using the usual gravity separation, magnetic separation, flotation and other physical beneficiation methods to separate titanium and iron, the efficiency is low, and it is difficult to select titanium concentrate or iron concentrate with high grade and less impurities; at the same time, TiO ₂ The recovery efficiency is not high. After the vanadium-titanium-magnetite raw ore is separated by ore dressing, about 54% of TiO ₂ enters the iron ore concentrate. After smelting in the blast furnace, almost all of the _{TiO 2 enters} the slag phase, forming a high Slag; In addition, due to the high content of impurities such as S, Si, and Al in the iron concentrate, the above reasons not only lead to low utilization coefficient of smelting blast furnace, high energy consumption, waste of titanium resources, but also large amount of slag and serious environmental pollution.

CN2011100879566 discloses "a method for beneficiating ilmenite", which is a method for obtaining titanium concentrate and iron concentrate by magnetically separating vanadium-titanium magnetite raw ore through grinding, alkali leaching pretreatment, filtration, and regrinding. In this method, the vanadium-titanium magnetite raw ore containing 32.16% iron and 12.11% _TiO2 is processed through grinding, alkali leaching pretreatment, filtration, and magnetic separation after regrinding to form iron concentrate containing 59.30% iron and iron containing TiO ₂ 20.15% titanium concentrate. Since this method is aimed at raw ilmenite ore, which contains high gangue minerals such as SiO ₂ , Al ₂ O ₃ , CaO, and MgO, the alkaline leaching process will preferentially occur on minerals such as SiO ₂ , Al ₂ O ₃ , etc. Alkaline leaching compounds similar to titanium are formed during the alkaline leaching process. The amount of NaOH alkali consumed by alkaline leaching of ilmenite raw ore is 469Kg/t raw ore, which is high in cost; It is very difficult to achieve effective separation of silicon compounds formed after alkali leaching of ore minerals in subsequent magnetic separation, which also restricts the improvement of iron concentrate grade and titanium concentrate grade after alkali leaching of ilmenite raw ore. At the same time, the method uses two grinding processes to change the physical and chemical properties of the mineral surface, which increases the complexity and process cost of the method. In short, the process of this method is complicated, and the alkali consumption is large and the cost is high during the treatment process; at the same time, it is impossible to obtain higher-grade iron ore concentrates and titanium concentrates.

CN201310183580.8 discloses "a method for wet treatment of vanadium-titanium iron concentrate to prepare titanium liquid", and proposes a method for separating ferrotitanium by washing with hydrochloric acid. The invention is a method for wet treatment of vanadium-titanium magnetite concentrate to prepare titanium liquid, including hydrochloric acid leaching of vanadium-titanium magnetite concentrate, molten salt reaction, re-pickling, sulfuric acid acid dissolution, filtration and other processes to obtain titanium liquid. It is aimed at extracting titanium concentrate. The process is complicated. In the process of hydrochloric acid leaching, hydrochloric acid needs to react with iron and vanadium to dissolve into the filtrate, which consumes a large amount of hydrochloric acid and has high cost. At the same time, NaOH is used to react with titanium and silicon in the molten salt process. Consume alkali. In addition, because hydrochloric acid is used in the leaching process of this method, the chloride ions in the hydrochloric acid corrode the equipment greatly, which is not easy for industrial production. The method is mainly applicable to the recovery and utilization of titanium in low-vanadium-depleted titanium magnetite concentrate with high vanadium and low iron content.

CN201410164253.2 discloses a "method for reselecting vanadium-titanium magnetite concentrate by using alkali leaching, pickling, desliming and gravity-magnetism combination". After 5 hours, pickling in H ₂ SO ₄ solution after filtering, then desliming the acid leaching filter cake, adding water to the grit obtained from the desliming operation to make slurry for gravity separation, and then magnetic separation for gravity separation tailings , were obtained TFe content of 63% ~ 69% iron concentrate, TiO ₂ content of 60% ~ 82% titanium concentrate. This method realizes high-efficiency sorting of vanadium-titanium magnetite concentrate, but because alkali leaching is only used in the reaction, the reaction is carried out at a temperature of 280-370°C for 0.5-5 hours, the chemical reaction temperature is high, the time is long, and after the reaction The content of _SiO2 and _TiO2 is as high as 3%, and the content of impurities is high, which reduces the utilization coefficient of the blast furnace and increases the cost of ironmaking; at the same time, the amount of alkali consumed in the inventive method is as high as 100kg/t of concentrate, and the alkali consumption is relatively high. Resource utilization is not high.

Contents of the invention

In order to overcome the deficiencies of the above-mentioned beneficiation methods, the technical problem to be solved by the present invention is to provide a low cost, high recovery quality and efficiency, simple process, and good operability using oxidation based on the effective combination of physical and chemical beneficiation methods. The methods of alkali leaching, pickling, desliming and re-selection of vanadium-titanium magnetite concentrate achieve efficient separation of titanium and iron in vanadium-titanium magnetite concentrate, improve the iron grade before entering the furnace, and reduce the amount of TiO ₂ , The content of impurities such as S, Si, and Al can increase the utilization factor of the blast furnace, reduce the discharge of blast furnace slag, reduce the cost of ironmaking, and at the same time improve the comprehensive utilization rate of _TiO2 resources and reduce environmental pollution.

In order to realize the purpose of the present invention, technical scheme of the present invention is achieved like this:

A method for re-selecting vanadium-titanium magnetite concentrate utilizing oxidative alkali leaching, pickling, desliming and re-magnetization of the present invention is characterized in that it comprises the following steps:

1) Oxidative alkaline leaching

The TFe content ranges from 50% to 55%, the _TiO2 content ranges from 10% to 15%, the _SiO2 content ranges from 3% to 6%, the _Al2O3 content ranges from ₃ % to 6%, and the S content > 0.5%. Vanadium-titanium magnetite concentrate is placed in an alkali solution with a mass concentration of 5% to 52%, and an oxidizing agent is added, and then alkaline leaching reaction is performed at a temperature of 220°C to 330°C for 0.5 to 2 hours, and the reactant is filtered to obtain a filtrate With alkali leaching filter cake A, described filtrate is fed into recovery treatment system;

2) pickling

Add water to the alkali leaching filter cake A in step 1) to make a slurry with a solid-to-liquid mass ratio of 1:1-10, and then place it in a H ₂ SO ₄ solution with a mass concentration of 1%-10%, at 50-90°C pickling under conditions for 5 to 60 minutes, and filtering the pickling reactants to obtain the filtrate and acid leaching filter cake B, and the filtrate is fed into the recovery treatment system;

3) Desliming

Add water to the acid leaching filter cake B in step 2) to prepare a slurry with a mass concentration of 21% to 25%, and use a ∮ 3.0 to 5.0 meter desliming bucket to perform desliming operations to obtain sand settling C and overflow D;

4) Gravity and magnetic re-election

Add water to the grit C in step 3) to make a slurry with a mass concentration of 36% to 41% for gravity separation to obtain gravity concentrate E and gravity tailings F; then add water to the gravity separation tailings F to make mass The slurry with a concentration of 30% to 34% is subjected to magnetic separation to obtain magnetic separation concentrate G and magnetic separation tailings H;

The gravity separation concentrate E and the magnetic separation concentrate G are merged into the final iron concentrate with a TFe content ranging from 64% to 70%, and the magnetic separation tailings H and the overflow D are combined into a _TiO2 content ranging from 60% to 82% of the final titanium concentrate.

The alkaline solution is any one of NaOH aqueous solution, KOH aqueous solution or mixed aqueous solution of NaOH and KOH.

The oxidizing agent is oxygen or H ₂ O ₂ , the amount of oxygen added is 20-120 psi, and the amount of H ₂ O ₂ added is 50-200 kg/t _{of ore} .

The re-election adopts the spiral chute of ￠0.6～￠1.2m for re-election.

The magnetic separation adopts a drum type magnetic separator of 0.12T-0.15T for magnetic separation.

The magnetic separation adopts a 0.03T-0.05T magnetic dehydration tank for magnetic separation.

The magnetic separation adopts a 0.12T-0.15T drum magnetic separator and a 0.03T-0.05T magnetic dehydration tank to carry out two-stage magnetic separation.

The advantages of the present invention are:

The process of oxidative alkali leaching chemically reacts Ti, S, Si, Al and other elements in the vanadium-titanium magnetite concentrate to form corresponding salts, which converts the iron in the vanadium-titanium magnetite concentrate into the form of iron oxide. Different from vanadium-titanium magnetite concentrate, the SiO ₂ content > 20% and Al ₂ O ₃ content > 7% in ilmenite raw ore are much higher than the SiO ₂ content < 6% and Al ₂ O 3 content in vanadium-titanium magnetite concentrate. ₃ content <6%, in the process of alkali leaching ilmenite raw ore, since the alkali leaching process will preferentially occur on SiO ₂ , Al ₂ O ₃ and other minerals, the alkali leaching vanadium-titanium magnetite The amount of raw ore alkali is less, and the introduction of O ₂ oxidizes the S-containing compound, oxidizes FeTiO ₃ , accelerates the reaction, reduces the reaction temperature, shortens the reaction time, and has better effect, greatly reducing energy consumption and equipment investment. For example, when using NaOH oxidation alkali leaching, the amount of alkali consumed by the present invention is less than 90kg/t concentrate, which is more than 5.2 times lower than the amount of alkali consumed by alkali leaching raw ore 469kg/t _{raw ore} . The amount of alkali is reduced by 10kg/t of concentrate; the introduction of O ₂ makes the alkali leaching reaction temperature drop to 220°C, and the reaction time is less than 2 hours.

The pickling process effectively dissolves the oxo acid salts and sulfides such as Ti, Si, Al after alkali leaching, and dissociates them from the iron concentrate. In addition, since the present invention uses sulfuric acid for pickling, the reaction conditions are mild, the equipment is less corroded, the cost is low, and it is more favorable for industrialized production.

The desliming process is classified according to the particle size and specific gravity of the minerals. The titanium compound produced after alkaline leaching has a finer particle size and a smaller specific gravity than the magnetite minerals. The specific gravity of titanium and iron is quite different, realizing the effective separation of titanium and iron.

Coupled with the combination of gravity and magnetic beneficiation, the grade of iron concentrate is increased from 50% to 55% to 64% to 70%. At the same time, the S content in the separated iron concentrate is greatly reduced from more than 0.50% to less than 0.10%. The content of SiO ₂ is reduced from 3% to 6% to less than 1%, the content of Al ₂ O ₃ is reduced from 3% to 6% to less than 1.8%, and the content of TiO ₂ is reduced from more than 12% to less than 6%. At the same time, it can also be obtained Titanium concentrate with a TiO ₂ content of 60% to 82%.

The present invention comprehensively utilizes oxidative alkali leaching, pickling, desliming and gravity-magnetism combined re-selection of vanadium-titanium magnetite concentrate, realizes efficient separation of titanium and iron in vanadium-titanium magnetite concentrate, and reduces TiO ₂ , S, Si, Al entering blast furnace The content of other impurities can increase the utilization factor of blast furnace, reduce the discharge of blast furnace slag, reduce the cost of ironmaking, create better conditions for subsequent smelting, and improve the comprehensive utilization rate of titanium resources.

Description of drawings

Fig. 1 is a process flow diagram of the present invention.

Fig. 2 is the process flow diagram of the present invention adopting two-stage magnetic separation.

Fig. 3 is a process flow diagram of another embodiment of the present invention using two-stage magnetic separation.

Detailed ways

The specific embodiment of the present invention will be further described below in conjunction with accompanying drawing:

Example 1:

As shown in Figure 1.

1) Oxidative alkaline leaching

Put the vanadium-titanium magnetite concentrate with a TFe content of 51.0%, a TiO ₂ content of 14.1%, a SiO ₂ content of 4.57%, an Al ₂ O ₃ content of 4.79%, and a S content of 0.77% in NaOH with a mass concentration of 20%. In the alkaline solution, 22psi of _O2 was introduced, and then the alkali leaching reaction was carried out at a temperature of 230°C for 45 minutes, and the reactant was filtered to obtain the filtrate and the alkali leaching filter cake A, and the NaOH consumption was 53.1 kg/t for the ore. Said filtrate is fed into the recovery treatment system, and its chemical reaction formula is:

4mFeTiO ₃ +8NaOH +mO ₂ 2mFe ₂ O ₃ ↓+4Na ₂ O·(TiO ₂ ) _m ↓+4H ₂ O m≥1

pFe ₃ O ₄ ·q（FeO·TiO ₂ ) +2rNaOH pFe ₃ O ₄ ↓+qFeO↓+ (Na ₂ O) _r ·(TiO ₂ ) _q ↓+rH ₂ O

Al ₂ O ₃ +2NaOH 2NaAlO ₂ + H ₂ O

tSiO ₂ +2NaOH Na ₂ O·(SiO ₂ ) _t ↓+ H ₂ O

3FeS ₂ +6NaOH 3FeS↓+Na2SO3 _{+ 2Na2S + 3H2O}

4FeS ₂ + 11O ₂ 2Fe ₂ O ₃ + 8SO ₂

4FeO+O ₂ 2Fe ₂ O ₃

2SO ₂ +O ₂ +4NaOH 2Na ₂ SO ₄ + 2H ₂ O

2) pickling

Add water to the alkali leaching filter cake A in step 1) to make a slurry with a mass solid-to-liquid ratio of 1: ₂ , then place it in a _H2SO4 solution with a mass concentration of 3%, pickle at 75°C for 10 minutes, and remove the acid Wash reactant and filter, get filtrate and acid leaching filter cake B, described filtrate is fed into recovery treatment system, and its chemical reaction formula is:

Na ₂ O·(TiO ₂ ) _x +H ⁺ (H ₂ O)·(TiO ₂ ) _x ↓+Na ⁺

Na ₂ O·(SiO ₂ ) _t +H ⁺ (H ₂ O)·(SiO ₂ ) _t ↓+Na ⁺

NaAlO ₂ +4H ⁺ Al ³⁺ +Na ⁺ +2H ₂ O

3) Desliming

Add water to the acid leaching filter cake B in step 2) to prepare a slurry with a mass concentration of 22%, and use a ∮3.0m desliming bucket to perform desliming operations to obtain sand settling C and overflow D;

4) Gravity and magnetic re-election

Add water to the grit C in step 3) to make a slurry with a mass concentration of 37%, and put it into a ￠1.2-meter spiral chute for gravity separation to obtain gravity separation concentrate E and gravity separation tailings F;

Add water to the gravity separation tailings F to prepare a slurry with a mass concentration of 32% and feed it into a 0.15T drum magnetic separator for magnetic separation to obtain magnetic separation concentrate G and magnetic separation tailings H;

The gravity separation concentrate E and the magnetic separation concentrate G are combined into a final iron concentrate with a TFe content of 64.1%, wherein the _SiO2 content is 0.94 _% , the _Al2O3 content is 1.27%, and the S content is 0.02% ; The magnetic separation tailings H and the overflow D are merged into TiO ₂ content of 61.8% titanium concentrate.

Example 2:

As shown in Figure 1.

1) Oxidative alkaline leaching

The vanadium-titanium magnetite concentrate with a TFe content of 51.6%, a TiO ₂ content of 13.9%, a SiO ₂ content of 4.35%, an Al ₂ O ₃ content of 4.33%, and a S content of 0.57% was placed in NaOH with a mass concentration of 27%. In the alkaline solution, 75psi of _O2 was introduced, and then the alkaline leaching reaction was carried out at a temperature of 315°C for 1.0 hour, and the reactant was filtered to obtain the filtrate and the alkaline leaching filter cake A, and the NaOH consumption was 83.4 kg/t for the ore. Described filtrate is given into recovery treatment system, and its chemical reaction formula is with embodiment 1;

2) pickling

Add water to the alkali leaching filter cake A in step 1) to make a slurry with a mass solid-to-liquid ratio of 1:4, then place it in a H ₂ SO ₄ solution with a mass concentration of 5%, pickle it at 80°C for 60 minutes, and remove the acid Wash reactant and filter, get filtrate and acid leaching filter cake B, described filtrate is fed into recovery treatment system, and its chemical reaction formula is with embodiment 1;

3) Desliming

Add water to the filtered ilmenite concentrate B in step 2) to prepare a slurry with a mass concentration of 21%, and use a ∮5.0m desliming hopper to perform desliming operations to obtain sand settling C and overflow D;

4) Gravity and magnetic re-election

Add water to the grit C in step 3) to prepare a slurry with a mass concentration of 36%, and feed it into a 0.6-meter spiral chute for gravity separation to obtain gravity concentration ore E and gravity separation tailings F;

Then add water to the gravity separation tailings F to prepare a slurry with a mass concentration of 33% and feed it into a 0.12T drum magnetic separator for magnetic separation to obtain magnetic separation concentrate G and magnetic separation tailings H;

The gravity separation concentrate E and the magnetic separation concentrate G are combined into a final iron concentrate with a TFe content of 69.9%, wherein the _SiO2 content is 0.31 _% , the _Al2O3 content is 0.27%, and the S content is 0.01%; The magnetic separation tailings H and the overflow D are combined into a titanium concentrate with a _TiO content of 65.2%.

Example 3:

As shown in Figure 1.

1) Oxidative alkaline leaching

The vanadium-titanium magnetite concentrate with a TFe content of 52.6%, a TiO ₂ content of 12.2%, a SiO ₂ content of 3.35%, an Al ₂ O ₃ content of 5.37%, and a S content of 0.71% was placed in NaOH with a mass concentration of 33%. In the alkaline solution, add 59kg/t of H ₂ O _{2 fed to the ore} , and then perform alkaline leaching reaction at a temperature of 255°C for 1.5 hours, and filter the reactant to obtain the filtrate and alkaline leaching filter cake A, and the NaOH consumption is 85.5 kg/ t feeds the ore, and the described filtrate is fed into the recovery treatment system, and its chemical reaction formula is:

2mFeTiO ₃ +4NaOH+mH ₂ O ₂ mFe ₂ O ₃ ↓+2Na ₂ O·(TiO ₂ ) _m ↓+(m+2)H ₂ O m≥1

pFe ₃ O ₄ ·q（FeO·TiO ₂ ) +2rNaOH pFe ₃ O ₄ ↓+qFeO↓+ (Na ₂ O) _r ·(TiO ₂ ) _q ↓+rH ₂ O

Al ₂ O ₃ +2NaOH 2NaAlO ₂ + H ₂ O

tSiO ₂ +2NaOH Na ₂ O·(SiO ₂ ) _t ↓+ H ₂ O

3FeS ₂ +6NaOH 3FeS↓+Na2SO3 _{+ 2Na2S + 3H2O}

2FeS ₂ + 11H ₂ O ₂ Fe ₂ O ₃ +4SO ₂ + 11H ₂ O

2FeO+H ₂ O ₂ Fe ₂ O ₃ + H ₂ O

SO ₂ +H ₂ O ₂ +2NaOH Na ₂ SO ₄ + 2H ₂ O

2) pickling

Add water to the alkali leaching filter cake A in step 1) to make a pulp with a mass solid-to-liquid ratio of 1:3.2, then place it in a H ₂ SO ₄ solution with a mass concentration of 7.5%, pickle it at 50°C for 55 minutes, and remove the acid Wash reactant and filter, get filtrate and acid leaching filter cake B, described filtrate is fed into recovery treatment system, and its chemical reaction formula is with embodiment 1;

3) Desliming

Add water to the filtered ilmenite concentrate B in step 2) to prepare a slurry with a mass concentration of 24%, and use a ∮5.0-meter desliming bucket to perform desliming operations to obtain sand settling C and overflow D;

4) Gravity and magnetic re-election

Add water to the grit C in step 3) to prepare a slurry with a mass concentration of 41%, and put it into a 0.9-meter spiral chute for gravity separation to obtain gravity separation concentrate E and gravity separation tailings F;

Then add water to the gravity separation tailings F to prepare a slurry with a mass concentration of 31%, and give it to a magnetic dehydration tank with an entry field strength of 0.03T for magnetic separation to obtain magnetic separation concentrate G and magnetic separation tailings H;

The gravity separation concentrate E and the magnetic separation concentrate G are combined into a final iron concentrate with a TFe content of 66.2%, wherein the _SiO2 content is 0.55 _% , the _Al2O3 content is 0.91%, and the S content is 0.02%. The magnetic separation tailings H and the overflow D are combined into a titanium concentrate with a _TiO content of 63.2%.

Example 4:

As shown in Figure 1.

1) Oxidative alkaline leaching

The vanadium-titanium magnetite concentrate with a TFe content of 53.7%, a TiO ₂ content of 11.8%, a SiO ₂ content of 4.15%, an Al ₂ O ₃ content of 4.98%, and a S content of 0.69% was placed in NaOH with a mass concentration of 40%. In the alkaline solution, 105 psi of O ₂ was introduced, and then the alkaline leaching reaction was carried out at 280°C for 2.0 hours, and the reactant was filtered to obtain the filtrate and the alkaline leaching filter cake A, and the NaOH consumption was 88.6 kg/t for the ore. Described filtrate is given into recovery treatment system, and its chemical reaction formula is with embodiment 1;

2) pickling

Add water to the alkali leaching filter cake A in step 1) to make a slurry with a mass solid-to-liquid ratio of 1: ₆ , then place it in a _H2SO4 solution with a mass concentration of 6.5%, pickle at 70°C for 25 minutes, and remove the acid Wash reactant and filter, get filtrate and acid leaching filter cake B, described filtrate is fed into recovery treatment system, and its chemical reaction formula is with embodiment 1;

3) Desliming

Add water to the filtered ilmenite concentrate B in step 2) to make a slurry with a mass concentration of 24%, and use a ∮3.0m desliming bucket to perform desliming operations to obtain sand settling C and overflow D;

4) Gravity and magnetic re-election

Add water to the grit C in step 3) to prepare a slurry with a mass concentration of 40% and put it into a ￠1.2m spiral chute for gravity separation to obtain gravity concentrate E and gravity tailings F; Add water to form an ore slurry with a mass concentration of 30%, and conduct magnetic separation in a magnetic dehydration tank with an entry field strength of 0.05T to obtain magnetic separation concentrate G and magnetic separation tailings H;

The gravity separation concentrate E and the magnetic separation concentrate G are combined into a final iron concentrate with a TFe content of 67.0%, wherein the _SiO2 content is 0.62 _% , the _Al2O3 content is 0.71%, and the S content is 0.01%; The magnetic separation tailings H and the overflow D are combined into a titanium concentrate with a _TiO2 content of 71.3%.

Example 5:

as shown in picture 2.

1) Oxidative alkaline leaching

The vanadium-titanium magnetite concentrate with a TFe content of 54.1%, a TiO ₂ content of 11.2%, a SiO ₂ content of 3.89%, an Al ₂ O ₃ content of 5.05%, and a S content of 0.72% was placed in KOH with a mass concentration of 25%. In the alkaline solution, 120psi of O ₂ was introduced, and then the alkali leaching reaction was carried out at 220°C for 2.0 hours, and the reactant was filtered to obtain the filtrate and the alkali leaching filter cake A, and the KOH consumption was 87.8 kg/t for the ore. Said filtrate is fed into the recovery treatment system, and its chemical reaction formula is:

4mFeTiO ₃ +8KOH+mO ₂ 2mFe ₂ O ₃ ↓+4K ₂ O·(TiO ₂ ) _m ↓+4H ₂ O m≥1

pFe ₃ O ₄ ·q（FeO·TiO ₂ ) +2rKOH pFe ₃ O ₄ ↓+qFeO↓+ (K ₂ O) _r ·(TiO ₂ ) _q ↓+rH ₂ O

Al ₂ O ₃ +2KOH 2KAlO ₂ + H ₂ O

tSiO ₂ +2KOH K ₂ O·(SiO ₂ ) _t ↓+ H ₂ O

3FeS ₂ +6KOH 3FeS↓+K ₂ SO ₃ +2K ₂ S+3H ₂ O

4FeS ₂ + 11O ₂ 2Fe ₂ O ₃ + 8SO ₂

4FeO+O ₂ 2Fe ₂ O ₃

2SO ₂ +O ₂ +4KOH 2K ₂ SO ₄ + 2H ₂ O

2) pickling

Add water to the alkali leaching filter cake A in step 1) to make a slurry with a mass solid-to-liquid ratio of 1:8.3, then place it in a _H2SO4 solution with a mass concentration of ₅ %, pickle it at 85°C for 30 minutes, and remove the acid Wash reactant and filter, get filtrate and acid leaching filter cake B, described filtrate is fed into recovery treatment system, and its chemical reaction formula is:

K ₂ O·(TiO ₂ ) _x +H ⁺ (H ₂ O)·(TiO ₂ ) _x ↓+ K ⁺

K ₂ O·(SiO ₂ )t+H+ (H ₂ O)·(SiO ₂ ) t↓+ K +

KAlO ₂ +4H+ Al3+ +K++2H ₂ O

3) Desliming

Add water to the filtered ilmenite concentrate B in step 2) to prepare a slurry with a mass concentration of 23%, and use a ∮5.0-meter desliming bucket to perform desliming operations to obtain grit C and overflow D;

4) Gravity and magnetic re-election

Add water to the grit C in step 3) to prepare a slurry with a mass concentration of 41%, and put it into a 0.6-meter spiral chute for gravity separation to obtain gravity concentrate E and gravity tailings F; Add water to form an ore slurry with a mass concentration of 33%, and conduct a stage of magnetic separation on a drum magnetic separator with an entry field strength of 0.12T to obtain a stage of magnetic separation concentrate G1 and a stage of magnetic separation tailings H1; then a stage of magnetic separation with a concentration of 32% Concentrate G1 uses a magnetic dehydration tank with a field strength of 0.03T to carry out the second-stage magnetic separation to obtain the second-stage magnetic separation concentrate G2 and the second-stage magnetic separation tailings H2;

The gravity separation concentrate E and the magnetic separation concentrate G2 are merged into a final iron concentrate with a TFe content of 68.7%, wherein the _SiO2 content is 0.30 _% , the _Al2O3 content is 0.34%, and the S content is 0.01%; The magnetic separation tailings H1 and H2 are merged into the final tailings, and the overflow D is the final titanium concentrate with a _TiO2 content of 81.8%.

Embodiment 6:

As shown in Figure 3.

1) Oxidative alkaline leaching

The vanadium-titanium magnetite concentrate with a TFe content of 50.7%, a TiO ₂ content of 14.5%, a SiO ₂ content of 4.38%, an Al ₂ O ₃ content of 4.96%, and a S content of 0.81% was placed in KOH with a mass concentration of 10%. In the alkaline solution, add 102kg/t of H ₂ O _{2 to the ore} , and then perform alkaline leaching reaction at a temperature of 295°C for 1.0 hour, and filter the reactant to obtain the filtrate and alkaline leaching filter cake A, and the KOH consumption is 78.6kg/ t feeds the ore, and the described filtrate is fed into the recovery treatment system, and its chemical reaction formula is:

2mFeTiO ₃ +4KOH+mH ₂ O ₂ mFe ₂ O ₃ ↓+2K ₂ O·(TiO ₂ ) _m ↓+(m+2)H ₂ O m≥1

pFe ₃ O ₄ ·q（FeO·TiO ₂ ) +2rKOH pFe ₃ O ₄ ↓+qFeO↓+ (K ₂ O) _r ·(TiO ₂ ) _q ↓+rH ₂ O

Al ₂ O ₃ +2KOH 2KAlO ₂ + H ₂ O

tSiO ₂ +2KOH K ₂ O·(SiO ₂ ) _t ↓+ H ₂ O

3FeS ₂ +6KOH 3FeS↓+K ₂ SO ₃ +2K ₂ S+3H ₂ O

2FeS ₂ + 11H ₂ O ₂ Fe ₂ O ₃ +4SO ₂ + 11H ₂ O

2FeO+H ₂ O ₂ Fe ₂ O ₃ + H ₂ O

SO ₂ +H ₂ O ₂ +2KOH K ₂ SO ₄ + 2H ₂ O

2) pickling

Add water to the alkali leaching filter cake A in step 1) to make a pulp with a mass solid-to-liquid ratio of 1:9, then place it in an ₈ % _H2SO4 solution, pickle at 60°C for 35 minutes, and remove the acid Wash reactant and filter, get filtrate and acid leaching filter cake B, described filtrate is fed into recovery treatment system, and its chemical reaction formula is with embodiment 5;

3) Desliming

Add water to the filtered ilmenite concentrate B in step 2) to prepare a slurry with a mass concentration of 23%, and use a ∮ 3.0-meter desliming hopper to perform desliming operations to obtain sand settling C and overflow D;

4) Gravity and magnetic re-election

Add water to the grit C in step 3) to prepare a slurry with a mass concentration of 37% and put it into a ￠0.9-meter spiral chute for gravity separation to obtain gravity concentrate E and gravity tailings F; Add water to form a pulp with a mass concentration of 32% and use a magnetic dehydration tank with a field strength of 0.05T to perform a stage of magnetic separation to obtain a stage of magnetic separation concentrate G1 and a stage of magnetic separation tailings H1; G1 conducts the second-stage magnetic separation to the drum magnetic separator with an entrance field strength of 0.15T, and obtains the second-stage magnetic separation concentrate G2 and the second-stage magnetic separation tailings H2;

The gravity separation concentrate E and the magnetic separation concentrate G2 are merged into a final iron concentrate with a TFe content of 65.5%, wherein the _SiO2 content is 0.42 _% , the _Al2O3 content is 0.27%, and the S content is 0.01%; The magnetic separation tailings H1 and H2 are merged into the final tailings, and the overflow D is the final titanium concentrate with a _TiO2 content of 67.1%.

Embodiment 7:

As shown in Figure 3.

1) Oxidative alkaline leaching

The content of TFe is 52.1%, the content of TiO ₂ is 13.0%, the content of SiO ₂ is 4.26%, the content of Al ₂ O ₃ is 4.85%, and the vanadium-titanium magnetite concentrate with S content of 0.84% is placed in NaOH mass concentration of 22% and Into the mixed alkaline solution with KOH mass concentration of 5%, 89psi of O ₂ was introduced, and then the alkali leaching reaction was carried out at 260°C for 75 minutes, and the reactant was filtered to obtain the filtrate and alkali leaching filter cake A, NaOH consumption 32.6kg/t ore feeding, KOH consumption 49.3 kg/t ore feeding, the filtrate is fed into the recovery treatment system, and its chemical reaction formula is the same as that of embodiment 1 and embodiment 5;

2) pickling

Add water to the alkali leaching filter cake A in step 1) to make a pulp with a mass solid-to-liquid ratio of ₁ :9, then place it in a _H2SO4 solution with a mass concentration of 9%, pickle at 90°C for 20 minutes, and remove the acid Wash reactant and filter, get filtrate and acid leaching filter cake B, described filtrate is fed into recovery treatment system, and its chemical reaction formula is with embodiment 1 and embodiment 5;

3) Desliming

Add water to the filtered ilmenite concentrate B in step 2) to prepare a slurry with a mass concentration of 22%, and use a ∮ 3.0-meter desliming bucket to perform desliming operations to obtain grit C and overflow D;

4) Gravity and magnetic re-election

Add water to the grit C in step 3) to prepare a pulp with a mass concentration of 40% and put it into a 0.9-meter spiral chute for gravity separation to obtain gravity concentrate E and gravity tailings F; Add water to form a pulp with a mass concentration of 31%. Use a magnetic dehydration tank with a field strength of 0.05T to perform a stage of magnetic separation to obtain a stage of magnetic separation concentrate G1 and a stage of magnetic separation tailings H1; G1 conducts the second-stage magnetic separation to the drum magnetic separator with an entrance field strength of 0.15T, and obtains the second-stage magnetic separation concentrate G2 and the second-stage magnetic separation tailings H2;

The gravity separation concentrate E and the magnetic separation concentrate G2 are merged into a final iron concentrate with a TFe content of 66.4%, wherein the _SiO2 content is 0.45 _% , the _Al2O3 content is 0.29%, and the S content is 0.01%; The magnetic separation tailings H1 and H2 are merged into the final tailings, and the overflow D is the final titanium concentrate with a _TiO2 content of 68.2%.

Embodiment 8:

As shown in Figure 3.

1) Oxidative alkaline leaching

The vanadium-titanium magnetite concentrate with TFe content of 52.6%, _TiO2 content of 12.7%, _SiO2 content of 4.46%, _Al2O3 content of 5.05%, and S content of 0.74% was placed in _NaOH mass concentration of 20% and Add _192kg /t of H ₂ O ₂ to the mixed alkali solution with a KOH mass concentration of 6%, and then perform an alkali leaching reaction at a temperature of 265°C for 70 minutes, and filter the reactant to obtain a filtrate and an alkali leaching filter cake A, NaOH consumption 30.6kg/t feeds ore, KOH consumption 46.8kg/t feeds ore, and described filtrate is fed into recovery treatment system, and its chemical reaction formula is the same as embodiment 3 and embodiment 6;

2) pickling

Add water to the alkali leaching filter cake A in step 1) to make a slurry with a mass solid-to-liquid ratio of ₁ :8.5, then place it in a _H2SO4 solution with a mass concentration of 9.5%, pickle it at 80°C for 30 minutes, and remove the acid Wash reactant and filter, get filtrate and acid leaching filter cake B, described filtrate is fed into recovery treatment system, and its chemical reaction formula is with embodiment 1 and embodiment 5;

3) Desliming

Add water to the filtered ilmenite concentrate B in step 2) to prepare a slurry with a mass concentration of 22%, and use a ∮ 3.0-meter desliming bucket to perform desliming operations to obtain grit C and overflow D;

4) Gravity and magnetic separation

Add water to the grit C in step 3) to prepare a pulp with a mass concentration of 40% and put it into a 0.9-meter spiral chute for gravity separation to obtain gravity concentrate E and gravity tailings F; Add water to form a pulp with a mass concentration of 31%. Use a magnetic dehydration tank with a field strength of 0.05T to perform a stage of magnetic separation to obtain a stage of magnetic separation concentrate G1 and a stage of magnetic separation tailings H1; G1 conducts the second-stage magnetic separation to the drum magnetic separator with an entrance field strength of 0.15T, and obtains the second-stage magnetic separation concentrate G2 and the second-stage magnetic separation tailings H2;

The gravity separation concentrate E and the magnetic separation concentrate G2 are combined into a final iron concentrate with a TFe content of 67.2%, wherein the _SiO2 content is 0.47 _% , the _Al2O3 content is 0.89%, and the S content is 0.01%; The magnetic separation tailings H1 and H2 are merged into the final tailings, and the overflow D is the final titanium concentrate with a _TiO2 content 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.