CN116081685A - Acidolysis method in hydrochloric acid titanium dioxide industrial production flow of high-phosphorus titanium concentrate - Google Patents
Acidolysis method in hydrochloric acid titanium dioxide industrial production flow of high-phosphorus titanium concentrate Download PDFInfo
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01G—COMPOUNDS CONTAINING METALS NOT COVERED BY SUBCLASSES C01D OR C01F
- C01G23/00—Compounds of titanium
- C01G23/04—Oxides; Hydroxides
- C01G23/047—Titanium dioxide
- C01G23/053—Producing by wet processes, e.g. hydrolysing titanium salts
- C01G23/0536—Producing by wet processes, e.g. hydrolysing titanium salts by hydrolysing chloride-containing salts
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01G—COMPOUNDS CONTAINING METALS NOT COVERED BY SUBCLASSES C01D OR C01F
- C01G23/00—Compounds of titanium
- C01G23/02—Halides of titanium
- C01G23/022—Titanium tetrachloride
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- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P10/00—Technologies related to metal processing
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Abstract
The invention discloses an acidolysis method in an industrial production flow of titanium dioxide by a hydrochloric acid method of high-phosphorus titanium concentrate, which can ensure industrial production of an acidolysis process system of titanium dioxide by the hydrochloric acid method, is corresponding to other titanium dioxide production methods, remarkably improves acidolysis rate of titanium concentrate, improves concentration of titanium liquid, does not produce low-concentration titanium liquid in the whole acidolysis process, reduces the consumption of hydrochloric acid, improves efficiency of reduced iron powder and stability of acidolysis titanium liquid, has obvious dephosphorization effect, and is beneficial to preparing high-quality pigment titanium dioxide.
Description
Technical Field
The invention relates to the technical field of titanium dioxide and titanium dioxide production, in particular to an acidolysis method in a hydrochloric acid method titanium dioxide industrial production flow of high-phosphorus titanium concentrate.
Background
Titanium dioxide is the best white pigment in the world at present, is widely applied to the industrial fields of paint, plastics, paper making, rubber, printing ink, chemical fiber, electronics, ceramics and the like, is the most important inorganic chemical product, and the sales value of the titanium dioxide is the third position of the sales value of the inorganic chemical product in the world. Therefore, the average consumption of titanium dioxide can relatively measure the living standard and the industrial level of people in one country.
Currently, the mature technology of titanium dioxide industrialized production in the world is a sulfuric acid method and a chlorination method. The sulfuric acid process titanium dioxide is produced by acidolysis of titanium concentrate or titanium slag with sulfuric acid to produce titanyl sulfate solution, and the titanyl sulfate solution is treated by the processes of ferric iron reduction by iron powder, ferrous iron removal by freezing crystallization, hydrolysis, filtration and washing, bleaching and reduction, salt treatment, drying, calcination, post-treatment and the like to obtain the sulfuric acid process titanium dioxide. The method has the advantages of easily obtained ore sources, mature process technology, long process flow, high consumption of sulfuric acid and water, great difficulty in fully utilizing the byproduct ferrous sulfate, difficult waste acid and wastewater treatment, large environmental pollution and higher comprehensive cost at the present stage. The production of titanium dioxide in China is mainly based on a sulfuric acid method. Production of titanium dioxide by a chlorination method: the titanium tetrachloride is prepared by using chlorine and petroleum coke through boiling chlorination or fused salt chlorination of rutile ore or high titanium slag, and then the titanium tetrachloride is subjected to refining, gas phase oxidation, post-treatment and other processes to obtain the titanium dioxide by the chlorination process. The advantages are that: short flow and high product quality. Disadvantages: the raw materials are controlled, the high-temperature chlorination and high-temperature oxidation have high requirements on the process manufacturing of equipment, the equipment structure is complex, and the investment is large. Because chlorine is adopted as a main raw material, the safety production risk is high. The waste water and waste acid are produced in large quantity and are difficult to treat. The developed nations abroad mainly use the titanium white production of the chloride process, and at present, the titanium white industry of the chloride process in China only has a few enterprises such as the Dragon boa Baili Union and the China Xin titanium industry and the like to produce a small amount of titanium white.
The production process of the titanium dioxide by the hydrochloric acid method is explored for decades, and some research results are presented, but the industrial requirements are not met in practice. The titanium pigment is produced by acidolysis of titanium concentrate or titanium slag with hydrochloric acid to produce titanium liquid. The following process is divided into two routes: the titanium dioxide powder is prepared by the processes of ferric iron removal through iron powder reduction, concentration, ferrous chloride removal through freezing crystallization, hydrolysis, filtering and washing, drying, calcination, post-treatment and the like; secondly, extracting and separating Ti 4+ And Fe (Fe) 2+ 、Fe 3+ 、Ca 2+ 、Mg 2+ Equi-metallicAnd (3) carrying out processes such as hydrolysis (or spray heating hydrolysis), filtering, washing, drying, calcining, post-treatment and the like on the refined titanium liquid to obtain the titanium pigment by the hydrochloric acid method. Two main preparation processes of titanium dioxide by the global hydrochloric acid method are as follows: the US ANI process (main patent US 6440383) and the canadian CTL process (main patent CA 2513309) target the extraction of elemental titanium. There are also some reports of achieving an effective separation of titanium element by extracting each metal element. However, the existing production process of titanium dioxide by a hydrochloric acid method is still not mature, the acidolysis rate and the concentration of titanium concentrate are not high, the stability of titanium concentrate is low, the extraction efficiency is low, the separation effect of an extractant is poor, pigment titanium white is difficult to produce, the recycling of hydrochloric acid is not thorough, the solid waste cannot be comprehensively utilized, and the environmental protection problem is not completely solved. Only the technology and technology corporation of Fujian Kunzhong color materials reported at present adopts the hydrochloric acid extraction process to produce the pearlite pigment of the titanium dioxide.
Disclosure of Invention
The invention mainly solves the technical problem of providing the acidolysis method in the industrial production flow of the titanium dioxide by the hydrochloric acid method of the high-phosphorus titanium concentrate, which can ensure the industrial production of the acidolysis process system of the titanium dioxide by the hydrochloric acid method, is corresponding to other production methods of titanium dioxide, obviously improves the acidolysis rate of the titanium concentrate, improves the concentration of titanium liquid, does not produce low-concentration titanium liquid in the whole acidolysis process, reduces the consumption of hydrochloric acid, improves the efficiency of reduced iron powder and the stability of acidolysis titanium liquid, has obvious dephosphorization effect, and is beneficial to preparing high-quality pigment titanium dioxide.
In order to solve the technical problems, the invention adopts the following technical scheme: an acidolysis method in the industrial production flow of titanium dioxide powder by a hydrochloric acid method of high-phosphorus titanium concentrate comprises the following steps: (1) The raw material of the acid leaching titanium concentrate is titanium concentrate powder subjected to preactivation grinding; (2) Acid hydrolysis acid is prepared from filter cakes formed by regenerated acid washing, acid leaching and filtering, and Ti in filter cakes 4+ All are transferred into acidolysis acid; adding the titanium concentrate fine powder after preactivation grinding, stirring and mixing, and performing preliminary acidolysis to further improve Ti 4+ Concentration; (3) Ti existing in the normal temperature ore mixing stage 4+ When iron powder, ti is added 4+ Reduction to Ti 3+ To realize that Ti always exists in acidolysis process 3+ ，Fe 3+ Immediately reduced by iron powder to Fe 2+ Realizing a reduction acidolysis system; (4) Introducing hydrogen chloride gas, heating the system to 88-95 ℃ by utilizing the dissolution heat of the hydrogen chloride gas, maintaining the acidolysis temperature of the system, increasing the acidity of the system, stirring for reaction, maintaining the concentration of free hydrochloric acid in an acidolysis kettle to be more than 270g/L, (5) adding a dephosphorization flocculation complexing agent into acidolysis slurry at 88-95 ℃ for high-temperature electric neutralization-adsorption bridging dephosphorization reaction, flocculating phosphorus-containing polymer colloid, titanium dioxide colloid and orthosilicic acid colloid 0.4-0.6 hour before acidolysis reaction is ended; and (3) after the temperature is reduced to 83-86 ℃, discharging, directly performing hot filtration, performing solid-liquid separation to obtain acidolysis solution, and washing a filter cake by using regenerated acid produced by a chloride roasting system to prepare acidolysis acid.
According to the characteristic of mineral mosaic of raw materials of titanium concentrate, the titanium concentrate fine materials subjected to activation grinding by a vertical mill and a stirring mill are fed into an acidolysis system, and the activated titanium concentrate has the characteristics of easy acidolysis of each group of titanium concentrate with good dissociability and high powder surface energy, and the granularity is controlled to be D max < 38 μm (400 mesh).
Washing acidolysis filter cake formed by acidolysis filtering by using regenerated acid produced by chloride salt roasting system to prepare acidolysis acid, and Ti in filter cake 4+ All the titanium dioxide is transferred into acidolysis acid, and compared with the known process, the whole production process does not generate low-concentration titanium liquid (commonly known as small-scale water in industry);
adding acidolysis acid (concentration is 28-30wt%) into acidolysis kettle according to a certain ore-acid ratio (mass-volume ratio), then adding activated titanium concentrate, mixing ore at normal temperature.
In addition to the patent application, other patent and literature reports and production processes for preparing titanium dioxide by a hydrochloric acid method and preparing titanium dioxide by a sulfuric acid method are that after acidolysis reaction is finished, iron powder is added to reduce Fe 3+ Is Fe 2+ The main reaction process is as follows: 2Fe 3+ +Fe→2Fe 2+ Part of Ti 4+ +Fe→Ti 3+ +Fe 2+ To ensure Fe in solution 3+ Is totally reduced to Fe 2+ . Because the acidity is lower after acidolysis is finished, the stability of the titanium liquid is reduced, the iron powder is easy to be coated by metatitanic acid colloid generated by early hydrolysis in the reduction process in the prior process steps, the reduction rate is slow and incomplete, the iron powder consumption is high,the stability of the titanium liquid is poor. The invention adopts Ti existing in the normal temperature ore mixing stage 4+ When iron powder, ti is added 4+ Reduction to Ti 3+ To maintain Ti always existing in acidolysis process 3+ Realizing a reductive acidolysis system, and Fe generated in the full acidolysis process 3+ Is instantly reduced to Fe 2+ . The innovation of acidolysis into a reduction system is as follows: the main reaction process is as follows: ti (Ti) 4+ +Fe→Ti 3+ +Fe 2+ ，Fe 3+ +Ti 3+ →Fe 2+ +Ti 4+ . According to the simultaneous equilibrium principle, the acidolysis reaction FeO.TiO is facilitated 2 +6HCl+2H 2 O→FeCl 2 +TiCl 4 ·5H 2 O and Fe 2 O 3 +6HCl→2FeCl 3 +3H 2 O is carried out, so that the acidolysis rate and acidolysis rate are improved, and Fe is ensured 3+ Improves the utilization rate of iron powder and avoids Fe in a hydrochloric acid system 3+ And the titanium-phosphorus-titanium complex compound is complexed with phosphorus and titanium to form colloid which influences the filtering performance and stability of the titanium liquid, so that the early hydrolysis of the titanium liquid is avoided, and the stability of the titanium liquid is improved.
Introducing hydrogen chloride gas generated by hydrochloric acid resolving or chloride roasting system, heating the system to 88-95 ℃ by utilizing the dissolution heat of the hydrogen chloride gas, maintaining the acidolysis temperature of the system, increasing the acidity of the system, and stirring and reacting for 1.5 hours. In the reaction, the concentration of free hydrochloric acid in the acidolysis kettle is maintained to be more than 270g/L, which is helpful for direct thermal filtration of acidolysis slurry without sedimentation.
And adding the dephosphorization flocculation complexing agent into the acidolysis slurry at 88-95 ℃ 0.4-0.6 hours before the acidolysis reaction is terminated, realizing the electric neutralization-adsorption bridging dephosphorization reaction at a high temperature state, and achieving the purpose of flocculating the phosphorus-containing polymer colloid, the titanium dioxide colloid and the orthosilicate colloid. And (3) after the temperature is reduced to 83-86 ℃, discharging, directly performing hot filtration, performing solid-liquid separation to obtain acidolysis solution, and washing a filter cake by using regenerated acid produced by a chloride roasting system to prepare acidolysis acid. The dephosphorization flocculation complexing agent is formed by compounding ultra-high molecular weight cationic polyacrylamide and an inorganic-organic compound dephosphorization agent, and comprises the following components in parts by weight: 20-80 parts of cationic polyacrylamide and 20-80 parts of special inorganic-organic composite dephosphorizing agent. AcidolysisThe dosage of the dephosphorization flocculation complexing agent in the liquid is 80-100 g/m 3 . The inorganic-organic composite dephosphorizing agent is formed by compounding polymeric ferric sulfate, PDMDAAC homopolymer and copolymer and chitin.
The beneficial effects of the invention are as follows:
the acidolysis rate of the titanium concentrate is more than 95%;
the titanium liquid concentration can reach as high as Ti 4+ ：200g/L；
The stability of the titanium liquid is more than 500;
deep dephosphorization of acidolysis slurry, wherein P in the titanium liquid is less than 30ppm, and high-quality titanium liquid of a high-grade rutile titanium white pigment precursor is produced by subsequent seed crystal hydrolysis;
deep dephosphorization of acidolysis slurry, and guarantee of FeCl of subsequent freezing crystallization 2 ·4H 2 P in O is less than 10ppm, and high-quality ferric oxide powder can be produced through a chloride roasting system;
due to the adoption of Ti-containing alloy 4+ The hydrochloric acid solution is taken as acidolysis acid, and low-concentration titanium liquid (commonly known as small-scale water in industry) is not generated in the whole production process;
the H of acidolysis acid is reduced by the introduction of hydrogen chloride gas generated by hydrochloric acid analysis or a chloride salt roasting system + The concentration requirement is that the concentration of free hydrochloric acid in an acidolysis pot is maintained to be more than 270g/L, which is helpful for direct thermal filtration of acidolysis slurry without sedimentation;
the invention lays a foundation for the industrial production of titanium dioxide by a hydrochloric acid method, and the production line is being constructed.
The specific embodiment is as follows:
the following detailed description of the preferred embodiments of the invention is provided to enable those skilled in the art to more readily understand the advantages and features of the invention and to make a clear and concise definition of the scope of the invention.
The embodiment of the invention comprises the following steps:
an acidolysis method in the industrial production flow of titanium dioxide by hydrochloric acid method of high-phosphorus titanium concentrate, which aims to solve the problems that titanium concentrate acidolysis rate and titanium liquid concentration are low, iron powder consumption and acid consumption are high, titanium liquid stability is low, titanium white pigment is difficult to produce due to poor quality of titanium liquid in the existing production process of titanium dioxide by hydrochloric acid method, and the like.
Example 1
In the embodiment, the titanium concentrate is Panzhihua titanium concentrate, and the TiO 2 The content of FeO is 46.1%, the content of Fe is 36.0%, fe 2 O 3 The content is 5.15%, the P content is 0.047%, and D max Less than or equal to 150 mu m (100 meshes). Pre-activating and grinding the titanium concentrate powder by a vertical mill to obtain acidolysis titanium concentrate fine powder with the granularity of D 98 ＜36μm，D max < 38 μm (400 mesh).
700L acidolysis acid (HCl: 320.34g/L, ti) 4+ (in TiO) 2 Meter): 27.52g/L, fe 2+ :16.98 g/L) was added to a closed volume of 1m 3 And stirring is started, and then 280kg of titanium concentrate fine materials are added into the acidolysis reaction kettle to be stirred and mixed. Mineral acid ratio (mass volume ratio) 1:2.5.
8kg of iron powder (elemental iron content 95%) was added to give Fe 3+ Reduction to Fe 2+ Ensure Ti in acidolysis slurry at the end of acidolysis 3+ Reaching 1.5-2 g/L.
Introducing hydrogen chloride gas obtained by hydrochloric acid analysis, heating the system to 90 ℃ by utilizing the dissolution heat of the hydrogen chloride gas, maintaining the temperature of the system, improving the acidity of the system, and stirring for acidolysis for 1.5 hours. The acidolysis tail gas generated in acidolysis process is condensed and absorbed by resolved hydrochloric acid generated by a hydrochloric acid resolving system.
130g of dephosphorization flocculation complexing agent (pre-dissolved, 40wt% of ultra-high molecular weight cationic polyacrylamide, 60wt% of inorganic-organic compound dephosphorization agent) is added, and stirring is continued for 0.5 hour. The concentration of free hydrochloric acid in the acidolysis reaction kettle is maintained to be more than 270 g/L.
And sucking condensable gas by utilizing a tail gas system, reducing the effective acid concentration of the titanium liquid, discharging and thermally filtering when the temperature reaches 85 ℃.
Clear titanium solution (acidolysis slurry hot filtration followed by freeze crystallization for ferrous separation) results: ti in titanium liquid 4+ ：203.46g/L，Ti 3+ :1.25g/L, P:25.53ppm; acidolysis rate of titanium concentrate: 97.39 percent, the titanium liquid is deeply dephosphorized, the clear titanium liquid is purple, and the stability is more than 500.
Example 2
In the embodiment, the titanium concentrate is Panzhihua titanium concentrate, and the TiO 2 45.84% FeO 34.57% Fe 2 O 3 The content is 5.25%, the P content is 0.079%, and D max 74 μm (200 meshes). Pre-activating and grinding the titanium concentrate powder by a vertical mill to obtain acidolysis titanium concentrate fine powder with the granularity of D 98 ＜35.3μm，D max < 37 μm (400 mesh).
700L acidolysis acid (HCl: 320.34g/L, ti) 4+ (in TiO) 2 Meter): 27.52g/L, fe 2+ :16.98 g/L) was added to a closed volume of 1m 3 And stirring, and then adding 350kg of titanium concentrate fine materials into the acidolysis reaction kettle, stirring and mixing. Mineral acid ratio (mass volume ratio) 1:2.0.
9.96kg of iron powder (elemental iron content 95%) was added to make Fe 3+ Reduction to Fe 2+ Ensure Ti in acidolysis slurry at the end of acidolysis 3+ Reaching 1.5-2 g/L.
Introducing hydrogen chloride gas obtained by hydrochloric acid analysis, heating the system to 90 ℃ by utilizing the dissolution heat of the hydrogen chloride gas, maintaining the temperature of the system, improving the acidity of the system, and stirring for acidolysis for 1.5 hours. The acidolysis tail gas generated in acidolysis process is condensed and absorbed by resolved hydrochloric acid generated by a hydrochloric acid resolving system.
163g of dephosphorization flocculation complexing agent (pre-dissolved, 60wt% of ultra-high molecular weight cationic polyacrylamide, 40wt% of inorganic-organic compound dephosphorization agent) is added, and stirring is continued for 0.5 hour. The concentration of free hydrochloric acid in the acidolysis reaction kettle is maintained to be more than 270 g/L.
And sucking condensable gas by utilizing a tail gas system, reducing the effective acid concentration of the titanium liquid, discharging and thermally filtering when the temperature reaches 85 ℃.
Clear titanium solution (acidolysis slurry hot filtration followed by freeze crystallization for ferrous separation) results: ti in titanium liquid 4+ ：253.17g/L，Ti 3+ :1.36g/L, P:38.14ppm; acidolysis rate of titanium concentrate:96.84 percent, the titanium liquid is deeply dephosphorized, the clear titanium liquid is purple, and the stability is more than 500.
Example 3
In the embodiment, the raw material is TiO in the mineral separation process 2 Panzhihua titanium middling with content which does not meet the taste requirement of titanium concentrate, tiO 2 The content is 37.51 percent, the FeO content is 38.57 percent, and the Fe 2 O 3 The content is 7.20%, the P content is 0.051%, and Dmax is less than or equal to 74 μm (200 meshes). Pre-activating and grinding the titanium concentrate powder by a vertical mill to obtain acidolysis titanium concentrate fine powder with the granularity of D 98 < 35.3 μm, dmax < 37 μm (400 mesh).
700L acidolysis acid (HCl: 320.34g/L, ti) 4+ (in TiO) 2 Meter): 27.52g/L, fe 2+ :16.98 g/L) was added to a closed volume of 1m 3 And stirring, and then adding 350kg of titanium concentrate fine materials into the acidolysis reaction kettle, stirring and mixing. Mineral acid ratio (mass volume ratio) 1:2.0.
13.79kg of iron powder (elemental iron content 95%) was added to make Fe 3+ Reduction to Fe 2+ Ensure Ti in acidolysis slurry at the end of acidolysis 3+ Reaching 1.5-2 g/L.
Introducing hydrogen chloride gas obtained by hydrochloric acid analysis, heating the system to 90 ℃ by utilizing the dissolution heat of the hydrogen chloride gas, maintaining the temperature of the system, improving the acidity of the system, and stirring for acidolysis for 1.5 hours. The acidolysis tail gas generated in acidolysis process is condensed and absorbed by resolved hydrochloric acid generated by a hydrochloric acid resolving system.
163g of dephosphorization flocculation complexing agent (pre-dissolved, 60wt% of ultra-high molecular weight cationic polyacrylamide, 40wt% of inorganic-organic compound dephosphorization agent) is added, and stirring is continued for 0.5 hour. The concentration of free hydrochloric acid in the acidolysis reaction kettle is maintained to be more than 270 g/L.
And sucking condensable gas by utilizing a tail gas system, reducing the effective acid concentration of the titanium liquid, discharging and thermally filtering when the temperature reaches 85 ℃.
Clear titanium solution (acidolysis slurry hot filtration followed by freeze crystallization for ferrous separation) results: ti in titanium liquid 4+ ：236.59g/L，Ti 3+ :1.04g/L, P:29.27ppm; acidolysis rate of titanium concentrate: 95.37 percent,the deep dephosphorization of the titanium liquid, the purple color of the clear titanium liquid and the stability of the clear titanium liquid are more than 500.
The raw materials of the titanium concentrates purchased in the embodiment 1 and the embodiment 2 are high-phosphorus titanium concentrates, the P content of the high-phosphorus titanium concentrates is different, the granularity of the raw materials is different, and the chemical components are slightly different. Wherein the titanium concentrate in example 1 is 10 ore, D max Less than or equal to 150 mu m (100 meshes), and the P content is 0.047 percent; in example 2, the titanium concentrate was 20 ores, D max Less than or equal to 74 mu m (200 meshes), and the P content is 0.079 percent.
The mineral acid ratios used in example 1 and example 2 were different. The mineral acid ratio used in example 1 was 1:2.5 and the mineral acid ratio used in example 2 was 1:2.0.
The amounts and the compounding compositions of the dephosphorization flocculation complexing agents used in the example 1 and the example 2 are different, 130g (the cationic polyacrylamide with the ultra-high molecular weight accounts for 40wt percent, the inorganic-organic compound dephosphorization agent accounts for 60wt percent) is used in the example 1, and 163g (the cationic polyacrylamide with the ultra-high molecular weight accounts for 60wt percent, the inorganic-organic compound dephosphorization agent accounts for 40wt percent) is used in the example 2.
Can expand the source of titanium-bearing ore resources and realize the production of titanium white powder of low-grade titanium concentrate by hydrochloric acid method.
The titanium raw material used in example 2 is Panzhihua high-phosphorus titanium concentrate, and the titanium raw material used in example 3 is TiO in the beneficiation process 2 The content of the Panzhihua titanium middling does not reach the grade requirement of the titanium concentrate, the corresponding iron powder consumption is 13.79kg, and other conditions are the same.
The foregoing description is only illustrative of the present invention and is not intended to limit the scope of the invention, and all equivalent processes or direct or indirect applications in other related technical fields using the content of the present invention are included in the scope of the present invention.
Claims (8)
1. An acidolysis method in the industrial production flow of titanium dioxide powder by a hydrochloric acid method of high-phosphorus titanium concentrate comprises the following steps: (1) The raw material of the acid leaching titanium concentrate is titanium concentrate powder subjected to preactivation grinding; (2) Preparing acidolysis acid with concentration of 28-30wt% from filter cake formed by regenerated acid washing, acid leaching and filtering, and Ti in filter cake 4+ All are transferred into acidolysis acid; then pre-activating and grinding the titaniumFine ore concentrate is added, the mass-volume ratio of mineral acid is 1:2-1:3, and the mixture is stirred and mixed at normal temperature, so that Ti is further improved 4+ Concentration; (3) Ti existing in the normal temperature ore mixing stage 4+ When iron powder, ti is added 4+ Reduction to Ti 3+ To realize that Ti always exists in acidolysis process 3+ ，Fe 3+ Immediately reduced by iron powder to Fe 2+ Realizing a reduction acidolysis system; ensure Ti in acidolysis slurry at the end of acidolysis 3+ Reaching 1.5-2 g/L; (4) Introducing hydrogen chloride gas, heating the system to 88-95 ℃ by utilizing the dissolution heat of the hydrogen chloride gas, maintaining the acidolysis temperature of the system, increasing the acidity of the system, stirring for reaction, maintaining the concentration of free hydrochloric acid in an acidolysis kettle to be more than 270g/L, (5) adding a dephosphorization flocculation complexing agent into acidolysis slurry at 88-95 ℃ for high-temperature electric neutralization-adsorption bridging dephosphorization reaction, flocculating phosphorus-containing polymer colloid, titanium dioxide colloid and orthosilicic acid colloid 0.4-0.6 hour before acidolysis reaction is ended; and (3) after the temperature is reduced to 83-86 ℃, discharging, directly performing hot filtration, performing solid-liquid separation to obtain acidolysis solution, and washing a filter cake by using regenerated acid produced by a chloride roasting system to prepare acidolysis acid.
2. Acidolysis method according to claim 1, characterized in that the raw material of the titanium concentrate is a pre-activated ground fine material of titanium concentrate by a vertical mill, a stirred mill, the particle size of which is controlled to D max ＜38μm。
3. The acidolysis method of claim 1, wherein the dephosphorization flocculation complexing agent is formed by compounding ultra-high molecular weight cationic polyacrylamide and an inorganic-organic compound dephosphorization agent, and comprises the following components in parts by weight: 20 to 80 parts of cationic polyacrylamide, 20 to 80 parts of inorganic-organic composite dephosphorizing agent, and 80 to 100g/m of dephosphorizing flocculation complexing agent 3 The inorganic-organic composite dephosphorizing agent is formed by compounding polymeric ferric sulfate, PDMDAAC homopolymer and copolymer and chitin.
4. The acidolysis method as claimed in claim 1, wherein the hydrogen chloride gas in the step (4) is generated by hydrochloric acid desorption or a chloride roasting system.
5. An acidolysis process as claimed in claim 1, wherein step (2) washes the filter cake using regenerated acid produced by a chloride roasting system.
6. The acidolysis method as claimed in claim 1, wherein the step (5) is stirred for 1.5 hours.
7. The acidolysis method as claimed in claim 1, wherein the dephosphorization flocculation complexing agent is added 0.5 hours before the termination of the acidolysis reaction in the step (5).
8. The acidolysis method of claim 1, wherein after the reaction in the step (5), a tail gas system is used for sucking the condensable gas, reducing the effective acid concentration of the titanium liquid, and discharging and hot filtering when the temperature reaches 85 ℃.
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