CA2599564C - 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 PDFInfo
- Publication number
- CA2599564C CA2599564C CA2599564A CA2599564A CA2599564C CA 2599564 C CA2599564 C CA 2599564C CA 2599564 A CA2599564 A CA 2599564A CA 2599564 A CA2599564 A CA 2599564A CA 2599564 C CA2599564 C CA 2599564C
- Authority
- CA
- Canada
- Prior art keywords
- reactor
- solids
- separator
- gas
- cooler
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Fee Related
Links
Classifications
-
- 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
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°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 reducing conditions.
Description
Process and Plant for the Heat Treatment of Solids Containing Titanium The present invention relates to a process for the heat treatment of solids containing titanium, in which fine-grained solids are heated to a temperature of 700 to 1000 C in a reactor with circulating fluidized bed and are discharged from the reactor together with waste gases into a downstream separator, in which the solids are separated from the waste gases and are recirculated to the reactor at least partly and/or phase by phase. Furthermore, the invention relates to a corresponding plant.
Such processes and plants are used for instance for the magnetizing calcination of ilmenite (X*TiO2Y*FeOZ*Fe203). In the past, a reactor with stationary fluidized bed was used for the magnetizing calcination of ilmenite, which reactor has, however, only a small control range and a low reaction density. In addition, when using a reactor with stationary fluidized bed, only a comparatively low flow rate is possible with respect to the container volume.
The temperature and retention time control also frequently is unfavorable in the case of such reactors with stationary fluidized bed.
Therefore, it is also known to effect a magnetizing calcination of ilmenite under oxidizing conditions in reactors with a circulating fluidized bed. For this purpose, hot gas is introduced into the reactor through a tuyere bottom (gas distributor) for fluidizing the solids. This hot gas is mostly generated in an external burner, in which e.g. natural gas or fuel oil and ambient air are burnt. The solids discharged from the reactor together with the waste gases are separated from the waste gases in a separator and at least partly recirculated to the reactor.
For controlling the recirculation of solids from the separator into the reactor a so-called "L-valve" is used, which can be controlled by supplying gas.
Before the further processing of the ilmenite calcined in the reactor, the same must be cooled. To this end it is known, for instance, to use a fluidized-bed cooler, in which the product heat is dissipated. In these known processes and
Such processes and plants are used for instance for the magnetizing calcination of ilmenite (X*TiO2Y*FeOZ*Fe203). In the past, a reactor with stationary fluidized bed was used for the magnetizing calcination of ilmenite, which reactor has, however, only a small control range and a low reaction density. In addition, when using a reactor with stationary fluidized bed, only a comparatively low flow rate is possible with respect to the container volume.
The temperature and retention time control also frequently is unfavorable in the case of such reactors with stationary fluidized bed.
Therefore, it is also known to effect a magnetizing calcination of ilmenite under oxidizing conditions in reactors with a circulating fluidized bed. For this purpose, hot gas is introduced into the reactor through a tuyere bottom (gas distributor) for fluidizing the solids. This hot gas is mostly generated in an external burner, in which e.g. natural gas or fuel oil and ambient air are burnt. The solids discharged from the reactor together with the waste gases are separated from the waste gases in a separator and at least partly recirculated to the reactor.
For controlling the recirculation of solids from the separator into the reactor a so-called "L-valve" is used, which can be controlled by supplying gas.
Before the further processing of the ilmenite calcined in the reactor, the same must be cooled. To this end it is known, for instance, to use a fluidized-bed cooler, in which the product heat is dissipated. In these known processes and
2 plants it is, however, possible that changes in the magnetizing calcined ilmenite occur during the cooling period, so that the positive magnetic properties achieved beforehand are deteriorated again.
Therefore, it is the object of the present invention to provide a process as mentioned above, in which ilmenites can be treated that are not suited for magnetizing calcination under oxidizing conditions, wherein changes of the product after the heat treatment are largely avoided.
In accordance with one aspect of this invention, this object substantially is solved in that the ilmenite is calcined under reducing conditions.
In one aspect, there is provided a process for the heat treatment of solids containing titanium, in which fine-grained solids are heated to a temperature of 700 to 1000 C in a reactor with a circulating fluidized bed and are partly discharged from the reactor together with waste gases into a downstream separator, in which the solids are separated from the waste gases and are recirculated to the reactor at least partly and/or phase by phase, and wherein fuel is supplied to the reactor and combusted with an oxygen-containing gas to generate a reducing gas in the reactor such that the heat treatment of the solids is performed under reducing conditions. Also provided is a plant for performing the disclosed process for the heat treatment of solids containing titanium comprising a reactor with circulating fluidized bed, downstream of which a separator is provided, and upstream of the reactor and/or the separator a solids preheating device is provided and downstream of the reactor and/or the separator an injection cooler is provided. The reactor has a lance assembly opening into the same and/or bottom tuyeres, which are connected with at least one supply conduit that supplies gaseous fuel and an oxygen-containing gas to the reactor.
To improve the product quality and to avoid changes of the product after the heat treatment downstream of the reactor and/or the separator preferably a cooling apparatus, which allows for a relatively rapid cooling of the product. This may be effected by indirect cooling in an irrigation or shower cooler or by direct cooling by means of water injection. Preferably, an injection cooler is provided, in which the solids are cooled to below 250 C by injecting a coolant and possibly are cooled further in another cooler, for instance a fluidized-bed cooler, downstream =
2a of the injection cooler, fluidizing gas being introduced into the injection cooler with a gas velocity that the Particle-Froude-Number in the fluidized bed is between 0.01 and 10, in particular between 0.1 and 1.
Preferably, the Particle-Froude-Number at the bottom of the fluidized-bed cooler is between 0.1 and 0.25, in particular about 0.17. At the top of the fluidized-bed Gooier, the Particle-Froude-Number preferably is between 0.35 and 0.55, in particular about 0.47.
The Particle-Froude-Numbers are each defined by the following equation:
Frp liC . ¨PI *d *
p g Pf
Therefore, it is the object of the present invention to provide a process as mentioned above, in which ilmenites can be treated that are not suited for magnetizing calcination under oxidizing conditions, wherein changes of the product after the heat treatment are largely avoided.
In accordance with one aspect of this invention, this object substantially is solved in that the ilmenite is calcined under reducing conditions.
In one aspect, there is provided a process for the heat treatment of solids containing titanium, in which fine-grained solids are heated to a temperature of 700 to 1000 C in a reactor with a circulating fluidized bed and are partly discharged from the reactor together with waste gases into a downstream separator, in which the solids are separated from the waste gases and are recirculated to the reactor at least partly and/or phase by phase, and wherein fuel is supplied to the reactor and combusted with an oxygen-containing gas to generate a reducing gas in the reactor such that the heat treatment of the solids is performed under reducing conditions. Also provided is a plant for performing the disclosed process for the heat treatment of solids containing titanium comprising a reactor with circulating fluidized bed, downstream of which a separator is provided, and upstream of the reactor and/or the separator a solids preheating device is provided and downstream of the reactor and/or the separator an injection cooler is provided. The reactor has a lance assembly opening into the same and/or bottom tuyeres, which are connected with at least one supply conduit that supplies gaseous fuel and an oxygen-containing gas to the reactor.
To improve the product quality and to avoid changes of the product after the heat treatment downstream of the reactor and/or the separator preferably a cooling apparatus, which allows for a relatively rapid cooling of the product. This may be effected by indirect cooling in an irrigation or shower cooler or by direct cooling by means of water injection. Preferably, an injection cooler is provided, in which the solids are cooled to below 250 C by injecting a coolant and possibly are cooled further in another cooler, for instance a fluidized-bed cooler, downstream =
2a of the injection cooler, fluidizing gas being introduced into the injection cooler with a gas velocity that the Particle-Froude-Number in the fluidized bed is between 0.01 and 10, in particular between 0.1 and 1.
Preferably, the Particle-Froude-Number at the bottom of the fluidized-bed cooler is between 0.1 and 0.25, in particular about 0.17. At the top of the fluidized-bed Gooier, the Particle-Froude-Number preferably is between 0.35 and 0.55, in particular about 0.47.
The Particle-Froude-Numbers are each defined by the following equation:
Frp liC . ¨PI *d *
p g Pf
3 with effective velocity of the gas flow in m/s Af = effective density of the fluidizing gas in kg/m3 Ps = density of a solid particle in kg/m3 (apparent density) dp = mean diameter in m of the particles of the reactor inventory (or the secondary agglomerates formed) during operation of the reactor gravitational constant in m/s2.
When using this equation it should be considered that dp does not designate the mean diameter (d_50) of the material used, but the mean diameter of the io reactor inventory formed during operation of the reactor, which can differ significantly from the mean diameter of the material used (primary particles).
In this process in accordance with the invention, the product withdrawn from the reactor or the separator first of all is cooled very much in the cooling apparatus to e.g. about 100 to 200 C within a very short time. Changes in the magnetizingly calcined ilmenite during the cooling period largely can be avoided in this way. Due to the rapid cooling, a particularly high product quality of the magnetizingly calcined ilmenite thus can be achieved. This high product quality ensures a high degree of separation during a subsequent magnetic separation.
Due to the large temperature range during cooling it is necessary to not only take care of changes in the product, but to also properly adjust the quantity and velocity of the gas introduced for fluidization into the injection cooler, which is preferably used as the cooling apparatus, so that the fluidized bed does not expand too much when the injected coolant is evaporated. In accordance with the invention, the gas velocity of the fluidizing gas in the injection cooler therefore is chosen such that a comparatively dense fluidized bed is obtained.
The fluidized bed is denser at the bottom of the injection cooler than at the top of the injection cooler, as the coolant injected is evaporated there. In the fluidized-bed cooler downstream of the injection cooler, the product heat no longer usable in the process is dissipated.
When using this equation it should be considered that dp does not designate the mean diameter (d_50) of the material used, but the mean diameter of the io reactor inventory formed during operation of the reactor, which can differ significantly from the mean diameter of the material used (primary particles).
In this process in accordance with the invention, the product withdrawn from the reactor or the separator first of all is cooled very much in the cooling apparatus to e.g. about 100 to 200 C within a very short time. Changes in the magnetizingly calcined ilmenite during the cooling period largely can be avoided in this way. Due to the rapid cooling, a particularly high product quality of the magnetizingly calcined ilmenite thus can be achieved. This high product quality ensures a high degree of separation during a subsequent magnetic separation.
Due to the large temperature range during cooling it is necessary to not only take care of changes in the product, but to also properly adjust the quantity and velocity of the gas introduced for fluidization into the injection cooler, which is preferably used as the cooling apparatus, so that the fluidized bed does not expand too much when the injected coolant is evaporated. In accordance with the invention, the gas velocity of the fluidizing gas in the injection cooler therefore is chosen such that a comparatively dense fluidized bed is obtained.
The fluidized bed is denser at the bottom of the injection cooler than at the top of the injection cooler, as the coolant injected is evaporated there. In the fluidized-bed cooler downstream of the injection cooler, the product heat no longer usable in the process is dissipated.
4 Preferably, water is injected into the injection cooler as coolant. The gas content in the fluidized bed of the injection cooler then can include between 50 and 70%, in particular about 60 % steam.
With the process in accordance with the invention, all kinds of ores containing titanium, in particular those which additionally contain iron oxides, can be heat-treated effectively. In particular, the process is suited for the magnetizing calcination of ilmenite. The mean particle size (d_50) of the solids supplied to the reactor preferably is between 75 and 350 pm, in particular between about 100 and 150 urn. The maximum grain size of the solids supplied to the reactor is about 2 mm, preferably less than 250 pm. The grain size of the ilmenite magnetizingly calcined in the reactor preferably lies in the same ranges indicated above.
The generation of the amount of heat necessary for the operation of the reactor can be effected in any way known to the expert for this purpose. In accordance with a preferred embodiment of the invention it is provided to cover the required amount of heat by supplying hot gases or preheated solids. It is preferred to introduce a gaseous reducing agent, e.g. molecular hydrogen, gas mixtures containing molecular hydrogen, carbon monoxide or gas mixtures containing carbon monoxide, e.g. reformer gas, into the reactor. It is also possible to produce the above mentioned reducing gas in the reactor, e.g. by the unterstoichiometrical burning of fuels such as natural gas, oil or coal.
In the process in accordance with the invention, a particularly high product quality can be achieved when the retention time of the solids in the reactor is between 10 and 50 minutes, in particular about 30 minutes. The Particle-Froude-Number in the reactor can lie in a range from about 0.3 to 30, in particular between 0.5 and 15.
The energy consumption of the process can be reduced in that in the separator at least part of the waste gas of the reactor is separated from solids and supplied to a preheating stage upstream of the reactor. The preheating stage
With the process in accordance with the invention, all kinds of ores containing titanium, in particular those which additionally contain iron oxides, can be heat-treated effectively. In particular, the process is suited for the magnetizing calcination of ilmenite. The mean particle size (d_50) of the solids supplied to the reactor preferably is between 75 and 350 pm, in particular between about 100 and 150 urn. The maximum grain size of the solids supplied to the reactor is about 2 mm, preferably less than 250 pm. The grain size of the ilmenite magnetizingly calcined in the reactor preferably lies in the same ranges indicated above.
The generation of the amount of heat necessary for the operation of the reactor can be effected in any way known to the expert for this purpose. In accordance with a preferred embodiment of the invention it is provided to cover the required amount of heat by supplying hot gases or preheated solids. It is preferred to introduce a gaseous reducing agent, e.g. molecular hydrogen, gas mixtures containing molecular hydrogen, carbon monoxide or gas mixtures containing carbon monoxide, e.g. reformer gas, into the reactor. It is also possible to produce the above mentioned reducing gas in the reactor, e.g. by the unterstoichiometrical burning of fuels such as natural gas, oil or coal.
In the process in accordance with the invention, a particularly high product quality can be achieved when the retention time of the solids in the reactor is between 10 and 50 minutes, in particular about 30 minutes. The Particle-Froude-Number in the reactor can lie in a range from about 0.3 to 30, in particular between 0.5 and 15.
The energy consumption of the process can be reduced in that in the separator at least part of the waste gas of the reactor is separated from solids and supplied to a preheating stage upstream of the reactor. The preheating stage
5 can, for instance, comprise a heat exchanger such as a Venturi preheater, and a separator such as a cyclone or the like. In this way, the solids supplied to the reactor are dried and preheated, whereby the heat treatment in the reactor is facilitated. A multi-stage preheating of solids is also possible, the waste gas of the reactor being cooled step by step.
In accordance with a development of this invention it is provided that the waste gases of the reactor together with the e.g. steam-loaded waste gases of the injection cooler are cleaned in a waste gas cleaning stage downstream of the preheating stage. The gases then can possibly be recirculated to the process.
In accordance with a preferred embodiment of the invention it is provided that the recirculation of solids from the separator into the reactor is effected in a self-regulating manner. In this way, an intensive internal and external re-mixing of the solids treated in the reactor can be effected, so that a uniform temperature and reaction profile is achieved in the reactor.
A plant in accordance with the invention, which is in particular suited for performing the process described above, includes a reactor with circulating fluidized bed, downstream of which a separator is provided. Downstream of the reactor and/or the separator there is furthermore provided a cooling apparatus formed as an injection cooler and downstream of the same a separate fluidized-bed cooler. In the injection cooler, the product can be cooled quickly, i.e.
within few seconds, to temperatures between e.g. 100 and 200 C by injecting for instance water. This rapid first cooling is decisive for the product quality, as for instance during the magnetizing calcination of ilmenite changes in the product are possible during a too long cooling time. The final cooling of the product then
In accordance with a development of this invention it is provided that the waste gases of the reactor together with the e.g. steam-loaded waste gases of the injection cooler are cleaned in a waste gas cleaning stage downstream of the preheating stage. The gases then can possibly be recirculated to the process.
In accordance with a preferred embodiment of the invention it is provided that the recirculation of solids from the separator into the reactor is effected in a self-regulating manner. In this way, an intensive internal and external re-mixing of the solids treated in the reactor can be effected, so that a uniform temperature and reaction profile is achieved in the reactor.
A plant in accordance with the invention, which is in particular suited for performing the process described above, includes a reactor with circulating fluidized bed, downstream of which a separator is provided. Downstream of the reactor and/or the separator there is furthermore provided a cooling apparatus formed as an injection cooler and downstream of the same a separate fluidized-bed cooler. In the injection cooler, the product can be cooled quickly, i.e.
within few seconds, to temperatures between e.g. 100 and 200 C by injecting for instance water. This rapid first cooling is decisive for the product quality, as for instance during the magnetizing calcination of ilmenite changes in the product are possible during a too long cooling time. The final cooling of the product then
6 is effected in the separate fluidized-bed cooler, which is provided downstream of the injection cooler.
Preferably, cooling coils are provided in the fluidized-bed cooler, through which a coolant is passed countercurrently. These cooling coils can for instance be combined to form cooling bundles.
In the fluidized-bed cooler, the product heat no longer usable in the process can be dissipated particularly effectively, when the same has two or more chambers io through whose bottom fluidizing gas is introduced by means of a blower.
The fluidizing gas on the one hand is used for cooling the product and at the same time effects an intensive intermixing of the solids to be cooled.
For adjusting the temperatures necessary for the heat treatment of the solids, the reactor preferably has a separate upstream burning chamber, in which the hot gas is produced. It, however, is equally possible to provide a lance assembly and/or bottom tuyeres opening into the same, e.g. disposed laterally, which are connected with a supply conduit for especially gaseous reducing agents, so that the fuel is burnt inside the reactor.
In accordance with a preferred embodiment of the invention, a self-regulating U-shaped seal is provided between the reactor and the separator, by means of which the supply of solids from the separator into the reactor is controlled.
An expensive control system, for instance by using an L-valve known from the prior art, thus can be omitted.
To decrease the energy consumption of the plant, a preheating stage can be provided upstream of the reactor, in which the solids are dried and preheated.
The preheating stage includes e.g. a drier, which is connected with the waste gas conduit of the separator downstream of the reactor, so that the heat present in the waste gas stream can be utilized for predrying/ preheating the solids.
Preferably, cooling coils are provided in the fluidized-bed cooler, through which a coolant is passed countercurrently. These cooling coils can for instance be combined to form cooling bundles.
In the fluidized-bed cooler, the product heat no longer usable in the process can be dissipated particularly effectively, when the same has two or more chambers io through whose bottom fluidizing gas is introduced by means of a blower.
The fluidizing gas on the one hand is used for cooling the product and at the same time effects an intensive intermixing of the solids to be cooled.
For adjusting the temperatures necessary for the heat treatment of the solids, the reactor preferably has a separate upstream burning chamber, in which the hot gas is produced. It, however, is equally possible to provide a lance assembly and/or bottom tuyeres opening into the same, e.g. disposed laterally, which are connected with a supply conduit for especially gaseous reducing agents, so that the fuel is burnt inside the reactor.
In accordance with a preferred embodiment of the invention, a self-regulating U-shaped seal is provided between the reactor and the separator, by means of which the supply of solids from the separator into the reactor is controlled.
An expensive control system, for instance by using an L-valve known from the prior art, thus can be omitted.
To decrease the energy consumption of the plant, a preheating stage can be provided upstream of the reactor, in which the solids are dried and preheated.
The preheating stage includes e.g. a drier, which is connected with the waste gas conduit of the separator downstream of the reactor, so that the heat present in the waste gas stream can be utilized for predrying/ preheating the solids.
7 Further developments, advantages and possible applications of the invention can also be taken from the following description of an embodiment and the drawing. All features described and/or illustrated form the subject-matter of the invention per se or in any combination, independent of their inclusion in the claims or their back-reference.
The only Figure shows a process diagram of a process and a plant in accordance with an embodiment of the present invention.
In the process as shown in the Figure, which is suited in particular for the io magnetizing calcination of solids containing titanium, such as ilmenite, moist solids are introduced into a preheating stage via a screw conveyor 1. This preheating stage comprises a Venturi drier 2, in which the raw material is suspended, dried and preheated, and a separator 3, e.g. a cyclone, downstream of the Venturi drier 2. The solids separated from waste gases in the separator 3 are charged into a reactor 4.
The reactor 4 constitutes a fluidized-bed reactor with a circulating fluidized bed.
For fluidizing the solids, bottom tuyeres are provided in the reactor 4, through which gas, e.g. air or mixtures with air, is introduced by means of a blower 5.
Via lateral lances 6, natural gas is supplied to the reactor 4, which is burnt inside the reactor together with the fluidizing gas. Alternatively or in addition, fuel can be introduced into the reactor 4 via a conduit 7 by means of bottom tuyeres. In this combustion the gas composition, e.g. the content of CO and CO2, is adjusted such that the ilmenite is magnetically calcined or roasted.
The reducing potential of the gas depends on the relation CO:CO2.
In the fluidized-bed reactor 4, the solids are carried upwards by the fluidizing gas. Part of the solids separate out in the reactor and are thereby recirculated to the circulating fluidized bed, in order to be carried upwards again by the fluidizing gas. Together with a waste gas stream from the reactor 4, the other part of the solids is discharged upwards through a conduit 8 and in a
The only Figure shows a process diagram of a process and a plant in accordance with an embodiment of the present invention.
In the process as shown in the Figure, which is suited in particular for the io magnetizing calcination of solids containing titanium, such as ilmenite, moist solids are introduced into a preheating stage via a screw conveyor 1. This preheating stage comprises a Venturi drier 2, in which the raw material is suspended, dried and preheated, and a separator 3, e.g. a cyclone, downstream of the Venturi drier 2. The solids separated from waste gases in the separator 3 are charged into a reactor 4.
The reactor 4 constitutes a fluidized-bed reactor with a circulating fluidized bed.
For fluidizing the solids, bottom tuyeres are provided in the reactor 4, through which gas, e.g. air or mixtures with air, is introduced by means of a blower 5.
Via lateral lances 6, natural gas is supplied to the reactor 4, which is burnt inside the reactor together with the fluidizing gas. Alternatively or in addition, fuel can be introduced into the reactor 4 via a conduit 7 by means of bottom tuyeres. In this combustion the gas composition, e.g. the content of CO and CO2, is adjusted such that the ilmenite is magnetically calcined or roasted.
The reducing potential of the gas depends on the relation CO:CO2.
In the fluidized-bed reactor 4, the solids are carried upwards by the fluidizing gas. Part of the solids separate out in the reactor and are thereby recirculated to the circulating fluidized bed, in order to be carried upwards again by the fluidizing gas. Together with a waste gas stream from the reactor 4, the other part of the solids is discharged upwards through a conduit 8 and in a
8 downstream separator 9, for instance a cyclone, separated from the gas stream for the most part. Through a conduit 10, the solids from the separator 9 are recirculated to the fluidized-bed reactor 4. By means of this intensive internal and external remixing a particularly uniform temperature and reaction profile is achieved inside the fluidized-bed reactor 4.
The control of the amount of solids recirculated from the separator 9 into the fluidizedbed reactor 4 is effected via a self-regulating U-shaped seal 11 which is provided in the conduit 10. As a result, a control and regulating unit for metering the amount of solids recirculated into the fluidized-bed reactor 4 can be omitted.
The gas stream separated from the solids in the separator 9 is supplied to the Venturi drier 2, so that the heat content of the gas stream leaving the separator
The control of the amount of solids recirculated from the separator 9 into the fluidizedbed reactor 4 is effected via a self-regulating U-shaped seal 11 which is provided in the conduit 10. As a result, a control and regulating unit for metering the amount of solids recirculated into the fluidized-bed reactor 4 can be omitted.
The gas stream separated from the solids in the separator 9 is supplied to the Venturi drier 2, so that the heat content of the gas stream leaving the separator
9 is utilized for drying and preheating the solids.
From the fluidized-bed reactor 4 and/or the separator 9 hot solids are withdrawn and supplied to an injection cooler 13 via conduits 12a and 12b, respectively.
In the injection cooler 13, the hot solids are fluidized in a stationary fluidized bed.
For this purpose, air is introduced into the injection cooler 13 as fluidizing air via a blower 14. The gas velocity of the fluidizing gas is chosen such that the fluidization in the injection cooler 13 is low, so that the stationary fluidized bed expands only little. At the same time, water is injected into the injection cooler 13 as coolant via conduit 15. The water is evaporated in the injection cooler 13, so that the stationary fluidized bed in the upper region of the injection cooler 13 expands more than in the bottom region of the injection cooler. By injecting water, the hot product is quickly cooled to temperatures of e.g. below 200 C.
Downstream of the injection cooler 13 a separate fluidized-bed cooler 16 is provided, in which the product heat no longer usable in the process is dissipated. In the illustrated embodiment, the fluidized-bed cooler has two chambers 16a and 16b, into which e.g. water is countercurrently introduced as coolant through schematically illustrated cooling coils 17, whereby the product is further cooled to the temperature necessary for the further processing, such as the magnetic separation. Via a blower 18, air is introduced into the two chambers i6a and 16b of the fluidized-bed cooler 16, in order to fluidize and cool the product. The cooled product then is supplied to the further processing via a conduit 19.
Via conduits, the separator 3 of the preheating stage, the injection cooler 13 as well as the fluidized-bed cooler 16 are connected with a waste gas cleaning stage 20, which for instance has a bag filter. In this waste gas cleaning stage 20, the gas streams partly containing solids and/or steam are cleaned. Via conduit 21, the solids can be charged from the waste gas cleaning stage 20 into the fluidized-bed cooler 16.
Example (magnetizing calcination of ilmenite) In a plant for the magnetizing calcination of ilmenite as shown in the Figure, t/h of moist ilmenite from a storage tank are charged via the screw conveyor 1 is into the Venturi drier 2. In the Venturi drier 2, the moist ilmenite was suspended, dried and preheated by hot waste gases from the separator 9. In the cyclone 3, which is provided downstream of the Venturi drier 2, the dried and preheated ilmenite was separated from the gas stream and introduced into the reactor 4 with circulating fluidized bed.
The waste gas of the cyclone 3 was supplied to the waste gas cleaning stage 20, partly recirculated and oxidized and supplied to a chimney. The dry ilmenite dust separated in the waste gas cleaning stage 20 was passed through a conduit directly into the product stream 19.
Via the blower 5, 46,000 Nm3/h of gas, consisting of 15,000 Nm3/h air and 31,000 Nm3/h recirculated waste gas, were introduced into the fluidized-bed reactor 4 for fluidization. At the same time, about 1,800 Nm3/h of natural gas were supplied to the reactor 4 via the lateral lances 6 as well as conduit 7 and were burnt in the fluidized bed together with air. The reducing gas obtained leads to a temperature of the ilmenite charged into the fluidized-bed reactor 4 of about 800 C, the Particle-Froude-Number in the reactor being about 1.2. A
magnetizing calcination of the ilmenite was achieved with retention times of the 5 solids between 10 and 50 minutes.
Together with the waste gases of the reactor 4, the solids were transported into the separator 9, separated there and for the most part recirculated to the reactor 4 through conduit 10. An amount of ilmenite product, which corresponds to the amount charged into the reactor 4, was supplied to the injection cooler
From the fluidized-bed reactor 4 and/or the separator 9 hot solids are withdrawn and supplied to an injection cooler 13 via conduits 12a and 12b, respectively.
In the injection cooler 13, the hot solids are fluidized in a stationary fluidized bed.
For this purpose, air is introduced into the injection cooler 13 as fluidizing air via a blower 14. The gas velocity of the fluidizing gas is chosen such that the fluidization in the injection cooler 13 is low, so that the stationary fluidized bed expands only little. At the same time, water is injected into the injection cooler 13 as coolant via conduit 15. The water is evaporated in the injection cooler 13, so that the stationary fluidized bed in the upper region of the injection cooler 13 expands more than in the bottom region of the injection cooler. By injecting water, the hot product is quickly cooled to temperatures of e.g. below 200 C.
Downstream of the injection cooler 13 a separate fluidized-bed cooler 16 is provided, in which the product heat no longer usable in the process is dissipated. In the illustrated embodiment, the fluidized-bed cooler has two chambers 16a and 16b, into which e.g. water is countercurrently introduced as coolant through schematically illustrated cooling coils 17, whereby the product is further cooled to the temperature necessary for the further processing, such as the magnetic separation. Via a blower 18, air is introduced into the two chambers i6a and 16b of the fluidized-bed cooler 16, in order to fluidize and cool the product. The cooled product then is supplied to the further processing via a conduit 19.
Via conduits, the separator 3 of the preheating stage, the injection cooler 13 as well as the fluidized-bed cooler 16 are connected with a waste gas cleaning stage 20, which for instance has a bag filter. In this waste gas cleaning stage 20, the gas streams partly containing solids and/or steam are cleaned. Via conduit 21, the solids can be charged from the waste gas cleaning stage 20 into the fluidized-bed cooler 16.
Example (magnetizing calcination of ilmenite) In a plant for the magnetizing calcination of ilmenite as shown in the Figure, t/h of moist ilmenite from a storage tank are charged via the screw conveyor 1 is into the Venturi drier 2. In the Venturi drier 2, the moist ilmenite was suspended, dried and preheated by hot waste gases from the separator 9. In the cyclone 3, which is provided downstream of the Venturi drier 2, the dried and preheated ilmenite was separated from the gas stream and introduced into the reactor 4 with circulating fluidized bed.
The waste gas of the cyclone 3 was supplied to the waste gas cleaning stage 20, partly recirculated and oxidized and supplied to a chimney. The dry ilmenite dust separated in the waste gas cleaning stage 20 was passed through a conduit directly into the product stream 19.
Via the blower 5, 46,000 Nm3/h of gas, consisting of 15,000 Nm3/h air and 31,000 Nm3/h recirculated waste gas, were introduced into the fluidized-bed reactor 4 for fluidization. At the same time, about 1,800 Nm3/h of natural gas were supplied to the reactor 4 via the lateral lances 6 as well as conduit 7 and were burnt in the fluidized bed together with air. The reducing gas obtained leads to a temperature of the ilmenite charged into the fluidized-bed reactor 4 of about 800 C, the Particle-Froude-Number in the reactor being about 1.2. A
magnetizing calcination of the ilmenite was achieved with retention times of the 5 solids between 10 and 50 minutes.
Together with the waste gases of the reactor 4, the solids were transported into the separator 9, separated there and for the most part recirculated to the reactor 4 through conduit 10. An amount of ilmenite product, which corresponds to the amount charged into the reactor 4, was supplied to the injection cooler
10 through conduits 12a and 12b, respectively. The average particle size (d_50) both of the ilmenite charged into the reactor 4 and of the calcined ilmenite was about 100 to 150 pm with a maximum grain size of about 250 pm.
The injection cooler 13 was operated as stationary fiuidized bed by supplying is about 6300 Nm3/h of recirculated waste gas as fluidizing gas into the injection cooler 13 via the blower 14. At the same time, about 8 m3 h of water were introduced into the injection cooler 13 via conduit 15, so that the hot ilmenite was cooled to about 150 C within few seconds. Due to the evaporating water, the steam was about 60% of the total amount of gas in the fluidized bed of the injection cooler 13. The gas velocity of the fluidizing gas introduced via the blower 14 was chosen such that the Particle-Froude-Number at the bottom of the injection cooler 13 was about 0.17 and at the top of the injection cooler about 0.47.
The final cooling of the product was effected in the two chambers 16a and 16b of the fluidized-bed cooler 16. For fluidization, about 6000 Nrn3/h of recirculated waste gas were introduced into the fluidized-bed cooler 16 via the blower 18.
At the same time, cooling water was countercurrently passed through the chambers 16a and 16b via conduit 17. In the chambers 16a and 16b, the =
conduit 17 had cooling bundles.
The injection cooler 13 was operated as stationary fiuidized bed by supplying is about 6300 Nm3/h of recirculated waste gas as fluidizing gas into the injection cooler 13 via the blower 14. At the same time, about 8 m3 h of water were introduced into the injection cooler 13 via conduit 15, so that the hot ilmenite was cooled to about 150 C within few seconds. Due to the evaporating water, the steam was about 60% of the total amount of gas in the fluidized bed of the injection cooler 13. The gas velocity of the fluidizing gas introduced via the blower 14 was chosen such that the Particle-Froude-Number at the bottom of the injection cooler 13 was about 0.17 and at the top of the injection cooler about 0.47.
The final cooling of the product was effected in the two chambers 16a and 16b of the fluidized-bed cooler 16. For fluidization, about 6000 Nrn3/h of recirculated waste gas were introduced into the fluidized-bed cooler 16 via the blower 18.
At the same time, cooling water was countercurrently passed through the chambers 16a and 16b via conduit 17. In the chambers 16a and 16b, the =
conduit 17 had cooling bundles.
11 In this way, a reducing magnetizing calcination of ilmenite could be effected, and due to the rapid cooling no changes were detected during the cooling period, so that the calcined ilmenite had a high product quality.
12 List of Reference Numerals 1 screw conveyor 2 Venturi drier 3 cyclone 4 fluidized-bed reactor 5 blower 6 lance 7 conduit 8 conduit 9 separator 10 conduit 11 U-shaped seal 12a, 12b conduit
13 injection cooler
14 blower
15 conduit
16 fluidized-bed cooler 16a, 16b chamber
17 conduit
18 blower
19 conduit
20 waste gas cleaning stage
21 conduit
Claims (29)
1. A process for the heat treatment of solids containing titanium, in which fine-grained solids are heated to a temperature of 700 to 1000°C in a reactor with a circulating fluidized bed and are partly discharged from the reactor together with waste gases into a downstream separator, in which the solids are separated from the waste gases and are recirculated to the reactor at least partly and/or phase by phase, and wherein fuel is supplied to the reactor and combusted with an oxygen-containing gas to generate a reducing gas in the reactor such that the heat treatment of the solids is performed under reducing conditions.
2. The process as claimed in claim 1, wherein downstream of the reactor and/or the separator a cooling apparatus comprising an injection cooler is provided, in which the solids are cooled to below 250°C by injecting a coolant, and that fluidizing gas is introduced into the injection cooler with such a gas velocity that the Particle-Froude-Number in the fluidized bed is between 0.01 and 10.
3. The process as claimed in claim 2 wherein the cooling apparatus is a fluidized-bed injection cooler.
4. The process as claimed in claim 2 or 3, wherein the Particle-Froude-Number in the fluidized bed is between 0.1 and 1.
5. The process as claimed in any one of claims 2 to 4, wherein the Particle-Froude-Number at the bottom of the injection cooler is between 0.1 and 0.25.
6. The process as claimed in claim 5, wherein the Particle-Froude-Number at the bottom of the injection cooler is approximately 0.17.
7. The process as claimed in any one of claims 2 to 6, wherein the Particle-Froude-Number at the top of the injection cooler is between 0.35 and 0.55.
8. The process as claimed in claim 7, wherein the Particle-Froude-Number at the bottom of the injection cooler is approximately 0.47.
9. The process as claimed in any one of claims 2 to 8, wherein the gas content of the fluidized bed in the injection cooler includes 50 to 70% steam.
10. The process as claimed in any one of claims 2 to 9, wherein the gas content of the fluidized bed in the injection cooler includes approximately 60% steam.
11. The process as claimed in any one of claims 2 to 10, wherein downstream of the injection cooler a fluidized-bed cooler is provided.
12. The process as claimed in any one of claims 1 to 11, wherein ilmenite is used as starting material.
13. The process as claimed in any one of claims 1 to 12, wherein the solids supplied to the reactor have a mean grain size (d_50) between 75 and 250 pm.
14. The process as claimed in claim 13 wherein the mean grain size (d_50) is between 100 and 150 pm.
15. The process as claimed in claim 12, wherein the solids supplied to the reactor have a maximum grain size of 2 mm.
16. The process as claimed in claim 12, wherein the solids supplied to the reactor have a maximum grain size of in particular of less than 350 µm.
17. The process as claimed in any one of claims 1 to 16, wherein the fuel supplied to the reactor is gaseous and is introduced through lances and/or through bottom tuyeres, and at least partially air is introduced as fluidizing gas.
18. The process as claimed in any one of claims 1 to 17, wherein the average retention time of the solids in the reactor is between 10 and 50 min.
19. The process as claimed in claim 18, wherein the average retention time of the solids in the reactor approximately 30 min.
20. The process as claimed in any one of claims 1 to 19, wherein at least part of the waste gas of the reactor is separated from solids in the separator and supplied to a preheating stage with a drier and a separator upstream of the reactor for drying and preheating the solids to be supplied to the reactor.
21. The process as claimed in claim 20, wherein the waste gases of the reactor together with steam-loaded waste gases of the injection cooler are cleaned in a waste gas cleaning stage downstream of the preheating stage.
22. The process as claimed in any one of claims 1 to 21, wherein the recirculation of solids from the separator into the reactor is effected in a self-regulating manner.
23. A plant for performing a process for the heat treatment of solids containing titanium as claimed in any one of claims 1 to 22, comprising a reactor with circulating fluidized bed, downstream of which a separator is provided, and upstream of the reactor and/or the separator a solids preheating device is provided and downstream of the reactor and/or the separator an injection cooler is provided and wherein the reactor has a lance assembly opening into the same and/or bottom tuyeres, which are connected with at least one supply conduit that supplies gaseous fuel and an oxygen-containing gas to the reactor.
24. The plant as claimed in claim 23 wherein the gaseous fuel and oxygen-containing gas are supplied as a mixture.
25. The plant as claimed in claim 24, wherein downstream of the reactor a fluidized-bed cooler is provided.
26. The plant as claimed in claim 25, wherein the fluidized-bed cooler has cooling coils through which a coolant is passed countercurrently.
27. The plant as claimed in claim 25 or26, wherein the fluidized-bed cooler has two or more chambers through whose bottom fluidizing gas is introduced by means of a blower.
28. The plant as claimed in any one of claims 23 to 27, wherein between the reactor and the separator a self-regulating U-shaped seal is provided for controlling the supply of solids from the separator into the reactor.
29. The plant as claimed in any one of claims 23 to 28, wherein upstream of the reactor a preheating stage for the solids is provided, whose drier is connected with a waste gas conduit of the separator downstream of the reactor.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DE102005012524A DE102005012524A1 (en) | 2005-03-16 | 2005-03-16 | Process and plant for the heat treatment of titanium-containing solids |
| DE102005012524.7 | 2005-03-16 | ||
| PCT/FI2006/000086 WO2006097569A1 (en) | 2005-03-16 | 2006-03-14 | Process and plant for the heat treatment of solids containing titanium |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CA2599564A1 CA2599564A1 (en) | 2006-09-21 |
| CA2599564C true CA2599564C (en) | 2016-05-24 |
Family
ID=36926902
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA2599564A Expired - Fee Related CA2599564C (en) | 2005-03-16 | 2006-03-14 | Process and plant for the heat treatment of solids containing titanium |
Country Status (8)
| Country | Link |
|---|---|
| CN (1) | CN101142329A (en) |
| AU (1) | AU2006224490B2 (en) |
| CA (1) | CA2599564C (en) |
| DE (1) | DE102005012524A1 (en) |
| NO (1) | NO20075289L (en) |
| UA (1) | UA91354C2 (en) |
| WO (1) | WO2006097569A1 (en) |
| ZA (1) | ZA200503457B (en) |
Families Citing this family (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103031433B (en) * | 2011-09-30 | 2014-07-30 | 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 |
| CN103031432B (en) * | 2011-09-30 | 2014-09-24 | 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 |
| 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 |
| EP3153776A1 (en) | 2015-10-08 | 2017-04-12 | Improbed AB | Bed management cycle for a fluidized bed boiler and corresponding arrangement |
| EP3153775A1 (en) | 2015-10-08 | 2017-04-12 | Improbed AB | Method for operating a fluidized bed boiler |
| CN105567933A (en) * | 2015-12-16 | 2016-05-11 | 宁波高新区世代能源科技有限公司 | Efficient energy-saving and environment-friendly stainless steel heat treating machine |
| DE102016103349A1 (en) * | 2016-02-25 | 2017-08-31 | Outotec (Finland) Oy | Method and device for thermal treatment of a contaminated solid |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
-
2005
- 2005-03-16 DE DE102005012524A patent/DE102005012524A1/en not_active Withdrawn
- 2005-04-29 ZA ZA200503457A patent/ZA200503457B/en unknown
-
2006
- 2006-03-14 CA CA2599564A patent/CA2599564C/en not_active Expired - Fee Related
- 2006-03-14 CN CNA2006800082984A patent/CN101142329A/en active Pending
- 2006-03-14 WO PCT/FI2006/000086 patent/WO2006097569A1/en not_active Application Discontinuation
- 2006-03-14 AU AU2006224490A patent/AU2006224490B2/en not_active Ceased
- 2006-03-14 UA UAA200709472A patent/UA91354C2/en unknown
-
2007
- 2007-10-16 NO NO20075289A patent/NO20075289L/en not_active Application Discontinuation
Also Published As
| Publication number | Publication date |
|---|---|
| AU2006224490B2 (en) | 2010-07-22 |
| DE102005012524A1 (en) | 2006-09-21 |
| WO2006097569A1 (en) | 2006-09-21 |
| UA91354C2 (en) | 2010-07-26 |
| AU2006224490A1 (en) | 2006-09-21 |
| CN101142329A (en) | 2008-03-12 |
| NO20075289L (en) | 2007-12-10 |
| CA2599564A1 (en) | 2006-09-21 |
| ZA200503457B (en) | 2006-02-22 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CA2510926C (en) | Fluidized bed method and plant for the heat treatment of solids containing titanium | |
| CA2599564C (en) | Process and plant for the heat treatment of solids containing titanium | |
| US4076796A (en) | Carrying out endothermic processes in fast fluidized reactor with conventionally fluidized holding reactor | |
| AU2003294752B2 (en) | Method and plant for the heat treatment of solids containing iron oxide using a fluidized bed reactor | |
| AU2006201957B2 (en) | Process and plant for producing char and fuel gas | |
| US9175226B2 (en) | Process and plant for producing char and fuel gas | |
| EA009505B1 (en) | A direct reduction process and apparatus | |
| CA2566320C (en) | A direct reduction apparatus and process | |
| EA010277B1 (en) | Method and plant for producing low-temperature coke | |
| CN109982775B (en) | Method and apparatus for heat treatment in a fluidized bed reactor | |
| CA2536990C (en) | Process and plant for the heat treatment of solids containing titanium | |
| EP1756324A1 (en) | Direct reduction process using a single fluidised bed |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| EEER | Examination request | ||
| MKLA | Lapsed |
Effective date: 20200831 |