CN106319126A

CN106319126A - System and method for vanadium titano-magnetite fluidization oxidation and reduction

Info

Publication number: CN106319126A
Application number: CN201610862732.0A
Authority: CN
Inventors: 孙昊延; 朱庆山; 潘锋; 王珍
Original assignee: Institute of Process Engineering of CAS
Current assignee: Institute of Process Engineering of CAS
Priority date: 2016-09-28
Filing date: 2016-09-28
Publication date: 2017-01-11
Anticipated expiration: 2036-09-28
Also published as: CN106319126B

Abstract

The invention discloses a system and a method for vanadium titano-magnetite fluidization oxidation and reduction. A four-section fluidized bed is adopted to carry out fluidization oxidation and reduction on vanadium titano-magnetite fine ore; and a fluidized bed reaction body is formed by boiling beds connected in series. Through the technological design of a pre-oxidation treatment and low-gas-velocity reaction fluidized bed, the vanadium titano-magnetite powder fluidization performance can be obviously improved, the reaction efficiency is improved, and the process energy consumption is reduced. The vanadium titano-magnetite fine ore is firstly preheated and dried, enters a low-temperature oxidation bed so as to be subjected to oxidation treatment, then enters a prereduction bed so as to be subjected to prereduction, and finally complete final reduction through a two-stage high-temperature final reduction bed; oxidization tail gas is used for preheating and drying the vanadium titano-magnetite fine ore; after reduction tail gas is heat-exchanged with oxidization air, oxidization components are cleaned and removed, and the reduction tail gas is recycled; and a gas utilization scheme has the advantages of high reaction efficiency and high energy utilization ratio.

Description

A kind of for the redox system and method for vanadium titano-magnetite fluidization

Technical field

The invention belongs to the relevant chemical industry of vanadium titano-magnetite, field of metallurgy, be specifically related to a kind of vanadium titano-magnetite fine ore stream The redox system and method for stateization.

Background technology

Vanadium, titanium are universally acknowledged scarce resource and grand strategy material, the vanadium reserves in the whole world about 98% and the titanium of 91% Reserves are composed and are stored in the complex mineral based on vanadium titano-magnetite.It is said that in general, the low (TiO of vanadium titano-magnetite titaniferous grade₂< 14wt.%), mainly as blast furnace raw material smelt iron, vanadium, and need to dilute with addition of common iron mine, finally because of TiO in blast furnace slag₂Rich Intensity low (～22wt.%), titaniferous thing complicated (Ti mutually_xO_y, Ti (C, N)), particle size distribution tiny (< 10um), it is difficult to reclaim wherein Titanium resource.The molten method abbreviated system in two steps of the direct-reduction-electric furnace proposed in recent years, is taking into account long flow process smelt iron, vanadium Element simultaneously, in conjunction with Low Temperature Solid-Phase prereduction, can be smelted by V-Ti-magnetite, improve TiO in follow-up melting slag₂Content in Titanium slag grade (> 50wt.%), thus meet titanium slag upgrading upgrading and have valency to utilize demand, finally realize Fe, V, Ti valuable element Comprehensive utilizes.

First step technique direct-reduction in two-step method short route belongs to non-blast furnace ironmaking technique, and this technique has and do not uses The advantages such as coke, pollutant emission are low, are that instead of the developing direction of traditional high furnace superintendent flow process ironmaking scheme.According to being used reduction Agent is sorted out, and non-blast furnace DRI oxide process is divided into two kinds of the gentle base of coal base.Coal base technique has rotary kiln, rotary hearth furnace Deng, gas base technique has shaft furnace, fluid bed etc..Comparing coal base technique, gas base technique has temperature and operates low, the high spy of reaction efficiency Point, using reducibility gas particularly without use coal is reducing agent, and cleaning reduction advantage highlights, and is main direct-reduction Technique.Specifically for reactor angle, gas base flow fluidized bed reactor has and directly processes that fine ore, heat and mass be good, reduction effect The high outstanding advantages of rate, thus be considered as ideal efficient iron ore direct reducing reactor, main representative technique FIOR, Circored, FINMET etc. are had to carry out pilot scale or industrialization practice.

FIOR technique is developed by Exxon research and engineering company, with hydrogen-rich gas (H₂～85vol%) it is reducing agent, adopt Connecting with level Four fluid bed, the first order is preheated fluidification bed, and latter three grades is reduction fluid bed (US 5082251, US 5192486).Within 1976,400,000 tons/year of commercial plants are built up at Venezuela Puerto Ordaz.High grade iron fine ore is by one Level fluid bed sequentially enters to fourth stage fluid bed.First order preheated fluidification sheet solely uses natural gas or coal gas and air burning After heat smoke, temperature is 780 DEG C, gas speed 0.8m/s.Being entered by fourth stage fluid bed after reducing gases is heated, adverse current is to second Level fluid bed, centre is no longer heat up.Second and third, four reduction fluid beds temperature be respectively 700 DEG C, 780 DEG C, 790 DEG C, reduction Gas speed 1m/s, resultant metal rate～90%.Use hydrogen rich gas can reduce high temperature height degree of metalization in fine iron ore reduction process to glue Knot defluidization situation occurs, and is also suitably added antitack agent to control fluidized state during reduction simultaneously.

Circored technique is developed by Lu Qi Usiminas, using hydrogen as single reducing agent, uses two-step fluidized bed string Connection reduction, including a circulating fluid bed reactor and a bubbling fluidized bed reactor (horizontal transverse multi-section) (US5603748, US5833734).1996 have built up hot wafering production capacity first at Trinida Trinidad is 500,000 t/a's Factory.First the thin fine iron ore of 0.1-1mm is heated to 800 DEG C, subsequently in recycle stream in the preheater of fluid bed by this technique Fluidized bed reactor is reduced to degree of metalization 70%, enters back into bubbling fluidized bed reactor and is reduced to degree of metalization 92%.Wherein follow Ring fluid bed gas speed 4-6m/s, response time 20-30min, reaction temperature 850-900 DEG C, bubbling fluidized bed gas speed 0.5-0.6m/ S, response time 45-240min, reaction temperature 630 DEG C.Although first paragraph recirculating fluidized bed reaction efficiency is high, fine ore soap-free emulsion polymeization, But required high cycle speed.Used by second segment, gas speed is low, but it is low to consider that bonding defluidization controls whole reduction temperature, and reduction efficiency is low unavoidably.

FINMET technique is developed jointly with FIOR company by VAI, with natural gas conversion gas as reducing agent, uses level Four Turbulent Flow Type fluid bed is connected, without preheating fluid bed (US6569377).Within 1999, build up 500,000 in BHP DRI company of Australia Ton/year commercial plant.First fine iron ore enters back into fluid bed reduction after preheater stokehold is preheated to 100 DEG C.The first order is reduced Fluidized-bed temperature is about 550 DEG C, and temperature steps up, and fourth stage reduction fluidized-bed temperature reaches about 800 DEG C, finished product metal Rate～93%.Need during reduction to prevent fine ore reduction bonding defluidization by increase granularity (limiting 12mm) and addition antitack agent Generation.

In recent years, development based on direct reduction processes of Iron ores, many v-ti magnetites combining difference direct-reduction technique Ore deposit two-step method short route scheme is developed.Part direct-reduction technique have employed what coal base pelletizing or gas base pelletizing reduced Method, joins carbon rotary hearth furnace direct reduction process (CN 1641045A), Panzhihua Iron and Steel Group in designing such as Sichuan Long Mang group The carbon-burdened pellet high-temperature direct reduction method (CN 1814813A, CN 104862441A) of design, Chongqing steel enterprise, middle smelting Schreyerite acid pellet shaft kiln directly reduced method (CN 103451419A, the CN of engineering company of CCID design 102424876A, CN 103255255A) etc., these methods are required for entering back into after vanadium titano-magnetite fine ore pelletizing in advance also Former reactor, inside joining carbon method also needs coal blending pelletizing.And coal blending can introduce coal non-ferrous impurities, reduce in follow-up melting slag TiO₂Grade, gas base pelletizing then adds reducing gases heat and mass resistance, reduces gas base directly reducing efficiency.

Also some schemes are had to apply fine ore fluidized bed gas base directly reducing technology method.As patent CN 102127611A, Patent CN 202007243U etc. proposes the scheme using thtee-stage shiplock fluid bed direct-reduction v-ti magnetite fine ore, through stokehold After preheating, temperature is that the v-ti magnetite fine ore of 600-700 DEG C sequentially enters one-level, two grades and three grades of reduction fluid beds, reverse On reducing gas effect under, it is achieved reduction reaction is concurrently given birth in fluidization.Reduction temperature is between 650-850 DEG C, and preheating is situated between Matter is reduction tail gas.The fine ore fluidized bed gas base directly reducing technology of these vanadium titano-magnetites typically directly uses similar non-blast furnace to refine The multi-stage series fluid bed scheme of ferrum FIOR, Circored, FINMET, or stokehold tail gas pre-heating system is set before fluid bed, Only for the purpose of drying and dehydrating and simple raising fine ore charging temperature, with common iron ore concentrate fluid bed gas in mineral reaction principle Base directly reducing is identical, does not take into full account vanadium titano-magnetite self mineralogical character, the most do not solve high temperature height reduction efficiency with Contradiction between contingent fine ore high temperature height degree of metalization.

To sum up, in conjunction with mineralogical character, by technique and technological innovation, on the premise of not introducing external antitack agent, reduce Fine ore fluidized bed operating gas velocity, improves goods fluid reducing property, ensures high temperature height reduction efficiency simultaneously, is to realize reducing fluidisation Bed reduction vanadium titano-magnetite process energy consumption, improves the key of economy.

Summary of the invention

It is an object of the invention to provide a kind of vanadium titano-magnetite redox system and method for fine ore fluidization, pass through These apparatus and method can realize vanadium titano-magnetite fine ore oxidation-treated after by while high temperature height reduction efficiency, reduce fine ore Fluidized bed process gas speed also avoids exogenous impurity to introduce.

The invention provides a kind of for the redox system of vanadium titano-magnetite fluidization, described system includes fine ore material Storehouse and feeder, fine ore preheater 1, oxidation bed 2, prereduction bed 3, several whole reduction bed unit and product feed bins 6；

Described fine ore preheater 1 includes several cyclone separator and several oxidation bed feeders, in ore fines feed bin Fine ore enters oxidation bed 2 by oxidation bed feeder after feeder enters cyclone separator circulation preheating and separates.Described ore deposit Powder preheater can realize vanadium titano-magnetite fine ore through cyclone separator with from the oxidation of oxidation bed cyclone separator gas outlet The breeze that after tail gas preheating, the particle diameter thickness that obtains is different enters oxidation bed body.

Described oxidation bed 2 includes aoxidizing fluid bed body 20, oxidation bed gas heater 21, oxidation bed the first discharger 22, oxidation bed the second discharger 23 and oxidation bed cyclone separator 24, the bottom discharging opening of described oxidation bed cyclone separator 24 Connect with described oxidation bed the second discharger 23；Described oxidation bed the first discharger 22 and oxidation bed the second discharger 23 and first The charging aperture of level reduction bed connects；Oxidation bed offgas outlet is connected 1 with fine ore preheater.Mineral powder granular quilt in described oxidation bed 2 Fluidization high-temperature oxydation, obtain after oxidation coarse granule fine ore be directly entered prereduction fluid bed body, obtain after oxidation Fine grained fine ore oxidized bed cyclone separator enters prereduction fluid bed body after separating.

Described prereduction bed 3 includes prereduction fluid bed body 30, prereduction bed the first discharger 32, prereduction bed second Discharger 33 and prereduction bed cyclone separator 34；The reduction of prereduction bed the first discharger 32 and first order reduction bed unit eventually The charging aperture of bed connects, and prereduction bed cyclone separator 34 and prereduction bed the second discharger 33 connect, described prereduction bed the The charging aperture of the reduction bed of two dischargers 33 and first order reduction bed unit eventually connects.Through prereduction fluid bed in prereduction bed 3 Coarse granule fine ore after prereduction is directly entered the first order eventually reduction bed unit, after prereduction after fine grained fine ore through prereduction Bed cyclone separator enters first order reduction fluid bed body eventually after separating.

The described bed unit of reduction eventually includes whole fluid bed body, eventually reduction bed gas heater, eventually the reduction bed first of reducing Discharger, eventually reduction bed the second discharger and eventually reduction bed cyclone separator；The discharging opening of the described bed cyclone separator of reduction eventually Connecting with reduction bed the second discharger eventually, described whole reduction bed the first discharger connects with the charging aperture of next stage reduction bed unit eventually Connecing, described bed the second discharger of reduction eventually is connected with the charging aperture of next stage reduction bed unit eventually, afterbody reduction sheet eventually Bed the first discharger that reduces the end of unit is connected with feed bin with reduction bed the second discharger eventually；The gas of reduction bed cyclone separator eventually The gas access of the reduction bed gas heater of outlet and previous stage reduction bed unit eventually connects, the gas of described prereduction bed 3 The bed cyclone separator gas exit line that reduces the end of inlet duct and first order reduction bed unit eventually connects.Fine ore is through the most also In former bed after high temperature reduction, coarse granule is directly expelled to next stage eventually reduction fluid bed body by reducing bed body eventually, thin Grain is discharged into next stage reduction fluid bed body eventually after cyclone separator separates；The reduction fine ore of the reduction bed of afterbody Entering product feed bin after discharge, eventually reduction bed cyclone separator expellant gas reduces sheet as after heated as upper level The reproducibility unstrpped gas of unit, first order reduction bed cyclone separator expellant gas is former as the reproducibility of prereduction bed unit Material gas.

As the basic skill of those skilled in the art, the number of the cyclone separator arranged in breeze preheater 1 and The number of oxidation bed feeder can change according to practical situation.

Preferably, described fine ore preheater 1 includes first order cyclone separator 11, second level cyclone separator the 12, the 3rd Level cyclone separator 13, oxidation bed the first feeder 14 and oxidation bed the second feeder 15；

Going out of the first order cyclone separator 11 of the discharging opening of described ore fines feed bin and feeder and described fine ore preheater 1 QI KOU is connected, and the bottom discharge mouth of described first order cyclone separator 11 is connected with the charging aperture of oxidation bed feeder 14, The gas outlet of described first order cyclone separator 11 is connected with the entrance of second level cyclone separator 12；

The bottom discharge mouth of described second level cyclone separator 12 is connected with the entrance of first order cyclone separator 11, institute The entrance of the gas outlet and third-stage cyclone separator 13 of stating second level cyclone separator 12 is connected；

The bottom discharge mouth of described third-stage cyclone separator 13 is connected with the charging aperture of oxidation bed feeder 15, described The gas outlet of third-stage cyclone separator 13 is connected with external vent gas treatment facility；

Oxidation bed first feeder 14 of described fine ore preheater 1 and the discharging opening of oxidation bed the second feeder 15 are with described The charging aperture of the oxidation fluid bed body 20 of oxidation bed 2 is connected；The gas outlet of described oxidation bed cyclone separator 24 is with described The entrance of the first order cyclone separator 11 of fine ore preheater 1 is connected.

Preferably, the giving vent to anger of the bottom air inlet of described oxidation fluid bed body 20 and described oxidation bed gas heater 21 Mouth is connected, and the gas outlet, top of described oxidation fluid bed body 20 is connected with the entrance of described oxidation bed cyclone separator 24 Connecing, the discharging opening of described oxidation fluid bed body 20 is connected with the charging aperture of described oxidation bed the first discharger 22, described oxygen The bottom discharge mouth changing bed cyclone separator 24 is connected with the charging aperture of described oxidation bed the second discharger 23；

The discharging opening of described oxidation bed the first discharger 22 and described oxidation bed the second discharger 23 and prereduction fluid bed The charging aperture of body 30 is connected.

The gas heater of oxidation bed can be provided source of the gas by external combustion gas herein.

Preferably, the whirlwind of the bottom air inlet of described prereduction fluid bed body 30 and first order reduction bed unit eventually divides It is connected from the gas outlet of device, the gas outlet, top of described prereduction fluid bed body 30 and described prereduction bed cyclone separator The entrance of 34 is connected, the discharging opening of described prereduction fluid bed body 30 and the charging of described prereduction bed the first discharger 32 Mouth is connected；The bottom discharge mouth of described prereduction bed cyclone separator 34 and the charging of described prereduction bed the second discharger 33 Mouth is connected.

Preferably, described the first whole reduction bed unit 4 He is included for the redox system of vanadium titano-magnetite fluidization Second whole reduction bed unit 5, described first eventually reduction bed unit 4 include one-level reduction fluid bed body 40, one-level reduction eventually eventually Bed gas heater 41, one-level reduction bed the first discharger 42, one-level reduction bed the second discharger 43 eventually eventually and one-level reduction eventually Bed cyclone separator 44, described second eventually reduction bed unit 5 include two grades of reduction fluid bed bodies 50, two grades reduction bed gas eventually eventually Body heater 51, two grades reduction bed the first discharger 52, two grades reduction bed the second discharger 53 eventually eventually and two grades of reduction bed rotations eventually Wind separator 54；

The discharging opening of described prereduction bed the first discharger 32 and prereduction bed the second discharger 33 and one-level reduction stream eventually The charging aperture changing bed body 40 is connected, and the bottom air inlet of described one-level reduction fluid bed body 40 eventually is with described one-level the most also The gas outlet of former bed gas heater 41 is connected, the gas outlet, top and described of described one-level reduction fluid bed body 40 eventually The entrance of level reduction bed cyclone separator 44 eventually is connected, the discharging opening and described of described one-level reduction fluid bed body 40 eventually The charging aperture of level reduction bed discharger 42 eventually is connected；

The bottom discharge mouth of described one-level reduction bed cyclone separator 44 eventually and described one-level reduction bed the second discharger eventually The charging aperture of 43 is connected；The air inlet of described one-level reduction bed gas heater 41 eventually divides with described two grades of whole reduction bed whirlwind It is connected from the gas outlet of device 54；

The discharging opening of described one-level reduction bed the first discharger 42 eventually and one-level reduction bed the second discharger 43 eventually is with described The charging apertures of two grades of whole reduction fluid bed bodies 50 are connected, described two grades eventually reduction fluid bed bodies 50 bottom air inlet with The gas outlet of described two grades of whole reduction bed gas heaters 51 is connected, and the tops of described two grades of whole reduction fluid bed bodies 50 go out QI KOU is connected with the entrance of described level two grades reduction bed cyclone separator 54 eventually, described two grades of whole reduction fluid bed bodies 50 Discharging opening is connected with the charging aperture of described two grades of whole reduction bed first dischargers 52；Described two grades of whole reduction bed cyclone separator The bottom discharge mouth of 54 is connected with the charging aperture of described two grades of whole reduction bed second dischargers 53；

Described two grades of eventually discharging opening of reduction bed the first dischargers 52 and two grades reduction bed the first dischargers 53 eventually and products The charging aperture of feed bin 6 is connected.

Preferably, described oxidation bed 2, prereduction bed 3 and bed unit of reducing eventually are fluidizing fluid-bed, under fluid bed body Portion is that air inlet gas speed fluidizes section, i.e. 0.2-0.8m/s, and top is that sending down the abnormal ascending QI speed expands fluidisation section, and upper inner diameter is lower inner diameter 1.3-2 again.

In the present invention, the top sending down the abnormal ascending QI speed of oxidation bed and reduction bed expands fluidisation section, and because internal diameter expands, gas speed drops naturally Low.

In the present invention, raw material breeze coarse granule in warm and fine grain input and output material respectively are by first Oxidation bed feeder 14 and the second oxidation bed feeder 15 realize, coarse granule in oxidation stage and fine grain enter respectively Discharging is realized by oxidation bed the first discharger 22 and oxidation bed the second discharger 23, the coarse granule in reduction phase and Fine grain input and output material respectively is by one-level reduction bed the first discharger 32 and one-level reduction bed the second discharger 33, second-stage reduction Bed the first discharger 42 and second-stage reduction bed the second discharger 43 realize.

Preferably, described system also includes heat exchanger 7, the air inlet of described oxidation bed gas heater 21 and described heat The air outlet of exchanger 7 is connected, and gases exit line and the described heat of the cyclone separator arranged on reduction bed eventually are handed over The air inlet of parallel operation 7 is connected.

Preferably, the steam line included by this device all can arrange control valve.

Preferably, the described system for the reduction of vanadium titano-magnetite fluidization high temperature Quick Oxidation also includes that reducing gases is pressurizeed Device, described reducing gases prelum is positioned on the entrance pipe of reduction bed.

Preferably, the described system for the reduction of vanadium titano-magnetite fluidization high temperature Quick Oxidation still further comprises washing Device 8, it is arranged on the tail gas pipeline of reduction bed.

It is furthermore preferred that the tail gas pipeline behind described scrubber is divided into the first branch road and the second branch road, the first branch road and tail gas Processing means connects, and the gas access of the gas heater of the second branch road and reduction bed connects, the gas conduct in the second branch road Reducing gases enters the gas heater of reduction bed.

It is furthermore preferred that be provided with carbon dioxide eliminating device on described second branch road.

It is furthermore preferred that be provided with reduction tail gas prelum on described second branch road.

Following one is provided for the redox system of vanadium titano-magnetite fluidization in embodiments of the invention, This system includes ore fines feed bin and feeder, fine ore preheater 1, oxidation bed 2, prereduction bed 3, eventually reduction bed 4 and 5, product material Storehouse 6, heat exchanger 7, scrubber 8, reduction tail gas prelum 9, carbon dioxide eliminating device 10, reducing gases prelum 15.

Described fine ore preheater 1 includes that first order cyclone separator 11, second level cyclone separator 12, third level whirlwind divide From device 13, oxidation bed feeder 14 and 15.

Described oxidation bed 2 includes aoxidizing fluid bed body 20, oxidation bed gas heater 21, oxidation bed discharger 22 and 23, oxidation bed cyclone separator 24.

Described prereduction bed 3 includes prereduction fluid bed body 30, prereduction bed discharger 32 and 33, prereduction bed whirlwind Separator 34.

Described eventually reduction bed 4 and 5 include the one-level reduction bed gas heater 41 eventually of reduction fluid bed body 40, one-level eventually, One-level reduction bed discharger 42 and 43, one-level reduction bed cyclone separator 44 eventually eventually, two grades of whole reduction fluid bed bodies 50, two grades Reduction bed gas heater 51, two grades reduction bed discharger 52 eventually and 53, two grades of whole reduction bed cyclone separator 54 eventually.

Going out of the first order cyclone separator 11 of the discharging opening of described ore fines feed bin and feeder and described fine ore preheater 1 QI KOU is connected, and the bottom discharge mouth of described first order cyclone separator 11 is connected with the charging aperture of oxidation bed feeder 14, The gas outlet of described first order cyclone separator 11 is connected with the entrance of second level cyclone separator 12.Described second level whirlwind The bottom discharge mouth of separator 12 is connected with the entrance of first order cyclone separator 11, described second level cyclone separator 12 Gas outlet is connected with the entrance of third-stage cyclone separator 13.The bottom discharge mouth of described third-stage cyclone separator 13 and oxygen The charging aperture changing bed feeder 15 is connected, the gas outlet of described third-stage cyclone separator 13 and external vent gas treatment facility phase Connect.

The discharging opening of the oxidation bed feeder 14 and 15 of described fine ore preheater 1 and the oxidation fluid bed of described oxidation bed 2 The charging aperture of body 20 is connected, the bottom air inlet of described oxidation fluid bed body 20 and described oxidation bed gas heater 21 Gas outlet be connected, the gas outlet, top of described oxidation fluid bed body 20 and the entrance of described oxidation bed cyclone separator 24 Being connected, the discharging opening of described oxidation fluid bed body 20 is connected with the charging aperture of described oxidation bed discharger 22.Described oxygen The gas outlet changing bed cyclone separator 24 is connected with the entrance of the first order cyclone separator 11 of described fine ore preheater 1, institute The charging aperture of the bottom discharge mouth and described oxidation bed discharger 23 of stating oxidation bed cyclone separator 24 is connected.Described oxidation bed The air inlet of gas heater 21 is connected with the air outlet of described heat exchanger 7.

The discharging opening of the oxidation bed discharger 22 and 23 of described oxidation bed 2 and the prereduction fluid bed of described prereduction bed 3 The charging aperture of body 30 is connected, the bottom air inlet of described prereduction fluid bed body 30 and the one-level of the described bed 4 of reduction eventually The gas outlet of reduction bed cyclone separator 44 is connected eventually, and the gas outlet, top of described prereduction fluid bed body 30 is pre-with described The entrance of reduction bed cyclone separator 34 is connected, and the discharging opening of described prereduction fluid bed body 30 goes out with described prereduction bed The charging aperture of glassware 32 is connected.Protocercal tail is gone back with described heat exchanger 7 in the gas outlet of described prereduction bed cyclone separator 33 Gas air inlet is connected, and the bottom discharge mouth of described prereduction bed cyclone separator 33 enters with described prereduction bed discharger 33 Material mouth is connected.

The discharging opening of the prereduction bed discharger 32 and 33 of described prereduction bed 3 is whole also with the one-level of the described bed 4 of reduction eventually The charging aperture of former fluid bed body 40 is connected, the bottom air inlet of described one-level reduction fluid bed body 40 eventually and described one-level The gas outlet of reduction bed gas heater 41 is connected eventually, the gas outlet, top of described one-level reduction fluid bed body 40 eventually and institute The entrance stating one-level reduction bed cyclone separator 44 eventually is connected, the discharging opening of described one-level reduction fluid bed body 40 eventually and institute The charging aperture stating one-level reduction bed discharger 42 eventually is connected.The bottom discharge mouth of described one-level reduction bed cyclone separator 44 eventually It is connected with the charging aperture of described one-level reduction bed discharger 43 eventually.The air inlet of described one-level reduction bed gas heater 41 eventually The gas outlet of reduction bed cyclone separator 54 whole with two grades of described reduction bed 5 is connected.

The discharging opening of the one-level reduction bed discharger 42 and 43 eventually of the described bed 4 of reduction eventually and two grades of ends of described reduction bed 5 The charging aperture of reduction fluid bed body 50 is connected, the bottom air inlet and described two of described two grades of whole reduction fluid bed bodies 50 The gas outlet of level eventually reduction bed gas heater 51 is connected, described two grades eventually reduction fluid bed bodies 50 gas outlet, top with The entrance of described level two grades reduction bed cyclone separator 54 eventually is connected, the discharging opening of described two grades of whole reduction fluid bed bodies 50 It is connected with the charging aperture of described two grades of whole reduction bed dischargers 52.The bottom of described two grades of whole reduction bed cyclone separator 54 goes out Material mouth is connected with the charging aperture of described two grades of whole reduction bed dischargers 53.Entering of described two grades of whole reduction bed gas heaters 51 QI KOU is connected with the gas outlet of the gas outlet of carbon dioxide eliminating device 10 and external reducing gases prelum 15.

The discharging opening of two grades of the described bed 5 of reduction eventually reduction bed discharger 52 and 53 eventually and the charging aperture phase of product feed bin 6 Connect.The air inlet of described heat exchanger 7 is connected with external air supplies, described heat exchanger 7 go back protocercal tail Gas gas outlet is connected with the air inlet of described scrubber 8.The gas outlet of described scrubber 8 and the air inlet of described prelum 9 It is connected with external vent gas treatment facility.The gas outlet of described prelum 9 is connected with the air inlet of carbon dioxide eliminating device 10.

The bottom inflow of described oxidation bed feeder 14 and 15 is by the burning tail of external described oxidation bed gas heater 21 Air stripping confession, the bottom inflow of described oxidation bed discharger 22,23 and described two grades of whole reduction bed dischargers 52,53 is by external nitrogen Thering is provided, the bottom inflow of described prereduction bed discharger 32,33 and described one-level reduction bed discharger 42,43 eventually is by external reduction Air stripping confession, described oxidation bed gas heater 21, described one-level reduction bed gas heater 41 eventually and described two grades of whole reduction beds The thermal source of gas heater 51 is provided by external combustion gas, and described steam line is provided with control valve.

The invention also discloses and utilize aforesaid system to carry out the redox method of vanadium titano-magnetite fluidization, including:

Vanadium titano-magnetite fine ore through cyclone separator and from oxidation bed cyclone separator gas outlet oxidized tail gas preheat After the different breeze of the particle diameter thickness that obtains enter oxidation bed body, the coarse granule fine ore after fluidization high-temperature oxydation directly enters Entering prereduction fluid bed body, the fine grained fine ore oxidized bed cyclone separator after oxidation enters prereduction fluid bed after separating Body；Coarse granule fine ore after prereduction fluid bed prereduction is directly entered the first order eventually reduction bed unit, after prereduction after Fine grained fine ore after prereduction bed cyclone separator separates, enter the first order eventually reduction fluid bed body；

Fine ore through in eventually reduction bed after high temperature reduction, coarse granule is directly expelled to next stage eventually by reducing bed body eventually Reduction fluid bed body, fine grained is discharged into next stage reduction fluid bed body eventually after cyclone separator separates；Last The reduction fine ore of the reduction bed of level enters product feed bin after discharging, and reduction bed cyclone separator expellant gas is as heated eventually Afterwards as the reproducibility unstrpped gas of upper level reduction bed unit, first order reduction bed cyclone separator expellant gas is as in advance The reproducibility unstrpped gas of reduction bed unit.

Preferably, vanadium titano-magnetite fine ore is entered first order cyclone separator 11 by the discharging opening of ore fines feed bin and feeder Gas outlet and with the oxidized tail gas heat exchange from oxidation bed cyclone separator 24 gas outlet, subsequently enter second level cyclone separator 12 entrances, separate via second level cyclone separator 12, its bottom discharge mouth the coarse granule fine ore discharged enters first order rotation Wind separator 11 entrance again with the oxidized tail gas heat exchange from oxidation bed cyclone separator 24 gas outlet after enter oxidation bed enter The charging aperture of glassware 14；

The fine grained fine ore being entrained with by second level cyclone separator 12 gas outlet separates through second level cyclone separator 13 After be directly entered the charging aperture of oxidation bed feeder 15；Vanadium titano-magnetite fine ore after fine ore preheater 1 preheats is by oxidation bed Feeder 14 and 15 discharging opening enters oxidation fluid bed body 20 and aoxidizes；

Coarse granule fine ore after oxidation enters prereduction fluid bed body 30 via oxidation bed discharger 22 and carries out prereduction, Fine grained fine ore oxidized bed cyclone separator 24 after oxidation is entered prereduction fluid bed by oxidation bed discharger 23 after separating Body 30 carries out prereduction；

Vanadium titano-magnetite fine ore is after prereduction, and coarse granule fine ore enters one-level reduction eventually via prereduction bed discharger 32 Fluid bed body 40 carries out for the first time eventually reduction, fine grained fine ore after prereduction bed cyclone separator 34 separates by prereduction bed Discharger 33 enters one-level reduction fluid bed body 40 eventually and carries out reduction the most eventually；

Used by one-level reduction fluid bed body 40 eventually, reducing gas is from two grades of whole reduction bed cyclone separator 54 gas outlets The reducing gases through one-level reduction bed gas heater 41 heating eventually discharged；Vanadium titano-magnetite fine ore after for the first time eventually reduction, Coarse granule fine ore enters two grades of whole reduction fluid bed bodies 50 via one-level reduction bed discharger 42 eventually and carries out second time reduction eventually, Fine grained fine ore is entered two grades of ends also by one-level reduction bed discharger 43 eventually after reduction bed cyclone separator 44 separates eventually through one-level Former fluid bed body 50 carries out second time reduction eventually；

Second time is reduced after terminating eventually, and vanadium titano-magnetite thick reduced powder mineral products are discharged through two grades of whole reduction bed dischargers 52 To product feed bin 6, thin reduced powder mineral products after through two grades, reduction bed cyclone separator 54 separate eventually by two grades of reduction bed dischargings eventually Device 53 is expelled to product feed bin 6.

Preferably, described vanadium titano-magnetite fine ore is natural minerals selecting and purchasing or processing acquisition, and all iron content is 45- 65wt%, TiO₂Content is the iron ore fine ore of 8-15wt%, and the particle diameter of described vanadium titano-magnetite fine ore is 0.005-0.5mm.

Preferably, described oxidation bed, prereduction bed and the bed that reduces eventually all use low gas velocity to operate, and described low gas velocity is 0.2-0.8m/s。

Preferably, the inlet oxidation exhaust temperature of the first order cyclone separator of described fine ore preheater is 650-800 DEG C, The oxidizing temperature of described oxidation bed is 700-825 DEG C, and the pre-reduction temperature of described prereduction bed is 700-850 DEG C, and described end is also The whole reduction temperature of former bed is 850-950 DEG C.

Preferably, described oxidizing gas is air or the gas with oxygen as main component, and described reducing gas is Coal gas or reformation gas, with H₂It is effective ingredient with CO.

Preferably, described oxidation and reduction process are carried out under operation pressure 4-9atm.

Preferably, raw material breeze its coarse granule and fine grained in preheating, oxidation and reduction process realizes input and output material respectively Control.

A kind of vanadium titano-magnetite based on said system fluidization is provided redox in embodiments of the invention Method, described method includes:

Fine ore and gas enter into and through described system simultaneously as follows: vanadium titano-magnetite fine ore by ore fines feed bin and The discharging opening of feeder enter first order cyclone separator 11 gas outlet and with from oxidation bed cyclone separator 24 gas outlet Oxidized tail gas heat exchange, subsequently entered second level cyclone separator 12 entrance, separates via second level cyclone separator 12, by its end The coarse granule fine ore that portion discharging opening is discharged enter first order cyclone separator 11 entrance again with from oxidation bed cyclone separator The charging aperture of oxidation bed feeder 14 is entered after the oxidized tail gas heat exchange of 24 gas outlets.By second level cyclone separator 12 gas outlet The fine grained fine ore being entrained with is directly entered the charging aperture of oxidation bed feeder 15 after second level cyclone separator 13 separates.Warp Vanadium titano-magnetite fine ore after fine ore preheater 1 preheating is entered oxidation fluid bed body by oxidation bed feeder 14 and 15 discharging opening 20 aoxidize.Oxidizing gas is added by the most oxidized bed gas heater 21 after over-heat-exchanger 7 with reduction exhaust gas heat exchange Hot-air supply after heat.Coarse granule fine ore after oxidation enters prereduction fluid bed body 30 via oxidation bed discharger 22 and enters Row prereduction, the fine grained fine ore oxidized bed cyclone separator 24 after oxidation is entered pre-going back by oxidation bed discharger 23 after separating Former fluid bed body 30 carries out prereduction.Reducing gas used by prereduction fluid bed body 30 divides from one-level reduction bed whirlwind eventually The reducing gases discharged from device 44 gas outlet.Vanadium titano-magnetite fine ore is after prereduction, and coarse granule fine ore is via prereduction bed discharging Device 32 enters one-level reduction fluid bed body 40 eventually and carries out reduction the most eventually, and fine grained fine ore is through prereduction bed cyclone separator Entered one-level reduction fluid bed body 40 eventually by prereduction bed discharger 33 after 34 separation to carry out reducing the most eventually.One-level is the most also Reducing gas used by former fluid bed body 40 is gone back from two grades of whole reduction bed cyclone separator 54 gas outlet discharges eventually through one-level The reducing gases of former bed gas heater 41 heating.Vanadium titano-magnetite fine ore is after reduction the most eventually, and coarse granule fine ore is via one Level reduction bed discharger 42 eventually enters two grades of whole reduction fluid bed bodies 50 and carries out second time reduction eventually, and fine grained fine ore is through one-level Entered one-level reduction fluid bed body 50 eventually by one-level reduction bed discharger 43 eventually after reduction bed cyclone separator 44 separates eventually to enter The reduction eventually of row second time.Used by two grades of whole reduction fluid bed bodies 50, reducing gas washs from scrubbed device 8, prelum 9 adds Reduction tail gas after pressure and carbon dioxide eliminating device 10 carbon dioxide removal, and supplement through the external of reducing gases prelum 15 pressurization New reducing gases, heats as two grades of reduction fluidisations eventually through two grades of whole reduction bed gas heaters 51 after the mixing of two parts reducing gases again The thermal reduction gas of bed body 50.Second time is reduced after terminating eventually, and vanadium titano-magnetite thick reduced powder mineral products are through two grades of whole reduction beds Discharger 52 is expelled to product feed bin 6, thin reduced powder mineral products after through two grades, eventually reduction bed cyclone separator 54 separate by two grades Reduction bed discharger 53 is expelled to product feed bin 6 eventually, and reduction fine ore cooling stores or hot for its follow-up production and application.Prereduction The reduction tail gas that bed cyclone separator 34 gas outlet is discharged, first carries out heat exchange through heat exchanger 7 and oxidic raw materials gas air, Enter back into scrubber 8 subsequently to wash, wherein part by reduction tail gas prelum 9 pressurize Posterior circle utilize, be partially into external Exhaust gas processing device is for the heating burning of each heater 21,41,51.

First of the present invention enters after being improved by the preheating of vanadium titano-magnetite fine ore preheated device in isolated oxidation bed Row oxidation processes, oxidizing gas is air or the gas with oxygen as main component.

The present invention further improvement is that oxidation bed, prereduction bed and the bed that reduces eventually all use low gas velocity to operate, described Low gas velocity is 0.2-0.8m/s.

Another oxidation bed, prereduction bed and the whole reduction bed of being improved by of the present invention is fluidizing fluid-bed, and fluid bed is originally Body bottom be air inlet gas speed fluidize section, top is sending down the abnormal ascending QI speed expanding reach, and raw material breeze preheating, oxidation and reduction process in its Coarse granule and fine grained realize input and output material respectively and control.

Relative to prior art, present invention have the advantage that:

First vanadium titano-magnetite fine ore carries out low-temperature oxidation process in isolated oxidation bed, it is possible to be effectively improved mineral self Reaction efficiency also reduces restoring operation gas speed, thus can realize high temperature fast restore and fluidization stability is greatly improved.

After vanadium titano-magnetite fine ore is preheated, oxidation bed aoxidizes, series connection enters prereduction bed and the bed that reduces eventually, prereduction bed The most external gas heats, and after making full use of oxidation, temperature of charge carries out prereduction, and the heating of reduction bed external gas realizes high temperature eventually High efficiency is reduced, and system entirety fine ore material heat utilization rate is high.

Oxic gas exchanges temperature raising with reduction exhaust gas heat and recycles reduction waste heat from tail gas, oxidized tail gas before entering heater Recycling oxidized tail gas waste heat for fine ore preheater, reduction tail gas mixes with external reducing gases the most again as also Primordial Qi enters reduction fluidized bed circulation and utilizes, and system overall gas material heat energy and chemical energy usage rate are high.

Design the expansion of fluidizing fluid-bed body upper part sending down the abnormal ascending QI speed and raw material fine ore coarse granule and fine grain whirlwind and stream Change the bed body mode that input and output material controls respectively, it is possible to ensure uniform alumina and the reduction of large or fine granule.

Using the present invention that vanadium titano-magnetite fine ore is carried out fluidization oxidoreduction, after low-temperature oxidation processes, mineral are certainly Body reaction efficiency improves, and subsequent high temperature reduction action required gas prompt drop is low, and fluidized state is stable, and high temperature reduction efficiency is high, from root Avoid the operation of conventional art high gas velocity on Ben, reaction temperature is low, easily bond defluidization, needs procedure coercion stabilization fluid state not Foot.Design fluidizing fluid-bed body variable-diameter structure and large or fine granule independence input and output material, it is possible to ensure that product process uniform quality is steady Fixed.Reasonable Arrangement energy and material technical process flow to simultaneously, arrange middle prereduction fluid bed, make full use of fine ore and gas Heat energy and chemical energy, it is possible to decrease fluid bed reduction vanadium titano-magnetite fine ore process energy consumption, improve macroeconomic.

Accompanying drawing explanation

Accompanying drawing is used for providing explains the further of the present invention, and constitutes a part for description, with the reality of the present invention Execute example together for explaining the present invention, be not intended that limitation of the present invention.

Fig. 1 is the redox system schematic of vanadium titano-magnetite fluidization of the present invention.

Reference

0, ore fines feed bin and feeder；1, fine ore preheater；11, first order cyclone separator；12, second level cyclonic separation Device；13, third-stage cyclone separator；14, oxidation bed the first feeder；15, oxidation bed feeder；2, oxidation bed；20, oxidation stream Change bed body；21, oxidation bed gas heater；22, oxidation bed the first discharger；23, oxidation bed the second discharger；24, oxidation Bed cyclone separator；3, prereduction bed；30, prereduction fluid bed body；32, prereduction bed the first discharger；33, prereduction bed Second discharger；34, prereduction bed cyclone separator；4, the first whole reduction bed；5, the second whole reduction bed；40, one-level reduction eventually Fluid bed body；41, one-level reduction bed gas heater eventually；42, one-level reduction bed the first discharger eventually；43, one-level reduction eventually Bed the second discharger；44, one-level reduction bed cyclone separator eventually；50, two grades of whole reduction fluid bed bodies；51, two grades of reduction eventually Bed gas heater；52, two grades of whole reduction bed first dischargers；53, two grades of whole reduction bed second dischargers；54, two grades of ends are also Former bed cyclone separator；6, product feed bin；7, heat exchanger；8, scrubber；9, reduction tail gas prelum；10, carbon dioxide de Except device；15, reducing gases prelum.

Detailed description of the invention

For making the object, technical solutions and advantages of the present invention clearer, attached below in conjunction with in the embodiment of the present invention Figure, carries out clear, complete description to the technical scheme in the embodiment of the present invention, it is clear that described embodiment is the present invention A part of embodiment rather than whole embodiments.Based on the embodiment in the present invention, those of ordinary skill in the art are not having Have and make all other embodiments obtained under creative work premise, broadly fall into the scope of protection of the invention.

Embodiment 1

As it is shown in figure 1, a kind of redox system of vanadium titano-magnetite fluidization, system includes ore fines feed bin and feeder 0, fine ore preheater 1, oxidation bed 2, prereduction bed 3, eventually reduction bed 4 and 5, product feed bin 6, heat exchanger 7, scrubber 8, reduction Tail gas prelum 9, carbon dioxide eliminating device 10, reducing gases prelum 15.

Fine ore preheater 1 includes first order cyclone separator 11, second level cyclone separator 12, third-stage cyclone separator 13, oxidation bed the first feeder 14 and oxidation bed the second feeder 15.Oxidation bed 2 includes aoxidizing fluid bed body 20, oxidation bed Gas heater 21, oxidation bed the first discharger 22 and oxidation bed the second discharger 23, oxidation bed cyclone separator 24.Prereduction Bed 3 includes prereduction fluid bed body 30, prereduction bed discharger 32 and prereduction bed the second discharger 33, prereduction bed whirlwind Separator 34.First eventually reduction bed 4 and second reduction bed 5 eventually include one-level reduction fluid bed body 40, one-level reduction bed eventually eventually Gas heater 41, one-level reduction bed the first discharger 42 eventually and one-level reduction bed the second discharger 43, one-level reduction bed eventually eventually Cyclone separator 44, two grades of whole reduction fluid bed bodies 50, two grades whole bed first that reduces of reduction bed gas heaters 51, two grades eventually Discharger 52 and two grades of whole reduction bed the second discharger 53, two grades reduction bed cyclone separator 54 eventually.

The gas outlet phase of the discharging opening of ore fines feed bin and feeder 0 and the first order cyclone separator 11 of fine ore preheater 1 Connecting, the bottom discharge mouth of first order cyclone separator 11 is connected with the charging aperture of oxidation bed feeder 14, first order whirlwind The gas outlet of separator 11 is connected with the entrance of second level cyclone separator 12.The bottom discharge of second level cyclone separator 12 Mouth is connected with the entrance of first order cyclone separator 11, the gas outlet of second level cyclone separator 12 and third level cyclonic separation The entrance of device 13 is connected.The charging aperture phase of the bottom discharge mouth of third-stage cyclone separator 13 and oxidation bed the second feeder 15 Connecting, the gas outlet of third-stage cyclone separator 13 is connected with external vent gas treatment facility.

Oxidation bed first feeder 14 of fine ore preheater 1 and the discharging opening of oxidation bed the second feeder 15 and oxidation bed 2 The charging aperture of oxidation fluid bed body 20 be connected, bottom air inlet and the oxidation bed gas of oxidation fluid bed body 20 heat The gas outlet of device 21 is connected, and the gas outlet, top of oxidation fluid bed body 20 is connected with the entrance of oxidation bed cyclone separator 24 Connecing, the discharging opening of oxidation fluid bed body 20 is connected with the charging aperture of oxidation bed the first discharger 22.Oxidation bed cyclonic separation The gas outlet of device 24 is connected with the entrance of the first order cyclone separator 11 of fine ore preheater 1, oxidation bed cyclone separator 24 Bottom discharge mouth be connected with the charging aperture of oxidation bed the second discharger 23.The air inlet of oxidation bed gas heater 21 and heat The air outlet of exchanger 7 is connected.

Oxidation bed first discharger 22 of oxidation bed 2 and the discharging opening of oxidation bed the second discharger 23 and prereduction bed 3 The charging aperture of prereduction fluid bed body 30 is connected, the bottom air inlet of prereduction fluid bed body 30 and reduction bed 4 eventually The gas outlet of one-level reduction bed cyclone separator 44 eventually is connected, the gas outlet, top of prereduction fluid bed body 30 and prereduction The entrance of bed cyclone separator 34 is connected, the discharging opening of prereduction fluid bed body 30 and the charging of prereduction bed discharger 32 Mouth is connected.The gas outlet of prereduction bed cyclone separator 34 is connected with the reduction tail gas air inlet of heat exchanger 7, prereduction The bed bottom discharge mouth of cyclone separator 34 is connected with the charging aperture of prereduction bed the second discharger 33.

Prereduction bed first discharger 32 of prereduction bed 3 and the discharging opening of prereduction bed the second discharger 33 reduce with whole The charging aperture of the one-level of bed 4 reduction fluid bed body 40 eventually is connected, the bottom air inlet of one-level reduction fluid bed body 40 eventually Be connected with the gas outlet of one-level eventually reduction bed gas heater 41, the gas outlet, top of one-level reduction fluid bed body 40 eventually with The entrance of one-level reduction bed cyclone separator 44 eventually is connected, and the discharging opening of one-level reduction fluid bed body 40 eventually is with one-level the most also The charging aperture of former bed the first discharger 42 is connected.The bottom discharge mouth of one-level reduction bed cyclone separator 44 eventually is with one-level the most also The charging aperture of former bed the second discharger 43 is connected.The air inlet of one-level reduction bed gas heater 41 eventually and the two of reduction bed 5 The gas outlet of level reduction bed cyclone separator 54 eventually is connected.

The discharging opening of one-level reduction bed first discharger 42 eventually of whole reduction bed 4 and one-level reduction bed the second discharger 43 eventually The charging aperture of reduction fluid bed body 50 whole with two grades of reduction bed 5 is connected, the bottom of two grades of whole reduction fluid bed bodies 50 The gas outlet of air inlet and two grades of whole reduction bed gas heaters 51 is connected, and the tops of two grades of whole reduction fluid bed bodies 50 go out The entrance of QI KOU and level two grades reduction bed cyclone separator 54 eventually is connected, two grades eventually reduction fluid bed bodies 50 discharging opening with The charging aperture of two grades of whole reduction bed first dischargers 52 is connected.Two grades eventually reduction bed cyclone separator 54 bottom discharge mouth with The charging aperture of two grades of whole reduction bed second dischargers 53 is connected.The air inlet of two grades of whole reduction bed gas heaters 51 and dioxy The gas outlet changing carbon remover 10 is connected with the gas outlet of external reducing gases prelum 15.

Two grades of whole reduction bed 5 reduction bed the first dischargers 52 eventually and the discharging opening of two grades of whole reduction bed second dischargers 53 It is connected with the charging aperture of product feed bin 6.The air inlet of heat exchanger 7 is connected with external air supplies, and heat is handed over The reduction tail gas gas outlet of parallel operation 7 is connected with the air inlet of scrubber 8.The gas outlet of scrubber 8 and the air inlet of prelum 9 It is connected with external vent gas treatment facility.The gas outlet of prelum 9 is connected with the air inlet of carbon dioxide eliminating device 10.

The bottom inflow of oxidation bed the first feeder 14 and oxidation bed the second feeder 15 is heated by external oxidation bed gas The combustion tail gas of device 21 provides, and oxidation bed the first discharger 22, oxidation bed the second discharger 23 and two grades reduction bed first eventually goes out The bottom inflow of 52, two grades of glassware reduction bed the second discharger 53 eventually is provided by external nitrogen, prereduction bed the first discharger 32, The bottom of prereduction bed the second discharger 33 and one-level reduction bed the second discharger 43 eventually of reduction bed the first discharger 42, one-level eventually Air inlet is provided by external reducing gases, oxidation bed gas heater 21, one-level reduction bed gas heater 41 eventually and two grades of reduction eventually Bed gas heater 51 thermal source provided by external combustion gas, steam line on be provided with control valve.

Oxidation bed 2 in the present embodiment, prereduction bed 3, the first whole reduction bed 4 and the second whole reduction bed 5, being boiling and fluidizing Bed, fluid bed body lower part is that air inlet gas speed fluidizes section, and top is sending down the abnormal ascending QI speed expanding reach, and upper inner diameter is the 1.3-of lower inner diameter 2 times.

Embodiment 2

Above-mentioned vanadium titano-magnetite fluidization oxidation-reduction system is used to carry out the redox side of vanadium titano-magnetite fluidization Method comprises the following steps: vanadium titano-magnetite fine ore is entered first order cyclone separator by the discharging opening of ore fines feed bin and feeder 0 11 gas outlets and with the oxidized tail gas heat exchange from oxidation bed cyclone separator 24 gas outlet, subsequently enter second level cyclonic separation Device 12 entrance, separates via second level cyclone separator 12, its bottom discharge mouth the coarse granule fine ore discharged enters the first order Cyclone separator 11 entrance enters oxidation bed with after the oxidized tail gas heat exchange from oxidation bed cyclone separator 24 gas outlet again The charging aperture of the first feeder 14.The fine grained fine ore being entrained with by second level cyclone separator 12 gas outlet is through second level whirlwind Separator 13 is directly entered the charging aperture of oxidation bed the second feeder 15 after separating.Vanadium titanium magnetic after fine ore preheater 1 preheats Iron mine fine ore is entered oxidation fluid bed body 20 by oxidation bed the first feeder 14 and oxidation bed the second feeder 15 discharging opening and enters Row oxidation.After oxidizing gas is by after over-heat-exchanger 7 with reduction exhaust gas heat exchange, the most oxidized bed gas heater 21 heats Hot-air supply.Coarse granule fine ore after oxidation enters prereduction fluid bed body 30 via oxidation bed the first discharger 22 and enters Row prereduction, the fine grained fine ore oxidized bed cyclone separator 24 after oxidation is entered by oxidation bed the second discharger 23 after separating Prereduction fluid bed body 30 carries out prereduction.Reducing gas used by prereduction fluid bed body 30 is from one-level reduction bed rotation eventually The reducing gases that wind separator 44 gas outlet is discharged.Vanadium titano-magnetite fine ore is after prereduction, and coarse granule fine ore is via prereduction bed First discharger 32 enters one-level reduction fluid bed body 40 eventually and carries out reduction the most eventually, and fine grained fine ore revolves through prereduction bed Wind separator 34 is entered one-level reduction fluid bed body 40 eventually by prereduction bed the second discharger 33 after separating to be carried out the most eventually Reduction.Used by one-level reduction fluid bed body 40 eventually, reducing gas is from two grades of reduction bed cyclone separator 54 gas outlet discharges eventually The reducing gases through one-level eventually reduction bed gas heater 41 heating.Vanadium titano-magnetite fine ore after for the first time eventually reduction, thick Grain fine ore enters two grades of whole reduction fluid bed bodies 50 via one-level reduction bed the first discharger 42 eventually and carries out second time reduction eventually, Fine grained fine ore is entered two grades by one-level reduction bed the second discharger 43 eventually after reduction bed cyclone separator 44 separates eventually through one-level Reduction fluid bed body 50 carries out second time reduction eventually eventually.Reducing gas used by two grades of whole reduction fluid bed bodies 50 is hung oneself and is washed Wash that device 8 washs, prelum 9 pressurizes and reduction tail gas after carbon dioxide eliminating device 10 carbon dioxide removal, and adds through reducing gases The external of depressor 15 pressurization supplements new reducing gases, adds through two grades of whole reduction bed gas heaters 51 after the mixing of two parts reducing gases again Heat is as the thermal reduction gas of two grades of whole reduction fluid bed bodies 50.Second time is reduced after terminating eventually, the thick reduced powder of vanadium titano-magnetite Mineral products are expelled to product feed bin 6 through two grades of whole reduction bed first dischargers 52, and thin reduced powder mineral products are through two grades of whole reduction beds Cyclone separator 54 is expelled to product feed bin 6 by two grades of whole reduction bed second dischargers 53 after separating, and reduction fine ore cooling stores Or it is hot for its follow-up production and application.The reduction tail gas that prereduction bed cyclone separator 34 gas outlet is discharged, first through heat exchange Device 7 and oxidic raw materials gas air carry out heat exchange, enter back into scrubber 8 subsequently and wash, and wherein part is pressurizeed by reduction tail gas Device 9 pressurize Posterior circle utilize, be partially into external exhaust gas processing device for each heater 21,41,51 heating burn.

Embodiment 3

Using the present invention to process raw ore chemical composition wt.% is 55.86%TFe, 15.00%FeO, 63.19%Fe₂O₃、 13.71%TiO₂, 2.21%SiO₂, 1.16%MgO, 3.18%Al₂O₃, 1.57%V₂O₅, the v-ti magnetite breeze of 0.22%CaO Ore deposit, fine ore granularity is 0.01-0.3mm.First oxidation processes is carried out at oxidation fluid bed according to after fine ore pre-heating drying of the present invention, 800 DEG C aoxidize 30 minutes, and oxic gas speed is 0.29m/s, operate pressure 2.0atm, and oxic gas is air, the two of vanadium titano-magnetite Valency ferrum oxidizability reaches 39.61%.Subsequently, the vanadium titano-magnetite fine ore entrance prereduction fluid bed through oxidation processes carries out pre- Reduction, 780 DEG C of prereduction 15 minutes.Subsequently enter reduction fluid bed eventually and carry out whole reduction, whole reduction temperature 860 DEG C, go back eventually The former time amounts to 70 minutes.The gas speed of three reduction beds is 0.6m/s, operates pressure 5.2atm, and reducing gases is coal gas, End, degree of metalization was up to 91.1%, material recovery rate>96%, resultant metal rate deviation<2.4%.

Embodiment 4

Using the present invention to process raw ore chemical composition wt.% is 54.54%TFe, 32.16%FeO, 42.18%Fe₂O₃、 10.77%TiO₂, 3.81%SiO₂, 3.72%MgO, 3.54%Al₂O₃, 0.67%V₂O₅, the v-ti magnetite breeze of 0.39%CaO Ore deposit, fine ore granularity is 0.01-0.25mm.First carry out at oxidation at oxidation fluid bed according to after fine ore pre-heating drying of the present invention Reason, 775 DEG C aoxidize 45 minutes, and oxic gas speed is 0.21m/s, operate pressure 3.2atm, and oxic gas is air, vanadium titano-magnetite Ferrous oxidising degree reaches 44.07%.Subsequently, the vanadium titano-magnetite fine ore entrance prereduction fluid bed through oxidation processes is carried out Prereduction, 750 DEG C of prereduction 20 minutes.Subsequently entering reduction fluid bed eventually and carry out whole reduction, end, reduction temperature 880 DEG C, whole Recovery time amounts to 75 minutes.The gas speed of three reduction beds is 0.64m/s, operates pressure 7.3atm, and reducing gases is natural gas Reformation gas, final degree of metalization up to 90.3%, material recovery rate>97%, resultant metal rate deviation<2.3%.

Last it is noted that above example is only in order to illustrate technical scheme, it is not intended to limit；Although With reference to previous embodiment, the present invention is described in detail, it will be understood by those within the art that: it still may be used So that the technical scheme described in foregoing embodiments to be modified, or wherein portion of techniques feature is carried out equivalent； And these amendment or replace, do not make appropriate technical solution essence depart from various embodiments of the present invention technical scheme spirit and Scope.

Claims

1., for the redox system of vanadium titano-magnetite fluidization, described system includes ore fines feed bin and feeder, powder Ore deposit preheater (1), oxidation bed (2), prereduction bed (3), several whole reduction bed unit and product feed bins (6)；It is characterized in that:

Described fine ore preheater (1) includes several cyclone separator and several oxidation bed feeders, the powder in ore fines feed bin Ore deposit enters oxidation bed (2) by oxidation bed feeder after feeder enters cyclone separator circulation preheating and separates；

Described oxidation bed (2) includes aoxidizing fluid bed body (20), oxidation bed gas heater (21), oxidation bed the first discharger (22), oxidation bed the second discharger (23) and oxidation bed cyclone separator (24), under described oxidation bed cyclone separator (24) Portion's discharging opening and described oxidation bed the second discharger (23) connect；Described oxidation bed the first discharger (22) and oxidation bed second go out Glassware (23) is connected with the charging aperture of first order reduction bed；Oxidation bed offgas outlet is connected (1) with fine ore preheater；

Described prereduction bed (3) includes prereduction fluid bed body (30), prereduction bed the first discharger (32), prereduction bed Two dischargers (33) and prereduction bed cyclone separator (34)；Prereduction bed the first discharger (32) and first order reduction sheet eventually The charging aperture of the reduction bed of unit connects, and prereduction bed cyclone separator (34) and prereduction bed the second discharger (33) connect, institute The charging aperture of the reduction bed stating prereduction bed the second discharger (33) and first order reduction bed unit eventually connects；

Described eventually reduction bed unit includes reducing eventually fluid bed body, eventually reduction bed gas heater, eventually reduction bed the first discharging Device, eventually reduction bed the second discharger and eventually reduction bed cyclone separator；The discharging opening of the described bed cyclone separator of reduction eventually and end Reduction bed the second discharger connects, and described bed the first discharger of reduction eventually is connected with the charging aperture of next stage reduction bed unit eventually, Described bed the second discharger of reduction eventually is connected with the charging aperture of next stage reduction bed unit eventually, afterbody reduction bed unit eventually Reduction bed the first discharger and bed the second discharger that reduces eventually are connected with feed bin eventually；The gas outlet of reduction bed cyclone separator eventually Connecting with the gas access of the reduction bed gas heater of previous stage reduction bed unit eventually, the gas of described prereduction bed (3) enters The bed cyclone separator gas exit line that reduces the end of mouth pipeline and first order reduction bed unit eventually connects.

It is the most according to claim 1 for the redox system of vanadium titano-magnetite fluidization, it is characterised in that:

Described fine ore preheater (1) includes first order cyclone separator (11), second level cyclone separator (12), third level whirlwind Separator (13), oxidation bed the first feeder (14) and oxidation bed the second feeder (15)；

Going out of first order cyclone separator (11) of the discharging opening of described ore fines feed bin and feeder and described fine ore preheater (1) QI KOU is connected, and the bottom discharge mouth of described first order cyclone separator (11) is connected with the charging aperture of oxidation bed feeder (14) Connecing, the gas outlet of described first order cyclone separator (11) is connected with the entrance of second level cyclone separator (12)；

The bottom discharge mouth of described second level cyclone separator (12) is connected with the entrance of first order cyclone separator (11), institute The entrance of the gas outlet and third-stage cyclone separator (13) of stating second level cyclone separator (12) is connected；

The bottom discharge mouth of described third-stage cyclone separator (13) is connected with the charging aperture of oxidation bed feeder (15), described The gas outlet of third-stage cyclone separator (13) is connected with external vent gas treatment facility；

The oxidation bed the first feeder (14) of described fine ore preheater (1) and the discharging opening of oxidation bed the second feeder (15) and institute The charging aperture of oxidation fluid bed body (20) stating oxidation bed (2) is connected；Giving vent to anger of described oxidation bed cyclone separator (24) Mouth is connected with the entrance of the first order cyclone separator (11) of described fine ore preheater (1).

The bottom air inlet of described oxidation fluid bed body (20) is connected with the gas outlet of described oxidation bed gas heater (21) Connecing, the gas outlet, top of described oxidation fluid bed body (20) is connected with the entrance of described oxidation bed cyclone separator (24), The discharging opening of described oxidation fluid bed body (20) is connected with the charging aperture of described oxidation bed the first discharger (22), described oxygen The bottom discharge mouth changing bed cyclone separator (24) is connected with the charging aperture of described oxidation bed the second discharger (23)；

The discharging opening of described oxidation bed the first discharger (22) and described oxidation bed the second discharger (23) and prereduction fluid bed The charging aperture of body (30) is connected.

Going out of the cyclone separator of the bottom air inlet of described prereduction fluid bed body (30) and first order reduction bed unit eventually QI KOU is connected, the gas outlet, top of described prereduction fluid bed body (30) and described prereduction bed cyclone separator (34) Entrance is connected, the discharging opening of described prereduction fluid bed body (30) and the charging of described prereduction bed the first discharger (32) Mouth is connected；The bottom discharge mouth of described prereduction bed cyclone separator (34) and described prereduction bed the second discharger (33) Charging aperture is connected.

Described include the first eventually reduction bed unit (4) and second reduction eventually for the redox system of vanadium titano-magnetite fluidization Bed unit (5), the described first whole reduction bed unit (4) includes the whole bed gas that reduces of one-level reduction fluid bed body (40) eventually, one-level Reduction bed the first discharger (42) eventually of body heater (41), one-level, one-level reduction bed the second discharger (43) eventually and one-level are the most also Former bed cyclone separator (44), the described second whole reduction bed unit (5) includes that two grades are reduced fluid bed body (50), two grades of ends eventually Reduction bed gas heater (51), two grades of eventually reduction bed the first discharger (52), two grades eventually reduction bed the second discharger (53) and Two grades of reduction bed cyclone separator (54) eventually；

The discharging opening of described prereduction bed the first discharger (32) and prereduction bed the second discharger (33) and one-level reduction stream eventually The charging aperture changing bed body (40) is connected, the bottom air inlet of described one-level reduction fluid bed body (40) eventually and described one-level The gas outlet of reduction bed gas heater (41) is connected eventually, the gas outlet, top of described one-level reduction fluid bed body (40) eventually It is connected with the entrance of described one-level reduction bed cyclone separator (44) eventually, going out of described one-level reduction fluid bed body (40) eventually Material mouth is connected with the charging aperture of described one-level reduction bed discharger (42) eventually；

The bottom discharge mouth of described one-level reduction bed cyclone separator (44) eventually and described one-level reduction bed the second discharger eventually (43) charging aperture is connected；The air inlet of described one-level reduction bed gas heater (41) eventually and described two grades of reduction bed rotations eventually The gas outlet of wind separator (54) is connected；

The discharging opening of reduction bed the first discharger (42) eventually of described one-level and one-level reduction bed the second discharger (43) eventually is with described The charging aperture of two grades of whole reduction fluid bed body (50) is connected, the bottom inflow of described two grades of whole reduction fluid bed body (50) Mouth is connected with the gas outlets of described two grades of whole reduction bed gas heater (51), described two grades of reduction fluid bed bodies (50) eventually The entrance of gas outlet, top and described level two grades reduction bed cyclone separator (54) eventually be connected, described two grades of reduction fluidisations eventually The discharging opening of bed body (50) is connected with the charging aperture of described two grades of whole reduction bed the first discharger (52)；Described two grades of ends are also The bottom discharge mouth of former bed cyclone separator (54) is connected with the charging aperture of described two grades of whole reduction bed the second discharger (53)；

Described two grades of eventually discharging opening of reduction bed the first discharger (52) and two grades reduction bed the first discharger (53) eventually and products The charging aperture of feed bin (6) is connected.

System the most according to claim 1, it is characterised in that described oxidation bed (2), prereduction bed (3) and the bed that reduces eventually Unit is fluidizing fluid-bed, and fluidizing fluid-bed body lower part is that air inlet gas speed fluidizes section, and top is sending down the abnormal ascending QI speed expanding reach, on Portion's internal diameter is 1.3-2 times of lower inner diameter.

7. utilize the arbitrary described system of claim 1-6 to carry out the redox method of vanadium titano-magnetite fluidization, bag Include:

Vanadium titano-magnetite fine ore obtains through cyclone separator with after the oxidized tail gas preheating of oxidation bed cyclone separator gas outlet To the different breeze of particle diameter thickness respectively enter oxidation bed body, the coarse granule fine ore after fluidization high-temperature oxydation directly enters Entering prereduction fluid bed body, the fine grained fine ore oxidized bed cyclone separator after oxidation enters prereduction fluid bed after separating Body；Coarse granule fine ore after prereduction fluid bed prereduction is directly entered first order reduction bed unit eventually, after prereduction Fine grained fine ore enters first order reduction fluid bed body eventually after prereduction bed cyclone separator separates；

Fine ore through in eventually reduction bed after high temperature reduction, coarse granule is directly expelled to next stage reduction eventually by reducing bed body eventually Fluid bed body, fine grained is discharged into next stage reduction fluid bed body eventually after cyclone separator separates；Afterbody The reduction fine ore of reduction bed enters product feed bin after discharging, and reduction bed cyclone separator expellant gas is made after heated eventually For the reproducibility unstrpped gas of upper level reduction bed unit, first order reduction bed cyclone separator expellant gas is as prereduction The reproducibility unstrpped gas of bed unit.

Method the most according to claim 7, it is characterised in that described vanadium titano-magnetite fine ore is natural minerals selecting and purchasing or adds Work obtains, and all iron content is 45-65wt%, TiO₂Content is the iron ore fine ore of 8-15wt%, described vanadium titano-magnetite fine ore Particle diameter be 0.005-0.5mm.

Method the most according to claim 7, it is characterised in that described oxidation bed, prereduction bed and the bed that reduces eventually all use Low gas velocity operates, and described low gas velocity is 0.2-0.8m/s, operates pressure 4-9atm.

Method the most according to claim 7, it is characterised in that the first order cyclone separator of described fine ore preheater Inlet oxidation exhaust temperature is 650-800 DEG C, and the oxidizing temperature of described oxidation bed is 700-825 DEG C, described prereduction bed pre- Reduction temperature is 700-850 DEG C, and the whole reduction temperature of the described bed of reduction eventually is 850-950 DEG C.

11. method according to claim 7, it is characterised in that described oxidizing gas is air or is main with oxygen The gas of composition, described reducing gas is coal gas or reformation gas, with H₂It is effective ingredient with CO.

12. methods according to claim 7, it is characterised in that it is thick in preheating, oxidation and reduction process for raw material breeze Granule and fine grained realize input and output material respectively and control.