Anhydrous aluminum chloride production system

Abstract

The present application relates to the technical field of aluminium chloride, and particularly relates to a production system of anhydrous aluminium chloride, which comprises a reaction unit, a feeding unit, a heat exchange unit, a buffer unit and a crystallization unit, the heat exchange unit comprises a heat exchange shell and a plurality of heat exchange pipes, the bottom wall of the heat exchange shell is gradually inclined upwards in a direction away from a chlorination furnace, and the buffer unit is used for buffering the aluminium chloride and the molten salt carried by the aluminium chloride so as to separate the molten salt from the aluminium chloride; the feeding unit is used for feeding the chlorination furnace, the generated aluminium chloride enters the crystallization unit to form crystallization after passing through the heat exchange unit and the buffer unit in sequence, thereby forming a complete and continuous production system, and most of the molten salt can flow back to the chlorination furnace along the inclined heat exchange shell during the cooling process of the aluminium chloride, the remaining molten salt is left in the buffer unit after being buffered and cooled by the buffer unit, thereby most or even all of the molten salt carried by the aluminium chloride gas can be removed, and the crystallization purity of the aluminium chloride is improved.

Description

TECHNICAL FIELD

[0001] The present application relates to the technical field of aluminum chloride, in particular to a production system of anhydrous aluminum chloride. BACKGROUND

[0002] The traditional production method of aluminum chloride is aluminum ingot melting method, which sends molten high-purity aluminum ingot into a sealed chlorination furnace to react with chlorine gas to generate aluminum chloride, and then captures and obtains after condensation, however, the preparation method uses high-purity aluminum as raw material, resulting in high production cost.

[0003] At present, anhydrous aluminum chloride is generated by reacting aluminum oxide, petroleum coke, mixed molten salt and chlorine gas in a chlorination furnace, and then the finished product is obtained by cooling and crystallization, the preparation method is more and more popular because of lower cost, however, the high-temperature generated aluminum chloride carries part of the molten salt, resulting in low purity of aluminum chloride product. SUMMARY

[0004] The technical problem to be solved by the present application is that in the prior art, when aluminum oxide is used as a raw material to prepare aluminum chloride, high-temperature generated aluminum chloride carries part of the molten salt, resulting in low purity of aluminum chloride product, and the present application provides a production system of anhydrous aluminum chloride.

[0005] In order to solve the above technical problems, the present application adopts the following technical scheme: a production system of anhydrous aluminum chloride, comprising:

[0006] A reaction unit comprising a chlorination furnace;

[0007] A feeding unit comprising an aluminum oxide conveying line, a petroleum coke conveying line, a mixed molten salt conveying line and a chlorine gas conveying line connected to the chlorination furnace at the output end;

[0008] A heat exchange unit for heat exchange between low-temperature air and high-temperature aluminum chloride gas, comprising a heat exchange shell and a plurality of heat exchange pipes suspended in the heat exchange shell, the bottom wall of the heat exchange shell gradually inclines upward away from the chlorination furnace to make the molten salt carried in the aluminum chloride flow back to the chlorination furnace;

[0009] A buffer unit for buffering the aluminum chloride and the molten salt carried therein from the heat exchange unit to separate the molten salt from the aluminum chloride;

[0010] And a crystallization unit for crystallizing the gaseous aluminum chloride from the buffer unit.

[0011] Further, the aluminum oxide conveying line comprises an aluminum oxide storage tank, a plurality of aluminum oxide intermediate bins and an aluminum oxide switching valve for connecting the aluminum oxide storage tank and any one of the aluminum oxide intermediate bins;

[0012] The petroleum coke conveying line comprises a petroleum coke storage tank, a plurality of petroleum coke intermediate storages, and a petroleum coke switching valve for connecting the petroleum coke storage tank with any one of the petroleum coke intermediate storages.

[0013] The feeding port of the chlorination furnace is provided with a mixing bin, a screw feeder is arranged in the mixing bin, a plurality of alumina intermediate storages correspond to the petroleum coke intermediate storages one by one, and the outlet ends of the alumina intermediate storages and the corresponding petroleum coke intermediate storages are provided with a mixed conveying pipeline for conveying the proportionally mixed two to the mixing bin.

[0014] Further, the mixed molten salt conveying line comprises a molten salt circulating kettle, a molten salt heating furnace for heating the molten salt circulating kettle, and a first conveying pump for conveying the mixed molten salt in the molten salt heating furnace to the chlorination furnace.

[0015] Further, a flushing pipeline and a backflow pipeline are arranged between the molten salt circulating kettle and the buffer unit, a second conveying pump for conveying the mixed molten salt in the molten salt circulating kettle to the buffer unit to flush the molten salt adhered to the inner wall of the buffer unit is arranged on the flushing pipeline, and a valve is arranged on the backflow pipeline.

[0016] Further, the buffer unit comprises a plurality of cascade arranged elution towers, the gas inlet of the elution tower located at the head end is connected with the material outlet of the heat exchange unit, and the gas outlet of the elution tower located at the tail end is connected with the crystallization unit.

[0017] Further, a conveying pipeline is arranged between the elution tower and the crystallization unit, and a heat preservation mechanism is installed on the conveying pipeline, and the output end of the heat preservation mechanism is connected with the outlet of the heat exchange unit.

[0018] Further, the heat exchange tube comprises an inner tube and an outer tube sleeved outside the inner tube, the top of the inner tube is communicated with the low-temperature air inlet of the heat exchange shell, the bottom is communicated with the inner cavity of the outer tube, and the top of the outer tube is communicated with the outlet of the heat exchange shell.

[0019] Further, a first pneumatic butterfly valve, a first fast feeding mechanism, a first slow feeding mechanism, an alumina loss-on-ignition balance, and a first pneumatic flap valve are sequentially arranged between the outlet of the alumina intermediate storage and the mixed conveying pipeline.

[0020] A second pneumatic butterfly valve, a second fast feeding mechanism, a second slow feeding mechanism, a petroleum coke loss-on-ignition balance, and a second pneumatic flap valve are sequentially arranged between the outlet of the petroleum coke intermediate storage and the mixed conveying pipeline.

[0021] Further, the production system further comprises:

[0022] A dust collector, the inlet of which is communicated with the crystallizer for collecting the residual material in the crystallizer.

[0023] The tail gas buffer tank is communicated with the dust collector for balancing system pressure.

[0024] The salt discharge tank is communicated with the chlorination furnace for transferring residual materials in the chlorination furnace.

[0025] Further, the crystallization unit comprises a plurality of crystallizers and a plurality of air hammers for knocking the crystallizers, and the outlet of each crystallizer is sequentially provided with a third pneumatic butterfly valve, a discharge buffer tank, a fourth pneumatic butterfly valve, a turnover barrel and a weigher.

[0026] The present application has the following beneficial effects: the present application uses the feeding unit to feed the chlorination furnace, the generated aluminum trichloride enters the crystallization unit to form crystals after the heat exchange unit and the buffer unit, thereby forming a complete and continuous production system, and most of the molten salt can be returned to the chlorination furnace along the inclined heat exchange shell during the cooling process of the aluminum trichloride, and the remaining molten salt is left in the buffer unit after being buffered and cooled by the buffer unit, so that most or even all of the molten salt carried by the aluminum trichloride gas can be removed, and the crystallization purity of the aluminum trichloride is improved. BRIEF DESCRIPTION OF DRAWINGS

[0027] The present application will be further described below in combination with the drawings and examples.

[0028] Figure 1 is a structural schematic diagram of the present application;

[0029] Figure 2 is a structural schematic diagram of the alumina conveying line and the petroleum coke conveying line;

[0030] Figure 3 is a structural schematic diagram of the heat exchange unit;

[0031] Figure 4 is a top view of the heat exchange unit;

[0032] In the drawings:

[0033] 1, chlorination furnace;

[0034] 2, alumina conveying line; 201, alumina storage tank; 202, alumina intermediate bin; 203, alumina switching valve; 204, first pneumatic butterfly valve; 205, first fast feeding mechanism; 206, first slow feeding mechanism; 207, alumina loss-in-weight scale; 208, first pneumatic flap valve; 209, mixed conveying pipeline;

[0035] 3, petroleum coke conveying line; 301, petroleum coke storage tank; 302, petroleum coke intermediate bin; 303, petroleum coke switching valve; 304, second pneumatic butterfly valve; 305, second fast feeding mechanism; 306, second slow feeding mechanism; 307, petroleum coke loss-in-weight scale; 308, second pneumatic flap valve;

[0036] 4. mixed molten salt conveying line; 401. molten salt circulating kettle; 402. molten salt heating furnace; 403. first conveying pump;

[0037] 5. chlorine conveying line;

[0038] 6. heat exchange unit; 601. heat exchange shell; 602. heat exchange pipe; 6021. inner pipe; 6022. outer pipe;

[0039] 7. buffer unit; 701. elution tower;

[0040] 8. crystallization unit; 801. crystallizer; 802. air hammer; 803. third pneumatic butterfly valve; 804. discharge buffer; 805. fourth pneumatic butterfly valve; 806. turnover barrel; 807. weigher;

[0041] 9. mixing bin;

[0042] 10. screw feeder;

[0043] 11. flushing pipeline;

[0044] 12. reflux pipeline;

[0045] 13. second conveying pump;

[0046] 14. conveying pipeline;

[0047] 15. heat preservation mechanism;

[0048] 16. dust collector;

[0049] 17. tail gas buffer tank;

[0050] 18. salt discharge tank. DETAILED DESCRIPTION

[0051] The application will now be described in further detail with reference to the drawings. These drawings show only the essential features of the application and are not to scale. The drawings are schematic representations only of the basic structure of the application and therefore only show those features relevant to the present application. Directions and references (e.g. up, down, left, right, etc.) can be used only to aid in the description of features in the drawings. The following detailed description is therefore not to be taken in a limiting sense and the scope of the subject matter sought to be protected is defined only by the claims as appended and equivalents thereof.

[0052] As shown in Figure 1 and Figure 2 , a system for producing anhydrous aluminum chloride comprises:

[0053] a reaction unit comprising a chlorination furnace 1;

[0054] The feeding unit comprises an alumina conveying line 2, a petroleum coke conveying line 3, a mixed molten salt conveying line 4 and a chlorine conveying line 5, which are connected with the chlorination furnace 1, and are used to convey alumina, petroleum coke, mixed molten salt and chlorine into the chlorination furnace 1 respectively for reaction to generate aluminum chloride gas, wherein the alumina and petroleum coke enter the chlorination furnace 1 from the middle part, the chlorine enters the chlorination furnace 1 from the bottom part, and the mixed molten salt enters the chlorination furnace 1 from the top part;

[0055] The heat exchange unit 6 is used to exchange heat between the low-temperature air and the high-temperature aluminum chloride gas to output the heated air and the cooled aluminum chloride gas, and comprises a heat exchange shell 601 and a plurality of heat exchange pipes 602 suspended in the heat exchange shell 601, and the bottom wall of the heat exchange shell 601 is gradually inclined upward in the direction away from the chlorination furnace 1 to make the molten salt carried in the aluminum chloride gas flow back to the chlorination furnace 1; the low-temperature air enters the heat exchange unit 6 through a dehumidifier and an air pump in sequence, and the dehumidifier is used to remove the moisture in the low-temperature air.

[0056] The high-temperature aluminum chloride gas in the chlorination furnace 1 exchanges heat with the low-temperature air in the heat exchange pipes 602 in the heat exchange unit 6, the low-temperature air is located inside the heat exchange pipes 602, and the aluminum chloride gas is located outside the heat exchange pipes 602, and the two do not contact each other; the high-temperature molten salt carried in the aluminum chloride gas is cooled synchronously with the cooling of the aluminum chloride gas, and drips along the pipe wall of the heat exchange pipes 602 to the bottom wall of the heat exchange shell 601, and then flows back to the chlorination furnace 1 along the inclined bottom wall.

[0057] The buffer unit 7 is used to buffer the aluminum chloride from the heat exchange unit 6 to separate the molten salt from the aluminum chloride; the aluminum chloride gas cooled in the heat exchange unit 6 enters the buffer unit 7, and the molten salt carried in the aluminum chloride gas can remain in the buffer unit 7 after being buffered, and the aluminum chloride gas flows out of the buffer unit 7.

[0058] The crystallization unit 8 is used to crystallize the gaseous aluminum chloride from the buffer unit 7.

[0059] Firstly, the alumina conveying line 2, the petroleum coke conveying line 3, the mixed molten salt conveying line 4 and the chlorine conveying line 5 convey alumina, petroleum coke, mixed molten salt and chlorine into the chlorination furnace 1 respectively for reaction to generate aluminum chloride gas; then the high-temperature aluminum chloride gas exchanges heat with the low-temperature air in the heat exchange pipes 602 in the heat exchange unit 6 to output the cooled aluminum chloride gas, and the molten salt carried in the aluminum chloride gas is cooled synchronously; most of the molten salt flows back to the chlorination furnace 1 along the inclined bottom wall of the heat exchange shell 601; then the aluminum chloride gas enters the buffer unit 7 for buffering, and the remaining small amount of molten salt carried in the aluminum chloride gas remains in the buffer unit 7 to separate the molten salt from the aluminum chloride gas; finally, the aluminum chloride gas enters the crystallization unit 8 for crystallization, and the finished product after crystallization is conveyed to a packaging workshop for packaging.

[0060] In some examples, the alumina conveying line 2 comprises an alumina storage tank 201, a plurality of alumina intermediate bins 202, and alumina switching valves 203 for connecting the alumina storage tank 201 with any one of the alumina intermediate bins 202. In this embodiment, two alumina intermediate bins 202 are provided, and the alumina switching valves 203 are used to switch the connection state of the two alumina intermediate bins 202 with the alumina storage tank 201.

[0061] The petroleum coke conveying line 3 comprises a petroleum coke storage tank 301, a plurality of petroleum coke intermediate bins 302, and petroleum coke switching valves 303 for connecting the petroleum coke storage tank 301 with any one of the petroleum coke intermediate bins 302. In this embodiment, two petroleum coke intermediate bins 302 are provided, and the petroleum coke switching valves 303 are used to switch the connection state of the two petroleum coke intermediate bins 302 with the petroleum coke storage tank 301.

[0062] The feed inlet of the chlorination furnace 1 is provided with a mixing bin 9, and a screw feeder 10 is arranged in the mixing bin 9. The plurality of alumina intermediate bins 202 and the plurality of petroleum coke intermediate bins 302 are one-to-one corresponding, and the outlet ends of the alumina intermediate bins 202 and the petroleum coke intermediate bins 302 corresponding thereto are provided with mixed conveying pipelines 209 for conveying the proportionally mixed alumina and petroleum coke to the mixing bin 9. In this embodiment, two mixed conveying pipelines 209 are provided, and the two mixed conveying pipelines 209, the two alumina intermediate bins 202, and the two petroleum coke intermediate bins 302 are one-to-one corresponding, respectively.

[0063] During feeding, the alumina falls onto the mixed conveying pipeline 209 through the alumina storage tank 201 and the alumina intermediate bin 202 in sequence, and the petroleum coke also falls onto the mixed conveying pipeline 209 through the petroleum coke storage tank 301 and the petroleum coke intermediate bin 302 in sequence. The mixed conveying pipeline 209 conveys the alumina and the petroleum coke thereon to the mixing bin, and the screw feeder 10 feeds the mixed alumina and petroleum coke into the chlorination furnace 1.

[0064] In some examples, the mixed molten salt conveying line 4 comprises a molten salt circulating kettle 401, a molten salt heating furnace 402 for heating the molten salt circulating kettle 401, and a first conveying pump 403 for conveying the mixed molten salt in the molten salt heating furnace 402 to the chlorination furnace 1. After the mixed molten salt in the molten salt circulating kettle 401 is heated to a certain temperature by the molten salt heating furnace 402, it is fed into the chlorination furnace 1 by the first conveying pump 403. When the temperature is too high, the molten salt circulating kettle 401 can be cooled by a blower.

[0065] In some examples, the molten salt circulating kettle 401 is provided with a flushing pipeline 11 and a backflow pipeline 12, the flushing pipeline 11 is provided with a second conveying pump 13 for conveying the mixed molten salt in the molten salt circulating kettle 401 to the buffer unit 7 to flush the molten salt adhered to the inner wall of the buffer unit 7, and the backflow pipeline 12 is provided with a valve including an upper pneumatic plug valve and a manual plug valve; the input end of the flushing pipeline 11 is located on the molten salt circulating kettle 401, and the output end is located on the buffer unit 7; the input end of the backflow pipeline 12 is located on the buffer unit 7, and the output end is located on the molten salt circulating kettle 401; after the molten salt carried by the aluminum chloride gas is buffered and cooled in the buffer unit 7, it adheres to the inner wall of the buffer unit 7 and slides along the inner wall, and then enters the molten salt circulating kettle 401 through the backflow pipeline 12; after long-term use, the high-boiling-point molten salt will adhere to the inner wall of the buffer unit 7; at this time, the molten salt in the molten salt circulating kettle 401 can be conveyed to the buffer unit 7 through the second conveying pump 13 during the production gap, and the molten salt in the buffer unit 7 is sprayed and flushed through a spray head, etc., to flush the adhered molten salt to the bottom of the buffer unit 7, and then re-enter the molten salt circulating kettle 401 along the backflow pipeline 12.

[0066] In some examples, the buffer unit 7 includes a plurality of cascade arranged elution towers 701, the gas inlet of the elution tower 701 located at the head end is connected with the material outlet of the heat exchange unit 6, and the gas outlet of the elution tower 701 located at the tail end is connected with the crystallization unit 8; the aluminum chloride gas enters the plurality of elution towers 701 in sequence to be buffered and cooled, and the spray head in the elution tower 701 can flush the molten salt adhered to the inner wall thereof.

[0067] In some examples, the elution tower 701 is provided with a conveying pipeline 14 between the elution tower 701 and the crystallization unit 8, the conveying pipeline 14 is provided with a heat preservation mechanism 15, the output end of the heat preservation mechanism 15 is connected with the outlet of the heat exchange unit 6 for outputting the heated air after the high-temperature aluminum chloride gas is heat exchanged with the low-temperature air, the heated air can be used as a heat source to heat the conveying pipeline 14, so as to avoid the aluminum chloride from being crystallized in the conveying pipeline 14 due to excessive cooling during long-distance conveying or excessive cooling caused by the contact between the aluminum chloride and the conveying pipeline 14.

[0068] In some examples, the heat exchange pipe 602 includes an inner pipe 6021 and an outer pipe 6022 sleeved outside the inner pipe 6021, the top of the inner pipe 6021 is communicated with the low-temperature air inlet of the heat exchange shell 601, the bottom is communicated with the inner cavity of the outer pipe 6022, the top of the outer pipe 6022 is communicated with the outlet of the heat exchange shell 601 for outputting the heated air, the low-temperature air enters the inner pipe 6021 from the low-temperature air inlet, and then enters the inner cavity of the outer pipe 6022 from the bottom of the inner pipe 6021, the cooling cavity is formed between the outer peripheral wall of the inner pipe 6021 and the inner peripheral wall of the outer pipe 6022 to heat exchange with the high-temperature aluminum chloride gas entering the heat exchange shell 601.

[0069] The top wall of the heat exchange shell 601 is parallel to the bottom wall to form a heat exchange shell 601 with an overall inclined structure. When low-temperature air is continuously introduced into the heat exchange pipe 602, a low-temperature environment is formed in the entire heat exchange shell 601, so that the aluminum chloride gas can be cooled not only when it contacts the heat exchange pipe 602, but also when it contacts the wall surface of the heat exchange shell 601. At this time, the molten salt can flow back not only along the bottom wall of the heat exchange shell 601, but also along the top wall of the heat exchange shell 601.

[0070] The plurality of heat exchange pipes 602 are arranged in the heat exchange shell 601 in a staggered manner and are divided into a plurality of rows in the direction from the chlorination furnace 1 to the buffer unit 7. Each row of heat exchange pipes 602 is staggered and gradually moves upward to form an overall inclined structure, which is consistent with the inclined direction of the heat exchange shell 601.

[0071] In some examples, the outlet of the alumina intermediate bin 202 and the mixed conveying pipeline 209 are sequentially provided with a first pneumatic butterfly valve 204, a first fast feeding mechanism 205, a first slow feeding mechanism 206, an alumina loss-on-ignition balance 207, and a first pneumatic flap valve 208. The first fast feeding mechanism 205 and the first slow feeding mechanism 206 are both spiral feeding mechanisms. The first fast feeding mechanism 205 can quickly send the alumina from the outlet of the alumina intermediate bin 202 to the next tool to improve the feeding speed. The first slow feeding mechanism 206 is used to stably send the alumina to the alumina loss-on-ignition balance 207 to improve the weighing accuracy.

[0072] The outlet of the petroleum coke intermediate bin 302 and the mixed conveying pipeline 209 are sequentially provided with a second pneumatic butterfly valve 304, a second fast feeding mechanism 305, a second slow feeding mechanism 306, a petroleum coke loss-on-ignition balance 307, and a second pneumatic flap valve 308. The second fast feeding mechanism 305 and the second slow feeding mechanism 306 are both spiral feeding mechanisms. The second fast feeding mechanism 305 can quickly send the petroleum coke from the outlet of the petroleum coke intermediate bin 302 to the next tool to improve the feeding speed. The second slow feeding mechanism 306 is used to stably send the petroleum coke to the petroleum coke loss-on-ignition balance 307 to improve the weighing accuracy.

[0073] In some examples, the production system further comprises:

[0074] A dust collector 16, the inlet of which communicates with the crystallization unit 8 for collecting the remaining material in the crystallizer 801. An air hammer 802 is externally provided for knocking the dust collector 16 to knock off the crystals attached to the inner wall of the dust collector 16. A fifth pneumatic butterfly valve and a turnover barrel are provided at the bottom of the dust collector 16.

[0075] A tail gas buffer tank 17, the inlet of which communicates with the dust collector 16 for balancing the system pressure. There are a plurality of tail gas buffer tanks 17, which are sequentially connected in series.

[0076] and a salt discharge tank 18, the inlet of which is communicated with the chlorination furnace 1 for transferring the residual material in the chlorination furnace 1, when the chlorination furnace 1 is overhauled, the residual material in the chlorination furnace 1 can be transferred to the salt discharge tank 18 for temporary storage.

[0077] In some examples, the crystallization unit 8 comprises a plurality of crystallizers 801 and a plurality of air hammers 802 for knocking the crystallizers 801, the outlet of each crystallizer 801 is sequentially provided with a third pneumatic butterfly valve 803, a discharge buffer tank 804, a fourth pneumatic butterfly valve 805, a turnover barrel 806 and a weighing device 807, after the aluminum chloride gas forms crystals in the crystallizer 801, the crystals can be knocked off to the bottom of the crystallizer 801 by the air hammer 802, and then sequentially pass through the third pneumatic butterfly valve 803, the discharge buffer tank 804 and the fourth pneumatic butterfly valve 805 into the turnover barrel 806, and then flow to the packaging workshop after being weighed by the weighing device 807.

[0078] Working principle:

[0079] When feeding, the alumina falls onto the mixed conveying pipeline 209 through the alumina storage tank 201 and the alumina intermediate bin 202 in turn, the petroleum coke also falls onto the mixed conveying pipeline 209 through the petroleum coke storage tank 301 and the petroleum coke intermediate bin 302 in turn, the mixed conveying pipeline 209 conveys the alumina and the petroleum coke thereon to the mixing bin, the spiral feeder 10 sends the mixed alumina and petroleum coke into the chlorination furnace 1, and the first conveying pump 403 conveys the mixed molten salt to the chlorination furnace 1, and the chlorine conveying line 5 conveys chlorine to the chlorination furnace 1, and then the alumina and the petroleum coke are reacted together to generate aluminum chloride gas.

[0080] Then the high-temperature aluminum chloride gas enters the heat exchange unit 6 to exchange heat with the low-temperature air in the heat exchange pipe 602, and outputs the cooled aluminum chloride gas, and in the process, the molten salt carried by the aluminum chloride gas is cooled synchronously, most of the molten salt flows back to the chlorination furnace 1 along the obliquely arranged heat exchange shell 601, and then the aluminum chloride gas enters the buffer unit 7 for buffering and cooling, and the remaining small amount of molten salt carried by the aluminum chloride gas remains in the buffer unit 7 to realize the separation of the molten salt from the aluminum chloride gas, part of the molten salt in the buffer unit 7 slides along the inner wall, and then enters the molten salt circulating kettle 401 through the reflux pipeline 12, and the other part of the molten salt adheres to the inner wall of the buffer unit 7, at this time, the molten salt in the molten salt circulating kettle 401 can be conveyed to the buffer unit 7 through the second conveying pump 13 during the production gap, and the molten salt in the buffer unit 7 is sprayed and flushed through the spray head, so that the adhered molten salt is flushed to the bottom of the buffer unit 7, and then flows back to the molten salt circulating kettle 401 through the reflux pipeline 12, and finally the aluminum chloride gas flowing out of the buffer unit 7 enters the crystallization unit 8 for crystallization, and the finished product after crystallization is conveyed to the packaging workshop for packaging.

[0081] With the above ideal embodiments according to the present application as the inspiration, through the above description, relevant staff can make various changes and modifications without deviating from the technical idea of the present application. The technical scope of the present application is not limited to the content of the specification, and must be determined according to the scope of the claims.

Claims

1. A production system for anhydrous aluminum trichloride, characterized in that: include: The reaction unit includes a chlorination furnace (1); The feeding unit includes an alumina conveying line (2), a petroleum coke conveying line (3), a mixed molten salt conveying line (4), and a chlorine conveying line (5) whose output ends are connected to the chlorination furnace (1). The heat exchange unit (6) is used to exchange heat between low-temperature air and high-temperature aluminum trichloride gas. It includes a heat exchange shell (601) and a plurality of heat exchange tubes (602) suspended in the heat exchange shell (601). The bottom wall of the heat exchange shell (601) gradually slopes upward in a direction away from the chlorination furnace (1) so that the molten salt carried in the aluminum trichloride is cooled and flows back to the chlorination furnace (1). Buffer unit (7) is used to buffer aluminum trichloride and the molten salt it carries from heat exchange unit (6) in order to separate the molten salt from aluminum trichloride; and crystallization unit (8), used to crystallize gaseous aluminum trichloride from buffer unit (7); The alumina conveying line (2) includes an alumina storage tank (201), a number of alumina intermediate silos (202), and an alumina switching valve (203) for connecting the alumina storage tank (201) to any one of the alumina intermediate silos (202). The petroleum coke conveying line (3) includes a petroleum coke storage tank (301), a number of petroleum coke intermediate silos (302), and a petroleum coke switching valve (303) for connecting the petroleum coke storage tank (301) with any one of the petroleum coke intermediate silos (302). The chlorination furnace (1) is provided with a mixing chamber (9) at its feed inlet. The mixing chamber (9) is provided with a screw feeder (10). Several alumina intermediate chambers (202) correspond one-to-one with several petroleum coke intermediate chambers (302). The outlet ends of the alumina intermediate chambers (202) and the corresponding petroleum coke intermediate chambers (302) are provided with mixing conveying pipelines (209) for conveying the proportionally mixed materials to the mixing chamber (9). The buffer unit (7) includes several rinsing towers (701) arranged in series. The air inlet of the rinsing tower (701) at the first end is connected to the material outlet of the heat exchange unit (6), and the air outlet of the rinsing tower (701) at the last end is connected to the crystallization unit (8). A conveying pipeline (14) is provided between the washing tower (701) and the crystallization unit (8). A heat preservation mechanism (15) is installed on the conveying pipeline (14). The output end of the heat preservation mechanism (15) is connected to the heated air outlet of the heat exchange unit (6).

2. The anhydrous aluminum trichloride production system according to claim 1, characterized in that: The mixed molten salt conveying line (4) includes a molten salt circulation vessel (401), a molten salt heating furnace (402) for heating the molten salt circulation vessel (401), and a first conveying pump (403) for conveying the mixed molten salt in the molten salt heating furnace (402) to the chlorination furnace (1).

3. The anhydrous aluminum trichloride production system according to claim 2, characterized in that: A flushing pipeline (11) and a return pipeline (12) are provided between the molten salt circulation vessel (401) and the buffer unit (7). The flushing pipeline (11) is equipped with a second delivery pump (13) for conveying the mixed molten salt in the molten salt circulation vessel (401) to the buffer unit (7) to flush the molten salt adhering to the inner wall of the buffer unit (7).

4. The anhydrous aluminum trichloride production system according to claim 1, characterized in that: The heat exchange tube (602) includes an inner tube (6021) and an outer tube (6022) sleeved outside the inner tube (6021). The top of the inner tube (6021) is connected to the low-temperature air inlet on the heat exchange shell (601), and the bottom is connected to the inner cavity of the outer tube (6022). The top of the outer tube (6022) is connected to the heated air outlet of the heat exchange shell (601).

5. The anhydrous aluminum trichloride production system according to claim 1, characterized in that: The alumina intermediate silo (202) outlet and the mixing conveying pipeline (209) are sequentially provided with a first pneumatic butterfly valve (204), a first fast feeding mechanism (205), a first slow feeding mechanism (206), an alumina loss-in-weight scale (207) and a first pneumatic flap valve (208). Between the outlet of the petroleum coke intermediate silo (302) and the mixing and conveying pipeline (209), a second pneumatic butterfly valve (304), a second fast feeding mechanism (305), a second slow feeding mechanism (306), a petroleum coke loss-in-weight scale (307), and a second pneumatic flap valve (308) are sequentially provided.

6. The anhydrous aluminum trichloride production system according to claim 1, characterized in that: The production system also includes: The dust collector (16) has its inlet connected to the crystallization unit (8) for collecting the remaining material in the crystallization unit (8); The exhaust gas buffer tank (17) has its inlet connected to the dust collector (16) to balance the system pressure; And a salt discharge box (18), whose inlet is connected to the chlorination furnace (1) for the transfer of remaining materials in the chlorination furnace (1).

7. The anhydrous aluminum trichloride production system according to claim 1, characterized in that: The crystallization unit (8) includes several crystallizers (801) and several air hammers (802) for striking the crystallizers (801). Each crystallizer (801) is provided with a third pneumatic butterfly valve (803), a discharge buffer tank (804), a fourth pneumatic butterfly valve (805), a turnover bucket (806), and a weighing device (807) in sequence at its outlet.

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