CN203173849U - Circulating entrained-flow bed device for modifying titanium concentrate - Google Patents
Circulating entrained-flow bed device for modifying titanium concentrate Download PDFInfo
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- CN203173849U CN203173849U CN2013201585738U CN201320158573U CN203173849U CN 203173849 U CN203173849 U CN 203173849U CN 2013201585738 U CN2013201585738 U CN 2013201585738U CN 201320158573 U CN201320158573 U CN 201320158573U CN 203173849 U CN203173849 U CN 203173849U
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Abstract
The utility model discloses a circulating entrained-flow bed device for modifying titanium concentrate capable of realizing continuous production. The circulating entrained-flow bed device comprises an entrained-flow bed reactor, a titanium concentrate feeding system, a gas inlet system, a waste heat utilizing system and a discharging system, wherein the entrained-flow reactor comprises an oxidizing roasting entrained-flow bed reactor and a reduction roasting entrained-flow bed reactor, each entrained-flow bed reactor comprises an airflow distributing section, a gas-solid reaction section, an airflow sorting section and a discharging section and is provided with a gas inlet, a modified gas inlet, a titanium concentrate feeding port, a returning material feeding port, a tail gas outlet and a material outlet, and the material outlet comprises a large-specific-gravity material outlet and a small-specific-gravity material outlet. By adopting the circulating entrained-flow bed device, the requirement on the granularity of raw materials is low, the applicability is strong, the reaction is adequate and rapid, the production efficiency is high, the production period is short, the energy consumption is low, simplicity in operation is realized, and the modification effect is good.
Description
Technical field
The utility model relates to a kind of ilmenite concentrate modification circulating current bed apparatus, belongs to chemical machinery field.
Background technology
Artificial rutile claims titania again, mean the chemical process method of utilizing, with component separating such as the most of iron in the ilmenite concentrate and calcium, magnesium go out produce a kind of on composition and structure properties the rich titanium material identical with natural rutile, its TiO2 content is looked the fluctuation between 88% ~ 96% that do not coexist of complete processing, is the high-quality surrogate of natural rutile.Artificial rutile is few because of good product quality, foreign matter content, the high quality raw material of fluidizing chlorination in Chang Zuowei titanium sponge or the chloride process titanium dioxide powder production process.
At present, adopting ilmenite production Production of Artificial Rutile method abroad mainly is BCA method, bubble method, Shi Yuanfa etc., has all realized large-scale industrial production, and these inventions have been conventionally known to one of skill in the art.And the domestic focus of paying close attention in recent years is the process study for preparing artificial rutile with the salt acid leaching process.The production of salt acid leaching process mainly is by ilmenite concentrate and hydrochloric acid reaction, optionally impurity such as the iron in the ilmenite concentrate, calcium, magnesium, vanadium, manganese is leached and separates, thereby obtain TiO
2The artificial rutile that content is higher, its reaction formula is as follows:
FeO.TiO
2+2HCl=2FeCl
2+TiO
2+?H
2O
CaO.TiO
2+2HCl=2CaCl
2+TiO
2+?H
2O
MgO.TiO
2+2HCl=2MgCl
2+TiO
2+?H
2O
MnO.TiO
2+2HCl=2MnCl
2+TiO
2+?H
2O
No matter domestic or external hydrochloric acid leaches the production technology for preparing artificial rutile, ilmenite concentrate all will carry out redox modification roasting before leaching removal of impurities, this mainly is because during ilmenite oxidizing roasting, most iron wherein change ferric iron into, and reducing roasting is reduced to ferrous iron with ferric iron again.So make the ilmenite experience return the process of ilmenite to the high ferro titanium ore from ilmenite, though be irrational from thermodynamics, but this process is not simple titanium valence state to be changed, atomic rearrangement has importantly taken place, interatomic crystallization educational level has weakened greatly, ilmenite crystalline network imperfect, lax, the easy broken ring that becomes on the microcosmic; On the macroscopic view, slit, micropore have appearred in the particle surface of titanium, and surface free energy increases.The ilmenite reactive behavior is strengthened greatly on the whole, thereby has created more favorably dynamic conditions for leaching reaction.Studies have shown that: directly carry out the corrosion reaction as if not pre-treatment of ilmenite, owing to do not have fe in the ore deposit, can't form galvanic cell, the corrosion reaction can't be carried out.If directly hydrochloric acid leaches, following reaction will take place:
FeO.TiO
2+4HCl=TiOCl
2+2H
2O+FeCl
2
2TiOCl
2+2H
2O=?2TiO
2↓+4HCl
This will cause the yield of titanium to reduce and increase the Pulverization ratio of product, and raw ore is carried out pre-treatment, except the ilmenite concentrate reactive behavior increases, and amorphous TiO in the ore deposit
2Because the higher rutile type crystalline structure that changed into of temperature, its sour dissolving power greatly reduces, and has avoided the generation of Pulverization ratio to a certain extent, thereby reaches enrichment TiO
2Purpose, its chemical equation is as follows:
FeO.TiO
2+O
2=?Fe
2O
3.TiO
2
TiO
2(Anatase) high temperature → TiO
2(Rutile)
FeO.?TiO
2+2HCl=FeCl
2+?TiO
2+?H2O
Wherein, TiO
2(Rutile) be insoluble to hydrochloric acid.
For the modification of ilmenite concentrate, mainly contain three kinds of methods at present:
(1) rotary kiln method for pretreating
In the Production of Artificial Rutile method, BCA method, Becher reduction bubble method and Shi Yuanfa adopt rotary kiln that ilmenite concentrate is carried out pre-treatment, and this has been that the technician is known in the industry.When adopting the rotary kiln pre-treatment to handle ilmenite concentrate, generally ilmenite concentrate is added from the kiln tail with screw conveying device, utilize the kiln body that tilts to rotate and make material preceding mobile vertically, and material in moving process and combustion gas and modified gas meet and be heated and oxidation or reduction reaction take place, reaction is finished the back and is fallen into collector by kiln hood and collect to enter down and go on foot operation.Adopt rotary kiln handle ilmenite concentrate have simple to operate, device mature and reliable, production capacity big, advantage such as can produce continuously, but have also that temperature of reaction is low, ingredient requirement is high, defectives such as the easy ring formation of rotary kiln, on-stream time are short.
(2) mechanical grinding process
The Chinese patent publication number is that the patent of invention of CN 101177297A discloses and a kind ofly prepares the method for high-quality artificial rutile with high contents of calcium and magnesium rock ore deposit, and its processing step is followed successively by: ball milling activation, the leaching of hydrochloric acid normal pressure, solid-liquid separation, washing drying, calcining, particulate granulation.This method by mechanical ore grinding device modification ilmenite concentrate, activate its surface, improved the leaching performance of ilmenite concentrate to a certain extent, finally obtained the higher artificial rutile product of grade.But there are problems such as product Pulverization ratio height, fine powder product granulation difficulty in this technology.
(3) fluidized-bed method for pretreating
Problem at above-mentioned two kinds of methods appearance, there is relevant scholar to propose to adopt fluidization pre-processing titanium concentrate both at home and abroad, fluidized-bed modification ilmenite concentrate comprises oxidizing roasting and reducing roasting, when ilmenite concentrate adopts fluidized bed processing technology, can increase heat transfer and the mass transfer distance of contact area, shortening gas and the granule interior of ilmenite concentrate and gas, have advantages such as raw material sources are wide, material reaction speed is fast, the product Pulverization ratio is low.But fluidized-bed needs ilmenite concentrate to reach thinner granularity and could realize fluidization in fluidized-bed, so the adaptability to raw material of fluidized-bed is not strong for the granularity requirements height of raw material ilmenite concentrate.
In addition, the Chinese patent publication number is that the patent of invention of CN 101412536A discloses the method that a kind of high contents of calcium and magnesium vanadium titano-magnetite prepares artificial rutile.This method is raw material to climb western vanadium titano-magnetite, at first it is carried out fluidization oxidizing roasting in certain temperature, with the fluidization of material reducing roasting after the oxidizing roasting, the material after the modification is leached with certain density hydrochloric acid fluidization then, last solid-liquid separation, drying and calcining obtain product again.The bright spot of this method maximum is to have introduced the fluidized-bed modification technology.
The deficiency that fluidizer has avoided rotary kiln modification ilmenite concentrate and mechanical ore grinding modification ilmenite concentrate to exist to a certain extent, but the equipment complexity that still has fluidizer, the fluidization operation has strict control, device operational requirement height to gas velocity, granularity requirements height, raw material granularity range accommodation for the ilmenite concentrate raw material are narrow, the fluidized-bed materials inside is prone to channel and defective such as turbulent, is difficult to realize producing continuously.
The utility model content
The purpose of this utility model just is at above-mentioned the deficiencies in the prior art, the ilmenite concentrate modification circulating current bed apparatus that provides a kind of serialization to produce, this device is low for the granularity requirements of raw material, adaptability to raw material is strong, sufficient reacting is rapid, production efficiency is high, with short production cycle, energy consumption is low, simple to operate, modified effect is good.
To achieve these goals, the technical solution adopted in the utility model is such:
A kind of ilmenite concentrate modification circulating current bed apparatus, comprise the air flow bed reactor, the ilmenite concentrate charging system, gas enters system, bootstrap system and discharge system, described air flow bed reactor comprises oxidizing roasting air flow bed reactor and reducing roasting air flow bed reactor, described air flow bed reactor comprises air-flow distribution section, the gas-solid reaction section, pneumatic separation section and discharging section, be provided with fuel gas inlet, the modified gas entrance, the ilmenite concentrate opening for feed, the returns opening for feed, tail gas outlet and material outlet, described material outlet comprises big proportion material outlet and little proportion material outlet.
Described modified gas entrance is arranged on described air-flow distribution section bottom, fuel gas inlet is arranged on air-flow distribution pars infrasegmentalis, ilmenite concentrate opening for feed and returns opening for feed are arranged on described gas-solid reaction pars infrasegmentalis, and the tail gas outlet is arranged on the discharging section top, and material outlet is arranged on the discharging section bottom.
The internal diameter ratio of described air-flow distribution section, the gentle flow point selections of gas-solid reaction section is 6: 15: 5～3: 9: 2, and the length ratio is 1: 2.4: 1～1: 3: 1.
In order to make gas distribution even, described air-flow distribution section is provided with modified gas sparger and combustion gas sparger.High-temperature fuel gas and modified gas mix and make constant flow rate by sparger after entering reactor by fuel gas inlet and modified gas entrance.
Described ilmenite concentrate charging system comprises ilmenite concentrate feed bin, ilmenite concentrate preheater and self-conveyor feed.
Described gas enters system and comprises hotblast stove and modified gas storage tank.
Described bootstrap system is made up of pipeline and cyclone.
Described discharge system comprises feed bin and self-conveyor feed.
Described feed bin comprise already oxidised material feed bin, not the oxidation material feed bin, reduce material feed bin and the material feed bin that do not reduce.
Ilmenite concentrate feeds inside reactor by self-conveyor feed after the preheater preheating, the heat of preheater is provided by bootstrap system, the air flow bed reactor that the utility model provides is reaction medium and carrier with high-temperature fuel gas and modified gas, make ilmenite concentrate in reactor, be in certain flow state, have that the alternate contact area of gas-solid is big, full contact, heat and mass are effective, be swift in response, temperature is easy to advantages such as control; Air flow bed makes material present evenly good flow state simultaneously, sintering phenomenon when both having made it can not occur using rotary kiln, objectively also increased temperature of reaction, fast reaction speed, material is prone to channel and turbulent problem when having avoided using the fluidized-bed modification.Separately using simultaneously of high-temperature fuel gas and modified gas, the convenient flow of adjusting high-temperature fuel gas is applicable to varigrained ilmenite concentrate raw material to adjust gas flow rate, adaptability to raw material is strong, has enlarged the source of raw material.
In the utility model, the realization that most critical point separates for reaction mass, mainly utilize modification material and the different physical properties of the two proportion of unmodified material, general, the fullsized of ilmenite concentrate weighs about 4.0, and the material after the oxidizing roasting has been owing to absorbed oxygen element, and quality increases to some extent, volume dwindles approximately 6% after the simultaneous oxidation roasting than raw ore, and this causes the ilmenite concentrate fullsized after the oxidation modification to weigh more than 4.5.And during reducing roasting, because reducing gas captures the oxygen element in the oxidized ore, volume increases approximately about 10% after the material reducing roasting in addition, and the ilmenite concentrate fullsized after objectively causing reducing roasting to be finished heavily is down to about 4.0.Utilize almost identical air-flow thrust that the different material of proportion is subjected to and the composite factor of different gravity in airflow field, make it produce different casts at same horizontal plane, the less substance slinging of density is far away usually, otherwise distance is shorter.Therefore the utility model utilizes the difference of different specific weight materials casting distance, by regulating the flow velocity of high-temperature fuel gas and modified gas, in reactor, realized the separated in synchronization between modification ilmenite concentrate and the unreacted ilmenite concentrate, the two is collected respectively at pneumatic separation section different positions, the unreacted material returns by charging system and continues reaction, ilmenite concentrate material after modification is finished then is discharged from for next step operation and uses, and device has been realized serialization production on the whole.
In the utility model, taken full advantage of the difference of each section of reactor diameter, to obtain different reaction effects.In the air-flow section that distributes, diameter is less, utilizes less diameter to obtain gas flow rate faster, and reaction mass is flowed very soon from stationary state, has strengthened gas-solid two alternate contact strength and heat and mass effect; And gas-solid reaction section diameter increases, and gas flow rate slows down, and the lift velocity of ilmenite concentrate material reduces, and makes reaction mass and modified gas full contact, has increased temperature of charge and roasting time, objectively also plays the effect that has reduced energy consumption; In the pneumatic separation section, diameter diminishes, and by contraction gas velocity is accelerated, its carrying material is gone out with the certain speed impelling by it, apart from difference, unmodified material and modification material are separately come the continuity production of implement device according to the materials casting of different specific weight.
According to the difference of industrial scale from 10000 tons/year～50000 tons/year, the diameter of the air flow bed reactor air-flow distribution section that the ilmenite concentrate modification is used is 1200mm～3000mm, the maximum diameter of gas-solid reaction section is 2400mm～7200mm, and the internal diameter ratio of generally controlling air-flow distribution section, the gentle flow point selections of gas-solid reaction section is 6: 15: 5～3: 9: 2.In order to make reactor that the enough reaction times be arranged, the height of control air-flow distribution section is at 2000～3500mm, the height of control gas-solid reaction section is at 6000～8600mm, and the length of pneumatic separation section is at 2000～3200 mm, and three's length ratio is 1: 2.4: 1～1: 3: 1.
Compare with more novel fluosolids roasting technology with traditional ilmenite concentrate rotary kiln roasting, utilizing the utility model device to prepare artificial rutile has following advantage:
(1) production efficiency height, the production cycle shortens
The utility model device can make ilmenite concentrate be in certain flow state in reactor, advantage such as have that the alternate contact area of gas-solid is big, full contact, heat and mass are effective, be swift in response, objectively shorten the production cycle, improved the production efficiency of device.
(2) energy consumption is few
Ilmenite concentrate and modified gas are in the short period of time, fully contact under the higher temperature, reduced energy consumption to a certain extent, in addition, device has utilized waste heat fully, with the fuel of reducing roasting tail gas as oxidizing roasting, oxidized tail gas is used for the preheating ilmenite concentrate, has reclaimed waste heat preferably, saved the consumption of the energy.
(3) simple to operate
Ilmenite concentrate is in flow state in modifying process, only require that gas velocity gets final product greater than a certain steady state value, and with respect to the strictness control of fluidization operation to gas velocity, its operation wants much simple.
(4) realized the scale operation of installing
The industrial scale of present domestic artificial rutile is 1000 tons/year～5000 tons/year, adopts circulating current bed apparatus scale of the present utility model to reach and can arrive 10000 tons/year～30000 tons/year, is domestic initiation, has reached economic scale.
(5) the raw material granularity requirement is low, and adaptability to raw material is strong
This device with high-temperature fuel gas and modified gas as the fluidised power of ilmenite concentrate raw material and carrier, high-temperature fuel gas and modified gas add inside reactor respectively, mix by sparger, under certain gas speed scope, all can operate, but improved operation capacity, the flow that only need adjust high-temperature fuel gas to the ilmenite concentrate of different-grain diameter distribution can obtain preferable reaction effect, so the adaptability of ilmenite concentrate raw material is strong.
(6) modified effect is good
Because the alternate contact area of ilmenite concentrate gas-solid in reactor is big, full contact, heat and mass are effective, can react under comparatively high temps, this has promoted the degree of depth and range that reaction is carried out to a great extent; And the cyclone of bootstrap system is not only recycled high-temperature gas in the device, also the trickle ore particle that has in the gas can be discharged system, and the size-grade distribution of modification material is improved.The two objectively makes the material modified effect improve.
Description of drawings
Fig. 1 is the structure iron of the utility model circulating current bed apparatus;
Fig. 2 is the structural representation of air flow bed reactor among Fig. 1.
Marginal data:
1-ilmenite concentrate feed bin; 2-ilmenite concentrate preheater; 3,8,10,15-self-conveyor feed; 4,11-hotblast stove; 5-oxidizing roasting fluidized-bed reactor; The already oxidised material feed bin of 6-; 7-is the oxidation material feed bin not; 9,16-cyclone; 12-reducing roasting air flow bed reactor; 13-does not reduce the material feed bin; 14-has reduced the material feed bin;
501-modified gas sparger; 502-combustion gas sparger; 503-air-flow distribution section; 504-gas-solid reaction section; 505-pneumatic separation section; 508-modified gas entrance; The 509-fuel gas inlet; 510-ilmenite concentrate opening for feed; 511-returns opening for feed; The big proportion material outlet of 512-; The little proportion material outlet of 513-; The outlet of 514-tail gas; The 515-discharging section.
Embodiment
In order to be expressly understood the purpose of this utility model, technical scheme and beneficial effect more, below in conjunction with accompanying drawing the utility model is described further, but protection domain of the present utility model is not limited in following examples.
The utility model provides a kind of circulating current bed apparatus of using for the modification of Production of Artificial Rutile ilmenite concentrate.In the utility model, because ilmenite concentrate is carrier with the hot gas flow, the alternate contact area of gas-solid is big, full contact, heat and mass are effective, therefore, have that adaptability to raw material is strong, sufficient reacting is rapid, simple to operate, energy consumption is low and the advantage of can serialization producing.The utility model utilizes the difference of different specific weight materials casting distance, by regulating the flow velocity of combustion gas and modified gas, has realized the separated in synchronization between modification ilmenite concentrate and the unreacted ilmenite concentrate in reactor, and device has been realized serialization production on the whole.
Referring to Fig. 1, a kind of ilmenite concentrate modification circulating current bed apparatus of the utility model comprises that air flow bed reactor, ilmenite concentrate charging system, gas enter system, bootstrap system and discharge system.
(1) described ilmenite concentrate charging system comprises ilmenite concentrate feed bin 1, ilmenite concentrate preheater 2 and self-conveyor feed 3 or 10, is used for to the ilmenite concentrate solid materials of fluidized-bed reactor conveying after preheating.The ilmenite concentrate feed bin is used for the storage of raw materials, according to the practical situation of producing ilmenite concentrate is added in the pre-hot aggregate bin, enters by self-conveyor feed after the ilmenite concentrate preheating and carries out modified-reaction in the air flow bed reactor.
(2) described gas enters system and comprises hotblast stove 4,11 and the modified gas storage tank.Hotblast stove mainly provides high-temperature fuel gas, for modified gas provides certain heat.The modified gas storage tank provides oxidizing roasting with modified gas and reducing roasting modified gas respectively according to the modifying function difference.The flow of high-temperature fuel gas and modified gas can be regulated according to the practical situation of reaction.
(3) described bootstrap system is made up of pipeline and cyclone 9 or 16, mainly be that the high-temperature tail gas that fluidized-bed reactor comes out is recycled the preheating ilmenite concentrate, fine particles ore deposit in the ilmenite concentrate is collected, make it not enter into step operation down, objectively improve the size-grade distribution of ilmenite concentrate.
(4) described discharge system comprises feed bin and self-conveyor feed 8 or 15.Described feed bin comprise already oxidised material feed bin 6, not oxidation material feed bin 7, reduce material feed bin 14 and the material feed bin 13 that do not reduce.It mainly acts on is that the ilmenite concentrate after the modification is discharged reactor, and unreacted material Returning reactor is continued modification.
At length explain according to the air flow bed reactor in the utility model air flow bed device below in conjunction with Fig. 2.
Referring to Fig. 2, air flow bed reactor described in the utility model comprises oxidizing roasting air flow bed reactor 5 and reducing roasting air flow bed reactor 12, described air flow bed reactor comprises air-flow distribution section 503, gas-solid reaction section 504, pneumatic separation section 505 and discharging section 515, be provided with fuel gas inlet 509, modified gas entrance 508, ilmenite concentrate opening for feed 510, returns opening for feed 511, tail gas outlet 514 and material outlet, described material outlet comprises big proportion material outlet 512 and little proportion material outlet 513.
Described modified gas entrance 508 is arranged on described air-flow distribution section 503 bottoms, fuel gas inlet 509 is arranged on air-flow distribution section 505 bottoms, ilmenite concentrate opening for feed 510 and returns opening for feed 511 are arranged on described gas-solid reaction section 504 bottoms, tail gas outlet 514 is arranged on discharging section 515 tops, and material outlet is arranged on discharging section 515 bottoms.
The internal diameter ratio of described air-flow distribution section, the gentle flow point selections of gas-solid reaction section is 6: 15: 5～3: 9: 2, and the length ratio is 1: 2.4: 1～1: 3: 1.
In order to make gas distribution even, described air-flow distribution section is provided with modified gas sparger 501 and combustion gas sparger 502.The modified gas sparger adopts the filler mode.High-temperature fuel gas and modified gas mix and make constant flow rate by sparger after entering reactor by fuel gas inlet and modified gas entrance.
With reference to Fig. 1,2, ilmenite concentrate experiences following course in the utility model air flow bed device:
At first, ilmenite concentrate comes out from feed bin 1, and oxidized roasting tail gas is preheating to certain temperature preheater 2, by self-conveyor feed 3 it is added the people in air flow bed reactor 5 with certain speed then, meanwhile, hotblast stove combustion gas and modified gas are added in the reactor 5 simultaneously.When ilmenite concentrate enters reactor, hot gas flow is heated certain temperature and keeps certain speed with its lifting and in air-flow distributes section 503, when ilmenite concentrate enters gas-solid reaction section 504, because gas velocity descends, the ilmenite concentrate lift velocity also reduces, this has prolonged the material reaction time to a certain extent, when ilmenite concentrate enters pneumatic separation section 503, because the contraction of air flow bed reactor diameter, gas velocity accelerates, the thrust that its material that carries is subjected to strengthens, and material can show different cast because proportion is different under this reactive force, and the material of collector difference " impelling " distance separates and collects.In oxidizing roasting, heavy material enters into reducing roasting by self-conveyor feed 10 discharges and carries out reducing roasting with air flow bed reactor 12, and the material that proportion is little is then continued reaction in self-conveyor feed 8 Returning reactors 5; In like manner, in reducing roasting, the material that material proportion is bigger is reacted by continuation in self-conveyor feed 15 Returning reactors 12, and the material that proportion is little is discharged from the reaction of participating in next step operation.
In said process, the tail gas of oxidizing roasting is used for the preheating ilmenite concentrate after by cyclone 9 dedustings, and the tail gas of reducing roasting is used as the fuel gas of oxidizing roasting after by cyclone 16 dedustings.Ilmenite concentrate in the dust-precipitator can be used as the raw material of titanium white production.
Claims (9)
1. ilmenite concentrate modification circulating current bed apparatus, comprise the air flow bed reactor, the ilmenite concentrate charging system, gas enters system, bootstrap system and discharge system, described air flow bed reactor comprises oxidizing roasting air flow bed reactor and reducing roasting air flow bed reactor, it is characterized in that: described air flow bed reactor comprises air-flow distribution section, the gas-solid reaction section, pneumatic separation section and discharging section, be provided with fuel gas inlet, the modified gas entrance, the ilmenite concentrate opening for feed, the returns opening for feed, tail gas outlet and material outlet, described material outlet comprises big proportion material outlet and little proportion material outlet.
2. a kind of ilmenite concentrate modification circulating current bed apparatus according to claim 1, it is characterized in that: described modified gas entrance is arranged on described air-flow distribution section bottom, fuel gas inlet is arranged on air-flow distribution pars infrasegmentalis, ilmenite concentrate opening for feed and returns opening for feed are arranged on described gas-solid reaction pars infrasegmentalis, the tail gas outlet is arranged on the discharging section top, and material outlet is arranged on the discharging section bottom.
3. a kind of ilmenite concentrate modification circulating current bed apparatus according to claim 1 and 2, it is characterized in that: the internal diameter ratio of described air-flow distribution section, the gentle flow point selections of gas-solid reaction section is 6: 15: 5～3: 9: 2, and the length ratio is 1: 2.4: 1～1: 3: 1.
4. a kind of ilmenite concentrate modification circulating current bed apparatus according to claim 1 is characterized in that: the described air-flow section that distributes is provided with modified gas sparger and combustion gas sparger.
5. a kind of ilmenite concentrate modification circulating current bed apparatus according to claim 1, it is characterized in that: described ilmenite concentrate charging system comprises ilmenite concentrate feed bin, ilmenite concentrate preheater and self-conveyor feed.
6. a kind of ilmenite concentrate modification circulating current bed apparatus according to claim 1, it is characterized in that: described gas enters system and comprises hotblast stove and modified gas storage tank.
7. a kind of ilmenite concentrate modification circulating current bed apparatus according to claim 1, it is characterized in that: described bootstrap system is made up of pipeline and cyclone.
8. a kind of ilmenite concentrate modification circulating current bed apparatus according to claim 1, it is characterized in that: described discharge system comprises feed bin and self-conveyor feed.
9. a kind of ilmenite concentrate modification circulating current bed apparatus according to claim 8 is characterized in that: described feed bin comprise already oxidised material feed bin, not the oxidation material feed bin, reduce material feed bin and the material feed bin that do not reduce.
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| CN2013201585738U CN203173849U (en) | 2013-04-02 | 2013-04-02 | Circulating entrained-flow bed device for modifying titanium concentrate |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103145182A (en) * | 2013-04-02 | 2013-06-12 | 宜宾天原集团股份有限公司 | Circulating air bed device for modification of titanium concentrate |
| CN112138862A (en) * | 2020-08-13 | 2020-12-29 | 中国矿业大学 | Method for improving magnetic composition of medium for coal dressing |
| CN114659340A (en) * | 2022-03-17 | 2022-06-24 | 江西东鹏新材料有限责任公司 | Manufacturing device and manufacturing method of super battery-grade lithium hydroxide |
-
2013
- 2013-04-02 CN CN2013201585738U patent/CN203173849U/en not_active Expired - Lifetime
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103145182A (en) * | 2013-04-02 | 2013-06-12 | 宜宾天原集团股份有限公司 | Circulating air bed device for modification of titanium concentrate |
| CN103145182B (en) * | 2013-04-02 | 2014-08-13 | 宜宾天原集团股份有限公司 | Circulating air bed device for modification of titanium concentrate |
| CN112138862A (en) * | 2020-08-13 | 2020-12-29 | 中国矿业大学 | Method for improving magnetic composition of medium for coal dressing |
| CN112138862B (en) * | 2020-08-13 | 2022-03-29 | 中国矿业大学 | Method for improving magnetic composition of medium for coal dressing |
| CN114659340A (en) * | 2022-03-17 | 2022-06-24 | 江西东鹏新材料有限责任公司 | Manufacturing device and manufacturing method of super battery-grade lithium hydroxide |
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