CN107963653B - Gradient control method for temperature of molten salt chlorination system - Google Patents
Gradient control method for temperature of molten salt chlorination system Download PDFInfo
- Publication number
- CN107963653B CN107963653B CN201711377251.1A CN201711377251A CN107963653B CN 107963653 B CN107963653 B CN 107963653B CN 201711377251 A CN201711377251 A CN 201711377251A CN 107963653 B CN107963653 B CN 107963653B
- Authority
- CN
- China
- Prior art keywords
- dust collector
- salt chlorination
- titanium tetrachloride
- slurry
- chlorination furnace
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01G—COMPOUNDS CONTAINING METALS NOT COVERED BY SUBCLASSES C01D OR C01F
- C01G23/00—Compounds of titanium
- C01G23/02—Halides of titanium
- C01G23/022—Titanium tetrachloride
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Life Sciences & Earth Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- General Life Sciences & Earth Sciences (AREA)
- Geology (AREA)
- Inorganic Chemistry (AREA)
- Electrolytic Production Of Metals (AREA)
- Manufacture And Refinement Of Metals (AREA)
Abstract
A temperature gradient control method of a molten salt chlorination system adopts the molten salt chlorination temperature gradient control system and comprises a molten salt chlorination furnace and a temperature gradient control system 1#Dust collector, 2#Dust collector, 1#Titanium tetrachloride leaching tower, 1#TetrachloroTitanium dioxide leaching circulation tank, return molten salt chlorination furnace slurry control valve and return flow 1#Dust collector slurry control valve and return 2#The mud control valve of the dust collector controls the outlet temperature of the fused salt chlorination furnace of the fused salt chlorination temperature gradient control system to be 450-650 ℃ and 1 ℃ in the production process#The outlet temperature of the dust collector is 350-400 ℃ and 2#The outlet temperature of the dust collector is 180-230 ℃. The advantages are that: simple process, easy operation make high boiling point chloride impurity can in time discharge system in the gas that molten salt chlorination furnace reaction produced, prevent impurity chloride excessive deposit in the system.
Description
Technical Field
The invention relates to a gradient control method for the temperature of a molten salt chlorination system.
Background
The large-scale molten salt chlorination production system is already in domestic industrial production. In the production of molten salt chlorination, a molten salt chlorination furnace is a main reaction generating device and has the function that under the condition that high titanium slag exists in a molten salt medium and a reducing agent (carbon), chlorine gas chloridizes titanium oxide and other oxides in the high titanium slag into chloride, and the main component of furnace gas of the chlorine gas is TiCl4、AlCl3、FeCl3And removing most chloride impurities through a dust collection process, and obtaining a liquid titanium tetrachloride product through a leaching processAnd (5) preparing the product. When the productivity of the molten salt chlorination furnace is improved to 130t/d-150t/d, the purification of the high-temperature titanium tetrachloride gas containing impurities generated by the molten salt chlorination furnace is very critical in the production operation process of the molten salt chlorination system. In order to purify titanium tetrachloride gas and reduce the backward movement of impurity chlorides, it is necessary to control the temperature of high-boiling-point impurity chloride-containing high-temperature titanium tetrachloride gas generated by a molten salt chlorination furnace reaction, so as to effectively remove impurities in the titanium tetrachloride gas. If not take effective measure or control effect not good, high boiling point chloride impurity discharge system in time, impurity chloride can deposit in the system, reaches after the certain degree, can make the system pipeline block up, causes system pressure shakiness, or excessive sedimentary impurity chloride can drop naturally to the dust arrester jar of dust arrester in, and when the impurity chloride who drops was bulky, it breaks away from the drop from the dust arrester to cause the dust arrester jar easily. When the titanium recovery rate is serious, the system needs to be stopped for cleaning, so that the titanium recovery rate is reduced, the energy consumption is increased, and the cost is increased.
Disclosure of Invention
The technical problem to be solved by the invention is to provide the molten salt chlorination system temperature gradient control method capable of effectively removing impurity chlorides of the chlorination gas of the molten salt chlorination furnace in the process of producing titanium dioxide by the molten salt chlorination method, the process is simple and easy to operate, high-boiling-point chloride impurities in the gas generated by the reaction of the molten salt chlorination furnace can be timely discharged out of the system, and the impurity chlorides are prevented from being excessively deposited in the system.
The technical scheme adopted by the invention is as follows:
gradient control method for temperature of molten salt chlorination system, and gradient control system for temperature of molten salt chlorination 1#The solid content of the crude titanium tetrachloride slurry in the leaching circulation tank is less than or equal to 30 percent, the temperature is less than or equal to 130 ℃, and the crude titanium tetrachloride slurry is placed in a fused salt chlorination furnace 1#Dust collector and 2#The tower top of the dust collector is provided with liquid mud sprayed by an atomizing nozzle 1#Atomizing nozzle of dust collector and 2#The atomizing nozzle of the dust collector sprays liquid slurry by introducing nitrogen gas 1#The crude titanium tetrachloride slurry in the leaching circulation tank is sprayed to a fused salt chlorination furnace 1 through a slurry return pump, a pipeline and an atomizing nozzle#Dust collector and 2#The dust collector is characterized in that mass transfer and heat transfer are carried out on liquid slurry sprayed by the atomizing nozzle and reaction gas generated by the reaction of the molten salt chlorination furnace, the reaction gas is cooled, and high-boiling-point impurities (ferric trichloride, manganese dichloride and the like) in the reaction gas are changed into solid and are retained in the chlorination furnace and the chlorination furnace 1#Dust collector and 2#The titanium tetrachloride in the sprayed slurry is heated and gasified and enters into the reaction gas, and the solid impurities in the slurry are retained in the chlorination furnace and the reaction gas 1#Dust collector and 2#Removing in a dust collector; in the course of returning coarse titanium tetrachloride mud, the opening of the valve is controlled, and the valve is adjusted to enter a fused salt chlorination furnace 1#Dust collector and 2#The amount of mud in the dust collector is such that the outlet of the fused salt chlorination furnace is 1#Dust collector and 2#The temperature of the dust collector is stable; in the production process, the outlet temperature of the chlorination furnace is controlled to be 450-650 ℃ and 1#The outlet temperature of the dust collector is 350-400 ℃ and 2#The outlet temperature of the dust collector is 180-230 ℃.
Further, the molten salt chlorination temperature gradient control system comprises a molten salt chlorination furnace and a system 1#Titanium tetrachloride Leaching circulation tank, 1#The slurry outlet of the titanium tetrachloride leaching circulation tank is communicated with the fused salt chlorination furnace through a pipeline at 1#A pipeline between the titanium tetrachloride leaching circulation tank and the fused salt chlorination furnace is provided with a slurry pump returning titanium tetrachloride, and the outlet of the slurry pump returning titanium tetrachloride is connected with a pump 1 through a pipeline#Titanium tetrachloride leaching tower; the fused salt chlorination furnace is sequentially connected with 1 through a pipeline#Dust collector, 2#Dust collector and 1#Titanium tetrachloride leaching tower; 1 is described#Outlet at bottom of titanium tetrachloride leaching tower and 1#The slurry inlets of the titanium tetrachloride leaching circulation tank are communicated through pipelines; in a fused salt chlorination furnace, 1#Dust collector, 2#A slurry inlet pipeline of the dust collector is respectively provided with a slurry return control valve of the fused salt chlorination furnace and a slurry return 1#Dust collector slurry control valve and return 2#The outlet pipeline of the fused salt chlorination furnace is provided with a fused salt chlorination furnace outlet temperature meter T1, 1#An outlet pipeline of the dust collector is provided with a pipe 1#Dust collector outlet thermometer T2, 2#An outlet pipeline of the dust collector is provided with 2#Dust collector outlet temperature T3; in 1#Dust collector, 2#The inlet of the dust collector is also connected with a nitrogen inlet pipeline.
Furthermore, the auxiliary (atomization) nitrogen pressure is kept between 0.2MPa and 0.5 MPa.
Further, control goes to 1#Titanium tetrachloride leaching tower titanium tetrachloride-containing slurry amount and pumping excess 1#Titanium tetrachloride-containing mud control 1 in leaching circulation tank#The liquid level of the leaching circulation tank is stabilized at 1 m-1.1 m.
Further, the outlet pressure of the slurry pump is controlled to be 1.2MPa to 1.5MPa, and the flow is controlled to be 80m3/h～100m3/h。
The invention has the beneficial effects that: the process is simple and easy to operate, high-boiling-point chloride impurities in gas generated by the reaction of the molten salt chlorination furnace can be discharged out of the system in time, the impurity chlorides are prevented from being excessively deposited in the system, the fouling thermal resistance of a heat exchanger of a titanium tetrachloride leaching system is effectively reduced, the system pressure is stable, and the smoke is extremely less excessive. The production period of a titanium tetrachloride leaching system is prolonged, the titanium recovery rate is improved, and the production cost and potential safety hazards are reduced.
Drawings
FIG. 1 is a schematic diagram of a molten salt chlorination temperature gradient control system of the present invention;
in the figure: fused salt chlorination furnace 1#Dust collector 2#Dust collector 3, 1#Titanium tetrachloride leaching tower 1#Titanium tetrachloride leaching circulation tank, slurry pump returning titanium tetrachloride, slurry control valve returning molten salt chlorination furnace and 1#Dust collector mud control valve 2#Dust collector slurry control valve ninthly, fused salt chlorination furnace outlet temperature T1, 1#Dust collector outlet temperature T2, 2#Dust collector outlet temperature T3.
Detailed Description
Examples
As shown in the figure, the molten salt chlorination temperature gradient control system comprises a molten salt chlorination furnace (1)#Titanium tetrachloride leaching cycleGroove (c 1)#The slurry outlet of the titanium tetrachloride leaching circulation tank is communicated with the fused salt chlorination furnace 1 through a pipeline#A slurry pump containing titanium tetrachloride is arranged on a pipeline between the titanium tetrachloride leaching circulation tank and the molten salt chlorination furnace, and an outlet of the slurry pump containing titanium tetrachloride is also connected with a pipeline 1#Titanium tetrachloride leaching tower IV; the fused salt chlorination furnace is connected with a furnace 1 in sequence through a pipeline#Dust collector 2#Dust collector 3 and 1#Titanium tetrachloride leaching tower IV; 1 is described#Outlet at bottom of titanium tetrachloride leaching tower and 1#The slurry inlets of the titanium tetrachloride leaching circulation tank are communicated through pipelines; in a molten salt chlorination furnace 1#Dust collector 2#A slurry inlet pipeline of the dust collector (c) is respectively provided with a slurry return control valve (c) of the fused salt chlorination furnace (c) and (c) 1#Dust collector mud control valve 2#A dust collector mud control valve, wherein an outlet pipeline of the fused salt chlorination furnace is provided with a fused salt chlorination furnace outlet temperature meter T1, 1#An outlet pipeline of the dust collector II is provided with 1#Dust collector outlet thermometer T2, 2#An outlet pipeline of the dust collector (c) is provided with 2#Dust collector outlet temperature T3; in 1#Dust collector 2#And a mud inlet of the dust collector III is also connected with a nitrogen inlet pipeline.
In a fused salt chlorination furnace, 1#Dust collectors 2 and 2#The dust collector and the liquid mud sprayed by the atomizing nozzle arranged at the top part 1#Atomizing nozzle of dust collector and 2#The atomizing nozzle of the dust collector leads the atomizing nozzle to spray liquid slurry by introducing nitrogen;
in production, 1#The temperature of the coarse titanium tetrachloride slurry in the titanium tetrachloride leaching circulation tank is less than or equal to 130 ℃, and the coarse titanium tetrachloride slurry is respectively pumped into a fused salt chlorination furnace (I) and a fused salt chlorination furnace (1) under the action of a slurry pump (II) which returns titanium tetrachloride#Dust collectors 2 and 2#In the dust collector, reaction gas generated by the reaction of the fused salt chlorination furnace and crude titanium tetrachloride slurry are subjected to mass transfer and heat transfer in the fused salt chlorination furnace, and the reaction gas is cooled to ensure that high-boiling-point impurities (III) in the reaction gasFerric chloride, manganese dichloride and the like) into solid and remain at the bottom of the first fused salt chlorination furnace, titanium tetrachloride in the sprayed crude titanium tetrachloride slurry is heated and gasified and enters into reaction gas, and solid impurities remain at the bottom of the first fused salt chlorination furnace; the reaction gas enters 1 from a fused salt chlorination furnace#Dust collector II, reacting gas and coarse titanium tetrachloride slurry in 1#Solid impurities are left 1 after mass transfer and heat transfer in the dust collector II#Dust collector bottom, reaction gas from 1#Dust collector 2#In the dust collector (c), the reaction gas and the coarse titanium tetrachloride slurry are in a range of 2#Solid impurities are left in the dust collector 2 after mass transfer and heat transfer#Dust collector bottom, reaction gas entering 1#Titanium tetrachloride leaching tower IV; pumping coarse titanium tetrachloride slurry into a slurry pump (1)#Titanium tetrachloride leaching tower (2) for spraying#Dust collector (III) enters into 1#Reaction gas of a titanium tetrachloride leaching tower IV;
in the process of returning coarse titanium tetrachloride mud, the mud control valve of the molten salt chlorination furnace is controlled to return to 1 and seventh#Dust collector mud control valve 2#The opening degree of the mud control valve of the dust collector is adjusted to enter the fused salt chlorination furnace 1#Dust collectors 2 and 2#The amount of mud in the dust collector leads the outlet of the fused salt chlorination furnace to be 1#Dust collector outlet 2#The outlet temperature of the dust collector is stable;
introduction of 1#Dust collectors 2 and 2#Nitrogen in the dust collector guarantees the atomization effect of slurry and ensures the sufficient mass and heat transfer in the system; 1#The solid content of titanium tetrachloride slurry in the titanium tetrachloride leaching circulation tank is controlled to be less than or equal to 30 wt%, so that the pipeline of the system is prevented from being blocked.
Under the normal production condition, the slurry pump containing titanium tetrachloride is started, the outlet pressure is controlled to be 1.2MPa to 1.5MPa, and the flow is controlled to be 80m3/h～100m3H; control introduction of 1#Dust collectors 2 and 2#The pressure of nitrogen in the dust collector (c) is 0.2-0.5 MPa, a slurry control valve of the molten salt chlorination furnace is opened, and the opening of a valve is adjusted according to the outlet temperature T1 of the molten salt chlorination furnaceControlling the outlet temperature T1 of a chlorination furnace to be 450-650 ℃; opening return 1#Dust collector mud control valve (1)#Dust collector outlet temperature T2 regulating valve opening degree, control 1#The outlet temperature T2 of the dust collector II is 350-400 ℃; opener return 2#Mud control valve of dust collector according to 2#Dust collector and outlet temperature T3 regulating valve opening, control 2#And the outlet temperature T3 of the dust collector is 180-230 ℃.
Example 1
As shown in figure 1, a molten salt chlorination temperature gradient control system is adopted, under the normal production condition, a slurry pump returning titanium tetrachloride is started, the outlet pressure is controlled to be 1.5MPa, and the flow is controlled to be 100m3H; control introduction of 1#Dust collectors 2 and 2#The nitrogen pressure of the dust collector (c) is 0.5MPa, a slurry control valve of the molten salt chlorination furnace is opened, the opening of a valve is adjusted according to the outlet temperature T1 of the molten salt chlorination furnace, and the outlet temperature T1 of the molten salt chlorination furnace is controlled to be 450-500 ℃; opening return 1#Dust collector mud control valve (1)#Dust collector outlet temperature T2 regulating valve opening degree, control 1#The outlet temperature T2 of the dust collector is 350-370 ℃; opener return 2#Mud control valve of dust collector according to 2#Dust collector and outlet temperature T3 regulating valve opening, control 2#The outlet temperature T3 of the dust collector is 180-200 ℃.
Example 2
As shown in figure 1, a molten salt chlorination temperature gradient control system is adopted, under the normal production condition, a slurry pump returning titanium tetrachloride is started, the outlet pressure is controlled to be 1.2MPa, and the flow is controlled to be 80m3/h m3H; control introduction of 1#Dust collectors 2 and 2#The nitrogen pressure of the dust collector (c) is 0.2MPa, a slurry control valve of the molten salt chlorination furnace is opened, the opening of the valve is adjusted according to the outlet temperature T1 of the molten salt chlorination furnace, and the outlet temperature T1 of the molten salt chlorination furnace is controlled to be 600-650 ℃; opening return 1#Dust collector and slurry control valve (1)#Dust collector outlet temperature T2 regulating valve opening degree, control 1#The outlet temperature T2 of the dust collector is 380-400 ℃; opener return 2#Dust collector and mud control valve according to 2#Dust collector and outlet temperature T3 regulating valve opening, control 2#The outlet temperature T3 of the dust collector is 210-230 ℃.
Example 3
As shown in figure 1, a molten salt chlorination temperature gradient control system is adopted, under the normal production condition, a slurry pump returning titanium tetrachloride is started, the outlet pressure is controlled to be 1.4MPa, and the flow is controlled to be 90m3H; control introduction of 1#Dust collectors 2 and 2#The nitrogen pressure of the dust collector (c) is 0.3MPa, a slurry control valve of the molten salt chlorination furnace is opened, the opening of the valve is adjusted according to the outlet temperature T1 of the molten salt chlorination furnace, and the outlet temperature T1 of the molten salt chlorination furnace is controlled to be 500-550 ℃; opening return 1#Dust collector mud control valve (1)#The opening of an adjusting valve for the outlet temperature T2 of the dust collector is controlled to be 1#The outlet temperature T2 of the dust collector is 370-380 ℃; opener return 2#Mud control valve of dust collector according to 2#The opening of an adjusting valve for the outlet temperature T3 of the dust collector is controlled to be 2#The outlet temperature T3 of the dust collector is 200-220 ℃.
Comparative example 1
As shown in figure 1, a molten salt chlorination temperature gradient control system is adopted, and a return 1 is closed#A mud control valve of the dust collector is opened, a mud pump returning titanium tetrachloride is started, the outlet pressure is controlled to be 1.4MPa, and the flow is controlled to be 90m3H; control introduction of 1#Dust collectors 2 and 2#The pressure of nitrogen in the dust collector (c) is 0.3MPa, a slurry control valve of the molten salt chlorination furnace is opened, the opening of the valve is adjusted according to the outlet temperature T1 of the molten salt chlorination furnace, and the outlet temperature T1 of the molten salt chlorination furnace is controlled to be 650-700 ℃; opener return 2#Mud control valve of dust collector according to 2#The opening of an adjusting valve for the outlet temperature T3 of the dust collector is controlled to be 2#The outlet temperature T3 of the dust collector is 200-220 ℃.
In industrial production, sampling is carried out for 1 time every 8 hours, solid content is analyzed, and 1 is adjusted according to the analysis result#The solid content in the titanium tetrachloride leaching circulation tank is less than or equal to 30 percent, the molten salt chlorination furnace discharges waste salt once every 24 hours, and a salt sample is taken for analysis; when the slag amount in the dust collecting slag tank reaches 80 percentAnd discharging slag and taking a slag sample for analysis. The comparative results before and after the operation according to the method are analyzed as follows:
TABLE 1 comparison of slag tapping
TABLE 2 comparative analysis (wt%) of the slag sample
TABLE 3 comparative analysis (wt%) of waste salt sample
| FeCl2 | MnCl2 | NaCl | ΣTi | C | SiO2 | Water insoluble substance | |
| Example 3 | 6.37 | 8.18 | 29.5 | 0.74 | 6.57 | 1.36 | 18.75 |
| Comparative example 1 | 4.57 | 6.42 | 28.11 | 1.04 | 25.06 | 2.08 | 31.94 |
According to the comparison of the sampling analysis data, after the method is operated, the impurity content in the waste salt discharged by the fused salt chlorination furnace is increased, the total slag amount of the dust collector is increased, so that the impurity content of the reaction gas of the fused salt chlorination furnace is reduced, and 1#The operation period of the titanium tetrachloride leaching circulation tank is prolonged to be more than 3 months, the recovery rate of the titanium of the system is increased, and the cost is reduced.
By adopting the operation methods of the example 1 and the example 2, compared with the comparative example 1, the results are the same as the example 3, the impurity content in the waste salt discharged by the fused salt chlorination furnace is increased, the total slag amount of the dust collector is increased, the impurity content of the reaction gas of the fused salt chlorination furnace is reduced, 1#The operation period of the titanium tetrachloride leaching circulation tank is prolonged, the recovery rate of the titanium of the system is increased, and the cost is reduced.
The above description is only exemplary of the present invention and is not intended to limit the present invention, and various modifications and changes may be made by those skilled in the art. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (4)
1. A temperature gradient control method of a molten salt chlorination system is characterized by comprising the following steps: molten salt chlorination temperature gradient control system 1#The solid content of the crude titanium tetrachloride slurry in the titanium tetrachloride leaching circulation tank is less than or equal to 30 percent, the temperature is less than or equal to 130 ℃, and the crude titanium tetrachloride slurry is placed in a molten salt chlorination furnace 1#Dust collector and 2#The dust collector slurry inlet is provided with an atomizing nozzle for spraying liquid slurry, 1#Atomizing nozzle of dust collector and 2#The atomizing nozzle of the dust collector sprays liquid slurry by introducing nitrogen gas 1#Coarse titanium tetrachloride slurry in the leaching circulation tank is sprayed to a fused salt chlorination furnace 1 through a titanium tetrachloride slurry returning pump, a pipeline and an atomizing nozzle#Dust collector and 2#The dust collector controls a slurry control valve of the molten salt chlorination furnace to return to 1 in the process of returning coarse titanium tetrachloride slurry#Dust collector mud control valve, Return 2#The opening of a mud control valve of a dust collector is adjusted to enter a fused salt chlorination furnace 1#Dust collector and 2#The amount of mud in the dust collector is such that the outlet of the fused salt chlorination furnace is 1#Dust collector and 2#The temperature of the dust collector is stable; in the production process, 1#The temperature of the titanium tetrachloride-containing mud in the leaching circulation tank is less than or equal to 130 ℃; 1#Dust collector and 2#The nitrogen gas feeding pressure of the dust collector is controlled to be 0.2MPa ~ 0.5.5 MPa, the outlet temperature of the chlorination furnace is controlled to be 450 ℃, ~ 650 ℃, 1 DEG C#Outlet temperature of dust collector 350 deg.C ~ 400 deg.C 2#The outlet temperature of the dust collector is 180 ℃ and ~ 230 ℃ respectively.
2. The molten salt chlorination system temperature gradient control method of claim 1, which is characterized by comprising the following steps: the molten salt chlorination temperature gradient control system comprises a molten salt chlorination furnace and a molten salt chlorination furnace 1#Titanium tetrachloride Leaching circulation tank, 1#The slurry outlet of the titanium tetrachloride leaching circulation tank is communicated with the fused salt chlorination furnace through a pipeline at 1#A slurry pump returning titanium tetrachloride is arranged on a pipeline between the titanium tetrachloride leaching circulation tank and the fused salt chlorination furnace, and the outlet of the slurry pump returning titanium tetrachloride is also connected with a pump 1 through a pipeline#Titanium tetrachloride leaching tower; the fused salt chlorination furnace is sequentially connected with 1 through a pipeline#Dust collector, 2#Dust collector and 1#Titanium tetrachloride leaching tower; 1 is described#Outlet at bottom of titanium tetrachloride leaching tower and 1#The slurry inlets of the titanium tetrachloride leaching circulation tank are communicated through pipelines; in a fused salt chlorination furnace, 1#Dust collector, 2#A slurry inlet pipeline of the dust collector is respectively provided with a slurry return control valve of the fused salt chlorination furnace and a slurry return 1#Dust collector slurry control valve and return 2#The outlet pipeline of the fused salt chlorination furnace is provided with a fused salt chlorination furnace outlet temperature meter T1, 1#An outlet pipeline of the dust collector is provided with a pipe 1#Dust collector outlet thermometer T2, 2#An outlet pipeline of the dust collector is provided with 2#Dust collector outlet temperature T3; in 1#Dust collector, 2#The mud inlet of the dust collector is also connected with a nitrogen inlet pipeline.
3. The method for controlling the temperature gradient of the molten salt chlorination system according to claim 1, wherein the pressure of an outlet of a mud pump of a back chlorination furnace and a dust collector is 1.2MPa ~ 1.5.5 MPa, and the flow rate is 80m3/h ~100m3/h。
4. The molten salt chlorination system temperature gradient control method of claim 1, which is characterized by comprising the following steps: by controlling access to 1#Titanium tetrachloride containing slurry amount of titanium tetrachloride leaching tower to control 1#The liquid level of the leaching circulation tank is stabilized at 1m ~ 1.1.1 m.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201711377251.1A CN107963653B (en) | 2017-12-19 | 2017-12-19 | Gradient control method for temperature of molten salt chlorination system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201711377251.1A CN107963653B (en) | 2017-12-19 | 2017-12-19 | Gradient control method for temperature of molten salt chlorination system |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN107963653A CN107963653A (en) | 2018-04-27 |
| CN107963653B true CN107963653B (en) | 2019-12-31 |
Family
ID=61994530
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201711377251.1A Active CN107963653B (en) | 2017-12-19 | 2017-12-19 | Gradient control method for temperature of molten salt chlorination system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN107963653B (en) |
Families Citing this family (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109052459B (en) * | 2018-08-22 | 2021-05-25 | 攀钢集团攀枝花钢铁研究院有限公司 | For preparing TiCl4Chlorination furnace and furnace temperature control method thereof |
| CN110372033A (en) * | 2019-08-19 | 2019-10-25 | 中国恩菲工程技术有限公司 | Titanium dioxide synthesis system |
| CN112408468A (en) * | 2020-11-13 | 2021-02-26 | 云南国钛金属股份有限公司 | Slurry returning device and method for chlorination furnace |
| CN113233501B (en) * | 2021-06-29 | 2022-06-03 | 攀钢集团攀枝花钛材有限公司 | Salt discharging device at bottom of fused salt chlorination furnace |
| CN114212818A (en) * | 2021-12-31 | 2022-03-22 | 宜宾天原海丰和泰有限公司 | Method for clearing blockage of flue gas pipeline of chlorination furnace |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103112888A (en) * | 2013-03-15 | 2013-05-22 | 金川集团股份有限公司 | Titanium tetrachloride production system and method for recycling titanium tetrachloride from slurry |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101337689B (en) * | 2008-08-26 | 2010-12-01 | 攀钢集团有限公司 | Method for producing titanium tetrachloride using low grade titan raw material |
-
2017
- 2017-12-19 CN CN201711377251.1A patent/CN107963653B/en active Active
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103112888A (en) * | 2013-03-15 | 2013-05-22 | 金川集团股份有限公司 | Titanium tetrachloride production system and method for recycling titanium tetrachloride from slurry |
Also Published As
| Publication number | Publication date |
|---|---|
| CN107963653A (en) | 2018-04-27 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN107963653B (en) | Gradient control method for temperature of molten salt chlorination system | |
| CN101307456B (en) | Pickling waste acid regeneration process | |
| CN103112888B (en) | Titanium tetrachloride production system and method for recycling titanium tetrachloride from slurry | |
| CN101462766A (en) | Technique for cooling titanic chloride burner gas | |
| CN103011269B (en) | Process and system for purifying titanium tetrachloride by removing vanadium | |
| CN105984896B (en) | A kind of purification prepares the system and method for high purity vanadic anhydride powder | |
| EP3252013B1 (en) | System and method for producing high-purity vanadium tetraoxide powder | |
| CN103613126B (en) | A kind of method and system removing vanadium impurity from titanic tetrachloride | |
| CN101760250A (en) | Novel technique for cooling of coke-oven gas | |
| CN206828643U (en) | Cupric alkaline etching liquid circular regeneration equipment for reclaiming | |
| CN103964496B (en) | A kind of titanium tetrachloride production system and technique | |
| CN111318042A (en) | Device system and method for producing modified urea | |
| CN204051381U (en) | A kind of device for recovering tail gas purging system | |
| CN106430216B (en) | A kind of chlorosilane method for treating waste liquid | |
| CN103466549B (en) | High-purity chlorine gas rectifying technology and equipment thereof | |
| CN101417813A (en) | Recovery method and equipment of vanadium-containing slurry produced from titanic chloride refining process | |
| CN104556070A (en) | Method and device for recycling high-purity silica | |
| CN209906673U (en) | Device for producing crude phenol by sodium phenolate carbon dioxide pressurization method | |
| CN108273282B (en) | Vapor phase low-order heat recovery system of trioxymethylene synthetic distillation tower and recovery method thereof | |
| CN110980741A (en) | Tetrachlorosilane hydrogenation system and method for preparing trichlorosilane by using same | |
| CN216890136U (en) | Two-stage dust removal device for preparing titanium tetrachloride | |
| CN111533164B (en) | Vanadium removal method for titanium tetrachloride in boiling chlorination system | |
| CN106051704A (en) | System for recovering high temperature coal gas waste heat with molten salt | |
| CN109835949A (en) | A kind of system and method for vanadium slag cleaning chlorination production high purity vanadic anhydride | |
| CN209322469U (en) | A kind of system avoiding transformation quencher spray head blocking |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| CB02 | Change of applicant information |
Address after: 121000 Jin Ti Road 1, Taihe District, Jinzhou, Liaoning Applicant after: CITIC titanium Limited by Share Ltd Address before: 121000 Jin Ti Road 1, Taihe District, Jinzhou, Liaoning Applicant before: Jinzhou titanium Limited by Share Ltd |
|
| CB02 | Change of applicant information | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |