CN101142329A - Process and plant for the heat treatment of solids containing titanium - Google Patents

Process and plant for the heat treatment of solids containing titanium Download PDF

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Publication number
CN101142329A
CN101142329A CNA2006800082984A CN200680008298A CN101142329A CN 101142329 A CN101142329 A CN 101142329A CN A2006800082984 A CNA2006800082984 A CN A2006800082984A CN 200680008298 A CN200680008298 A CN 200680008298A CN 101142329 A CN101142329 A CN 101142329A
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reactor
separator
cooler
solid
gas
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A-N·贝扎维
L·弗曼尼克
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Metso Outotec Oyj
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Outokumpu Technology Oyj
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    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B34/00—Obtaining refractory metals
    • C22B34/10—Obtaining titanium, zirconium or hafnium
    • C22B34/12—Obtaining titanium or titanium compounds from ores or scrap by metallurgical processing; preparation of titanium compounds from other titanium compounds see C01G23/00 - C01G23/08
    • C22B34/1204—Obtaining titanium or titanium compounds from ores or scrap by metallurgical processing; preparation of titanium compounds from other titanium compounds see C01G23/00 - C01G23/08 preliminary treatment of ores or scrap to eliminate non- titanium constituents, e.g. iron, without attacking the titanium constituent
    • C22B34/1209—Obtaining titanium or titanium compounds from ores or scrap by metallurgical processing; preparation of titanium compounds from other titanium compounds see C01G23/00 - C01G23/08 preliminary treatment of ores or scrap to eliminate non- titanium constituents, e.g. iron, without attacking the titanium constituent by dry processes, e.g. with selective chlorination of iron or with formation of a titanium bearing slag
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B1/00—Preliminary treatment of ores or scrap
    • C22B1/02—Roasting processes
    • C22B1/10—Roasting processes in fluidised form
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B34/00—Obtaining refractory metals
    • C22B34/10—Obtaining titanium, zirconium or hafnium
    • C22B34/12—Obtaining titanium or titanium compounds from ores or scrap by metallurgical processing; preparation of titanium compounds from other titanium compounds see C01G23/00 - C01G23/08
    • C22B34/1218—Obtaining titanium or titanium compounds from ores or scrap by metallurgical processing; preparation of titanium compounds from other titanium compounds see C01G23/00 - C01G23/08 obtaining titanium or titanium compounds from ores or scrap by dry processes
    • C22B34/1227—Obtaining titanium or titanium compounds from ores or scrap by metallurgical processing; preparation of titanium compounds from other titanium compounds see C01G23/00 - C01G23/08 obtaining titanium or titanium compounds from ores or scrap by dry processes using an oxygen containing agent
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B5/00—General methods of reducing to metals
    • C22B5/02—Dry methods smelting of sulfides or formation of mattes
    • C22B5/12—Dry methods smelting of sulfides or formation of mattes by gases
    • C22B5/14—Dry methods smelting of sulfides or formation of mattes by gases fluidised material

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • General Life Sciences & Earth Sciences (AREA)
  • Geology (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Mechanical Engineering (AREA)
  • Materials Engineering (AREA)
  • Manufacturing & Machinery (AREA)
  • Metallurgy (AREA)
  • Organic Chemistry (AREA)
  • Geochemistry & Mineralogy (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
  • Crucibles And Fluidized-Bed Furnaces (AREA)
  • Manufacture And Refinement Of Metals (AREA)
  • Inorganic Compounds Of Heavy Metals (AREA)

Abstract

This invention relates to a process and a plant for the heat treatment of solids containing titanium. For this purpose, the fine-grained solids are heated to a temperature of 700 to 1000 DEG C in a reactor (4) with circulating fluidized bed and are partly discharged from the reactor (4) together with waste gases into a downstream separator (9). In the same, the solids are separated from the waste gases and are recirculated to the reactor (4) at least partly and/or phase by phase. According to the invention, the heat treatment is performed under oxidizing conditions.

Description

The thermal treatment process of solids containing titanium and equipment
The present invention relates to a kind of thermal treatment process of solids containing titanium, wherein in having the reactor of circulating fluidized bed, the solid of particulate is heated to 700 to 1000 ℃ of temperature, and enter the separator in downstream from reactor with waste gas, solid separates with waste gas in separator, and is re-circulated to reactor at least in part and/or by stages.In addition, the present invention relates to a kind of corresponding apparatus.
This technology and equipment for example are applied to ilmenite (X*TiO 2Y*FeOZ*Fe 2O 3) magnetization calcining.Use reactor magnetization calcination of ilmenite in the past, but this reactor only have little span of control and low reaction density with stationary fluidized bed.In addition, when use has the reactor of stationary fluidized bed, consider vessel volume, only may reach quite low flow velocity.For this reactor with stationary fluidized bed, the control of temperature and hold-time also usually is ill.
Therefore, it also is known magnetizing calcining in having the reactor of circulating fluidized bed under oxidizing condition.For this purpose, in reactor, be blown into hot gas with the solid fluidisation by tuyere bottom (gas distributor).This hot gas externally produces in the burner mostly, and for example Sweet natural gas or oil fuel and ambient air wherein burn.With the solid that waste gas is discharged from reactor, in separator, separate and be re-circulated in the reactor at least in part with waste gas.Again circulate from separator and enter reactor in order to control solid, use one so-called " L valve ", can control by supply gas.
In further treatment reactor, before the incinerating ilmenite, it must be cooled off., be well known that for this reason, for example use fluidized bed cooler, the heat of the product that scatters and disappears therein.But, in these known technologies and equipment, the variation of calcination of ilmenite in the cooling period process, may occur magnetizing, thereby the magnetic property in the front that had before reached descends once more.
Therefore, the purpose of this invention is to provide a kind of aforesaid technology, wherein can handle being unsuitable for magnetization incinerating ilmenite under oxidizing condition, thereby avoid the model change after the thermal treatment greatly.
According to the present invention, this purpose realizes by calcination of ilmenite under reductive condition.
In order to improve the quality of products and for fear of the model change after thermal treatment, the downstream of reactor and/or separator is refrigerating unit preferably, it can realize chilled product at a good pace.This can cool off indirectly by irrigation or spray cooler, perhaps by directly cooling of water spray.Preferably, shower cooler is provided, wherein by ejected coolant with below the solid cooled to 250 ℃, and may in another water cooler in shower cooler downstream, further cool off, fluidized bed cooler for example, fluidizing agent enters particle-froude-number that the gas velocity of shower cooler makes fluidized-bed between 0.01 to 10, particularly between 0.1 to 1.Preferably, the particle-froude-number bottom fluidized bed cooler is about 0.17 especially between 0.1 to 0.25.At the fluidized bed cooler top, particle-froude-number preferably between 0.35 to 0.55, is about 0.47 especially.
Each particle-froude-number is defined by following equation:
Fr p = u ( ρ s - ρ f ) ρ f * d p * g
In the formula,
U is the effective velocity of air-flow, m/s;
ρ fBe the effective density of fluidizing agent, kg/m 3
ρ sBe density of solid particles, kg/m 3(apparent density);
d pIt is the mean diameter of reactor content particle m in the reactor operation process (the perhaps secondary granule of Xing Chenging);
G is a universal gravity constant, m/s 2
When using this equation, should consider d pMean diameter (the d that does not represent material therefor 50), but the mean diameter of the reactor content that in the reactor operation process, forms, this mean diameter with used material (primary particle) is obviously different.
In technology according to the present invention, the product that takes out from reactor or separator at first obviously is cooled to for example about 100 to 200 ℃ in very short time refrigerating unit.Can avoid magnetizing the variation of calcination of ilmenite in the cooling period process by this way.Because cooling can obtain the extra high magnetization calcination of ilmenite of quality product fast.High production assurance is the separation degree height in magnetic resolution process subsequently.Because temperature range is big in process of cooling, therefore must not only to note the variation of product, and to regulate quantity and the speed that the input shower cooler is used for fluidizing gas rightly, shower cooler is preferably as refrigerating unit, and is too many thereby fluidized-bed can not expand when the refrigerant volatilization of spraying.According to the present invention, the gas velocity of the fluidizing agent in the shower cooler is chosen as obtains quite thick fluidized-bed thus.Fluidized-bed is dense at the top of shower cooler at the bottom of shower cooler ratio, because the refrigerant that sprays volatilizees at the top.Fluidized bed cooler in the shower cooler downstream, the product heat that will die in technology distributes.
Preferably, eject water to shower cooler as refrigerant.Be included in steam between 50 to 70%, particularly about 60% steam at the gas content of the fluidized-bed of shower cooler thus.
According to technology of the present invention, contain the ore of titanium for all, particularly those also contain the ore of the oxide compound of iron, can heat-treat effectively.Particularly, this technology is suitable for magnetizing calcination of ilmenite.Be fed to the solid mean particle size (d of reactor 50) preferably between 75 to 350 μ m, particularly between 100 to 150 μ m.The solid maximum particle size that is fed to reactor is 2mm approximately, preferably less than 250 μ m.The granularity of magnetization incinerating ilmenite preferably is in the above-mentioned same range as in reactor.
Producing the required heat of reactor work can be this known any way of expert on the one hand.According to a preferred embodiment of the present invention, providing required heat is by supplying the solid of hot gas or preheating.Preferably, to reactor input gaseous reducing agent, for example molecular hydrogen, the gaseous mixture that contains molecular hydrogen, carbon monoxide or contain the gaseous mixture of carbon monoxide are as reformation coal gas.In reactor, produce above-mentioned reducing gas and also be fine, for example the burning that is lower than stoichiometric ratio by fuel (as Sweet natural gas, oil or coal).
In technology according to the present invention, when the hold-time of solid in reactor between 10 to 50 minutes, when being about 30 minutes especially, can reach extra high quality product.Particle-froude-number in the reactor is in about scope of 0.3 to 30, particularly between 0.5 to 15.
The energy expenditure of technology can reduce because in separator, reactor exhaust of at least a portion and solids constituent from and be fed to the preheating station of reactor upstream.Preheating station can comprise, for example such as the heat exchanger of Venturi preheater, and such as separators such as whirlwind.By this way, will be fed to the solid drying and the preheating of reactor, promote the thermal treatment in the reactor thus.Multistage pre-hot solids also is fine, and the waste gas of reactor progressively cools off.
According to development of the present invention, can provide the waste gas of reactor to clean at the exhaust gas cleaning station in preheating station downstream with the waste gas that for example shower cooler is mixed with steam.Then, gas can be re-circulated in the technology.
According to a preferred embodiment of the present invention, solid is re-circulated to reactor from separator and carries out in the inherent regulation mode.By this way, can realize the inside and outside mixing again of processed solid intensive in reactor, thereby in reactor, realize uniform temperature and reaction profile.
An apparatus according to the invention is particularly suitable for carrying out above-mentioned technology, comprises the reactor with circulating fluidized bed, has separator in its downstream.Downstream at reactor and/or separator can also have refrigerating unit, and refrigerating unit forms shower cooler, and its downstream is independent fluidized bed cooler.In shower cooler, by spraying for example water, product is cooled off fast, promptly reaches for example temperature between 100 to 200 ℃ in several seconds.This cooling for the first time fast is conclusive for quality product, because for example magnetize in the calcination process at ilmenite, may occur model change in oversize cooling time in the process.In addition, the final cooling of product is to carry out in independent fluidized bed cooler, and this fluidized bed cooler is in the shower cooler downstream.
Preferably, have cooling coil in fluidized bed cooler, refrigerant is oppositely by this cooling coil.This cooling coil for example can be combined to form cooling tube bundle.
When fluidized bed cooler has two or more chambers, when fluidizing agent is imported through its bottom by gas blower, in fluidized bed cooler, distribute the product heat of dying in the technology especially effectively.Fluidizing agent is used for chilled product on the one hand, is used to the strong mixing mutually of solid that is cooled simultaneously.
Handle required temperature in order to regulate solid thermal, reactor preferably has independent combustion chamber, upstream, wherein produces hot gas.But it can provide the spray gun assembly and/or the bottom tuyeres of for example arranged transversely of opening in the combustion chamber equally, and spray gun assembly and/or bottom tuyeres are used to connect the supply line of special gaseous reducing agent, thereby makes fuel in the reactor internal combustion.
According to a preferred embodiment of the present invention, the sealing of inherent regulation U-shaped is set between reactor and separator, controls solid thus and be fed to reactor from separator.Can omit a kind of Controlling System of costliness thus, for example use the known L valve of prior art.
For the water that reduces equipment can consume, in the reactor upstream preheating station is set, solid is drying and preheating in this reactor.Preheating station comprises for example moisture eliminator, the exhaust pipeline of the separator in its ligation device downstream, thereby utilize the heat that exists in the off-gas flows predrying/pre-hot solids.
From following embodiment description and accompanying drawing, can draw other development of the present invention, advantage and possible application.Here describe and/or illustrated all features itself or be combined to form theme of the present invention with any, and no matter it comprise in the claims or its support reference in.
An only width of cloth figure represents the artwork of technology and equipment according to an embodiment of the invention.
In technique shown in the drawings, this technique is particularly suitable for magnetization calcining solids containing titanium, and ilmenite is for example inputted preheating station by screw conveyor 1 with moist solids. This preheating station comprises venturi drier 2, and its Raw is suspended, drying and preheating; And at the separator 3 in venturi drier 2 downstreams, for example cyclone separator. The solid that in separator 3, separates with the waste gas reactor 4 of packing into.
Reactor 4 consists of the fluidized-bed reactor with recirculating fluidized bed. For fluidized solid, in reactor 4, have bottom tuyeres, utilize hair-dryer 5 to input thus gas, for example air or have the mixture of air. By lateral lances 6 natural gas supply is arrived reactor 4, in reactor, burn with fluidizing gas. Selectable or in addition, fuel can utilize bottom tuyeres to pass through pipeline 7 input reactors 4. In this burning, adjustments of gas composition, for example CO and CO2Content, make ilmenite magnetization calcining or baking. The reduction potential of gas depends on CO:CO2Relation.
In fluidized-bed reactor 4, solid is fluidized gas and upwards drives. The part solid is separated in reactor, is re-circulated to thus recirculating fluidized bed, again upwards drives in order to be fluidized gas. Another part solid is upwards discharged by pipeline 8 with the off-gas flows of reactor 4, and enters downstream separator 9, cyclone separator for example, and most of and gas stream from. By pipeline 10 solid of separator 9 is re-circulated to fluidized-bed reactor 4. By this strong inside and outside again mixing, in fluidized-bed reactor 4 inner especially uniformly temperature and the reaction profile of forming.
By being arranged on the self-regulation U-shaped sealing 11 in the pipeline 10, can control the amount of solids that is re-circulated to fluidized-bed reactor 4 from separator 9. As a result, can omit control and the regulon that metering is re-circulated to the amount of solids of fluidized-bed reactor 4.
The gas flow that separates with solid in separator 9 is fed to venturi drier 2, thereby utilizes the dry and pre-hot solids of heat of the gas flow that leaves separator 9.
Take out the solid of heat from fluidized-bed reactor 4 and/or separator 9, and be fed to shower cooler 13 by pipeline 12a and 12b respectively. In shower cooler 13, fluidisation hot solids in stationary fluidized bed. For this reason, by air blast 14 air is inputted shower cooler 13 as fluidization air. The selection of the gas velocity of fluidizing gas is so that the fluidisation of shower cooler 13 is low, and is very little thereby stationary fluidized bed only expands. Simultaneously, by pipeline 15 with water as refrigerant injection in shower cooler 13. Water evaporates in shower cooler 13, thereby surpasses the bottom section of shower cooler in the expansion of the stationary fluidized bed in shower cooler 13 districts. By injection water, hot product is cooled fast to for example is lower than 200 ℃ temperature.
Have independent fluidized bed cooler 16 in the downstream of shower cooler 13, wherein distribute the product heat that in technique, does not re-use. In the illustrated embodiment, fluidized bed cooler has two chamber 16a and 16b, and for example water is oppositely inputted wherein through the cooling coil 17 that schematically shows as cooling agent, need thus product further to be cooled to the further temperature of processing, for example Magnetic Isolation. For fluidisation and cooling products, air is inputted two chamber 16a and the 16b of fluidized bed cooler 16 by air blast 18. Then, the product with cooling is fed to subsequently processing procedure by pipeline 19.
Be connected with exhaust gas cleaning station 20 by separator 3, shower cooler 13 and the fluidized bed cooler 16 of pipeline with preheating station, the exhaust gas cleaning station for example has bag filter. In this exhaust gas cleaning station 20, the gas flow that part is contained solid and/or steam cleans. Solid is by pipeline 21 fluidized bed cooler 16 of packing into from exhaust gas cleaning station 20.
Embodiment (the magnetization calcining of ilmenite)
In ilmenite shown in the drawings magnetization calciner, by screw conveyor 1 with 43t/h with moist ilmenite from the hold tank venturi drier 2 of packing into.In venturi drier 2, the hot waste gas of separator 9 is with moist ilmenite suspension, drying and preheating.In the cyclonic separator 3 that is in venturi drier 2 downstreams, separate with gas stream with the ilmenite of preheating dry, and input has the reactor 4 of circulating fluidized bed.
The waste gas feed of cyclonic separator 3 is to exhaust gas cleaning station 20, partly circulation and oxidation and be fed to chimney again.To directly enter product flow 19 through pipeline by 20 isolating dry ferrotianium calxs at the exhaust gas cleaning station.
By gas blower 5, with 46000Nm 3The gas of/h (comprises 15000Nm 3The air of/h and 31000Nm 3/ h is round-robin waste gas again) inlet flow fluidized bed reactor 4 carries out fluidisation.Simultaneously, will about 1800Nm 3The Sweet natural gas of/h is fed to reactor 4 by lateral lances 6 and pipeline 7, and burns with air in fluidized-bed.The reducing gas that obtains thus makes the temperature that is contained in the ilmenite in the fluidized-bed reactor 4 reach about 800 ℃, and the particle-froude-number in the reactor is about 1.2.The magnetization of ilmenite calcining is to realize between 10 to 50 minutes the time in the solid hold-time.
Solid is transported to separator 9 with the waste gas of reactor 4, and it is re-circulated to reactor 4 in this separation and great majority by pipeline 10.Quantity is fed to shower cooler 13 by pipeline 12a and 12b respectively corresponding to the ilmenite product of the quantity of the reactor 4 of packing into.The ilmenite of reactor 4 and the mean particle size (d of the ilmenite after the calcining pack into 50) being about 100 to 150 μ m, maximum particle size is about 250 μ m.
The operation of shower cooler 13 is as stationary fluidized bed, with 6300Nm 3/ h round-robin waste gas again is fed to shower cooler 13 as fluidizing agent by gas blower 14.Simultaneously, by pipeline 15 with 8m 3/ h water input shower cooler 13, thus hot ilmenite in seconds is cooled to about 150 ℃.Because evaporation of water, about 60% of the gas gross of the fluidized-bed of shower cooler 13 is a steam.The gas velocity of the fluidizing agent that is blown into by gas blower 14 is chosen to make the particle-froude-number of shower cooler 13 bottoms to be about 0.17, is about 0.47 at shower cooler 13 tops.
The final cooling of product is carried out in two chamber 16a of fluidized bed cooler 16 and 16b.For fluidisation, will about 6000Nm 3/ h round-robin waste gas again imports fluidized bed coolers 16 by gas blower 18.Simultaneously, water coolant passes through pipeline 17 oppositely through chamber 16a and 16b.In chamber 16a and 16b, pipeline 17 has cooling tube bundle.
By this way, can realize the reduction magnetic calcining of ilmenite, and because cooling fast do not detect variation in the cooling period process, thereby calcination of ilmenite has high quality product.
List of reference numerals
1 screw conveyor
2 venturi drier
3 cyclonic separators
4 fluidized-bed reactors
5 gas blowers
6 spray guns
7 pipelines
8 pipelines
9 separators
10 pipelines
The sealing of 11 U-shapeds
12a, the 12b pipeline
13 shower coolers
14 gas blowers
15 pipelines
16 fluidized bed coolers
16a, the 16b chamber
17 pipelines
18 gas blowers
19 pipelines
20 exhaust gas cleaning stations
21 pipelines

Claims (22)

1. the technology of a thermal treatment solids containing titanium, wherein fine-grained solids is heated to 700 to 1000 ℃ in having the reactor of circulating fluidized bed (4), and partly be discharged into the separator (9) in downstream from reactor (4) with waste gas, solid separates with waste gas in separator (9) and is re-circulated to reactor (4) at least in part and/or by stages, it is characterized in that thermal treatment carries out under reductive condition.
2. technology according to claim 1, it is characterized in that having refrigerating unit in the downstream of reactor (4) and/or separator (9), fluidised-bed spray water cooler (13) preferably, in shower cooler (13) by ejected coolant with below the solid cooled to 250 ℃, and fluidizing agent is imported shower cooler (13), gas velocity be set at make fluidized-bed particle-froude-number between 0.01 to 10, particularly between 0.1 to 1.
3. technology according to claim 2 is characterized in that particle-froude-number in shower cooler (13) bottom between 0.1 and 0.25, is about 0.17 especially.
4. according to claim 2 or 3 described technologies, it is characterized in that particle-froude-number at shower cooler (13) top between 0.35 and 0.55, is about 0.47 especially.
5. each the described technology that requires according to aforesaid right is characterized in that the fluidized bed gas content in shower cooler (13) comprises 50 to 70%, is about 60% steam especially.
6. each the described technology that requires according to aforesaid right is characterized in that having fluidized bed cooler (16) in the downstream of shower cooler (13).
7. each the described technology that requires according to aforesaid right is characterized in that ilmenite is as raw material.
8. according to each described technology of aforesaid right requirement, it is characterized in that being fed to the solid mean particle size (d of reactor (4) 50) between 75 to 250 μ m, particularly between 100 to 150 μ m.
9. technology according to claim 7, the solid maximum particle size that it is characterized in that being fed to reactor (4) is 2mm, particularly less than 350 μ m.
10. each the described technology that requires according to aforesaid right is characterized in that supplying fuel to reactor (4), produces reducing gas with the burning of oxygen-containing gas by it in reactor (4).
11. technology according to claim 10 is characterized in that gaseous fuel, preferably Sweet natural gas by spray gun (6) and/or by bottom tuyeres input reactor (4), and inputs to the small part air as fluidizing agent.
12. each the described technology according to aforesaid right requires is characterized in that the mean holding time of solid in reactor (4) between 10 to 50 minutes, is about 30 minutes especially.
13. each described technology according to the aforesaid right requirement, what it is characterized in that reactor (4) separates and is fed to the preheating station (2,3) with moisture eliminator (2) and separator (3) of reactor (4) upstream substantially to small part waste gas with solid in separator (9), be used for the solid that dry and preheating is fed to reactor (4).
14. technology according to claim 13 is characterized in that the waste gas that is loaded with steam of the waste gas of reactor (4) with shower cooler (13), in the exhaust gas cleaning station (20) in preheating station (2,3) downstream cleaning.
15. require each described technology according to aforesaid right, it is characterized in that solid is re-circulated to reactor (4) from separator (9) and carries out in the inherent regulation mode.
16. an execution requires the equipment of the technology of each described thermal treatment solids containing titanium according to aforesaid right, comprise reactor (4) with circulating fluidized bed, the downstream of reactor (4) has separator (9), it is characterized in that having the solid primary heater unit, have shower cooler (13) in its downstream in the upstream of reactor (4) and/or separator (9).
17. equipment according to claim 16 is characterized in that having fluidized bed cooler (16) in reactor (4) downstream.
18. equipment according to claim 17 is characterized in that fluidized bed cooler (16) has cooling coil, refrigerant flows through described cooling coil upstream.
19. according to claim 17 or 18 described equipment, it is characterized in that fluidized bed cooler (16) has two or more chambers (16a, 16b), fluidizing agent flows through the bottom of described chamber by gas blower (18).
20. each described equipment according to claim 16 to 19, it is characterized in that reactor (4) has spray gun assembly (6), it is open in reactor (4) and/or the bottom tuyeres, and reactor (4) and/or bottom opening link to each other with special gaseous combustion supply line (7).
21. according to each described equipment of claim 16 to 20, it is characterized in that between reactor (4) and separator (9), having inherent regulation U-shaped sealing (11), be used to control the solid supply from the separator to the reactor.
22., it is characterized in that having solid preheating station (2,3), the exhaust pipeline of the separator (9) in its moisture eliminator (2) ligation device (4) downstream in reactor (4) upstream according to each described equipment of claim 16 to 21.
CNA2006800082984A 2005-03-16 2006-03-14 Process and plant for the heat treatment of solids containing titanium Pending CN101142329A (en)

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UA (1) UA91354C2 (en)
WO (1) WO2006097569A1 (en)
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CN102410706A (en) * 2011-11-03 2012-04-11 云南新立有色金属有限公司 Fluidized bed drying method of ilmenite powder
CN103031433A (en) * 2011-09-30 2013-04-10 中国科学院过程工程研究所 Fluidized oxidation roasting-fluidized reduction roasting system and roasting process for titaniferous iron concentrate
CN103031432A (en) * 2011-09-30 2013-04-10 中国科学院过程工程研究所 System for fluidized oxidizing/reducing roasting modification of titaniferous iron concentrate and roasting process
CN108291714A (en) * 2015-10-08 2018-07-17 因姆普朗伯德公司 Method for running fluidized-bed combustion boiler
CN108700289A (en) * 2015-10-08 2018-10-23 因姆普朗伯德公司 Bed management cycle for fluidized-bed combustion boiler and corresponding device
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DE2524540C2 (en) * 1975-06-03 1986-04-24 Metallgesellschaft Ag, 6000 Frankfurt Process for performing endothermic processes
AU765620B2 (en) * 1998-11-23 2003-09-25 Outotec Oyj Process of reducing ilmenite
DE10260737B4 (en) * 2002-12-23 2005-06-30 Outokumpu Oyj Process and plant for the heat treatment of titanium-containing solids

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ZA200503457B (en) 2006-02-22
CA2599564A1 (en) 2006-09-21
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NO20075289L (en) 2007-12-10
CA2599564C (en) 2016-05-24

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