Reverse-flow feeding and gas taking device of variable-diameter reactor

Abstract

The invention relates to a countercurrent feeding and gas taking device of a variable-diameter reactor, and relates to the field of environmental protection equipment, the variable-diameter reactor is provided with a feeding section, one end of a material channel and one end of a gas pipe are fixedly connected with a rack, one end of the gas pipe sleeves the outer side of the other end of the material channel, the other end of the gas pipe extends into the feeding section, and the outer wall of the gas pipe and the feeding section are sealed through a fish scale sealing plate; an air outlet is formed in one end side wall of the air pipe; the length of the gas pipe in the variable-diameter reactor is greater than that of the feeding section; the vertical gate is vertically connected with the rack in a sliding mode and closes or opens one end of the material channel. The material channel is fixedly arranged and can be sealed through the vertical gate, the material channel is sealed through the material and the vertical gate at the same time, oxygen entering the variable-diameter reactor is reduced, and the anoxic environment of pyrolysis is guaranteed. The air pipe is fixedly arranged, the air outlet of the air pipe can be fixedly connected with a subsequent air guide pipe, and sealing performance is good. And the length of the gas pipe in the variable-diameter reactor is greater than that of the feeding section, so that most pyrolysis gas in the variable-diameter reactor can be conveniently led out from the gas pipe.

Description

Technical Field

[0001] The present invention relates to the field of environmental protection equipment, and particularly to a variable-diameter reactor countercurrent feeding and gas-taking device. Background Art

[0002] The invention patent application No. CN2021110059139 discloses a fluidized bed and a biomass reactor. The integrated reactor composed of a fluidizer and a pyrolysis reactor adopts a horizontal rotation mode, and has functions of homogenizing and refining materials such as extruding, stir-frying, and grinding the materials, overcoming the disadvantages that the existing biomass pyrolysis gasification furnaces (such as vertical furnaces, fluidized bed furnaces, and entrained flow bed furnaces) must perform pre-treatment such as pre-homogenization, pre-compaction, and pre-refinement on the materials.

[0003] In this patent, the feeding and gas outlet position adopts a double-layer structure with an inner and outer sleeve of a feeding cylinder and an exhaust cylinder, and relies on the material to seal the feeding cylinder. However, the sealing performance between the inside of the feeding cylinder and between the exhaust cylinder and the subsequent gas pipe cannot reach the best, and the heat loss in the integrated reactor and the entry of external oxygen will affect the pyrolysis efficiency in the integrated reactor. Summary of the Invention

[0004] The technical problem to be solved by the present invention is how to improve the sealing performance of the feeding and gas outlet position of the reactor.

[0005] The technical solution for the present invention to solve the above technical problem is as follows: A variable-diameter reactor countercurrent feeding and gas-taking device includes a variable-diameter reactor, a frame, a vertical gate, a material channel, and a gas pipe. The variable-diameter reactor has a feeding section. One end of the material channel and one end of the gas pipe are both fixedly connected to the frame. The variable-diameter reactor is rotationally connected to the frame. One end of the gas pipe is sleeved outside the other end of the material channel. The other end of the gas pipe extends into the feeding section. The space between the outer wall of the gas pipe and the feeding section is sealed by a fish-scale sealing plate. One end of the material channel has a feeding port, and one side wall of one end of the gas pipe has a gas outlet. The length of the gas pipe located inside the variable-diameter reactor is greater than the length of the feeding section. The vertical gate is vertically slidably connected to the frame, and the vertical gate closes or opens one end of the material channel.

[0006] The beneficial effects of the present invention are as follows: The feeding and gas outlet position of the variable-diameter reactor is realized by a three-layer structure of a feeding section, a gas pipe, and a material channel. The material channel is fixedly arranged and can be closed by a vertical gate. At the same time, when feeding, there is material blocking inside the material channel, and both the material and the vertical gate realize the blocking of the material channel, reducing the entry of oxygen into the variable-diameter reactor and ensuring an oxygen-deficient environment for pyrolysis. The gas pipe is also fixedly arranged, and the gas outlet of the gas pipe can be fixedly connected to the subsequent gas guide pipe, with good sealing performance. The pyrolysis gas flowing countercurrently in the variable-diameter reactor passes between the material channel and the gas pipe and is discharged through the gas outlet to the subsequent gas guide pipe. At the same time, the outer wall of the gas pipe and the feeding section are sealed by a fish-scale sealing plate to ensure that there is no gas leakage at the position where the feeding section rotates in cooperation with the gas pipe. The length of the gas pipe located inside the variable-diameter reactor is greater than the length of the feeding section, that is, the gas pipe extends into the space of the variable-diameter reactor subsequent to the feeding section, which is beneficial to leading out most of the pyrolysis gas in the variable-diameter reactor from the gas pipe.

[0007] On the basis of the above technical solutions, the present invention can be further improved as follows.

[0008] Further, the variable-diameter reactor countercurrent feeding and gas-taking device further includes a pusher hydraulic cylinder, the pusher hydraulic cylinder is fixedly connected to the frame, and the piston rod of the pusher hydraulic cylinder faces the material channel.

[0009] The beneficial effect of adopting the above further solution is: When feeding, the vertical gate is opened, the pusher hydraulic cylinder extends, and the material is pushed into the material channel. Or, when feeding bulk materials, the pusher hydraulic cylinder extends, appropriately compresses the material towards the vertical gate, then the vertical gate is opened, and the pusher hydraulic cylinder continues to extend and pushes the material into the material channel.

[0010] Further, the variable-diameter reactor countercurrent feeding and gas-taking device further includes a horizontal gate, the horizontal gate is horizontally slidably connected to the frame, the area between the pusher hydraulic cylinder and the vertical gate is the feeding area, and the horizontal gate closes or opens the upper part of the feeding area.

[0011] The beneficial effect of adopting the above further solution is: The horizontal gate and the vertical gate are alternately opened to realize feeding, further reducing the entry of oxygen into the feeding section.

[0012] Further, the variable-diameter reactor countercurrent feeding and gas-taking device further includes a bottom plate and a lift, the bottom plate is fixedly connected to the lift, and the lift drives the bottom plate to rise to be flush with the lower side of the material channel or to descend.

[0013] The beneficial effects of adopting the above further solution are as follows: When feeding bulk materials, the bottom plate rises to be flush with the lower side of the feed channel, serving as the bottom support and sealing plate of the feeding area, and the materials are fed into the feeding area from above the feeding area. When feeding packaged materials, the materials can either be fed from above the feeding area, or the elevator can be driven to lower the bottom plate, then place the packaged materials on the bottom plate, and subsequently the bottom plate rises to be flush with the lower side of the feed channel to send the packaged materials to the feeding area. In this way, the feeding of both types of materials can be taken into account, and the variable-diameter reactor countercurrent feeding gas-taking device of this solution has high versatility.

[0014] Further, both the feeding section and the gas pipe are cylindrical.

[0015] Further, the variable-diameter reactor further has a conical section and a discharging section. One end of the conical section is connected and communicated with the feeding section, and the other end is connected and communicated with the discharging section. The discharging section has a discharging port and a plurality of fluidization holes. One end of the inner side of the discharging port along the circumferential direction of the discharging section is hinged with a discharging door. The diameter of the conical section gradually decreases from one end to the other end. A guiding plate is fixed on the inner wall of the conical section. The diameter of one end of the conical section is larger than that of the feeding section, and the radius difference between the two is H.

[0016] The beneficial effects of adopting the above further solution are as follows: The feeding section, conical section, and discharging section of the variable-diameter reactor provide a reaction space with a suitable diameter ratio for the materials at different reaction stages, improving its space utilization rate and saving investment costs. And it provides an internal driving force for the countercurrent of materials and gas in the variable-diameter reactor.

[0017] Further, a cylindrical section is also provided between the feeding section and the conical section. The diameter of the cylindrical section is equal to the diameter of the end of the conical section close to the feeding section, and a material-lifting plate is fixed on the inner wall of the cylindrical section.

[0018] The beneficial effects of adopting the above further solution are as follows: The cylindrical section of the variable-diameter reaction kettle provides a larger initial reaction space for lightweight materials, increasing the output within a certain investment intensity and site area; providing a longer sufficient homogenization time for heterogeneous materials, which is beneficial to the stability of the products.

[0019] Further, the length of the cylindrical section is L3, the diameter of the cylindrical section is D3, and L3 / D3 = 0.1 - 10.

[0020] The beneficial effects of adopting the above further solution are as follows: The cylindrical section can obtain a reasonable initial reaction time of the materials under this length-diameter ratio.

[0021] Preferably, L3 / D3 = 1.

[0022] Further, the length of the conical section is L2, and L2 / H = 5 - 15.

[0023] The beneficial effects of adopting the above further scheme are as follows: A reasonable material advancing slope is set in the conical section, providing a suitable subsequent reaction space for the material.

[0024] Preferably, L2 / H = 10.

[0025] Further, the diameter of the discharge section is D1, and the length of the discharge section is L1, where L1 / D1 = 1 - 6.

[0026] The beneficial effects of adopting the above further scheme are as follows: In the case of this length-diameter ratio of the discharge section, a better material fluidization effect can be obtained.

[0027] Preferably, L1 / D1 = 3. BRIEF DESCRIPTION OF THE DRAWINGS

[0028] Figure 1 is a schematic cross-sectional structure diagram of the variable-diameter reactor of the present invention; Figure 2 is a schematic structure diagram when feeding at the bottom of the feeding area of the countercurrent feeding and gas-taking device of the variable-diameter reactor of the present invention; Figure 3 is Figure 2 a partial enlarged view of point A in the feeding section; Figure 4 is a schematic structure diagram when feeding at the top of the feeding area of the countercurrent feeding and gas-taking device of the variable-diameter reactor of the present invention; Figure 5 is a schematic structure diagram when feeding the material to the feeding section of the countercurrent feeding and gas-taking device of the variable-diameter reactor of the present invention.

[0029] In the drawings, the list of components represented by each reference numeral is as follows: 1. Feeding section; 2. Cylindrical section; 3. Conical section; 4. Discharge section; 5. Discharge port; 6. Material lifting plate; 7. Guide plate; 8. Pushing hydraulic cylinder; 9. Cross gate; 10. Bottom plate; 11. Lift; 12. Vertical gate; 13. Material channel; 14. Fish-scale sealing plate; 15. Air pipe; 16. Driven gear; 17. Support ring; 18. Roller; 19. Motor; 20. Driving gear; 21. Guide air pipe. DETAILED DESCRIPTION OF THE INVENTION

[0030] The principles and features of the present invention will be described below. The examples given are only used to explain the present invention and are not intended to limit the scope of the present invention.

[0031] As Figures 1 - 5As shown in the figure, this embodiment provides a variable-diameter reactor countercurrent feeding and gas-taking device. A variable-diameter reactor countercurrent feeding and gas-taking device includes a variable-diameter reactor, a frame, a vertical gate 12, a material channel 13, and a gas pipe 15. The variable-diameter reactor has a feeding section 1. One end of the material channel 13 and one end of the gas pipe 15 are both fixedly connected to the frame. The variable-diameter reactor is rotationally connected to the frame. One end of the gas pipe 15 is sleeved outside the other end of the material channel 13. The other end of the gas pipe 15 extends into the feeding section 1. The space between the outer wall of the gas pipe 15 and the feeding section 1 is sealed by a fish-scale sealing plate 14. One end of the material channel 13 has a feeding port, and one side wall of one end of the gas pipe 15 has an air outlet. The length of the gas pipe 15 inside the variable-diameter reactor is greater than the length of the feeding section 1. The vertical gate 12 is vertically slidably connected to the frame, and the vertical gate 12 closes or opens one end of the material channel 13.

[0032] The feeding and gas-taking position of the variable-diameter reactor is realized by a three-layer structure from outside to inside of the feeding section 1, the gas pipe 15, and the material channel 13. The material channel 13 is fixedly arranged and can be closed by the vertical gate 12. At the same time, there is material blocking inside the material channel 13 during feeding. Both the material and the vertical gate 12 realize the blocking of the material channel 13, reducing the entry of oxygen into the variable-diameter reactor and ensuring an oxygen-deficient environment for pyrolysis. The gas pipe 15 is also fixedly arranged. The air outlet of the gas pipe 15 can be fixedly connected to the subsequent gas guide pipe 21, and the sealing performance is good. The countercurrent pyrolysis gas in the variable-diameter reactor passes between the material channel 13 and the gas pipe 15 and is discharged to the subsequent gas guide pipe 21 through the air outlet. At the same time, the space between the outer wall of the gas pipe 15 and the feeding section 1 is sealed by a fish-scale sealing plate 14 to ensure that there is no gas leakage at the position where the feeding section 1 and the gas pipe 15 are rotationally matched. The length of the gas pipe 15 inside the variable-diameter reactor is greater than the length of the feeding section 1, that is, the gas pipe 15 extends into the space of the variable-diameter reactor subsequent to the feeding section 1, which is beneficial to leading out most of the pyrolysis gas in the variable-diameter reactor from the gas pipe 15.

[0033] In one specific example, when the variable-diameter reactor countercurrent feeding and gas-taking device is applied to an existing fluidized bed, the device of this solution is used to replace the feeding and pyrolysis structures such as the comprehensive reactor, fluidizer, and pusher cylinder in the existing fluidized bed. The air outlet at one end of the gas pipe 15 is used to connect to the gas guide pipe 21, and a crude gas induced draft fan is provided on the gas guide pipe 21.

[0034] Specifically, one end of the gas pipe 15 is closed and sealed with the outer side wall of the material channel 13, and an air outlet is provided on one side wall of one end of the gas pipe 15.

[0035] Specifically, as Figure 3As shown in the figure, a motor 19 is fixed on the frame. The output shaft of the motor 19 is fixedly connected to the driving gear 20. An outer wall of the feeding section 1 is coaxially and fixedly provided with a driven gear 16. The driven gear 16 is in transmission connection with the driving gear 20. An outer wall of the feeding section 1 is further fixedly provided with a support ring 17. Two rotatable idler rollers 18 are spaced on the frame. The rotating shaft of the idler roller 18 is parallel to the variable-diameter reactor. The support ring 17 is mounted on the two idler rollers 18. The motor 19 drives the variable-diameter reactor to rotate through the driving gear 20 and the driven gear 16. The idler rollers 18 provide support for the variable-diameter reactor and rotate therewith. One end of the variable-diameter reactor away from the feeding section 1 is rotatably connected to the fluidization chamber, or is also rotatably mounted on the frame by adopting an idler roller structure.

[0036] On the basis of the above technical solution, the variable-diameter reactor countercurrent feeding and gas-taking device further includes a pusher hydraulic cylinder 8. The pusher hydraulic cylinder 8 is fixedly connected to the frame. A piston rod of the pusher hydraulic cylinder 8 faces the material channel 13.

[0037] During feeding, the vertical gate 12 is opened, the pusher hydraulic cylinder 8 extends, and the material is pushed into the material channel 13. Or, when loose material (i.e., unpacked loose material) is fed, the pusher hydraulic cylinder 8 extends, presses the material against the vertical gate 12 appropriately, then the vertical gate 12 is opened, and the pusher hydraulic cylinder 8 continues to extend and pushes the material into the material channel 13.

[0038] On the basis of the above technical solution, the variable-diameter reactor countercurrent feeding and gas-taking device further includes a horizontal gate 9. The horizontal gate 9 is horizontally slidably connected to the frame. The area between the pusher hydraulic cylinder 8 and the vertical gate 12 is the feeding area. The horizontal gate 9 closes or opens the upper part of the feeding area.

[0039] The horizontal gate 9 and the vertical gate 12 are alternately opened to achieve feeding, further reducing the entry of oxygen into the feeding section 1.

[0040] Specifically, when feeding from the top of the feeding area, as Figure 4 shown, first open the horizontal gate 9 and feed the material; then close the horizontal gate 9. As Figure 5 shown, open the vertical gate 12, and the pusher hydraulic cylinder 8 pushes the material in the feeding area into the feeding section 1.

[0041] On the basis of the above technical solution, the variable-diameter reactor countercurrent feeding and gas-taking device further includes a bottom plate 10 and a lifter 11. The bottom plate 10 is fixedly connected to the lifter 11. The lifter 11 drives the bottom plate 10 to rise to be flush with the lower side of the material channel 13 or to descend.

[0042] When loose material is fed, as Figure 4As shown, the bottom plate 10 rises to be flush with the lower side of the material channel 13, serving as the bottom support and sealing plate of the feeding area. Materials are fed into the feeding area from above the feeding area. When feeding bailed materials (i.e., materials packed in bundles), the materials can either be fed from above the feeding area or, as Figure 2 shown, the elevator 11 is driven to lower the bottom plate 10, then the bailed materials are placed on the bottom plate 10, and subsequently the bottom plate 10 rises to be flush with the lower side of the material channel 13 to send the bailed materials to the feeding area. In this way, the feeding of two types of materials can be taken into account, and the variable-diameter reactor countercurrent feeding gas-taking device of this solution has high versatility.

[0043] Preferably, as Figure 2 shown, the bailed materials are fed into the feeding area from the bottom by the elevator 11, and during the process of feeding the bailed materials or sending them into the feeding section 1, the cross gate 9 is always closed. The frame is provided with a through hole at the bottom of the feeding area for the up-and-down movement of the bottom plate 10. The bottom plate 10 is in sealing cooperation with the through hole at the bottom of the feeding area. When the bottom plate 10 rises to be flush with the lower side of the material channel 13, the bottom plate 10 can seal the through hole at the bottom of the feeding area.

[0044] Based on the above technical solution, both the feeding section 1 and the air pipe 15 are cylindrical.

[0045] Optionally, the material channel 13 is cylindrical or prismatic. In one specific example, the material channel 13 is a cylindrical shape with a square cross-section.

[0046] Based on the above technical solution, the variable-diameter reactor further has a conical section 3 and a discharging section 4. One end of the conical section 3 is connected and communicated with the feeding section 1, and the other end is connected and communicated with the discharging section 4. The discharging section 4 has a discharging port 5 and a plurality of fluidization holes. One end of the inner side of the discharging port 5 along the circumferential direction of the discharging section 4 is hinged with a discharging door. The diameter of the conical section 3 gradually decreases from one end to the other end. A guiding plate 7 is fixed on the inner wall of the conical section 3. The diameter of one end of the conical section 3 is larger than the diameter of the feeding section 1, and the radius difference between the two is H.

[0047] Existing fluidized beds use equal-diameter reactors (cylindrical). For many unprepared but low-density biomass materials (such as straw, branches and leaves, foam, etc.), a larger initial space diameter-to-material ratio of the reactor is required (the diameter-to-material ratio refers to the ratio of the reactor diameter to the material diameter (particle size)). However, such materials are very easy to shrink when heated. As the diameter-to-material ratio increases, the equal-diameter reactor will cause waste of space, increase in cost, and reduction in thermal efficiency.

[0048] Among them, the material guiding plate 7 is used to push the material from the feeding section 1 to the discharging section 4 during the rotation of the variable-diameter reactor. Optionally, the material guiding plate 7 is spiral, and one, two or more are provided along the circumferential direction of the conical section 3, that is, a single-spiral material guiding structure, a double-spiral material guiding structure or a multi-spiral material guiding structure is provided; or, the material guiding plate 7 is a flat plate or an arc-shaped plate, and a plurality of material guiding plates 7 are arranged at intervals along a spiral line in the conical section 3.

[0049] Specifically, as the variable-diameter reactor rotates, the discharge door can cover or open the discharge port 5. By switching the forward and reverse rotations of the variable-diameter reactor, the opening and closing state of the discharge door when it is located on the lower side of the variable-diameter reactor can be changed, so as to realize discharging without stopping the machine.

[0050] On the basis of the above technical solution, a cylindrical section 2 is further provided between the feeding section 1 and the conical section 3. The diameter of the cylindrical section 2 is equal to the diameter of the conical section 3 at the end close to the feeding section 1, and a material lifting plate 6 is fixed on the inner wall of the cylindrical section 2.

[0051] The cylindrical section 2 of the variable-diameter reaction kettle provides a larger initial reaction space for light materials, increases the output within a certain investment intensity and site area; provides a longer sufficient homogenization time for heterogeneous materials, which is beneficial to the stability of the product.

[0052] Specifically, the other end of the air pipe 15 extends into the cylindrical section 2.

[0053] In this solution, the feeding section 1, the cylindrical section 2, the conical section 3 and the discharging section 4 of the variable-diameter reactor provide a reaction space with a suitable diameter ratio for the material at different reaction stages, improve its space utilization rate, and save investment costs. And it provides an internal driving force for the countercurrent of the material and gas in the variable-diameter reactor.

[0054] Specifically, the inner diameter of the cylindrical section 2 is larger than the inner diameter of the feeding section 1.

[0055] Specifically, when non-preformed but low-density biomass enters the variable-diameter reactor from the material channel 13, the temperature of the biomass is low at this time. Rotation causes the compressed material to expand and loosen, and a larger space is required to tumble in the variable-diameter reactor. Otherwise, if the space is too small, a material wall is easily formed. Therefore, a cylindrical section 2 with a suddenly increased diameter is designed to facilitate the tumbling of the material. And, the feeding section 1 and the cylindrical section 2 are connected by an annular plate perpendicular to the axis of the feeding section 1. The feeding section 1 and the cylindrical section 2 are transitioned through a right-angle structure to avoid material jamming and forming a material wall. As the material tumbles and is heated, a thermal shrinkage reaction (drying) occurs and the particle size decreases; as the material moves forward, the temperature becomes higher and higher. The material completes the thermal shrinkage and partial pyrolysis reactions in the cylindrical section 2 and forms a coke mass.

[0056] Subsequently, the coke-like materials enter the conical section 3, where the temperature becomes higher and higher, the volatile components volatilize, the particle size becomes smaller and smaller, the required diameter of the variable-diameter reactor decreases, and the reaction space reduces. Therefore, the conical section 3 is designed as a cone, meeting the requirements of the reaction process.

[0057] Finally, the materials that have completed the pyrolysis reaction form carbon particles and are further carbonized in the discharge section 4. At this time, the particle diameter is the smallest. Therefore, the discharge section 4 is located at the apex of the conical section 3.

[0058] Specifically, a plurality of lifting plates 6 are circumferentially and spacedly arranged along the cylindrical section 2. In one specific example, there are 2 or 4 lifting plates 6.

[0059] Specifically, the lifting plate 6 is an arc-shaped plate, that is, a plate bent in a C shape. One end of it is fixedly connected to the cylindrical section 2, and the other end bends forward in the rotation direction of the cylindrical section 2; furthermore, it can also be set as an arc-shaped plate that bends obliquely towards the conical section 3. When the variable-diameter reactor rotates, the lifting plate 6 brings the agglomerated materials and powder materials to the upper part of the top of the variable-diameter reactor and gradually pours them out, making them fluidize in the space of the variable-diameter reactor, increasing the surface area of the materials in contact with the heat medium and the reaction time, and increasing the reaction efficiency. When the lifting plate 6 bends obliquely towards the conical section 3, while the variable-diameter reactor rotates, the materials can also be pushed along the axial direction of the variable-diameter reactor towards the conical section 3.

[0060] On the basis of the above technical solution, the length of the cylindrical section 2 is L3, the diameter of the cylindrical section 2 is D3, and L3 / D3 = 0.1 - 10.

[0061] The cylindrical section 2 can achieve a reasonable initial reaction time of the materials at this length-diameter ratio.

[0062] Specifically, the diameter of the feeding section 1 is D2, and D3 = 2*H + D2.

[0063] Preferably, L3 / D3 = 1.

[0064] On the basis of the above technical solution, the length of the conical section 3 is L2, and L2 / H = 5 - 15.

[0065] The conical section 3 is provided with a reasonable slope for the advancement of the materials, providing a suitable subsequent reaction space for the materials.

[0066] Preferably, L2 / H = 10.

[0067] On the basis of the above technical solution, the diameter of the discharge section 4 is D1, the length of the discharge section 4 is L1, and L1 / D1 = 1 - 6.

[0068] The discharge section 4 can obtain a better fluidization effect of the materials at this length-diameter ratio.

[0069] Preferably, L1 / D1 = 3.

[0070] In the description of the present invention, the meaning of "a plurality of" is at least two, such as two, three, etc., unless otherwise specifically defined.

[0071] In the description of this specification, the descriptions with reference to terms such as "one embodiment", "some embodiments", "examples", "specific examples" or "some examples", etc. mean that the specific features, structures, materials or characteristics described in connection with the embodiment or example are included in at least one embodiment or example of the present invention. In this specification, the schematic expressions of the above terms do not necessarily refer to the same embodiment or example. Moreover, the specific features, structures, materials or characteristics described can be combined in a suitable manner in any one or more embodiments or examples. In addition, without contradiction, those skilled in the art can combine and combine the different embodiments or examples described in this specification and the features of different embodiments or examples.

[0072] In the description of the present invention, it should be noted that unless otherwise clearly specified and defined, the terms "installed", "connected" and "connected" should be understood in a broad sense. For example, it can be a fixed connection, a detachable connection, or an integral connection; it can be directly connected, or indirectly connected through an intermediate medium, and it can be the communication inside two components. For those of ordinary skill in the art, the specific meanings of the above terms in the present invention can be understood according to specific situations.

[0073] The above are only the preferred embodiments of the present invention and are not intended to limit the present invention. Any modifications, equivalent replacements, improvements, etc. made within the spirit and principle of the present invention shall be included in the protection scope of the present invention.

Claims

1. A variable-diameter reactor countercurrent feeding and gas-taking device, characterized in that, It includes a variable-diameter reactor, a frame, a vertical gate (12), a feed channel (13) and an air pipe (15). The variable-diameter reactor has a feed section (1). One end of the feed channel (13) and one end of the air pipe (15) are both fixedly connected to the frame. The variable-diameter reactor is rotationally connected to the frame. One end of the air pipe (15) is sleeved outside the other end of the feed channel (13). The other end of the air pipe (15) extends into the feed section (1). The space between the outer wall of the air pipe (15) and the feed section (1) is sealed by a fish-scale sealing plate (14). One end of the feed channel (13) has a feed port, and one side wall of one end of the air pipe (15) has an air outlet. The length of the air pipe (15) located inside the variable-diameter reactor is greater than the length of the feed section (1). The vertical gate (12) is vertically slidably connected to the frame, and the vertical gate (12) closes or opens one end of the feed channel (13).

2. The variable-diameter reactor countercurrent feeding and gas-taking device according to claim 1, characterized in that, It further includes a pusher hydraulic cylinder (8). The pusher hydraulic cylinder (8) is fixedly connected to the frame, and the piston rod of the pusher hydraulic cylinder (8) faces the feed channel (13).

3. The variable-diameter reactor countercurrent feeding and gas-taking device according to claim 2, characterized in that, It further includes a horizontal gate (9). The horizontal gate (9) is horizontally slidably connected to the frame. The area between the pusher hydraulic cylinder (8) and the vertical gate (12) is the feeding area, and the horizontal gate (9) closes or opens the upper part of the feeding area.

4. The variable-diameter reactor countercurrent feeding and gas-taking device according to claim 3, characterized in that, It further includes a bottom plate (10) and a lifter (11). The bottom plate (10) is fixedly connected to the lifter (11), and the lifter (11) drives the bottom plate (10) to rise to be flush with the lower side of the feed channel (13) or to descend.

5. The variable-diameter reactor countercurrent feeding and gas-taking device according to claim 1, characterized in that, Both the feed section (1) and the air pipe (15) are cylindrical.

6. The variable-diameter reactor countercurrent feeding and gas-taking device according to any one of claims 1-5, characterized in that, The variable-diameter reactor further has a conical section (3) and a discharge section (4). One end of the conical section (3) is connected and communicated with the feed section (1), and the other end is connected and communicated with the discharge section (4). The discharge section (4) has a discharge port (5) and a plurality of fluidization holes. One end along the circumferential direction of the inner side of the discharge port (5) of the discharge section (4) is hinged with a discharge door. The diameter of the conical section (3) gradually decreases from one end to the other end. A guiding plate (7) is fixed on the inner wall of the conical section (3). The diameter of one end of the conical section (3) is greater than the diameter of the feed section (1), and the radius difference between the two is H.

7. The variable-diameter reactor countercurrent feeding and gas-taking device according to claim 6, characterized in that, A cylindrical section (2) is further provided between the feed section (1) and the conical section (3). The diameter of the cylindrical section (2) is equal to the diameter of the end of the conical section (3) close to the feed section (1), and a material-lifting plate (6) is fixed on the inner wall of the cylindrical section (2).

8. The variable-diameter reactor countercurrent feeding and gas-taking device according to claim 7, characterized in that, The length of the cylindrical section (2) is L3, the diameter of the cylindrical section (2) is D3, and L3 / D3 = 0.1 - 10.

9. The variable-diameter reactor countercurrent feeding and gas-taking device according to claim 6, characterized in that, The length of the conical section (3) is L2, and L2 / H = 5 - 15.

10. The variable-diameter reactor countercurrent feeding and gas-taking device according to claim 6, characterized in that, The diameter of the discharge section (4) is D1, the length of the discharge section (4) is L1, and L1 / D1 = 1 - 6.

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