JPS5839895B2 - Chlorination method for ilmenite or similar titanium ores - Google Patents

Description

[Detailed Description of the Invention] The present invention makes it possible to co-produce titanium tetrachloride and iron-free titanium ore from ilmenite or similar titanium ores by two-stage chlorination including recovery and reuse of dilute chlorine. This invention relates to a method for chlorinating ilmenite or similar titanium ores.

At present, chlorination treatment methods for ilmenite or titanium ores similar to it (hereinafter simply referred to as ilmenite) are broadly divided into two processes.

One method involves simultaneously chlorinating iron and titanium in the ore using chlorine together with coke, cooling the resulting mixed gas of iron chloride and titanium tetrachloride, and precipitating high-boiling iron chloride as a solid phase. This is a method to separate titanium tetrachloride from the gaseous phase.

The other method is the selective chlorination of ilmenite, in which ilmenite is reacted with chlorine in the presence of a limited amount of coke, for example, coke at a weight of 10 g, and the iron content in the ore is selectively chlorinated. This is a method of producing so-called synthetic rutile by concentrating titanium oxide in the residue to a Tie2 of about 95%, and then reacting the synthesized rutile with chlorine in the presence of coke to produce titanium tetrachloride.

However, in the former case, the iron chloride separated from titanium tetrachloride is used as a sewage treatment agent or is discarded.

To recover chlorine from solid iron chloride, solid iron chloride is reheated to volatilize and react with oxygen in the gas phase, but there are losses associated with handling solid iron chloride, which is highly hygroscopic.
In other words, operational troubles such as blockage of transport routes and ore feeding equipment, and the resulting environmental pollution become a problem.

Furthermore, in this method, the high-temperature chlorination furnace produced gas is cooled to first precipitate iron chloride as a solid phase, and this solid iron chloride is reheated, so the thermoeconomic irrationality is a major drawback of this method. It has become.

On the other hand, since the latter is originally intended for the production of synthetic rutile,
It is necessary to increase the TiO2 grade and improve the commercial value. Therefore, the ore taken out from the chlorination furnace after the reaction is magnetically sorted to separate the ore in the middle of the reaction with high iron content as a magnetic material, and then the ore is separated into a non-magnetic material. Synthetic rutile is produced through processes such as flotation or wind sieving to separate the excess solid carbonaceous reducing material that collects in the rutile.

The synthetic rutile thus produced is further chlorinated in the presence of a solid carbonaceous reducing agent to produce titanium tetrachloride.

Further, regarding the iron chloride produced in this selective chlorination method, as described in US Pat. No. 3,925,057, for example, the chlorination furnace gas containing the iron chloride is
1. A method is adopted in which the chlorine is introduced into a dechlorination furnace and reacted with oxygen, converting it into chlorine and iron oxide.

However, the chlorine separated in this way is added in excess of the stoichiometric amount to the carbon dioxide and, to a lesser extent, the sealing nitrogen used in various parts of the equipment, or sometimes to the reaction with iron chloride. Since the chlorine is diluted with oxygen, etc., the chlorine can be separated from the mixed gas by pressurization, liquefaction by cooling, or absorption into a solvent such as carbon tetrachloride.

However, liquefying the above-mentioned mixed gas in this case requires high pressure and deep cooling, which burdens the electricity costs.
Further, in absorption into a solvent, there is a problem in that the loss of the solvent to the exhaust gas is large.

The present invention solves the above-mentioned drawbacks of the conventional method and makes it possible to co-produce titanium tetrachloride and iron-free titanium ore from ilmenite or similar titanium ores through two-stage chlorination including recovery and reuse of dilute chlorine. The present invention provides a method for chlorinating ilmenite or similar titanium ores that enables the chlorination of ilmenite or similar titanium ores. a roasting step of oxidizing roasting; (b) primary chlorination in which the roasted ore obtained in the step is selectively chlorinated in the presence of a solid carbonaceous reducing material to convert mainly iron in the roasted ore to iron chloride; step, (c) a dechlorination step of reacting the produced gas mainly composed of iron chloride and carbon dioxide from the step with oxygen or a molecular oxygen-containing gas to convert the iron chloride into chlorine and iron oxide; ) After separating the fine iron oxide and unreacted iron chloride accompanying the chlorine-containing recovered gas from the above step, the chlorine-containing recovered gas is separated from the reaction layer obtained in the second chlorination step and the solid carbonaceous reducing material. A secondary chlorination step in which titanium tetrachloride and iron-free titanium ore are co-produced by reacting in the presence of ilmenite or similar titanium ores.

Next, the present invention will be explained with reference to the drawings.

FIG. 5 is a system diagram of equipment used to implement an embodiment of the present invention.

In the figure, in the first roasting step, raw material ilmenite 10 is dried in a drying furnace 1 by the waste heat of an oxidizing roasting furnace 2, and then enters the oxidizing roasting furnace 2.

In the oxidation roasting furnace 2, the temperature inside the furnace is maintained in the range of 900°C to 1000°C by blowing fuel 11 of heavy oil and air 12, and the FeO content remaining in the ore is reduced to 6.5% by weight φ. In the following 1, oxidative roasting is performed as shown by the following formula (1).

The effect of oxidative roasting is to prevent the increase in the viscosity of the reaction layer due to the formation of ferrous chlorides, suppress the formation of titanium tetrachloride, and generate FeCl3, thereby improving selectivity in the chlorination reaction that leads to the next primary chlorination step. The goal is to provide the following.

When the oxidation roasting temperature is 900°C or less, the roasted product does not become Fe2TiO3, but Fe2O3 and TiO2 are each in a liberated state, or Fe2TiO5
In this case, titanium tetrachloride is likely to be generated as a composite of one or more of Fe 203 and other compounds of TiO2, or a mixture thereof, making selective chlorination of iron difficult.

Of course, there is a limit to the amount of iron that can be removed by selective chlorination, and if the reaction proceeds beyond that limit, titanium will also react in parallel.

Therefore, in order to keep the limit of the iron concentration that can be selectively chlorinated as low as possible, it is necessary to ensure the production of Fe2Ti05 by oxidative roasting.

In the primary chlorination step of the second step, the roasted ore obtained in the previous step is continuously or intermittently fed into the first chlorination furnace 3, and at the same time coke 13 as a solid carbonaceous reducing material is roasted. The stoichiometric amount required to combine with the oxygen of iron oxide in the burnt ore is 2
Chlorine 14 is added in an amount equal to or less than 1 times the stoichiometric amount for converting the iron oxide to FeCl 3 or 10% in excess of the stoichiometric amount to convert the iron oxide to FeCl 3 to carry out chlorination in a fluidized state. Let's do it.

The reaction temperature is 800°C or higher, preferably 900-1000°C.
At 'C, a selective chlorination reaction shown by the following formula (2) is carried out to produce iron chloride.

The third step, the dechlorination step, consists mainly of iron chloride and carbon dioxide produced in the previous step, as well as a small amount of sealing nitrogen used in the first chlorination furnace 3, a trace amount of COI, and impurities in the raw ore, such as A mixed gas containing chlorides such as manganese, and sometimes unreacted chlorine, is introduced into the dechlorination furnace 4, where oxygen or a molecular oxygen-containing gas is added to the iron chloride in a range of stoichiometric amount to 10 molar excess. 15 is blown in and reacts with the iron chloride, converting the iron chloride into chlorine and iron oxide.

The reaction temperature is 500 to 900 DEG C., and a dechlorination reaction shown by the following equation (3) is carried out, producing iron oxide and recovering chlorine diluted with CO2.

Although it is not shown in the above equation (3), oxygen is consumed due to the oxidation of a small amount of CO or a part of MnCl2 in the generated gas of the first chlorination furnace 3, but the amount is small. Therefore, there is no need to take this into account.

In the final secondary chlorination step, the chlorine-containing recovered gas from the dechlorination furnace 4 in the previous step contains chlorine and carbon dioxide as main components.
In addition, it contains a small amount of nitrogen, unreacted iron chloride, and sometimes oxygen added in excess of the reaction amount, and is accompanied by fine iron oxide, so the chlorine-containing recovered gas is passed through a cyclone,
The iron oxide 16 was separated and discharged by treatment with a dust treatment device 5 consisting of a combination of part or all of a dust chamber, a gas cooler, a bag filter, an electrostatic precipitator, etc., and solid iron chloride precipitated by cooling the gas was separated. Later, that-! 1 into the second chlorination furnace 6.

This separated unreacted iron chloride 17 is returned to the dechlorination furnace 4.

On the other hand, the reaction amount 18 of the first chlorination furnace 3 in the second chlorination step differs depending on the type of ore, but in all cases, the average composition contains unreacted iron in an amount exceeding the selective chlorination limit value. This is extracted from the first chlorination furnace 3 and once received in the storage tank 8 or directly introduced into the second chlorination furnace 6.

This reaction amount 18 is TiO in the state extracted from the chlorination furnace 3.
2 grades range from 85 to 92φ, residual iron is Fe2O3
Generally, the diameter is 5φ or more, but in the case of ilmenite that is highly weathered and has good selective chlorination properties, it may be 5φ or less.

In addition, the reaction amount 18 contains excess coke 13 that remained unconsumed in the selective chlorination process of the primary chlorination process.

The second chlorination furnace 6 uses a fluidized fluidized furnace like the first chlorination furnace 3, but in order to activate the chlorination reaction and increase the recovery rate of chlorine as titanium tetrachloride, the second chlorination furnace 6 is Coke 19 is replenished.

This replenished coke 19 is fed to the second chlorination furnace 6 based on the 10 to 20 weight ratio of the reaction amount 18 of the first chlorination furnace 3, and is based on the properties of the raw material ilmenite, the operation condition button for dechlorination, and the following. It can be varied depending on the purpose of ore processing.

For example, when excess oxygen is used in the reaction in the dechlorination furnace 4, free oxygen is contained in the chlorine-containing recovered gas 20 introduced into the second chlorination furnace 6, and the solid carbonaceous reducing material is It is necessary to adjust the replenishment amount of solid carbonaceous reducing material by taking into consideration the consumption of solid carbonaceous reducing material.

The reaction temperature of the second chlorination furnace 6 is 800° C. or higher, preferably around 950° C., and the reaction of the following equation (4) occurs in parallel with the chlorination of the iron remaining in the reaction amount 18.

During this reaction in the second chlorination furnace 6, the chlorine-containing recovered gas 20 from the dechlorination furnace 14 chlorinates approximately - amount of the reaction amount 18 introduced into the second chlorination furnace 6 to form titanium tetrachloride, High-grade titanium ore 21 that has been sufficiently deironated remains as a residue.

The produced gas containing titanium tetrachloride and a small amount of iron chloride is treated in a gas treatment device 9 by a known method to first separate iron chloride 17, then recover it as crude titanium tetrachloride 22, and the remaining gas is After gas cleaning, the waste gas 23 is discharged into the atmosphere.

Further, the deironated titanium ore 21 as a residue is extracted from the second chlorination furnace 6 and subjected to, for example, flotation or Wilfl treatment.
ey Table'! Alternatively, by separating excess solid carbonaceous reducing material using a beneficiation means such as an Air Table or the like, synthetic rutile with Ti02=95% or more can be obtained.

As described above, the present invention aims to co-produce titanium tetrachloride and iron-free titanium ore from ilmenite through two-stage chlorination including reuse of chlorine gas recovered in a diluted state during the dechlorination process. It makes it seem possible.

Furthermore, in the above, if it is necessary to convert the entire amount of the reaction ore into titanium tetrachloride, the first chlorination furnace 3
If approximately the same amount of chlorine as that injected into the second chlorination furnace 6 is introduced into the second chlorination furnace 6 from another nozzle or mixed with the chlorine-containing recovery gas from the dechlorination furnace 4, The entire amount of iron and titanium in the introduced reactive ore can be chlorinated.

In that case, the amount of chlorine newly introduced into the second chlorination furnace 6 is of course adjusted depending on the composition of the raw material ilmenite.

The effects of the present invention are as follows.

(1) In the conventional selective chlorination method of ilmenite aimed only at producing synthetic rutile, dilute chlorine recovered from iron chloride is expensive to separate and recover from accompanying gases such as CO2 and N2. Although the efficiency is low, the present invention utilizes this recovered dilute chlorine for chlorination of titanium oxide in its original state without concentrating and separating it, and recovers it as titanium tetrachloride, making it easy to separate it from the accompanying gas. It also has good recovery efficiency.

Moreover, approximately half of the titanium content in the reaction ore treated in the first chlorination furnace is recovered as deironated high-grade titanium ore, and this titanium ore can be synthesized by simply separating the excess solid carbonaceous reducing material. becomes.

As described above, the present invention completely eliminates the need for recovery equipment for dilute chlorine, which is a problem in conventional selective chlorination methods.

(2) In the conventional direct chlorination method of producing titanium tetrachloride directly from ilmenite, a large amount of by-product iron chloride is separated as a solid phase. The thermoeconomic disadvantages of heating, vaporization and the engineering problems of losses and environmental pollution associated with the handling of hygroscopic solid iron chloride can be solved or at least significantly reduced by the present invention.

In other words, most of the iron in the raw material ilmenite is removed as iron chloride in the primary chlorination process, and this iron chloride can be treated in the next dechlorination process without being processed outside the furnace. Both the unreacted iron chloride and the iron chloride produced from the secondary chlorination step are small amounts, and their handling is much easier than in the conventional direct chlorination method.

The dechlorination reaction is completely automatic due to the amount of heat possessed by the gas produced in the primary chlorination process and the reaction heat of the iron chloride oxidation reaction.
-thermal, and the return of the iron chloride to the dechlorination step serves as a means for temperature control of the dechlorination reaction.

As described above, the present invention makes it possible to co-produce titanium tetrachloride and iron-free titanium ore from ilmenite or similar titanium ores through two-stage chlorination including recovery and reuse of dilute chlorine. The present invention provides a similar method for chlorinating titanium ore, and its industrial value is extremely large.

Next, the present invention will be explained in more detail with reference to Examples, but the present invention is not limited to the following Examples unless it exceeds the gist thereof.

Example l Ti02=53.3'%, Fe0=20.4%
, Fe203-19.8%, Mn0-1.63%
, 5i02 = 1.68%, A1203 = 19.1%, etc. Australian ilmenite was heated in air to 950 °C, and the residual divalent iron in the ore was oxidized in state 1 as FeO of 1.63%. Roasted.

This roasted ore was transferred to a quartz tube fluidized bed type reaction tube (first chlorination furnace) with an inner diameter of 10C1n heated in an electric furnace at a rate of 75g/lni!
At the same time, calcined petroleum coke that has been crushed to 20 mesh or less (Tyler standard, the above particle size is based on this standard) is fed continuously at a rate of 1.5 t, and at the same time 8% of the calcined ore is added to the roasted ore in the reaction tube. It was added to the roasted ore at the ore feed port.

13.5Nl/r11i of chlorine from the bottom of the reaction tube! Selective chlorination of the iron content in the roasted ore was carried out at a fluidized bed height of 60 crIl and a temperature of 950°C.

The reaction ore was continuously extracted by overflow, and the average grade of this extracted ore was Ti02 = 89.2%, Fe2
03 = 6.28%, 5i02 = 1.05 excellent, A120
3 = 1.02 tons, and about 2.8 tons of the petroleum coke was mixed in.

On the other hand, the gas produced by the selective chlorination reaction in the first chlorination furnace was introduced into the cylindrical empty column dechlorination furnace and reacted with oxygen.

This dechlorination furnace is a castable furnace with a furnace length of 180 crf1 and an inner diameter of 25 cm, and the outer plate is surrounded by an iron plate.

Electric heating resistance wire was inserted vertically into the wall of the castable along its circumference, thereby heating the furnace.

Two dechlorination furnaces of the same type are connected at the bottom of the furnace, and the gas produced by the first chlorination furnace introduced from the top of the first tower mixes with oxygen injected from three nozzles on the furnace wall downstream of 25 cfr1, and reacts. While doing so, it is extracted from the top of the second tower.

The temperature near the day when the chloride gas was introduced into the first tower was 900°C, with a temperature gradient decreasing toward the downstream, and the temperature near the outlet of the second tower was adjusted to 650°C.

Oxygen had a purity of 99.8%, and 6.8 Nl/min of oxygen was heated to about 300° C. through a preheating furnace and introduced into the dechlorination furnace.

The chlorine-containing recovery gas from the dechlorination furnace is cooled while passing through a dust chamber, and unreacted iron chloride is recovered together with fine iron oxide particles in the next bag filter. It was returned to the chlorine furnace.

The second chloride is electrically heated from the outside in a quartz fluidized bed reaction tube of the same type as the first chloride, and the temperature of the fluidized bed is 900°.
Adjusted to C.

The reaction ore extracted from the first chloride is stored in a hopper, and is further transferred to the second chloride feed hopper.
The second chloride was introduced continuously at /m=.

At the same time, 12 cups of the same coke used in the second chloride step was added to the reaction ore at the feed port for the second chloride feed ore.

The temperature of the fluidized bed was adjusted to 900° C.K., and the chlorine-containing recovered gas from the dechlorination furnace, which was sucked through a bag filter by a blower, was blown into the fluidized bed through the second chlorination bottom nozzle.

The second chloride gas was cooled while passing through the dust chamber, and iron chloride was precipitated as a solid phase, but this iron chloride was returned to the dechlorination furnace.

The gas leaving the dust chamber is cooled by an indirect cooling tower with cold water and a freezing trap, and the titanium tetrachloride vapor is condensed.
Separated from waste gas.

On the other hand, the reaction residue overflowing from the reaction tube as secondary chloride was extracted at about 259/mTj1 and
After separating the residual coke in the residue using a ley table, the residue obtained by drying had Ti02 = 96.8%,
Fe203=0.67g, Mn0-0.06%, 5i
It had a composition of 02=0.92% and M2O3-1,03φ.

Example 2 Reaction factors used in the secondary chlorination step of chlorinating the first-chlorination reaction ore using the recovered gas containing chlorine as the main component from the dechlorination furnace, that is, the temperature, the proportion of the reducing agent, The effects of chlorine partial pressure, residual oxygen concentration, etc. were investigated.

The experiment was conducted using the same equipment as in Example 1, and a batch test was conducted by injecting gas at a volumetric rate of 121/ml yr into [0 kg] of the following reaction ore at one time.

The composition of the first-chloride reaction ore used was Ti02 = 88
．． 9φ, Fe 203~6.13%, Mn0=0.2
2%, 5i02-1.14%, Al1203=1.
The experimental conditions were a temperature of 880 to 960°C, a partial pressure of chlorine of 0.16 to 1.0 atm, a calcined petroleum coke as a reducing agent, and an amount of addition of 5 to 20 parts by weight based on the reaction ore. Ta.

The experimental results are shown in FIGS. 1 to 4.

In the figure, XTiO2 is the value obtained by dividing the amount of reacted T,02 by the amount of T,02 in the initial raw material ore.
)- is a parameter indicating the progress of the reaction.

Figures 1 and 2 show the situation 10 minutes after the start of the reaction, and Figure 3 shows the situation 15 minutes after the start of the reaction.

FIG. 1 shows the influence of the amount of coke added on the reaction. According to FIG. 1, when the amount of coke is around 5 yen, the reaction is more sensitive than when the amount of coke is higher than that.

Therefore, in order to maintain steady operation within this range, the amount of coke must be strictly controlled.

From the results shown in FIG. 2, it can be seen that the influence of chlorine partial pressure on the reaction is linear, and it is relatively easy to control the reaction conditions with respect to fluctuations in chlorine partial pressure.

FIG. 3 shows the influence of temperature on a mixed gas having a chlorine partial pressure of 0.6, a carbon dioxide partial pressure of 0.3, and a nitrogen partial pressure of 0.1.

In addition, Figure 4 shows the influence of unreacted oxygen contained in the chlorine-containing recovery gas of the dechlorination furnace on the reaction rate of the reactive ore applied to the secondary chloride. It is necessary to add stoichiometrically reactive coke in advance.

As described above, the reaction in the second chlorination furnace can be controlled without reducing the reaction efficiency in response to fluctuations in operating conditions by considering the data shown in FIGS. 1 to 4.

Example 3 The same ilmenite as in Example 1 was dried in a rotary kiln at a rate of 88 kg/hr, and then dried with an inner diameter of 50 cm.
The ore was fed to the $ oxidation roasting furnace.

The oxidation roasting furnace is a fluidized bed reactor that injects heavy oil and burns it with air at 65 Nm'/Hr and maintains the temperature at 900 to 980°C.

The average residence time of the three ores in the furnace was 4 hours, and the FeO of the ore taken out from the furnace was suppressed to 2φ or less.

The roasted ore overflowing from the oxidation roasting furnace was introduced into the chlorination stage through a double bell damper.

The first chlorination furnace is a fluidized fluidized furnace with an inner diameter of 40 cIn.
24ONl/mi kept at 0°C and blown in from the bottom of the furnace
n of chlorine reacts with the ore in the presence of calcined petroleum coke with a fineness of 20 mesh or less introduced at a rate of 7.2 kg/Hr (8% relative to the ore) to selectively chlorinate iron. I set it.

The average residence time of the ore in the first chlorination furnace was 2.5 hours, and the average composition of the extracted reaction ore was Ti02 = 85.9%.
Fe20s = 5.54%, MnO = 0.6%
, 5iO2 = 1.43%, M2O5 = 1.84%, and 4.0% coke was mixed in.

The reacted ore extracted from the first chlorination reactor was stored in a storage tank.

The gas produced in the first chlorination reactor was as large as FeCl35 = 51.4 volume and Co2 = 38.6 volume, and the remaining 10 volumes were N2 and a small amount of unreacted C12. Introduced into the dechlorination furnace, 135N7/771i!
The iron chloride was converted to chlorine and iron oxide by reacting with the oxygen of t.

The dechlorination furnace is a cylindrical sky tower furnace with an inner diameter of 80 cm and a furnace length of 27 cm.
Two furnaces of the same type with a diameter of 0 cm are connected at the bottom of the furnace.

The first chlorination furnace gas is injected downward from the center of the top of the first furnace of the dechlorination furnace, and the oxygen is injected from six nozzles on the wall of the first furnace and mixed with the first chlorination furnace gas.

The temperature near the chlorination furnace gas inlet of the dechlorination furnace was set at 900°C, with a temperature gradient decreasing toward the downstream, and the temperature reached 600°C at the exit of the second chlorination furnace. There is.

The chlorine-containing recovered gas from the dechlorination furnace is sent to a dust chamber and gas cooler to precipitate most of the entrained iron oxide, and a bag filter removes precipitated iron chloride and fine particles of iron oxide by cooling.

The iron chloride removed by the bag filter was returned to the dechlorination furnace together with fine iron oxide particles.

The composition of the gas after passing through the bag filter is Cl2=
55.8 volume φ, Co2 = 36.1 volume φ, remaining 8
．． One volume φ contained N2 and a small amount of 02.

On the other hand, the reaction ore of the first chlorination furnace is continuously fed to the second chlorination furnace of the same type as the first chlorination furnace at a rate of 54kp/hr.
At the same time, the same coke used in the first chlorination furnace was
It was added to the reacted ore at a rate of 1 kg/hr (15 kg/hr).

The chlorine-containing recovery gas from the dechlorination furnace was blown into the second chlorination residue from the bottom of the furnace by suctioning it with a blower through a bag filter.

The composition of the second chloride produced gas is ■2=27.1 volume φ,
CO = 22.5 capacity TiC14 = 40.9 capacity φ
, FeCl3 = 6.0 capacity φ, of which FeCl3
was separated as solid FeCl3 by cooling the gas and returned to the dechlorination furnace.

The gas is further cooled in a water cooling tower, and the titanium tetrachloride condensed in the condenser is approximately 50 kg/hrfTic4
= 96.5%, Al2Cl2s=0.2, 5iC
It had a composition of A4=1.2% and FeC13=1%.

On the other hand, about 20k due to overflow from the second chloride
The iron-free titanium ore extracted at a rate of g/hr was separated from coke by flotation and dried to produce synthetic rutile, whose composition was TiO2 = 97.2%, Fe203 = o.
, 48%, Mn0=0.04%5i02=0
．． 88'%, AA203 = 1.25% f.

[Brief explanation of the drawings] Figure 1 shows 1 stage after the start of the reaction in the secondary chlorination step of the present invention.
A graph diagram showing the relationship between the amount of coke added and the degree of reaction progress after 0 minutes have elapsed; FIG. Figure 3 is a graph showing the relationship between temperature and reaction progress 15 minutes after the start of the reaction, Figure 4 is a graph showing the relationship between oxygen partial pressure and reaction progress, and Figure 5 is a graph showing the relationship between oxygen partial pressure and reaction progress. 1 is a system diagram of an apparatus used to implement an embodiment of the present invention. Click the button on the diagram, 1...Drying oven, 2...Oxidation roasting oven, 3
...Second chlorination furnace, 4.Dechlorination furnace, 5.Dust treatment device, 6.Second chlorination furnace, 7.Heat exchanger, 8
... Reactive ore storage tank, 9... Gas treatment device, 10...
Ilmenite, 11...Fuel, 12...Air, 13
, 19...Coke 14...Chlorine, 15...Oxygen or molecular oxygen-containing gas, 16...Iron oxide, 17.
...Iron chloride, 18...Reaction ore, 20...Chlorine-containing recovered gas, 21...Deiron-free titanium ore, 22...Titanium tetrachloride, 23, 24...Waste gas.

Claims (1)

[Scope of Claims] 1. A process for chlorinating ilmenite or similar titanium ores, including (a) a roasting step of oxidizing and roasting ilmenite or similar titanium ores; (b) a roasted ore obtained in the step; a primary chlorination step in which the iron content of the roasted area is selectively chlorinated in the presence of a solid carbonaceous reducing agent; or a dechlorination step in which the iron chloride is converted into chlorine and iron oxide by reacting with a molecular oxygen-containing gas; (d) after separating the fine iron oxide and unreacted iron chloride accompanying the chlorine-containing recovered gas from the step; , a secondary chlorination process in which the chlorine-containing recovered gas is reacted with the reaction form obtained in the secondary chlorination process in the presence of a solid carbonaceous reducing material to co-produce titanium tetrachloride and iron-free titanium ore; A method for chlorinating ilmenite or similar titanium ores consisting of a combination of .