Device and method for directly preparing coke from weakly caking coal

Abstract

The invention discloses a device and a method for directly preparing coke from weakly caking coal, and belongs to the technical field of coal mineral processing. The device comprises a fluidized bed, a dryer, a hot gas-solid separator, a dry distillation kettle and a cooling device, pulverized coal enters the fluidized bed through a pulverized coal injection tank, carbon monoxide and water vapor enter the fluidized bed through a gas flow nozzle at the bottom of the fluidized bed, two gas flows reversely collide and then enter a catalyst layer, reaction gas is activated, active hydrogen substances are generated, the activated gas serves as fluidizing gas to fluidize the pulverized coal added into the fluidized bed, and tackifying modification is conducted in the fluidized bed; in addition, a tar spraying device is arranged at the top of the fluidized bed, so that the pulverized coal can be secondarily tackified; according to the device and the method, the problems of difficulty in tackifying and discharging of the pulverized coal and discontinuous production process are solved, and a novel device and a novel method are provided for directly preparing coke from the weakly caking coal.

Description

Technical Field

[0001] The invention belongs to the technical field of coal mineral processing, and in particular relates to a device and method for directly preparing coke from weakly sticky coal. Background Art

[0002] With the gradual depletion of high-quality coal resources, the development and utilization of weakly caking coals have received increasing attention. These weakly caking coals cannot form sufficient bonding force during the coking process, resulting in the inability to effectively bond the coal particles, thus failing to form high-strength coke, such as anthracite and lean coal. On the other hand, at high temperatures, the fluidity of weakly caking coals is poor, resulting in the inability to form a good plastic state during the coking process, further affecting the formation of coke. Existing coking technologies and equipment are mostly aimed at coals with good bonding properties, and the use of weakly caking coals requires new technologies and equipment improvements. If weakly caking coals are directly used to prepare coke through viscosity-enhancing modification technology, not only the utilization rate of weakly caking coals is improved, but also the coking cost can be reduced.

[0003] Chinese patent CN118179422A discloses "a coal modification and thickening reaction device and method", which injects uniformly mixed coal powder, water, and catalyst into a reactor, injects CO gas, turns on a stirrer to stir the materials, and heats up to a preset temperature to thicken and modify the coal powder. After the reaction is completed, all valves are closed, cooled to room temperature, the remaining gas in the kettle is discharged, and then the blind plug in the kettle is opened for solid-liquid separation. The solid product obtained by separation is the modified thickening coal that can be used for coking. The catalyst of the present invention enters the modified coal, increases the ash content of the coal, and thus affects the quality of the thickening coal. In addition, the reaction is in one reactor, and the coal agglomerates after cooling after thickening, which has the problem of difficulty in discharging, and continuous production cannot be achieved.

[0004] Chinese patent CN103113909A discloses "a method for modifying and thickening low-rank coal". This method mixes low-rank coal, solvent water and catalyst evenly and places them in a high-pressure reactor, introduces reducing gas, heats to 380 °C for modification, cools to room temperature after the reaction is completed for solid-liquid separation, and the solid product obtained by separation is the modified thickening coal that can be used for coking. The catalyst contains a promoter S, and the catalyst enters the modified coal, which not only increases the ash content of the coal, but also increases its sulfur content, thereby affecting the quality of the thickening coal. In addition, the reaction is in one reactor, and the coal agglomerates after cooling after thickening, which has the problem of difficult discharge, and continuous production cannot be achieved.

[0005] Chinese patent CN103113909A discloses "a device for converting coke oven flue gas into weakly sticky coal using waste heat". The device passes coke oven flue gas with waste heat into a fluidized bed, and uses a feeder to feed weakly sticky coal into the bottom of the fluidized bed. The coal powder at the bottom is heated by the coke oven flue gas and fluidized and modified. Finally, the sticky coal is discharged from the bottom of the fluidized bed through a discharger. The feed port and discharge port of the fluidized bed are both located at the bottom, so it is impossible to feed during discharge, and the production process is discontinuous. At the same time, since it is modified only by temperature, the sticky effect is not significant.

[0006] Chinese patent CN111411007A discloses "a method for producing coking coal by hydrogenation of low-rank coal catalyzed by Ca". In this method, low-rank coal powder, water and Ca-based catalyst are added into a reactor and evenly mixed, a certain proportion of carbon monoxide and nitrogen mixture is introduced into the reactor, and the temperature is raised to a set temperature for viscosity modification. After the reaction is completed, the reactor is cooled to room temperature, and the solid and liquid are separated. The obtained solid product is a highly adhesive coal that can partially replace coking coal. Due to the coal agglomeration after the reaction, there is a problem of difficulty in discharging, and continuous production cannot be achieved.

[0007] Although many methods for coking weakly sticky coal have been disclosed, there are few reports on devices for implementing these processes; in particular, there is a lack of a device and method for directly making coke from weakly sticky coal with a continuous production process, uniform material mixing and sufficient reaction. Summary of the invention

[0008] The present invention overcomes the shortcomings of the prior art and proposes a device and method for directly preparing coke from weakly caking coal, so as to more effectively improve the viscosity-enhancing effect of weakly caking coal. The present invention is achieved through the following technical solutions: A device for directly making coke from weakly sticky coal, comprising a fluidized bed, a dryer, a hot gas-solid separator, a retort and a cooling device; the top outlet of the fluidized bed is connected to the inlet of the dryer, the outlet of the dryer is connected to the inlet of the hot gas-solid separator, the solid phase outlet of the hot gas-solid separator is connected to the retort; the outlet of the retort is connected to the cooling device; The interior of the fluidized bed is divided into two parts, the upper part is provided with a tar nozzle, a coal powder injection tank, a coal crushing blade, a shaft rod, a servo motor, and an upper variable diameter gas distribution plate; the lower part is provided with a lower variable diameter gas distribution plate, a carbon monoxide airflow nozzle, and a water vapor airflow nozzle; The tar nozzle is arranged on the top of the fluidized bed and connected to the tar spraying device; the tar nozzle includes a tar channel and a water vapor channel, the tar channel is located in the middle, the water vapor channels are symmetrically arranged on both sides of the tar channel in a downwardly inclined shape, and are connected to the tar channel; the water vapor channel is provided with a C-shaped branch; the water vapor heats and atomizes the tar through the first inclined outlet, and the second inclined outlet performs secondary atomization on the descending tar; The pulverized coal injection tanks are symmetrically and fixedly connected to both sides of the fluidized bed wall; The coal crushing blade is fixedly connected to the shaft rod, the shaft rod is rotatably connected to the center of the upper variable diameter gas distribution plate, and the shaft rod is electrically connected to the servo motor; The upper variable diameter gas distribution plate is arranged in contact with the upper surface of the catalyst layer, and the lower variable diameter gas distribution plate is arranged in contact with the lower surface of the catalyst layer; the upper variable diameter gas distribution plate and the lower variable diameter gas distribution plate have the same structure, both of which have a large lower aperture and a small upper aperture, and the upper and lower apertures are both smaller than the diameter of the catalyst in the catalyst layer; A plurality of carbon monoxide airflow nozzles are evenly and fixedly connected to the wall of the fluidized bed, one of the carbon monoxide airflow nozzle inlets is connected to the gas phase outlet of the cyclone separator, and the other is connected to the carbon monoxide pipeline, and the carbon monoxide airflow nozzle is inclined downward to form an angle of 30°-60° with the wall of the fluidized bed; The plurality of water vapor air flow nozzles are evenly and fixedly connected to the wall of the fluidized bed, and the water vapor air flow nozzle is located as a whole below the carbon monoxide air flow nozzle; the water vapor air flow nozzle inlet is connected to the steam generator, and the angle formed by the water vapor air flow nozzle obliquely upward and the wall of the fluidized bed is 20°-30°.

[0009] Furthermore, taking the first steam air flow nozzle on the left side of the fluidized bed as a reference, a steam air flow nozzle is set every 72° counterclockwise rotation around the axis of the fluidized bed, and the longitudinal spacing distance between each steam air flow nozzle is 1 / 4D, and the lateral spacing distance between each steam air flow nozzle is 1 / 5πD, where D is the inner diameter of the fluidized bed.

[0010] Furthermore, taking the first carbon monoxide airflow nozzle on the left side of the fluidized bed as a reference, a carbon monoxide airflow nozzle is arranged every 72° clockwise rotation around the axis of the fluidized bed, and the longitudinal spacing distance of each carbon monoxide airflow nozzle is 1 / 4D, and the lateral spacing distance of each carbon monoxide airflow nozzle is 1 / 5πD.

[0011] Furthermore, the pulverized coal injection tank is located at a height of 1 / 3H from the top of the fluidized bed, where H is the height of the fluidized bed.

[0012] Furthermore, it also includes a gas separation and purification device; the gas phase outlet of the hot gas-solid separator and the gas separation and purification device are connected through a pipeline, and the carbon dioxide outlet of the gas separation and purification device is connected to the cooling medium inlet of the cooling device.

[0013] Furthermore, the cooling medium inlet of the cooling device is also connected to a carbon dioxide pipeline.

[0014] Furthermore, it also includes a cyclone separator; the cooling device production outlet is connected to the cyclone separator, the solid outlet of the cyclone separator 31 produces coke powder, and the gas outlet pipe of the cyclone separator is connected to the carbon monoxide gas flow nozzle.

[0015] Furthermore, it also includes a cooler; the gas product outlet at the top of the dry distillation kettle is connected to the cooler, and the liquid phase outlet of the cooler is connected to a tar delivery pump; and the tar delivery pump is connected to a tar spraying device.

[0016] A method for directly making coke from weakly caking coal, based on the device for directly making coke from weakly caking coal, comprises the following steps: The coal powder is sprayed into the fluidized bed, and carbon monoxide and water vapor are sprayed from the carbon monoxide airflow nozzle and the water vapor airflow nozzle respectively, and the coal crushing blade is started. Multiple carbon monoxide airflow nozzles spray at the same time to form a clockwise vortex downward airflow, and multiple water vapor airflow nozzles spray at the same time to form a counterclockwise vortex upward airflow. The two airflows collide in reverse to enhance the mixing effect, and the mixed air mass is carried by the excess water vapor through the catalyst layer. After the reaction gas is activated and reacted, the active substance is generated to fluidize and thicken the coal powder; At the same time, the tar nozzle is opened to spray tar to increase the viscosity of the fluidized coal powder for the second time; Subsequently, the thickened coal powder is taken out from the top of the fluidized bed and sent to the dryer for drying and dehydration. The thickened coal powder is separated by a hot gas-solid separator and then sent to a retort for coking. The solid product of the retort is cooled by a cooling device, and carbon dioxide is used as the cooling medium of the cooling device. The product of the cooling device is separated and purified, and the gaseous product carbon monoxide is sent to the carbon monoxide gas flow nozzle of the fluidized bed, and the solid product is coke powder.

[0017] The beneficial effects of the present invention compared with the prior art are as follows: 1. The present invention provides a device and method for directly making coke from weakly sticky coal. The sticky coal is extracted from the top of the fluidized bed, and then enters the dry distillation area for coking after drying and hot gas-solid separation. There is no need to stop the machine to discharge the material, which greatly improves the continuity of sticky coking and greatly reduces the energy and time costs.

[0018] 2. Set up multiple water vapor and carbon monoxide airflow nozzles, so that the carbon monoxide gas forms a vortex downward airflow, and the water vapor forms a vortex upward airflow. The two airflows collide in reverse to enhance the mixing effect, and the excess water vapor carries the mixed gas mass through the catalyst layer. Based on the principle of reverse collision to enhance mixing, the two reaction gases are mixed evenly, generating more active hydrogen substances and improving the viscosity-increasing effect.

[0019] 3. By adjusting the aperture of the variable-diameter gas distribution plate, the catalyst layer is fixed between the two plates, which is convenient for catalyst recovery and regeneration; the aperture of the variable-diameter gas distribution plate is large at the bottom and small at the top. When the mixed reaction gas flow passes through the variable-diameter gas distribution plate, the large flow is divided into several small flows, increasing the contact area with the catalyst layer and making the reaction more complete.

[0020] 4. Recover carbon dioxide, another product of the reverse water-gas shift reaction, and utilize the captured carbon dioxide to pass it into the cooling zone. It can serve as a gas cooling medium and react with a portion of unstable coke powder to generate carbon monoxide to supplement the carbon monoxide required for fluidized bed viscosity increase, promote carbon emission reduction and carbon neutrality, and improve coke reactivity and the utilization value of weakly sticky coal. BRIEF DESCRIPTION OF THE DRAWINGS

[0021] Figure 1 It is a schematic diagram of the overall structure of the device for directly producing coke from weakly caking coal according to the present invention; Figure 2 It is a schematic diagram of the structure of the tar nozzle; Figure 3 It is a schematic diagram of the structure of the catalyst layer and the upper and lower variable diameter gas distribution plates; Figure 4 It is a schematic diagram of the structure of the coal crushing blade; Figure 5 yes Figure 1 Schematic diagram of the cross section AA in the figure; the curved arrows in the figure indicate the downward airflow; Figure 6 yes Figure 1 Schematic diagram of the cross section of the middle BB; the curved arrows in the figure indicate the upward airflow; Among them: 2-drying kettle; 3-cooling device; 4-separation and purification device; 10-fluidized bed; 11-tar spraying device; 12-coal powder spraying tank; 13-coal crushing blade; 14-servo motor; 16-catalyst layer; 17-carbon monoxide air flow nozzle; 18-water vapor air flow nozzle; 19-steam generator; 20-dryer; 21-cooler; 22-hot gas-solid separator; 31-cyclone separator; 111-tar delivery pump; 112-tar nozzle; 131-axial rod; 151-upper variable diameter gas distribution plate; 152-lower variable diameter gas distribution plate. DETAILED DESCRIPTION

[0022] In order to make the technical problems, technical solutions and beneficial effects to be solved by the present invention clearer, the present invention is further described in detail in conjunction with the embodiments and the accompanying drawings. It should be understood that the specific embodiments described herein are only used to explain the present invention and are not intended to limit the present invention. The technical solutions of the present invention are described in detail below in conjunction with the embodiments and the accompanying drawings, but the scope of protection is not limited thereto.

[0023] Example 1 See also Figures 1 to 6 This embodiment proposes a device for directly producing coke from weakly sticky coal: it includes a fluidized bed 10 for viscosity modification, a retort 2, a cooling device 3, a cooler 21, a separator 31, a gas separation and purification device 4, a steam generator 19, a dryer 20, and a hot gas-solid separator 22.

[0024] The interior of the fluidized bed 10 is divided into two parts, the upper and lower parts, by the catalyst layer 16. The upper part is provided with a tar nozzle 112, a coal powder injection tank 12, a coal crushing blade 13, an axial rod 131, a servo motor 14, and an upper variable diameter gas distribution plate 151; the lower part is provided with a lower variable diameter gas distribution plate 152, a carbon monoxide gas flow nozzle 17, and a water vapor gas flow nozzle 18. The upper variable diameter gas distribution plate 151 is arranged in contact with the upper surface of the catalyst layer 16, and the lower variable diameter gas distribution plate 152 is arranged in contact with the lower surface of the catalyst layer 16.

[0025] like Figure 2 As shown, the tar nozzle 112 is snapped onto the central axis of the top of the fluidized bed 10 and is connected to the tar spraying device 11 arranged outside the fluidized bed 10; the tar nozzle 112 is roughly in the shape of a "Z" character, including a tar channel and a water vapor channel, the tar channel is located in the middle position, the water vapor channels are symmetrically arranged on both sides of the tar channel in a downwardly inclined state, connected to the tar channel, and the water vapor channel is provided with a "C"-shaped branch; the water vapor heats and atomizes the tar through the first inclined outlet, and the second inclined outlet can perform secondary atomization on the descending tar, so that the tar droplets are more dispersed during spraying, thereby improving the viscosity-increasing effect.

[0026] The pulverized coal injection tank 12 is symmetrically fixedly connected to the left and right sides of the fluidized bed 10 wall, and is located at a height of 1 / 3H from the top of the fluidized bed 10, where H is the height of the fluidized bed 10. The pulverized coal injection tank 12 is used to inject pulverized coal into the upper half of the fluidized bed 10.

[0027] The coal crushing blade 13 is welded to the shaft rod 131, and the shaft rod 131 is rotatably connected to the center of the upper variable diameter gas distribution plate 151, and the shaft rod 131 is electrically connected to the servo motor 14, which is located on one side of the outer wall of the fluidized bed 10. The servo motor 14 drives the coal crushing blade 13 to rotate together with the shaft rod 131.

[0028] like Figure 3 As shown, the length of the coal crushing blade 13 is set to 2 / 5D, which breaks up the large pieces of coal powder that cannot be fluidized and re-fluidizes them; D is the inner diameter of the fluidized bed 10.

[0029] like Figure 4As shown, both sides of the upper variable diameter gas distribution plate 151 and the lower variable diameter gas distribution plate 152 are clamped on the inner wall of the fluidized bed 10, and the upper variable diameter gas distribution plate 151 and the lower variable diameter gas distribution plate 152 have the same structure, both of which have a large lower aperture and a small upper aperture, but the upper and lower apertures are smaller than the diameter of the catalyst in the catalyst layer 16, so that the catalyst is filled in the form of a fixed bed; in addition, the upper variable diameter gas distribution plate 151 and the lower variable diameter gas distribution plate 152 can also separate the large flow stream reaction gas flow into several small streams, increase the contact area between the reaction gas and the catalyst layer 16, make the reaction more complete, and generate more active hydrogen substances.

[0030] like Figure 5 As shown, the carbon monoxide gas flow nozzle 17 is welded to the wall of the fluidized bed 10, one inlet of the carbon monoxide gas flow nozzle 17 is connected to the gas phase outlet of the cyclone separator 31, and the other inlet is connected to the carbon monoxide pipeline, and the angle formed by the carbon monoxide gas flow nozzle 17 and the wall of the fluidized bed 10 is between 30-60°; the angle between the carbon monoxide gas flow nozzle 17 and the radial tangent of the fluidized bed 10 is 36°; taking the first carbon monoxide gas flow nozzle 17 on the left side of the fluidized bed 10 as a reference, a carbon monoxide gas flow nozzle 17 is arranged every 72° clockwise rotation around the axis, and the longitudinal spacing distance of each carbon monoxide gas flow nozzle 17 is 1 / 4D, and the lateral spacing distance of each carbon monoxide gas flow nozzle 17 is 1 / 5πD.

[0031] like Figure 6 As shown, the water vapor airflow nozzle 18 is welded to the wall of the fluidized bed 10, and the water vapor airflow nozzle 18 is located as a whole below the carbon monoxide airflow nozzle 17; the inlet of the water vapor airflow nozzle 18 is connected to the steam generator 19, and the angle formed by the water vapor airflow nozzle 18 and the wall of the fluidized bed 10 is between 20-30°, and the angle between the water vapor airflow nozzle 18 and the radial tangent of the fluidized bed 10 is 36°; taking the first water vapor airflow nozzle 18 on the left side of the fluidized bed as a reference, a water vapor airflow nozzle 18 is set every 72° counterclockwise rotation around the axis, and the longitudinal spacing distance of each water vapor airflow nozzle 18 is 1 / 4D, and the lateral spacing distance of each water vapor airflow nozzle 18 is 1 / 5πD.

[0032] By adopting the above technical scheme, when the coal powder is sprayed into the fluidized bed 10, carbon monoxide and water vapor are sprayed at the same time, and the coal crushing blade is started, the five carbon monoxide airflow nozzles 17 spray at the same time to form a clockwise vortex downward airflow, and the five water vapor airflow nozzles 18 spray at the same time to form a counterclockwise vortex upward airflow. The two airflows collide in reverse to enhance the mixing effect, and the excess water vapor carries the mixed air mass through the catalyst layer 16. After the reaction gas is activated and reacted, active hydrogen, carbon dioxide and other substances are generated to fluidize and thicken the coal powder; in addition, the tar nozzle 112 sprays tar on the fluidized coal powder for secondary thickening, so as to achieve the thickening modification of the weakly sticky coal powder.

[0033] like Figure 1 As shown, the retort 2 is fixedly connected to the cooling device 3. The temperature of the retort 2 is 800-1050°C.

[0034] The top outlet of the fluidized bed 10 is connected to the inlet of the dryer 20, the outlet of the dryer 20 is connected to the inlet of the hot gas-solid separator 22, the solid phase outlet of the hot gas-solid separator 22 is connected to the retort 2, the gas phase outlet of the hot gas-solid separator 22 is connected to the gas separation and purification device 4 through a pipeline, and the carbon dioxide outlet of the gas separation and purification device 4 is connected to the bottom of the cooling device 3.

[0035] The cooling device 3 is also connected to the captured carbon dioxide pipeline.

[0036] The extraction port of the cooling device 3 is connected to the cyclone separator 31, the solid outlet of the cyclone separator 31 extracts coke powder, and the gas outlet pipeline is connected to the carbon monoxide gas flow nozzle 17; The gas product outlet at the top of the dry distillation kettle 2 is connected to the cooler 21, and the liquid phase outlet of the cooler 21 is connected to the tar delivery pump 111. The tar delivery pump 111 is connected to the tar spraying device 11. The gas phase outlet of the cooler 21 produces coke oven gas.

[0037] The coal powder is sprayed into the fluidized bed 10, and carbon monoxide and water vapor are sprayed into the fluidized bed 10 at the same time. The coal crushing blade 13 is started, and the five carbon monoxide airflow nozzles 17 are sprayed at the same time to form a clockwise vortex downward airflow. The five water vapor airflow nozzles 18 are sprayed at the same time to form a counterclockwise vortex upward airflow. The two airflows collide in reverse to enhance the mixing effect, and the excess water vapor carries the mixed air mass through the catalyst layer 16. After the reaction gas is activated and reacted, active hydrogen and other substances are generated to fluidize and thicken the coal powder. In addition, the tar nozzle 112 sprays tar to perform secondary viscosity enhancement on the fluidized coal powder.

[0038] Subsequently, the thickened coal powder is taken out from the top of the fluidized bed 10 and sent to the dryer 20 for drying and dehydration, and the thickened coal powder is separated out through the hot gas-solid separator 22, and then the thickened coal powder is sent to the retort 2 for coking, and the gaseous product of the retort 2 is cooled by the cooler 21 to separate the liquid tar, which is sent to the tar nozzle 112 for atomization spraying through the tar delivery pump 111; the solid product of the retort 2 is cooled by the cooling device 3, and its cooling medium is carbon dioxide, part of which comes from the gas separation and purification device 4, and the other part comes from the captured carbon dioxide, the product carbon monoxide of the cooling device 3 is taken out and sent to the cyclone separator 31, and the separated and purified gaseous product carbon monoxide is sent to the carbon monoxide gas flow nozzle 17 of the fluidized bed 10, and the solid product is coke powder.

[0039] Example 2 This embodiment proposes a method for directly preparing coke from weakly caking coal. The device for directly preparing coke from weakly caking coal described in Example 1 is used to carry out a coal modification test using lignite as raw material.

[0040] The lignite was screened using a 150-mesh sieve, wherein the lignite input amount was 20 g, the catalyst input amount was 0.17 g, the flow rate of the single steam airflow nozzle 18 was 127 mL / min, the flow rate of the single carbon monoxide airflow nozzle 17 was 106 mL / min, the tar spraying amount was 50 mL, the reaction temperature was 330 °C, the reaction pressure was 4.5 MPa, and the reaction time was 60 min. After the reaction was completed, the thickened coal powder was naturally cooled to room temperature and taken out.

[0041] The modified coal was measured using a bonding index tester in accordance with GB / T 5447-2014, and the bonding index of the product was 96.

[0042] Example 3 This embodiment proposes a method for directly preparing coke from weakly caking coal. The device for directly preparing coke from weakly caking coal described in Example 1 is used to carry out a coal modification test using long flame coal as raw material.

[0043] The long flame coal was screened with a 150-mesh sieve, wherein the long flame coal input amount was 20 g, the catalyst input amount was 0.25 g, the flow rate of the single steam air flow nozzle 18 was 104 mL / min, the flow rate of the single carbon monoxide air flow nozzle 17 was 87 mL / min, the tar spraying amount was 50 mL, the reaction temperature was 340 °C, the reaction pressure was 3.7 MPa, and the reaction time was 60 min. After the reaction was completed, the thickened coal powder was naturally cooled to room temperature and taken out.

[0044] The modified coal was measured using a bonding index tester in accordance with GB / T 5447-2014, and the bonding index of the product was 91.

[0045] Example 4 This embodiment proposes a method for directly preparing coke from weakly caking coal. The device for directly preparing coke from weakly caking coal described in Example 1 is used to carry out a coal modification test using lean coal as raw material.

[0046] The lean coal was screened with a 150-mesh sieve, wherein the lean coal input amount was 20 g, the catalyst input amount was 0.5 g, the single steam air flow nozzle 18 had a flow rate of 104 mL / min, the single carbon monoxide air flow nozzle 17 had a flow rate of 87 mL / min, the tar spraying amount was 50 mL, the reaction temperature was 350 °C, the reaction pressure was 3.7 MPa, and the reaction time was 60 min. After the reaction was completed, the thickened coal powder was naturally cooled to room temperature and taken out.

[0047] The modified coal was measured using a bonding index tester in accordance with GB / T 5447-2014, and the bonding index of the product was 65.

[0048] Example 5 This embodiment proposes a method for directly preparing coke from weakly caking coal. The device for directly preparing coke from weakly caking coal described in Example 1 is used to carry out a coal modification test using lean coal as raw material.

[0049] The lean coal was screened with a 150-mesh sieve, wherein the lean coal input amount was 20 g, the catalyst input amount was 0.44 g, the single steam air flow nozzle 18 had a flow rate of 113 mL / min, the single carbon monoxide air flow nozzle 17 had a flow rate of 94 mL / min, the tar spraying amount was 50 mL, the reaction temperature was 370 °C, the reaction pressure was 4 MPa, and the reaction time was 60 min. After the reaction was completed, the thickened coal powder was naturally cooled to room temperature and taken out.

[0050] The modified coal was measured using a bonding index tester in accordance with GB / T 5447-2014, and the bonding index of the product was 83.

[0051] Example 6 This embodiment proposes a method for directly preparing coke from weakly caking coal. The device for directly preparing coke from weakly caking coal described in Example 1 is used to carry out a coal modification test using lean coal as raw material.

[0052] The lean coal was screened with a 150-mesh sieve, wherein the lean coal input amount was 20 g, the catalyst input amount was 0.25 g, the single steam air flow nozzle 18 had a flow rate of 113 mL / min, the single carbon monoxide air flow nozzle 17 had a flow rate of 94 mL / min, the tar spraying amount was 50 mL, the reaction temperature was 340 °C, the reaction pressure was 4 MPa, and the reaction time was 60 min. After the reaction was completed, the thickened coal powder was naturally cooled to room temperature and taken out.

[0053] The modified coal was measured using a bonding index tester in accordance with GB / T 5447-2014, and the bonding index of the product was 77.

[0054] The summary table of viscosity increase results is as follows: The experiment was conducted using lignite as raw material, and the reaction conditions were carried out according to the above lignite viscosity increasing standard to explore the effects of the two airflow nozzle angles on the viscosity increasing effect. ∠1 represents the angle formed by the carbon monoxide airflow nozzle 17 obliquely downward and the wall of the fluidized bed 10, and ∠2 represents the angle formed by the water vapor airflow nozzle 18 obliquely upward and the wall of the fluidized bed 10. The solid product was measured using a viscosity index measuring instrument in accordance with GB / T 5447-2014.

[0055] Example 7 This embodiment proposes a method for directly making coke from weakly caking coal, using the device for directly making coke from weakly caking coal described in Example 1, using a 150-mesh sieve to screen the lignite, wherein the lignite input amount is 20 g, the catalyst input amount is 0.17 g, ∠1 is between 10-80°, ∠2 is between 20-30°, the flow rate of a single steam air flow nozzle 18 is 127 mL / min, the flow rate of a single carbon monoxide air flow nozzle 17 is 106 mL / min, the tar spraying amount is 50 mL, the reaction temperature is 330°C, the reaction pressure is 4.5MPa, and the reaction time is 60 min. After the reaction is completed, the thickened coal powder is naturally cooled to room temperature and taken out.

[0056] The modified coal was measured using a bonding index tester in accordance with GB / T 5447-2014, and the bonding index of the product was between 90 and 96.

[0057] Example 8 This embodiment proposes a method for directly making coke from weakly caking coal, using the device for directly making coke from weakly caking coal described in Example 1, using a 150-mesh sieve to screen the lignite, wherein the lignite input amount is 20 g, the catalyst input amount is 0.17 g, ∠1 is between 30-60°, ∠2 is between 10-50°, the flow rate of a single steam air flow nozzle 18 is 127 mL / min, the flow rate of a single carbon monoxide air flow nozzle 17 is 106 mL / min, the tar spraying amount is 50 mL, the reaction temperature is 330°C, the reaction pressure is 4.5MPa, and the reaction time is 60 min. After the reaction is completed, the thickened coal powder is naturally cooled to room temperature and taken out.

[0058] The modified coal was measured using a caking index tester in accordance with GB / T 5447-2014, and the caking index of the product was between 81 and 96.

[0059] Example 9 This embodiment proposes a method for directly making coke from weakly caking coal, using the device for directly making coke from weakly caking coal described in Example 1, using a 150-mesh sieve to screen the lignite, wherein the lignite input amount is 20 g, the catalyst input amount is 0.17 g, ∠1 is between 30-60°, ∠2 is between 20-30°, the flow rate of a single steam air flow nozzle 18 is 127 mL / min, the flow rate of a single carbon monoxide air flow nozzle 17 is 106 mL / min, the tar spraying amount is 50 mL, the reaction temperature is 330°C, the reaction pressure is 4.5MPa, and the reaction time is 60 min. After the reaction is completed, the thickened coal powder is naturally cooled to room temperature and taken out.

[0060] The modified coal was measured using a bonding index tester in accordance with GB / T 5447-2014, and the bonding index of the product was stable at around 96.

[0061] The summary table of adhesion index is as follows: It can be seen that when the angle formed by the carbon monoxide gas flow nozzle 17 obliquely downward and the wall of the fluidized bed 10 is 50°, and the angle formed by the water vapor gas flow nozzle 18 obliquely upward and the wall of the fluidized bed 10 is 30°, the viscosity index of the lignite is significantly increased to 96.33.

[0062] The above content is a further detailed description of the present invention in combination with a specific preferred embodiment. It cannot be determined that the specific embodiments of the present invention are limited to this. For ordinary technicians in the technical field to which the present invention belongs, several simple deductions or substitutions can be made without departing from the present invention, which should be regarded as belonging to the present invention and the scope of patent protection determined by the submitted claims.

Claims

1. A device for directly producing coke from weakly caking coal, characterized in that: The invention comprises a fluidized bed (10), a dryer (20), a hot gas-solid separator (22), a retort (2) and a cooling device (3); the top outlet of the fluidized bed (10) is connected to the inlet of the dryer (20), the outlet of the dryer (20) is connected to the inlet of the hot gas-solid separator (22), the solid phase outlet of the hot gas-solid separator (22) is connected to the retort (2); the outlet of the retort (2) is connected to the cooling device (3); The interior of the fluidized bed (10) is divided into upper and lower parts by the catalyst layer (16); the upper part is provided with a tar nozzle (112), a coal powder injection tank (12), a coal crushing blade (13), an axial rod (131), a servo motor (14), and an upper variable diameter gas distribution plate (151); and the lower part is provided with a lower variable diameter gas distribution plate (152), a carbon monoxide gas flow nozzle (17), and a water vapor gas flow nozzle (18); The tar nozzle (112) is arranged on the top of the fluidized bed (10) and is connected to the tar spraying device (11); the tar nozzle (112) comprises a tar channel and a water vapor channel, the tar channel is located in the middle, and the water vapor channels are symmetrically arranged on both sides of the tar channel in a downwardly inclined state and are connected to the tar channel; the water vapor channel is provided with a C-shaped branch; the water vapor heats and atomizes the tar through the first inclined outlet, and the second inclined outlet performs secondary atomization on the descending tar; The pulverized coal injection tank (12) is symmetrically fixedly connected to two sides of the wall of the fluidized bed (10); The coal crushing blade (13) is fixedly connected to the shaft rod (131), the shaft rod (131) is rotatably connected to the center of the upper variable diameter gas distribution plate (151), and the shaft rod (131) is electrically connected to the servo motor (14); The upper variable-diameter gas distribution plate (151) is arranged in contact with the upper surface of the catalyst layer (16), and the lower variable-diameter gas distribution plate (152) is arranged in contact with the lower surface of the catalyst layer (16); the upper variable-diameter gas distribution plate (151) and the lower variable-diameter gas distribution plate (152) have the same structure, with a large aperture at the bottom and a small aperture at the top, and both the upper and lower apertures are smaller than the diameter of the catalyst in the catalyst layer (16); A plurality of the carbon monoxide gas flow nozzles (17) are evenly distributed and fixedly connected to the wall of the fluidized bed (10), the inlet of the carbon monoxide gas flow nozzle (17) is connected to the carbon monoxide pipeline, and the carbon monoxide gas flow nozzle (17) is inclined downward and forms an angle of 30°-60° with the wall of the fluidized bed (10); The plurality of water vapor air flow nozzles (18) are evenly distributed and fixedly connected to the wall of the fluidized bed (10), and the water vapor air flow nozzles (18) are located as a whole below the carbon monoxide air flow nozzles (17); the inlet of the water vapor air flow nozzles (18) is connected to the steam generator (19), and the angle formed by the water vapor air flow nozzles (18) obliquely upwards and the wall of the fluidized bed (10) is 20°-30°.

2. The device for directly producing coke from weakly caking coal according to claim 1, characterized in that: Taking the first water vapor air flow nozzle (18) on the left side of the fluidized bed as a reference, a water vapor air flow nozzle (18) is arranged every 72° counterclockwise rotation around the axis of the fluidized bed (10), and the longitudinal spacing distance of each water vapor air flow nozzle (18) is 1 / 4D, and the lateral spacing distance of each water vapor air flow nozzle (18) is 1 / 5πD, where D is the inner diameter of the fluidized bed (10).

3. The device for directly producing coke from weakly caking coal according to claim 2, characterized in that: Taking the first carbon monoxide gas flow nozzle (17) on the left side of the fluidized bed (10) as a reference, a carbon monoxide gas flow nozzle (17) is arranged every 72° clockwise rotation around the axis of the fluidized bed (10), and the longitudinal spacing distance of each carbon monoxide gas flow nozzle (17) is 1 / 4D, and the lateral spacing distance of each carbon monoxide gas flow nozzle (17) is 1 / 5πD.

4. The device for directly producing coke from weakly caking coal according to claim 1, characterized in that: The pulverized coal injection tank (12) is located at a height of 1 / 3H from the top of the fluidized bed (10), where H is the height of the fluidized bed (10).

5. The device for directly producing coke from weakly caking coal according to claim 1, characterized in that: It also includes a gas separation and purification device (4); the gas phase outlet of the hot gas-solid separator (22) and the gas separation and purification device (4) are connected via a pipeline, and the carbon dioxide outlet of the gas separation and purification device (4) is connected to the cooling medium inlet of the cooling device (3).

6. The device for directly producing coke from weakly caking coal according to claim 5, characterized in that: The cooling medium inlet of the cooling device (3) is also connected to a carbon dioxide pipeline.

7. The device for directly producing coke from weakly caking coal according to claim 1, characterized in that: It also includes a cyclone separator (31); the extraction outlet of the cooling device (3) is connected to the cyclone separator (31); the solid outlet of the cyclone separator (31) extracts coke powder; and the gas outlet pipeline of the cyclone separator (31) is connected to the inlet of the carbon monoxide gas flow nozzle (17).

8. The device for directly producing coke from weakly caking coal according to claim 1, characterized in that: It also includes a cooler (21); the gas product outlet at the top of the dry distillation kettle (2) is connected to the cooler (21); the liquid phase outlet of the cooler (21) is connected to a tar delivery pump (111); and the tar delivery pump (111) is connected to the tar spraying device (11).

9. A method for directly producing coke from weakly caking coal, characterized in that: A device for directly producing coke from weakly caking coal according to any one of claims 1 to 8; comprising the following steps: The pulverized coal is sprayed into the fluidized bed (10), and carbon monoxide and water vapor are sprayed from the carbon monoxide airflow nozzle (17) and the water vapor airflow nozzle (18) respectively, and the coal crushing blade (13) is started, and multiple carbon monoxide airflow nozzles (17) spray simultaneously to form a clockwise vortex downward airflow, and multiple water vapor airflow nozzles (18) spray simultaneously to form a counterclockwise vortex upward airflow. The two airflows collide in reverse to enhance the mixing effect, and the excess water vapor carries the mixed air mass through the catalyst layer (16). After the reaction gas is activated and reacts, an active substance is generated to fluidize and thicken the pulverized coal; At the same time, the tar nozzle (112) is opened to spray tar to the fluidized coal powder for secondary viscosity enhancement; Subsequently, the thickened coal powder is taken out from the top of the fluidized bed (10) and sent to the dryer (20) for drying and water removal. The thickened coal powder is separated by the hot gas-solid separator (22). The thickened coal powder is then sent to the dry distillation kettle (2) for coking. The solid product in the dry distillation kettle (2) is cooled by the cooling device (3). The cooling medium of the cooling device (3) is carbon dioxide. The product of the cooling device (3) is separated and purified. The gas phase product carbon monoxide is sent to the carbon monoxide gas flow nozzle (17) of the fluidized bed (10), and the solid product is coke powder.

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