An apparatus and method for pyrolyzing rich-oil pulverized coal to produce coal tar

Abstract

The present invention discloses a device and method for pyrolyzing rich-oil pulverized coal to produce coal tar. The device mainly consists of a pyrolysis reactor, a multi-stage separator, an oil-gas separation unit, a semi-coke feed balancer, a preheated gas generator, etc. The device uses low-rank rich-oil pulverized coal with a smaller particle size and difficult to comprehensively utilize as raw material, burns part of its carbon-containing substances (semi-coke) to supply energy for the pyrolysis reaction, and then extracts coal tar through a multi-stage gas-solid separation system, and distinguishes semi-coke with different particle sizes; after the semi-coke is appropriately distributed, the fine-particle semi-coke enters the preheated gas generator to burn and supply energy for the system, part of the coarse-particle semi-coke is burned to supplement heat supply and at the same time serves as a heat carrier for internal circulation, and the medium-particle semi-coke is sent out of the device for uses such as gasification, power generation, and preparation of carbon materials. The present invention has a high tar yield, a high energy efficiency level, a lower requirement for the feed particle size range, and at the same time the overall structure of the device is simple and easy to operate, and has good application prospects.

Description

Technical Field

[0001] The invention belongs to the technical field of coal conversion, and particularly relates to a device and method for preparing coal tar by pyrolyzing oil-rich foamy coal. Background Art

[0002] During the mining and processing of low-rank coal, a large amount of low-rank oil-rich foam coal will be produced. The foam coal has a small particle size (0-13mm) and is cheap. It is currently mainly used as fuel for power generation, industrial boilers, cement lime burning, brick making, etc. Its outstanding oil and gas properties and its properties as a chemical raw material are often ignored, which invisibly causes a huge waste of resources.

[0003] Patent CN1640988A discloses a method for producing coal tar by pyrolysis of coal, in which pulverized coal is placed in an internal heating rotary furnace, hot gas is introduced to pyrolyze it, and the coal tar and coal gas escaping from the internal heating rotary furnace are washed with water spray, and coal tar is obtained after separation. This method can process coal powder with larger particle size, but the tar yield is low and the overall energy efficiency of the device is not high. At the same time, the structure of the rotary furnace is relatively complex and the processing and manufacturing are difficult. Patent CN103387839A discloses a method and device for extracting coal tar from carbon-containing materials and preparing synthesis gas, in which a pyrolysis gasification device is coupled. The device has strict requirements on the particle size of coal powder, a complex structure, and is not easy to operate stably. Summary of the invention

[0004] In order to overcome the shortcomings of the above-mentioned prior art, the purpose of the present invention is to provide a device and method for pyrolyzing oil-rich foamy coal to produce coal tar, so as to improve the tar yield and energy efficiency level, and have wide requirements on particle size. At the same time, it has a simple structure, convenient operation, and low investment, and is suitable for pyrolyzing low-order oil-rich foamy coal to extract coal tar.

[0005] In order to achieve the above object, the technical solution adopted by the present invention is:

[0006] A device for preparing coal tar by pyrolyzing oil-rich foamy coal, comprising a pyrolysis reactor, wherein the oil and gas product outlet of the pyrolysis reactor is connected to a multi-stage gas-solid separator, and the solid phase outlets of each stage of the gas-solid separator are all connected to a semi-coke feed balancer, and the semi-coke feed balancer distributes the semi-coke particles separated by each stage of the gas-solid separator, and a part of the semi-coke particles enters a preheating gas generator for combustion to provide heat for pyrolysis, or to provide heat for pyrolysis and raw material preheating at the same time, and the other part is sent out as activated coke; the gas phase outlet of the last stage of the gas-solid separator is connected to an oil-gas separation unit, and the oil-gas separation unit processes the gas phase product to obtain coal gas and tar;

[0007] The pyrolysis reactor includes a combustion chamber, a return material chamber, a pyrolysis chamber, a separation chamber and a storage chamber; wherein the combustion chamber is located at the bottom and is directly connected to the pyrolysis chamber; the separation chamber is located above the pyrolysis chamber and separates the pyrolysis products into oil gas and semicoke; the storage chamber is an annular area between the pyrolysis chamber and the reactor outer wall, and the return material chamber is located between the storage chamber and the combustion chamber, and the obtained semicoke is sent back to the combustion chamber through the storage chamber and the return material chamber.

[0008] In one embodiment, an internal circulation separator is disposed in the separation chamber. The internal circulation separator is a cylindrical structure with an open bottom and a spherical closure at the top, sleeved on the top of the cylindrical pyrolysis chamber, and having axial and radial distances from the pyrolysis chamber. The inner wall of the internal circulation separator is connected to the outer wall of the pyrolysis chamber by a baffle extending downward in a spiral shape, and the outer wall of the internal circulation separator is connected to the inner wall of the reactor by a baffle extending upward in a spiral shape.

[0009] In one embodiment, a plurality of level balance devices for controlling the return of semicoke are arranged in the return material chamber. The level balance device includes a controller and a balancer. The balancer includes a housing and an actuator. The housing is a cavity, and there is a semicoke inlet connected to the return material chamber above the cavity and a semicoke outlet connected to the combustion chamber below the cavity; the actuator extends into the cavity and, under the control of the controller, blocks or opens the semicoke inlet and / or blocks or opens the semicoke outlet, thereby closing or opening the return material passage with the route of return material chamber - semicoke inlet - cavity - semicoke outlet - combustion chamber.

[0010] In one embodiment, the controller controls the opening amount of the actuator for the semicoke inlet and / or the semicoke outlet.

[0011] In one embodiment, the level balance device further includes a level gauge and a static pressure gauge; the level gauge and the static pressure gauge are installed in the storage chamber to jointly determine the material level in the storage chamber, and the controller controls the closing or opening action of the actuator according to the level signal.

[0012] In one embodiment, the actuator includes a pneumatic system, a columnar plug, a slide rail and a connecting rod; the slide rail is in a cuboid shape and is attached to the semicoke inlet and / or the semicoke outlet. A cylindrical chute is opened on the slide rail, one side of the chute is open, and a plurality of round holes are opened on the other side. The pneumatic system drives the columnar plug to slide in the chute through the connecting rod, and different sliding positions enable the semicoke inlet and / or the semicoke outlet to communicate with the cavity through different numbers of round holes.

[0013] In one embodiment, the semi-coke feed balancer includes a storage bin, a feeding bin, and a feeding cone; the storage bin is above the feeding bin and the two are directly connected. The storage bin is partitioned into two parts by a baffle with a channel in the middle and lower part, and particle inlets are respectively connected to the two parts; the feeding cone is arranged in the feeding bin, one side of the cross-section of the feeding cone is a semi-ellipse, the other side is a semi-circle, or both sides are asymmetric semi-ellipses, and the longitudinal section of the feeding cone is in a shape that tapers from the middle to both sides; the feeding cone is configured to be rotatable along the vertical axis, and there is a particle outlet at the bottom of the feeding bin.

[0014] In one embodiment, two feeding ridges along the up-and-down direction of the bin wall are symmetrically arranged in the feeding bin.

[0015] The present invention also provides a method for pyrolyzing rich oil coal fines to produce coal tar by using the device for pyrolyzing rich oil coal fines to produce coal tar, which comprises the following steps:

[0016] Step 1), pressurize the coal fines to 0.8 - 5.0 MPa, preheat and then exchange heat with the high-temperature flue gas from the start-up furnace or the preheating gas generator to raise the temperature to 100 - 150 °C; in the start-up stage, heat is provided by the start-up furnace, and after normal operation, heat is provided by the preheating gas generator;

[0017] Step 2), the preheated coal fines enter the pyrolysis chamber, are mixed and heat-exchanged with the high-temperature flue gas and semi-coke particles from the combustion chamber, and the temperature is raised to 500 - 650 °C, and the pyrolysis reaction is completed during the upward movement in the pyrolysis chamber;

[0018] Step 3), after the pyrolysis reaction is completed, the semi-coke and the oil gas are successively separated through the separation chamber and the multi-stage gas-solid separator. The separated gas phase is further processed by the oil-gas separation unit to obtain coal gas and tar; the semi-coke separated by the separation chamber enters the storage chamber, then enters the combustion chamber through the return chamber, is mixed with oxygen and the high-temperature soot transported by the preheating gas generator, and after combustion and heat exchange, continues to enter the pyrolysis chamber to complete the internal circulation process; the semi-coke particles separated by the multi-stage gas-solid separator enter the semi-coke feed balancer;

[0019] Step 4), after being distributed by the semi-coke feed balancer, a part of the semi-coke particles enters the preheating gas generator to burn for heating the pyrolysis, or simultaneously for heating the pyrolysis and preheating the raw materials, and the other part is sent out as activated coke.

[0020] In one embodiment, in the said step 3), the material level balancing device jointly determines the material level in the storage chamber through the level gauge and the static pressure gauge. After reaching the threshold value, the controller controls the pneumatic system of the actuator to pull the connecting rod and the columnar plug to connect the storage chamber with the combustion chamber; when the semi-coke burns in the combustion chamber, the oxygen concentration at the oil gas outlet of the reactor and the temperature at the outlet of the separation chamber are monitored in real time, and the oxygen input amount is controlled. When the material level in the storage chamber is lower than the threshold value, the material level balancing device performs the opposite operation to isolate the storage chamber from the combustion chamber;

[0021] In step 4), the semicoke feed balancer is controlled by a feed controller. Under normal operating conditions, the fine-particle semicoke separated by gas-solid separators of different levels is sent into the preheating gas generator for combustion, and the coarse-particle semicoke is sent out of the device for further processing and utilization. When the operating conditions change, the feed controller calculates the increase or decrease in the semicoke feed based on the oxygen input, semicoke input, combustion temperature, flue gas outlet temperature, and dust content in the flue gas in the preheating gas generator. When the feed rate needs to be increased, the feed controller controls the rotating deflector cone to adjust the particle flow area in different regions of the feed bin, sending more semicoke into the preheating gas generator to supply energy for the pyrolysis system. Conversely, more semicoke is sent out of the pyrolysis device.

[0022] Compared with the prior art, the beneficial effects of the present invention are as follows:

[0023] The present invention uses low-rank oil-rich pulverized coal with a smaller particle size as the raw material, and performs a rapid and efficient pyrolysis reaction in a pyrolysis reactor. The pulverized coal with a smaller particle size has a large specific surface area and a high mass and heat transfer rate, which is conducive to increasing the yield of coal tar. The device is provided with multiple-stage gas-solid separators to distinguish semicoke particles of different particle sizes. The fine-particle semicoke is used for combustion to supply energy for the pyrolysis reaction, the medium-particle-size semicoke is sent out of the device for gasification, power generation, preparation of carbon materials, etc., and the coarse-particle semicoke is used for supplementary heating or as a heat carrier for internal circulation. This can not only effectively control the particle size in the reaction system and make full use of semicoke with different particle sizes, improving the energy utilization efficiency, but also is conducive to improving the quality of coal tar products. Description of the Drawings

[0024] Figure 1 It is a schematic diagram of the overall device of the present invention.

[0025] Figure 2 It is a logistics line diagram of the pyrolysis reactor of the present invention.

[0026] Figure 3 It is a schematic diagram of the structure of the internal circulation separator in the separation chamber of the pyrolysis reactor of the present invention.

[0027] Figure 4 It is a schematic diagram of the connection between the internal circulation separator in the separation chamber of the pyrolysis reactor and the inner wall of the pyrolysis reactor of the present invention.

[0028] Figure 5 It is a connection diagram of the level balance device of the present invention.

[0029] Figure 6 It is a schematic diagram of the structure of the balancer of the level balance device of the present invention.

[0030] Figure 7 It is a schematic diagram of the structure of the actuator of the balancer of the present invention.

[0031] Figure 8 For Figure 7View in the A direction in the middle.

[0032] Figure 9 This is a schematic structural view of the semicoke feeding balancer of the present invention.

[0033] Figure 10 This is a schematic cross-sectional view of the material guiding bin of the semicoke feeding balancer of the present invention.

[0034] Figure 11 This is a schematic structural view of the baffle in the storage bin of the semicoke feeding balancer of the present invention.

[0035] In the figure: 1, start-up furnace; 2, lock hopper system; 3, preheater; 4, temperature and oxygen concentration monitoring controller; 5, oxygen control valve; 6, pyrolysis reactor; 7, primary separator; 8, secondary separator; 9, oil-gas separation unit; 10, semicoke feeding balancer; 10-1, particle inlet; 10-2, storage bin; 10-3, material guiding bin; 10-4, material guiding cone; 10-5, particle outlet; 10-6, transmission device; 10-3-1, material guiding ridge; 11, preheated gas generating furnace; 12, feeding controller; 13, combustion chamber; 14, return material chamber; 15, pyrolysis chamber; 16, separation chamber; 16-1, internal circulation separator; 16-2, baffle; 17, storage chamber; 18, material level balancing device; 19, level gauge; 20, static pressure gauge; 21, controller; 22, balancer; 22-1, semicoke inlet; 22-2, semicoke outlet; 22-3, housing; 22-4, auxiliary fluidizing gas injection pipeline; 22-5, cavity; 22-6, actuator; 22-6-1, pneumatic system; 22-6-2, columnar plug; 22-6-3, slide rail; 22-6-4, connecting rod; 22-6-5, round hole; a to k, equipment pipelines; m equipment pipeline; A to E, signal lines; M1, pulverized coal; M2, start-up furnace fuel; M3, coal gas; M4, tar; M5, semicoke or activated coke; M6, semicoke; M7, oxygen. Detailed implementation manners

[0036] The technical solution of the present invention will be further described below in conjunction with the accompanying drawings, but the present invention is not limited to the following implementation cases.

[0037] As Figure 1As shown in the figure, the device for pyrolyzing rich-oil pulverized coal to produce coal tar according to the present invention includes a pyrolysis reactor 6, a multi-stage gas-solid separator, a semi-coke feed balancer 10, a preheated gas generator 11, and an oil-gas separation unit 9. Among them, the pyrolysis reaction is carried out in the pyrolysis reactor 6, and its oil-gas product outlet is connected to the multi-stage gas-solid separator. Each stage of the gas-solid separator conducts sequential gas-solid separation, and its solid phase outlets are all connected to the semi-coke feed balancer 10. After the semi-coke feed balancer 10 distributes the semi-coke particles separated by each stage of the gas-solid separator, a part of them enters the preheated gas generator 11 to burn for heat supply for pyrolysis (or simultaneously for heat supply for pyrolysis and raw material preheating), and the other part is sent out as activated coke; the gas phase outlet of the last stage of the gas-solid separator is connected to the oil-gas separation unit 9, and the gas phase product is processed by the oil-gas separation unit 9 to obtain coal gas M3 and tar M4.

[0038] Reference Figure 2 , the pyrolysis reactor 6 of the present invention includes a combustion chamber 13, a return material chamber 14, a pyrolysis chamber 15, a separation chamber 16, and a storage chamber 17; among them, the combustion chamber 13 is located at the bottommost, the separation chamber 16 is located at the upper part, and between them are the return material chamber 14, the pyrolysis chamber 15, and the storage chamber 17. The combustion chamber 13 is directly connected to the pyrolysis chamber 15; the storage chamber 17 is an annular area between the pyrolysis chamber 15 and the outer wall of the pyrolysis reactor 6. The return material chamber 14 is located between the storage chamber 17 and the combustion chamber 13. The separation chamber 16 separates the pyrolysis products into oil-gas and semi-coke; the obtained semi-coke is sent back to the combustion chamber 13 through the storage chamber 17 and the return material chamber 14 to complete the cycle.

[0039] The device of the present invention uses low-rank rich-oil pulverized coal with a smaller particle size and difficult to comprehensively utilize as the raw material, burns part of its carbon-containing substances (semi-coke) to supply energy for the pyrolysis reaction, and then through a multi-stage gas-solid separation system, extracts coal tar and distinguishes semi-coke with different particle sizes; after the semi-coke is appropriately distributed, the fine particle semi-coke enters the preheated gas generator to burn for system energy supply, the coarse particle semi-coke is partially burned for supplementary heat supply and at the same time serves as a heat carrier for internal circulation, and the medium particle size semi-coke is sent out of the device for uses such as gasification, power generation, and preparation of carbon materials. The present invention has a high tar yield, a high energy efficiency level, and a relatively low requirement for the feed particle size range.

[0040] Exemplarily, for a parameter setting of the present invention, the height-diameter ratio of the combustion chamber 13 is 1.5 - 3.5. At this parameter, the high-temperature gas and solid from the preheated gas generator can achieve better mixing and heat exchange with the internal circulation semi-coke.

[0041] Refer again Figure 1, in some embodiments of the present invention, some peripheral auxiliary devices are further included, mainly including a start-up furnace 1, a lock hopper system 2, a preheater 3, a temperature and oxygen concentration monitoring and control device 4, an oxygen control valve 5, and a feed controller 12. These devices are all conventional components, and any one or several of them can be cancelled according to requirements. And for the convenience of description, the multi-stage gas-solid separator of the present invention is set to two stages, namely a primary separator 7 and a secondary separator 8.

[0042] According to this embodiment, the start-up furnace 1 and the lock hopper system 2 are respectively connected to the preheater 3 through pipelines a and b, and then connected to the feed inlet of the pyrolysis reactor 6 through pipeline c; the upper product (mainly oil and gas) outlet of the pyrolysis reactor 6 is connected to the primary separator 7 through pipeline d, and then sequentially connected to the secondary separator 8 and the oil and gas separation unit 9 through pipelines e and f.

[0043] The solid-phase outlets of the primary separator 7 and the secondary separator 8 are respectively connected to the semicoke feed balancer 10 through pipelines g and h; the semicoke feed balancer 10 is connected to the preheating gas generator 11 through pipeline i; the preheating gas generator 11 is respectively connected to the bottom of the combustion chamber 13 of the pyrolysis reactor 6 and the preheater 3 through pipelines j and k.

[0044] The feed controller 12 is connected to the semicoke feed balancer 10 and the preheating gas generator 11 through signal lines A and B.

[0045] The temperature and oxygen concentration monitoring and control device 4 is respectively connected to pipeline d, the separation chamber 16, and the oxygen control valve 5 through signal lines C, D, and E;

[0046] The oxygen control valve 5 is connected to the combustion chamber 13 through pipeline m.

[0047] See Figure 3 and Figure 4 , in some embodiments of the present invention, an internal circulation separator 16-1 is provided inside the separation chamber 16. The internal circulation separator 16-1 is a columnar structure with an open bottom and a spherical closed top, sleeved on the top of the columnar pyrolysis chamber 15, and having an axial and radial distance from the pyrolysis chamber 15. The inner wall of the internal circulation separator 16-1 is connected to the outer wall of the pyrolysis chamber 15 by a baffle extending downward in a spiral shape, and the angle between the baffle and the horizontal plane is 55° to 75°, and the number of baffles is 6 to 8. The height-to-diameter ratio of the cylindrical part of the internal circulation separator 16-1 is 1.2 to 2.5, and the ratio of the cross-sectional area of the annular gap (i.e., the space between the inner wall of the pyrolysis chamber 15 and the inner wall of the cylindrical part of the internal circulation separator 16-1) to the cross-sectional area of the pyrolysis chamber 15 is 0.9 to 1.3; the outer wall of the internal circulation separator 16-1 is connected to the inner wall of the pyrolysis reactor 6 by a baffle 16-2 extending upward in a spiral shape, and the angle between the baffle 16-2 and the horizontal plane is 45° to 60°, and the number of baffles 16-2 is 10 to 16.

[0048] In some embodiments of the present invention, a plurality of level balancing devices 18 for controlling the return of semicoke are arranged in the return chamber 14, preferably 8 to 10 groups are arranged. Refer to Figure 5 , the level balancing device 18 mainly includes a controller 21 and a balancer 22, and may further include a level gauge 19 and a static pressure gauge 20 when achieving the automatic control target. At this time, the level gauge 19 and the static pressure gauge 20 are installed in the storage chamber 17 to jointly determine the level of the storage chamber 17. The level gauge 19 and the static pressure gauge 20 are connected to the controller 21 by signal input lines, and the controller 21 is connected to the balancer 22 by a signal output line to control the action of the balancer 22 according to the level signal to achieve return material control.

[0049] In some embodiments of the present invention, refer to Figure 6 , the balancer 22 mainly includes a housing 22-3 and an actuator 22-6. The housing 22-3 has a cavity 22-5 inside. The longitudinal section of the cavity 22-5 can be semi-circular, and the radius first increases and then decreases from top to bottom. There is a semicoke inlet 22-1 connecting to the return chamber 14 above it, and a semicoke outlet 22-2 connecting to the combustion chamber 13 below it. The actuator 22-6 extends into the cavity 22-5. Under the control of the controller 21, it blocks or opens the semicoke inlet 22-1, and / or blocks or opens the semicoke outlet 22-2, thereby closing or opening the return material passage with the route of return chamber 14 - semicoke inlet 22-1 - cavity 22-5 - semicoke outlet 22-2 - combustion chamber 13. Exemplarily, the housing 22-3 is also provided with 3 auxiliary fluidizing gas injection pipelines 22-4, and the included angles with the horizontal plane are 80° - 100°, 40° - 50°, and 25° - 35° respectively. Preferably, the controller 21 can not only control the opening and closing, but also further control the opening amount of the actuator 22-6 for the semicoke inlet 22-1 and / or the semicoke outlet 22-2. When receiving the level signal, it can control the closing or opening action of the actuator 22-6 according to the level signal.

[0050] In some embodiments of the present invention, refer to Figure 7 and Figure 8, the actuator 22-6 mainly includes a pneumatic system 22-6-1, a columnar plug 22-6-2, a slide rail 22-6-3 and a connecting rod 22-6-4. Among them, the slide rail 22-6-3 is in the shape of a cuboid and is attached to the semicoke inlet 22-1 and / or the semicoke outlet 22-2. A cylindrical chute is provided on the slide rail 22-6-3. Obviously, the direction of the chute is the same as that of the slide rail 22-6-3. One side of the chute is open, and a number of round holes 22-6-5 are provided on the other side. In this embodiment, the ratio d2 / D of the opening distance of the chute to the diameter of the chute is 0.5-0.65, and the ratio d1 / D of the diameter of the round hole 22-6-5 to the diameter of the chute is 0.45-0.6. Two connecting rods 22-6-4 are connected to the columnar plug 22-6-2 in the chute, and the connecting rods 22-6-4 are connected to the pneumatic system 22-6-1 to obtain power. The function of connecting two connecting rods 22-6-4 here is to obtain balance, rather than an inevitable limitation on the number of connecting rods. The pneumatic system 22-6-1 drives the columnar plug 22-6-2 to slide in the chute through the connecting rods 22-6-4, and different sliding positions enable the semicoke inlet 22-1 and / or the semicoke outlet 22-2 to communicate with the cavity 22-5 through different numbers of round holes 22-6-5.

[0051] In some embodiments of the present invention, referring to Figure 9 and Figure 10 , the semicoke feeding balancer 10 mainly includes a storage bin 10-2, a feeding bin 10-3 and a feeding cone 10-4. The storage bin 10-2 is above the feeding bin 10-3 and the two are directly connected. The storage bin 10-2 is partitioned into two parts by a baffle with a channel in the middle and lower part. The structure of the baffle can be referred to Figure 11 as shown. The length of the channel is less than 1.6R2. At least one particle inlet 10-1 is respectively connected to the two parts. Correspondingly, two particle outlets 10-5 are also respectively connected to the feeding bin 10-3 in the similar direction. The feeding cone 10-4 is arranged in the feeding bin 10-3 and can be connected to a transmission device 10-6. One side of the cross-section of the feeding cone 10-4 is a semi-ellipse, the other side is a semi-circle, or both sides are asymmetric semi-ellipses, or both sides are other asymmetric shapes, and it first increases and then decreases along the axial direction. The feeding cone 10-4 is configured to be able to rotate along the vertical axis, and its longitudinal section is in the shape of gradually tapering from the middle to both sides. Exemplarily, when one side is a semi-ellipse and the other side is a semi-circle, the ratio R1 / R2 of the short axis length of the ellipse to the radius of the semi-circle is 0.4-0.6. Two guiding ridges 10-3-1 are symmetrically arranged in the feeding bin 10-3 to reduce the mixing of large and small particles. The two guiding ridges 10-3-1 are arranged along the up and down direction of the bin wall and can be connected to the center line of the feeding cone 10-4. Loosening gas can be provided at the bottom of the storage bin 10-2 and in the feeding bin 10-3 to assist the flow of particles.

[0052] The method for pyrolyzing pulverized coal to produce coal tar according to the present invention includes the following steps:

[0053] 1) Pressurization and preheating of raw materials.

[0054] Pressurize pulverized coal M1 to 0.8 - 5.0 MPa, and after preheating, exchange heat with high-temperature flue gas from start-up furnace 1 or preheated gas generator 11 to raise the temperature to 100 - 150 °C; during the start-up stage, heat is provided by start-up furnace 1, and after normal operation, heat is provided by preheated gas generator 11.

[0055] In the foregoing embodiment of the present invention with auxiliary equipment, pulverized coal M1 is first pressurized to 0.8 - 5.0 MPa by the lock hopper system 2, and after entering the preheater 3, it exchanges heat with high-temperature flue gas from start-up furnace 1 or preheated gas generator 11 to raise the temperature to 100 - 150 °C (during the start-up stage, heat is provided by start-up furnace 1, and after normal operation, heat is provided by preheated gas generator 11).

[0056] 2) Pyrolysis of raw materials.

[0057] The preheated pulverized coal M1 enters the pyrolysis chamber 15, mixes and exchanges heat with high-temperature flue gas and semi-coke particles from the combustion chamber 13, and the temperature is raised to 500 - 650 °C. The pyrolysis reaction is completed during the upward movement in the pyrolysis chamber 15.

[0058] 3) Separation of oil gas and semi-coke.

[0059] After the pyrolysis reaction is completed, the semi-coke and oil gas pass through the separation chamber 16 and a multi-stage gas-solid separator (such as the aforementioned primary separator 7 and secondary separator 8) for separation in sequence. The separated gas phase is further processed by the oil gas separation unit 9 to obtain coal gas M3 and tar M4. The semi-coke separated by the separation chamber 16 enters the storage chamber 17, and then enters the combustion chamber 13 through the return chamber 14, mixes with oxygen and high-temperature soot transported by the preheated gas generator 11, and after combustion and heat exchange, continues to enter the pyrolysis chamber 15 to complete the internal circulation process; the semi-coke particles separated by the multi-stage gas-solid separator enter the semi-coke feed balancer 10;

[0060] In the embodiment of the present invention with the level balancing device 18, the level balancing device 18 jointly determines the material level in the storage chamber 17 through the level gauge 19 and the static pressure gauge 20. After reaching the threshold value, the controller 21 controls the pneumatic system 22-6-1 of the actuator 22-6 to pull the connecting rod 22-6-4 and the columnar plug 22-6-2, and the storage chamber 17 and the combustion chamber 13 can be connected. The semi-coke particles enter the combustion chamber 13 and are mixed with the oxygen transported by the oxygen pipeline m and the high-temperature soot transported by the preheating gas generator 11. After combustion and heat exchange, they continue to enter the pyrolysis chamber 15 to complete the internal circulation process. When the semi-coke burns in the combustion chamber 13, the temperature and oxygen concentration monitoring controller 4 monitors the oxygen concentration at the oil and gas outlet of the pyrolysis reactor 6 and the temperature at the outlet of the separation chamber 16 in real time, and controls the oxygen control valve 5 to adjust the oxygen input. When the material level in the storage chamber 17 is lower than the threshold value, the level balancing device 18 performs the opposite operation to isolate the storage chamber 17 from the combustion chamber 13, and the semi-coke particles separated by the primary separator 7 and the secondary separator 8 enter the semi-coke feed balancer 10.

[0061] 4) Combustion and utilization of semi-coke.

[0062] After being separated by the multi-stage separator, the semi-coke particles are distributed by the semi-coke feed balancer 10. Part of them enter the preheating gas generator 11 for combustion to supply heat to the system, and the other part is sent out of the device as activated coke M5 for further processing and utilization.

[0063] The semi-coke feed balancer 10 is controlled by the feed controller 12. Under normal operating conditions, the fine-grained semi-coke separated by the secondary separator 8 is mainly sent into the preheating gas generator 11 for combustion, and the coarse-grained semi-coke separated by the primary separator 7 is mainly sent out of the device for further processing and utilization. When the operating conditions change, the feed controller 12 calculates the increase or decrease in the semi-coke feed according to the oxygen input, semi-coke input, combustion temperature, flue gas outlet temperature, flue gas dust content, etc. in the preheating gas generator 11. When the feed rate needs to be increased, the feed controller 12 rotates the guide cone 10-4 through the transmission device 10-6 of the semi-coke feed balancer 10 to adjust the particle flow area in different regions of the feed bin 10-3, and sends more semi-coke into the preheating gas generator 11 to supply energy for the pyrolysis system. Conversely, more semi-coke is sent out of the pyrolysis device for other uses such as gasification, power generation, and carbon material preparation.

[0064] Through the above steps and methods, it is possible to realize that the low-rank oil-rich pulverized coal supplies energy to the system at the cost of burning part of its own carbon-containing substances (semi-coke), obtain coal tar after gas-solid separation, and the semi-coke is rationally utilized according to the particle size range. The system has a high coal tar yield, a high energy efficiency level, and relatively simple structure and convenient operation.

[0065] The above is only the specific embodiment of the present invention, and it does not limit the present invention in any way. The protection scope of the present invention shall be subject to the protection scope of the claimed rights.

Claims

1. An apparatus for pyrolyzing rich oil bituminous coal to produce coal tar, characterized in that, It includes a pyrolysis reactor (6). The oil and gas product outlet of the pyrolysis reactor (6) is connected to a multi-stage gas-solid separator. The solid phase outlets of each stage of the gas-solid separator are all connected to a semi-coke feed balancer (10). The semi-coke feed balancer (10) distributes the semi-coke particles separated by each stage of the gas-solid separator, and a part of them enters a preheated gas generator (11) to burn for pyrolysis heat supply, or simultaneously supply heat for pyrolysis and raw material preheating, and the other part is sent out as activated coke. The gas phase outlet of the last stage of the gas-solid separator is connected to an oil and gas separation unit (9), and the oil and gas separation unit (9) processes the gas phase product to obtain gas and tar. The pyrolysis reactor (6) includes a combustion chamber (13), a return material chamber (14), a pyrolysis chamber (15), a separation chamber (16) and a storage chamber (17). Among them, the combustion chamber (13) is located at the bottom and is directly connected to the pyrolysis chamber (15). The separation chamber (16) is located above the pyrolysis chamber (15) and separates the pyrolysis products into oil and gas and semi-coke. The storage chamber (17) is an annular area between the pyrolysis chamber (15) and the outer wall of the reactor (6). The return material chamber (14) is located between the storage chamber (17) and the combustion chamber (13), and the obtained semi-coke is sent back to the combustion chamber (13) through the storage chamber (17) and the return material chamber (14). The semi-coke feed balancer (10) includes a storage bin (10-2), a guide bin (10-3) and a guide cone (10-4). The storage bin (10-2) is above the guide bin (10-3) and the two are directly connected. The storage bin (10-2) is separated into two parts by a baffle with a channel in the middle and lower part, and particle inlets (10-1) are respectively connected to the two parts. The guide cone (10-4) is arranged in the guide bin (10-3). One side of the cross-section of the guide cone (10-4) is a semi-ellipse, the other side is a semi-circle, or both sides are asymmetric semi-ellipses. The longitudinal section of the guide cone (10-4) is a shape that tapers from the middle to both sides. The guide cone (10-4) is configured to be able to rotate along the vertical axis, and there is a particle outlet (10-5) at the bottom of the guide bin (10-3).

2. The device for pyrolyzing rich oil bituminous coal to produce coal tar according to claim 1, characterized in that, An internal circulation separator (16-1) is installed in the separation chamber (16). The internal circulation separator (16-1) is a columnar structure with an open bottom and a spherical closure at the top. It is sleeved on the top of the columnar pyrolysis chamber (15) and has an axial and radial distance from the pyrolysis chamber (15). The inner wall of the internal circulation separator (16-1) is connected to the outer wall of the pyrolysis chamber (15) by a baffle extending downward in a spiral shape, and the outer wall of the internal circulation separator (16-1) is connected to the inner wall of the reactor (6) by a baffle (16-2) extending upward in a spiral shape.

3. The device for pyrolyzing rich oil bituminous coal to produce coal tar according to claim 1, characterized in that, A plurality of material level balancing devices (18) for controlling the return of semi-coke are arranged in the return material chamber (14). The material level balancing device (18) includes a controller (21) and a balancer (22). The balancer (22) includes a housing (22-3) and an actuator (22-6). The inside of the housing (22-3) is a cavity (22-5). Above the cavity (22-5), there is a semi-coke inlet (22-1) accessing the return material chamber (14), and below, there is a semi-coke outlet (22-2) accessing the combustion chamber (13). The actuator (22-6) extends into the cavity (22-5). Under the control of the controller (21), it blocks or opens the semi-coke inlet (22-1), and / or blocks or opens the semi-coke outlet (22-2), thereby closing or opening the return material passage with the route of return material chamber (14) - semi-coke inlet (22-1) - cavity (22-5) - semi-coke outlet (22-2) - combustion chamber (13).

4. The device for pyrolyzing rich oil pulverized coal to produce coal tar according to claim 3, characterized in that, The controller (21) controls the opening amount of the actuator (22-6) for the semi-coke inlet (22-1) and / or the semi-coke outlet (22-2).

5. The device for pyrolyzing rich oil bituminous coal to produce coal tar according to claim 3, characterized in that, The material level balancing device (18) further includes a level gauge (19) and a static pressure gauge (20). The level gauge (19) and the static pressure gauge (20) are installed in the storage chamber (17) to jointly determine the material level in the storage chamber (17). The controller (21) controls the closing or opening action of the actuator (22-6) according to the level signal.

6. The device for pyrolyzing rich oil bituminous coal to produce coal tar according to claim 3 or 4 or 5, characterized in that, The actuator (22-6) includes a pneumatic system (22-6-1), a columnar plug (22-6-2), a slide rail (22-6-3), and a connecting rod (22-6-4). The slide rail (22-6-3) is in the shape of a cuboid and is attached to the semi-coke inlet (22-1) and / or the semi-coke outlet (22-2). A cylindrical chute is opened on the slide rail (22-6-3). One side of the chute is open, and several round holes (22-6-5) are opened on the other side. The pneumatic system (22-6-1) drives the columnar plug (22-6-2) to slide in the chute through the connecting rod (22-6-4). Different sliding positions enable the semi-coke inlet (22-1) and / or the semi-coke outlet (22-2) to communicate with the cavity (22-5) through different numbers of round holes (22-6-5).

7. The device for pyrolyzing rich oil bituminous coal to produce coal tar according to claim 1, characterized in that, Two guide ridges (10-3-1) along the up and down direction of the bin wall are symmetrically arranged in the guide bin (10-3).

8. A method for pyrolyzing rich oil pulverized coal to produce coal tar by using the device for pyrolyzing rich oil pulverized coal for producing coal tar according to claim 1, characterized in that, Including the following steps: Step 1), pressurize the pulverized coal to 0.8 - 5.0 MPa, preheat it, and then exchange heat with the high-temperature flue gas from the start-up furnace (1) or the preheated gas generator (11) to raise the temperature to 100 - 150 °C. During the start-up stage, heat is provided by the start-up furnace (1), and after normal operation, heat is provided by the preheated gas generator (11). Step 2), the preheated pulverized coal enters the pyrolysis chamber (15), mixes and exchanges heat with the high-temperature flue gas and semi-coke particles from the combustion chamber (13), and the temperature is raised to 500 - 650 °C. The pyrolysis reaction is completed during the upward movement in the pyrolysis chamber (15). Step 3), after the pyrolysis reaction is completed, the semicoke and the oil-gas pass through the separation chamber (16) and the multi-stage gas-solid separator for separation successively. The separated gas phase is further processed by the oil-gas separation unit (9) to obtain coal gas and tar. The semicoke separated by the separation chamber (16) enters the storage chamber (17), and then enters the combustion chamber (13) through the return material chamber (14), where it is mixed with oxygen and the high-temperature soot conveyed by the preheated gas generator (11). After combustion and heat exchange, it continues to enter the pyrolysis chamber (15) to complete the internal circulation process. The semicoke particles separated by the multi-stage gas-solid separator enter the semicoke feed balancer (10). Step 4), after being distributed by the semicoke feed balancer (10), a part of the semicoke particles enter the preheated gas generator (11) for combustion to supply heat for pyrolysis, or supply heat for both pyrolysis and raw material preheating simultaneously, and the other part is sent out as activated coke.

9. The method for pyrolyzing rich oil pulverized coal to produce coal tar according to claim 8, wherein In the said Step 3), the material level balance device (18) jointly determines the material level of the storage chamber (17) through the level gauge (19) and the static pressure gauge (20). After reaching the threshold value, the controller (21) controls the pneumatic system (22-6-1) of the actuator (22-6) to pull the connecting rod (22-6-4) and the columnar plug (22-6-2) to connect the storage chamber (17) with the combustion chamber (13). When the semicoke burns in the combustion chamber (13), the oxygen concentration at the oil-gas outlet of the reactor (6) and the temperature at the outlet of the separation chamber (16) are monitored in real time, and the oxygen input amount is controlled. When the material level of the storage chamber (17) is lower than the threshold value, the material level balance device (18) performs the opposite operation to isolate the storage chamber (17) from the combustion chamber (13). In the said Step 4), the semicoke feed balancer (10) is controlled by the feed controller (12). Under normal working conditions, the fine-particle semicoke separated by different stages of the gas-solid separator is sent into the preheated gas generator (11) for combustion, and the coarse-particle semicoke is sent out of the device for further processing and utilization. When the working conditions change, the feed controller (12) calculates the increase or decrease amount of the semicoke feed according to the oxygen input amount, the semicoke input amount, the combustion temperature, the flue gas outlet temperature, and the dust content in the flue gas in the preheated gas generator (11). When the feed amount needs to be increased, the feed controller (12) controls the rotating deflector cone (10-4) to adjust the particle flow area in different regions of the feed bin (10-3) to send more semicoke into the preheated gas generator (11) for supplying energy to the pyrolysis system. On the contrary, more semicoke is sent out of the pyrolysis device.

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