CN103146863A

CN103146863A - Process for non-slag production of iron, aluminum and titanium by utilizing reduction molten-salt growth method

Info

Publication number: CN103146863A
Application number: CN2013101039413A
Authority: CN
Inventors: 胡长春; 胡晓雪
Original assignee: Individual
Current assignee: Individual
Priority date: 2013-03-14
Filing date: 2013-03-14
Publication date: 2013-06-12
Anticipated expiration: 2033-03-14
Also published as: CN103146863B; WO2014139335A1

Abstract

The invention relates to a process for non-slag production of iron, aluminum and titanium by utilizing a reduction molten-salt growth method, belonging to the technical fields of metal smelting and inorganic salts. The process comprises the steps of: (1) adding ammonium sulfate into a molten-salt reaction tank; (2) adding high-temperature molten slag; (3) introducing ammonia gas into a low-temperature waste heat generator; (4) introducing aluminum sulfate, titanyl sulfate, silicon dioxide and calcium sulfate into a first solid-liquid tank; (5) rectifying ammonia water and pumping the ammonia water into a smelting separation furnace cracking pipe; (6) introducing cracked gas into a rotary kiln; (7) conveying liquid ammonia into an aluminum sulfate solution tank; (8) hydrolyzing aluminum sulfate and titanyl sulfate; and (9) separating aluminum sulfate and titanyl sulfate by utilizing a second solid-liquid tank. The process has the advantages that red mud can be recycled and turned into wealth from waste; and the worldwide problems that the latent heat energy of the high-temperature molten slag cannot be effectively utilized and valuable elements cannot be extracted are thoroughly solved. Compared with the prior art, the process has the advantages that the total investment is substantially decreased, the production cost is one fifth of that of a Bayer process, and any pollution is avoided; and the comprehensive energy consumption is relatively low, the heat can be repeatedly used, the process is green and environment-friendly, and a metallurgy age of hydrogen industrial production is realized.

Description

Iron, aluminium, titanium reduction molten-salt growth method are without the slag production technique

Technical field

The invention belongs to ferrous metal, non-ferrous metal metallurgy and inorganic salt technical field, be specifically related to a kind of iron, aluminium, titanium reduction molten-salt growth method without the slag production technique.

Background technology

At present, steel industry, the high-temperature molten slag that extracts after iron is discarded, and its latent heat wave in vain is useless or utilization ratio is very low; Titanium white production is only extracted titanium, and other is also all discarded; The hydrometallurgy electrolytic nickel is produced, and other is also all discarded also only to extract nickel; Metallurgy of copper is also like this.These traditional productions, processing method have been not suitable for environmental requirement.They had both caused the pollution of environment, had caused again the wave of resource useless, and a large amount of heat energy wave in vain is useless, thereby production cost can be in any more.

After Aluminium industry used bauxite to extract aluminum oxide, all the other were all discharged as waste residue, so produced a large amount of pollutents---red mud, its pH of leaching solution is 12.1～13.0.More than one hundred million tons of red muds have been stored up in the whole world so far, and in alumina producing, annual continuous new a large amount of red mud that produces again causes directly many-sided and indirectly impact on the mankind's production, life.It is generally acknowledged that sodium salt content is that 30～400mg/L is the suitable scope at public water source, and the sodium salt degree of wastewater from red mud is up to 26348mg/L, the wastewater from red mud of high sodium salt degree like this enters water body, and its pollution is self-evident.For solving this difficult problem, people once attempted to use blast furnace process, magnetic method (comprising the superconducting magnetic separation method) or flotation process, extract the iron in red mud, and " digestion " red mud of storing up in a large number by this, but, because the iron in red mud exists with states such as deep oxidation iron, molysite, therefore magnetic method (comprising the superconducting magnetic separation method), gravity separation method or flotation process can't be extracted iron wherein at all; And blast furnace process, because wherein contain relatively large aluminium, titanium and compound thereof, due to the unusual thickness of these materials, the carrying out that has not only stoped the gas-solid-liquid phase reaction in the blast furnace, and make the blast furnace " scum " can not; Although can mix a large amount of calcium containing compounds to solve " thickness " problem, just greatly increased production cost, substantially there is no benefit, lost practicality, so no longer be used.

I have applied for following Chinese invention patent: 1, the applying date is on June 2nd, 2012, and application number is 201210199691.3 and is called " a kind of bauxite or red mud of utilizing carries out the processing method of producing without slag "; 2, the applying date is on July 27th, 2012, and application number is 201210279677.4, and name is called " a kind of iron, aluminium, titanium integrated process are without the slag production technique "; 3, the applying date is on January 21st, 2012, and application number is 201210025393.2, and name is called " smelting system of the rotary kiln melting furnace of continuous temperature control "; 4, the applying date is on January 21st, 2012, and application number is 201210025404.7, and name is called " rotary kiln gas-distribution system for dynamic boiling bed ".Above patent, at first solved blast furnace process " scum " in the prior art can not problem, reduced widely production cost; Next is to make poisonous red mud resource utilization, to obtain fe, its rate of recovery can reach more than 99%, has solved the problem of red mud occupation of land, contaminate environment.Although this is a large good recycling economy technology, but still exists following shortcoming: it does not also accomplish low cost, the efficient comprehensive recycling of heat energy fully.Though can obtain byproducts such as silicon titanium aluminum alloy, microlite, but the contained latent heat of high-temperature molten slag after extracting is not utilized well, still caused the wave of resource useless, solid pollutant zero release in the entire process, liquid zero emission and gas qualified discharge, environmental protection are produced in inreal realization.

Summary of the invention

the technical problem to be solved in the present invention is: overcome the deficiencies in the prior art, a kind of iron is provided, aluminium, titanium reduction molten-salt growth method is without the slag production technique, it can thoroughly solve, and in prior art, high-temperature molten slag latent heat can not utilize or can not utilize fully, himself valuable element can not extraction and application global problem, and residue contamination environment, the wasting of resources, production capacity is hanged down inferior problem, reach low-cost, objectionable impurities is become efficient resource high-effectly, really realize the zero release of production whole process solid pollutant, liquid zero emission and gas qualified discharge, environmental protection.

The technical solution adopted for the present invention to solve the technical problems is: iron, aluminium, titanium reduction molten-salt growth method is characterized in that: comprise the steps: 1 without the slag production technique) add appropriate ammoniumsulphate soln in the molten salt react ion tank; 2) high-temperature molten slag is joined in the molten salt react ion tank that fills appropriate ammoniumsulphate soln; 3) will be input to low-temperature cogeneration from the ammonia that the ammonia outlet of molten salt react ion tank is exported, generate electricity.

Preferably, also comprise the steps: 4) will generate from the reaction of molten salt react ion tank liquid aluminium sulphate and the solidliquid mixtures such as titanyl sulfate, solid-state silicon-dioxide and calcium sulfate of solidliquid mixture outlet output, be transported in the first solid-liquid separation.

Preferably, also comprise the steps: 5) ammoniacal liquor after the low-temperature cogeneration of flowing through, be transported to the ammonia rectifying tower and carry out rectifying; With the part of the pure liquefied ammonia of purifying out, pump in molten minute stove cracking tube; 6) will from molten minute stove cracking tube hydrogen, nitrogen splitting gas out, be passed in rotary kiln through the rotary kiln air distribution disk.

Preferably, also comprise the steps: 7) will through another part liquefied ammonia of ammonia rectifying tower purification generation, be transported in the alum liquor tank.

Preferably, also comprise the steps: 8) carry out solid-liquid separation by the first solid-liquid separation, obtain solid silica, calcium sulfate; The liquid aluminium sulphate that obtains simultaneously, titanyl sulfate etc. are transported to are hydrolyzed in the hydrolysis reaction tank; 9) through being hydrolyzed and again carrying out solid-liquid separation by the second solid-liquid separation, obtain titanium dioxide solid and liquid aluminium sulphate; Liquid aluminium sulphate enters in the alum liquor tank.

Preferably, also comprising the steps: 10) solid aluminum hydroxide, ammonium sulfate solution that the liquefied ammonia in the alum liquor tank and Tai-Ace S 150 are reacted generation be transported to the 3rd solid-liquid separation and carry out solid-liquid separation, obtain solid aluminum hydroxide and separate out ammonium sulfate solution; Ammonium sulfate solution is placed in the ammoniumsulphate soln tank; 11) by the pressurization of ammonium sulfate pump, ammonium sulfate solution is input in the molten salt react ion tank through fluid inlet, then reacts with high-temperature molten slag.

Preferably, also comprise the steps: 12) with the water that the ammonia rectifying tower extracts, be transported in the hydrolysis reaction tank for hydrolysis.

Preferably, step 1) in, add appropriate ammonium sulfate in the molten salt react ion tank by the fluid inlet of molten salt react ion tank.

Preferably, step 2) in, will through rotary kiln prereduction, molten minute stove melting and reducing high-temperature molten slag out, by the molten high-temperature molten slag entrance of the high-temperature molten slag outlet of stove through the molten salt react ion tank that divide, be input in the molten salt react ion tank; High-temperature molten slag and ammonium sulfate reaction produce the solidliquid mixtures such as ammonia, liquid aluminium sulphate and titanyl sulfate, solid-state silicon-dioxide and calcium sulfate.

Preferably, step 3) in, ammonia is by the ammonia outlet output of molten salt react ion tank top, through vacuum pressure unit pressurized stream through low-temperature cogeneration; Low-temperature cogeneration utilizes the working medium heat exchange, and the sheathed screw decompressor generates electricity.

Preferably, step 4) in, the solidliquid mixtures such as liquid aluminium sulphate and titanyl sulfate, solid-state silicon-dioxide and calcium sulfate in transfer roller is pressed and delivered to neutralization tank, then are transported in the first solid-liquid separation.

Preferably, step 5) in, ammoniacal liquor is transported to the ammonia rectifying tower by aqua ammonia pump and carries out rectifying; Pure liquefied ammonia uses ammonia pump, is transported in molten minute stove cracking tube.

Preferably, step 7) in, use ammonia pump that pure liquefied ammonia is transported in the alum liquor tank, be used for generating ammonium sulfate liquid and solid aluminum hydroxide.

Compared with prior art, the invention has the beneficial effects as follows: the present invention can effectively with the high-temperature molten slag resource utilization, be turned waste into wealth; It can thoroughly solve the global problem that the high-temperature molten slag calorific potential can't effectively be utilized, the valuable metal element can't extract.The present invention has fully effectively utilized high-temperature molten slag self heat and has contained high characteristic, adds ammonium sulfate thoroughly reaction with it, the acid-soluble materials such as wherein aluminium, titanium is produced leach, and this is that the conventional acid leaching method can not be compared; It can all extract valuable metal in high-temperature molten slag, extract aluminum oxide and iron in needle-like ferro-aluminum ore deposit, has accomplished that the institute of " Bayer process ", " sintering process ", " integrated process " can not; When utilizing bauxite to use device of the present invention to produce aluminium, iron, titanium, the contaminate environment with regard to no longer producing red mud, thus thoroughly changed the production status of aluminum oxide.Bauxite is joined ilmenite production titanium dioxide and be need not special manufacturer, and does not produce any pollution, and production cost is low.The present invention is that ferrous metal, non-ferrous metal, inorganic chemicals industry, organic synthesis, chemical industry ammonia processed and building material industry etc. are inter-trade, the combination of cross-cutting technology, and it has thoroughly changed high pollution, the high energy consumption of titanium dioxide production industry, the present situation of high price.The present invention can promote on a large scale, then there is no need to set up special titanium white production producer; This type of extensive comprehensive utilization factory both can satisfy the demand in domestic titanium dioxide market, makes titanium dioxide market revert to the reasonable price of natural abundance reserves.Gross investment of the present invention has decrease than prior art, production cost very low (be existing bayer's process 1/5th), and do not produce any pollution, comprehensive energy consumption is very low, heat energy repeatedly reuses, and environmental protection realizes the arrival in metallurgical epoch of hydrogen industrial production.

Description of drawings

Fig. 1 is the structured flowchart of implementing device of the present invention;

Fig. 2 is the sectional structure schematic diagram of rotary kiln in Fig. 1.

Be labeled as in figure:

1, rotary kiln; 1a, rotary kiln air distribution disk; 2, molten minute stove; 2a, high-temperature molten slag outlet; 2b, molten minute stove cracking tube;

3, molten salt react ion tank; 3a, ammonia outlet; 3b, high-temperature molten slag entrance; 3c, fluid inlet;

3d, reaction generate the solidliquid mixture outlet; 4, vacuum pressure unit; 5, low-temperature cogeneration; 6, aqua ammonia pump;

7, ammonia rectifying tower; 7a, water out; 7b, liquefied ammonia outlet; 8, ammonia pump; 9, transfer roller; 10, neutralization tank;

11, the first solid-liquid separation; 12, hydrolysis reaction tank; 13, the second solid-liquid separation; 14, alum liquor tank;

15, the 3rd solid-liquid separation; 16, ammoniumsulphate soln tank; 17, ammonium sulfate pump.

Embodiment

As shown in Figure 1, 2, be to implement one of device of the present invention, its structure is as follows: comprise rotary kiln 1, molten minute stove 2, molten salt react ion tank 3, vacuum pressure unit 4 and low-temperature cogeneration 5, rotary kiln 1 head is communicated with molten minute stove 2 afterbodys by enclosed passage; Rotary kiln 1 head arranges rotary kiln air distribution disk 1a; Stove 2 heads arranged high-temperature molten slag outlet 2a in molten minute, and stove 2 tops arranged a molten minute stove cracking tube 2b in molten minute; Molten salt react ion tank 3 tops arrange ammonia outlet 3a, and top arranges high-temperature molten slag entrance 3b, and on the tank skin of side, interval 90 degree are symmetrical arranged four fluid inlet 3c, and the bottom arranges reaction and generates solidliquid mixture outlet 3d;

High-temperature molten slag outlet 2a is communicated with by enclosed passage with high-temperature molten slag entrance 3b, and fluid inlet 3c is lower than high-temperature molten slag entrance 3b, and high-temperature molten slag entrance 3b exports 2a lower than high-temperature molten slag; The ammonia outlet 3a at molten salt react ion tank 3 tops is communicated with low-temperature cogeneration 5 through vacuum pressure unit 4, and low-temperature cogeneration 5 sheathed screw decompressors generate electricity;

Also comprise aqua ammonia pump 6, ammonia rectifying tower 7 and ammonia pump 8, be provided with water out 7a and liquefied ammonia outlet 7b on ammonia rectifying tower 7; Aqua ammonia pump 6, ammonia rectifying tower 7, ammonia pump 8, molten minute stove cracking tube 2b, rotary kiln air distribution disk 1a order successively are communicated with;

The transfer roller 9, neutralization tank 10, the first solid-liquid separation 11, hydrolysis reaction tank 12, the second solid-liquid separation 13 and the alum liquor tank 14 that also comprise order connection successively; Transfer roller 9 generates solidliquid mixture outlet 3d with reaction and is communicated with, and the water out 7a of ammonia rectifying tower 7 is communicated with hydrolysis reaction tank 12, and the liquefied ammonia outlet 7b of ammonia rectifying tower 7 is communicated with molten minute stove cracking tube 2b, alum liquor tank 14 respectively through ammonia pump 8.

Alum liquor tank 14 also is communicated with the 3rd solid-liquid separation 15, the three solid-liquid separation 15 and also is communicated with the fluid inlet 3c of molten salt react ion tank 3 by ammonium sulfate pump 16, ammonium sulfate pump 17.

Below in conjunction with accompanying drawing embodiment, the present invention is described further:

As shown in Figure 1, 2, iron, aluminium, titanium reduction molten-salt growth method comprise the steps: without the slag production technique

1) the fluid inlet 3c by molten salt react ion tank 3 adds appropriate ammonium sulfate in molten salt react ion tank 3;

2) will realize the high-temperature molten slag that slag iron is separated through rotary kiln 1 prereduction, molten minute stove 2 melting and reducings, by the molten high-temperature molten slag entrance 3b of the high-temperature molten slag outlet 2a of stove 2 through molten salt react ion tank 3 that divide, be input in molten salt react ion tank 3; High-temperature molten slag and ammonium sulfate wherein react, and produce the solidliquid mixtures such as ammonia, liquid aluminium sulphate and titanyl sulfate, solid-state silicon-dioxide and calcium sulfate;

3) ammonia of reaction generation, by the ammonia outlet 3a output of molten salt react ion tank 3, through 4 pressurizations of vacuum pressure unit, the low temperature exhaust heat of flowing through sends out 5, and low-temperature cogeneration 5 utilizes the working medium heat exchange, and the sheathed screw decompressor generates electricity;

4) will generate from the reaction of molten salt react ion tank 3 liquid aluminium sulphate and the solidliquid mixtures such as titanyl sulfate, solid-state silicon-dioxide and calcium sulfate of solidliquid mixture outlet 3d output, in transfer roller 9 is pressed and delivered to neutralization tank 10, add sulfuric acid further neutralization wherein be transported in the first solid-liquid separation 11 after the ammonia of contained remnants;

5) with the ammoniacal liquor after low temperature exhaust heat 5 generatings, be transported to ammonia rectifying tower 7 by aqua ammonia pump 6 and carry out rectifying; With the part of the pure liquefied ammonia of purifying out, use ammonia pump 8 to be transported in molten minute stove cracking tube 2b in the anti-material of furnace roof of molten minute stove 2;

6) will be from molten minute stove cracking tube 2b hydrogen, nitrogen splitting gas out, 1a is passed in rotary kiln 1 through the rotary kiln air distribution disk;

7) will through another part liquefied ammonia of ammonia rectifying tower 7 purification generations, use ammonia pump 8 to be transported in alum liquor tank 14;

8) carry out solid-liquid separation by the first solid-liquid separation 11, obtain solid silica, calcium sulfate is separated out; The liquid aluminium sulphate that obtains simultaneously, titanyl sulfate etc. are transported to are hydrolyzed in hydrolysis reaction tank 12;

9) hydrolysis in hydrolysis reaction tank 12, more again carry out solid-liquid separation by the second solid-liquid separation 13, obtain titanium dioxide solid and liquid aluminium sulphate; Liquid aluminium sulphate enters in alum liquor tank 14;

10) Tai-Ace S 150 in alum liquor tank 14 with react from the pure liquefied ammonia of ammonia pump 8, generate solid aluminum hydroxide, ammonium sulfate solution; Solid aluminum hydroxide, ammonium sulfate solution are transported to the 3rd solid-liquid separation 15 carry out solid-liquid separation, obtain the solid aluminum hydroxide ammonium sulfate solution; Ammonium sulfate solution is placed in ammoniumsulphate soln tank 16;

11) by 17 pressurizations of ammonium sulfate pump, the ammonium sulfate solution in ammoniumsulphate soln tank 16 is input in molten salt react ion tank 3 through fluid inlet 3c, then reacts with high-temperature molten slag;

12) water that ammonia rectifying tower 7 is extracted is transported in hydrolysis reaction tank 12, is used for hydrolysis.

Principle of work of the present invention and working process are as follows:

As shown in Figure 1, 2, the mixture of process carbon, hydrogen prereduction in rotary kiln 1, enter molten minute stove 2 by enclosed passage, carrying out melting slag iron through a superfusion minute stove 2 separates, the heating molten steel that restores is by molten minute stove 2 bottoms outflows, and the top high-temperature molten slag enters into molten salt react ion tank 3 by high-temperature molten slag outlet 21 through high-temperature molten slag entrance 3b;

Add appropriate ammonium sulfate in molten salt react ion tank 3 by fluid inlet 3c, after high-temperature molten slag enters, aluminium wherein, titanium pyrolytic decomposition sulfate of ammoniac, form new mineral sulfates, pyrolytic decomposition ammonia, the elements such as the vanadium that the aluminium sesquioxide in high-temperature molten slag, titanium dioxide and acid is simultaneously melted, scandium are combined with sulfate radical and are formed new water-soluble vitriol, have namely generated respectively the solidliquid mixtures such as ammonia steam, liquid aluminium sulphate and titanyl sulfate, solid-state silicon-dioxide and calcium sulfate;

Ammonia steam is by the ammonia outlet 3a output at molten salt react ion tank 3 tops, through 4 pressurizations of vacuum pressure unit, the low-temperature cogeneration 5 of flowing through; Low-temperature cogeneration 5 utilizes the working medium heat exchange that the ammonia steam cooling is generated as ammoniacal liquor, and the sheathed screw decompressor generates electricity;

The ammonia steam becomes ammoniacal liquor after low-temperature cogeneration 5 coolings, be transported to ammonia rectifying tower 7 by aqua ammonia pump 6; Ammoniacal liquor is purified through ammonia rectifying tower 7, and generation water and purity are the pure liquefied ammonia more than 99%.Wherein, the sub-fraction of these pure liquefied ammonia is directly pumped into the molten minute stove cracking tube 2b that is arranged in the molten minute stove 2 anti-materials of furnace roof, and a molten minute stove cracking tube 2b is cracked into hydrogen, nitrogen mixed gas with them; Due to the endothermic pyrolysis of ammonia, effectively reduced the temperature of the furnace roof fire resisting material of molten minute stove 2, played the effect of protecting anti-material, extended the life-span of anti-material;

From molten minute stove cracking tube 2b hydrogen, nitrogen splitting gas out, enter in rotary kiln 1 by rotary kiln air distribution disk 1a; Add hydrogen under the condition of coal based ferrum redactum, just improved the reduction ratio of iron; Under the prerequisite of this high reduction ratio, can reduce effectively, significantly in reduction temperature to 1000 degree, thereby thoroughly solve the global problems such as ring formation, spin of rotary kiln 1; Low-cost hydrogen reduction iron, nickel, ilmenite have been realized;

Another most of liquefied ammonia through ammonia rectifying tower 7 is purified and produced is transported in alum liquor tank 14, is used for generating ammonium sulfate liquid and solid aluminum hydroxide;

The solidliquid mixtures such as liquid aluminium sulphate and titanyl sulfate, solid-state silicon-dioxide and calcium sulfate, reaction generation solidliquid mixture outlet 3d discharge by molten salt react ion tank 3 bottoms, in transfer roller 9 is transported to neutralization tank 10, adds sulfuric acid and be used for further extracting valuable element in neutralization tank 10; Above-mentioned solidliquid mixture enters the first solid-liquid separation 11 again and carries out solid-liquid separation, generates solid silica, calcium sulfate and liquid aluminium sulphate, titanyl sulfate etc.; The solid such as silicon-dioxide, calcium sulfate is used for making high-grade material glass etc., and its iron-holder is the PPM level; After liquid aluminium sulphate, titanyl sulfate enter into hydrolysis reaction tank 12 and be hydrolyzed, again carry out solid-liquid separation by the second solid-liquid separation 12, obtain titanium dioxide solid and liquid aluminium sulphate; Liquid aluminium sulphate enters in alum liquor tank 14;

In alum liquor tank 14, react from the liquefied ammonia of ammonia rectifying tower 7 and Tai-Ace S 150 wherein, generated solid aluminum hydroxide, ammonium sulfate solution; Carry out solid-liquid separation through the 3rd solid-liquid separation 15, obtain solid aluminum hydroxide and ammonium sulfate solution; Ammonium sulfate solution is placed in ammoniumsulphate soln tank 16, then by 17 pressurizations of ammonium sulfate pump, is input in molten salt react ion tank 3 through fluid inlet 3c, then reacts with high-temperature molten slag;

Alum liquor in alum liquor tank 14 can also pass in neutralization tank 10, is used for further extracting valuable element;

The ammonia vapour stream through the water that ammonia rectifying tower 7 extracts, enters in hydrolysis reaction tank 12 after low-temperature cogeneration 5, is used for replenishing of hydrolysis water.

Like this, make ammonia and sulfuric acid can only do a small amount of replenishing, thereby realize the also use that follows of ammonia, sulfuric acid.

The part chemical equation is:

3(NH4)2SO4+AI2O3＝AI2(SO4)3+4NH3+6H2O+N2

(NH4)2SO4+TIO2＝TIOSO4+2NH3+H2O

6NH3·H2O+AI2(SO4)3＝3(NH4)2SO4+2AI(OH)3

The above is only preferred embodiment of the present invention, is not to be the present invention to be done the restriction of other form, and any those skilled in the art may utilize the technology contents of above-mentioned announcement to be changed or be modified as the equivalent embodiment of equivalent variations.But every technical solution of the present invention content that do not break away to any simple modification, equivalent variations and remodeling that above embodiment does, still belongs to the protection domain of technical solution of the present invention according to technical spirit of the present invention.

Claims

1. iron, aluminium, titanium reduction molten-salt growth method without the slag production technique, is characterized in that: comprise the steps:

1) add appropriate ammoniumsulphate soln in the molten salt react ion tank;

2) high-temperature molten slag is joined in the molten salt react ion tank;

3) will be transported to low-temperature cogeneration by the ammonia of ammonia outlet output, generate electricity.

2. iron according to claim 1, aluminium, titanium reduction molten-salt growth method without the slag production technique, is characterized in that: also comprise the steps:

4) will react liquid aluminium sulphate and titanyl sulfate, solid-state silicon-dioxide and the calcium sulfate solidliquid mixture that generates solidliquid mixture outlet output, be passed in the first solid-liquid separation.

3. iron according to claim 2, aluminium, titanium reduction molten-salt growth method without the slag production technique, is characterized in that: also comprise the steps:

5) will flow through ammoniacal liquor after low-temperature cogeneration carries out rectifying; With the liquefied ammonia of purifying out, pump in molten minute stove cracking tube;

6) will from molten minute stove cracking tube hydrogen, nitrogen splitting gas out, be passed in rotary kiln.

4. iron according to claim 3, aluminium, titanium reduction molten-salt growth method without the slag production technique, is characterized in that: also comprise the steps:

7) will through the liquefied ammonia of ammonia rectifying tower purification generation, be transported in the alum liquor tank.

5. arbitrary described iron, aluminium, titanium reduction molten-salt growth method are without the slag production technique according to claim 2 to 4, it is characterized in that: also comprise the steps:

8) carry out solid-liquid separation by the first solid-liquid separation, obtain solid silica, calcium sulfate; With liquid aluminium sulphate, the titanyl sulfate that obtains simultaneously, be transported in the hydrolysis reaction tank and be hydrolyzed;

9) through being hydrolyzed and carrying out solid-liquid separation by the second solid-liquid separation, obtain titanium dioxide solid and liquid aluminium sulphate; Liquid aluminium sulphate enters in the alum liquor tank.

6. iron according to claim 5, aluminium, titanium reduction molten-salt growth method without the slag production technique, is characterized in that: also comprise the steps:

10) solid aluminum hydroxide, the ammonium sulfate solution that the Tai-Ace S 150 in the alum liquor tank and liquefied ammonia are reacted generation are transported to the 3rd solid-liquid separation and carry out solid-liquid separation, obtain solid aluminum hydroxide and ammonium sulfate solution; Ammonium sulfate solution is placed in the ammoniumsulphate soln tank;

11) ammonium sulfate solution is input in the molten salt react ion tank, then reacts with high-temperature molten slag.

7. iron according to claim 6, aluminium, titanium reduction molten-salt growth method without the slag production technique, is characterized in that: also comprise the steps:

12) water that the ammonia rectifying tower is extracted is transported in the hydrolysis reaction tank.

8. iron according to claim 7, aluminium, titanium reduction molten-salt growth method without the slag production technique, is characterized in that: step 1) in, add appropriate ammoniumsulphate soln in the molten salt react ion tank by the fluid inlet of molten salt react ion tank.

9. iron according to claim 8, aluminium, titanium reduction molten-salt growth method are without the slag production technique, it is characterized in that: step 2) in, will be through rotary kiln prereduction, molten minute stove melting and reducing high-temperature molten slag out, by the molten high-temperature molten slag entrance of the high-temperature molten slag outlet of stove through the molten salt react ion tank that divide, be input in the molten salt react ion tank; High-temperature molten slag and ammonium sulfate reaction produce the solidliquid mixtures such as ammonia, liquid aluminium sulphate and titanyl sulfate, solid-state silicon-dioxide and calcium sulfate.

10. iron according to claim 9, aluminium, titanium reduction molten-salt growth method are without the slag production technique, it is characterized in that: step 3) in, ammonia is by the ammonia outlet output of molten salt react ion tank top, through vacuum pressure unit pressurized stream through low-temperature cogeneration, low-temperature cogeneration utilizes the working medium heat exchange, and the sheathed screw decompressor generates electricity.

11. iron according to claim 10, aluminium, titanium reduction molten-salt growth method are without the slag production technique, it is characterized in that: step 4) in, the solidliquid mixtures such as liquid aluminium sulphate and titanyl sulfate, solid-state silicon-dioxide and calcium sulfate, after neutralizing in transfer roller is pressed and delivered to neutralization tank, then be transported in the first solid-liquid separation.

12. iron according to claim 11, aluminium, titanium reduction molten-salt growth method is characterized in that: step 5 without the slag production technique) in, ammoniacal liquor is transported to the ammonia rectifying tower by aqua ammonia pump and carries out rectifying; Use ammonia pump, pure liquefied ammonia is transported in molten minute stove cracking tube.

13. iron according to claim 12, aluminium, titanium reduction molten-salt growth method is characterized in that: step 7 without the slag production technique) in, use ammonia pump that pure liquefied ammonia is pumped in the alum liquor tank.