DE2030079A1 - Process for processing titanium oxide ores - Google Patents

Description

DR. SERG DIPL-ING. STAPF

8 MUNICH β. HILBLESTRASSB 2O

Dr. Uta Dipl.-Infl. Stapf. I MOnttwn %

Your sign Your letter Under sign Dotum

| Q, JUDl 19 ΛΙ

Attorney file 19 762
Be / Sch

Laportβ Industries Limited Xondon W 1 / England

"Process for the preparation of titanium oxide ores ¹¹

This invention relates to the processing of titanium oxide ores, which also contain iron oxides, to form them of an ore with a higher titanium content.

Titanium oxide is usually present in nature found of iron oxides. A commonly used ore

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009852/1960

is ilmenite, which is given the general formula FeTiO 'fann. It has been proposed to extract the titanium contained in the ores by reacting them with chlorine in the presence of carbon. The product is a mixture of chlorides, which contains titanium and other metal chlorides. The chloride mixture thus formed can be fractionated are distilled, whereby one obtains relatively pure titanium chloride. Chlorination has also been suggested carry out in a selective manner, the mixture of chlorides thus formed or a suitable fraction of the Mixtures of the chlorides contain a larger proportion of titanium in the form of the chloride compared to the ore or with the residual Ore or a suitable fraction thereof is enriched in titanium oxide over the starting ore.

It has been proposed (see US Pat. No. 3,484,198) to prepare an ore containing titanium and iron oxides by treating the ore with elemental carbon and bromine in the presence of an inert carrier gas at a; Brings elevated temperature below 100O ⁰ C in contact. Such a process results in the formation of iron tribromide and carbon oxides, but not significant amounts of titanium bromides. The titanium content of the ore remains as a residue, which consists primarily of titanium oxide.

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bath

It has now been found, surprisingly, that if instead of an inert carrier gas uses a carrier gas that does not contain more than 50 vol. # oxygen, the conditioning reaction runs faster and delivers a product that contains a larger proportion of titanium oxide. It Accordingly, the present invention provides a process for the preparation of titanium oxide and iron oxide-containing Ores, for which the ore is mixed with elemental carbon and bromine in the presence of a carrier gas that is between 1 and Contains 50 vol. # Oxygen and brings it into contact at a temperature between 500 and 1100 ° C.

The iron bromides are usually found in the stream of reaction products and the carrier gas leaving the bed. This stream is hereinafter referred to as the "product gas" stream designated. When iron tribromide is formed it usually breaks down in the product gas stream to form an equilibrium mixture, the iron dibromide, bromine and Contains iron tribromide. The iron bromides can be separated from the product gas stream by means of condensation Product gas stream is after the Eisenbroiuide removed therefrom If iron tribromide was formed, bromine was contained, which can be removed therefrom by conventional means, for example by aqueous alkali scrubbers.

Eb can be useful to describe the process according to the invention in 009852/1960

the way to carry out that a mixture of bromine and the Carrier gas, hereinafter referred to as "feed gas", through a bed of intimately mixed ore and elemental Carbon is passed. Preferably the feed gas is passed through the bed in such a way that a fluidized bed is formed. In order to carry out the fluidization of the bed, as is known to the person skilled in the art, the Particles of bed are sufficiently small in size * In copending patent application attorney's file 19 761 of the applicant is a process for processing of an ore in a fluidized bed and every object described there, with the exception of those objects which are necessarily restricted by working with an inert carrier gas, for the method of the present invention Invention can be used.

The iron bread can lead to the formation of iron oxides and bromine be oxidized. The bromine can be fed back into the cycle to form further iron bromides. It can be expedient be able to oxidize all of the Msenbromide with the release of bromine with just enough air. There may also be a permanent excess. Advantageously the gas thus formed contains bromide and oxygen in such an amount that if you use it, if desired, with your product gas, from which the iron bromide is removed diluted it as a feed gas mixture of

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Carrier gas and bromine for the production of other iron bromides can be used.

The iron bromides can be oxidized, for example in a fluidized bed using powdered or granular iron bromides, or in a floating or rapid roaster or in a test bed reaction vessel which contains pellets or granules of the iron bromides. The temperature used for the oxidation will depend on the equipment used. Generally, a temperature is preferably at least 45O ⁰ C.

The amount of carbon should desirably be at least sufficient to bind the oxygen of the iron oxides and the carrier gas. If the titanium oxide in the ore is to be chlorinated to form titanium trachloride, it may be advisable to add sufficient carbon before the ore is brominated, the intended chlorination of the processed ore without further addition of To enable carbon. In this case it may be desirable to chlorinate the processed ore, before it has cooled down. In a batch procedure, this can be done using the same device with appropriate Shut-off valves and a cleaning device to reduce the loss of bromine. With a continuous Process can according to the present invention,

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as will be described below, the digested ore are continuously removed, the bromine separated from this and the open-minded lirz into one suitable chlorination vessel. The gas used for cleaning is advantageously the product gas after the iron bromides have been removed from it.

The cleaning gases are expediently circulated as at least part of the carrier gas. At temperatures below about 73O ⁰ C the rate of reaction of the iron oxide is so slow that the complete removal of the iron oxide is difficult, if not impossible. Nevertheless, some processing will take place at a low temperature. For these considerations, it is preferred to carry out the ^{process according to the invention between 800 and 105O 0 O.}

In principle, the method according to the invention can be used with anyone Ratio of bromine to carrier gas can be carried out. If the bromine ratio is too high, e.g. greater than 15 VoI # it'll attack the titanium oxide a little · If vice versa the bromine ratio is too low, for example below 5 vol. # the reaction rate with the iron oxide may become too slow and the reaction may be slow in view of that Irons remain incomplete in a given time. In view of these considerations, it is preferred that the

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carry out inventive method in such a way that a bromine ratio in the carrier gas between 8 and 12 VoI «# used.

In view of the high cost of bromine, it is essential in an economic Verfahi ^v s to limit the loss of bromine to a minimum.

It is therefore preferred, if possible, to use the method of present invention so that the loss of bromine is minimized in the product gas after the iron bromides have been removed from it. To this To achieve, the inventive method is preferably carried out in such a way that the entire in the Bed introduced bromine reacts with the iron oxide only to form egg dibromide or, less preferably, with the titanium oxide to form titanium bromides. The bromine desirably should not react with or without the iron oxide to form unstable iron tribromide React "the bed, entrained in the product gas, pass through. It is difficult to use the process of the invention carry out in such a way that the iron oxide completely removed in a discontinuous reaction because at the end of the reaction the concentration of iron oxide in the bed is low. This is particularly true if the reaction occurs in a granular ore and coal

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substance-containing bed is carried out because in that ■ -deHE bed canalization occur in all reaction stages can.

It is often desirable to carry out the process according to the invention continuously. Because of the difficulties caused by channeling through the bed, it may be useful to do the procedure in one Perform series of beds, including the product gas from one bed to the next as feed gas. If desired, additional bromine or additional Oxygen or both can be supplied at each stage. For example, if four beds are available, will the first bed product gas as the second bed feed gas; the second bed product gas as the feed gas of the third bed and the product gas of the third bed as the feed gas of the fourth bed used. If the ore in the first bed is sufficient is digested, the feed gas is fed directly to the second bed and the digested ore the first bed can be removed, the bed can be reloaded with ore and coal, and the product gas from the fourth Bed can be used as the feed gas for the first bed. The ore in the second bed can then be removed, additional ore and carbon can be charged and the product gas from the first bed used as feed gas

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will.

Preferably, fluidized beds are used in series in a continuous process. It therefore provides the present invention in further respects a process which is suitable for the preparation of titanium and iron oxides in a continuous process, for which a gaseous mixture of bromine and a carrier gas containing between 1 and 50 $ oxygen through a first Bed containing ore and elemental carbon passes the mixture of carrier gas, unreacted bromine, iron dibromide and carbon oxides from the first bed through a second bed also containing ore and elemental carbon, feeds ore and elemental carbon to the second bed while removing part of the partially processed second bed into the first bed and removing part of the processed ore from the first bed, both beds being fluidized by gases passed through them and kept at a temperature below 110O ⁰ O .

This continuous process is not based on working limited to two beds and in principle any number of beds can be used. For an economical process, more than five beds can be considered turn out to be uneconomical and there are trips three or four

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Suitable for beds.

Ilmenite ores generally contain manganese, vanadium and chromium oxides or derivatives thereof in minor proportions. It was found that the method according to the invention, at least in certain embodiments, converts them to manganese, vanadium and chromium bromides. Such a one Conversion is not as fast as that of the iron oxide, but faster than that of the titanium oxide in the ore. Accordingly, the terms "iron oxide" and "iron bromide" are included in this specification, unless that unless otherwise stated, not the presence of other metal oxides or bromides as they occur in natural ores, the end.

To make the present invention easier to understand, an embodiment of the invention will now be described with reference to the accompanying drawings, which shows a schematic representation of an apparatus for the continuous implementation of the invention.

A vessel in which the reaction is carried out contains a vertical cylinder 1, the conical end caps 2 and 3 has. The cylinder 1 is divided into three vertically separated reaction zones 4, 5 and 6 by two on either side tapered separating devices 7 and 8 divided, where the axes of the cones coincide with the axis of the cylinder

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which 1 matches. Me reaction zones are round Holes 9 and 10 within separators 7 and 8 at the apex of each double cone and through overflow lines 11 and 12, which run through the separators 7 and 8. The reaction zone 4 has a gas inlet tube 13 at the top of the end cap 2 and one with valve provided outlet pipe 14-, which through the end cap 2 runs. The reaction zone 6 has a valved solids inlet tube 15 through the end cap 3 runs, and an outlet pipe for product gas 16 on. The separators 7 and 8 each have a round closure part 17 or 18, which is arranged so that it sits in the cone drawn downwards in each separating device, whereby the round holes 9 and 10 are closed. The entire device described so far is made of quartz glass and contained in a furnace 19.

The lower ends of the solids inlet pipe 5 and the Overflow lines 11 and 12 usually extend to the bottom of the Reaction zones 6 and 4 and 5, respectively. The upper ends of the outlet conduit 14 and the overflow lines 11 and 12 are sufficient essentially over the lower ends of the overflow lines 11 and 12 and the inlet pipe I5, mostly in the upper Part of the reaction zones 4 or 5 and 6, which increases the height of the bed in each reaction zone is determined. The upper part of the overflow line 12 is sufficiently below the

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Height of the outlet pipe 16 to avoid solid material is carried out via the outlet line 16 from the reaction zone 6.

The outlet pipe for product gas 16 is "at one end an air-cooled quartz gas cooler 20 with the other connected to a cyclone 21. Aggregate-forming rollers 22 are for the solids on the cyclone 21 and a storage hopper 23 provided for the solid aggregates. A pump 24 is connected to the gas outlet of the cyclone 21 and this in turn is through line 25 with a scrubber (not shown) and / or a preheater 26 connected.

A second cylindrical reaction vessel 27 has a Valved solids inlet tube 28 and a gas outlet tube 31 at its upper end on .. The lower end the reaction vessel 27 is provided with a turntable 29, whereby a gap 35 is formed between the turntable and the bottom of the reaction vessel 27. The lower The end of the reaction vessel 27 also has a valve provided funnel 34, which is the lower end of the reaction vessel and the turntable 29 contains oxygen-containing Gas can enter the funnel 34 and from it through the gap 35 into the reaction vessel 27 by means of a pump 32 be pumped through a gas inlet pipe 30. The solid

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funnel 23 is provided with a valved inlet pipe 28 connected, causing the pesticides to enter the reaction vessel 27 are fed. .

The preheater 26 and the gas outlet pipe 31 are with the cylindrical reaction vessel 1 via the gas inlet pipe 13 tied together. The fresh gas inlet pipe 33 is also connected to the cylindrical reaction vessel 1 via the gas inlet pipe 13 connected.

The operation of the device described above will now be described with reference to the drawing. At the beginning of the operating process, the reaction zones 4, 5 and 6 contain beds containing particulate mixtures of ore and carbon at a level below the upper ends of the outlet line 14 and the overflow lines 11 and 11, respectively. The beds in the reaction zones 4, 5 and 6 are swirled by passing a gas through the lines 33 and 13 into the reaction zone 4. The velocity of the gas through the reaction zone must be at least sufficient to create a fluidized bed, but not so great that it blows the solids out of the bed. The gases from the reaction zone 4 pass through the round hole 9 to the reaction zone 5 and then through the round hole 10 to the reaction zone 6. The passage of the gas lifts the ball locks 17 and 18 out of their seats

009852/1960

in the downwardly drawn cone of the separation devices 7 and 8. The required for fluidization of the bed in the reaction zone 5 and 6 the gas velocity ± w is substantially sufficient to prevent the particles of the bed or in the reaction zones 4 · 5 by the round holes 9 and 10 fall. The gas passes from reaction zone 6 through product gas outlet line 16, cooler 20 and cyclone 21. From cyclone 21 the gas passes through pump 24 and line 23 to a sodium hydroxide scrubber (not shown).

After the beds are swirled or after they are swirled the reaction vessel 1 is heated. When the reaction vessel 1 is at a suitable temperature, a Bromine-containing gas through lines 33 and 13 instead of the gas initially used, taking care that there is no significant loss of speed or pressure while changing the gases, in this way to eliminate the possibility that the turbulence of a bed will cease, the bromine reacts with the ore and the carbon in the reaction zone 4 forming iron dibromide and carbon oxides. The product gas from reaction zone 4, which usually contain bromine occurs, as described above, in the reaction zone 5. The bromine reacts with the ore and the coal in of reaction zone 5, where there is iron dibromide and carbon

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forms oxides. The product gas from reaction zone 5, the Reaction products in reaction zone 4 and in general also contains bromine, runs into the reaction zone 6. The bromine reacts with the ore and the carbon in the reaction ion 6 to form iron dibromide and carbon oxides. The product gas from reaction zone 6, but the reaction product from reaction zones 4 and 5t normally no substantial amounts of bromine is contained, leaves the reactor through the product gas outlet 16 ^

A fresh mixture of ore and carbon is put into the Reaction zone 6 introduced through ore inlet tube 15 When the amount of ore and carbon in the bed of the reaction zone 6 is such that the upper part of the fluidized bed above the level of the upper part of the overflow pipe 12 is, partially processed ore and coal falls from the bed of the reaction zone 6 through the overflow line 12 in the reaction zone 5 ·· When the ore and carbon amount in the bed of the reaction zone 5 is so large that the upper Part of the fluidized bed above the level of the upper overflow line 11, partially processed ore and coal falls from the bed of reaction zone 5 down through the Overflow line 11 into the reaction zone 4. When the quantity « Ore and carbon in the bed of reaction zone 4 is such that the upper part of the fluidized bed is above the level the outlet line 14 is, ore falls that is not yet completely

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recycled and carbon down through the outlet line 14 for further processing. The mixture of ore and carbon can then be introduced through inlet line 15 either batchwise or continuously; the overflow through lines 12, 11 and 14 takes place accordingly batchwise or continuously.

The product gas from outlet line 16 is cooled in cooler 20 where the iron dibromide condenses to a finely divided solid. The solid iron dibromide is separated from the gaseous reaction product in the cyclone 21 and runs through the aggregate-forming rollers 22 into the hopper 23. The gaseous reaction products are fed by the pump 24, either through the line 25 to the sodium hydroxide scrubber (not shown), or through the The preheater 26 is fed into the circuit through the inlet line 13 with the bromine-containing gas in the reaction vessel 1 .

The solid iron dibromide is from the funnel 23 through the Inlet line 28 is fed to the reaction vessel 27, where it reacts with the oxygen-containing gas. The sourest off-stop gas is passed into the reaction vessel 27 the inlet line 3Q into the funnel 34 and then through the Gap 35 passed. The oxygen-containing gas flows downward through the reaction vessel in countercurrent to the direction

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processing of iron dibromide. The iron dibromide turns into iron oxides oxidized. The rotation of the turntable 29 enables the iron oxides to circulate through the gap '35' appropriate speed to fall.

The turntable 29 rotates at such a speed and the amount of iron dibromide supplied to the reaction vessel 27 is so large that the bed in the reaction vessel 27 has a suitable and approximately constant height. That Bromine-containing gas that is formed is returned to the reactor 1 through the inlet pipe 13.

The following examples illustrate the invention. Example 1 is a comparative example that compares to Example 2 shows that the use of oxygen is a delivers improved results.

example 1

The procedure of this example is done in a vertical way cylindrical reaction vessel with a 15 cm diameter and 180 cm long, with tapered ends at each end. A 4 cm shower knife gas inlet tube was tapered in the lower Closure and a solids inlet pipe and a gas product output line in the upper conical termination provided «The outlet line for gaseous pro-

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dukte has a diameter of 6 cm, with a Long range is an air-cooled cooler all in one large boiler with a capacity of 225 l ends in which most of the solid products were collected. the Gases were fed from the large kettle to a cyclone where further solids were separated. Then the Gases fed to an alkali scrubber, an oxidizing chamber (for oxidizing any carbon monoxide) and then drained. The reaction vessel and its outlet and inlet conduits were made of quartz glass. The reaction vessel also contained sampling points and thermal walls. The reaction vessel was placed in an oven introduced, which was heated to the desired reaction temperature.

A mixture of 7.7 kg Australian ilmenite and 7 »7 Petrol cakes geeigneterwise were pulverized, was fed to the reaction vessel and fluidized with nitrogen, had until the temperature of the bed is increased while adjusting the temperature of the oven at 37o ⁰ G. Nitrogen was passed through a Bromverdampfer and a mixture of nitrogen and bromine was stirred at 13O ⁰ C, wherein it contained bromine $ 11.8 Vol., The reaction vessel at an approximately constant speed, the 2.92 kg / hr. Bromine was fed in. After 5.75 hours, the flow of bromine was switched off and the reactor was cooled with nitrogen, during which

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BAD ORICHNAi,

19 the fluidized bed condition was still maintained in the bed.

Analysis of the gas leaving the cyclone showed that it contained essentially no bromine for the first hour and gradually increasing amounts of bromine thereafter. Analysis of samples from the bed showed that the ilmenite gradually lost its iron content as the rate decreased during the course of the reaction. At the end of the reaction time, the bed contained petroleum coke and a digested ilmenite ore with 90.3% by weight of TiO ₂ and 3.4% by weight of iron, which is present as oxides. The products collected in the large kettle and cyclone consisted of iron dibromide (and broaids of other metals) and no iron trihromide was present. No significant amount of titanium was lost from the bed.

Example 2

Example 1 was repeated, but instead of a mixture of nitrogen and bromine, a mixture of nitrogen, Oxygen and bromine, the 12.3 vol. # Of bromine and 9.8 vol. # Contained oxygen. The feed rate was 3.05 kg / hour. Bromine.

Analysis of the gas leaving the cyclone showed that it contained essentially no bromine for the first two hours and that the broo content rises quickly thereafter

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increased a constant value. Analysis of samples from bed showed that the ilmenite had lost its iron content, with most of the iron content being lost in the two hour period. At the end of the reaction, the bed contained petroleum coke and processed ilmenite ore with a content of 95.3% by weight of TiO ₂ and 0.8% by weight of iron as oxides. The products collected in the large kettle and cyclone were iron dibromide (and bromides of other metals) rather than iron tribromide. No significant amount of titanium was lost from bed.

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Example 3

This example serves to explain a continuously cyclical flow or fluidized bed bromination process and is carried out in the apparatus described above with reference to the accompanying drawing.

The mixture containing ilmenite (analysis 54.5 # TiO ₂ , 31 # Fe present as oxides) and petroleum coke in a weight ratio of 3.0 to 1 is used. The reaction vessel is; ' charged with this mixture, fluidized with dry nitrogen through line 33 and heated to 870 ⁰ O. A gas containing 10 vol. # Bromine, 7.4 vol. % Oxygen, the balance being nitrogen, is then used in place of the dry nitrogen. After 10 hours after steady conditions have been set, the current of the reaction zone 5 to the reaction zone 6 through the round hole 10 gases contain 1 vol. # Bromine and the gases leaving the reaction zone 6 by the Auiaßleitung 16, etc. only contain small amounts of bromine and essentially no iron tribromide. Iron dibromide condenses in the air-cooled cooler 16 and is separated from the output gases in the cyclone 21.

After passing it through the aggregate-forming rollers 22 in has run a storage funnel 23, the iron dibromide is fed to the reaction vessel 27 · It is

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sufficient additional iron dibromide added to allow bromine releases. Sufficient initially is supplied to form a bed and ^{air preheated to 50O 0} C is pumped by pump 32 through inlet pipe 30 and travels up through the bed where it reacts to form iron oxides and release bromine. The bromine is entrained in the stream of unreacted air and leaves the reaction vessel via the outlet line 31.

When steady conditions are reached, iron dibromide is transferred to the reaction vessel 27 from the storage funnel 23 fed at the same speed as is formed in reaction vessel 1. The iron dibromide becomes complete oxidized in the reaction vessel 27 and iron oxides are through the gap 35 in the storage funnel 34 · with a Removed speed corresponding to the speed at which iron dibromide is supplied to the reaction vessel 27 will. Air is in the reaction vessel 27 with a fed at such a rate that the gas leaving the reaction vessel 27 through the gas outlet line 31 Contains 13.5 vol. # Bromine and 10 vol. # Oxygen.

The gas from the gas outlet line 31 is fed back to the reaction vessel 1 via the gas inlet line 13. A sufficient amount of the starting gases from the cyclone 21 is fed by the pump 24 via the preheater 26 to the reaction vessel 1 fed through the gas inlet pipe 13 so that

009852/1960

the concentration of bromine in the gas feed in the reaction vessel 1 through the gas inlet line 13 to 10 VoI, # is held.

Under constant conditions, 2.84 kg / day. Ilmenite (mixed with the appropriate amount of carbon) converted with formation of 1.57 kg / hour. processed ore (analysis 94 $ fiOp »1 # iron, which is present as oxides). The bromine loading ratio through the inlet line 13 into the reaction vessel 1 is 2.4 kg / hour. Additional iron dibromide is used to compensate for bromine losses according to, OO25 kg / hour. Bromine supplied.

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Claims (1)

- 24 claims ; 1. A process for the preparation of titanium oxide "· and iron oxide-containing ores, characterized in that the ore with elemental carbon and bromine in the presence of a carrier gas containing between 1 and 50 vol. # Oxygen, at a temperature between 500 and 110o ⁰ O brings in contact. 2. The method according to claim 1, characterized in that the ore is mixed with elemental carbon and with a Feed gas containing bromine, oxygen and the carrier gas is brought into contact. 3. The method according to claim 2, characterized in that the feed gas is passed through a bed of ore and carbon is directed in such a way that a fluidized bed is formed. 4. The method according to claim 1 or 2, characterized in that one selects such working conditions that a Product gas containing carrier gas, carbon oxides, iron dibromide, iron tribomide and bromine is formed. 5. The method according to claim 4, characterized in that the iron tribromide as it is formed to iron dibromide is decomposed, -25- 009852/1960 6. The method according to claim 4 or 5, characterized in that that the iron dibromide content of the product gas to one Solid is condensed. . 7. The method according to claim 6 daduroh characterized in that the solid iron dibromide with the formation of iron oxide and Bromine can be oxidized. 8. The method according to claim 7, characterized in that the iron bromides are oxidized ^{at a temperature of at least 450 0 O.} 9. The method according to claim 7 or 8 daduroh characterized that bromine as (part of the feed gas in the circuit to be led. 10. The method according to claim 9, characterized in that the oxidation using an excess of oxygen " which is part of the feed gas. 11. The method according to any one of the preceding claims, characterized in that the amount of carbon in the bed is sufficient to provide enough carbon for the subsequent chlorination of the titanium oxide. 12. The method according to one of the preceding claims -26- 00985 2/1960 characterized in that the reaction occurs at a tempera door is carried out in the range of 800 to 1O5O ° G, 13 · Method according to An sprue II 12, characterized in that the reaction is ^{carried out at 87O 0} C «: · Method according to one of the preceding claims © thereby characterized in that a bromine ratio of between 5 and 15 vol. # is used in the feed gas. Method according to claim 14, characterized in that that a bromine ratio in the feed gas of between 8 and 12 vol. # is used. 16. Process for the preparation of titanium and iron oxides containing Ore in a continuous process, characterized in that one is a gaseous mixture of bromine and a carrier gas between 1 and 5O # Construction material contains, through the first bed, the ore and Contains elemental carbon, conducts the mixture of carrier gas, unreacted bromine, iron dibromide and carbon oxides passes from the first bed through a second bed, which also contains ore and elemental carbon, Introducing ore and elemental carbon into the second bed while getting some of the partially recycled second bed introduces into the first bed and part of the -27- 009852/1960 processed ore removed from the first bed, whereby both beds are operated as a fluidized bed by means of gases passed through and at a temperature of below 110O ⁰ O, 17. The method according to claim 16, characterized in that that three or four beds are used. 18. The method according to claim 12 or 13, characterized in that that the mixture of titanium ore and carbon is used in a weight ratio of 1: 1 to 3 * 1. 19. Process for the preparation of titanium and iron oxides containing Ore essentially as previously described in Example 2 or 3. 20. Processed ore, provided that it has been processed according to any of the preceding claims is made. 009852/1960 Blank page