KR101900827B1 - Manufacturing apparatus of titanium tetrachloride - Google Patents

Abstract

An apparatus of manufacturing titanium tetrachloride is introduced. The apparatus includes a reaction part where a first product which includes iron chloride formed by the reaction of ore containing iron and titanium, chlorine, and a carbon source, and a second product which includes titanium tetrachloride formed by the reaction of precipitate containing titanium, chlorine, and a carbon source are generated; a first condensation part which is connected to the reaction part and performs selectively the condensation of the first product among the first product and the second product moved from the reaction part; and a second condensation part which is connected to the first condensation part and performs the condensation of the second product moved from the first condensation part. It is possible to obtain high purity iron chloride and titanium tetrachloride.

Description

TECHNICAL FIELD [0001] The present invention relates to a titanium tetrachloride (TiCl4)

The present invention relates to an apparatus for producing titanium tetrachloride using an ore containing iron and titanium.

The conventional apparatus for producing titanium tetrachloride (TiCl ₄ ) is characterized in that the ore such as aluminum (FeTiO ₃ ) is partially reduced with a carbon source or the like and leached into dilute sulfuric acid. First, the ore is charged into a rotary kiln together with a carbon source, and the Fe ₂ O ₃ contained in the ore is partially reduced with FeO at 800 ° C to 950 ° C. In this process, CO and CO ₂ gases are generated.

The partially reduced ore is slowly cooled to prevent reoxidation, then the unreacted carbon source is separated and the ore without Fe ₂ O ₃ is sent to the leaching process.

In the leaching step, the spent sulfuric acid generated in the process of producing high purity titanium dioxide (TiO ₂ ) by the sulfuric acid method is leached into dilute sulfuric acid regenerated by the use of ammonia as shown in the following formula.

TiO ₂ · FeO + H ₂ SO ₄ = FeSO ₄ + TiO ₂ + H ₂ O -

Therefore, in the conventional method as described above, since titanium tetrachloride has to be prepared from titanium dioxide after extracting high purity titanium dioxide from ores such as ilmenite, the process by the production apparatus is complicated and the process time is long.

It should be understood that the foregoing description of the background art is merely for the purpose of promoting an understanding of the background of the present invention and is not to be construed as an admission that the prior art is known to those skilled in the art.

KR 2001-0021618

A titanium tetrachloride production apparatus capable of obtaining iron chloride and titanium tetrachloride from vapor ore containing iron and titanium and capable of obtaining high purity iron chloride and titanium tetrachloride through selective condensation.

According to an aspect of the present invention, there is provided an apparatus for producing titanium tetrachloride, comprising: a ore containing iron and titanium; Goat; And a carbon source to produce a first product containing iron chloride and a precipitate containing titanium, wherein the precipitate; Goat; And a carbon source to produce a second product containing titanium tetrachloride; A first condenser connected to the reaction unit and selectively condensing the first product among the first product and the second product moved from the reaction unit; And a second condenser connected to the first condenser and condensing the second product moved from the first condenser.

Wherein the reaction unit comprises the ore; Goat; And a carbon source; And a first temperature controller disposed outside the reaction body and maintaining the temperature of the internal space at 800 ° C to 1100 ° C.

Wherein the reaction part has one end communicated with the internal space and the other end connected with the first condensing part; And a second temperature controller disposed outside the moving path and maintaining the temperature inside the moving path at 700 ° C to 800 ° C.

The reaction section being connected to an upper portion of the reaction body, the hopper providing the ore to the internal space; A gas supplier connected to a lower portion of the reaction body and supplying chlorine or an inert gas to the internal space; And a carbon source supplier connected to an upper portion of the reaction body and supplying a carbon source to the inner space.

Wherein the reaction unit comprises: a supply path for connecting the gas supply unit and the internal space; And a control valve installed on the supply path and interrupting the entry and exit of chlorine or an inert gas.

The first condensing portion is connected to the moving path, and the first condensing space formed therein for condensing the first product may be maintained at 20 ° C to 250 ° C.

Wherein the first condensing portion includes a first condensing body having the first condensing space therein; A first condensing passage for communicating the moving passage and the first condensing space; And a first opening / closing valve installed on the first condensing passage for controlling the entry and exit of the first product and the second product.

The first condenser may further include a third temperature controller disposed outside the first condenser to maintain the temperature inside the first condenser at 700 ° C to 800 ° C.

The second condensing portion is connected to the first condensing body, and the second condensing space formed therein for condensing the second product may be maintained at 20 ° C or lower.

Wherein the second condensing portion includes a second condensing body having the second condensing space therein; An accumulator coupled to the second condensing body and storing the condensed second product in the second condensing body; A second condensing passage for communicating the first condensing space and the second condensing space; And a second opening / closing valve installed on the second condensing passage for controlling the entry / exit of the second product.

And a purifier connected to the second condenser and configured to purify the condensed second product.

According to the titanium tetrachloride production apparatus of the present invention as described above, it is possible to obtain gaseous iron chloride and titanium tetrachloride from iron ore ore-containing ores and selectively condense them to obtain high purity iron chloride and titanium tetrachloride.

1 is a view showing an apparatus for producing titanium tetrachloride according to an embodiment of the present invention.
FIG. 2 is a view showing a refining unit according to an embodiment of the present invention.

Hereinafter, preferred embodiments of the present invention will be described with reference to the accompanying drawings.

1, an apparatus for producing titanium tetrachloride according to an embodiment of the present invention will be described.

The apparatus for producing titanium tetrachloride according to an embodiment of the present invention includes a reactor 100, a first condenser 200, and a second condenser 300.

The reaction part (100) reacts with the iron and titanium-containing ore charged into the reaction part (100) and the chlorine and carbon source supplied to the inside, thereby producing a first product containing iron chloride and a precipitate containing titanium, The carbon source may be reacted to produce a second product containing titanium tetrachloride.

An ore containing iron and titanium may be charged in the space provided in the reaction part 100. The ores containing iron and titanium may be iron (Fe) in the form of iron oxide (FeO, Fe ₂ O ₃ ) and titanium (Ti) in the form of titanium oxide (TiO ₂ ). As the ore, rutile containing titanium, and anatase may be used. Preferably, a low cost Ilmenite ore can be used.

The reaction part 100 may be maintained at a temperature of 800 ° C. or higher so that the reaction of chlorine (Cl ₂ ) and a carbon source supplied to the inside of the ore and the inside can be performed. Specifically, carbon sources such as Cokes, Charcoal and the like can be used and become a source of carbon (C). Ore containing iron and titanium can be activated at temperatures above 800 ° C and can be expressed as FeTiO ₃ .

Activation of ore may mean the removal of unnecessary components from the ore and the state in which iron oxide or titanium oxide can react well with chlorine and carbon sources.

The first chlorination reaction in which the iron oxides of the following formulas (1) and (2) react with chlorine due to the reaction of ore with chlorine and carbon source in the reaction part 100 can be performed first. The affinity between iron and chlorine is higher than the affinity between titanium and chlorine, so that the iron chloride reaction takes priority.

The first chlorination reaction as shown in the following formulas (1) and (2) can be performed first at a temperature of 800 캜 or more for about 90 minutes. As the amount of ore increases, the flow rate of chlorine supplied can also increase. Preferably, the flow rate of chlorine can be determined to be about 1000 sccm per kg of ore.

FeTiO ₃ + C + Cl ₂ = FeCl ₂ + CO + TiO ₂ - (1)

2FeTiO ₃ + 2C + 3Cl ₂ = 2FeCl ₃ + 2CO + 2TiO ₂ - (2)

Due to the first chlorination reaction, a gaseous first product containing iron chloride such as FeCl ₂ and FeCl ₃ can be produced. Carbon monoxide (CO) and unreacted chlorine may be further included.

Further, due to the chloride reaction 1 can be a precipitate of a solid phase that contains a titanium oxide such as TiO ₂ produced. An unreacted carbon source and the like may be further included.

After the first chlorination reaction, the secondary chlorination reaction in which the titanium oxide of the following formulas (3) and (4) reacts with chlorine due to the reaction of the chlorides and the carbon source with the solid precipitate in the reaction section 100 can be performed.

TiO ₂ + C + 2Cl ₂ = TiCl ₄ + CO ₂ - (3)

TiO ₂ + 2C + 2Cl ₂ = TiCl ₄ + 2CO ????? (4)

The second chlorination reaction may produce a second product comprising titanium tetrachloride (TiCl ₄ ). Carbon monoxide, carbon dioxide (CO ₂ ) and unreacted chlorine may be further included.

The inside of the reaction part 100 can be maintained at 800 DEG C or higher so that the second product containing titanium tetrachloride formed from the chloride of the liquid is converted into the vapor phase.

The first condensing part 200 is connected to the reaction part 100, and the first product moved from the reaction part 100 can be condensed.

Preferably, in the case of the first condensing part 200, an internal space communicating with the space inside the reaction part 100 may be provided. The space inside the first condenser 200 can be maintained at a temperature of 20 ° C to 250 ° C. Accordingly, it is possible to condense the gaseous first product containing the iron chloride transferred from the reaction section 100 into a solid phase. The iron chloride such as FeCl ₃ collected in the first condenser 200 can be used as a separate resource such as a wastewater treatment material.

The passage through which the reaction part 100 and the first condenser 200 are connected can control the flow of gas through a valve or the like.

More specifically, as the first chlorination reaction and the second chlorination reaction are performed in the reaction section 100, the reaction section 100 and the first condensation section 200 are connected to each other while the first product and the second product are produced, Can be opened. Or the passage through which the reaction part 100 and the first condenser 200 are connected for the movement of the first product and the second product after the first chlorination reaction and the second chlorination reaction may be opened.

The second condenser 300 is connected to the first condenser 200 and the second product moved from the first condenser 200 can be condensed.

Preferably, in the case of the second condensing part 300, an internal space communicating with the space inside the first condensing part 200 may be provided. The space inside the second condenser 300 can be maintained at a temperature of 20 ° C or lower. Accordingly, it is possible to condense the gaseous second product containing titanium tetrachloride, which has been moved from the second condenser 300, into a liquid phase.

More specifically, the first condensation of the first product is performed at 20 ° C to 250 ° C of the first condenser 200, and the second product, which is still in the vapor phase, can be transferred to the second condenser 300. The second product moved to the second condenser 300 can be condensed only at a temperature of 20 ° C or lower.

The reaction unit 100 of the apparatus for producing titanium tetrachloride according to an embodiment of the present invention may include a reaction body 110 and a first temperature controller 120.

The reaction body 110 may be provided with an inner space 111 through which a reaction of ore and chlorine and carbon is performed.

The ore and the carbon source are laminated from the lower part of the inner space 111 of the reaction body 110 and the chlorine can be supplied to the lower part of the reaction body 110. Thus, the reaction of ore with chlorine and carbon source can be performed in the inner space 111.

The first temperature regulator 120 is disposed outside the reaction body 110 and can maintain the temperature of the internal space 111 at 800 ° C to 1100 ° C.

A temperature of 800 or more is required as an effective temperature for the reaction of iron oxide and chlorine and carbon source of ore. When the temperature is higher than 1100 ° C, when the ore or carbon source is present in the form of powder, coagulation phenomena may occur between powders, which may result in ineffective fluidization.

The first temperature regulator 120 may form a temperature for activating the ore charged in the inner space 111. It is also possible to form a temperature at which the reaction of ore with chlorine and carbon source occurs. Such temperature may be 800 ° C to 1100 ° C as mentioned above.

The reaction part 100 of the apparatus for producing titanium tetrachloride according to an embodiment of the present invention may further include a traveling path 130 and a second temperature controller 140.

The transfer passage 130 may be branched so that one end thereof communicates with the inner space 111 and the other end thereof is connected to the first condenser 200 and the second condenser 300.

The first product and the second product generated from the reaction part 100 may be communicated with the inner space 111 so as to be moved through the transfer path 130. [ The other end may communicate with the space inside the first condensing part 200 so that the first product and the second product are moved to the first condensing part 200.

The second temperature regulator 140 is disposed outside the transfer path 130 and can maintain the temperature inside the transfer path 130 at 700 ° C to 800 ° C.

The temperature inside the traveling path 130 is increased to 700 through the second temperature regulator 140 to move the first product and the second product to the first condensing part 200 while being maintained in the vapor phase through the moving path 130 Deg.] C to 800 [deg.] C.

The temperature at which the iron chloride in the first product can maintain the gaseous phase may be sufficient.

The reaction part 100 of the apparatus for producing titanium tetrachloride according to an embodiment of the present invention may further include a hopper 150, a gas feeder 160, and a carbon source feeder 170.

The hopper 150 is connected to the upper part of the reaction body 110 and can supply ore into the internal space 111. The ore containing iron and titanium may be charged from the hopper 150 to the upper part of the reaction body 110 and stacked from the lower part of the inner space 111.

The gas feeder 160 is connected to the lower portion of the reaction body 110 and can supply chlorine or an inert gas to the internal space 111.

The gas supplier 160 may supply chlorine from the lower portion of the reaction body 110 to the inner space 111 to cause chlorination reaction with iron and titanium of the ore. Meanwhile, the gas feeder 160 may blow an inert gas such as nitrogen (N ₂ ) into the inner space 111. The first product and the second product in the gaseous phase can be moved to the first condenser 200 by being blown from the bottom of the reaction body 110. Further, the second product in the gaseous phase after the condensation of the first product in the first condenser 200 can be moved to the second condenser 300.

The carbon source supplier 170 is connected to the upper part of the reaction body 110 and can supply the carbon source to the inner space 111. The carbon source feeder 170 may charge the carbon source of the carbon source from the upper portion of the reaction body 110 into the internal space 111 so that the oxygen present in the ore may react with the carbon.

The reaction part 100 of the titanium tetrachloride production system according to an embodiment of the present invention may further include a supply path 180 and a control valve 190.

The supply path 180 can communicate the gas supply unit 160 and the internal space 111. The gas feeder 160 and the reaction body 110 are connected to each other through the feed path 180 so that chlorine or an inert gas can be introduced into the inner space 111 along the feed path 180.

The regulating valve 190 is installed on the supply path 180 and is capable of interrupting the flow of chlorine or inert gas.

By controlling the flow rate of chlorine through the opening and closing of the control valve 190 provided on the supply path 180, the first chlorination reaction and the second chlorination reaction are induced for a sufficient time for the iron and the titanium of the ore to react with chlorine can do. Further, the flow of the inert gas may be controlled to induce the movement of the first product and the second product to the first condenser 200. Also, the movement of the second product to the second condenser 300 can be induced.

The first condenser 200 of the apparatus for producing titanium tetrachloride according to an embodiment of the present invention is connected to the transfer path 130 and has a first condensation space 211 formed therein for condensing the first product, 250 < 0 > C.

The first product and the second product may be moved along the path 130 connected to the reaction part 100 at one end and connected to the first condensing part 200 at the other end. The first condensing space 211 may be provided in the first condensing part 200 and the first condensing space 211 may communicate with the inner space 111 via the moving path 130.

The gaseous iron in the gaseous phase contained in the first product may be changed to a liquid phase at a temperature of about 250 ° C or lower and may change to a solid phase at 20 ° C to 250 ° C.

The first condensation space 211 is maintained at 20 ° C to 250 ° C such that at least the first product of the first product and the second product in the gaseous phase, such as FeCl ₂ and FeCl ₃ , can condense into a solid phase. Therefore, it is possible to collect the iron chloride condensed in the solid phase in the first condensing space 211.

Temperatures at which the iron chloride can be maintained in the solid phase may be sufficient.

The first condenser 200 of the apparatus for producing titanium tetrachloride according to an embodiment of the present invention may include a first condenser main body 210, a first condenser furnace 220 and a first opening / closing valve 230.

The first condensing body 210 may have a first condensing space 211 therein. Accordingly, the condensation of the first product among the first product and the second product in the first condensing space 211 can be performed first.

The first condensing passage 220 can communicate the moving passage 130 and the first condensing space 211 with each other. One end of the first condensing passage 220 is connected to the moving passage 130 and the other end of the first condensing passage 220 is connected to the first condensing main body 210 so that the moving passage 130 and the first condensing space 211 can communicate with each other.

The first opening and closing valve 230 is installed on the first condensing passage 220 and can interrupt the entry and exit of the first product and the second product. More specifically, while the first chlorination reaction and the second chlorination reaction proceed in the inner space 111, the first opening / closing valve 230 is opened to move the first product and the second product to the first condensation main body 210 . The first opening and closing valve 230 is closed during the first chlorination reaction and the second chlorination reaction in the inner space 111 and then the first opening and closing valve 230 is closed after the first chlorination reaction and the second chlorination reaction progresses To open the first and second products to the first condensing body 210.

The first condenser 200 of the apparatus for producing titanium tetrachloride according to an embodiment of the present invention may further include a third temperature controller 240.

The third temperature regulator 240 is disposed outside the first condensing passage 220 and can maintain the temperature inside the first condensing passage 220 at 700 ° C to 800 ° C.

The temperature inside the first condensing passage 220 is changed to 700 through the third temperature regulator 240 so that the first product is maintained in the vapor phase via the first condensing passage 220 and is moved to the first condensing section 200. [ Deg.] C to 800 [deg.] C. The first product is moved to the first condensing space 211 while maintaining the gaseous state.

The temperature at which the iron chloride in the first product can maintain the gaseous phase may be sufficient.

The second condensing part 300 of the apparatus for producing titanium tetrachloride according to an embodiment of the present invention is connected to the first condensing body 210 and the second condensing space 311 formed therein for condensing the second product is connected to the Lt; 0 > C or less.

The second condenser 300 may be connected to the first condenser 200 so that the gaseous second product not condensed in the first condenser 200 may be moved to the second condenser 300. The second condensing space 311 may be provided in the second condensing unit 300 and the second condensing space 311 may communicate with the first condensing space 211. [

The gaseous titanium tetrachloride contained in the second product may be changed into a liquid state at 20 ° C or lower.

The second condensation space 311 is maintained at 20 ° C or lower so that at least titanium tetrachloride can be condensed into a liquid phase in the second product of the vapor phase. Therefore, in the second condensing space 311, the titanium tetrachloride condensed in the liquid phase can be collected.

The temperature at which the titanium tetrachloride can maintain the liquid phase may suffice.

The second condenser 300 of the apparatus for producing titanium tetrachloride according to an embodiment of the present invention may include a second condenser body 310, a storage device 320, and a second condenser 330.

The second condensing part 300 may have a second condensing space 311 therein. Condensation of the second product in the second condensing space 311 can thus be achieved.

The reservoir 320 is connected to the second condensing body 310 and can store the condensed second product in the second condensing body 310.

Preferably, the reservoir 320 may be connected to the lower portion of the second condensing body 310. Also, the space formed inside the storage unit 320 can communicate with the second condensation space 311. Accordingly, the second product condensed in the liquid state in the second condensing space 311 falls into the space formed in the storage unit 320 by its own weight, and the second product can be stored in the storage unit 320.

The second condensing passage (330) can communicate the first condensing space (211) and the second condensing space (311). The second condensing passage 330 has one end connected to the first condensing main body 210 and the other end connected to the second condensing main body 310 to communicate the first condensing space 211 and the second condensing space 311 .

The second on-off valve 340 is installed on the second condensing passage 330 and can interrupt the entry and exit of the second product. More specifically, the second on-off valve 340 is opened to move the second product according to the second chlorination reaction from the first condensing main body 210 to the second condensing main body 310, close the second on-off valve 340 The movement of the first product to the second condensing body 310 due to the first chlorination reaction may be disallowed.

Referring to FIG. 2, an apparatus for producing titanium tetrachloride according to an embodiment of the present invention may further include a purification unit 400.

The purifier 400 is connected to the second condenser 300 and the condensed second product can be purified. Accordingly, it may be possible to obtain titanium tetrachloride of high purity.

And may be connected to the storage device 320 constituting the second condenser 300. The second product in the liquid phase condensed from the storage device 320 is moved to the purification part 400 and the second product can be vaporized again by application of high temperature heat. As the second product in the gaseous phase passes through the multi-stage vapor column, impurities are removed and ultimately high purity titanium tetrachloride can be obtained.

The operation of the titanium tetrachloride production apparatus according to one embodiment of the present invention will be described with reference to FIGS. 1 and 2. FIG.

Ore containing iron and titanium may be charged into the inner space 111 of the reaction body 110 through the hopper 150. Preferably, the ore can be activated in an atmosphere where the temperature is maintained at 800 ° C to 1100 ° C through the first temperature controller 120.

In addition, chlorine is supplied to the inner space 111 of the reaction body 110 through the gas feeder 160, and the carbon source can be supplied through the carbon source feeder 170.

The reaction of ores, chlorine and carbon sources can be effected at a temperature of 800 ° C to 1100 ° C for a time sufficient to allow both iron and titanium in the ore to react with chlorine. First, the iron chloride ore may react with chlorine and a carbon source as shown in the formulas (1) and (2) to produce a first chlorination-containing first product. Next, a reaction with the precipitate remaining in the inner space 111 can be performed. The titanium chloride of the precipitate may be reacted with chlorine and the carbon source as shown in the above formulas (3) and (4) to proceed the second chlorination reaction in which a second product containing titanium tetrachloride is produced.

The first product and the second product in the gaseous phase are present in the inner space 111 according to the reactions of the formulas (1) to (4) in the reaction body 110.

While the first chlorination reaction and the second chlorination reaction proceed in the inner space 111, the first opening and closing valve 230 may be opened to move the first product and the second product to the first condensation body 210. Closing valve 230 is closed during the first chlorination reaction and the second chlorination reaction in the inner space 111 and then the first opening and closing valve 230 is closed after the first chlorination reaction and the second chlorination reaction progresses, The first product and the second product may be moved to the first condensing body 210.

The second on-off valve 340 may be closed while the first product is being condensed in the first condensing space 211. Thereby minimizing movement of the first product to the second body.

The first product and the second product can be moved into the first condensation space 211 of the first condensation body 210 along the transfer path 130 and the first condensation path 220. In the case of the transfer path 130, the temperature is maintained at 700 ° C. to 800 ° C. through the second temperature regulator 140 so that the first product can maintain the gaseous state.

The temperature of the first condensing space 211 can be maintained at 20 to 250 ° C. At 20 ° C to 250 ° C, the iron chloride of at least the first product of the first product and the second product may condense to a solid phase.

The uncompacted second product may move from the first condensing space 211 to the second condensing space 311 of the second condensing body 310 along the second condensing path 330.

The temperature of the second condensing space 311 can be maintained at 20 ° C or lower. The titanium tetrachloride of at least the second product can be condensed into a liquid phase at a temperature of 20 DEG C or lower. The condensed second liquid product may be transferred to and stored in the reservoir 320.

The liquid second product is transferred from the storage unit 320 to the purification unit 400, and is vaporized again, and then, through the multi-stage purification tower, high purity titanium tetrachloride can be obtained.

Hereinafter, effects of the selective chlorination reaction according to the present invention will be described with reference to Experimental Examples and Comparative Examples. These experimental examples are only for illustrating the present invention, and the present invention is not limited thereto.

Experimental Example

The ore, chlorine and carbon source containing iron and titanium were fed in the reaction part maintained at 950 ℃ for about 240 minutes.

Then, the temperature of the first condensation body, in which the first product and the second product generated by the reaction were collected, was maintained at 200 ° C to control the first product to a solid state and the second product to a gaseous state.

The second product of the vapor phase was transferred to the second condensation body and was then collected at below 20 ° C to examine the components. Components of the first product and the second product are shown in Tables 1 and 2 below, respectively.

Component (wt%) MnO FeO _x FeCl ₃ The first product 3.3 0.30 96.40

Component (ppm) Li Be Mg Al P Ca V Cr Mn Fe Co Ni Ti The second product One One 16 44 One 8 826 14 5 680 One 71 Remainder

In Table 1, it can be seen that most of the components are composed of FeCl ₃ as the first product.

Table 2 shows the remaining chlorides by discharging all chlorine and the like by purge of nitrogen gas. It can be seen that most of them are made of titanium tetrachloride, which is Ti chloride, except metal chlorides which are treated as impurities. It can be confirmed that no iron component was present in the second product except for a small amount of Fe chloride.

The iron chloride and titanium tetrachloride obtained per kg of ore were 1.08 kg and 1.12 kg, respectively. Each of which is separately collected in the first condenser and the second condenser.

Comparative Example

The ore, chlorine, and carbon source containing iron and titanium were fed to an arbitrary space maintained at a temperature of 950 ° C and reacted for about 30 minutes.

The product was then collected by the reaction and the components were investigated. The components of the product are shown in Tables 3 and 4 below.

Component (wt%) CaO FeCl ₃ TiO ₂ FeO _x MgO Al ₂ O ₃ product 0.4 54.4 24.7 19.3 1.1 1.1

Component (ppm) Li Be Mg Al P Ca V Cr Mn Fe Co Ni Ti product One One 160 120 6 One 1890 34 3 6700 One 3 Remainder

Table 3 shows the product by reaction, and the components of the residue are shown separately in Table 4.

The amount of collected iron chloride and titanium tetrachloride was comparable or less than that of the experimental examples. Further, unlike the experimental example in which iron chloride and titanium tetrachloride can be obtained in a separated state and the production process can be shortened, chloride and titanium tetrachloride are not separately collected in the comparative example.

While the present invention has been particularly shown and described with reference to specific embodiments thereof, it will be understood by those skilled in the art that various changes in form and details may be made therein without departing from the spirit and scope of the invention as defined by the following claims It will be apparent to those of ordinary skill in the art.

100: Reaction part 110: Reaction body
111: internal space 120: first temperature regulator
130: transfer path 140: second temperature regulator
150: hopper 160: gas feeder
170: Carbon source feeder 180: Feeder
190: regulating valve 200: first condenser
210: first condensing body 211: first condensing space
220: first condensing furnace 230: first opening / closing valve
240: third temperature regulator 300: second condenser
310: second condensing body 311: second condensing space
320: Storage device 330: Second condensation furnace
340: second opening / closing valve 400:

Claims (11)

Ores containing iron and titanium; Goat; And a carbon source to produce a first product containing iron chloride and a precipitate containing titanium, wherein the precipitate; Goat; And a carbon source to produce a second product containing titanium tetrachloride;
A first condenser connected to the reaction unit and selectively condensing the first product among the first product and the second product moved from the reaction unit; And
And a second condensing part connected to the first condensing part and condensing the second product moved from the first condensing part,
The reaction unit may include the ore; Goat; And a carbon source; And a moving path having one end communicated with the internal space and the other end connected with the first condensing portion,
Wherein the first condensing portion includes: a first condensing body having a first condensing space in which the first product is condensed; A first condensing passage for communicating the moving passage and the first condensing space; And a first opening / closing valve installed on the first condensing passage for interrupting entrance / exit of the first product and the second product. The method according to claim 1,
The reaction unit includes:
And a first temperature controller disposed outside the reaction body and maintaining the temperature of the internal space at 800 ° C to 1100 ° C. The method according to claim 1,
The reaction unit includes:
And a second temperature controller disposed outside the traveling path for maintaining a temperature inside the traveling path at 700 ° C to 800 ° C. The method of claim 2,
The reaction unit includes:
A hopper connected to an upper portion of the reaction body and providing the ore to the inner space;
A gas supplier connected to a lower portion of the reaction body and supplying chlorine or an inert gas to the internal space; And
And a carbon source supplier connected to an upper portion of the reaction body and supplying a carbon source to the inner space. The method of claim 4,
The reaction unit includes:
A supply passage communicating the gas supply unit and the inner space; And
And a control valve installed on the supply path for controlling the entry and exit of chlorine or an inert gas. The method according to claim 1,
Wherein the first condenser comprises:
Wherein the first condensing space is maintained at 20 占 폚 to 250 占 폚. delete The method according to claim 1,
Wherein the first condenser comprises:
And a third temperature controller disposed outside the first condensing furnace and maintaining the temperature inside the first condensing furnace at 700 ° C to 800 ° C. The method according to claim 1,
Wherein the second condenser comprises:
Wherein the second condensing space is formed inside the first condensing body so that the second product is condensed. The method of claim 9,
Wherein the second condenser comprises:
A second condensing main body having the second condensing space therein;
An accumulator coupled to the second condensing body and storing the condensed second product in the second condensing body;
A second condensing passage for communicating the first condensing space and the second condensing space; And
And a second on-off valve installed on the second condensing passage for controlling the entry and exit of the second product. The method according to claim 1,
And a refining unit connected to the second condensing unit and configured to refine the condensed second product.

Images