A superheated steam coal humidity control device and method for producing crystalline carbon precursor

Abstract

The present invention relates to a superheated steam coal humidity control device and method for producing a crystalline carbon precursor, the device comprises a material transportation path composed of a pulverizer, a screening machine, a hopper, an inner tube of a telescopic transport pipe, a drying tower, a spiral conveyor belt and a coking oven connected in sequence, and a steam circulation path composed of a waste heat recovery device of the coking oven, a waste heat recovery pipeline, an outer tube of a telescopic transport pipe, a condensed water pipeline, a steam generator, a steam pipeline, a superheater, an superheated steam pipeline and a drying tower connected in sequence. The method comprises a material transportation process: after the coking coal is pulverized and screened, it passes through the inner tube of the telescopic transport pipe and the raw material conveying pipeline and enters the spiral conveyor belt in the drying tower, and is dried by absorbing water in the process of being transported to the bottom of the tower; a steam circulation process: the waste heat of the coking oven is condensed through the outer tube of the telescopic transport pipe, heated by the steam generator and the superheater to form superheated steam and enter the drying tower. The present invention can ensure that the humidity of the raw coal after the coal humidity control process is less than 6%.

Description

Technical Field

[0001] The present invention belongs to the technical field of coal humidity control, and in particular relates to a superheated steam coal humidity control device and method for producing a crystalline carbon precursor. Background Art

[0002] Crystalline carbon precursor refers to the precursor material used to produce crystalline carbon, including amorphous, plate-shaped, flaky, spherical or fibrous natural graphite or artificial graphite or a combination thereof, soft carbon, hard carbon, carbonization product of mesophase pitch, sintered coke or a combination thereof. Sintered coke powder is an ideal crystalline carbon precursor, but in the process of preparing sintered coke powder from coal, due to the high water content of coal, the sintering process of coal coke powder often leads to high energy consumption, large wastewater discharge and poor quality of the obtained coke powder. Therefore, in actual operation, a step of coal moisture control technology is often added before sintering. Coal moisture control technology (coal moisture control, CMC) is the abbreviation of "coal moisture control process for charging furnace", that is, to remove part of the moisture of coking coal before charging, keep the moisture of charging coal controlled at about 6%, and then charge the furnace for coking production. Coal moisture control technology is different from coal preheating and coal drying. It has strict moisture control measures to ensure the constant moisture of coke oven coal.

[0003] The existing coal moisture control technology mainly includes direct heat exchange type coal moisture control technology, composite bed coal moisture control technology, indirect coal moisture control technology, etc. Coal moisture control technology can control the moisture content of the coal charged to the furnace at about 6%, effectively reduce the total energy consumption of coking, increase the coke output, improve the quality of coke, increase the proportion of weakly cohesive coal, and reduce coking wastewater. However, the existing coal moisture control technology also has certain shortcomings. After the moisture content of the coal is reduced, the dust in the transportation and coal loading process increases by about 1 times, the graphite formation of the carbonization chamber furnace wall and the riser is accelerated, and the slag content in the crude tar increases.

[0004] Superheated steam drying technology is an ideal drying technology. Since there is a reversal point in superheated steam drying, the drying rate of superheated steam drying is faster than that of traditional drying methods. In addition, due to the presence of steam, dust can be effectively reduced during the coking process, thereby slowing down the rate of graphite deposition on the furnace wall and riser of the carbonization chamber. However, superheated steam drying technology has not yet been used in the coal moisture control process. The main difficulty is that hot steam drying requires high airtightness of the equipment, while the coking coal feeding process causes the airtightness of the equipment to drop significantly. In addition, the temperature of superheated steam is above 100°C, while the temperature of coking coal raw materials is only the ambient temperature. In the early stage of the material entering the equipment, energy exchange often occurs, resulting in steam condensation, which increases the moisture content of the material and reduces the effect of the moisture control process.

[0005] However, the existing coal moisture control technology leads to increased dust pollution, accelerated graphite formation on the furnace wall and riser of the carbonization chamber, and uneven quality of coke powder, which in turn leads to high cost and unstable quality of crystalline carbon prepared from the obtained coking coal powder. Summary of the invention

[0006] The present invention aims to address the problems in existing coal moisture control technologies, such as increased dust pollution, accelerated graphite formation on the furnace wall and riser of the carbonization chamber, and uneven quality of coke powder after the moisture content of coal is reduced, as well as the problem that when using superheated steam drying technology to control coal moisture, the airtightness of the equipment is greatly reduced due to the coking coal feeding process, and the moisture content of the material is increased due to heat exchange between the coking coal raw materials and the superheated steam, thereby reducing the effect of the moisture control process. The present invention provides a superheated steam coal moisture control device and method for the production of crystalline carbon precursors, and uses superheated steam drying technology to control coal moisture to overcome the above-mentioned problems.

[0007] In order to solve the above technical problems, the present invention adopts the following technical solutions:

[0008] A superheated steam coal humidity control device for producing a crystalline carbon precursor, comprising a coking oven, wherein the device further comprises a pulverizer, a screening machine, a hopper, a sleeve-type transport pipe, a drying tower, a spiral conveyor belt, a steam generator, a superheater, a material conveying pipeline, a waste heat recovery pipeline, a condensate pipeline, a steam pipeline and a superheated steam pipeline, wherein the sleeve-type transport pipe comprises an outer cylinder and an inner pipe arranged therein, the pulverizer outlet is connected to the screening machine inlet, the screening machine outlet is connected to the hopper inlet, the hopper outlet is connected to the inlet of the inner pipe of the sleeve-type transport pipe, the outlet of the inner pipe is connected to the feed inlet of the drying tower through a material conveying pipeline, the spiral conveyor belt is arranged in the drying tower, the upper end and the lower end of the spiral conveyor belt are respectively connected to the feed inlet and the discharge port of the drying tower, the discharge port of the drying tower is connected to the inlet of the coking oven through a raw material conveying pipeline, and thus a material transport path is formed;

[0009] The waste heat recovery device of the coke oven is connected to the outer tube of the sleeve-type transport pipe through the waste heat recovery pipeline, the outlet of the outer tube of the sleeve-type transport pipe is connected to the inlet of the steam generator through the condensed water pipeline, the outlet of the steam generator is connected to the inlet of the superheater through the steam pipeline, the outlet of the superheater is connected to the steam inlet arranged at the bottom of the drying tower through the hot steam pipeline, and the steam outlet arranged at the top of the drying tower is connected to the inlet of the steam generator through the condensed water pipeline, forming a steam circulation path. The sleeve-type transport pipe is adopted, the inner tube is in the material transportation path, and the outer tube is in the steam circulation path. The waste heat steam of the outer tube indirectly heats the coking coal raw material in the inner tube, increases the material temperature, so that the temperature of the material is already high when entering the drying tower, and will not cause a large amount of condensation of superheated steam, solves the problem of superheated steam condensation, thereby improving the effect of coal moisture adjustment, and can ensure that the raw coal humidity after the coal moisture adjustment process is less than 6%, while reducing the generation of dust during the coking process.

[0010] Furthermore, the spiral conveyor is spiral from top to bottom, and a feed valve and a discharge valve are respectively provided at the feed port and the discharge port of the drying tower; a flow valve is provided on the material conveying pipeline in front of the feed valve. The spiral conveyor can make the coking raw materials fully contact with the superheated steam in the drying tower, be dried by water absorption, and have a good drying effect.

[0011] Furthermore, the feed valve and the discharge valve are both spiral gate valves, and the flow valve is a palate gate, a fan gate or a gate valve. The spiral gate valve has a good sealing effect and can ensure the airtightness of the drying tower. The above flow valve can be used to conveniently control the transportation speed of the coking raw materials.

[0012] Furthermore, the drying tower is a vertical drying tower, and the spiral conveyor belt is connected to the feed port and the discharge port of the drying tower through a seal. The vertical drying tower can make the coking raw materials fully contact with the superheated steam in the drying tower, be dried by water absorption, and have a good drying effect.

[0013] Furthermore, the sealing member is a flange or a sealing ring. The flange or the sealing ring is selected for sealing, which has a good sealing effect and is convenient for maintenance and overhaul.

[0014] Furthermore, the outer tube of the sleeve-type transport tube is a hollow annular cylinder.

[0015] Furthermore, the outer surfaces of the waste heat recovery pipe, condensed water pipe, steam pipe and superheated steam pipe are all provided with a thermal insulation layer. Adding the thermal insulation layer achieves the purpose of energy saving.

[0016] A method for adjusting the humidity of coal using superheated steam for producing a crystalline carbon precursor, the method comprising the following steps:

[0017] (A) Material transportation process: coking coal is sent from the silo to the pulverizer for crushing. After the crushed coking coal particles are screened by the screening machine, the qualified coking coal particles are sent to the hopper as coking raw materials. The coking raw materials are transported to the top of the drying tower through the inner tube of the sleeve-type transport pipe and the raw material conveying pipeline. They enter the starting end of the spiral conveyor belt through the spiral feed valve at the inlet of the drying tower, and are transported to the bottom of the drying tower under the action of the spiral conveyor belt. The coking raw materials that have been dried by water absorption are output from the discharge valve at the outlet of the drying tower and enter the coking oven through the raw material conveying pipeline for coking;

[0018] (B) Steam circulation process: The waste heat and water vapor generated by the coking oven are recovered by the waste heat recovery device, and transported to the outer tube of the sleeve-type transport pipe through the waste heat recovery pipeline for condensation. The condensed water and residual steam after condensation enter the steam generator through the condensed water pipeline to generate steam again. The steam enters the superheater through the steam pipeline and is heated to form superheated steam. The superheated steam enters the bottom of the drying tower through the steam inlet of the drying tower through the superheated steam pipeline, diffuses from the bottom of the drying tower to the top of the drying tower, exchanges energy with the coking raw materials on the spiral conveyor belt and absorbs moisture in the coking raw materials, and finally forms condensed water, which is output from the steam outlet at the top of the drying tower and circulated into the steam generator.

[0019] Furthermore, in the material transportation process (A), the feed valve controls the feed of the drying tower, the flow valve controls the flow of the coking raw material into the drying tower, and the thickness of the coking raw material layer on the conveying surface of the spiral conveyor is controlled to be 30-50mm, preferably 35-45mm, and most preferably 40mm by adjusting the flow rate of the flow valve; the density of the screening machine is 4-10 meshes, so that the particle size of the coking coal particles is less than 5mm; the conveying speed of the spiral conveyor is 0.5-1.5m / min; and the discharge of the drying tower is controlled by the discharge valve. The raw material layer thickness of 30-50mm on the spiral conveyor, the particle size is less than 5mm, and the transmission speed is controlled at 0.5-1.5m / min. Such parameter coordination can accurately control the contact time of the coking raw material with the superheated steam in the drying tower, and the coordination with the superheated steam parameters described below can control the humidity of the coking raw material to be less than 6%.

[0020] Furthermore, in the steam cycle process (B), the steam heating process is as follows: the steam generator heats the incoming condensed water and the remaining steam into boiling water at 100°C, and then continues to heat the boiling water into wet saturated steam. After the wet saturated steam is transmitted to the superheater, the superheater continuously heats the wet saturated steam, and after all the water changes from liquid to gas, it becomes dry saturated steam. The dry saturated steam is continuously heated to become superheated steam, and the temperature of the superheated steam is 130-180°C, preferably 145-165°C, and most preferably 160°C; the steam flow rate is 7-10kg / h, preferably 8.5-9.59kg / h, and most preferably 9kg / h. With the coordination of the above parameters, the humidity of the coking raw materials can be controlled within a range below 6%.

[0021] Compared with the prior art, the present invention has the following beneficial effects:

[0022] 1. In a superheated steam coal humidity control device for producing a crystalline carbon precursor of the present invention, the spiral conveyor belt is connected to the feed port and the discharge port of the drying tower through a seal, and the feed valve and the discharge valve use spiral valves to ensure that the raw material inlet and outlet paths of the drying tower are well sealed. At the same time, the steam inlet and outlet of the drying tower maintain good airtightness due to the existence of air pressure, thereby ensuring that the drying tower has good airtightness.

[0023] 2. The sleeve-type transport pipe is used to preheat the coking raw materials entering the drying tower, so that the temperature of the materials is already high when entering the drying tower, which will not cause a large amount of condensation of superheated steam, thereby improving the effect of coal moisture adjustment and ensuring that the humidity of the raw coal after the coal moisture adjustment process is less than 6%. This solves the problem in the prior art that the temperature of the coking coal raw material is the ambient temperature, and energy exchange occurs at the initial stage of the material entering the equipment, resulting in steam condensation and an increase in the moisture content of the material.

[0024] 3. The superheated steam coal moisture control device and method for producing a crystalline carbon precursor of the present invention utilizes superheated steam drying technology to control the moisture of the coal. The drying rate is faster, and due to the presence of steam, the dust in the coking process can be effectively reduced, thereby slowing down the rate of graphite formation on the furnace wall and riser of the carbonization chamber.

[0025] 4. The drying tower of the present invention adopts a vertical drying tower, which fully guarantees the energy exchange and water absorption efficiency between the superheated steam and the coking raw materials in the drying tower, thereby improving the effect of coal moisture adjustment.

[0026] 5. The present invention utilizes waste heat to achieve energy saving. BRIEF DESCRIPTION OF THE DRAWINGS

[0027] Figure 1 It is a schematic structural diagram of the superheated steam coal humidity control device for producing the crystalline carbon precursor of the present invention.

[0028] Among them, 1-crusher, 2-screener, 3-hopper, 4-sleeve transport pipe, 5-feed valve, 6-drying tower, 7-discharge valve, 8-coking oven, 9-steam generator, 10-superheater, 11-flow valve. DETAILED DESCRIPTION

[0029] The technical solution of the present invention is further described clearly and completely below in conjunction with the accompanying drawings and embodiments. Obviously, the described embodiments are only part of the embodiments of the present invention, rather than all of the embodiments. Based on the embodiments of the present invention, all other embodiments obtained by ordinary technicians in this field without creative work are within the scope of protection of the present invention.

[0030] Example 1

[0031] like Figure 1As shown, a superheated steam coal humidity control device for producing a crystalline carbon precursor comprises a coking oven, a pulverizer, a screening machine, a hopper, a sleeve-type transport pipe, a drying tower, a spiral conveyor belt, a steam generator, a superheater, a material conveying pipeline, a waste heat recovery pipeline, a condensate pipeline, a steam pipeline and a superheated steam pipeline, wherein the sleeve-type transport pipe comprises an outer cylinder and an inner pipe arranged therein, the pulverizer outlet is connected to the screening machine inlet, the screening machine outlet is connected to the hopper inlet, the hopper outlet is connected to the inlet of the inner pipe of the sleeve-type transport pipe, and the outlet of the inner pipe is connected to the inlet of the inner pipe of the sleeve-type transport pipe, and the outlet of the inner pipe passes through the material The material conveying pipeline is connected with the feed inlet of the drying tower, and a feed valve and a discharge valve are respectively provided at the feed inlet and the discharge outlet of the drying tower; a flow valve is provided on the material conveying pipeline in front of the feed valve; the spiral conveyor belt is spiral from top to bottom, arranged in the drying tower, and its upper end and lower end are respectively connected with the feed inlet and the discharge outlet of the drying tower through flanges, and the discharge outlet of the drying tower is connected with the inlet of the coking oven through the raw material conveying pipeline, forming a material transportation path; wherein the flow valve is a palate gate, and the outer tube of the sleeve-type conveying pipe is a hollow annular cylinder.

[0032] The waste heat recovery device of the coking oven is connected to the outer tube of the sleeve-type transport pipe through a waste heat recovery pipeline, the outlet of the outer tube of the sleeve-type transport pipe is connected to the inlet of the steam generator through a condensed water pipeline, the outlet of the steam generator is connected to the inlet of the superheater through a steam pipeline, the outlet of the superheater is connected to the steam inlet arranged at the bottom of the drying tower through a hot steam pipeline, and the steam outlet arranged at the top of the drying tower is connected to the inlet of the steam generator through a condensed water pipeline, forming a steam circulation path.

[0033] Wherein, the waste heat recovery pipeline, condensed water pipeline, steam pipeline and superheated steam pipeline are all provided with insulation layers.

[0034] A method for adjusting the humidity of coal using superheated steam for producing a crystalline carbon precursor comprises the following steps:

[0035] (A) Material transportation process: coking coal is sent from the silo to the pulverizer for crushing. After the crushed coking coal particles are screened by the screening machine, the qualified coking coal particles are sent to the hopper as coking raw materials. The coking raw materials are transported to the top of the drying tower through the inner tube of the sleeve-type transport pipe through the raw material conveying pipeline, and enter the starting end of the spiral conveyor belt through the spiral feed valve at the inlet of the drying tower. Under the action of the spiral conveyor belt, the coking raw materials that have been dried by water absorption are output from the discharge valve at the outlet of the drying tower and enter the coking oven through the raw material conveying pipeline for coking; wherein, the feed valve controls the feed of the drying tower, and the thickness of the coking raw material layer on the conveying surface of the spiral conveyor belt is controlled to be 30 mm by adjusting the flow rate of the flow valve; the density of the screening machine is 4 meshes, so that the particle size of the coking coal particles is less than 5 mm; the conveying speed of the spiral conveyor belt is 0.5 m / min; the discharge of the drying tower is controlled by the discharge valve.

[0036] (B) Steam circulation process: The waste heat and water vapor generated by the coking oven are recovered by the waste heat recovery device, and transported to the outer tube of the sleeve-type transport pipe through the waste heat recovery pipeline for condensation. The condensed water and residual steam after condensation enter the steam generator through the condensed water pipeline to generate steam again. The steam enters the superheater through the steam pipeline and is heated to form superheated steam. The superheated steam enters the bottom of the drying tower through the steam inlet of the drying tower through the superheated steam pipeline, diffuses from the bottom of the drying tower to the top of the drying tower, exchanges energy with the coking raw materials on the spiral conveyor belt and absorbs moisture in the coking raw materials, and finally forms condensed water, which is output from the steam outlet at the top of the drying tower and circulated into the steam generator. The steam heating process is as follows: the steam generator heats the incoming condensed water and the remaining steam into boiling water at 100°C, and then continues to heat the boiling water to become wet saturated steam. After the wet saturated steam is transmitted to the superheater, the superheater continuously heats the wet saturated steam until all the water changes from liquid to gas to become dry saturated steam. The dry saturated steam is continuously heated to become superheated steam, and the temperature of the superheated steam is 130°C; the steam flow rate is 10kg / h.

[0037] According to the test, the moisture content of the coking raw material after the hot steam coal moisture adjustment in this embodiment is 5%.

[0038] Example 2

[0039] The difference between this embodiment and the superheated steam coal humidity control device for producing a crystalline carbon precursor in embodiment 1 is that:

[0040] The flow valve uses a fan-shaped gate, and the spiral conveyor belt is connected to the feed inlet and discharge port of the drying tower through a sealing ring.

[0041] The difference between this embodiment and the method for adjusting the humidity of coal using superheated steam for producing a crystalline carbon precursor in embodiment 1 is that:

[0042] (A) Material transportation process: the feed valve controls the feed of the drying tower, and the thickness of the coking raw material layer on the conveying surface of the spiral conveyor is controlled to be 40 mm by adjusting the flow rate of the flow valve; the density of the screening machine is 6 meshes to make the particle size of the coking coal less than 5 mm; the conveying speed of the spiral conveyor is 1 m / min; the discharge of the drying tower is controlled by the discharge valve.

[0043] (B) Steam cycle flow: The steam heating process is as follows: the steam generator heats the incoming condensate and the remaining steam into boiling water at 100°C, and then continues to heat the boiling water to become wet saturated steam. After the wet saturated steam is transmitted to the superheater, the superheater continues to heat the wet saturated steam until all the water changes from liquid to gas to become dry saturated steam. The dry saturated steam is continuously heated to become superheated steam, and the temperature of the superheated steam is 145°C; the steam flow rate is 9kg / h.

[0044] According to the test, the moisture content of the coking raw material after the hot steam coal moisture adjustment in this embodiment is 3.9%.

[0045] Example 3

[0046] The difference between this embodiment and the superheated steam coal humidity control device for producing a crystalline carbon precursor in embodiment 1 is that:

[0047] The flow valve is a gate valve.

[0048] The difference between this embodiment and the method for adjusting the humidity of coal using superheated steam for producing a crystalline carbon precursor in embodiment 1 is that:

[0049] (A) Material transportation process: the feed valve controls the feed of the drying tower, and the thickness of the coking raw material layer on the conveying surface of the spiral conveyor is controlled to be 35 mm by adjusting the flow rate of the flow valve; the density of the screening machine is 8 meshes to make the particle size of the coking coal less than 5 mm; the conveying speed of the spiral conveyor is 1.0 m / min; the discharge of the drying tower is controlled by the discharge valve.

[0050] (B) Steam cycle flow: The steam heating process is as follows: the steam generator heats the incoming condensate and the remaining steam into boiling water at 100°C, and then continues to heat the boiling water to become wet saturated steam. After the wet saturated steam is transmitted to the superheater, the superheater continuously heats the wet saturated steam until all the water changes from liquid to gas to become dry saturated steam. The dry saturated steam is continuously heated to become superheated steam, and the temperature of the superheated steam is 160°C; the steam flow rate is 8.5kg / h.

[0051] According to the test, the moisture content of the coking raw material after the hot steam coal moisture adjustment in this embodiment is 5.9%.

[0052] Example 4

[0053] The superheated steam coal humidity control device for producing a crystalline carbon precursor in this embodiment is the same as that in Example 1.

[0054] The difference between this embodiment and the method for adjusting the humidity of coal using superheated steam for producing a crystalline carbon precursor in embodiment 1 is that:

[0055] (A) Material transportation process: the feed valve controls the feed of the drying tower, and the thickness of the coking raw material layer on the conveying surface of the spiral conveyor is controlled to be 45 mm by adjusting the flow rate of the flow valve; the density of the screening machine is 8 meshes to make the particle size of the coking coal less than 5 mm; the conveying speed of the spiral conveyor is 1.2 m / min; the discharge of the drying tower is controlled by the discharge valve.

[0056] (B) Steam cycle flow: The steam heating process is as follows: the steam generator heats the incoming condensate and the remaining steam into boiling water at 100°C, and then continues to heat the boiling water to become wet saturated steam. After the wet saturated steam is transmitted to the superheater, the superheater continuously heats the wet saturated steam until all the water changes from liquid to gas to become dry saturated steam. The dry saturated steam is continuously heated to become superheated steam, and the temperature of the superheated steam is 165°C; the steam flow rate is 9.59 kg / h.

[0057] According to the test, the moisture content of the coking raw material after the hot steam coal moisture adjustment in this embodiment is 3.6%.

[0058] Example 5

[0059] The superheated steam coal humidity control device for producing a crystalline carbon precursor in this embodiment is the same as that in Example 1.

[0060] The difference between this embodiment and the method for adjusting the humidity of coal using superheated steam for producing a crystalline carbon precursor in embodiment 1 is that:

[0061] (A) Material transportation process: the feed valve controls the feed of the drying tower, and the thickness of the coking raw material layer on the conveying surface of the spiral conveyor is controlled to be 50 mm by adjusting the flow rate of the flow valve; the density of the screening machine is 10 mesh so that the particle size of the coking coal particles is less than 5 mm; the conveying speed of the spiral conveyor is 1.5 m / min; the discharge of the drying tower is controlled by the discharge valve.

[0062] (B) Steam cycle flow: The steam heating process is as follows: the steam generator heats the incoming condensate and the remaining steam into boiling water at 100°C, and then continues to heat the boiling water to become wet saturated steam. After the wet saturated steam is transmitted to the superheater, the superheater continuously heats the wet saturated steam until all the water changes from liquid to gas to become dry saturated steam. The dry saturated steam is continuously heated to become superheated steam, and the temperature of the superheated steam is 180°C; the steam flow rate is 7kg / h.

[0063] According to the test, the moisture content of the coking raw material after the hot steam coal moisture adjustment in this embodiment is 4.2%.

[0064] Although the present invention has been described in detail with reference to the aforementioned embodiments, it is still possible for those skilled in the art to modify the technical solutions described in the aforementioned embodiments, or to make equivalent substitutions for some of the technical features therein. Any modifications, equivalent substitutions, improvements, etc. made within the spirit and principles of the present invention should be included in the protection scope of the present invention.

Claims

1. A superheated steam coal humidity control device for producing a crystalline carbon precursor, comprising a coking oven, characterized in that: It also includes a crusher, a screener, a hopper, a sleeve-type transport pipe, a drying tower, a spiral conveyor belt, a steam generator and a superheater. The sleeve-type transport pipe includes an outer tube and an inner tube arranged therein. The crusher outlet is connected to the screener inlet, the screener outlet is connected to the hopper inlet, the hopper outlet is connected to the inlet of the inner tube of the sleeve-type transport pipe, the outlet of the inner tube is connected to the feed inlet of the drying tower through a material conveying pipeline, the spiral conveyor belt is arranged in the drying tower, and its upper end and lower end are respectively connected to the feed inlet and the discharge port of the drying tower, and the discharge port of the drying tower is connected to the inlet of the coke oven through a raw material conveying pipeline, so as to form a material transportation path; The waste heat recovery device of the coke oven is connected to the outer tube of the sleeve-type transport pipe through a waste heat recovery pipeline, the outlet of the outer tube of the sleeve-type transport pipe is connected to the inlet of the steam generator through a condensed water pipeline, the outlet of the steam generator is connected to the inlet of the superheater through a steam pipeline, the outlet of the superheater is connected to the steam inlet arranged at the bottom of the drying tower through a hot steam pipeline, and the steam outlet arranged at the top of the drying tower is connected to the inlet of the steam generator through a condensed water pipeline, forming a steam circulation path; The spiral conveyor belt is spiral from top to bottom, and a feed valve and a discharge valve are respectively provided at the feed port and the discharge port of the drying tower; a flow valve is provided on the material conveying pipeline in front of the feed valve; The drying tower is a vertical drying tower, and the spiral conveyor belt is connected to the feed inlet and the discharge outlet of the drying tower through a sealing member.

2. The superheated steam coal humidity control device for producing a crystalline carbon precursor according to claim 1, characterized in that: The feed valve and the discharge valve are both spiral gate valves, and the flow valve is a palatal gate, a fan gate or a plug valve.

3. The superheated steam coal humidity control device for producing a crystalline carbon precursor according to claim 1, characterized in that: The sealing element is a flange or a sealing ring.

4. The superheated steam coal humidity control device for producing a crystalline carbon precursor according to claim 1, characterized in that: The outer tube of the sleeve-type transport tube is a hollow annular cylinder.

5. The superheated steam coal humidity control device for producing a crystalline carbon precursor according to claim 1, characterized in that: The outer surfaces of the waste heat recovery pipeline, condensed water pipeline, steam pipeline and superheated steam pipeline are all provided with insulation layers.

6. A method for utilizing a superheated steam coal humidity control device for producing a crystalline carbon precursor according to any one of claims 1 to 5, characterized in that: The method comprises the following steps: (A) Material transportation process: coking coal is sent from the silo to the pulverizer for crushing. After the crushed coking coal particles are screened by the screening machine, the qualified coking coal particles are sent to the hopper as coking raw materials. The coking raw materials pass through the inner tube of the sleeve-type transport pipe and are transported to the top of the drying tower through the raw material conveying pipeline. They enter the starting end of the spiral conveyor belt through the spiral feed valve at the inlet of the drying tower and are transported to the bottom of the drying tower under the action of the spiral conveyor belt. The coking raw materials that have been dried by water absorption are output from the discharge valve at the outlet of the drying tower and enter the coking oven through the raw material conveying pipeline for coking; (B) Steam circulation process: The waste heat and water vapor generated by the coking oven are recovered by a waste heat recovery device, transported to the outer tube of the sleeve-type transport pipe through a waste heat recovery pipeline for condensation, and the condensed water and residual steam after condensation enter the steam generator through a condensed water pipeline to generate steam again, and the steam enters the superheater through a steam pipeline and is heated to form superheated steam, and the superheated steam enters the bottom of the drying tower through the steam inlet of the drying tower through the superheated steam pipeline, diffuses from the bottom of the drying tower to the top of the tower, exchanges energy with the coking raw materials on the spiral conveyor belt and absorbs moisture in the coking raw materials, and finally forms condensed water, which is output from the steam outlet at the top of the drying tower and circulated into the steam generator; In the material transportation process (A), the feed valve controls the feed of the drying tower, the flow valve controls the flow of the coking raw material into the drying tower, and the thickness of the coking raw material layer on the conveying surface of the spiral conveyor is controlled to be 30-50 mm by adjusting the flow rate of the flow valve; the density of the screening machine is 4-10 meshes, so that the particle size of the coking coal particles is less than 5 mm; the conveying speed of the spiral conveyor is 0.5-1.5 m / min; the discharge of the drying tower is controlled by the discharge valve; In the (B) steam cycle process, the steam heating process is as follows: the steam generator heats the incoming condensed water and the remaining steam into boiling water at 100°C, and then continues to heat the boiling water to become wet saturated steam. After the wet saturated steam is transmitted to the superheater, the superheater continuously heats the wet saturated steam, and after all the water changes from liquid to gas, it becomes dry saturated steam. The dry saturated steam is continuously heated to become superheated steam, and the temperature of the superheated steam is 130-180°C; the steam flow rate is 7-10kg / h.

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