Organic solid waste baking pyrolysis system

Abstract

The utility model relates to an organic solid waste baking pyrolysis system which comprises a dryer, a baking reactor, a pyrolysis reactor, a burner, a semi-coke cooler and a separation device, the dryer is communicated with the baking reactor, the dryer can convey dried materials to the baking reactor, and the pyrolysis reactor is communicated with the burner. The baking reactor can convey baked materials to the pyrolysis reactor, the pyrolysis reactor can pyrolyze the materials into semi-coke materials and pyrolysis gas, the semi-coke materials can be conveyed into the semi-coke cooler, the combustor can introduce high-temperature flue gas after combustion into the pyrolysis reactor, at least part of the pyrolysis gas can be introduced into the baking reactor, and the semi-coke materials can be conveyed into the semi-coke cooler. The baking reactor is communicated with the separation device, so that a gas-liquid mixture in the baking reactor is separated into fuel gas, light tar and wood vinegar. According to the organic solid waste baking pyrolysis system, pyrolysis gas generated by pyrolysis of organic solid waste can be used for providing heat for the system, dependence on external energy is reduced, and the yield of heavy tar is reduced.

Description

Technical Field

[0001] The utility model relates to the technical field of organic solid waste treatment, in particular to an organic solid waste baking and pyrolysis system. Background Art

[0002] Organic solid waste is biodegradable solid or semi-solid waste containing organic matter, including domestic waste, municipal sludge, industrial waste, and agricultural and forestry waste. The energy utilization of organic solid waste is consistent with ecological, environmentally friendly, and sustainable socioeconomic and energy development. Due to the huge demand for energy, organic solid waste energy utilization technology has received widespread attention. Energy utilization pathways for organic solid waste include directly using organic solid waste as an energy source and using organic solid waste to produce other energy products. Solid recycled fuel is a solid fuel made from non-hazardous waste that meets relevant quality standards. It is a new type of fuel after refuse-derived fuel (RDF). Compared to using organic solid waste directly as fuel, preparing organic solid waste into solid recycled fuel can improve many of the fuel's physical and chemical properties, providing guarantees for equipment operation, combustion stability, and low pollutant emissions. Organic solid waste can be converted into fuel gas through bio-fermentation, gasification, and pyrolysis, improving the cleanliness and economy of the fuel.

[0003] In the related art, the technology of preparing solid recovered fuel and gas by pyrolysis of organic solid waste has the following technical problems:

[0004] 1. Organic solid waste has the disadvantages of high moisture content and low calorific value. Thermal conversion requires a large amount of heat. Existing systems often need to rely on external heat or consume other fuels.

[0005] 2. The yield of heavy tar from pyrolysis of organic solid waste is high, which causes blockage and corrosion of equipment pipelines, affecting the normal operation of the equipment.

[0006] 3. During the pyrolysis process of organic solid waste, the material is heated unevenly and the heat transfer rate is slow.

[0007] 4. The mechanical structure of the organic solid waste pyrolysis system is complex, the manufacturing is difficult, the production cost is high, and the feasibility is poor. Utility Model Content

[0008] The utility model aims to solve one of the technical problems in the related art at least to a certain extent.

[0009] To this end, an embodiment of the present invention proposes an organic solid waste baking pyrolysis system, which can use the pyrolysis gas generated by the pyrolysis of the organic solid waste itself to provide heat for the system, reduce dependence on external energy, and reduce the yield of heavy tar.

[0010] The organic solid waste torrefaction pyrolysis system of an embodiment of the present invention includes: a dryer, a torrefaction reactor, a pyrolysis reactor, a burner, a semi-coke cooler and a separation device, the dryer is connected to the torrefaction reactor, the dryer can transport the dried material to the torrefaction reactor, the torrefaction reactor is connected to the pyrolysis reactor, the torrefaction reactor can transport the torrefied material to the pyrolysis reactor, the pyrolysis reactor can pyrolyze the material into semi-coke material and pyrolysis gas, the semi-coke material can be transported to the semi-coke cooler to form solid recovered fuel, the pyrolysis reactor is connected to the burner, the burner can pass the high-temperature flue gas after combustion into the pyrolysis reactor, at least part of the pyrolysis gas can be passed into the torrefaction reactor, the torrefaction reactor is connected to the separation device to separate the gas-liquid mixture in the torrefaction reactor into fuel gas, light tar and liquid.

[0011] According to the organic solid waste torrefaction and pyrolysis system of the embodiment of the present invention, the moisture content of the organic solid waste can be reduced through the dryer, reducing the heat requirement for heating the organic solid waste to the torrefaction temperature and increasing the heating rate. Since the dried material is sequentially introduced into the torrefaction reactor and the pyrolysis reactor, the cross-linking reaction of the oxygen-containing functional groups of the organic solid waste during the torrefaction process can be utilized to suppress the formation of heavy tar. At least a portion of the pyrolysis gas can be introduced into the torrefaction reactor to serve as a heat source for the torrefaction reactor, thereby providing heat to the pyrolysis gas generated by the pyrolysis of the organic solid waste itself and reducing dependence on external energy. Moreover, after cooling, the heavy tar in the pyrolysis gas will condense on the surface of the torrefaction material and then enter the pyrolysis reactor for cracking, thereby further reducing the yield of heavy tar.

[0012] In some embodiments, the pyrolysis gas generated by the pyrolysis reactor can be introduced into the burner to generate the high-temperature flue gas.

[0013] In some embodiments, the baking reactor is a down-flow baking reactor, which includes a baking reactor shell and multiple baffles. The upper end of the baking reactor shell is provided with a feed port, and the lower end of the baking reactor shell is provided with a discharge port. The multiple baffles are arranged in the baking reactor shell along the upper and lower directions of the baking reactor shell. The multiple baffles and the inner wall of the baking reactor shell define a winding discharge channel, and the feed port is connected to the discharge port through the discharge channel.

[0014] In some embodiments, an air flow distributor is provided in the torrefaction reactor shell, and the air flow distributor is used to introduce pyrolysis gas into the torrefaction reactor shell. The air flow distributor is arranged adjacent to the lower end of the torrefaction reactor shell and is connected to the discharge channel.

[0015] In some embodiments, the pyrolysis reactor is a rotary kiln pyrolysis reactor with a partition wall, and the pyrolysis reactor has a first port and a second port arranged opposite to each other along its axial direction. The material can flow in the cylinder of the pyrolysis reactor along the direction from the first port to the second port, and the high-temperature flue gas enters the partition wall of the pyrolysis reactor and flows along the direction from the first port to the second port.

[0016] In some embodiments, the heat exchange side of the semi-coke cooler is connected to the heat exchange side of the dryer through a heat exchange pipeline.

[0017] In some embodiments, the organic solid waste baking and pyrolysis system also includes a flue gas heat exchanger, which is connected to the partition wall of the pyrolysis reactor. The high-temperature flue gas after heat exchange in the partition wall of the pyrolysis reactor is passed into the flue gas heat exchanger, and the flue gas heat exchanger is connected to the heat exchange pipeline and can exchange heat with the heat exchange pipeline.

[0018] In some embodiments, the separation device includes a condenser and an oil-water separator, the condenser is connected to the gas outlet of the baking reactor, the oil-water separator is connected to the condenser, the oil-water separator can separate the gas-liquid mixture into fuel gas and mixed liquid, and the oil-water separator can separate the mixed liquid into light tar and wood vinegar. BRIEF DESCRIPTION OF THE DRAWINGS

[0019] Figure 1 It is a schematic flow chart of an organic solid waste baking and pyrolysis system according to an embodiment of the present utility model.

[0020] Reference numerals:

[0021] 1. Dryer;

[0022] 2. baking reactor; 21. baking reactor housing; 22. baffle;

[0023] 3. Pyrolysis reactor; 31. First port; 32. Second port; 33. Cylinder; 34. Partition wall;

[0024] 4. Burner;

[0025] 5. Semi-coke cooler;

[0026] 6. Separation device; 61. Condenser; 62. Oil-water separator;

[0027] 7. Flue gas heat exchanger;

[0028] 81. Heat exchange pipeline; 82. Air flow distributor; 83. Screw conveyor. DETAILED DESCRIPTION

[0029] The embodiments of the present invention are described in detail below, and examples of the embodiments are shown in the accompanying drawings. The embodiments described below with reference to the accompanying drawings are exemplary and intended to be used to explain the present invention, but should not be understood as limiting the present invention.

[0030] Please refer to the following Figure 1 The organic solid waste baking and pyrolysis system according to an embodiment of the present invention is described.

[0031] like Figure 1 As shown, the organic solid waste torrefaction pyrolysis system of the present invention embodiment includes: a dryer 1, a torrefaction reactor 2, a pyrolysis reactor 3, a burner 4, a semi-coke cooler 5 and a separation device 6. For example, the pyrolysis reactor 3 is a rotary kiln pyrolysis reactor with a partition wall.

[0032] The dryer 1 is connected to the torrefaction reactor 2, and the dryer 1 can transport the dried material to the torrefaction reactor 2. The torrefaction reactor 2 is connected to the pyrolysis reactor 3, and the torrefaction reactor 2 can transport the torrefied material to the cylinder 33 of the pyrolysis reactor 3. The pyrolysis reactor 3 can pyrolyze the material into semi-coke material and pyrolysis gas. The semi-coke material can be transported to the semi-coke cooler 5 to form solid recovered fuel.

[0033] The pyrolysis reactor 3 is connected to the burner 4, and the burner 4 can pass the high-temperature flue gas after combustion into the partition wall 34 of the pyrolysis reactor 3. At least part of the pyrolysis gas can be passed into the torrefaction reactor 2. The torrefaction reactor 2 is connected to the separation device 6 to separate the gas-liquid mixture in the torrefaction reactor 2 into fuel gas, light tar and wood vinegar.

[0034] According to the organic solid waste torrefaction pyrolysis system of the embodiment of the present invention, the moisture content in the organic solid waste can be reduced through the dryer 1, the heat requirement for heating the organic solid waste to the torrefaction temperature can be reduced, and the heating rate can be increased. Since the dried material is sequentially introduced into the torrefaction reactor 2 and the pyrolysis reactor 3, the cross-linking reaction of the oxygen-containing functional groups of the organic solid waste during the torrefaction process can be utilized to suppress the formation of heavy tar. Moreover, since part of the pyrolysis gas can be introduced into the torrefaction reactor 2 as a heat source for the torrefaction reactor 2, the pyrolysis gas generated by the pyrolysis of the organic solid waste itself can provide heat for the system, reducing dependence on external energy. Moreover, after cooling, the heavy tar in the pyrolysis gas will condense on the surface of the torrefaction material and then enter the pyrolysis reactor for cracking, thereby further reducing the yield of heavy tar.

[0035] Optionally, the pyrolysis gas generated by the pyrolysis reactor 3 can be introduced into the burner 4 to generate high-temperature flue gas. It is understood that the organic solid waste roasting and pyrolysis system of the embodiment of the present invention can utilize the pyrolysis gas generated by the pyrolysis reactor 3 as the combustion feedstock for the burner 4, thereby serving as the heat source for the pyrolysis reactor 3. This allows the pyrolysis gas generated by the pyrolysis of the organic solid waste itself to provide heat for the system, reducing reliance on external energy sources.

[0036] Optionally, the torrefaction reactor 2 is a down-flow torrefaction reactor 2, comprising a torrefaction reactor housing 21 and a plurality of baffles 22. The upper end of the torrefaction reactor housing 21 is provided with an inlet, and the lower end of the torrefaction reactor housing 21 is provided with an outlet. The plurality of baffles 22 are arranged vertically within the torrefaction reactor housing 21. The plurality of baffles 22 and the inner wall of the torrefaction reactor housing 21 define a winding outlet passage, and the inlet is connected to the outlet through the outlet passage. It is understood that the dryer 1 can allow the dried organic material to enter the torrefaction reactor housing 21 through the inlet, and the torrefaction organic solid waste can be discharged through the outlet and transported to the pyrolysis reactor 3 via the screw conveyor 83.

[0037] The down-bed type roasting reactor 2 can prolong the residence time of the material in the roasting reactor 2. The organic solid waste can be continuously dispersed and turned under the stopping action of multiple baffles 22, which can make the organic solid waste roasted more fully. In addition, the cross-linking reaction of the oxygen-containing functional groups of the organic solid waste during the roasting process can inhibit the formation of heavy tar and reduce the yield of heavy tar.

[0038] It is understood that the pyrolysis gas carries tar vapor into the downer torrefaction reactor 2. As it comes into contact and exchanges heat with the cooler organic solid waste particles, the temperature drops, causing the heavy tar vapor to condense and adhere to the surface of the organic solid waste particles. It then enters the pyrolysis reactor 3 along with the organic solid waste particles for further cracking, producing semi-coke and pyrolysis gas. This process promotes the cracking of heavy tar within the system and reduces its yield.

[0039] Optionally, an air flow distributor 82 is provided within the torrefaction reactor housing 21 for introducing pyrolysis gas into the torrefaction reactor housing 21. The air inlet is located adjacent to the lower end of the torrefaction reactor housing 21 and communicates with the discharge channel via the air flow distributor 82. It will be appreciated that organic solid waste enters the torrefaction reactor housing 21 from top to bottom, while pyrolysis gas enters the torrefaction reactor housing 21 from bottom to top, thereby enabling efficient heat transfer through countercurrent heat exchange.

[0040] In the embodiments of the present application, the baking temperature is controlled at 200-300°C, and the pyrolysis temperature is controlled above 600°C to avoid the "window temperature" of 500-600°C for tar formation, thereby reducing the yield of tar. The baking treatment before pyrolysis promotes the cross-linking reaction of oxygen-containing functional groups in the organic solid waste, inhibiting the formation of heavy tar. The high-temperature pyrolysis gas is fully in contact with the low-temperature organic solid waste in the down-flow bed baking reactor 2, promoting the condensation of heavy tar on the surface of the organic solid waste particles, and then enters the pyrolysis reactor 3 with the organic solid waste to undergo a cracking reaction, further reducing the yield of heavy tar.

[0041] Optionally, the pyrolysis reactor 3 is a rotary kiln pyrolysis reactor with a partition wall. The pyrolysis reactor 3 has a first port 31 and a second port 32 arranged relative to each other along its axial direction. The material in the cylinder 33 of the pyrolysis reactor 3 can flow from the first port 31 to the second port 32, and the high-temperature flue gas in the partition wall 34 of the pyrolysis reactor 3 can flow from the first port 31 to the second port 32. It can be understood that the baked organic solid waste is constantly turned in the rotary kiln cylinder and is heated to above 600°C by the wall surface, causing a pyrolysis reaction, releasing pyrolysis gas, and generating semi-coke material. The high-temperature flue gas introduced into the partition wall 34 of the pyrolysis reactor 3 provides heat for the pyrolysis reaction. The flow direction of the high-temperature flue gas is opposite to the movement direction of the pyrolysis material, achieving a countercurrent heat exchange effect, which is conducive to improving the heat transfer efficiency.

[0042] In some embodiments, the heat exchange side of the semi-coke cooler 5 is connected to the heat exchange side of the dryer 1 via a heat exchange line 81. It is understood that the semi-coke cooler 5 can transfer the heat of the semi-coke material to the dryer 1 via the heat exchange line 81, thereby both cooling the semi-coke material and heating the dryer 1, thereby reducing heat loss in the system. The dryer 1 does not require an external heat source, reducing its dependence on external energy.

[0043] Specifically, the organic solid waste baking and pyrolysis system also includes a flue gas heat exchanger 7, which is connected to the partition wall 34 of the pyrolysis reactor 3. The high-temperature flue gas after heat exchange in the partition wall 34 of the pyrolysis reactor 3 is passed into the flue gas heat exchanger 7. The flue gas heat exchanger 7 is connected to the heat exchange pipeline 81 and can exchange heat with the heat exchange pipeline 81.

[0044] It is understood that after heat exchange, the high-temperature flue gas exits the partition wall 34 of the rotary kiln pyrolysis reactor 3 and enters the flue gas heat exchanger 7 to heat the condensed water discharged from the dryer 1. The semi-coke material generated by the pyrolysis of organic solid waste exits the barrel 33 of the pyrolysis reactor 3 and is cooled in the semi-coke cooler 5 before becoming solid recovered fuel. The condensed water exits the flue gas heat exchanger 7 and enters the semi-coke cooler 5. Further heating by the high-temperature semi-coke converts it into high-temperature steam, which is then passed into the dryer 1. This allows for waste heat recovery from the high-temperature flue gas and semi-coke material, improving energy efficiency.

[0045] In the example of this application, the separation device 6 includes a condenser 61 and an oil-water separator 62. The condenser 61 is connected to the gas outlet of the torrefaction reactor 2, and the oil-water separator 62 is connected to the condenser 61. The oil-water separator 62 separates the gas-liquid mixture into gas and a mixed liquid. The oil-water separator 62 further separates the mixed liquid into light tar and wood vinegar. It will be understood that after the pyrolysis gas is discharged from the downer torrefaction reactor 2, it enters the condenser 61, where it is cooled and separated into non-condensable gas and liquid products. The non-condensable gas is used as the gas product, and the liquid product passes through the oil-water separator 62 to produce light tar and wood vinegar.

[0046] Another embodiment of the present invention provides a method for baking and pyrolyzing organic solid waste, using an organic solid waste baking and pyrolyzing system according to an embodiment of the present invention. The method comprises the following steps:

[0047] Transporting the organic solid waste to the dryer 1 for drying;

[0048] The dried material is transported to the baking reactor 2 for baking;

[0049] The roasted material is transported to the pyrolysis reactor 3 for pyrolysis to form pyrolysis gas and semi-coke material;

[0050] Part of the pyrolysis gas is introduced into the burner 4 for combustion to generate high-temperature flue gas, which is introduced into the partition wall 34 of the pyrolysis reactor to serve as a heat source for the pyrolysis reactor 3. Another part of the pyrolysis gas is introduced into the torrefaction reactor 2 to serve as a heat source for the torrefaction reactor 2.

[0051] The semi-coke material is transported to the semi-coke cooler 5 to form solid recovered fuel. The semi-coke cooler 5 exchanges heat with the dryer 1 to provide heat to the dryer 1.

[0052] According to the method for baking and pyrolysis of organic solid waste according to the embodiment of the present invention, the moisture content of the organic solid waste can be reduced by the dryer 1, the heat requirement for heating the organic solid waste to the baking temperature can be reduced, and the heating rate can be increased. Since the dried material is sequentially introduced into the baking reactor 2 and the pyrolysis reactor 3, the cross-linking reaction of the oxygen-containing functional groups of the organic solid waste during the baking process can be utilized to suppress the formation of heavy tar. At least a portion of the pyrolysis gas can be introduced into the baking reactor 2 to serve as a heat source for the baking reactor 2, thereby providing heat to the pyrolysis gas generated by the pyrolysis of the organic solid waste itself, reducing dependence on external energy. In addition, the heavy tar in the cooled pyrolysis gas will condense on the surface of the baking material and then enter the pyrolysis reactor for cracking, thereby further reducing the yield of heavy tar.

[0053] In some embodiments, the pyrolysis temperature of the pyrolysis reactor 3 is above 600°C, and the baking temperature of the baking reactor 2 is between 200°C and 300°C. It is understandable that the pyrolysis temperature is controlled to be higher than 600°C to avoid the "window temperature" of 500-600°C for tar formation, thereby reducing the yield of tar. The baking temperature of the baking reactor 2 is between 200°C and 300°C, which can make the baking treatment before pyrolysis promote the cross-linking reaction of oxygen-containing functional groups in the organic solid waste and inhibit the formation of heavy tar. The high-temperature pyrolysis gas is fully in contact with the low-temperature organic solid waste in the down-flowing bed baking reactor 2, promoting the condensation of heavy tar on the surface of the organic solid waste particles, and then enters the pyrolysis reactor 3 with the organic solid waste to undergo cracking reaction, further reducing the yield of heavy tar.

[0054] Optionally, the dryer 1 dries the moisture content of the organic solid waste to less than 10%, the feeding time of the dried material in the baking reactor 2 is more than 30 seconds, and the baking time of the dried material in the baking reactor 2 is more than 30 minutes, thereby ensuring sufficient heat exchange between the organic solid waste and the pyrolysis gas and sufficient progress of the baking reaction.

[0055] A specific embodiment of the organic solid waste baking and pyrolysis system of the present invention is described below.

[0056] The organic solid waste raw material in this embodiment is domestic garbage.

[0057] The domestic garbage with an original moisture content of 40% is first crushed to a particle size of less than 30 mm, and then enters the steam paddle dryer 1 for drying to reduce the moisture content to less than 10%.

[0058] The dried domestic waste enters the descender-type torrefaction reactor 2. Its descent time in the descender is controlled to at least 30 seconds to ensure sufficient heat exchange between the domestic waste and the pyrolysis gas. After the pyrolysis gas is added, the domestic waste is heated to 300°C and deposited at the bottom of the descender, where a series of torrefaction reactions occur, including the decomposition of oxygen-containing functional groups. The torrefaction time is controlled to 30 minutes by varying the material accumulation height at the bottom of the descender and the speed of the conveyor screw at the bottom of the descender.

[0059] A conveyor screw at the bottom of the descending bed delivers the roasted domestic waste into the rotary kiln pyrolysis reactor 3 for pyrolysis. The domestic waste is heated to 700°C in the rotary kiln pyrolysis reactor 3 for 15 minutes, releasing pyrolysis gas and forming semi-coke. The pyrolysis gas consists of tar, water vapor, and non-condensable gases such as CO2 and CH4.

[0060] 20% of the pyrolysis gas is passed into burner 4, generating high-temperature flue gas at 1000°C. The remaining pyrolysis gas enters descending bed torrefaction reactor 2. The high-temperature flue gas is passed into the partition wall of rotary kiln pyrolysis reactor 3, providing heat for the pyrolysis of domestic waste, and the temperature drops to 700°C. After exiting the partition wall of rotary kiln pyrolysis reactor 3, the flue gas enters flue gas heat exchanger 7 for recovery and preheating, where it is cooled to 200°C before being purified and discharged.

[0061] The pyrolysis gas introduced into the down-flow roasting reactor 2 exchanges heat with the domestic waste and its temperature drops to 150° C. The heavy tar in the pyrolysis gas condenses on the surface of the domestic waste particles and is separated from the pyrolysis gas.

[0062] The pyrolysis gas is discharged from the descending bed and enters the condenser 61 to obtain light tar, wood vinegar and fuel gas.

[0063] The tar yield in this example is less than 5%, and the content of heavy tar components in the tar is less than 10%. The yield of solid recovered fuel is 10.8%, with a calorific value of 20 MJ / kg. The yield of gas is 43.2%, with a calorific value of 23.6 MJ / Nm3.

[0064] In summary, the organic solid waste baking and pyrolysis system and method of the embodiments of the present invention have at least the following technical effects:

[0065] 1. Improve the energy utilization efficiency of organic solid waste without relying on external energy and external fuel.

[0066] This utility model utilizes the heat released by the combustion of a portion of the pyrolysis gas to pyrolyze organic solid waste, without relying on external heat or supplemental fuel. Through the rational arrangement of material flows, the waste heat of the materials is fully utilized. High-temperature semi-coke and waste heat from flue gas are used to dry the organic solid waste, while waste heat from the pyrolysis gas is used to bake the organic solid waste, achieving high energy efficiency for the entire system.

[0067] 2. Organic solid waste is fully baked and treated.

[0068] The present invention utilizes an internal component down-bed to perform baking operations on organic solid waste, and heats the organic solid waste through convection heat exchange between high-temperature pyrolysis gas and the organic solid waste, which has a better heat transfer effect than the commonly used partition heat exchange. The baffle 22 in the down-bed causes the organic solid waste to be continuously dispersed and turned over during the falling process, and allows the organic solid waste to have sufficient residence time in the down-bed to ensure that the organic solid waste is fully baked. In addition, the organic solid waste is fully dried before the baking process, reducing the heat demand for heating the organic solid waste to the baking temperature, increasing the heating rate, and reducing the bonding effect between materials, thereby promoting the full dispersion of materials during the falling process of the down-bed, increasing the convection heat exchange area with the pyrolysis gas, and optimizing the heat transfer effect.

[0069] 3. The yield of heavy tar is low, which avoids equipment blockage and corrosion.

[0070] The present invention controls the baking temperature between 200-300°C and the pyrolysis temperature above 600°C, avoiding the "window temperature" of 500-600°C for tar formation and reducing the tar yield. The baking treatment before pyrolysis promotes cross-linking reactions of oxygen-containing functional groups in the organic solid waste, inhibiting the formation of heavy tar. The high-temperature pyrolysis gas fully contacts the low-temperature organic solid waste in the down-flowing bed baking reactor 2, promoting the condensation of heavy tar on the surface of the organic solid waste particles. The gas then enters the rotary kiln with the organic solid waste to undergo a cracking reaction, further reducing the heavy tar yield.

[0071] 4. The equipment has a simple structure, high operational reliability and is easy to scale up.

[0072] The utility model uses a steam paddle dryer 1, a downer roasting reactor 2, and a rotary kiln pyrolysis reactor 3 to dry, roast, and pyrolyze organic solid waste. These devices have good adaptability to materials, are not strict on material particle size, have a simple structure, are easy to scale up, and have high operational reliability.

[0073] In the description of the present invention, it should be understood that the terms "center", "longitudinal", "lateral", "length", "width", "thickness", "up", "down", "front", "back", "left", "right", "vertical", "horizontal", "top", "bottom", "inside", "outside", "clockwise", "counterclockwise", "axial", "radial", "circumferential" and the like to indicate orientations or positional relationships based on the orientations or positional relationships shown in the accompanying drawings, and are only for the convenience of describing the present invention and simplifying the description, and do not indicate or imply that the device or element referred to must have a specific orientation, be constructed and operated in a specific orientation, and therefore should not be understood as a limitation to the present invention.

[0074] 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 the technical features being referred to. Thus, a feature specified as "first" or "second" may explicitly or implicitly include at least one such feature. In the description of this utility model, "plurality" means at least two, such as two, three, etc., unless otherwise specifically defined.

[0075] In this utility model, unless otherwise specified or limited, the terms "installed," "connected," "connect," "fixed," etc. should be understood in a broad sense. For example, they can refer to fixed connection, detachable connection, or integration; mechanical connection, electrical connection, or communication; direct connection or indirect connection through an intermediate medium; internal communication between two elements or interaction between two elements, unless otherwise specified. For those skilled in the art, the specific meanings of the above terms in this utility model can be understood according to specific circumstances.

[0076] In the present invention, unless otherwise expressly specified or limited, when a first feature is "above" or "below" a second feature, it may mean that the first and second features are in direct contact, or the first and second features are in indirect contact through an intermediary. Furthermore, when a first feature is "above," "above," or "above" a second feature, it may mean that the first feature is directly above or diagonally above the second feature, or simply means that the first feature is at a higher level than the second feature. When a first feature is "below," "below," or "below" a second feature, it may mean that the first feature is directly below or diagonally below the second feature, or simply means that the first feature is at a lower level than the second feature.

[0077] In the present invention, the terms "one embodiment", "some embodiments", "example", "specific example", or "some examples" mean that the specific features, structures, materials or characteristics described in conjunction with the embodiment or example are included in at least one embodiment or example of the present invention. In this specification, the schematic expressions of the above terms do not necessarily refer to the same embodiment or example. Moreover, the specific features, structures, materials or characteristics described can be combined in any one or more embodiments or examples in a suitable manner. In addition, those skilled in the art can combine and combine different embodiments or examples described in this specification and the features of different embodiments or examples without contradiction.

[0078] Although the above embodiments have been shown and described, it is understood that the above embodiments are illustrative and cannot be understood as limitations on the present invention. Changes, modifications, substitutions and variations of the above embodiments made by ordinary technicians in this field are all within the scope of protection of the present invention.

Claims

1. An organic solid waste baking pyrolysis system, characterized in that: include: A dryer, a torrefaction reactor, a pyrolysis reactor, a burner, a semi-coke cooler and a separation device, wherein the dryer is connected to the torrefaction reactor and can transport the dried material to the torrefaction reactor, the torrefaction reactor is connected to the pyrolysis reactor and can transport the torrefied material to the pyrolysis reactor, the pyrolysis reactor can pyrolyze the material into semi-coke material and pyrolysis gas, the semi-coke material can be transported to the semi-coke cooler to form solid recovered fuel, the pyrolysis reactor is connected to the burner and can pass the high-temperature flue gas after combustion into the pyrolysis reactor, at least part of the pyrolysis gas can be passed into the torrefaction reactor, the torrefaction reactor is connected to the separation device to separate the gas-liquid mixture in the torrefaction reactor into fuel gas, light tar and wood vinegar.

2. The organic solid waste baking pyrolysis system according to claim 1, characterized in that: The pyrolysis gas generated by the pyrolysis reactor can be introduced into the burner to generate the high-temperature flue gas.

3. The organic solid waste baking pyrolysis system according to claim 1, characterized in that: The baking reactor is a down-flow baking reactor, comprising a baking reactor shell and a plurality of baffles. A feed port is provided at the upper end of the baking reactor shell, and a discharge port is provided at the lower end of the baking reactor shell. The plurality of baffles are arranged in the baking reactor shell along the vertical direction thereof. The plurality of baffles and the inner wall of the baking reactor shell define a winding discharge channel, and the feed port is connected to the discharge port through the discharge channel.

4. The organic solid waste baking pyrolysis system according to claim 3, characterized in that: An air flow distributor is provided in the torrefaction reactor shell, and is used to introduce pyrolysis gas into the torrefaction reactor shell. The air flow distributor is arranged adjacent to the lower end of the torrefaction reactor shell and is communicated with the discharge channel.

5. The organic solid waste baking and pyrolysis system according to claim 1, characterized in that: The pyrolysis reactor is a rotary kiln pyrolysis reactor with a partition wall. The pyrolysis reactor has a first port and a second port arranged opposite to each other along its axial direction. The material can flow in the cylinder of the pyrolysis reactor from the first port to the second port. The high-temperature flue gas enters the partition wall of the pyrolysis reactor and flows from the first port to the second port.

6. The organic solid waste baking and pyrolysis system according to claim 1, characterized in that: The heat exchange side of the semi-coke cooler is connected to the heat exchange side of the dryer through a heat exchange pipeline.

7. The organic solid waste baking and pyrolysis system according to claim 6, characterized in that: It also includes a flue gas heat exchanger, which is connected to the partition wall of the pyrolysis reactor. The high-temperature flue gas in the partition wall of the pyrolysis reactor is passed into the flue gas heat exchanger after heat exchange. The flue gas heat exchanger is connected to the heat exchange pipeline and can exchange heat with the heat exchange pipeline.

8. The organic solid waste roasting and pyrolysis system according to any one of claims 1 to 7, characterized in that: The separation device includes a condenser and an oil-water separator. The condenser is connected to the gas outlet of the roasting reactor. The oil-water separator is connected to the condenser. The oil-water separator can separate the gas-liquid mixture into fuel gas and mixed liquid. The oil-water separator can separate the mixed liquid into light tar and wood vinegar.

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