CN115180647B - Carbonization slag boiling chlorination method - Google Patents
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- CN115180647B CN115180647B CN202211025928.6A CN202211025928A CN115180647B CN 115180647 B CN115180647 B CN 115180647B CN 202211025928 A CN202211025928 A CN 202211025928A CN 115180647 B CN115180647 B CN 115180647B
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Abstract
The invention discloses a carbonization slag boiling chlorination method, which comprises the following steps: setting the chlorination conditions of a first-stage boiling chlorination furnace and a second-stage boiling chlorination furnace based on TiC content in the carbide slag, and boiling to the second-stage boilingIntroducing mixed gas into the boiled chloridizing furnace, wherein the first-stage boiled chloridizing furnace and the second-stage boiled chloridizing furnace are connected in series; adding carbonized residues into a first-stage boiling chlorination furnace for preliminary chlorination reaction; and discharging carbonized residues after the primary chlorination reaction into a secondary boiling chlorination furnace for deep chlorination reaction, discharging tailings after the reaction, and introducing residual gas in the secondary boiling chlorination furnace into the primary boiling chlorination furnace after cyclone dust removal. The method realizes Cl by setting two-stage boiling chlorination in series 2 Contact reaction with difficult-to-react carbide slag, low concentration Cl 2 The catalyst reacts with TiC on the surface layer of the new carbonized residue, so that the utilization rate of chlorine is improved, the consumption of alkali is greatly reduced, the production cost of titanium tetrachloride is reduced, the chlorination rate efficiency of the carbonized residue is improved, and the comprehensive chlorination effect is improved.
Description
Technical Field
The invention relates to the technical field of chemical engineering, in particular to a carbonization slag boiling chlorination method.
Background
The reserves of vanadium titano-magnetite in the world are rich, the reserves of China are named as the forepart of the fescue, the reserves in Panxi area reach billions of tons, and the total reserves of titanium resources are the first nationally. Vanadium titano-magnetite is a multi-element symbiotic ore, and iron (in the form of iron oxide) is contained in the ore by 30-34 wt%, and is mainly used as raw materials for extracting iron, vanadium and titanium.
The vanadium-titanium-iron concentrate produced in Panxi area contains a certain amount of TiO 2 The blast furnace is smelted and then enters blast furnace slag to be abandoned, so that the full utilization of the titanium resources in vanadium titano-magnetite in Panxi area is not realized, and the comprehensive utilization efficiency of the titanium resources in vanadium titano-magnetite in Panxi area is greatly influenced.
The existing blast furnace slag is carbonized at high temperature and selectively chlorinated at low temperature to generate TiCl 4 And the process flow effectively extracts Ti from the blast furnace slag. At present, the blast furnace slag thermal reduction treatment operation is stable, and TiO in slag 2 The reduction rate is stably controlled to be more than 85%, and the effect is good. The low-temperature selective chlorination process adopts single-stage boiling chlorination, so that the effective chlorination of the effective component TiC in the carbide slag is kept, the utilization rate of chlorine is low due to excessive chlorine in the furnace, the unit consumption of the chlorine is high, and the excessive chlorine needs to be absorbed by alkali liquor, so that the consumption of the alkali liquor is high; meanwhile, the chlorination efficiency of TiC in the carbonized slag also has the chlorination rateThe Ti utilization efficiency and the whole process economy in the blast furnace are seriously affected because the Ti utilization efficiency is lower and the stability is more than 85 percent.
Accordingly, there is a need in the art for an improved boiling chlorination process for carbonized residues.
Disclosure of Invention
In view of the above, the embodiment of the invention aims to provide a carbonization slag boiling chlorination method, which aims at solving the problems of low-temperature selective chlorination efficiency and high chlorine unit consumption of the existing carbonization slag.
Based on the above objects, an embodiment of the present invention provides a boiling chlorination method, including:
setting the chlorination conditions of a first-stage fluidizing chlorination furnace and a second-stage fluidizing chlorination furnace based on TiC content in the carbide slag, and introducing mixed gas into the second-stage fluidizing chlorination furnace, wherein the first-stage fluidizing chlorination furnace and the second-stage fluidizing chlorination furnace are connected in series;
adding carbonized residues into a first-stage boiling chlorination furnace for preliminary chlorination reaction;
and discharging carbonized residues after the primary chlorination reaction into a secondary boiling chlorination furnace for deep chlorination reaction, discharging tailings after the reaction, and introducing residual gas in the secondary boiling chlorination furnace into the primary boiling chlorination furnace after cyclone dust removal.
In some embodiments, the secondary fluidized bed chlorination furnace is the primary reactor, 55% -88% of the chlorination reaction is performed in the primary reactor, the primary fluidized bed chlorination furnace is the secondary reactor, and 20% -45% of the reaction is performed in the secondary reactor.
In some embodiments, the first stage ebullated chlorination furnace is configured to feed at an upper end and discharge at a lower end.
In some embodiments, the secondary fluidized bed chlorination furnace is configured to feed at a lower end and discharge at an upper end.
In some embodiments, the chlorination conditions include gas flow, temperature, and gas velocity.
In some embodiments, the reaction temperature of the secondary ebullated chlorination furnace is 20 to 40 ℃ higher than the reaction temperature of the primary ebullated chlorination furnace.
In some embodiments, the gas velocity in the secondary fluidized bed chlorination furnace is 0.03m/s to 0.05m/s greater than the gas velocity in the primary fluidized bed chlorination furnace.
In some embodiments, the gas supply pipes of the secondary and primary fluidizing chlorination furnaces are provided with a regulating valve and a flow meter, and the gas velocity in the fluidizing furnace is regulated by the regulating valve.
In some embodiments, the primary and secondary fluidized bed chlorination furnaces are provided with a fluidization discharge valve connection at the junction.
In some embodiments, the primary and secondary fluidized bed chlorination furnaces have the same reactor diameter.
The invention has at least the following beneficial technical effects:
the method of the invention realizes countercurrent contact of chlorine and carbide slag, increases concentration difference between reactants, improves reaction rate and realizes Cl by deeply analyzing the material characteristics of carbide slag and boiling chlorination reaction mechanism, arranging two-stage boiling chlorination in series, introducing chlorine into the two-stage boiling chlorination furnace, introducing residual gas in the two-stage boiling chlorination furnace into the one-stage boiling chlorination furnace 2 Contact reaction with refractory carbide slag (TiC on the surface layer has reacted), low concentration Cl 2 The titanium dioxide is reacted with TiC on the surface layer of the new carbonized slag, so that the utilization rate of chlorine is improved, the consumption of alkali is greatly reduced, the production cost of titanium tetrachloride is reduced, the chlorination rate efficiency of the carbonized slag is improved, the utilization rate of titanium element and chlorination in the carbonized slag is effectively improved, the comprehensive chlorination effect is improved, and the market competitiveness of the titanium dioxide extracting process of the blast furnace slag is enhanced.
Drawings
In order to more clearly illustrate the embodiments of the invention or the technical solutions in the prior art, the drawings that are necessary for the description of the embodiments or the prior art will be briefly described, it being obvious that the drawings in the following description are only some embodiments of the invention and that other embodiments may be obtained according to these drawings without inventive effort for a person skilled in the art.
FIG. 1 is a schematic diagram of an embodiment of a carbonization slag boiling chlorination process provided by the present disclosure;
fig. 2 is a schematic diagram of an embodiment of a carbonization slag boiling chlorination device provided by the invention.
In the figure:
1. a high-level stock bin; 2. a feeding screw and a matched variable frequency motor; 3. a fluidized U-shaped valve for feeding the carbide slag; 4. a fluidized chlorine flow meter; 5. a fluidizing chlorine regulating valve; 6. a fluidization nitrogen flow meter; 7. a fluidization nitrogen adjusting valve; 8. a fluidizing gas regulating valve of the second-stage fluidizing chlorination furnace; 9. a first-stage fluidizing chlorination furnace; 10. a primary fluidization U-shaped slag discharging valve; 11. a second-stage boiling chlorination furnace; 12. a tailings discharge valve; 13. a primary cyclone dust collector; 14. a first tailings silo; 15. a secondary cyclone dust collector; 16. and a second tailings bin.
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention more apparent, the following embodiments of the present invention will be described in further detail with reference to the accompanying drawings.
The terms "comprising" and "having" and any variations thereof in the description of the invention and the claims and the description of the drawings above are intended to cover a non-exclusive inclusion; the terms first, second and the like in the description and in the claims or in the above-described figures, are used for distinguishing between different objects and not necessarily for describing a sequential or chronological order. The meaning of "a plurality of" is two or more, unless specifically defined otherwise.
Furthermore, references herein to "an embodiment" mean that a particular feature, structure, or characteristic described in connection with the embodiment may be included in at least one embodiment of the present invention. The appearances of such phrases in various places in the specification are not necessarily all referring to the same embodiment, nor are separate or alternative embodiments mutually exclusive of other embodiments. Those of skill in the art will explicitly and implicitly appreciate that the embodiments described herein may be combined with other embodiments.
Aiming at the problems of low-temperature selective chlorination efficiency and high chlorine unit consumption of the existing carbide slag, the reaction of the carbide slag and the chlorine belongs to a typical gas-solid reaction and can be divided into two stages by deeply analyzing the material characteristics of the carbide slag and the boiling chlorination reaction mechanism. The first stage is a contact reaction, controlled by the TiC reaction. The main steps are as follows: under a certain temperature condition, tiC and Cl are arranged on the surface layer in the carbonized slag 2 The contact and reaction occur, and the reaction speed is high and the efficiency is high in the first stage. The second stage is permeation contact reaction, and is subjected to Cl 2 And controlling penetration in the carbonized residue particles. The main process is as follows: after the reaction of TiC on the surface layer of carbonized slag is completed, the TiC and Cl on the inner layer of carbonized slag 2 Can not be directly and effectively contacted with Cl 2 The reaction can only take place after the carbonized residue particles are penetrated into the carbonized residue particles and contacted with TiC, thus the reaction is subjected to Cl 2 Concentration of Cl 2 Penetration capacity and carbide slag surface particle cracking and channel control. In the same boiling chlorination reactor, the reaction late Cl is performed under the same operation condition 2 Low concentration and reduced permeability; the TiC content on the surface is low, the reaction is slow, the TiC reaction capacity in the carbide slag particles is weakened, meanwhile, chlorine gas cannot be fully reacted, the overall chlorination rate of the carbide slag is low, the utilization rate of the chlorine gas is low, and the alkali consumption is high.
Therefore, aiming at the problems existing in the prior art, the invention provides a carbonization slag boiling chlorination method which combines TiC and Cl 2 The reaction characteristics are that chlorine and carbonized slag are in countercurrent contact through two-stage boiling chlorination in series, the concentration difference between reactants is increased, the reaction rate is improved, and Cl is realized 2 Contact reaction with refractory carbide slag (TiC on the surface layer has reacted), low concentration Cl 2 The reaction with TiC on the surface layer of the new carbonized residue can not only improve the chlorination rate efficiency of the carbonized residue, but also improve the utilization rate of chlorine gas and greatly reduce the consumption of alkali.
As shown in fig. 1, a schematic diagram of an embodiment of a carbonization slag boiling chlorination method provided by the invention, the method comprises the following steps:
s1, setting the chlorination conditions of a first-stage fluidizing chlorination furnace and a second-stage fluidizing chlorination furnace based on TiC content in carbide slag, and introducing mixed gas into the second-stage fluidizing chlorination furnace;
s2, adding carbonized residues into a first-stage boiling chlorination furnace for preliminary chlorination reaction;
s3, discharging carbonized residues after the primary chlorination reaction into a secondary boiling chlorination furnace for deep chlorination reaction, discharging tailings after the reaction, and introducing residual gas in the secondary boiling chlorination furnace into the primary boiling chlorination furnace after cyclone dust removal.
Further, the secondary boiling chlorination furnace is a main reactor, 55% -88% of chlorination reaction is carried out in the main reactor, the primary boiling chlorination furnace is a secondary reactor, and 20% -45% of reaction is carried out in the secondary reactor. The carbonization slag of the primary boiling chlorination furnace adopts an upper feeding and lower discharging mode. The method can keep the continuous and stable in-and-out of the carbonization slag in the boiling chlorination furnace, the residence time of the carbonization slag is controllable, meanwhile, the concentration gradient of the reactant is increased as much as possible, the lowest chlorine concentration is in contact reaction with the carbonization slag with the highest TiC content, and the utilization efficiency of the chlorine is improved. The carbonization slag of the secondary boiling chlorination furnace adopts a lower feeding and upper discharging mode. The residence time of the carbide slag in the secondary boiling chlorination furnace is fully ensured to be stable, meanwhile, the chlorine in the secondary boiling chlorination furnace is excessive, the concentration is high, and the TiC in the carbide slag can be ensured to fully react.
In some embodiments, the primary boiling chlorination reactor and the secondary boiling chlorination reactor are independent and are designed to have the same diameter, and in other embodiments, different diameters may be designed according to material characteristics, and the same gas distributor may be designed or different gas distributors may be designed.
Further, the chlorination conditions include gas flow rate, temperature, gas velocity, and the like. The required chlorine amount is determined according to the diameter of the reactor, the fluidization gas speed and the TiC content in the carbide slag, the adding nitrogen amount is calculated, the chlorine and nitrogen are mixed in the mixing tank and then enter the secondary boiling reactor, the reaction stability in the reaction is maintained, the partial chlorine concentration is effectively prevented from being high, the reaction is severe, and the material is terminated because the reaction heat is released and cannot be discharged in time. In order to enhance the quick and efficient chlorination reaction of the carbonized residues, the reaction temperature of the secondary boiling chlorination furnace is 20-40 ℃ higher than that of the primary boiling chlorination furnace; the gas velocity in the second-stage boiling chlorination is 0.03-0.05 m/s higher than that in the first-stage boiling chlorination furnace.
Fig. 2 is a schematic diagram of an embodiment of a carbonization slag boiling chlorination device provided by the invention. The primary fluidizing chlorination furnace 9 and the secondary fluidizing chlorination furnace 11 are connected in series, and carbonized residues are conveyed from the carbonized residue high-level bin 1 through a feeding screw and a matched variable frequency motor 2 and sequentially pass through the primary fluidizing chlorination furnace 9 and the secondary fluidizing chlorination furnace 11. Wherein, the discharge valve between carbonization slag feed valve, first-stage boiling chlorination furnace and second-stage boiling chlorination furnace, the slag discharge valve of second-stage boiling chlorination furnace can select fluidization discharge valve, can keep the material unblocked (after first-stage chlorination, chlorination slag can effectively enter second-stage boiling chlorination furnace), can prevent effectively that gas in the chlorination furnace from flowing back, also can select stop valve, ball valve etc.. The primary boiling chlorination furnace 9 is provided with an independent nitrogen gas supply pipe, is provided with a fluidized chlorine gas regulating valve 5 and a fluidized nitrogen gas flowmeter 6, and is used for regulating and controlling the gas speed of the primary boiling chlorination furnace and ensuring a good fluidization state in a reactor in the furnace.
The method for realizing boiling chlorination of the steel climbing carbide slag by using the invention is described in detail below with reference to specific examples.
The embodiment is a semi-industrial test, wherein a first-stage boiling chlorination furnace 9 and a second-stage boiling chlorination furnace 11 are respectively selected from a phi 200 mm-in Kang Caizhi boiling chlorination reactor, a certain amount of liquid chlorine is gasified and then sent to a mixing tank to be mixed with a certain amount of bottled nitrogen to be decompressed and then mixed to be used as a fluidization medium and a reaction gas of the second-stage boiling chlorination reactor. The carbonized slag raw material is 1# blast furnace slag of iron works of Pan Steel group company, and the carbonized slag is finished after high-temperature reduction, crushing and grinding by an electric furnace on an demonstration line. The typical composition distribution is shown in Table 1. Wherein, the fluidized U-shaped valve is selected as the feeding valve 3 of the carbide slag and the primary fluidized U-shaped slag discharging valve 10, and the ball valve is selected as the tailing slag discharging valve 12.
The specific process comprises the following steps:
the carbonized slag (carbonized slag finished product produced by a high-temperature carbonization demonstration line) which is subjected to high-temperature carbonization reduction, crushed and ground into qualified granularity is added into a high-level stock bin 1 through a lifting device.
The sample analysis of the typical particle size distribution of the carbonized slag is shown in Table 1, the minimum fluidization velocity and minimum carry-out velocity of the carbonized slag are calculated according to the average particle size of the carbonized slag, and the gas velocity in the primary boiling chlorination reactor is controlled to be 0.11-0.28 m/s, preferablyThe gas velocity is 0.15m/s, the gas velocity in the two-stage boiling chlorination reaction is controlled to be 0.15-0.33 m/s, the gas velocity is preferably 0.20m/s, and the flow rate of the mixed gas introduced into the two-stage boiling chlorination reactor is 16.96m 3 /h～37.2m 3 And/h. The primary boiling chlorination reactor was not purged with nitrogen. The temperature of the second-stage boiling chlorination reaction is controlled between 450 and 550 ℃, and the temperature of the second-stage boiling chlorination reaction is controlled between 480 and 580 ℃.
According to TiC content in the carbide slag in Table 2, the chlorine amount is calculated, and the nitrogen amount is added according to the required gas problem.
According to the calculated results, setting the boiling chlorination conditions of carbonized slag such as the temperature of the primary boiling chlorination furnace, the temperature of the secondary boiling chlorination furnace and the like, opening a fluidized nitrogen regulating valve 7, and a fluidized chlorine regulating valve 5, regulating the opening of the valve according to the readings of a fluidized nitrogen flowmeter 6 and a fluidized chlorine flowmeter 4, controlling the chlorine flow and the nitrogen flow, and controlling the concentration of the mixed gas. Starting the boiling chlorination device, opening a fluidizing gas regulating valve 8 of the secondary boiling chlorination furnace, and controlling the fluidizing gas flow of the secondary boiling chlorination reactor.
The carbide slag enters a high-level stock bin 1, a feeding screw and a matched variable frequency motor 2 are started, a loosening gas regulating valve (not shown in the figure) and a conveying gas regulating valve (not shown in the figure) of a carbide slag feeding fluidization U-shaped valve 3 are opened, and the smoothness of the carbide slag feeding is kept. The spiral frequency is set to be 10Hz, the frequency is gradually increased after stabilizing for 5 minutes, the frequency is increased by 5Hz every 5 minutes, the final stabilization is carried out at 30Hz, the feeding amount is controlled at 25kg/h, and the carbonized residues are added into the reactor of the primary boiling chlorination furnace 9. And at the initial feeding stage, a loosening gas regulating valve and a conveying gas regulating valve of the primary fluidization slag discharging U-shaped valve 10 are closed, so that materials in the primary fluidizing chlorination furnace 9 cannot enter the secondary fluidizing chlorination furnace 11, and a carbide slag layer in the primary fluidizing chlorination reactor is formed.
After the carbonized slag is fed for 60 minutes, a loosening gas regulating valve and a conveying gas regulating valve of a primary fluidization U-shaped slag discharging valve 10 are gradually opened, and the chlorinated slag passing through the primary boiling chlorination furnace 9 is discharged into a secondary boiling chlorination furnace 11.
After the secondary boiling chlorination reactor is fed for 60 minutes, the secondary cyclone dust collector 15 is started, the tailings discharge valve 12 and the primary cyclone slag discharge valve (namely, the slag discharge valve connected below the primary cyclone dust collector 13 in fig. 2) are gradually opened, the secondary boiling chlorination reactor starts to discharge slag outwards, the slag discharge valve below the first tailings bin 14 is periodically opened, and the chlorinated tailings in the tailings bin are discharged out of the system, but a certain amount of chlorinated tailings in the first tailings bin 14 need to be kept, so that a material seal is formed.
The gas after primary cyclone dust removal enters the primary boiling chlorination furnace 9 again, the secondary chloride gas after the reaction in the primary boiling chlorination furnace 9 enters the secondary cyclone dust remover 15, a secondary cyclone slag discharging valve (namely a valve connected below the secondary cyclone dust remover 15 in fig. 2) is opened, so that the material slag enters the second tailings bin 16, a slag discharging valve below the second tailings bin 16 is periodically opened to collect tailings, and the gas after dust removal enters leaching treatment.
When the feeding is stable, the feeding amount reaches 20-28 kg/h, the primary and secondary boiling chlorination reactors reach a certain filling rate, after the material layer is stable, the average residence time of the carbonized slag of the primary boiling chlorination furnace is kept between 40 and 90min, the average residence time of the carbonized slag of the secondary boiling chlorination furnace is kept between 60 and 120min, and the system is balanced. And (5) detecting granularity and chemical components of the chlorinated tailings by sampling for multiple times. The typical particle size distribution of the carbide slag and the chlorinated tailings is shown in table 1, the main components of the carbide slag and the chlorinated tailings are shown in table 2, and the main chemical components of the chlorinated tail gas are shown in table 3.
TABLE 1 typical particle size distribution/%
TABLE 2 Chlorination tailings Main chemical composition/%
TABLE 3 main chemical composition of chlorinated tail gas/(vt%)
From tables 2 and 3, it can be seen that: the chlorination rate of the carbonized residues can be increased to more than 88% by utilizing the technology of the invention, and the chlorination rate is greatly increased compared with the chlorination rate (the average chlorination rate in 2021 is 82.5%) in normal production; cl in the chloridized tail gas 2 The content of Cl is reduced from 3.98% to 0.23% 2 The utilization rate is obviously improved.
In summary, the invention has the following advantages:
aiming at the problems of low boiling chlorination rate and low chlorine utilization rate of the carbide slag, by arranging two-stage boiling chlorination in series connection, the counter-current contact chlorination process of the carbide slag and the chlorine increases the concentration difference between reactants, improves the reaction rate, improves the chlorination efficiency of the carbide slag, and then discharges the carbide slag out of the system, improves the chlorination rate and the chlorine utilization rate of Ti in the blast furnace slag, realizes the efficient recycling of Ti in the blast furnace, and improves the economy of the whole flow. The method is simple and reliable; the continuous stability is good, and the efficiency is high; the equipment has the advantages of simple manufacture, less investment, small occupied area, good continuity, low energy consumption, stable operation, large treatment capacity and easy industrialization.
The foregoing is an exemplary embodiment of the present disclosure, but it should be noted that various changes and modifications could be made herein without departing from the scope of the disclosure as defined by the appended claims. The functions, steps and/or actions of the method claims in accordance with the disclosed embodiments described herein need not be performed in any particular order. Furthermore, although elements of the disclosed embodiments may be described or claimed in the singular, the plural is contemplated unless limitation to the singular is explicitly stated.
It should be understood that as used herein, the singular forms "a", "an", and "the" are intended to include the plural forms as well, unless the context clearly supports the exception. It should also be understood that "and/or" as used herein is meant to include any and all possible combinations of one or more of the associated listed items.
The foregoing embodiment of the present invention has been disclosed with reference to the number of embodiments for the purpose of description only, and does not represent the advantages or disadvantages of the embodiments.
Those of ordinary skill in the art will appreciate that: the above discussion of any embodiment is merely exemplary and is not intended to imply that the scope of the disclosure of embodiments of the invention, including the claims, is limited to such examples; combinations of features of the above embodiments or in different embodiments are also possible within the idea of an embodiment of the invention, and many other variations of the different aspects of the embodiments of the invention as described above exist, which are not provided in detail for the sake of brevity. Therefore, any omission, modification, equivalent replacement, improvement, etc. of the embodiments should be included in the protection scope of the embodiments of the present invention.
Claims (10)
1. A carbonization slag boiling chlorination method, which is characterized by comprising the following steps:
setting the chlorination conditions of a first-stage fluidizing chlorination furnace and a second-stage fluidizing chlorination furnace based on TiC content in the carbide slag, and introducing a mixed gas consisting of chlorine and nitrogen into the second-stage fluidizing chlorination furnace, wherein the first-stage fluidizing chlorination furnace and the second-stage fluidizing chlorination furnace are connected in series;
adding carbonized residues into the first-stage boiling chlorination furnace to perform preliminary chlorination reaction;
and discharging the carbonized residues after the preliminary chlorination reaction into the secondary boiling chlorination furnace for deep chlorination reaction, discharging tailings after the reaction, and introducing residual gas in the secondary boiling chlorination furnace into the primary boiling chlorination furnace after cyclone dust removal.
2. The carbonization slag boiling chlorination method according to claim 1, wherein the secondary boiling chlorination furnace is a main reactor, 55% -88% of chlorination reaction is performed in the main reactor, the primary boiling chlorination furnace is a secondary reactor, and 20% -45% of reaction is performed in the secondary reactor.
3. The method for boiling chlorination of carbonized residues according to claim 1, wherein the primary boiling chlorination furnace is arranged for feeding at the upper end and discharging at the lower end.
4. A carbonization slag boiling chlorination method according to claim 3, characterized in that the secondary boiling chlorination furnace is arranged for feeding at the lower end and discharging at the upper end.
5. The carbonization slag boiling chlorination process of claim 1, wherein the chlorination conditions include gas flow, temperature, and gas velocity.
6. The method for fluidizing chlorination of carbonized residues according to claim 5, wherein the reaction temperature of the second fluidizing chlorination furnace is 20 to 40 ℃ higher than the reaction temperature of the first fluidizing chlorination furnace.
7. The method for fluidizing chlorination of carbonized residues according to claim 5, wherein the gas velocity in the second fluidizing chlorination furnace is 0.03m/s to 0.05m/s higher than the gas velocity in the first fluidizing chlorination furnace.
8. The method for fluidizing chlorination of carbonized residues according to claim 7, wherein the gas supply pipes of the second fluidizing chlorination furnace and the first fluidizing chlorination furnace are provided with a regulating valve and a flow meter, and the gas velocity in the fluidizing chlorination furnace is regulated by the regulating valve.
9. The carbonization slag fluidizing chlorination method according to claim 1, wherein the primary fluidizing chlorination furnace and the secondary fluidizing chlorination furnace are connected at a connection point with a fluidizing discharge valve.
10. The method for fluidizing chlorination of carbonized residues according to claim 1, wherein the primary fluidizing chlorination furnace and the secondary fluidizing chlorination furnace have the same reactor diameter.
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| CN103979603B (en) * | 2014-05-26 | 2015-08-26 | 攀钢集团攀枝花钢铁研究院有限公司 | A kind of low-temperature boiling chlorination system |
| CN105986126B (en) * | 2015-01-30 | 2017-10-03 | 中国科学院过程工程研究所 | A kind of system and method for the efficient chlorination vanadium extraction of vanadium slag |
| CN105819500B (en) * | 2016-03-30 | 2017-07-11 | 攀钢集团攀枝花钢铁研究院有限公司 | The method for improving titanium-containing blast furnace slag chlorination efficiency |
| CN115180647B (en) * | 2022-08-25 | 2023-10-13 | 攀钢集团攀枝花钢铁研究院有限公司 | Carbonization slag boiling chlorination method |
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2022
- 2022-08-25 CN CN202211025928.6A patent/CN115180647B/en active Active
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2023
- 2023-05-11 WO PCT/CN2023/093529 patent/WO2024041037A1/en unknown
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103011267A (en) * | 2012-12-14 | 2013-04-03 | 攀钢集团攀枝花钢铁研究院有限公司 | Low-temperature boiling chloridizing process |
| CN109721099A (en) * | 2019-03-14 | 2019-05-07 | 攀枝花攀钢集团设计研究院有限公司 | Combined reaction furnace for low temperature chlorination producing titanium tetrachloride t 5 bx |
| CN111961771A (en) * | 2020-08-25 | 2020-11-20 | 攀钢集团攀枝花钢铁研究院有限公司 | Titanium-containing blast furnace slag chlorination device |
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| WO2024041037A1 (en) | 2024-02-29 |
| CN115180647A (en) | 2022-10-14 |
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