CN103031433B - Fluidized oxidation roasting-fluidized reduction roasting system and roasting process for titaniferous iron concentrate - Google Patents
Fluidized oxidation roasting-fluidized reduction roasting system and roasting process for titaniferous iron concentrate Download PDFInfo
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Abstract
The invention discloses a fluidized oxidation roasting-fluidized reduction roasting system and roasting process for titaniferous iron concentrate. The fluidized oxidation roasting-fluidized reduction roasting process for the titaniferous iron concentrate comprises the following steps of: performing oxidation roasting on titaniferous iron concentrate powder by adopting a fluidized bed oxidation reactor; enabling the oxidized powder to enter a fluidized bed reduction reactor and performing reduction roasting; cooling the reduced powder through a fluidized bed cooler; firstly burning tail gas exhausted from the fluidized bed reduction reactor in a combustion chamber so as to release the latent heat of unreacted reduction gas in the tail gas; mixing gas after burning with tail gas exhausted from the fluidized bed oxidation reactor; and then, entering a multi-stage cyclone preheater to exchange heat with the titaniferous iron concentrate powder to recover heat. The fluidized oxidation roasting-fluidized reduction roasting system for the titaniferous iron concentrate, disclosed by the invention has the advantages that the reaction efficiency is high; the heat can be fully utilized; the roasting process is good in economic efficiency and is suitable for large-scale continuous industrial production.
Description
Technical field
The present invention relates to chemical industry, metallurgical technology, relate in particular to a kind of concentrated ilmenite fluidization oxidizing roasting-fluidized reduction roasting system and sinter process.
Background technology
Increase along with chloride process titanium dioxide and titanium sponge output, both at home and abroad the demand of the required rich titanium of chlorination process material is significantly increased, the natural high-quality titanium ore (rutile ore) of occurring in nature seldom, be difficult to satisfy the demands, need low-grade ilmenite to carry out upgrading processing for this reason, prepare high-quality titanium slag or artificial rutile.The ilmenite of occurring in nature divides placer and rock ore deposit two classes, wherein especially abundant with rock ore reserves, as the vanadium titano-magnetite resource reserve of the Flos Bombacis Malabarici-Xichang Region of China (Panxi Diqu) has nearly 10,000,000,000 tons, wherein titanium exists with ore type ilmenite, and approximately 8.7 hundred million tons of reserves are (with TiO
2meter), account for 90% left and right of national titanium resource, the ore type ilmenite reserves of the states such as Canada, Australia, South Africa, the C.I.S. are also very abundant.It is long-term and will continue the hot subject of research both at home and abroad from ore type ilmenite, preparing high-quality titanium slag and artificial rutile always.
Ore type ilmenite can be write Fe TiO
3or FeOTiO
2, conventionally also have the elements such as silicon, aluminium, magnesium, calcium, manganese, vanadium to exist with the form of oxide compound, the concentrated ilmenite of different areas form and impurities difference larger, such as the TiO of the concentrated ilmenite of China's Panxi Diqu
2content is 44-47% only, and non-iron contamination is but up to 10-15%, and especially the calcium oxide (CaO) of the strict restriction of chlorination process, magnesium oxide (MgO), manganese oxide (MnO) equal size are especially up to 7-11%; Contrast therewith, the concentrated ilmenite TiO of Australia
2content is greater than 54% conventionally, and non-iron contamination is below 5%, and MnO content is generally in 1.5% left and right, and CaO and MgO are seldom.Concentrated ilmenite forms different, and having determined that the technique of rich titanium material is prepared in upgrading also should be different.
It is the process of removing the impurity such as iron wherein, silicon, aluminium, magnesium, calcium, manganese, vanadium that rich titanium material is prepared in concentrated ilmenite upgrading, especially the total content of the magnesium oxide of the follow-up chloridization process of impact, calcium oxide, manganese oxide etc. will be down to below 1.5%.Can the iron in concentrated ilmenite be reduced to the separation that molten iron is realized ferrotianium by the mode of electrosmelting, for of high grade, the low concentrated ilmenite of calcium magnesium manganese content, only by electrosmelting, just can obtain being applicable to the high-quality titanium slag of chloridization process, but, calcium magnesium manganese content high concentrated ilmenite low for grade, by titanium slag after electrosmelting, do not reach the requirement of chloridization process, the titanium slag TiO obtaining such as the concentrated ilmenite of Panxi Diqu after electrosmelting yet
2content is below 80%, and CaO+MgO is but up to 7-11%.Except electrosmelting, the process for upgrading of concentrated ilmenite also comprises reduction-rusting process and pickling process two classes.Although reduction-rusting process is very successful in Australia's application, this method is very weak to the removal ability of CaO, MgO, cannot meet the upgrading requirement of climbing western concentrated ilmenite, and acidleach is to climb the only way that high-quality titanium slag or artificial rutile are prepared in western concentrated ilmenite upgrading.
By acidleach, remove the elements such as iron in concentrated ilmenite, calcium, magnesium, manganese and studied decades both at home and abroad, acid leaching process can be divided into again: directly acidleach, oxidizing roasting-acidleach, reducing roasting-acidleach and several routes of oxidizing roasting-reducing roasting-acidleach.Because concentrated ilmenite structure is comparatively fine and close, directly acidleach speed is slower, in order to accelerate leaching velocity, often needs to adopt pressure leaching, and in addition, directly acidleach often causes the artificial rutile efflorescence of preparation, affects subsequent applications.Roasting can improve leaching velocity when reducing product Pulverization ratio, but independent oxidizing roasting or reducing roasting are improving leaching velocity and avoiding all also not fully up to expectations aspect product efflorescence.For example, Benilite company proposes to strengthen leaching by rotary kiln reducing roasting in US Patent No. 3967954 and US4019898, improves leaching yield, by add H in hydrochloric acid by adding elemental sulfur to form vitriol
2sO
4or vitriol reduces the Pulverization ratio of product.For another example Chinese invention patent ZL03136052.1 has proposed a kind of method of preparing artificial rutile by weak oxide-Leaching in Hydrochloric Acid, but the Pulverization ratio of product is too high, reach 14% left and right and (see steel vanadium titanium, 2004,25[1], 44-50), product efflorescence not only causes filtration difficulty, impact is produced, and follow-up chloridization process is also difficult to adapt to.Oxidizing roasting combines with reducing roasting, avoiding having unique advantage aspect product efflorescence, raising leaching efficiency, is the important pre-treatment means that concentrated ilmenite is prepared rich titanium material.United States Patent (USP) 5885324, 5830420, 6531110, Chinese patent ZL200810300703.0, ZL200810177520.4 etc. have proposed concentrated ilmenite or titanium slag to be carried out to the method for pre-treatment by oxidizing roasting and reducing roasting, the roasting part of these patents is comparatively similar, all propose to adopt fluidized-bed to be oxidized and reducing roasting, different is only embodied in roasting parameter, if the oxidizing roasting of United States Patent (USP) 5885324 and reducing roasting temperature are all 750-1000 ℃, and United States Patent (USP) 5830420 and 6531110 is mainly for titanium slag, oxidizing roasting temperature 1000-1100 ℃, reducing roasting temperature 700-900 ℃, the oxidizing roasting temperature 800-1100 ℃ that Chinese patent ZL200810300703.0 and ZL200810177520.4 propose, reducing roasting temperature 600-900 ℃.Another similitude is that these patents just propose a principle process, for specifically how implementing, as oxidizing roasting and how reducing roasting institute heat requirement is supplied with, how baking tail gases heat utilizes, how reducing roasting tail gas unreacted reducing gas reclaims etc. does not all relate to.In fact, single from roasting method, these patents do not embody very strong novelty, because concentrated ilmenite or titanium slag are carried out to oxidizing roasting and reducing roasting processing, at document more early, as the people such as Auger in the United States Patent (USP) 4097574 obtaining for 1978 and the people such as Ismail be published in International Journal of MineralProcessing, 1983, the just existing detailed disclosure of article on 10,161-164.Therefore, industry in the urgent need to be not again the principle process of " proposition " oxidation-reduction roasting, but how to realize the concrete technology of efficient oxidation roasting and reducing roasting.
United States Patent (USP) 4097574 has proposed a kind of technique of concentrated ilmenite being carried out to oxidizing roasting and reducing roasting, sees the appended schema of this patent.Concentrated ilmenite carries out oxidizing roasting 1.5-2h under air atmosphere, 593-871 ℃ (1100-1600 °F) in rotary kiln or fluidized-bed, oxidizing temperature maintains by combustion fuel, oxidizing roasting tail gas is directly emptying after cyclone dust removal, and the fine powder of collection returns to oxidizing roasting reactor.After oxidation, concentrated ilmenite is under hot state, be directly promoted to hot intermediate bunker by heat air conveying, and intermediate bunker is necessary by keeping system continuity, because follow-up reduction fluidized-bed is periodical operation.Concentrated ilmenite after oxidation enters reduction fluidized-bed from intermediate bunker, at hydrogen atmosphere, in 760-926 ℃ (1400-1700 °F), gauge pressure 20 normal atmosphere (300psi), be reduced to reduction degree and be greater than 85% rear discharge, enter reduced ore intermediate bunker, this intermediate bunker is also that to maintain system necessary continuously, then discharges and enter roasted ore water cooler from intermediate bunker, the in the situation that of isolated air, be cooled to behind 200 ℃ of left and right, send leaching section.Reduction adopts hydrogen to mix with the hydrogen obtaining from reduction fluidized-bed discharge tail gas recycle after pressurization, first with from reduction fluidized-bed discharge tail gas heat exchange tail gas heat exchanger, enter again gas preheater be heated to reduction reaction temperature above after, from bottom, enter reduction fluidized-bed, in fluidized-bed with through oxidation concentrated ilmenite generation reduction reaction after, from reduction furnace top, discharge, after tornado dust collector dedusting, enter tail gas heat exchanger and reactant gases heat exchange, then enter in tail gas washing tower and remove fine powder body wherein and react the water vapor producing by washing, mix with fresh reactant gases after drying again, thereby realize the recycle of unreacting gas.
Although above-mentioned patent has provided a concentrated ilmenite oxidizing roasting and the concrete implementing process of reducing roasting, and partly having utilized using waste heat from tail gas and reclaimed unreacted hydrogen in reduction tail gas, also there is following deficiency in this technique:
(1), oxidized still exports hot tail gas and directly discharges, and causes heating efficiency low;
(2), the circulation of tail gas of this technique is only applicable to pure H
2as reductive agent, if contain rare gas element in gas (as N
2), working cycle meeting accumulation; If contain CO reaction process can generate CO
2, CO
2only by washing, cannot effectively remove.And can only using pure hydrogen, as reductive agent, can make the application of this technique be subject to great restriction;
(3), reduction fluidized-bed adopts periodical operation, in order to realize operate continuously, need to establish two intermediate bunkers, not only makes complex system, periodical operation also makes system production capacity be restricted;
(4), the undeclared reduced ore of this technique is realized isolated air cooling by what equipment.
The above-mentioned deficiency of existing concentrated ilmenite oxidizing roasting-reducing roasting technique, has seriously limited the development that concentrated ilmenite develops, and is badly in need of a kind of concentrated ilmenite being carried out efficient oxidation roasting and reducing roasting and makes full use of system and the technique of roasting process energy.
Summary of the invention
The invention provides a kind of concentrated ilmenite fluidization oxidizing roasting-fluidized reduction roasting system, in order to solve defect of the prior art, have reaction efficiency high, Btu utilization is abundant, and the advantage of roasting process good economy performance is applicable to extensive continuous industry and produces.
Concentrated ilmenite fluidization oxidizing roasting-fluidized reduction roasting system, comprising: feed bin, screw feeder, mulitistage cyclone, tornado dust collector, bagroom, induced draft fan, chimney, feed valve, fluidized-bed oxidation reactor, heat of oxidation wind furnace, combustion chamber, middle material valve, fluid bed reduction reactor, reduced ore bleeder valve, fluidized bed cooler, nitrogen header pipe, gas main and air main;
Described fluidized-bed oxidation reactor comprises: oxidized still, oxidized still separator, oxidized still returning charge valve and oxidized still concurrent heating burner;
Described fluid bed reduction reactor comprises: reduction furnace, reduction furnace separator, reduction furnace returning charge valve and reduction furnace concurrent heating burner;
Described fluidized bed cooler comprises: cooling bed and steam regeneration device;
The discharge port of described feed bin is connected with the opening for feed of screw feeder by pipeline, and the discharge port of described screw feeder is connected with the inlet mouth of the one-level cyclone preheater of mulitistage cyclone by pipeline;
The air outlet of the one-level cyclone preheater of described mulitistage cyclone is connected with the inlet mouth of tornado dust collector by pipeline, and the air outlet of described tornado dust collector is connected with the inlet mouth of described bagroom by pipeline; The discharge port of described tornado dust collector is connected with the inlet mouth of the one-level cyclone preheater of mulitistage cyclone by pipeline;
The air outlet of described bagroom is connected with induced draft fan by pipeline, and described induced draft fan is connected with chimney by pipeline;
The discharge port of the last step cyclone preheater of described mulitistage cyclone is connected with feed valve by pipeline, and the inlet mouth of described last step cyclone preheater is connected with the air outlet of combustion chamber and the air outlet of oxidized still separator by pipeline;
The inlet mouth of described combustion chamber is connected by pipeline with air outlet, air main and the gas main of reduction furnace separator respectively by pipeline;
The inlet mouth of described feed valve is connected with air main by pipeline, and the discharge port of described feed valve is connected with the opening for feed of oxidized still by pipeline;
The inlet mouth of described oxidized still bottom is connected with heat of oxidation wind furnace air outlet by pipeline; The air outlet at described oxidized still top is connected with oxidized still separator inlet mouth by pipeline; The discharge port of described oxidized still separator is connected with the opening for feed of oxidized still returning charge valve by pipeline, and the air outlet of described oxidized still separator is connected with last step cyclone preheater inlet mouth by pipeline; The inlet mouth of described oxidized still returning charge valve bottom is connected with air main by pipeline, and the discharge port of described oxidized still returning charge valve is connected with the returning charge mouth of oxidized still bottom by pipeline;
Described oxidized still bottom is provided with oxidized still concurrent heating burner, and the inlet mouth of described oxidized still concurrent heating burner is connected with gas main and air main respectively by pipeline;
The inlet mouth of described heat of oxidation wind furnace is connected with air main and gas main by pipeline, and the air outlet of described heat of oxidation wind furnace is connected with the inlet mouth of oxidized still bottom by pipeline;
The discharge port on described oxidized still top is connected with the opening for feed of middle material valve by pipeline;
In the middle of described, the discharge port of material valve is connected with the opening for feed of reduction furnace bottom by pipeline;
The inlet mouth of described reduction furnace is connected with the air outlet of gas main and cooling bed by pipeline; The air outlet of described reduction furnace is connected with the inlet mouth of reduction furnace separator by pipeline; The air outlet of described reduction furnace separator is connected with air inlet of combustion chamber by pipeline, and the discharge port of described reduction furnace separator bottom is connected with reduction furnace returning charge valve opening for feed by pipeline; The inlet mouth of described reduction furnace returning charge valve bottom is connected with nitrogen header pipe by pipeline, and the discharge port of described reduction furnace returning charge valve is connected with the returning charge mouth of reduction furnace by pipeline;
Described reduction furnace bottom is provided with reduction furnace concurrent heating burner, and the inlet mouth of described reduction furnace concurrent heating burner is connected with gas main and air main by pipeline respectively; The discharge port on described reduction furnace top is connected with the opening for feed of reduced ore bleeder valve by pipeline;
The inlet mouth of described reduced ore bleeder valve bottom is connected with nitrogen header pipe by pipeline, and the discharge port of described reduced ore bleeder valve is connected with the opening for feed of cooling bed by pipeline;
The inlet mouth of described cooling bed bottom is connected with gas main by pipeline, the air outlet at described cooling bed top is connected with the inlet mouth of reduction furnace by pipeline, the top of described cooling bed is provided with discharge port, roasted ore thus discharge port discharge enters leaching section, and the water cooling tube of described cooling bed inside is connected with water vapour revivifier by pipeline.
The another technology characteristics of the present invention is: described mulitistage cyclone is three grades of cyclone preheaters, comprise: one-level cyclone preheater, secondary cyclone preheater and last step cyclone preheater, the inlet mouth of described one-level cyclone preheater is connected with the air outlet of described secondary cyclone preheater by pipeline, and the discharge port of described one-level cyclone preheater bottom is connected with the inlet mouth of secondary cyclone preheater by pipeline; The inlet mouth of described secondary cyclone preheater is connected with the air outlet of last step cyclone preheater by pipeline, and the discharge port of described secondary cyclone preheater bottom is connected with the inlet mouth of last step cyclone preheater by pipeline.
The another technology characteristics of the present invention is: the worm conveyor that the bottom of described bagroom is provided with, by the discharge port of worm conveyor, send the powder of collection back to raw material cabin.
The another technology characteristics of the present invention is: by heat of oxidation wind furnace preheated air and oxidized still concurrent heating burner combustion part coal gas, provide institute's heat requirement for oxidized still, preheated air temperature is 700～1000 ℃, preferred temperature is 800～900 ℃, described oxidized still concurrent heating burner arranges 4～8, and total tolerance that described oxidized still concurrent heating burner combustion produces is no more than from oxidized still bottom and passes into 1/3 of air capacity.
The another technology characteristics of the present invention is: described reduction furnace concurrent heating burner provides institute's heat requirement by combustion parts coal gas for reduction furnace, described reduction furnace concurrent heating burner arranges 4～8, and total tolerance of producing of reduction furnace concurrent heating burner combustion is no more than from reduction furnace bottom and passes into 1/3 of coal gas amount.
Another object of the present invention has been to provide a kind of technique that adopts described concentrated ilmenite fluidization oxidizing roasting-fluidized reduction roasting system to carry out the roasting of concentrated ilmenite fluidization oxidizing roasting-fluidized reduction, comprises the following steps:
Concentrated ilmenite powder is sent in mulitistage cyclone through screw feeder by feed bin, after completing heat exchange with mixed gas from combustion chamber and oxidized still, enter feed valve, concentrated ilmenite powder enters and in oxidized still, carries out oxidizing roasting from feed valve is discharged, concentrated ilmenite powder after oxidizing roasting is discharged by centre and is expected that valve enters reduction furnace and carries out reducing roasting from oxidized still, concentrated ilmenite powder after reducing roasting is discharged from reduction furnace, through reduced ore bleeder valve, enter cooling bed cooling, then send downstream leaching section; Described reduction furnace is discharged unreacted coal gas in tail gas and is entered combustion chambers burn heat release, enters mulitistage cyclone and concentrated ilmenite powder and carry out heat exchange to reclaim heat after the hot flue gas of discharging with oxidized still separator mixes.
The another technology characteristics of the present invention is: the mode of employing combustion chambers burn reclaims the energy of unreacted inflammable gas in reduction furnace separator outlet tail gas, and mixing with the hot flue gas of discharging from oxidized still separator air outlet, by the sensible heat of mulitistage cyclone recovered flue gas.
The another technology characteristics of the present invention is: when material valve guarantees that concentrated ilmenite powder flows to reduction furnace smoothly from oxidized still in the middle of described, also can avoid air in oxidized still and the coal gas in reduction furnace to be in contact with one another.
The another technology characteristics of the present invention is: when high temperature reduction roasting breeze being cooled under isolated air atmosphere by fluidized bed cooler, reclaim the sensible heat of high-temperature roasting breeze.
The another technology characteristics of the present invention is: water coolant flows to high temperature side from the low temperature side of cooling bed in the mode of adverse current, through the water coolant of heat exchange, enters water vapour revivifier, when producing water vapour, is cooled, and water cooling tube is sent in recirculation back to.
Employing fluidized-bed provided by the invention carries out efficient oxidation roasting, reducing roasting, cooling system and the technique of roasted ore to concentrated ilmenite.Realize in the following way:
(1) high-temperature tail gas of oxidized still being discharged and cold concentrated ilmenite powder heat exchange, the sensible heat of recovery oxidizing roasting high-temperature tail gas;
(2) high-temperature tail gas of reduction furnace being discharged burns, and discharges the latent heat of unreacted inflammable gas in reducing roasting tail gas, by sensible heat and the latent heat with cold concentrated ilmenite powder heat exchange recovery reducing roasting tail gas by combustion high temperature flue gas;
(3) between high-temperature tail gas/flue gas and cold concentrated ilmenite powder, adopt three grades of cyclone preheater heat exchange;
(4) by pneumatic blow-off valve, guarantee that the high temperature concentrated ilmenite that oxidized still is discharged flows to reduction furnace smoothly, and avoid air in oxidized still and the coal gas in reduction furnace to be in contact with one another simultaneously, ensure operating safety.
(5) adopt fluidized bed cooler, in cooling reducing roasting ore deposit, reclaimed the sensible heat of roasted ore, a part is for heat reduction coal gas, and a part is for generation of process water steam.
Adopt technique of the present invention to carry out oxidizing roasting and reducing roasting to concentrated ilmenite, have reaction efficiency high, the advantages such as Btu utilization is abundant, roasting process good economy performance, are applicable to extensive continuous industry and produce.
Accompanying drawing explanation
Accompanying drawing is used to provide a further understanding of the present invention, and forms a part for specification sheets, for explaining the present invention, is not construed as limiting the invention together with embodiments of the present invention.In the accompanying drawings:
Fig. 1 is the process flow sheet that concentrated ilmenite of the present invention carries out fluidization oxidizing roasting-fluidized reduction roasting system.
By reference to the accompanying drawings, in the embodiment of the present invention, Reference numeral is as follows:
1-feed bin 2-screw feeder 3-one-level cyclone preheater
4-secondary cyclone preheater 5-last step cyclone preheater 6-feed valve
7-1-oxidized still 7-2-oxidized still separator 7-3-oxidized still returning charge valve
Material valve 9-heat of oxidation wind furnace in the middle of 7-4-oxidized still concurrent heating burner 8-
10-1-reduction furnace 10-2-reduction furnace separator 10-3-reduction furnace returning charge valve
10-4-reduction furnace concurrent heating burner 11-combustion chamber 12-reduced ore bleeder valve
13-1-cooling bed 13-2-steam regeneration device 14-tornado dust collector
15-bagroom 16-induced draft fan 17-chimney
Embodiment
For making the object, technical solutions and advantages of the present invention clearer, below in conjunction with the accompanying drawing in the embodiment of the present invention, the technical scheme in the embodiment of the present invention is clearly and completely described, obviously, described embodiment is the present invention's part embodiment, rather than whole embodiment.Embodiment based in the present invention, those of ordinary skills, not making the every other embodiment obtaining under creative work prerequisite, belong to the scope of protection of the invention.
The typical concentrated ilmenite that the Panxi Diqu vanadium titano-magnetite of take obtains through ore dressing is narrated implementation process of the present invention as raw material, and the typical size of Panxi Diqu concentrated ilmenite distributes in Table 1, classical group becomes in Table 2.
Table 1. Panxi Diqu typical case concentrated ilmenite size-grade distribution
Table 2. Panxi Diqu typical case concentrated ilmenite typical case composition
| Form | CaO | Fe 2O 3 | FeO | MgO | MnO | SiO 2 | TiO 2 |
| wt％ | 0.95 | 5.62 | 35.74 | 6.50 | 0.63 | 3.65 | 46.91 |
Refer to Fig. 1 (solid materials stream that wherein filled arrows represents, hollow arrow represents gas material stream), the disclosed concentrated ilmenite of the present embodiment carries out fluidization oxidizing roasting-fluidized reduction roasting system, by feed bin 1, screw feeder 2, comprise one-level cyclone preheater 3, the mulitistage cyclone that secondary cyclone preheater 4 and last step cyclone preheater 5 form, feed valve 6, by oxidized still 7-1, oxidized still separator 7-2, the fluidized-bed oxidation reactor that oxidized still returning charge valve 7-3 and oxidized still concurrent heating burner 7-4 form, middle material valve 8, heat of oxidation wind furnace 9, by reduction furnace 10-1, reduction furnace separator 10-2, the fluid bed reduction reactor that reduction furnace returning charge valve 10-3 and reduction furnace concurrent heating burner 10-4 form, combustion chamber 11, reduced ore bleeder valve 12, fluidized bed cooler by cooling bed 13-1 and steam regeneration device 13-2 combination, tornado dust collector 14, bagroom 15, induced draft fan 16, chimney 17 combines.
The discharge port of feed bin 1 is connected with the opening for feed of screw feeder 2 by pipeline, and the discharge port of screw feeder 2 is connected with the inlet mouth of the one-level cyclone preheater 3 of mulitistage cyclone by pipeline;
The air outlet of the one-level cyclone preheater 3 of mulitistage cyclone is connected with the inlet mouth of tornado dust collector 14 by pipeline, and the air outlet of tornado dust collector 14 is connected with the inlet mouth of bagroom 15 by pipeline; The discharge port of tornado dust collector 14 is connected with the inlet mouth of the one-level cyclone preheater 3 of mulitistage cyclone by pipeline;
The air outlet of bagroom 15 is connected with induced draft fan 16 by pipeline, and induced draft fan 16 is connected with chimney 17 by pipeline;
The discharge port of the last step cyclone preheater of mulitistage cyclone is connected with feed valve by pipeline, and the inlet mouth of last step cyclone preheater 5 is connected with the air outlet of combustion chamber 11 and the air outlet of oxidized still separator 7-2 by pipeline;
The inlet mouth of combustion chamber 11 is connected by pipeline with air outlet, air main and the gas main of reduction furnace separator 10-2 respectively by pipeline;
The inlet mouth of feed valve 6 is connected with air main by pipeline, and the discharge port of feed valve 6 is connected with the opening for feed of oxidized still 7-1 by pipeline;
The inlet mouth of oxidized still 7-1 bottom is connected with the air outlet of heat of oxidation wind furnace 9 by pipeline; The air outlet at oxidized still 7-1 top is connected with the inlet mouth of oxidized still separator 7-2 by pipeline; The discharge port of oxidized still separator 7-2 is connected with the opening for feed of oxidized still returning charge valve 7-3 by pipeline, and the air outlet of oxidized still separator 7-2 is connected with last step cyclone preheater 5 inlet mouths by pipeline; The inlet mouth of oxidized still returning charge valve 7-3 bottom is connected with air main by pipeline, and the discharge port of oxidized still returning charge valve 7-3 is connected with the returning charge mouth of oxidized still 7-1 bottom by pipeline;
Oxidized still 7-1 bottom is provided with 4 (only having drawn 1 in figure for simplicity) oxidized still concurrent heating burner 7-4, and the inlet mouth of oxidized still concurrent heating burner 7-4 is connected with gas main and air main respectively by pipeline; The discharge port on oxidized still 7-1 top is connected with the opening for feed of middle material valve 8 by pipeline;
The inlet mouth of heat of oxidation wind furnace 9 is connected with air main and gas main by pipeline, and the air outlet of heat of oxidation wind furnace 9 is connected with the inlet mouth of oxidized still 7-1 bottom by pipeline;
The discharge port of middle material valve 8 is connected with the opening for feed of reduction furnace 10-1 bottom by pipeline;
The inlet mouth of reduction furnace 10-1 is connected with the air outlet of gas main and cooling bed 13-1 by pipeline; The air outlet of reduction furnace 10-1 is connected with the inlet mouth of reduction furnace separator 10-2 by pipeline; The air outlet of reduction furnace separator 10-2 is connected with combustion chamber 11 inlet mouths by pipeline, and the discharge port of reduction furnace separator 10-2 bottom is connected with reduction furnace returning charge valve 10-3 opening for feed by pipeline; The inlet mouth of reduction furnace returning charge valve 10-3 bottom is connected with nitrogen header pipe by pipeline, and the discharge port of reduction furnace returning charge valve 10-3 is connected with the returning charge mouth of reduction furnace by pipeline;
Reduction furnace 10-1 bottom is provided with 4 (only having drawn 1 in figure for simplicity) reduction furnace concurrent heating burner 10-4, and the inlet mouth of reduction furnace concurrent heating burner 10-4 is connected with air main with gas main by pipeline respectively; The discharge port on reduction furnace 10-1 top is connected with the opening for feed of reduced ore bleeder valve 10-3 by pipeline;
The inlet mouth of reduced ore bleeder valve 12 bottoms is connected with nitrogen header pipe by pipeline, and the discharge port of reduced ore bleeder valve 12 is connected with the opening for feed of cooling bed 13-1 by pipeline;
The inlet mouth of cooling bed 13-1 bottom is connected with gas main by pipeline, the air outlet at cooling bed 13-1 top is connected with the inlet mouth of reduction furnace 10-1 by pipeline, cooling bed 13-1 top is provided with discharge port, roasted ore thus discharge port discharge enters leaching section, and the water cooling tube of cooling bed 13-1 inside is connected with steam regeneration device 13-2 by pipeline.
Adopt above-mentioned concentrated ilmenite to carry out the technique that fluidization oxidizing roasting-fluidized reduction roasting system carries out concentrated ilmenite fluidization oxidizing roasting-reducing roasting, comprise the following steps: above-mentioned climbing after western concentrated ilmenite powder enters screw feeder 2 with the speed of 1.7 tons/hour by feed bin 1 sent into one-level cyclone preheater 3, and the concentrated ilmenite powder of carrying secretly in one-level cyclone preheater 3 air outlets returns to the inlet mouth of one-level cyclone preheater 3 after tornado dust collector 14 are collected, concentrated ilmenite powder enters secondary rotary wind preheater 4 from the discharge port of one-level cyclone preheater 3 bottoms is discharged, in last step cyclone preheater 5, after completing heat exchange, the tail gas of discharging with combustion chamber 11 and oxidized still separator 7-2 enters feed valve 6, from feed valve 6 is discharged, enter and in oxidized still 7-1, carry out oxidizing reaction, the powder of carrying secretly in oxidized still Exhaust Gas is after oxidized still separator 7-2 collects, by oxidized still returning charge valve, 7-3 returns in oxidized still 7-1, the average oxidization time of concentrated ilmenite is controlled at 0.5 hour, well-oxygenated concentrated ilmenite is discharged from oxidized still 7-1 upper part discharge port, through centre material valve 8, enter reduction furnace 10-1 and carry out reduction reaction, the powder of carrying secretly in reduction furnace 10-1 Exhaust Gas is collected through reduction furnace separator 10-2, by reduction furnace returning charge valve, 10-3 returns in reduction furnace 10-1, the average recovery time of concentrated ilmenite is controlled at 1.0 hours, concentrated ilmenite after reduction is discharged from reduction furnace 10-1 upper part discharge port, through reduced ore bleeder valve 12, enter in cooling bed 13-1 cooling, from the discharge port on cooling bed 13-1 top, discharge.
Pressurized air 300Nm
3/ h enters heat of oxidation wind furnace 9 from air main, coke-oven gas 20Nm
3/ h burns from gas main enters the burner of heat of oxidation wind furnace 9 together with air, the preheated air that forms 950 ℃ of left and right is discharged from heat of oxidation wind furnace 9 air outlets, from bottom, enter oxidized still 7-1, under fluidized state, carry out oxidizing reaction with concentrated ilmenite wherein; Coke-oven gas and air enter respectively 4 oxidized still concurrent heating burner 7-4 of circumferentially equidistant arrangement through connecting tube from gas main and air main, and each burner passes into 3Nm
3the coke-oven gas of/h and 18Nm
3/ h air, makes oxidized still temperature maintain 1000 ℃ by burning for oxidized still provides heat, and oxidized still 7-1 outlet tail gas enters the inlet mouth of last step cyclone preheater 5 after oxidized still separator 7-2 dedusting; Coke-oven gas 120Nm
3/ h enters reduction furnace 10-1, another road coke-oven gas 120Nm from bottom through connecting tube from gas main
3/ h enters cooling bed 13-1 from bottom through gas main, when the high temperature concentrated ilmenite of reduction is fluidized in cooling bed 13-1, coke-oven gas is heated to 150 ℃, from cooling bed 13-1 top, discharge, through connecting tube, also from bottom, enter reduction furnace 10-1, coke-oven gas and air enter respectively circumferentially 4 equidistant reduction furnace concurrent heating burner 10-4 from gas main and air main through connecting tube, and each burner passes into 12Nm
3the coke-oven gas of/h and 6Nm
3the air of/h, makes reduction furnace temperature maintain 750 ℃ by burning for reduction furnace provides heat, and reduction furnace 10-1 discharges tail gas after reduction furnace separator 10-2 dedusting and from the next coke-oven gas 10Nm of house steward
3/ h and the air 700Nm coming from air main
3/ h enters combustion chamber burner burning together, produce the high-temperature flue gas of 1200 ℃ of temperature first through last step cyclone preheater 5, again through secondary cyclone preheater 4 and one-level cyclone preheater 3, when flue gas is cooled to 200 ℃ of left and right, concentrated ilmenite is by stepped heating to 700 ℃ left and right; Flue gas enters tornado dust collector 14 dedustings from discharge at one-level cyclone preheater 3 tops, then enters after bagroom 15 dedustings, emptying through induced draft fan 16, chimney 17.
Described in table 1 and table 2, climb western concentrated ilmenite after the above-mentioned technique oxidizing roasting of the present invention, Fe in concentrated ilmenite
2o
3it is 1.83% that content reaches 41.45%, FeO content, and ferrous oxidation ratio reaches 94.87%; Fe in concentrated ilmenite after above-mentioned reduction
2o
3content is 2.92%, FeO content 38.29%, and ferric reduction ratio has reached 93.20%.The roasted ore obtaining through oxidation-reduction in 20% concentration HCl 105 ℃ leach 4 hours, obtain TiO in artificial rutile
2grade reaches 91.14%, and it is only 1.07% that calcium oxide and magnesium oxide amount to content, and the Pulverization ratio of product is below 2%.
Finally it should be noted that: above embodiment only, in order to technical scheme of the present invention to be described, is not intended to limit; Although the present invention is had been described in detail with reference to previous embodiment, those of ordinary skill in the art is to be understood that: its technical scheme that still can record aforementioned each embodiment is modified, or part technical characterictic is wherein equal to replacement; And these modifications or replacement do not make the essence of appropriate technical solution depart from the spirit and scope of various embodiments of the present invention technical scheme.
Claims (10)
1. concentrated ilmenite fluidization oxidizing roasting-fluidized reduction roasting system, is characterized in that, comprising: feed bin, screw feeder, mulitistage cyclone, tornado dust collector, bagroom, induced draft fan, chimney, feed valve, fluidized-bed oxidation reactor, heat of oxidation wind furnace, combustion chamber, middle material valve, fluid bed reduction reactor, reduced ore bleeder valve, fluidized bed cooler, nitrogen header pipe, gas main and air main;
Described fluidized-bed oxidation reactor comprises: oxidized still, oxidized still separator, oxidized still returning charge valve and oxidized still concurrent heating burner;
Described fluid bed reduction reactor comprises: reduction furnace, reduction furnace separator, reduction furnace returning charge valve and reduction furnace concurrent heating burner;
Described fluidized bed cooler comprises: cooling bed and steam regeneration device;
The discharge port of described feed bin is connected with the opening for feed of screw feeder by pipeline, and the discharge port of described screw feeder is connected with the inlet mouth of the one-level cyclone preheater of mulitistage cyclone by pipeline;
The air outlet of the one-level cyclone preheater of described mulitistage cyclone is connected with the inlet mouth of tornado dust collector by pipeline, and the air outlet of described tornado dust collector is connected with the inlet mouth of described bagroom by pipeline; The discharge port of described tornado dust collector is connected with the inlet mouth of the one-level cyclone preheater of mulitistage cyclone by pipeline;
The air outlet of described bagroom is connected with induced draft fan by pipeline, and described induced draft fan is connected with chimney by pipeline;
The discharge port of the last step cyclone preheater of described mulitistage cyclone is connected with the opening for feed of feed valve by pipeline, and the inlet mouth of described last step cyclone preheater is connected with the air outlet of combustion chamber and the air outlet of oxidized still separator by pipeline;
The inlet mouth of described combustion chamber is connected by pipeline with air outlet, air main and the gas main of reduction furnace separator respectively by pipeline;
The inlet mouth of described feed valve is connected with air main by pipeline, and the discharge port of described feed valve is connected with the opening for feed of oxidized still by pipeline;
The inlet mouth of described oxidized still bottom is connected with heat of oxidation wind furnace air outlet by pipeline; The air outlet at described oxidized still top is connected with oxidized still separator inlet mouth by pipeline; The discharge port of described oxidized still separator is connected with the opening for feed of oxidized still returning charge valve by pipeline, and the air outlet of described oxidized still separator is connected with last step cyclone preheater inlet mouth by pipeline; The inlet mouth of described oxidized still returning charge valve bottom is connected with air main by pipeline, and the discharge port of described oxidized still returning charge valve is connected with the returning charge mouth of oxidized still bottom by pipeline;
Described oxidized still bottom is provided with oxidized still concurrent heating burner, and the inlet mouth of described oxidized still concurrent heating burner is connected with gas main and air main respectively by pipeline;
The inlet mouth of described heat of oxidation wind furnace is connected with air main and gas main by pipeline, and the air outlet of described heat of oxidation wind furnace is connected with the inlet mouth of oxidized still bottom by pipeline;
The discharge port on described oxidized still top is connected with the opening for feed of middle material valve by pipeline;
In the middle of described, the discharge port of material valve is connected with the opening for feed of reduction furnace bottom by pipeline;
The inlet mouth of described reduction furnace is connected with the air outlet of gas main and cooling bed by pipeline; The air outlet of described reduction furnace is connected with the inlet mouth of reduction furnace separator by pipeline; The air outlet of described reduction furnace separator is connected with air inlet of combustion chamber by pipeline, and the discharge port of described reduction furnace separator bottom is connected with reduction furnace returning charge valve opening for feed by pipeline; The inlet mouth of described reduction furnace returning charge valve bottom is connected with nitrogen header pipe by pipeline, and the discharge port of described reduction furnace returning charge valve is connected with the returning charge mouth of reduction furnace by pipeline;
Described reduction furnace bottom is provided with reduction furnace concurrent heating burner, and the inlet mouth of described reduction furnace concurrent heating burner is connected with air main with gas main by pipeline respectively; The discharge port on described reduction furnace top is connected with the opening for feed of reduced ore bleeder valve by pipeline;
The inlet mouth of described reduced ore bleeder valve bottom is connected with nitrogen header pipe by pipeline, and the discharge port of described reduced ore bleeder valve is connected with the opening for feed of cooling bed by pipeline;
The inlet mouth of described cooling bed bottom is connected with gas main by pipeline, the air outlet at described cooling bed top is connected with the inlet mouth of reduction furnace by pipeline, described cooling bed top is provided with discharge port, roasted ore is discharged and is entered downstream leaching section through this discharge port, and the water cooling tube of described cooling bed inside is connected with water vapour revivifier by pipeline.
2. system according to claim 1, it is characterized in that: described mulitistage cyclone is three grades of cyclone preheaters, comprise: one-level cyclone preheater, secondary cyclone preheater and last step cyclone preheater, the inlet mouth of described one-level cyclone preheater is connected with the air outlet of described secondary cyclone preheater by pipeline, and the discharge port of described one-level cyclone preheater bottom is connected with the inlet mouth of secondary cyclone preheater by pipeline; The inlet mouth of described secondary cyclone preheater is connected with the air outlet of last step cyclone preheater by pipeline, and the discharge port of described secondary cyclone preheater bottom is connected with the inlet mouth of last step cyclone preheater by pipeline.
3. system according to claim 1, is characterized in that: the worm conveyor that the bottom of described bagroom is provided with, by the discharge port of worm conveyor, send the powder of collection back to raw material cabin.
4. system according to claim 1, it is characterized in that: by heat of oxidation wind furnace preheated air and oxidized still concurrent heating burner combustion part coal gas, provide institute's heat requirement for oxidized still, the temperature of preheated air is 700～1000 ℃, described oxidized still concurrent heating burner arranges 4～8, and total tolerance that described oxidized still concurrent heating burner combustion produces is no more than from oxidized still bottom and passes into 1/3 of air capacity.
5. system according to claim 1, it is characterized in that: described reduction furnace concurrent heating burner provides institute's heat requirement by combustion parts coal gas for reduction furnace, described reduction furnace concurrent heating burner arranges 4～8, and total tolerance of producing of reduction furnace concurrent heating burner combustion is no more than from reduction furnace bottom and passes into 1/3 of coal gas amount.
6. one kind is utilized the technique that system is carried out the roasting of concentrated ilmenite fluidization oxidizing roasting-fluidized reduction described in claim 1～5 any one, it is characterized in that, comprise the following steps: concentrated ilmenite powder is sent in mulitistage cyclone through screw feeder by feed bin, after completing heat exchange with mixed gas from combustion chamber and oxidized still separator, enter feed valve, concentrated ilmenite powder enters and in oxidized still, carries out oxidizing roasting from feed valve is discharged, concentrated ilmenite powder after oxidizing roasting is discharged by centre and is expected that valve enters reduction furnace and carries out reducing roasting from oxidized still, concentrated ilmenite powder after reducing roasting is discharged from reduction furnace, through reduced ore bleeder valve, enter cooling bed cooling, then send downstream leaching section, described reduction furnace is discharged unreacted coal gas in tail gas and is entered combustion chambers burn heat release, enters mulitistage cyclone and concentrated ilmenite powder and carry out heat exchange to reclaim heat after the hot flue gas of discharging with oxidized still separator mixes.
7. technique according to claim 6, it is characterized in that: the mode of employing combustion chambers burn reclaims the energy of unreacted inflammable gas in reduction furnace separator outlet tail gas, and mixing with the hot flue gas of discharging from oxidized still separator air outlet, by the sensible heat of mulitistage cyclone recovered flue gas.
8. technique according to claim 6, is characterized in that: when material valve guarantees that concentrated ilmenite powder flows to reduction furnace smoothly from oxidized still in the middle of described, also can avoid air in oxidized still and the coal gas in reduction furnace to be in contact with one another.
9. technique according to claim 6, is characterized in that: when high temperature reduction roasting breeze being cooled under isolated air atmosphere by fluidized bed cooler, reclaim the sensible heat of high temperature reduction roasting breeze.
10. technique according to claim 6, it is characterized in that: water coolant flows to high temperature side from the low temperature side of cooling bed in the mode of adverse current, water coolant through heat exchange enters water vapour revivifier, when producing water vapour, is cooled, and water cooling tube is sent in recirculation back to.
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