Dual media tfb gasification incinerator and method of waste gasification incineration

Abstract

This invention discloses a dual-medium TFB gasification incinerator and a method for implementing waste gasification incineration. The incinerator includes a furnace body, a gas-solid separator, a waste heat recovery device, and a furnace body support. The furnace body comprises a gasification section, a combustion section, and a heat exchange section connected sequentially from bottom to top. The combustion section and the heat exchange section are indirectly connected. The furnace body support includes at least one layer of crossbeams, which are higher than the connecting parts on the combustion section and face towards the furnace body. Each layer of crossbeams has a support plate on the side closest to the furnace body. Each support plate supports a stage of heat exchange furnace wall and a heat transfer oil coil located on the inner surface of that stage's heat exchange furnace wall. Flexible connection seals are provided between adjacent stages of heat exchange furnace walls and between the heat exchange furnace wall and the combustion section furnace wall. The furnace body portions of the gasification and combustion sections are suspended from the crossbeams adjacent to the connecting parts via the connecting parts. This incinerator has high flue gas heat exchange efficiency, high process heat utilization rate, effectively handles the thermal expansion sealing problem of the furnace body, has wide fuel adaptability, high efficiency, low emissions, system stability, and high safety.

Description

[0001] This application is a divisional application of China, filed on June 15, 2022, with application number 202210681582.9, entitled "Separation device and cooking appliance dual-medium TFB gasification incinerator and method for implementing waste gasification incineration". Technical Field

[0002] This invention relates to the field of gasification combustion, and more specifically, to a dual-medium TFB gasification incinerator and a method for implementing waste gasification incineration. Background Technology

[0003] Incineration is the optimal method for waste reduction, resource recovery, and harmless disposal. Existing waste incinerators mainly include fixed-bed incinerators, fluidized-bed incinerators, rotary kiln incinerators, and pyrolysis incinerators. The main technical means of fluidized-bed incinerators for treating waste is to use primary air to blow up and suspend inert bed material and waste to form a fluidized bed layer, using the inert bed material in the fluidized bed as a heat carrier to incinerate the waste entering the furnace. Turbulent fluidized bed (TFB) is one of the effective means of gasifying and incinerating waste, with many advantages such as wide fuel adaptability, very low initial emissions, and simple process flow. However, existing turbulent fluidized bed gasification incinerators still have room for improvement and optimization. Existing turbulent fluidized beds (TFBs) primarily use a single heat exchange medium, such as water or thermal oil. However, in practical applications, it is sometimes necessary to use two media simultaneously, such as when incinerating county-level waste while simultaneously supplying steam, or when supplying thermal oil to produce high-quality organic fertilizer. The high-temperature flue gas generated during the gasification and combustion of waste in the gasification incinerator carries a large amount of heat and a certain amount of ash. How to fully utilize the waste heat is an important issue in waste resource utilization. Using two media simultaneously is not a simple matter of one plus one equals two; it will bring many new problems, such as significant differences in their flow and heat transfer characteristics, and different structural requirements. In addition, thermal expansion and sealing are common problems in existing incinerators. If not handled properly, it can lead to instability in the furnace structure and pose significant safety hazards. Using two structures will bring even more new structural problems related to expansion and sealing. Summary of the Invention

[0004] This invention aims to at least partially solve one of the technical problems in related technologies. Therefore, one objective of this invention is to propose a dual-medium TFB gasification incinerator and a method for implementing waste gasification incineration. This dual-medium TFB gasification incinerator not only simultaneously provides both steam and thermal oil as media to meet different needs, but also features high flue gas heat exchange efficiency and high waste heat utilization. It achieves maximum thermal efficiency by using a stepped arrangement of water-cooled walls, thermal oil coils, thermal oil convection pipes, economizer pipes with water as the medium inside the pipes, and an air preheater to fully absorb heat. Furthermore, it effectively addresses the thermal expansion sealing problem between the lower furnace body (composed of water-cooled wall evaporation heating surfaces) and the upper furnace body (composed of thermal oil coils). It boasts advantages such as wide fuel adaptability, high efficiency, low emissions, system stability, and high safety.

[0005] In one aspect of the invention, a dual-medium TFB gasification incinerator is provided. According to an embodiment of the invention, the dual-medium TFB gasification incinerator includes: a furnace body, a gas-solid separator, and a waste heat recovery device connected in sequence; and a furnace body support, wherein:

[0006] The furnace body includes a gasification section, a combustion section, and a heat exchange section connected sequentially from bottom to top. The bottom of the gasification section is provided with a first air distribution device and a slag outlet. The gasification section includes an upper variable cross-section zone, a constant cross-section zone, and a lower variable cross-section zone arranged in an upper, middle, and lower manner. The cross-sectional area of ​​the upper variable cross-section zone gradually increases from top to bottom, and the cross-sectional area of ​​the lower variable cross-section zone gradually decreases from top to bottom. The cross-sectional area of ​​the upper variable cross-section zone is not less than the cross-sectional area of ​​the combustion section. The side of the combustion section is provided with a second air distribution device.

[0007] The furnace walls of the gasification section and the combustion section are both water-cooled walls; the furnace walls of the heat exchange section and the combustion section are indirectly connected, and the outer surface of the combustion section furnace wall is provided with a connecting part. The heat exchange section includes at least one stage of heat exchange furnace wall, with adjacent stages of heat exchange furnace walls arranged vertically and indirectly connected. The inner surface of each stage of the heat exchange furnace wall is provided with a set of heat transfer oil coils, and the flow direction of the heat transfer oil in each set of heat transfer oil coils is bottom in and top out. The top of the heat exchange section is provided with a hot flue gas outlet, and the hot flue gas outlet is connected to the waste heat recovery device through the gas-solid separator.

[0008] The waste heat recovery device is provided from top to bottom with a heat-conducting oil pipe, an economizer and an air preheater. The hot air outlet of the air preheater is connected to at least one of the gasification section air inlet and the combustion section air inlet.

[0009] The furnace support includes a steel frame body and at least one layer of support plates. The support plates are connected to the steel frame body and are higher than the connecting part and face the furnace body. Each layer of support plates supports one stage of the heat exchange furnace wall and the heat transfer oil coil provided on the inner surface of the heat exchange furnace wall of that stage. Soft connection seals are provided between adjacent heat exchange furnace walls and between the heat exchange furnace wall and the combustion section furnace wall. The furnace body parts of the gasification section and the combustion section are suspended by the connecting part on one layer of support plates located between the heat exchange furnace wall and the combustion section furnace wall. The support plates are arranged circumferentially around the furnace body. Alternatively, the furnace support also includes a first crossbeam. The first crossbeam is provided on the steel frame body at a portion higher than the connecting part and facing the furnace body. The furnace body parts of the gasification section and the combustion section are suspended by the connecting part on the first crossbeam. The first crossbeam is arranged circumferentially around the furnace body.

[0010] According to the dual-medium TFB gasification incinerator of the present invention, by using both heat transfer oil and water as the main cooling media, and by cascading water-cooled walls, heat transfer oil coils, heat transfer oil convection tube banks, economizer tube banks with water as the medium inside the tubes, and air preheaters, the maximum thermal efficiency is achieved by fully absorbing heat. On the one hand, it can achieve a heat exchange efficiency far higher than that of using heat transfer oil or water alone, and obtain process heat in the form of both hot oil and steam, which is convenient for use in chemical, food, organic fertilizer and other production operations; on the other hand, it can also provide gasification agent in the gasification section and / or combustion section. The combustion air is preheated to improve gasification and combustion efficiency while reducing production costs. In addition, by using a furnace body support to suspend the furnace body, the main furnace chamber is formed into a structure with the bottom suspended and the top supported. The joint between the furnace body support and the furnace body can also be used as a fixed end, allowing the furnace body to expand downward (due to gravity). During the expansion process, the furnace body's seal will not be affected. This can effectively solve the problem of thermal expansion and sealing between the lower furnace body composed of water-cooled wall evaporation heating surface and the upper furnace body composed of heat transfer oil coil, avoiding poor sealing due to thermal expansion and the resulting poor furnace body structural stability and safety issues.

[0011] According to another aspect of the present invention, a method for waste gasification and incineration using the aforementioned dual-medium TFB gasification incinerator is provided. According to an embodiment of the present invention, the method includes:

[0012] (1) The waste material is fed to the gasification section at the bottom of the furnace for gasification to obtain gasification gas and solid residue. The solid residue is discharged from the furnace intermittently.

[0013] (2) The gasified gas is introduced into the combustion section in the middle of the furnace body for combustion to obtain high-temperature flue gas after combustion;

[0014] (3) The high-temperature flue gas after combustion is cooled by heat exchange through a heat transfer oil coil to obtain medium-temperature flue gas;

[0015] (4) The medium-temperature flue gas is separated into gas and solid by a gas-solid separator to obtain primary purified flue gas;

[0016] (5) The primary purified flue gas enters the waste heat recovery device, and is discharged after heat exchange through the heat-conducting oil pipe, the economizer and the air preheater in sequence.

[0017] According to the waste gasification and incineration method of the above embodiments of the present invention, while incinerating waste, the high-temperature flue gas heat can be fully utilized step by step according to the flue gas flow, and the heat exchange efficiency can be improved. In addition, the above method can also effectively deal with the thermal expansion and sealing problem of the furnace body, avoiding the problems of poor furnace body structural stability or poor sealing due to thermal expansion, and thus the resulting safety hazards. Therefore, this method is not only simple in process and easy to operate, but also has a high energy grade, which can achieve full resource utilization and harmless treatment of waste, and also ensure the stability and safety of the furnace body structure.

[0018] Additional aspects and advantages of the invention will be set forth in part in the description which follows, and in part will be obvious from the description, or may be learned by practice of the invention. Attached Figure Description

[0019] The above and / or additional aspects and advantages of the present invention will become apparent and readily understood from the description of the embodiments taken in conjunction with the following drawings, in which:

[0020] Figure 1 This is a schematic diagram of the structure of a dual-medium TFB gasification incinerator according to an embodiment of the present invention.

[0021] Figure 2 This is a schematic diagram of the structure of a dual-medium TFB gasification incinerator according to another embodiment of the present invention.

[0022] Figure 3 This is a schematic diagram of the structure of a dual-medium TFB gasification incinerator according to yet another embodiment of the present invention.

[0023] Figure 4 This is a schematic diagram of the structure of a dual-medium TFB gasification incinerator according to yet another embodiment of the present invention.

[0024] Figure 5 This is a schematic diagram of the furnace structure of a dual-medium TFB gasification incinerator according to an embodiment of the present invention.

[0025] Figure 6 This is a schematic diagram of the structure of a ventilation and slag discharge system according to an embodiment of the present invention.

[0026] Figure 7This is a schematic diagram of a slag discharge valve according to an embodiment of the present invention.

[0027] Figure 8 This is a cross-sectional view of an ash removal device according to an embodiment of the present invention.

[0028] Figure 9 This is a schematic diagram of a structure in which a wear-resistant plate is provided on the heat exchange tube of a waste heat recovery device according to an embodiment of the present invention.

[0029] Figure 10 This is a structural schematic diagram of the cross-section of an abrasion-resistant plate according to an embodiment of the present invention.

[0030] Figure 11 This is a structural schematic diagram of the cross-section of the abrasion plate according to another embodiment of the present invention.

[0031] Figure 12 This is a side view of a single heat exchange tube and a wear-resistant plate according to an embodiment of the present invention.

[0032] Figure 13 This is a top view of a single heat exchange tube and a wear-resistant plate according to an embodiment of the present invention.

[0033] Figure 14 This is a structural schematic diagram showing the relative position of the anti-wear plate slope and the heat exchange tube according to an embodiment of the present invention.

[0034] Figure 15 This is a schematic diagram of the dimensions of the abrasion plate and the flat area of ​​the windward side of the heat exchange tube according to an embodiment of the present invention.

[0035] Figure 16 This is a schematic diagram of the structure of a waste heat recovery device according to an embodiment of the present invention, in which the heat transfer oil pipes or economizer pipes are arranged in parallel rows.

[0036] Figure 17 This is a schematic diagram of the structure of a waste heat recovery device according to an embodiment of the present invention, in which the heat transfer oil pipes or economizer pipes are arranged in an alternating parallel pattern.

[0037] Figure label:

[0038] 100-Furnace body; 110-Gasification section; 120-Combustion section; 130-Heat exchange section; 140-Flexible connection seal; 150-Steam drum; 111-Upper variable cross-section zone; 112-Equal cross-section zone; 113-Lower variable cross-section zone; 114-First air distribution device; 115-Slag outlet; 116-Bottom air inlet of gasification section; 117-Side wall air inlet of gasification section; 121-Air inlet of combustion section; 122-Connecting part; 131-Heat transfer oil coil; 132-Hot flue gas outlet; 133-Heat exchange furnace wall; 200-Gas-solid separator; 210-First Two ash outlets; 300-Waste heat recovery device; 310-Heat transfer oil pipe row; 311-Heat transfer oil heat exchanger tube; 320-Economizer; 321-Heat transfer water heat exchanger tube; 330-Air preheater; 331-First air preheater; 332-Second air preheater; 333-Baffle plate; 340-First ash outlet; 350-Flue gas outlet; 400-Furnace body support; 410-Steel frame body; 420-First crossbeam; 430-Support plate; 440-Second crossbeam; H-Total height of furnace body; L1-Length of combustion section; L2-Length of gasification section.

[0039] 1141-Main air distribution plate; 1142-Primary air chamber; 1143-Secondary air distribution plate; 161-Slag discharge air chamber; 162-Slag discharge channel; 1631-First slag discharge valve; 1632-Second slag discharge valve; 164-Fluidizing gas flow channel; 165-Fluidizing gas circulation inlet; 166-Large waste outlet; 1633-First rack; 1634-First reducer; 1635-First motor; 1636-Second rack; 1637-Second reducer; 1638-Second motor; 500-Ash discharge device; 510-Ash hopper; 520-Spiral scraper; 550-Gear; 540-Coupling; 530-Motor; 560-Temperature measuring element; 570-Limiting protrusion; 600-Abrasion plate; 610-Bracket; 611-First connecting hole; 620-Connecting rod; 621-Second connecting hole. Detailed Implementation

[0040] Embodiments of the present invention are described in detail below, examples of which are illustrated in the accompanying drawings, wherein the same or similar reference numerals denote the same or similar elements or elements having the same or similar functions throughout. The embodiments described below with reference to the accompanying drawings are exemplary and intended to explain the present invention, and should not be construed as limiting the present invention.

[0041] In the description of this invention, it should be understood that the terms "center," "length," "upper," "lower," "left," "right," "vertical," "horizontal," "top," "bottom," "inner," "outer," and "circumferential," etc., indicating orientation or positional relationships, are based on the orientation or positional relationships shown in the accompanying drawings and are only for the convenience of describing the invention and simplifying the description, and do not indicate or imply that the device or element referred to must have a specific orientation, or be constructed and operated in a specific orientation, and therefore should not be construed as a limitation of the invention. Furthermore, the terms "first" and "second" are used for descriptive purposes only and should not be construed as indicating or implying relative importance or implicitly specifying the number of indicated technical features. Thus, a feature defined as "first" or "second" may explicitly or implicitly include at least one of that feature. In the description of this invention, "a plurality of" means at least two, such as two, three, etc., unless otherwise explicitly specified. In this invention, unless otherwise explicitly specified and limited, terms such as "installation," "connection," "joining," and "fixing" should be interpreted broadly. For example, they can refer to a fixed connection, a detachable connection, or an integral part; they can refer to a mechanical connection or an electrical connection; they can refer to a direct connection or an indirect connection through an intermediate medium; they can refer to the internal communication of two components or the interaction between two components, unless otherwise explicitly limited. Those skilled in the art can understand the specific meaning of the above terms in this invention according to the specific circumstances. In this invention, unless otherwise explicitly specified and limited, "above" or "below" the second feature can mean that the first feature is in direct contact with the second feature, or that the first feature is in indirect contact through an intermediate medium. Furthermore, "above," "on top of," and "on top" can mean that the first feature is directly above or diagonally above the second feature, or simply that the first feature is at a higher horizontal level than the second feature. "Below," "below," and "under" the second feature can mean that the first feature is directly below or diagonally below the second feature, or simply that the first feature is at a lower horizontal level than the second feature.

[0042] In one aspect of the invention, a dual-medium TFB gasification incinerator is provided. According to an embodiment of the invention, reference is made to... Figure 1 Understanding this dual-media TFB gasification incinerator, it comprises: a furnace body 100, a gas-solid separator 200, and a waste heat recovery device 300 connected in sequence; and a furnace body support 400. Wherein:

[0043] The furnace body 100 includes a gasification section 110, a combustion section 120, and a heat exchange section 130 connected sequentially from bottom to top. The bottom of the gasification section 110 is provided with a first air distribution device 114 and a slag outlet 115. The gasification section 110 includes an upper variable cross-section zone 111, a constant cross-section zone 112, and a lower variable cross-section zone 113 arranged in an upper, middle, and lower manner. The cross-sectional area of ​​the upper variable cross-section zone 111 (perpendicular to the height direction of the furnace body) gradually increases from top to bottom, and the cross-sectional area of ​​the lower variable cross-section zone 113 (perpendicular to the height direction of the furnace body) gradually decreases from top to bottom. The cross-sectional area of ​​the upper variable cross-section zone 111 is not less than the cross-sectional area of ​​the combustion section 120 and the heat exchange section 130 (wherein, the combustion section 120 and the heat exchange section 130 can be independently arranged with constant cross-sections). The side of the combustion section 120 is provided with a second air distribution device.

[0044] The furnace walls of the gasification section 110 and the combustion section 120 are both water-cooled walls. The furnace walls of the heat exchange section 130 and the combustion section 120 are indirectly connected. The outer surface of the combustion section 120 furnace wall is provided with a connecting part 122. The heat exchange section 130 includes at least one stage of heat exchange furnace wall 133. Adjacent heat exchange furnace walls 133 are arranged vertically and indirectly connected. The inner surface of each heat exchange furnace wall 133 is provided with a set of heat transfer oil coils 131. The flow direction of the heat transfer oil in each set of heat transfer oil coils 131 is bottom in and top out (that is, the cold oil inlet of each set of heat transfer oil coils is located at the lower part of the heat exchange furnace wall 133, and the hot oil outlet is at the bottom). Located at the upper part of the heat exchange furnace wall 133, the heat transfer oil enters from the bottom and exits from the top to ensure that a small amount of steam or non-condensable gas will not adhere to the inner surface of the heat transfer oil pipe wall after the heat transfer oil is heated. The top of the heat exchange section 130 is provided with a hot flue gas outlet 132, which is connected to the waste heat recovery device 300 through a gas-solid separator 200. The waste heat recovery device 300 is provided with a heat transfer oil pipe bank 310, an economizer 320 and an air preheater 330 from top to bottom. The hot air outlet of the air preheater 330 is connected to at least one of the air inlet of the gasification section 110 and the air inlet of the combustion section 120.

[0045] The furnace body support 400 includes a steel frame body 410 and at least one layer of support plates 430. The support plates 430 are connected to the steel frame body 410, and are higher than the connecting part 122 and facing the furnace body 100. Each layer of support plates 430 supports a primary heat exchange furnace wall 133 and a heat transfer oil coil 131 provided on the inner surface of the primary heat exchange furnace wall 133. Soft connection seals 140 are provided between adjacent heat exchange furnace walls 133 and between the heat exchange furnace wall 133 and the furnace wall of the combustion section 120. The furnace body part of the gasification section 110 and the furnace body part of the combustion section 120 are also included. The furnace body is suspended by the connecting part 122 on a support plate 430 located between the heat exchange furnace wall 133 and the combustion section furnace wall 120. The support plate 430 can be arranged around the circumference of the furnace body. Alternatively, the furnace body support 400 can also include a first crossbeam 420. The first crossbeam 420 is located on the steel frame body 400 at a height above the connecting part 122 and facing the furnace body 100. The furnace body parts of the gasification section 110 and the combustion section 120 are suspended by the connecting part 122 on the first crossbeam 420. The first crossbeam 420 is arranged around the circumference of the furnace body. The steel frame body 410 is connected to the ground or other fixed surfaces to achieve overall fixation, support, and suspension. The support plate 430 can be arranged around the circumference of the furnace body. The adjacent heat exchange furnace walls 133 can be welded to the support plate 430 or fixedly connected in other ways. It is preferable to provide flexible connections (not shown) for sealing between the adjacent heat exchange furnace walls 133 and the support plate 430. Correspondingly, the lower part of the heat exchange furnace wall 133 connected to the combustion section 120 furnace wall can be welded to the support plate 430 or fixedly connected in other ways. It is preferable to provide flexible connections (not shown) for sealing between the combustion section 120 furnace wall and the support plate 430, and between the lower part of the heat exchange furnace wall 133 connected to the combustion section 120 furnace wall and the support plate 430. Furthermore, the flexible connection seal can be a metal flexible connection seal, such as using a copper busbar flexible connection to achieve the seal.

[0046] This dual-medium TFB gasification incinerator not only simultaneously provides both steam and thermal oil to meet different needs, but also boasts high flue gas heat exchange efficiency and high waste heat utilization. It achieves maximum thermal efficiency through a tiered configuration of water-cooled walls, thermal oil coils, thermal oil convection tube banks, economizer tube banks with water as the medium inside the tubes, and an air preheater to fully absorb heat. Furthermore, it effectively addresses the thermal expansion sealing problem between the lower furnace body (composed of water-cooled wall evaporation heating surfaces) and the upper furnace body (composed of thermal oil coils). It offers advantages such as wide fuel adaptability, high efficiency, low emissions, system stability, and high safety. It should be noted that in the dual-medium TFB gasification incinerator of this invention, "dual-medium" refers to the heat exchange media within the furnace body, namely water and thermal oil.

[0047] The following is for reference. Figures 1-15The furnace body 100, gas-solid separator 200, and waste heat recovery device 300 of the dual-medium TFB gasification incinerator are described in detail.

[0048] Furnace body 100

[0049] According to an embodiment of the present invention, reference Figure 1 To facilitate the suspension of the furnace body sections of the gasification section 110 and combustion section 120, both sections can be suspended via the connecting part 122 from a support plate 430 located between the heat exchange furnace wall 133 and the combustion section 120 furnace wall; or, refer to... Figure 2 It is understood that a first crossbeam 420 can be further provided on the furnace body support 400, with the first crossbeam 420 positioned on the steel frame body 400 above the connecting part 122 and facing the furnace body 100. This allows the furnace body portions of the gasification section 110 and the combustion section 120 to be suspended from the first crossbeam 420 via the connecting part 122. In this case, a support plate 430 located between the heat exchange furnace wall 133 and the combustion section 120 furnace wall can be provided on the first crossbeam 420 near the furnace body 100. It is understood that the support plate 430 can be integrally formed with the first crossbeam 420, or it can be connected in a detachable manner such as by screws or snap-fits, thereby achieving the connection between the support plate and the steel frame body. This simplifies the furnace structure and facilitates the assembly, disassembly, and maintenance of the furnace body. Furthermore, it is understood that the first crossbeam 420 can be arranged circumferentially along the furnace body 100.

[0050] According to an embodiment of the present invention, reference Figure 3 It is understood that the furnace support 400 may further include at least one layer of second crossbeams 440. The second crossbeams 440 may be located on the steel frame body 400 at a portion higher than the first crossbeam 420 and facing the furnace body 100. The number of layers of second crossbeams 440 may be equal to the number of layers of support plates 430 located between the heat exchange furnace walls 133. Each layer of support plates 430 located between two adjacent heat exchange furnace walls 133 is located on one layer of second crossbeams 440 on the side closest to the furnace body 100. It is understood that the support plates 430 may be integrally formed with the second crossbeams 440, or they may be connected by detachable methods such as screws or snap-fits, thereby achieving the connection between the support plates and the steel frame body. This facilitates the assembly, disassembly, and maintenance of the furnace body. Furthermore, it is understood that the second crossbeams 440 may be arranged circumferentially along the furnace body 100.

[0051] According to embodiments of the present invention, the furnace walls of the gasification section 110 and the combustion section 120 can both be water-cooled walls, preferably integrally formed membrane water-cooled walls. The suspended water-cooled walls can absorb thermal expansion and ensure good furnace tightness, reducing the furnace leakage coefficient, facilitating strict sealing, and improving gasification and combustion conditions within the furnace. Simultaneously, the use of water-cooled walls also facilitates the application of refractory material layers on the inner surface of the furnace. Furthermore, a steam drum 150 can be connected to the upper part of the water-cooled wall. The inlet of the steam drum 150 is connected to the upper header of the water-cooled wall, and the outlet of the steam drum is connected to the lower header of the water-cooled wall. This allows for steam-water separation of the steam obtained from the water-cooled wall heat exchange via the steam drum, and the separated water can be recycled as cooling water for the water-cooled wall. Additionally, a steam drum support (such as...) can be installed on a support plate 430 between the heat exchange furnace wall 133 and the combustion section 120 furnace wall. Figure 1 (as shown), or a steam drum support (such as) is installed on the first crossbeam 420. Figure 2 As shown in the figure, the steam drum 150 can be effectively fixed by the steam drum bracket.

[0052] According to an embodiment of the present invention, the first air distribution device 114 provided at the bottom of the gasification section 110 may include multiple directional air caps, which achieve the supply and uniform distribution of the gasifying agent. Furthermore, it is understood that after the waste enters the gasification section, primary air can be supplied to the gasification section as a gasifying agent through the first air distribution device, causing the waste to gasify and the material including the waste and the inert bed material to flow in a gas-solid two-phase turbulent fluidization manner. The type of gasifying agent is not particularly limited, and those skilled in the art can flexibly select it according to actual needs; for example, it may include one or more selected from air, oxygen, and water vapor.

[0053] According to an embodiment of the present invention, the gasification section 110 includes an upper variable cross-section zone 111, a constant cross-section zone 112, and a lower variable cross-section zone 113 arranged in an upper, middle, and lower configuration. The cross-sectional area of ​​the upper variable cross-section zone 111 gradually increases from top to bottom, while the cross-sectional area of ​​the lower variable cross-section zone 113 gradually decreases from top to bottom. The variable cross-section design of the gasification section allows for the superposition of multiple beds, forming a turbulent fluidized state dominated by internal circulation, enhancing mass and heat transfer, avoiding material accumulation at the bottom, meeting the requirements for centralized treatment of multiple types of waste in the same furnace, and further facilitating the complete gasification of waste. It is understood that the dual-media TFB gasification incinerator of the present invention is suitable for treating various types of difficult-to-treat organic solid wastes. The types of organic solid wastes applicable are not particularly limited, and those skilled in the art can flexibly select according to actual conditions. For example, it can treat waste plastics, waste tires, waste rubber, biological waste, sludge, papermaking waste, medical waste, etc. It can treat various forms and types of waste, including solid, liquid, and pseudo-fluid states, in the same furnace. Specifically, it can be added in stages at different heights according to the characteristics of the waste (such as moisture, particle size, or phase).

[0054] According to an embodiment of the present invention, reference Figure 4 It is understood that a third air distribution device may also be provided on the side of the gasification section 110. The third air distribution device may include a gasifying agent inlet 117 provided on the side wall of the gasification section. The third air distribution device may include multiple gasifying agent inlets 117 arranged circumferentially along the gasification section 110 or multiple layers of gasifying agent inlets 117 arranged along the height of the gasification section 110. Thus, in addition to supplying the gasifying agent to the gasification section through the bottom air inlet 116, primary air can also be supplied as a gasifying agent through the gasification section air inlet 117, so as to realize multi-stage air distribution in the gasification section and full gasification of waste materials.

[0055] According to an embodiment of the present invention, reference Figure 1 or Figure 4 It is understood that the second air distribution device located on the side of the combustion section 120 may include three layers of air inlets 121 arranged along the height direction of the furnace body 100, namely upper, middle and lower layers. Each layer of combustion section air inlets 121 may include one combustion section air inlet 121 or multiple combustion section air inlets 121 evenly distributed along the circumference of the side wall of the combustion section. Thus, secondary air can be supplied into the combustion section by the combustion section air inlets 121 as combustion aid, realizing multi-stage air distribution and precise temperature control in the combustion section, ensuring that the material has sufficient residence time and expected combustion temperature in the combustion section, thereby achieving complete combustion of waste.

[0056] According to an embodiment of the present invention, reference Figure 5 Understand that the length L1 of the combustion section 120 can be 1 / 4 to 1 / 3 of the total height H of the furnace body 100; the length L2 of the gasification section 110 can be 1 / 6 to 1 / 3 of the total height H of the furnace body 100, for example, 1 / 4, etc. Among these, when treating organic solid waste, in order to effectively suppress NO... x To prevent the initial formation of dioxins and other pollutants, the gasification temperature of organic solid waste in the gasification section is typically required to be maintained between 650 and 850°C. For example, the gasification temperature of ordinary organic solid waste is typically required to be maintained between 650 and 800°C, while the gasification temperature of hazardous organic waste is typically required to be maintained between 650 and 850°C. To ensure the complete decomposition of harmful substances such as dioxins, the residence time of the material in the combustion section is typically required to be no less than 2 seconds. The temperature of ordinary organic solid waste is typically required to be maintained at no less than 850°C, while the temperature of hazardous organic waste is typically required to be maintained at no less than 1100°C. In addition, the temperature of the high-temperature flue gas generated by organic solid waste after passing through the heat exchange section is expected to be controlled between 500 and 600°C to prevent ash with high alkali metal content in the flue gas from caking or adhering to the inner wall of the separator. In this invention, by controlling the segment ratio of the furnace body within the above range, it is more conducive to meeting the overall requirements of each stage of gasification, combustion, and heat exchange, and realizing the full resource utilization and harmless treatment of waste.

[0057] According to an embodiment of the present invention, the connection height between two adjacent heat exchange furnace walls 133 can be 300~500mm, for example, 350mm, 400mm or 450mm, etc., and the connection height between the heat exchange furnace wall 133 and the combustion section furnace wall can be 300~500mm, for example, 350mm, 400mm or 450mm, etc. It is understood that the connection part between two adjacent heat exchange furnace walls 133 and the connection part between the heat exchange furnace wall 133 and the combustion section furnace wall are provided with expansion sealing structures, such as soft connection seals. This not only facilitates the welding and other connection operations between the heat exchange section furnace walls and between the heat exchange section furnace wall and the combustion section furnace wall, but also helps to achieve soft connection seals, thereby helping to solve the thermal expansion sealing problem between the lower furnace body composed of the water-cooled wall evaporation heating surface and the upper furnace body composed of the heat transfer oil coil.

[0058] According to an embodiment of the present invention, the inner surface of the furnace wall of the gasification section 110 may be provided with a refractory material layer; furthermore, the inner surface of the furnace wall of the combustion section 120 may also be partially or completely covered with a refractory material layer, thereby avoiding direct contact and heat exchange between the high temperature environment inside the furnace and the water-cooled wall, reducing the degree of thermal expansion of the furnace body, reducing the heat absorption, which is conducive to maintaining the high temperature environment inside the furnace and reducing the wear of ash on the inner wall of the furnace.

[0059] According to an embodiment of the present invention, each set of heat transfer oil coils 131 can be arranged in a circumferential spiral upward along the heat exchange furnace wall 133. This arrangement can increase the radiative heat exchange area between the high-temperature flue gas and the heat transfer oil coils, enabling the high-temperature flue gas to achieve better heat exchange efficiency and effect during the directional flow of the heat exchange section. Furthermore, to further cope with thermal expansion and ensure the sealing of the furnace chamber, flexible connections can be provided between adjacent heat exchange furnace walls and the supporting plates connecting them, and between the furnace body and the hot flue gas outlet. These connections can be metal or non-metal flexible connections.

[0060] According to an embodiment of the present invention, in combination Figure 1 and Figure 6It is understood that the dual-medium TFB gasification incinerator may also include an air distribution and ash removal system. The air distribution and ash removal system includes the aforementioned first air distribution device 114 and an ash removal device. The first air distribution device 114 includes a main air distribution plate 1141, a primary air chamber 1142, and a secondary air distribution plate 1143. The main air distribution plate 1141 is located at the bottom of the furnace body 100. The primary air chamber 1142 is located at the bottom of the main air distribution plate 1141. The secondary air distribution plate 1143 is located outside the primary air chamber 1141. The secondary air distribution plate 1143 and the main air distribution plate 1141 are arranged in a stepped manner, and the height of the secondary air distribution plate 1143 is lower than that of the main air distribution plate 1141. The slag discharge device includes: a slag discharge chamber 161, a slag discharge channel 162, and a slag discharge valve. The slag discharge chamber 161 is located at the bottom of the secondary air distribution plate 1143, and the pressure of the slag discharge chamber 161 is greater than the pressure of the primary air chamber 1142. The slag discharge channel 162 is connected to the furnace body 100 and is located below the furnace body. The slag discharge channel 162 is located next to the end of the secondary air distribution plate 1143 away from the main air distribution plate 1141, and the slag discharge channel 162 has a slag outlet 115. The slag discharge valve includes a first slag discharge valve 1631 and a second slag discharge valve 1632. The first slag discharge valve 1631 and the second slag discharge valve 1632 are located opposite each other on the inner wall of the slag discharge channel 162. The second slag discharge valve 1632 is located below the first slag discharge valve 1631, and the width of the first slag discharge valve 1631 is smaller than the width of the slag discharge channel 162.

[0061] Currently, turbulent fluidized bed (TFB) is one of the effective means of gasifying waste. However, the waste contains irregular large pieces of material (such as bricks, stones, metal wires, etc.) that cannot be fluidized and need to be discharged through the ash discharge port at the bottom of the TFB. However, irregular large pieces of material (such as bricks, stones, metal wires, etc.) can easily get stuck in the middle area of ​​the gate valve in related technologies, causing blockage of the ash discharge port, or even accumulating on the air distribution plate, leading to deterioration of fluidization and thus affecting the normal operation of the gasification incinerator. By adopting this air distribution and slag removal system, the waste entering the furnace first falls onto the main air distribution plate. Under the action of the gasifying agent in the primary air chamber, the fine materials in the waste are fluidized, while the coarse materials (i.e., irregular large pieces of material) settle down and fall onto the secondary air distribution plate. Under the action of the gasifying agent in the slag removal air chamber, the fine materials mixed in with the coarse materials are fluidized, and the coarse materials enter the slag removal channel. Thus, the coarse and fine materials in the waste entering the furnace are automatically and fully separated. The slag removal channel is equipped with asymmetrical slag removal valves. There is a certain space between the first slag removal valve and the slag removal channel, so that the irregular large pieces of material will not be completely stuck on the first slag removal valve. The opposite second slag removal valve is set below the first slag removal valve, and the irregular large pieces of material will not be completely stuck on the second slag removal valve either. Thus, the first and second slag removal valves are superimposed to form a self-locking structure, locking the irregular materials and preventing the materials discharged from the furnace from leaking down, while also avoiding the problem of irregular large pieces of material getting stuck on the slag removal valves.

[0062] According to an embodiment of the present invention, reference Figure 6 The air distribution and slag removal system also includes a fluidizing gas flow channel 164. The fluidizing gas flow channel 164 is located above the slag removal air chamber 161 and is connected to the slag removal channel 162 and the furnace body 100. The fluidizing gas flow channel 164 is connected to the furnace body 100 through a fluidizing gas circulation inlet 165 and a large waste outlet 166 arranged vertically. The fluidizing gas circulation inlet 165 is located in the lower part of the furnace body 100, not higher than the top of the fluidizing gas flow channel 164. The fluidizing gas formed on the secondary air distribution plate 1143 enters the furnace above the main air distribution plate 1141 through the fluidizing gas flow channel 164 and the fluidizing gas circulation inlet 165. The large waste outlet 166 is located in the lower part of the furnace body, not lower than the main air distribution plate 1141. Irregular large pieces of material screened out by the main air distribution plate 1141 and the primary air chamber 1142 fall onto the secondary air distribution plate 1143 through the large waste outlet 166.

[0063] Furthermore, combined Figure 6 and Figure 7 Understanding the following: Let the aperture of the large waste outlet 166 be *a*, the aperture of the fluidizing gas circulation inlet 165 be *c*, the width of the fluidizing gas flow channel 164 be *d*, the aperture of the slag discharge channel 162 inlet be *b*, and the width of the slag discharge channel 162 be *w0*, where *b* = (1~1.5)a, *c* = (0.5~0.8)a, *d* = (1.5~2.0)b, and *w0* = (2.0~3.0)b. The above-described air distribution and slag discharge system, with its given structural dimensions, can achieve stable operation. The principles or effects of determining the dimensions of each part are as follows: The determination of dimension *a* depends on the material discharge flow rate and coarse / fine screening determined during the design phase, ensuring that both coarse and fine slag can be discharged from the furnace on schedule. The width 'd' needs to ensure that the discharged slag can achieve separation of coarse and fine slag on the secondary air distribution plate, and that fine slag can be carried back to the furnace at a reasonable gas velocity. If 'd' is too large, the gas velocity will be too low, and the particle size carried by the gas will be too small, resulting in too much fine slag being discharged from the furnace, disrupting the material screening balance in the furnace. If 'd' is too small, the gas velocity will be too high, the resistance will be too great, and the amount of fine slag returning to the furnace will also be reduced, thus disrupting the material screening balance. The width 'c' is limited to ensure that the gas-solid two-phase flow entering the furnace has a certain pressure drop, thereby preventing backflow. The size 'b' is determined based on the pressure balance on the secondary air distribution plate, mainly to form a coarse-fine separation mechanism. Coarse slag gradually falls into the slag discharge valve through 'b', while fine slag is blocked by the coarse slag at its corresponding slot and rises back into the fluidized gas flow channel in the furnace.

[0064] It is understandable that the shapes of the large-piece waste outlet 166, the fluidizing gas circulation inlet 165, and the inlet of the slag discharge channel 162 are not particularly limited, and those skilled in the art can select according to actual needs. For example, they can be circular or rectangular, etc. It should be noted that the aperture a of the large-piece waste outlet 166, the aperture c of the fluidizing gas circulation inlet 165, and the aperture b of the inlet of the slag discharge channel 162 can be independently understood as the minimum hole spacing. For example, taking the aperture a of the large-piece waste outlet 166 as an example, when the large-piece waste outlet 166 is circular, a can be understood as the inner diameter of the large-piece waste outlet 166; when the large-piece waste outlet 166 is rectangular, a can be understood as the short side dimension of the large-piece waste outlet 166.

[0065] According to an embodiment of the present invention, referring to Figure 7 Understand that taking the width of the slag discharge channel 162 as w0, the width of the first slag discharge valve 1631 as w1, and the width of the second slag discharge valve 1632 as w2, 0.5w0 ≤ w1 ≤ 0.75w0, 0.75w0 ≤ w2 < w0. Thus, appropriate spaces are left between the first slag discharge valve 1631 and the second slag discharge valve 1632 and the inner wall of the slag discharge channel 162. Irregular large pieces of materials will not be completely stuck on the first slag discharge valve 1631. With the second slag discharge valve 1632 arranged opposite below the first slag discharge valve 1631, irregular large pieces of materials will not be completely stuck on the second slag discharge valve 1632 either. Thus, the first slag discharge valve 1631 and the second slag discharge valve 1632 are superimposed to form a self-locking structure, locking irregular large pieces of materials, and the large pieces of materials will not leak downward. At the same time, the problem of irregular large pieces of materials being stuck and jammed on the slag discharge valve is avoided.

[0066] According to an embodiment of the present invention, the pressure in the primary air chamber 1142 can be 10 - 15 kPa. Thus, it can be further ensured that under the action of the primary air chamber 1142, the fine materials in the waste falling on the main air distribution plate 1141 are fluidized, and the large pieces of materials fall on the secondary air distribution plate 1143, thereby achieving the preliminary separation of fine materials and large pieces of materials.

[0067] According to an embodiment of the present invention, the pressure in the slag discharge air chamber 161 is 12 - 20 kPa. Thus, it can be further ensured that the fine materials mixed in the coarse materials are fluidized, and the coarse materials enter the slag discharge channel 162, thereby achieving the secondary separation of fine materials and large pieces of materials. At the same time, the high pressure in the slag discharge air chamber 161 provides the power required for the internal circulation of materials.

[0068] According to an embodiment of the present invention, the slag discharge valve may further include a first rack 1633, a first reducer 1634, and a first motor 1635 connected in sequence outside the slag discharge channel 162. The first rack 1633 is connected to the first slag discharge valve 1631. Under the action of the first reducer 1634, the first motor 1635 drives the first rack 1633 to move, and the first rack 1633 drives the first slag discharge valve 1631 to move, thereby realizing the opening and closing of the first slag discharge valve 1631. Similarly, the slag discharge valve may further include a second rack 1636, a second reducer 1637, and a second motor 1638 connected in sequence outside the slag discharge channel 162. The second rack 1636 is connected to the second slag discharge valve 1632. Under the action of the second reducer 1637, the second motor 1638 drives the second rack 1636 to move, and the second rack 1636 drives the second slag discharge valve 1632 to move, thereby realizing the opening and closing of the second slag discharge valve 1632.

[0069] According to an embodiment of the present invention, reference Figure 7 Understanding that when the slag discharge valve is closed, the angle α between the line connecting the end of the first slag discharge valve 1631 away from the inner wall of the slag discharge channel 162 and the end of the second slag discharge valve 1632 away from the inner wall of the slag discharge channel 162 and the horizontal plane is 5~15°. This makes the angle α smaller than the angle of repose of large pieces of material, further ensuring that the first slag discharge valve 1631 and the second slag discharge valve 1632 lock large pieces of material in the closed state, while also avoiding the problem of irregular large pieces of material getting stuck on the slag discharge valve.

[0070] According to an embodiment of the present invention, reference Figure 7 It is understood that the distance ΔH between the first slag discharge valve 1631 and the second slag discharge valve 1632 is (1 / 4~1 / 3)w0, which further ensures that the first slag discharge valve 1631 and the second slag discharge valve 1632 lock large pieces of material in the closed state, while avoiding the problem of irregular large pieces of material getting stuck on the slag discharge valve.

[0071] According to an embodiment of the present invention, reference Figure 6 It is understood that the angle between the main air distribution plate 1141 and the horizontal plane is 5~20°, and the angle between the secondary air distribution plate 1143 and the horizontal plane is 3~10°. This ensures that the fine materials in the waste are fully fluidized on the main air distribution plate and the secondary air distribution plate, and also ensures that the large pieces of material fall from the main air distribution plate to the secondary air distribution plate and from the secondary air distribution plate to the slag discharge channel.

[0072] According to an embodiment of the present invention, the valve plate thickness of the first slag discharge valve 1631 and the second slag discharge valve 1632 can each be independently 20~35mm. This can further ensure that, under the superimposed action of the first slag discharge valve 1631 and the second slag discharge valve 1632, irregular large pieces of material are locked in, so that large pieces of material will not leak down.

[0073] Gas-solid separator 200

[0074] According to an embodiment of the present invention, the fluidized material is gasified under the action of the gasifying agent. The gasified gas enters the combustion section and combustion occurs in the combustion section. The flue gas after combustion then enters the heat exchange section. After heat exchange is completed in the heat exchange section, it enters the gas-solid separator for gas-solid separation. Most of the ash is separated and discharged through the ash outlet (i.e., the second ash outlet 210) located at the bottom of the gas-solid separator 200.

[0075] According to an embodiment of the present invention, reference Figure 8 It is understood that the dual-medium TFB gasification incinerator may also include an ash discharge device 500, which is connected to the second ash outlet 210. The ash discharge device 500 may include: an ash hopper 510, a spiral scraper 520, a gear 550, a coupling 540, and a motor 530. The ash hopper 510 is cylindrical; the spiral scraper 520 is disposed inside the ash hopper 510; one end of the gear 550 is connected to the spiral scraper 520, and one end of the gear 550 is sealed to the ash hopper 510; the coupling 540 is connected to the other end of the gear 550; and the motor 530 is connected to the coupling 540. Municipal solid waste, industrial combustible waste, hazardous waste, and biomass generate large amounts of medium- and high-temperature gases during combustion or gasification. These gases contain medium- and high-temperature ash, which is typically a porous and loose state with low true density. This ash has strong adhesive properties and easily clumps together in various ash hoppers (such as the ash hopper under the separator in a fluidized bed, the ash hopper connecting the second and third channels of a grate, and the ash hopper under the tail shaft of various furnace types), leading to ash hopper blockage. To avoid this problem, this invention incorporates an ash discharge device. A motor drives a gear via a coupling, which in turn drives a spiral scraper to rotate left and right inside the ash hopper. This scrapes away the ash layer adhering to the inner wall of the ash hopper, ensuring smooth flow of medium- and high-temperature ash and preventing the ash from clumping together on the inner wall. Therefore, a highly reliable ash conveying effect can be achieved with lower energy consumption and less wear, ensuring that the medium- and high-temperature ash stream discharged from the gas-solid separator can be smoothly discharged through the ash hopper. In addition, the ash discharge device has a simple structure and is easy to achieve without deformation at medium and high temperatures, while conventional devices in the prior art have more complex structures and it is difficult to achieve the goal of not being deformed at medium and high temperatures.

[0076] According to embodiments of the present invention, the specific structure of the ash hopper 510 is not particularly limited, and those skilled in the art can choose according to actual needs. For example, according to a specific example of the present invention, refer to the appendix... Figure 8 The ash hopper 510 may include an integrally formed conical ash hopper and a straight ash hopper, with the conical ash hopper positioned above the straight ash hopper. Preferably, the gear 550 may be installed in the middle of the straight ash hopper.

[0077] According to an embodiment of the present invention, the spiral scraper 520 may include multiple sub-spiral scrapers, which can be connected by rivets to form a complete spiral scraper. Thus, a certain gap exists between adjacent sub-spiral scrapers. When the spiral scraper expands due to heat, the gap accommodates the expansion, thereby ensuring that the spiral scraper as a whole does not deform under heat. Further, according to a specific example of the present invention, the sub-spiral scrapers of the conical ash hopper can be spiral-shaped, rolled from heat-resistant steel sheets, shaped through heat treatment, and directly placed inside the ash hopper.

[0078] According to embodiments of the present invention, the material of the spiral scraper 520 is not particularly limited, as long as it can achieve the purpose of not being easily deformed at high temperatures. Those skilled in the art can choose arbitrarily according to actual needs. For example, the material of the spiral scraper 520 can be 2520 heat-resistant steel or heat-resistant steel with high nickel-chromium content such as 310, 314, and 316.

[0079] According to an embodiment of the present invention, the pitch of the spiral scraper 520 is ΔL = (1 / 2~3 / 2)D, where D is the average value of the outer diameter of the ash hopper within the pitch range. The pitch is defined as the distance between two adjacent threads measured along the helical direction, i.e., the axial distance between two corresponding points on the pitch diameter line of two adjacent threads. Therefore, by limiting the pitch of the spiral scraper 520 within the above range, the spiral scraper 520 can effectively scrape the inner wall of the ash hopper when it rotates at a certain angle. The inventors have found that if the pitch is too large, the spiral scraper 520 may not be able to effectively scrape the inner wall of the ash hopper; if the pitch is too small, it will cause energy waste and unnecessary wear on the inner wall of the ash hopper and the spiral scraper 520.

[0080] According to an embodiment of the present invention, the rotation angle of the spiral scraper 520 in the circumferential direction of the ash hopper 510 can be 60~90°. Therefore, limiting the rotation angle of the spiral scraper 520 in the circumferential direction of the ash hopper 510 within the above range achieves the purpose of sufficiently scraping the ash layer adhered to the inner wall of the ash hopper. The inventors have found that if the rotation angle is too small, the spiral scraper 520 may not be able to sufficiently scrape the inner wall of the ash hopper; if the rotation angle is too large, it will cause energy waste and unnecessary wear on the inner wall of the ash hopper and the spiral scraper 520. It is understood that the rotation of the spiral scraper 520 in the circumferential direction of the ash hopper 510 is a reciprocating rotation; that is, after the spiral scraper 520 rotates 60~90° in the circumferential direction of the ash hopper 510, the spiral scraper 520 stops rotating in the original direction and then rotates in the opposite direction. The rotation angle of the spiral scraper 520 in the circumferential direction of the ash hopper 510 can be controlled by a stepper motor 530 through pulse signals. However, the stepper motor 530 is expensive. Alternatively, it can be achieved by using a general motor 530 in conjunction with a limiting protrusion.

[0081] According to an embodiment of the present invention, the width of the spiral scraper 520 can be 1 / 4 to 1 / 3 of the circumference of the inner wall of the ash hopper where the spiral scraper 520 is located, and the corresponding circumferential angle can be 90 to 120°, which is greater than the rotation angle of 60 to 90°. This ensures that the ash layer adhered to the inner wall of the ash hopper is fully scraped. It should be noted that the spiral scraper 520 is curved in the width direction, and is in the shape of a strip-shaped cylinder, attached to the inner wall surface of the ash hopper 510.

[0082] According to an embodiment of the present invention, the reference Figure 8 As shown, the ash discharge device 500 may further include multiple limiting protrusions 570, which can be provided on the inner wall of the ash hopper. The function of the limiting protrusions 570 is to restrict the range of left and right rotation of the spiral ash scraper 520 within the ash hopper 510. When the spiral ash scraper 520 encounters the limiting protrusion 570 during rotation, the spiral ash scraper 520 stops rotating in the original direction and then rotates in the opposite direction. Thus, the rotation angle of the spiral ash scraper 520 in the circumferential direction of the ash hopper is limited to a range of 60~90°. Furthermore, the multiple limiting protrusions 570 can also break the flatness of the inner wall of the ash hopper, which to a certain extent prevents medium and high temperature ash from adhering to the inner wall of the ash hopper and causing caking.

[0083] According to an embodiment of the present invention, the reference Figure 8 As shown, the ash discharge device 500 may further include a temperature sensing element 560, which can be installed on the wall of the ash hopper 510 and extend into the ash hopper 510 to monitor the temperature fluctuation signal of the flowing ash in the ash hopper 510. It is understood that when the high-temperature ash flows normally in the ash hopper 510, there will be some temperature fluctuation. If the detected temperature stabilizes and does not fluctuate, it indicates that the ash in the ash hopper 510 is no longer flowing, that is, the ash hopper 510 is blocked by clumps of ash. At this time, it is necessary to start the motor 530 to drive the spiral scraper 520 to rotate and scrape the ash. Preferably, when the temperature sensing element 560 detects that the temperature fluctuation of the ash in the ash hopper is lower than 5℃ / 10min, the motor 530 can be started to drive the spiral scraper 520 to rotate and scrape the ash.

[0084] According to an embodiment of the present invention, the ash removal device 500 may further include a PLC control unit (not shown in the figure). The PLC control unit can be connected to the temperature sensing element 560 and the motor via electrical signals. The temperature sensing element 560 can transmit the detected temperature signal of the ash in the ash hopper to the PLC control unit. The PLC control unit analyzes the received temperature signal of the ash in the ash hopper and decides whether to start the motor to drive the spiral ash scraper to rotate based on the experimentally determined fluctuation amplitude and frequency. Thus, automated ash removal is achieved.

[0085] According to an embodiment of the present invention, the method for ash removal using the above-mentioned ash removal device may include: monitoring the temperature fluctuation of ash in the ash hopper using a temperature sensing element; starting the motor when the temperature fluctuation of ash in the ash hopper is below 5°C / 10min; the motor drives the gear through a coupling, and the gear drives the spiral ash scraper to rotate, thereby scraping away the ash layer adhering to the inner wall of the ash hopper; and stopping the motor after the ash layer on the inner wall of the ash hopper is cleaned. This ash removal method uses a temperature sensing element to monitor the temperature fluctuation of ash in the ash hopper. When the temperature fluctuation of ash in the ash hopper is below 5°C / 10min, the motor is started. The motor drives the gear through a coupling, and the gear drives the spiral ash scraper to rotate alternately clockwise and counterclockwise inside the ash hopper, thereby scraping away the ash layer adhering to the inner wall of the ash hopper. The motor stops after the ash layer on the inner wall of the ash hopper is cleaned. This ensures that the ash flow passes smoothly through the ash hopper, avoiding the problem of ash adhering to the inner wall of the ash hopper and forming clumps. It can achieve a highly reliable ash conveying effect with lower energy consumption and less wear, ensuring that the medium and high temperature ash flow passes smoothly through the ash hopper.

[0086] Waste heat recovery device 300

[0087] According to an embodiment of the present invention, reference Figures 1-4 It is understood that the waste heat recovery device 300 may be provided with at least one set of heat-conducting oil pipe rows 310 along its height direction; furthermore, each set of heat-conducting oil pipe rows 310 may be provided with multiple layers of staggered parallel heat-conducting oil heat exchange tubes 311 along the height direction of the waste heat recovery device 300. This arrangement can not only greatly increase the heat exchange area between the high-temperature flue gas and the heat-conducting oil pipe rows, thereby improving the heat exchange efficiency and effect, but also facilitate the settling of ash carried in the high-temperature flue gas during contact with the heat-conducting oil pipe rows, thus improving the flue gas purification effect. It is understood that in each set of heat-conducting oil pipe rows 310, the multiple layers of heat-conducting oil heat exchange tubes can be arranged independently in parallel or in series. In addition, the number of layers of heat-conducting oil heat exchange tubes 311 in each set of heat-conducting oil pipe rows 310 is not particularly limited, and those skilled in the art can flexibly choose according to actual needs.

[0088] According to an embodiment of the present invention, reference Figures 1-4 It is understood that in the waste heat recovery device 300, the economizer 320 can be set with one or more sets according to actual needs, and the upper part of the economizer 320 can also be connected to a steam drum (not shown).

[0089] According to an embodiment of the present invention, reference Figure 4It is understood that the air preheater 330 may further be provided with a partition 333, which divides the air preheater 330 into a first air preheater 331 arranged vertically or horizontally side by side and a second air preheater 332. The first air preheater 331 includes a first cold air inlet and a first hot air outlet, and the second air preheater 332 includes a second cold air inlet and a second hot air outlet. One of the first hot air outlet and the second hot air outlet is connected to the air inlet 121 of the combustion section 120, and the other is connected to the air inlet 116 and / or air inlet 117 of the vaporization section 110. It is understood that the first air preheater 331 and the second air preheater 332 are two relatively independent air preheating units. In actual operation, the pressure and temperature required for the gasifying agent supplied to the gasification section and the combustion air supplied to the combustion section are not exactly the same. For example, the temperature of the gasifying agent supplied to the gasification section can be 150~200℃ and the pressure can be 10~15kPa, while the temperature of the combustion air supplied to the combustion section can be 100~200℃ and the pressure can be 4~6kPa. When the partition is set horizontally, the air preheater 330 can be divided into two parts arranged vertically (the hot air temperature output by the upper air preheater is higher than that of the lower air preheater). When the partition is set vertically, the air preheater 330 can be divided into two parts arranged horizontally side by side (such as left and right). Based on the temperature and pressure requirements of the gasifying agent and the combustion air, one of the first air preheater and the second air preheater can be connected to the air inlet (116, and / or 117) of the gasification section and the other can be connected to the air inlet 121 of the combustion section, and the pressure of the two preheaters can be controlled respectively.

[0090] According to an embodiment of the present invention, reference Figure 4 It is understood that the waste heat recovery device 300 has a flue gas outlet 350 at the bottom and a first ash outlet 340 at the bottom. The flue gas outlet 350 is located below the air preheater 330 and is connected to the flue gas purification device.

[0091] According to an embodiment of the present invention, the heat transfer oil pipe array 310 may include at least one layer of heat transfer oil heat exchange pipes 311, and each layer of heat transfer oil heat exchange pipes 311 may include multiple spaced heat transfer oil heat exchange pipes 311, as shown in the reference. Figure 9 Understood, at least one heat exchanger tube has an anti-wear plate 600 on its windward side; and / or, the economizer 320 includes at least one layer of hot water heat exchanger tubes, each layer of hot water heat exchanger tubes including multiple spaced hot water heat exchanger tubes 321, and at least one hot water heat exchanger tube 321 has an anti-wear plate 600 on its windward side (reference). Figure 9 (Understanding). The wear-resistant plate 600 is detachably installed along the length of the heat exchange tube (refer to...). Figure 12 or Figure 13(Understanding), the cross-section of the abrasion plate 600 (which is perpendicular to the length of the abrasion plate) is triangular (e.g., Figure 10 (as shown) or triangular-like shapes with a hyperbolic structure (such as...) Figure 11 As shown), the vertices of the triangle (such as...) Figure 10 The intersection of plane e1 and plane f1) or the intersection of hyperbolas (such as...) Figure 11 The intersection of surface e2 and surface f2 is located on the side of the wear-resistant plate 600 away from the heat exchange tube. When using the dual-medium TFB gasification incinerator of this invention to treat biomass, garbage, sludge and various hazardous wastes, the generated flue gas usually has the characteristics of high moisture content, high alkali metal content, easy slagging and ash accumulation. When recovering the waste heat of the above flue gas, the convective heating surface of the convection heat exchange device (such as heat transfer oil pipe row, economizer) is mostly arranged in a pipe row. However, due to the characteristics of the above flue gas of high moisture content, high alkali metal content, easy slagging and ash accumulation, ash and slag are easily accumulated in the relatively flat area on the windward side of the heat exchange tube, which leads to failure and shutdown, affecting the normal and efficient operation of the high-efficiency incinerator. For the convection heat exchange device, the inventors found that the greater the curvature of the heat exchange tube, the less likely it is to accumulate ash, that is, the side of the convection heat exchange tube is not easy to accumulate ash, and the most likely place to accumulate ash is in the relatively flat area on the windward side of the heat exchange tube (such as the side of the convection heat exchange tube). Figure 15 In the area shown in g), by installing a wear-resistant plate on the windward side of the heat exchange tube, the inclined surface of the wear-resistant plate (such as...) can be utilized. Figure 10 (as shown on surfaces e1 and f1) or curved surfaces (such as...) Figure 11 (As shown in surfaces e2 and f2) This alters the movement path of ash in the flue gas, causing the ash to fall along the inclined or curved surface of the wear-resistant plate. This prevents direct contact between the ash in the flue gas and the windward surface of the heat exchange tubes, thus avoiding ash slagging on the windward surface of the heat exchange tubes. Furthermore, it reduces wear on the heat exchange tubes caused by ash. Additionally, the wear-resistant plate can be replaced when there is significant slagging, ash accumulation, or malfunction. Therefore, by installing a removable wear-resistant plate on the windward surface of the heat exchange tubes, and controlling the cross-section of the wear-resistant plate to be triangular or a hyperbolic triangular structure, the anti-slagging performance of the windward surface of the heat exchange tubes can be effectively improved, greatly reducing the probability of shutdown due to ash accumulation and significantly increasing the continuous operating time of incinerators, etc.

[0092] According to an embodiment of the present invention, reference Figure 9 or Figure 14As shown, the wear-resistant plate 600 can be suspended on the heat exchanger 311 for heat transfer oil or the heat exchanger tube 321 for heat transfer water. When the bottom of the wear-resistant plate 600 is directly in contact with the heat exchanger tube and fixed, although the problem of ash slagging and ash accumulation on the windward side of the heat exchanger tube can be solved, it will affect the effective contact area between the heat exchanger tube and the high-temperature flue gas, thus affecting the heat exchange efficiency and effect. By suspending the wear-resistant plate 600 on the heat exchanger tube, on the one hand, the windward side of the heat exchanger tube can have anti-slagging and anti-ash accumulation performance while ensuring heat exchange efficiency and effect. On the other hand, under the premise that the inclined or curved surface of the wear-resistant plate is fixed, by controlling the wear-resistant plate to have a certain suspension height, the probability of contact between ash in the high-temperature flue gas and the heat exchanger tube can be further reduced, thereby reducing the wear on the heat exchanger tube.

[0093] According to an embodiment of the present invention, reference Figures 10-11 or Figure 14 It is understood that the cross-section of the wear-resistant plate 600 (perpendicular to its length) can be a triangular or triangular-like shape, all of which are axisymmetric. The axis of symmetry of the triangle or triangular-like shape coincides with the perpendicular line from the vertex of the triangle or the intersection of the hyperbola to the central axis of the heat exchange tube. This not only solves the problem of ash slagging and accumulation on the windward side of the heat exchange tube, but also ensures that the heat exchange tube sections located on both sides of the wear-resistant plate achieve the same resistance to ash slagging and accumulation, as well as the same wear-resistant effect. Furthermore, it helps improve the uniformity of stress distribution on the wear-resistant plate during use.

[0094] According to an embodiment of the present invention, reference Figure 15 It is understood that the width W of the wear-resistant plate 600 near the heat exchange tube can be 0.2 to 0.5 times the outer diameter of the heat exchange tube, for example, it can be 0.25, 0.3, 0.35, 0.4, or 0.45 times the outer diameter of the heat exchange tube. If the width of the wear-resistant plate 600 near the heat exchange tube is too small, it is difficult to completely solve the problem of ash slagging and ash accumulation in the relatively flat area on the windward side of the heat exchange tube. If the width is too large, it will not only increase the raw material cost and the difficulty of fixing the wear-resistant plate, but may also affect the effective convective contact area between the heat exchange tube and the high-temperature flue gas, thus affecting the heat exchange effect. In this invention, by controlling the width of the wear-resistant plate near the heat exchange tube to the above-mentioned range, it is more conducive to ensuring the heat exchange effect while avoiding ash slagging and ash accumulation on the windward side of the heat exchange tube, and reducing the raw material cost and fixing difficulty of the wear-resistant plate.

[0095] According to an embodiment of the present invention, reference Figure 15 Understanding that when the width W of the wear-resistant plate 600 near the heat exchange tube is 0.2 to 0.5 times the outer diameter of the heat exchange tube, the height h of the wear-resistant plate 600 can be 0.05 to 0.1 times the outer diameter of the heat exchange tube. For example, the height h of the wear-resistant plate 600 can be 0.06, 0.07, 0.08, or 0.09 times the outer diameter of the heat exchange tube, etc. By controlling the height of the wear-resistant plate within the above range, the inclination surface of the wear-resistant plate can be controlled (e.g., Figure 10 (e1 and f1 surfaces in the model) or curved surfaces (such as...) Figure 11 The direction of the e2 and f2 surfaces in the design makes it easier for ash to slide away from the relatively flat area on the windward side of the heat exchange tube (refer to...). Figure 14 (Understanding the extension lines of surfaces e1 and f1), this not only better addresses the issue of ash accumulating and depositing in the relatively flat area on the windward side of the heat exchange tubes, but also helps reduce wear on the heat exchange tubes caused by ash flowing with the flue gas. Furthermore, based on the aforementioned dimensional conditions of the wear-resistant plate, and referring to... Figure 15 It is understood that the distance L3 between the side of the wear-resistant plate 600 closest to the heat exchange tube and the heat exchange tube can be 0.3 to 0.6 times the outer diameter of the heat exchange tube, for example, it can be 0.35, 0.4, 0.45, 0.5 or 0.55 times the outer diameter of the heat exchange tube. In particular, by controlling the distance between the side of the wear-resistant plate closest to the heat exchange tube and the heat exchange tube to be within the above range, it is more conducive to reducing the probability of ash in the flue gas coming into contact with the heat exchange tube, and ensuring that ash will not slag and accumulate on the windward side of the heat tube.

[0096] According to an embodiment of the present invention, reference Figure 14 It is understood that the extension lines of the inclined surfaces e1 and f1 of the wear-resistant plate can be located between two adjacent heat exchange tubes, or the extension lines of the asymptotes of the curved surfaces e2 and f2 of the wear-resistant plate can be located between two adjacent heat exchange tubes. This can further ensure that the installation of the wear-resistant plate can reduce the probability of ash in the flue gas coming into contact with the heat exchange tubes, and ensure that ash will not slag and accumulate on the windward side of the heat pipe.

[0097] According to an embodiment of the present invention, reference Figure 12 It is understood that the distance between the wear-resistant plate 600 and the heat exchange tube is adjustable. For the same wear-resistant plate, when the outer diameter of the heat exchange tube, the spacing between two adjacent heat exchange tubes, etc., change, the optimal distance between the wear-resistant plate and the heat exchange tube will also change. By controlling the adjustable distance between the wear-resistant plate and the heat exchange tube, it is more convenient to adjust the distance between the wear-resistant plate and the heat exchange tube according to the actual situation, thereby achieving better anti-slagging and anti-ash effects.

[0098] According to embodiments of the present invention, it is understood that the connection method between the wear-resistant plate 600 and the heat exchange tube is not particularly limited, and those skilled in the art can choose according to actual needs, as long as the two can be detachably connected, preferably with adjustable spacing between them. For example, refer to Figure 12It is understood that a bracket 610 can be provided at the top of the heat exchange tube, and at least one first connecting hole 611 can be provided on the bracket 610. A connecting rod 620 can be provided at the bottom of the anti-wear plate 600, and at least one second connecting hole 621 can be provided on the connecting rod 620 to match and connect with the first connecting hole 611. The heat exchange tube and the anti-wear plate 600 can be fixed by the bracket 610 and the connecting rod 620, for example, by bolt fixing, snap fixing or pin fixing, etc. This can not only realize the detachable connection between the anti-wear plate and the heat exchange tube, but also help to control the distance between the two.

[0099] According to an embodiment of the present invention, reference Figure 16 It is understood that the heat transfer oil pipe row 310 may include multiple rows of parallel heat transfer oil heat exchange pipes 311 arranged in sequence. In the entire row of heat transfer oil heat exchange pipes 311 closest to the flue gas inlet of the waste heat recovery device 300, each heat transfer oil heat exchange pipe 311 is provided with a wear-resistant plate 600 on its windward surface. Alternatively, the heat transfer oil pipe row 310 may include multiple rows of staggered parallel heat transfer oil heat exchange pipes 311. In at least two rows of staggered heat transfer oil heat exchange pipes 311 closest to the flue gas inlet of the waste heat recovery device 300, each heat transfer oil heat exchange pipe 311 is provided with a wear-resistant plate 600 on its windward surface. This can further prevent the problem of ash in the flue gas slagging and accumulating on the windward surface of the heat transfer oil heat exchange pipes.

[0100] According to an embodiment of the present invention, reference Figure 17 It is understood that the economizer 320 may include multiple rows of parallel hot water heat exchange tubes 321. In the row of hot water heat exchange tubes closest to the flue gas inlet of the waste heat recovery device 300, each hot water heat exchange tube 321 is provided with an anti-wear plate 600 on its windward surface. Alternatively, the economizer 320 may include multiple rows of staggered parallel hot water heat exchange tubes 321. In at least two rows of staggered hot water heat exchange tubes 321 closest to the flue gas inlet of the waste heat recovery device 300, each hot water heat exchange tube 321 is provided with an anti-wear plate 600 on its windward surface. This can further prevent the problem of ash in the flue gas accumulating and forming slag on the windward surface of the hot water heat exchange tubes.

[0101] In summary, the dual-medium TFB gasification incinerator of the above embodiments of the present invention can have the following beneficial effects:

[0102] (1) By using heat transfer oil and water as the main cooling medium, water-cooled walls, heat transfer oil coils, heat transfer oil convection tube banks, economizer tube banks with water as the medium inside the tubes, and air preheaters are set up in stages to achieve full heat absorption and obtain the maximum thermal efficiency. On the one hand, it can achieve a heat exchange efficiency much higher than that of using heat transfer oil or water alone, and obtain process heat in the form of two media, hot oil and steam, which is convenient for the use of process heat in chemical, food, organic fertilizer and other production operations; on the other hand, it can also preheat the gasifying agent in the gasification section and / or the combustion air in the combustion section. This method improves gasification and combustion efficiency while reducing production costs. Furthermore, by using a furnace support frame to suspend the furnace body, the main furnace chamber is structured as a bottom-suspended, top-supported structure. The joint between the furnace support frame and the furnace body can also be used as a fixed end, allowing the furnace body to expand downwards (due to gravity). During the expansion process, the furnace body's seal will not be affected. This effectively addresses the thermal expansion and sealing problem between the lower furnace body, which consists of water-cooled wall evaporation heating surfaces, and the upper furnace body, which consists of heat transfer oil coils. This avoids poor sealing due to thermal expansion, as well as subsequent issues related to poor furnace body structural stability and safety.

[0103] (2) By adopting the above-mentioned air distribution and slag discharge system, the waste entering the furnace can first fall onto the main air distribution plate. Under the action of the gasifying agent in the primary air chamber, the fine materials in the waste are fluidized, while the coarse materials (i.e., irregular large pieces of material) are deposited and fall onto the secondary air distribution plate. Under the action of the gasifying agent in the slag discharge air chamber, the fine materials mixed in the coarse materials are fluidized, and the coarse materials enter the slag discharge channel. Thus, the coarse and fine materials in the waste entering the furnace are automatically separated. The slag discharge channel is equipped with an asymmetrical slag discharge valve. There is a certain space between the first slag discharge valve and the slag discharge channel. Thus, the irregular large pieces of material will not be completely stuck on the first slag discharge valve. The corresponding second slag discharge valve is set below the first slag discharge valve. Similarly, the irregular large pieces of material will not be completely stuck on the second slag discharge valve. Thus, the first slag discharge valve and the second slag discharge valve are superimposed to form a self-locking structure, which locks the irregular materials and prevents the materials discharged from the furnace from leaking down. At the same time, it avoids the problem of irregular large pieces of material getting stuck on the slag discharge valve.

[0104] (3) By setting up the above-mentioned ash discharge device, the motor drives the gear through the coupling, and the gear drives the spiral ash scraper to rotate left and right in the ash hopper, thereby scraping the ash layer adhering to the inner wall of the ash hopper. This ensures that the medium- and high-temperature ash flow separated by the gasification separator can pass smoothly through the ash hopper, avoiding the problem of medium- and high-temperature ash adhering to the inner wall of the ash hopper and forming clumps. As a result, not only can a highly reliable ash conveying effect be obtained with lower energy consumption and less wear, ensuring that the medium- and high-temperature ash flow passes smoothly through the ash hopper, but the ash discharge device also has a simple structure and is easy to achieve without deformation at medium and high temperatures. Compared with the conventional devices in related technologies, which have more complex structures and are difficult to achieve without deformation at medium and high temperatures, this represents a significant improvement.

[0105] (4) By installing the aforementioned anti-wear plate on the windward side of the heat exchange tube, on the one hand, the inclined or curved surface of the anti-wear plate can be used to change the movement path of ash in the flue gas, causing the ash to fall along the inclined or curved surface of the anti-wear plate, thus avoiding direct contact between the ash in the flue gas and the windward side of the heat exchange tube, thereby preventing ash from slagging on the windward side of the heat exchange tube. On the other hand, it can also reduce the wear caused by ash on the heat exchange tube. In addition, when the anti-wear plate has obvious slagging, ash accumulation, or malfunction, it can be replaced. Thus, the anti-slagging performance of the windward side of the heat exchange tube can be effectively improved, the probability of shutdown due to ash accumulation and slagging can be greatly reduced, and the continuous operation time of the incinerator can be significantly increased.

[0106] (5) The incinerator can be used to process a variety of difficult wastes, and can process solid, liquid and semi-fluid wastes of various forms and types in the same furnace. The equipment is stable and durable, and can effectively deal with thermal expansion sealing problems and improve the heat exchange efficiency and effect of high temperature flue gas, so as to realize the recovery and reuse of process heat. Among them, depending on the energy grade, the process heat carried by hot oil and steam after heat exchange can be used for chemical, food, organic fertilizer and other operations.

[0107] According to another aspect of the present invention, a method for waste gasification and incineration using the aforementioned dual-medium TFB gasification incinerator is provided. According to an embodiment of the present invention, the method includes:

[0108] (1) The waste material is fed to the gasification section at the bottom of the furnace for turbulent gasification to obtain gasified gas and solid residue. The solid residue is intermittently discharged from the furnace. According to an embodiment of the present invention, the temperature of the gasification section is 650~850℃, the temperature of the gasifying agent supplied to the gasification section is 150~200℃, and the pressure is 10~15kPa. It should be noted that the selection of process parameters for the gasification section and the gasifying agent, as well as the selection of waste material and other related characteristics have been described in detail in the foregoing section and will not be repeated here.

[0109] (2) The gasified gas is introduced into the combustion section in the middle of the furnace body for combustion to obtain high-temperature flue gas after combustion. According to an embodiment of the present invention, the temperature of the combustion section is 850~1100℃; the temperature of the combustion air supplied to the combustion section is 100~200℃, and the pressure is 4~6kPa. It should be noted that the relevant characteristics such as the selection of process parameters of the combustion section and the combustion air have been described in detail in the foregoing section, and will not be repeated here.

[0110] (3) The high-temperature flue gas after combustion is cooled by heat exchange through a heat-conducting oil coil to obtain medium-temperature flue gas. According to an embodiment of the present invention, the temperature of the flue gas after heat exchange through the heat-conducting oil coil is 500~600℃. It should be noted that the relevant characteristics of the heat-conducting oil coil and heat exchange parameters have been described in detail in the foregoing section and will not be repeated here.

[0111] (4) Use a gas-solid separator to perform gas-solid separation on the medium-temperature flue gas to obtain primary purified flue gas.

[0112] (5) The primary purified flue gas enters the waste heat recovery device, and is discharged after heat exchange through the heat-conducting oil pipe, economizer, and air preheater in sequence. According to an embodiment of the present invention, the flue gas temperature after heat exchange through the heat-conducting oil pipe is 370~430℃, and the flue gas temperature after heat exchange through the air preheater is 170~190℃. It should be noted that the characteristics and contents related to the heat-conducting oil pipe, economizer, air preheater, and heat exchange effect have been described in detail in the foregoing section, and will not be repeated here.

[0113] According to embodiments of the present invention, the waste gasification incineration method may further include: using an air distribution and ash removal system to automatically and fully separate coarse and fine materials in the waste entering the furnace, and using a first and second ash removal valve stacked together to form a self-locking structure to lock irregular materials, preventing the material discharged from the furnace from leaking downwards, while also avoiding the problem of large irregular pieces of material getting stuck on the ash removal valve. It should be noted that the relevant features and contents of the air distribution and ash removal system have been described in detail in the foregoing sections and will not be repeated here.

[0114] According to embodiments of the present invention, the waste gasification incineration method may further include: utilizing an ash discharge device to ensure that the medium-to-high temperature ash stream discharged from the gas-solid separator can be smoothly discharged through the ash hopper, achieving a highly reliable ash conveying effect with lower energy consumption and less wear. Specifically, a motor drives a gear through a coupling, and the gear drives a spiral scraper to rotate left and right inside the ash hopper, thereby scraping away the ash layer adhering to the inner wall of the ash hopper, ensuring that the medium-to-high temperature ash stream passes smoothly through the ash hopper, and avoiding the problem of medium-to-high temperature ash adhering to the inner wall of the ash hopper and forming clumps. It should be noted that the relevant features and contents of the ash discharge device have been described in detail in the foregoing sections and will not be repeated here.

[0115] According to embodiments of the present invention, the waste gasification incineration method may further include: installing wear-resistant plates on the convection heat exchange tubes of the waste heat recovery device, thereby effectively improving the anti-slagging performance of the air-facing surface of the heat exchange tubes, greatly reducing the probability of furnace shutdown due to ash accumulation and slagging, and significantly increasing the continuous operating time of the incinerator, etc. It should be noted that the relevant features and contents of the wear-resistant plates have been described in detail in the foregoing sections and will not be repeated here.

[0116] In summary, the waste gasification and incineration method according to the above embodiments of the present invention can fully utilize the heat of high-temperature flue gas step by step according to the flue gas flow while incinerating waste, and improve heat exchange efficiency. Furthermore, the above method can effectively address the thermal expansion and sealing problem of the furnace body, avoiding structural instability or poor sealing due to thermal expansion, and thus preventing safety hazards. Therefore, this method is not only simple in process and easy to operate, but also has a high energy grade, achieving both full resource utilization and harmless treatment of waste, while ensuring the stability and safety of the furnace body structure. The beneficial effects of the air distribution and ash removal system, ash removal device, and wear-resistant plate have been described in detail in the foregoing sections and will not be repeated here. It should be noted that the features and effects described in the above embodiments of the present invention for the dual-medium TFB gasification incinerator are also applicable to this waste gasification and incineration method, and will not be repeated here.

[0117] In the description of this specification, the references to terms such as "one embodiment," "some embodiments," "example," "specific example," or "some examples," etc., indicate that a specific feature, structure, material, or characteristic described in connection with that embodiment or example is included in at least one embodiment or example of the present invention. In this specification, the illustrative expressions of the above terms do not necessarily refer to the same embodiment or example. Furthermore, the specific features, structures, materials, or characteristics described may be combined in any suitable manner in one or more embodiments or examples. Moreover, without contradiction, those skilled in the art can combine and integrate the different embodiments or examples described in this specification, as well as the features of different embodiments or examples.

[0118] Although embodiments of the present invention have been shown and described above, it is understood that the above embodiments are exemplary and should not be construed as limiting the present invention. Those skilled in the art can make changes, modifications, substitutions and variations to the above embodiments within the scope of the present invention.

Claims

1. A dual-medium TFB gasification incinerator, characterized in that, include: The furnace body, gas-solid separator, and waste heat recovery device are connected in sequence. And the furnace body support, including: The furnace body includes a gasification section, a combustion section, and a heat exchange section connected sequentially from bottom to top. The bottom of the gasification section is provided with a first air distribution device and a slag outlet. The gasification section includes an upper variable cross-section zone, a constant cross-section zone, and a lower variable cross-section zone arranged in an upper, middle, and lower manner. The cross-sectional area of ​​the upper variable cross-section zone gradually increases from top to bottom, and the cross-sectional area of ​​the lower variable cross-section zone gradually decreases from top to bottom. The cross-sectional area of ​​the upper variable cross-section zone is not less than the cross-sectional area of ​​the combustion section. The side of the combustion section is provided with a second air distribution device. The furnace walls of the gasification section and the combustion section are both water-cooled walls; the furnace walls of the heat exchange section and the combustion section are indirectly connected, and the outer surface of the combustion section furnace wall is provided with a connecting part. The heat exchange section includes at least one stage of heat exchange furnace wall, with adjacent stages of heat exchange furnace walls arranged vertically and indirectly connected. The inner surface of each stage of the heat exchange furnace wall is provided with a set of heat transfer oil coils, and the flow direction of the heat transfer oil in each set of heat transfer oil coils is bottom in and top out. The top of the heat exchange section is provided with a hot flue gas outlet, and the hot flue gas outlet is connected to the waste heat recovery device through the gas-solid separator. The waste heat recovery device is provided from top to bottom with a heat-conducting oil pipe, an economizer and an air preheater. The hot air outlet of the air preheater is connected to at least one of the gasification section air inlet and the combustion section air inlet. The furnace support includes a steel frame body and at least one layer of support plate. The support plate is connected to the steel frame body. The support plate is higher than the connecting part and faces the furnace body. Each layer of support plate supports one level of the heat exchange furnace wall and the heat transfer oil coil provided on the inner surface of the heat exchange furnace wall. Soft connection seals are provided between two adjacent levels of the heat exchange furnace wall and between the heat exchange furnace wall and the combustion section furnace wall. The furnace body portions of the gasification section and the combustion section are suspended by the connecting portion on a support plate located between the heat exchange furnace wall and the combustion section furnace wall, the support plate being arranged circumferentially around the furnace body; or, the furnace body support further includes a first crossbeam, the first crossbeam being disposed on the steel frame body at a portion higher than the connecting portion and facing the furnace body, the furnace body portions of the gasification section and the combustion section being suspended by the connecting portion on the first crossbeam, the first crossbeam being arranged circumferentially around the furnace body; It also includes an air distribution and slag removal system, which includes a first air distribution device and a slag removal device. The first air distribution device includes a main air distribution plate, which is located at the bottom of the furnace body. A primary air chamber is located at the bottom of the main air distribution plate; a secondary air distribution plate is located outside the primary air chamber, and the secondary air distribution plate and the main air distribution plate are arranged in a stepped manner, with the secondary air distribution plate being installed at a lower height than the main air distribution plate. The slag discharge device includes: a slag discharge air chamber located at the bottom of the secondary air distribution plate, wherein the pressure of the slag discharge air chamber is greater than the pressure of the primary air chamber; and a slag discharge channel connected to the furnace body and located below the furnace body, wherein the slag discharge channel is located adjacent to the end of the secondary air distribution plate away from the main air distribution plate, and wherein the slag discharge channel has the slag outlet. The slag discharge valve includes a first slag discharge valve and a second slag discharge valve. The first slag discharge valve and the second slag discharge valve are disposed opposite each other on the inner wall of the slag discharge channel. The second slag discharge valve is disposed below the first slag discharge valve, and the width of the first slag discharge valve is smaller than the width of the slag discharge channel. The steel frame body is connected to the ground or other fixed surfaces.

2. The dual-medium TFB gasification incinerator according to claim 1, characterized in that, The support plate, located between the heat exchange furnace wall and the combustion section furnace wall, is situated on the first crossbeam near the furnace body; and / or, The furnace support also includes at least one second crossbeam. The second crossbeam is located on the steel frame body at a portion higher than the first crossbeam and facing the furnace body. The number of layers of the second crossbeam is equal to the number of layers of the support plates located between the heat exchange furnace walls. Each layer of the support plate located between two adjacent heat exchange furnace walls is located on one layer of the second crossbeam on the side close to the furnace body.

3. The dual-medium TFB gasification incinerator according to claim 1 or 2, characterized in that, The upper part of the water-cooled wall is connected to a steam drum, the inlet of the steam drum is connected to the upper header of the water-cooled wall, and the outlet of the steam drum is connected to the lower header of the water-cooled wall. A steam drum support is provided on a support plate located between the heat exchange furnace wall and the combustion section furnace wall, or a steam drum support is provided on the first crossbeam; The steam drum is mounted on the steam drum support.

4. The dual-medium TFB gasification incinerator according to claim 1 or 2, characterized in that, At least one of the following conditions must be met: The length of the combustion section is 1 / 4 to 1 / 3 of the total height of the furnace body, and the length of the gasification section is 1 / 6 to 1 / 3 of the total height of the furnace body; The connection height between two adjacent heat exchange furnace walls is 300~500mm, and the connection height between the heat exchange furnace wall and the combustion section furnace wall is 300~500mm; The inner surface of the furnace wall in the gasification section is provided with a refractory material layer; The inner surface of the furnace wall in the combustion section is partially or entirely covered with a refractory material layer; The second air distribution device includes upper, middle and lower air inlets arranged along the height of the furnace body; Each set of heat transfer oil coils is arranged in a spiral pattern along the circumference of the heat exchange furnace wall. A flexible sealing connection is provided between the furnace body and the hot flue gas outlet; The air preheater is provided with a partition, which divides the air preheater into a first air preheater and a second air preheater arranged vertically or horizontally side by side. The first air preheater includes a first cold air inlet and a first hot air outlet, and the second air preheater includes a second cold air inlet and a second hot air outlet. One of the first hot air outlet and the second hot air outlet is connected to the combustion section air inlet, and the other is connected to the gasification section air inlet. The waste heat recovery device is provided with a flue gas outlet at the bottom and a first ash outlet at the bottom. The flue gas outlet is located below the air preheater and is connected to the flue gas purification device. The heat-conducting oil pipe bank is provided with multiple layers of staggered parallel heat-conducting oil pipes along the height direction of the waste heat recovery device.

5. The dual-medium TFB gasification incinerator according to claim 1, characterized in that, At least one of the following conditions must be met: The air distribution and slag removal system also includes a fluidized gas flow channel. The fluidized gas flow channel is located at the upper part of the slag removal air chamber and is connected to the slag removal channel and the furnace body. The fluidized gas flow channel is connected to the furnace body through fluidized gas circulation inlets and large waste outlets arranged vertically. The fluidized gas circulation inlets are located in the lower part of the furnace body in an area not higher than the top of the fluidized gas flow channel. The large waste outlets are located in the lower part of the furnace body in an area not lower than the main air distribution plate. Wherein: the aperture of the large waste outlet is a, the aperture of the fluidized gas circulation inlet is c, the width of the fluidized gas flow channel is d, the aperture of the slag removal channel inlet is b, and the width of the slag removal channel is w0, b=(1~1.5)a, c=(0.5~0.8)a, d=(1.5~2.0)b, w0=(2.0~3.0)b; Let w0 be the width of the slag discharge channel, w1 be the width of the first slag discharge valve, and w2 be the width of the second slag discharge valve, where 0.5w0 ≤ w1 ≤ 0.75w0 and 0.75w0 ≤ w2. <w0; The pressure in the primary air chamber is 10~15 kPa; The pressure in the slag discharge chamber is 12~20 kPa; The slag discharge valve also includes a first rack, a first reducer and a first motor connected in sequence outside the slag discharge channel, wherein the first rack is connected to the first slag discharge valve. The slag discharge valve also includes a second rack, a second reducer, and a second motor that are connected in sequence outside the slag discharge channel; the second rack is connected to the second slag discharge valve. The angle between the main air distribution plate and the horizontal plane is 5~20°, and the angle between the secondary air distribution plate and the horizontal plane is 3~10°. The valve plate thickness of the first slag discharge valve and the second slag discharge valve is 20~35mm each independently.

6. The dual-medium TFB gasification incinerator according to claim 5, characterized in that, When the slag discharge valve is closed, the angle α between the line connecting the end of the first slag discharge valve away from the inner wall of the slag discharge channel and the end of the second slag discharge valve away from the inner wall of the slag discharge channel and the horizontal plane is 5~15°; and / or, The distance ΔH between the first slag discharge valve and the second slag discharge valve is (1 / 4~1 / 3)w0.

7. The dual-medium TFB gasification incinerator according to claim 1 or 6, characterized in that, It also includes an ash discharge device, wherein the gas-solid separator has a second ash outlet at its bottom, and the ash discharge device is connected to the second ash outlet. The ash discharge device includes: Ash hopper, wherein the ash hopper is cylindrical; A spiral scraper is disposed inside the ash hopper; A gear, one end of which is connected to the spiral scraper, and the gear is sealed to the ash hopper; A coupling that is connected to the other end of the gear; An electric motor, which is connected to the coupling.

8. The dual-medium TFB gasification incinerator according to claim 7, characterized in that, At least one of the following conditions must be met: The spiral scraper includes multiple sub-spiral scrapers, and adjacent sub-spiral scrapers are connected by rivets. The pitch of the spiral scraper is ΔL = (1 / 2~3 / 2)D, where D is the average value of the outer diameter of the ash hopper within the pitch range; The rotation angle of the spiral scraper in the circumferential direction of the ash hopper is 60~90°; The width of the spiral scraper is 1 / 4 to 1 / 3 of the circumference of the inner wall of the ash hopper where the spiral scraper is located in the circumferential direction; The ash hopper includes an integrally formed conical ash hopper and a straight ash hopper, with the conical ash hopper positioned above the straight ash hopper; The ash discharge device further includes a temperature measuring element, which is disposed on the wall of the ash hopper and extends into the ash hopper to monitor the temperature fluctuation of the flowing ash in the ash hopper. The ash discharge device further includes: multiple limiting protrusions, which are disposed on the inner wall of the ash hopper; The ash removal device also includes a PLC control unit, which is connected to the temperature measuring element and the motor via electrical signals.

9. The dual-medium TFB gasification incinerator according to claim 1 or 8, characterized in that, The heat transfer oil pipe bank includes at least one layer of heat transfer oil heat exchange pipes, each layer of heat transfer oil heat exchange pipes includes multiple spaced heat transfer oil heat exchange pipes, and at least one heat transfer oil heat exchange pipe has an anti-wear plate on its windward side; and / or, the economizer includes at least one layer of hot water heat exchange pipes, each layer of hot water heat exchange pipes includes multiple spaced hot water heat exchange pipes, and at least one hot water heat exchange pipe has an anti-wear plate on its windward side. The wear-resistant plate is detachably installed along the length of the heat exchange tube. The cross-section of the wear-resistant plate is triangular or a triangular shape with a hyperbolic structure. The vertex of the triangle or the intersection of the hyperbolic curves is located on the side of the wear-resistant plate away from the heat exchange tube.

10. The dual-medium TFB gasification incinerator according to claim 9, characterized in that, At least one of the following conditions must be met: The wear-resistant plate is suspended on the heat exchange tube; Both the triangle and the triangular-like shape are axially symmetric figures, and the axis of symmetry of the triangle or the triangular-like shape coincides with the perpendicular line from the vertex of the triangle or the intersection of the hyperbola to the central axis of the heat exchange tube. The width of the wear-resistant plate on the side closest to the heat exchange tube is 0.2 to 0.5 times the outer diameter of the heat exchange tube; The height of the wear-resistant plate is 0.05 to 0.1 times the outer diameter of the heat exchange tube; The distance between the wear-resistant plate and the heat exchange tube on the side closest to the heat exchange tube is 0.3 to 0.6 times the outer diameter of the heat exchange tube; The distance between the wear-resistant plate and the heat exchange tube is adjustable; The heat exchange tube is provided with a bracket at the top, and the bracket is provided with at least one first connection hole. The wear-resistant plate is provided with a connecting rod at the bottom, and the connecting rod is provided with at least one second connection hole that matches and connects with the first connection hole. The heat exchange tube and the wear-resistant plate are fixed by the bracket and the connecting rod. The heat-conducting oil pipe bank includes multiple rows of parallel heat-conducting oil heat exchange pipes. In the row of heat-conducting oil heat exchange pipes closest to the flue gas inlet of the waste heat recovery device, each heat-conducting oil heat exchange pipe is provided with a wear-resistant plate on its windward side. The heat-conducting oil pipe bank includes multiple rows of staggered parallel heat-conducting oil heat exchange pipes. In the at least two rows of staggered heat-conducting oil heat exchange pipes closest to the flue gas inlet of the waste heat recovery device, each heat-conducting oil heat exchange pipe is provided with a wear-resistant plate on its windward surface. The economizer includes multiple rows of parallel hot water heat exchange tubes. In the row of hot water heat exchange tubes closest to the flue gas inlet of the waste heat recovery device, each hot water heat exchange tube is provided with an anti-wear plate on its windward side. The economizer includes multiple rows of staggered parallel hot water heat exchange tubes. In at least two rows of staggered hot water heat exchange tubes closest to the flue gas inlet of the waste heat recovery device, each hot water heat exchange tube is provided with an anti-wear plate on its windward side.

11. A method for waste gasification and incineration using a dual-medium TFB gasification incinerator according to any one of claims 1-10, characterized in that, include: (1) The waste material is fed to the gasification section at the bottom of the furnace for gasification to obtain gasification gas and solid residue. The solid residue is discharged from the furnace intermittently. (2) The gasified gas is introduced into the combustion section in the middle of the furnace body for combustion to obtain high-temperature flue gas after combustion; (3) The high-temperature flue gas after combustion is cooled by heat exchange through a heat transfer oil coil to obtain medium-temperature flue gas; (4) The medium-temperature flue gas is separated into gas and solid by a gas-solid separator to obtain primary purified flue gas; (5) The primary purified flue gas enters the waste heat recovery device, and is discharged after heat exchange through the heat-conducting oil pipe, the economizer and the air preheater in sequence.

12. The method according to claim 11, characterized in that, At least one of the following conditions must be met: The temperature of the gasification section is 650~850℃, and the temperature of the combustion section is 850~1100℃; The flue gas temperature after heat exchange through the heat transfer oil coil is 500~600℃, the flue gas temperature after heat exchange through the heat transfer oil pipe is 370~430℃, and the flue gas temperature after heat exchange through the air preheater is 170~190℃. The temperature of the gasifying agent supplied to the gasification section is 150~200℃ and the pressure is 10~15kPa; the temperature of the combustion air supplied to the combustion section is 100~200℃ and the pressure is 4~6kPa.

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