Self-heat-supply biomass pyrolysis-gasification poly-generation system and method

Abstract

The invention discloses a self-heating type biomass pyrolysis-gasification poly-generation system and method, belongs to the technical field of biomass energy conversion, and aims to reduce energy consumption and improve the reaction rate of pyrolysis carbon gasification. According to the system, the combustor is selected as an external heat source, gasified gas and non-condensable gas generated in the pyrolysis process can be used as fuel of the combustor, heat energy is provided for the rotary kiln reactor and the gasifier reactor, self heat supply of the system is achieved, and energy consumption is remarkably reduced. The material guide plates are obliquely arranged downwards, and the material guide plates in the two rows of material guide plate groups are arranged in a staggered manner in the height direction of the reaction cavity of the gasification furnace, so that a wave-shaped reaction runner is formed in the reaction cavity of the gasification furnace, and the reaction time can be effectively prolonged; meanwhile, the arranged driving mechanism can drive the material guide plate to swing up and down around the hinged part at the upper end of the material guide plate, so that the gasification retention time of the pyrolytic carbon can be controlled, the pyrolytic carbon can be scattered and prevented from caking, the rapid and sufficient reaction of the pyrolytic carbon and the gasifying agent is promoted, and the gasification rate is increased.

Description

Technical Field

[0001] This invention belongs to the field of biomass energy conversion technology, specifically relating to a self-heating biomass pyrolysis-gasification polygeneration system and method. Background Technology

[0002] Biomass is a widely available, abundant, and environmentally friendly green renewable energy source, encompassing all plants, microorganisms, and animals that feed on plants and microorganisms, as well as their waste products. Bamboo, as a typical biomass, is characterized by its short growth cycle, renewability, zero carbon emissions, and wide application in bamboo products. However, approximately 60%–70% of bamboo processing generates waste, containing about 65% cellulose, 23% lignin, and other substances. Therefore, the rational and efficient utilization of bamboo waste resources is particularly important. Thermal conversion is one of the effective ways to achieve high-value utilization of bamboo waste, converting it into high-value products such as biochar, bio-oil, and syngas. However, existing thermal conversion technologies for bamboo waste still face many technical bottlenecks, especially in terms of energy efficiency, product yield, and system integration, which urgently require improvement.

[0003] Currently, the pyrolysis of bamboo waste mainly uses rotary kilns or fixed-bed reactors. Rotary kilns are often used for the pyrolysis and carbonization of biomass because of their simple structure, convenient operation, relatively uniform heating of raw materials, strong applicability to materials, and generally no material jamming or blockage. However, the following problems still exist: (1) Low thermal efficiency: External heat source is required for heating, and heat is conducted through the kiln wall. The heat exchange area with the material is small, so the thermal efficiency is low, the external heat source has high energy consumption, and the heat loss is large. Usually, only 30% to 40% of the energy is used for material pyrolysis. Especially when lumpy bamboo waste is used as material, the material is often concentrated at the bottom of the kiln and is not easy to heat. (2) Uneven heat transfer: Traditional rotary kilns lack effective internal components to disperse the material. The material is easy to accumulate and clump, resulting in local overheating or insufficient pyrolysis, and the bio-oil yield is low (usually <30%). (3) Secondary cracking of oil and gas: The residence time of pyrolysis oil and gas in the high-temperature zone is too long, which easily cracks into non-condensable gas, reducing the yield of liquid products.

[0004] Existing patent application CN118274608A discloses a rotary kiln-type oxygen-free pyrolysis furnace with high heat exchange efficiency via an internally toothed surface. While this increases the heat exchange area through the use of internally toothed heat exchange surface technology, when used to process blocky bamboo waste, the bamboo blocks tend to stick to the tips of the teeth, resulting in limited improvement in actual heat exchange efficiency. Patent application CN117487577A discloses an externally heated biomass pyrolysis device, which employs a multi-layer heating structure to enhance heat transfer and increase production capacity. However, the increased structural complexity raises the difficulty of manufacturing and maintenance.

[0005] In addition, the gasification of pyrolytic char currently mostly uses fluidized bed or fixed bed gasifiers, mainly using air and / or steam as gasifying agents. The main problems with existing gasifiers are: (1) Low reaction rate: Pyrolytic char particles are prone to agglomeration, have a small specific surface area, and do not have sufficient contact with the gasifying agent, resulting in low gasification efficiency. (2) Requires auxiliary energy: Gasifiers require additional heating, such as electric heating or combustion supplementary heating, which consumes more energy and increases costs.

[0006] In summary, existing rotary kiln pyrolysis systems suffer from low heat and mass transfer efficiency, low yield and quality of pyrolysis products when processing bulk biomass. Furthermore, the subsequent gasification and utilization of pyrolysis char also faces challenges of low reaction efficiency and high energy consumption. Therefore, developing an integrated system and method that can effectively enhance heat and mass transfer, improve pyrolysis efficiency and product quality, and achieve efficient and low-consumption gasification of pyrolysis char, in order to realize the synergistic high-value multi-product utilization of bulk biomass such as bamboo waste, has become a key issue urgently needing to be addressed in this field. Summary of the Invention

[0007] This invention provides a self-heating biomass pyrolysis-gasification polygeneration system and method, which aims to reduce energy consumption and increase the reaction rate of pyrolysis char gasification.

[0008] The technical solution adopted by the present invention to solve its technical problem is: a self-heating biomass pyrolysis-gasification polygeneration system, including a pyrolysis unit, a gasification unit and a pyrolysis oil collection unit;

[0009] The pyrolysis unit includes a rotary kiln reactor having a first feed inlet, a first heating inlet, a rotary kiln flue gas outlet, a rotary kiln reaction chamber, a pyrolysis carbon outlet, and a pyrolysis oil and gas outlet, a first feeding mechanism connected to the first feed inlet, and an external heat source connected to the first heating inlet.

[0010] The gasification unit includes a gasifier reactor, which has a second feed port connected to the pyrolytic char outlet, a second heating port connected to an external heat source, a gasifier flue gas outlet, a gasifier reaction chamber, a biochar outlet, and a gasified gas outlet.

[0011] The pyrolysis oil collection unit has a pyrolysis oil and gas inlet connected to the pyrolysis oil and gas outlet, as well as a bio-oil outlet and a non-condensable gas outlet.

[0012] The external heat source is a burner, which has a fuel inlet connected to a gasified gas outlet and a non-condensable gas outlet to receive gasified gas and non-condensable gas as fuel.

[0013] The gasifier reaction chamber is equipped with a material guiding mechanism and a driving mechanism. The material guiding mechanism includes two rows of material guiding plates, each row of which includes at least two material guiding plates. The material guiding plates are inclined downwards and their upper ends are hinged to the cavity wall of the gasifier reaction chamber. The material guiding plates in the two rows of material guiding plates are staggered in the height direction of the gasifier reaction chamber and are all connected to the driving mechanism. The driving mechanism can drive the material guiding plates to swing up and down around their upper hinged parts and always maintain an inclined downward state.

[0014] Furthermore, the first feeding mechanism includes a first screw conveyor with a first feeding motor and a hopper connected to the feed inlet of the first screw conveyor via a second discharge airlock;

[0015] The first feed inlet is connected to the front end of the rotary kiln reaction chamber, the pyrolysis carbon outlet is connected to the lower rear end of the rotary kiln reaction chamber, and the pyrolysis oil and gas outlet is connected to the rear end of the rotary kiln reaction chamber.

[0016] The rotary kiln reaction chamber has a rotary kiln heating chamber inside its cavity wall. The first heating port is connected to the rear of the rotary kiln heating chamber, and the rotary kiln flue gas outlet is connected to the front of the rotary kiln heating chamber.

[0017] Furthermore, the rotary kiln reaction chamber is provided with a cylindrical internal component, and the inner wall of the internal component is provided with a lifting structure; the lifting structure includes at least three rows of lifting plate groups distributed circumferentially along the internal component, each lifting plate group includes at least two lifting plates distributed axially along the internal component, and the lifting plates in any two adjacent lifting plate groups are staggered.

[0018] Furthermore, the front of the lifting plate is provided with an inner protrusion, and the back of the lifting plate is provided with an outer protrusion;

[0019] And / or, one end of the lifting plate is connected to the inner wall of the internal component, and the other end is provided with a lifting hook that bends to one side, the bending direction of the lifting hook being the same as the rotation direction of the rotary kiln reactor; along the radial direction of the rotary kiln reactor, the length of the lifting plate is 1 / 10 to 1 / 5 of the radius of the rotary kiln reactor.

[0020] Furthermore, the second feed inlet is connected to the upper part of the gasifier reaction chamber, the biochar outlet is connected to the bottom of the gasifier reaction chamber, and the gasified gas outlet is connected to the top of the gasifier reaction chamber.

[0021] The gasifier reaction chamber is provided with a gasifier heating chamber inside the chamber wall. The second heating port is connected to the lower part of the gasifier heating chamber, and the gasifier flue gas outlet is connected to the upper part of the gasifier heating chamber.

[0022] The gasification unit also includes a charcoal canister, which is connected to a biochar outlet.

[0023] Furthermore, the second feed inlet is connected to the pyrolysis carbon outlet via a second feeding mechanism;

[0024] The second feeding mechanism includes a second screw conveyor with a second feeding motor;

[0025] The drive mechanism includes a crank disposed at the upper part of the gasifier reaction chamber and drivenly connected to the second feed motor, and a positioning shaft disposed along the height direction of the gasifier reaction chamber and movably connected to each guide plate; the positioning shaft is drivenly connected to the drive end of the crank.

[0026] The upper side of the guide plate is provided with dispersing teeth, and there are at least three dispersing teeth arranged sequentially along the inclined direction of the guide plate.

[0027] Furthermore, the pyrolysis oil collection unit includes a spray tower, a heavy oil collection tank, a first condenser, a second condenser, and a light oil collection tank;

[0028] The spray tower has a spray tower inlet that serves as the inlet for pyrolysis oil and gas, and a spray tower condensate oil outlet and a spray tower non-condensable oil and gas outlet.

[0029] The heavy oil collection tank is connected to the condensate outlet of the spray tower.

[0030] The first condenser has a first condenser inlet connected to the non-condensable oil and gas outlet of the spray tower, as well as a first condenser oil outlet and a first condenser gas outlet;

[0031] The second condenser has a second condenser inlet connected to the outlet of the first condenser, as well as a second condenser outlet and a second condenser oil outlet;

[0032] The light oil collection tank is connected to the oil outlet of the first condenser and the oil outlet of the second condenser, respectively.

[0033] The spray tower condensate oil outlet, the first condensate tank oil outlet, and the second condensate tank oil outlet are all bio-oil outlets. The second condensate tank gas outlet is a non-condensable gas outlet, which is connected to the fuel inlet via a second induced draft fan.

[0034] Furthermore, the system also includes a heat exchange unit, which includes a first heat exchanger and a second heat exchanger;

[0035] The gasifier reactor also has a gasifying agent addition port connected to the lower part of the gasifier reaction chamber; the first heat exchanger has a gasifying agent inlet, a gasifying agent outlet connected to the gasifying agent addition port, a first heat exchanger flue gas inlet connected to the rotary kiln flue gas outlet and / or the gasifier flue gas outlet, and a first heat exchanger flue gas outlet.

[0036] The second heat exchanger has an oxygen inlet, an oxygen outlet connected to a fuel inlet, a second heat exchanger flue gas inlet connected to a rotary kiln flue gas outlet and / or a gasifier flue gas outlet, and a second heat exchanger flue gas outlet.

[0037] Furthermore, the heat exchange unit also includes a flue gas processor, a first induced draft fan, and a blower;

[0038] The flue gas processor has a flue gas processor inlet connected to the flue gas outlet of the first heat exchanger, and a flue gas processor outlet.

[0039] The first induced draft fan is connected to the exhaust port of the flue gas processor;

[0040] The blower is connected to the oxygen supply inlet.

[0041] The present invention also provides a self-heating biomass pyrolysis-gasification polygeneration method, which uses biomass particles with a particle size of 2 to 30 mm as raw materials and uses the above-mentioned self-heating biomass pyrolysis-gasification polygeneration system to prepare bio-oil and biochar.

[0042] During the preparation process, the rotation speed of the rotary kiln reactor (6) is 1-2 r / min, the pyrolysis temperature is 550-600℃, the pyrolysis time is 35-45 min, the gasification temperature is 800-900℃, and the gasification time is 55-65 min.

[0043] The beneficial effects of this invention are: the system selects a burner as an external heat source and connects the gasification gas outlet and the non-condensable gas outlet to the fuel inlet of the burner. Thus, the gasification gas generated from pyrolysis carbon gasification and the non-condensable gas in pyrolysis oil and gas can be used as fuel for the burner to power the rotary kiln reactor and the gasification furnace reactor. This not only treats the reaction tail gas but also achieves the purpose of self-heating and reducing energy consumption, realizing an energy closed loop. By tilting the guide plates downwards and arranging them in a staggered pattern along the height of the gasifier's reaction chamber, a wave-shaped reaction flow channel is formed within the gasifier's reaction chamber. This extends the residence time of the pyrolytic carbon in the gasifier's reaction chamber, allowing it more time to absorb heat and react, effectively prolonging the reaction time. Simultaneously, the driving mechanism enables the guide plates to swing up and down around their upper hinged parts. On one hand, the driving mechanism can control the speed of the pyrolytic carbon flow to control the gasification residence time of the pyrolytic carbon. On the other hand, the swinging guide plates can disperse the pyrolytic carbon, preventing it from clumping and promoting a rapid and complete reaction between the pyrolytic carbon and the gasifying agent, thus increasing the gasification rate. Furthermore, the swinging guide plates can shake off the pyrolytic carbon adhering to their surface, preventing material accumulation from affecting the gasification reaction.

[0044] The technical effects brought about or directly generated by other technical features of the present invention will be described in detail in the following detailed description section. Attached Figure Description

[0045] Figure 1 This is a schematic diagram of the implementation structure of the system of the present invention;

[0046] Figure 2 This is a three-dimensional structural schematic diagram of the internal components in the system of this invention;

[0047] Figure 3 This is a side view of the guide plate in the system of the present invention.

[0048] The diagram is labeled as follows: 1-First feed motor; 2-First screw conveyor; 3-Transmission gear; 4-First support roller; 5-Rotary kiln heating chamber; 6-Rotary kiln reactor; 7-Second support roller; 8-Pyrolysis char outlet; 9-First feed airlock; 10-First heat exchanger; 11-Gasifying agent inlet; 12-Gasifying agent outlet; 13-Flue gas processor inlet; 14-Flue gas processor; 15-Flue gas processor outlet; 16-First induced draft fan; 17-Charcoal canister; 18-Biochar outlet; 19-Second heating port; 20-Gasifier reactor; 21-Guide plate; 22-Gasifier heating chamber; 23-Positioning shaft; 24-Dispersing teeth; 25-Gasifier flue gas outlet; 26-Gasification gas outlet; 27-Second screw conveyor; 28-Second feed motor; 29-Pyrolysis oil and gas outlet; 30-Spray tower inlet. ; 31-Spray tower; 32-Spray tower condensate oil outlet; 33-Heavy oil collection tank; 34-Light oil collection tank; 35-Spray tower non-condensable oil and gas outlet; 36-First condenser oil outlet; 37-First condenser air inlet; 38-First condenser; 39-First condenser air outlet; 40-Second condenser air inlet; 41-Second condenser; 42-Second condenser air outlet; 43-Second condenser oil outlet; 44-Second induced draft fan; 45-Fuel inlet; 46-Burner; 47-First heating port; 48-Rotary kiln flue gas outlet; 49-Oxygen supply outlet; 50-Second heat exchanger; 51-Second heat exchanger flue gas outlet; 52-Oxygen supply inlet; 53-Blower; 54-Hopper; 55-Second discharge airlock; 56-Internal components; 57-Lifting plate; 58-Inner protrusion; 59-Outer protrusion. Detailed Implementation

[0049] The present invention will be further described below with reference to the accompanying drawings and embodiments. The same reference numerals in the drawings denote components with the same or similar functions. Although various aspects of the embodiments are shown in the drawings, they are not necessarily drawn to scale unless specifically indicated otherwise.

[0050] In the description of this invention, it should be understood that the terms "center," "longitudinal," "lateral," "length," "width," "thickness," "upper," "lower," "front," "rear," "left," "right," "vertical," "horizontal," "top," "bottom," "inner," "outer," "clockwise," "counterclockwise," "axial," "radial," and "circumferential" indicate the orientation or position and dimensional relationship based on the orientation or position relationship shown in the accompanying drawings. They are only for the convenience of description and do not indicate or imply that the device or component referred to must have a specific orientation, or be constructed and operated in a specific orientation. Therefore, they should not be construed as limitations on this invention.

[0051] The terms "approximately" and "around" when describing numerical ranges typically indicate an allowable error within ±2%. The term "many" when indicating quantity usually refers to three or more; for example, "multiple" usually means three or more. The expression "mainly composed of or constitutes" can also include structural components not mentioned in the sentence. The term "transmission connection" refers to the connection method used to transmit power or motion in a mechanical system, such as direct connection or connection through couplings, reducers, gear assemblies, worm gear assemblies, etc. The term "rotatably set or connected" refers to the connection method between two parts, allowing one part to rotate relative to the other; this connection method usually uses mechanical components such as bearings, bushings, and shaft-hole fits. The term "and / or" merely describes the relationship between related objects, indicating that three relationships can exist, for example: A and / or B, which can represent: A alone, A and B simultaneously, or B alone. Diesel fractions below diesel do not include diesel fuel. Furthermore, the terms "first" and "second" are used for descriptive purposes only and should not be construed as indicating or implying relative importance.

[0052] like Figure 1 As shown, the self-heating biomass pyrolysis-gasification combined production system includes a pyrolysis unit, a gasification unit, and a pyrolysis oil collection unit.

[0053] The pyrolysis unit includes a rotary kiln reactor 6 having a first feed inlet, a first heating inlet 47, a rotary kiln flue gas outlet 48, a rotary kiln reaction chamber, a pyrolysis carbon outlet 8, and a pyrolysis oil and gas outlet 29; a first feeding mechanism connected to the first feed inlet; and an external heat source connected to the first heating inlet 47. The first feeding mechanism is used to transport materials into the rotary kiln reaction chamber, and it can be a screw conveyor, a pneumatic conveyor, or other types.

[0054] The gasification unit includes a gasifier reactor 20, which has a second feed port connected to the pyrolytic char outlet 8, a second heating port 19 connected to an external heat source, a gasifier flue gas outlet 25, a gasifier reaction chamber, a biochar outlet 18, and a gasification gas outlet 26.

[0055] The pyrolysis oil collection unit has a pyrolysis oil and gas inlet connected to the pyrolysis oil and gas outlet 29, as well as a bio-oil outlet and a non-condensable gas outlet;

[0056] The external heat source is burner 46, which is a device that sprays out fuel and combustion-supporting gas in a certain manner for mixed combustion. Burner 46 has a fuel inlet 45, which is connected to gasification gas outlet 26 and non-condensable gas outlet respectively, to receive gasification gas and non-condensable gas as fuel. In this way, the gasification gas produced by pyrolysis carbon gasification and the non-condensable gas in pyrolysis oil and gas can be used as fuel for burner 46 to power rotary kiln reactor 6 and gasification furnace reactor 20, which not only treats the reaction tail gas, but also achieves the purpose of system self-heating and energy consumption reduction.

[0057] The gasifier reaction chamber is equipped with a material guiding mechanism and a driving mechanism. The material guiding mechanism includes two rows of material guiding plates, each row of which includes at least two material guiding plates 21. The material guiding plates 21 are inclined downwards and their upper ends are hinged to the chamber wall of the gasifier reaction chamber. The material guiding plates 21 in the two rows of material guiding plates are staggered in the height direction of the gasifier reaction chamber and are all connected to the driving mechanism. The driving mechanism can drive the material guiding plates 21 to swing up and down around their upper hinged parts and always maintain an inclined downward state. The driving mechanism can be of various types, such as: electric push rod, pneumatic push rod and other telescopic mechanisms, reciprocating traction mechanisms, and crank rocker mechanisms.

[0058] This system fully pyrolyzes biomass through a rotary kiln reactor 6 to obtain high-yield pyrolysis oil and gas and pyrolysis char. The pyrolysis char is then gasified through a gasifier reactor 20 to obtain high-quality biochar. Simultaneously, the gasification gas and non-condensable gases generated during the pyrolysis-gasification coupling process are used as fuel, enabling the system to provide its own heat. This achieves full-scale, high-value utilization of biomass and further improves the economic benefits of biomass pyrolysis. By tilting multiple guide plates 21 downwards and arranging them in an alternating pattern, a wave-shaped reaction channel is formed in the gasifier reaction chamber. This extends the residence time of the pyrolytic carbon in the gasifier reaction chamber, allowing it more time to absorb heat and react, thus prolonging the effective reaction time. Simultaneously, the drive mechanism can drive the guide plates 21 to swing up and down around their upper hinged parts. On the one hand, the swing amplitude of the guide plates 21 can be controlled by the drive mechanism to control the speed of the pyrolytic carbon flow, thereby controlling the residence time of the pyrolytic carbon gasification. On the other hand, the swinging guide plates 21 can disperse the pyrolytic carbon, preventing it from clumping and promoting a rapid and complete reaction between the pyrolytic carbon and the gasifying agent, thus increasing the reaction rate. Furthermore, the swinging guide plates 21 can shake off the pyrolytic carbon adhering to their surface, preventing material accumulation from affecting the gasification reaction.

[0059] For example Figure 1 As shown, in some embodiments, the first feeding mechanism includes a first screw conveyor 2 equipped with a first feeding motor 1, and a hopper 54 connected to the feed inlet of the first screw conveyor 2 via a second discharge airlock 55. The first feeding motor 1 is the driving component of the first screw conveyor 2, used to drive the first screw conveyor 2 to transport materials into the rotary kiln reaction chamber. The hopper 54 is used to store materials to be pyrolyzed; the second discharge airlock 55 is used to control the discharge from the hopper 54 and to maintain the isolation of the internal and external pressure and atmosphere environments of the system while continuously discharging materials.

[0060] Specifically, for example Figure 1 As shown, the rotary kiln reaction chamber is the inner cavity of the rotary kiln reactor 6. The first feed inlet is connected to the front end of the rotary kiln reaction chamber, the pyrolysis carbon outlet 8 is connected to the lower rear end of the rotary kiln reaction chamber, and the pyrolysis oil and gas outlet 29 is connected to the rear end of the rotary kiln reaction chamber. The rotary kiln reaction chamber is equipped with a rotary kiln heating chamber 5 inside the cavity wall. The rotary kiln heating chamber 5 is used to provide residence space for the heat source medium to indirectly heat the material in the rotary kiln reaction chamber. The rotary kiln heating chamber 5 is usually annular and coaxial with the rotary kiln reaction chamber. The first heating port 47 is connected to the rear end of the rotary kiln heating chamber 5, and the rotary kiln flue gas outlet 48 is connected to the front end of the rotary kiln heating chamber 5.

[0061] For example Figure 1As shown, in some embodiments, the rotary kiln reactor 6 is rotatably mounted via a first support roller 4 and a second support roller 7, and is connected to the rotary kiln drive device via a transmission gear 3 mounted thereon. Typically, there are two first support rollers 4 and two second support rollers 7, arranged in a rectangular array to support the rotary kiln reactor 6. Driven by the rotary kiln drive device, the rotary kiln reactor 6 can rotate. The rotary kiln drive device is typically a rotary kiln drive motor or a rotary kiln drive motor and its accessories.

[0062] Combination Figure 1 and Figure 2 As shown, in some embodiments, the rotary kiln reaction chamber is provided with a cylindrical inner component 56, and the inner wall of the inner component 56 is provided with a lifting structure; the lifting structure includes at least three rows of lifting plate groups distributed circumferentially along the inner component 56, each lifting plate group includes at least two lifting plates 57 distributed axially along the inner component 56, and the lifting plates 57 in any two adjacent lifting plate groups are staggered. The lifting plates 57 can rotate with the rotary kiln reactor 6 to scatter the material in the rotary kiln reaction chamber. On the one hand, this increases the heating area of ​​the material, making the material heat evenly and improving the heat and mass transfer effect. On the other hand, the lifting plates 57 lift the material and then scatter it, reducing material agglomeration during pyrolysis and further improving pyrolysis efficiency. Furthermore, the staggered distribution of the lifting plates 57 in two adjacent lifting plate groups allows the material in all parts of the rotary kiln reaction chamber to be lifted and scattered in a wave-like manner, avoiding localized material accumulation and ensuring the continuity and uniformity of material tumbling. This method is suitable for the pyrolysis of most biomass, especially for the pyrolysis of blocky materials such as bamboo waste.

[0063] For example Figure 2 As shown, in some embodiments, the front side of the lifting plate 57 is provided with inner protrusions 58, which are usually multiple and evenly distributed on the front side of the lifting plate 57; the back side of the lifting plate 57 is provided with outer protrusions 59, which are usually multiple and evenly distributed on the back side of the lifting plate 57. The front side of the lifting plate 57 generally refers to the inner side of the lifting plate 57 used for lifting materials, and the other side of the lifting plate 57 is its back side. The inner protrusions 58 can prevent materials from being piled up and thus prevent them from being thrown out; at the same time, they can increase the heating area between the materials and the lifting plate 57. The outer protrusions 59 can break up the thrown materials, effectively preventing material pile-up and enhancing the uniform heating of blocky materials. The inner protrusions 58 and outer protrusions 59 can have various structures, preferably a semi-ellipsoidal protrusion structure.

[0064] For example Figure 2 As shown, in some embodiments, one end of the lifting plate 57 is connected to the inner wall of the inner component 56, and the other end is provided with a lifting hook that bends to one side. The bending direction of the lifting hook is the same as the rotation direction of the rotary kiln reactor 6, so as to lift the material more effectively.

[0065] In some embodiments, the length of the lifting plate 57 along the radial direction of the rotary kiln reactor 6 is 1 / 10 to 1 / 5 of the radius of the rotary kiln reactor 6, so that the lifting plate 57 can throw the material to a better height, ensuring that the material is thrown into a curtain shape, effectively increasing its heating area and optimizing heat and mass transfer.

[0066] Specifically, for example Figure 1 As shown, the gasifier reaction chamber is the inner cavity of the gasifier reactor 20. The second feed inlet is connected to the upper part of the gasifier reaction chamber, the biochar outlet 18 is connected to the bottom of the gasifier reaction chamber, and the gasification gas outlet 26 is connected to the top of the gasifier reaction chamber. A gasifier heating chamber 22 is provided inside the cavity wall of the gasifier reaction chamber. The gasifier heating chamber 22 is used to provide residence space for the heat source medium to indirectly heat the material in the gasifier reaction chamber. The gasifier heating chamber 22 is usually annular and coaxial with the gasifier reaction chamber. The second heating port 19 is connected to the lower part of the gasifier heating chamber 22, and the gasifier flue gas outlet 25 is connected to the upper part of the gasifier heating chamber 22. The gasifier reactor 20 is heated by both internal and external heating. The heat source medium is sent into the gasifier heating chamber 22 through the second heating port 19 to achieve external heating of the gasifier reactor 20. At the same time, some of the pyrolytic carbon entering the gasifier reaction chamber will react with oxygen to release heat, thus achieving internal heating of the gasifier reactor 20.

[0067] For example Figure 1 As shown, in some embodiments, the gasification unit further includes a charcoal tank 17, which is connected to a biochar outlet 18. The biochar generated after the pyrolysis char undergoes a gasification reaction can be collected in the charcoal tank 17 through the biochar outlet 18.

[0068] For example Figure 1As shown, in some embodiments, the second feed inlet is connected to the pyrolysis char outlet 8 via a second feeding mechanism; the second feeding mechanism includes a second screw conveyor 27 with a second feeding motor 28; the drive mechanism includes a crank disposed at the upper part of the gasifier reaction chamber and driven by the second feeding motor 28, and a positioning shaft 23 disposed along the height direction of the gasifier reaction chamber and movably connected to each guide plate 21; the positioning shaft 23 is driven by the drive end of the crank. The swing amplitude of the guide plate 21 is determined by the distance between the rotation axis of the crank and its drive end, and can be selected according to actual needs and gasification effect. The aforementioned drive mechanism is a crank-connecting rod mechanism mainly composed of a crank and a positioning shaft 23. It can simultaneously drive multiple guide plates 21 to swing. It is not only simple in structure, low in cost, and easy to maintain, but also connected to the second feed motor 28. It can flexibly adjust the flow rate and residence time of pyrolytic carbon in the gasifier reaction chamber. It can also work synchronously with the second screw conveyor 27 and adaptively adjust the swing frequency of the guide plates 21 according to the feeding speed of the second screw conveyor 27. This greatly improves the economy and practicality of the swing control of the guide plates 21 and helps to ensure the effect of pyrolytic carbon gasification.

[0069] For example Figure 1 As shown, in some embodiments, the feed inlet of the second screw conveyor 27 is connected to the pyrolytic carbon outlet 8 via the first feed air lock 9; the outlet of the second screw conveyor 27 is connected to the second feed inlet. The pyrolytic carbon generated after pyrolysis in the rotary kiln reactor 6 can enter the second screw conveyor 27 through the pyrolytic carbon outlet 8, and the second screw conveyor 27 feeds the pyrolytic carbon into the gasifier reaction chamber for gasification. The first feed air lock 9 controls the discharge of pyrolytic carbon and prevents gas from flowing from the gasifier reactor 20 into the rotary kiln reactor 6 when no material is being discharged.

[0070] To further improve the activation rate of pyrolytic carbon, in some embodiments, the feed plate 21 is provided with a reaction enhancement structure. The reaction enhancement structure can be of various types, such as multiple dispersing teeth 24 provided on the upper side of the feed plate 21. The dispersing teeth 24 are usually in the form of blocks or strips. When they are in the form of blocks, the multiple dispersing teeth 24 are evenly distributed on the upper side of the feed plate 21. When they are in the form of strips, the dispersing teeth 24 are arranged along the width direction of the feed plate 21. Another example is that the reaction enhancement structure is multiple aeration holes provided on the feed plate 21.

[0071] Preferred, combined Figure 1 and Figure 3As shown, based on the previous embodiment, the upper side of the guide plate 21 is provided with dispersing teeth 24, at least three of which are arranged sequentially along the inclined direction of the guide plate 21. This increases the contact area between the pyrolytic carbon and the gasifying agent, improving heat transfer and reaction efficiency. Furthermore, when the guide plate 21 swings up and down, the dispersing teeth 24 further disperse the pyrolytic carbon, effectively promoting the gasification reaction between the pyrolytic carbon and the gasifying agent, and improving activation efficiency.

[0072] For example Figure 1 As shown, in some embodiments, the pyrolysis oil collection unit includes a spray tower 31, a heavy oil collection tank 33, a first condenser 38, a second condenser 41, and a light oil collection tank 34.

[0073] The spray tower 31 has a spray tower inlet 30 as the inlet for pyrolysis oil and gas, a spray tower condensate oil outlet 32, and a spray tower non-condensable oil and gas outlet 35. The spray tower 31 is usually a circulating spray type spray tower 31, and the spray liquid is heavy oil condensed from the pyrolysis oil and gas. The pyrolysis oil and gas generated by the rotary kiln reactor 6 in the pyrolysis of the material can flow out through the pyrolysis oil and gas outlet 29 and enter the spray tower 31 through the spray tower inlet 30.

[0074] The heavy oil collection tank 33 is connected to the condensate outlet 32 ​​of the spray tower and is used to collect the part of the pyrolysis oil gas that is condensed down by the spray tower 31, i.e., heavy oil.

[0075] The first condenser 38 has a first condenser inlet 37 connected to the non-condensable oil and gas outlet 35 of the spray tower, as well as a first condenser oil outlet 36 and a first condenser outlet 39. The pyrolysis oil and gas that are not condensed by the spray tower 31 can flow out from the non-condensable oil and gas outlet 35 of the spray tower and enter the first condenser 38 through the first condenser inlet 37. After being condensed in the first condenser 38, light oil is obtained. The light oil can enter the light oil collection tank 34 through the first condenser outlet 36 and be collected.

[0076] The second condenser 41 has a second condenser inlet 40 connected to the first condenser outlet 39, a second condenser outlet 42, and a second condenser oil outlet 43; the pyrolysis oil gas that is not condensed by the first condenser 38 can flow out from the first condenser outlet 39 and enter the second condenser 41 through the second condenser inlet 40, and be condensed in the second condenser 41 to obtain light oil, which can be collected in the light oil collection tank 34 through the second condenser oil outlet 43;

[0077] The light oil collection tank 34 is connected to the oil outlet 36 of the first condenser and the oil outlet 43 of the second condenser, respectively, and is used to collect the portion of the pyrolysis oil gas that is condensed down through the oil outlet 36 of the first condenser and the oil outlet 43 of the second condenser, which is the light oil.

[0078] The spray tower condensate oil outlet 32, the first condensate tank oil outlet 36, and the second condensate tank oil outlet 43 are all bio-oil outlets, and the second condensate tank gas outlet 42 is a non-condensable gas outlet.

[0079] This pyrolysis oil collection unit can achieve three-stage condensation of pyrolysis oil and gas. The condensation process is as follows:

[0080] First-stage condensation: Pyrolysis oil and gas outlet 29 → Spray tower 31 → Heavy oil and first-stage uncondensed oil and gas

[0081] Heavy oil → Self-circulation within spray tower 31 → Heavy oil collection tank 33;

[0082] Second-stage condensation: First-stage uncondensed oil and gas → First condenser tank 38 → Light oil and second-stage uncondensed oil and gas

[0083] Light oil → Light oil collection tank 34;

[0084] Third-stage condensation: Second-stage non-condensable oil and gas → Second condenser 41 → Light oil and non-condensable gas

[0085] Light oil → Light oil collection tank 34

[0086] Non-condensable gas → Second condenser outlet 42 → Burner 46.

[0087] For example Figure 1 As shown, in some embodiments, the non-condensable gas outlet is connected to the fuel inlet 45 via a second induced draft fan 44. The second induced draft fan 44 can extract gas, which on the one hand can adjust the pressure inside the rotary kiln reactor 6 to a negative pressure to reduce the residence time of pyrolysis oil and gas in the rotary kiln reaction chamber and improve the pyrolysis oil yield; on the other hand, the non-condensable gas in the pyrolysis oil and gas can be used as fuel to reduce energy consumption and lay the foundation for the efficient conversion of biomass into bio-oil and biochar.

[0088] For example Figure 1 As shown, in some embodiments, the system further includes a heat exchange unit, which includes a first heat exchanger 10 and a second heat exchanger 50.

[0089] The gasifier reactor 20 also has a gasifying agent addition port connected to the lower part of the gasifier reaction chamber; the first heat exchanger 10 has a gasifying agent inlet 11, a gasifying agent outlet 12 connected to the gasifying agent addition port, a first heat exchanger flue gas inlet connected to the rotary kiln flue gas outlet 48 and / or the gasifier flue gas outlet 25, and a first heat exchanger flue gas outlet; the high-temperature flue gas discharged from the rotary kiln flue gas outlet 48 and / or the gasifier flue gas outlet 25 can enter the first heat exchanger 10 through the first heat exchanger flue gas inlet and exchange heat with the gasifying agent entering the first heat exchanger 10 through the gasifying agent inlet 11, realizing the waste heat recovery of the high-temperature flue gas; the heated gasifying agent flows out from the gasifying agent outlet 12 and enters the gasifier reaction chamber through the gasifying agent addition port to react with the pyrolytic carbon in a gasification reaction, which can further reduce the energy consumption of the gasifier reactor 20; the gasifying agent is usually air, H2O, etc.

[0090] The second heat exchanger 50 has an oxygen inlet 52, an oxygen outlet 49 connected to the fuel inlet 45, a second heat exchanger flue gas inlet connected to the rotary kiln flue gas outlet 48 and / or the gasifier flue gas outlet 25, and a second heat exchanger flue gas outlet 51. The high-temperature flue gas discharged from the rotary kiln flue gas outlet 48 and / or the gasifier flue gas outlet 25 can also enter the second heat exchanger 50 through the second heat exchanger flue gas inlet and exchange heat with the oxygen, air and other combustion-supporting gases that enter the second heat exchanger 50 through the oxygen inlet 52, thereby realizing the waste heat recovery of the high-temperature flue gas. The heated combustion-supporting gases flow out from the oxygen outlet 49 and enter the burner 46 through the fuel inlet 45 to mix with the fuel and assist combustion.

[0091] For example Figure 1 As shown, in some embodiments, the heat exchange unit further includes a flue gas processor 14, a first induced draft fan 16, and a blower 53; the flue gas processor 14 has a flue gas processor inlet 13 connected to the flue gas outlet of the first heat exchanger, and a flue gas processor outlet 15; the first induced draft fan 16 is connected to the flue gas processor outlet 15; the blower 53 is connected to an oxygen supply inlet 52, used to blow oxygen, air, and other combustion-supporting gases into the second heat exchanger 50. After the high-temperature flue gas is cooled by heat exchange in the first heat exchanger 10, it becomes low-temperature flue gas. The low-temperature flue gas can enter the flue gas processor 14 through the flue gas processor inlet 13. After treatment, the low-temperature flue gas becomes clean gas and flows out through the flue gas processor outlet 15, and is then discharged by the first induced draft fan 16.

[0092] Within this system, the flow paths of the fuel gas and flue gas are as follows:

[0093] 1) Combustion heating: Combustion gas + fuel (non-condensable gas + gasified gas) → burner 46 → high-temperature flue gas (heat source medium);

[0094] 2) A portion of the high-temperature flue gas → rotary kiln heating chamber 5 → first heat exchanger 10 and / or second heat exchanger 50 → low-temperature flue gas.

[0095] Another portion of the high-temperature flue gas → gasifier heating chamber 22 → first heat exchanger 10 and / or second heat exchanger 50 → low-temperature flue gas;

[0096] 3) Low-temperature flue gas → flue gas processor 14 → first induced draft fan 16 → exhaust.

[0097] This invention also provides a self-heating biomass pyrolysis-gasification polygeneration method, using biomass particles with a particle size of 2-30 mm as raw materials, and employing the above-mentioned self-heating biomass pyrolysis-gasification polygeneration system to prepare bio-oil and biochar; during the preparation process, the rotation speed of the rotary kiln reactor 6 is 1-2 r / min, the pyrolysis temperature is 550-600℃, the pyrolysis time is 35-45 min, the gasification temperature is 800-900℃, and the gasification time is 55-65 min.

[0098] Example 1

[0099] This embodiment uses bamboo waste with a particle size of 10-30 mm as raw material and applies the self-heating biomass pyrolysis-gasification polygeneration system and method provided by this invention to conduct experiments on the preparation of high-yield bio-oil and high-quality biochar. The specific process is as follows:

[0100] S1. Start burner 46. Initially, natural gas is used as fuel. After the system is running stably, the fuel is switched to gasified gas produced by pyrolysis carbon gasification and non-condensable gas in pyrolysis oil and gas.

[0101] S2. Control the flow rate of high-temperature flue gas through the first heating port 47. When the temperature of the rotary kiln heating chamber 5 reaches 550℃ (pyrolysis temperature), feed the raw material with a moisture content of about 10% into the rotary kiln reaction chamber through the first feeding mechanism.

[0102] S3. Control the rotation speed of the rotary kiln reactor 6 to 1 r / min to ensure that the residence time of the raw material in the rotary kiln reaction chamber is 40 min;

[0103] S4. The pyrolysis oil and gas produced by pyrolysis are condensed by spray tower 31, first condenser 38 and second condenser 41 to obtain bio-oil; heavy oil is used as the circulating spray liquid in spray tower 31 at a temperature of 50℃.

[0104] S5. The pyrolytic carbon produced by pyrolysis is fed into the gasifier reaction chamber through the second feeding mechanism; at the same time, the water vapor used as the gasification agent is preheated to about 200°C by the first heat exchanger 10 and then introduced into the gasifier reaction chamber through the gasification agent addition port, and the temperature of the gasifier reaction chamber is controlled at 800°C (gasification temperature) and the gasification reaction time is 60 min.

[0105] S6. The pyrolytic carbon entering the gasifier reactor 20 is shaken by the guide plate 21, and the dispersing teeth 24 on it disperse the pyrolytic carbon particles and fully gasify them to obtain biochar. The biochar is discharged into the carbon tank 17 through the biochar outlet 18.

[0106] Results: The bio-oil yield in this embodiment was 35.42 wt%, and the specific surface area of ​​biochar was 680 m². 2 / g.

[0107] Example 2

[0108] This embodiment uses bamboo waste with a particle size of 10-30 mm as raw material and applies the self-heating biomass pyrolysis-gasification polygeneration system and method provided by the present invention to conduct experiments on the preparation of high-yield bio-oil and high-quality biochar. The specific process is as in Example 1, except that the gasification temperature is controlled at 900℃.

[0109] Results: The bio-oil yield in this embodiment was 36.28 wt%, and the specific surface area of ​​biochar was 750 m². 2 / g.

[0110] Example 3

[0111] This embodiment uses bamboo waste with a particle size of 10-30 mm as raw material. The self-heating biomass pyrolysis-gasification polygeneration system and method provided by this invention are used to conduct experiments on the preparation of high-yield bio-oil and high-quality biochar. The specific process is the same as in Example 1, except that the pyrolysis temperature is controlled at 600℃, the gasification temperature is controlled at 900℃, and the gasification agent is 20% air + 80% water vapor.

[0112] Results: The bio-oil yield in this embodiment was 33.18 wt%, and the specific surface area of ​​biochar was 713 m². 2 / g.

[0113] Example 4

[0114] This embodiment uses bamboo chips with a particle size of 2-5 mm as raw material and applies the self-heating biomass pyrolysis-gasification polygeneration system and method provided by the present invention to conduct experiments on the preparation of high-yield bio-oil and high-quality biochar. The specific process is as in Example 1, except that the gasification temperature is controlled at 900℃.

[0115] Results: The bio-oil yield in this embodiment was 38.08 wt%, and the specific surface area of ​​biochar was 778 m². 2 / g.

[0116] The process parameters and results comparison of Examples 1-4 are detailed in Table 1.

[0117] Table 1: Comparison of process parameters and results for Examples 1-4

[0118]

[0119] The above embodiments and Table 1 verify the technical advantages of the self-heating biomass pyrolysis-gasification polygeneration system and method provided by the present invention, as detailed below:

[0120] (1) Increased bio-oil yield: In the core part of the pyrolysis unit, a densely staggered lifting plate 57 is innovatively arranged, which allows the raw material to be repeatedly lifted and scattered during the rotation of the rotary kiln reactor 6, forming a uniform thin layer, which greatly increases the heating surface area and allows the raw material to be heated to the target pyrolysis temperature in a short time. The rapid and uniform heating environment effectively suppresses the residence time of pyrolysis volatiles in the high-temperature zone, and avoids the secondary decomposition of products into small molecule gases caused by excessive cracking to the greatest extent. After multiple batches of experiments, this method can stably increase the bio-oil yield to 33% to 38%, which is higher than the yield of existing pyrolysis technology (30%), and significantly improves the economic feasibility of bio-oil as a liquid fuel or chemical feedstock.

[0121] (2) High added value of biochar: The oscillating guide plate 21 in the gasifier reactor 20 is designed with dispersing teeth 24, which significantly improves the reaction efficiency of pyrolysis carbon; the specific surface area of ​​the obtained biochar can reach 680-778 m² / g, and it can be used in environmental protection and materials fields such as wastewater / waste gas adsorption and purification, soil heavy metal passivation and organic matter enhancement, and electrode material preparation, which has extremely high application value and market prospects.

[0122] (3) Energy consumption and cost optimization: The self-heating closed-loop system directly introduces the non-condensable gases (mainly containing CO, CH4, H2, etc.) generated during the pyrolysis process and some of the surplus gasified gas generated during gasification into the burner 46 for combustion. The high-temperature flue gas generated by combustion is used to heat the rotary kiln reactor 6 and provides the necessary preheating energy for the gasification unit. This design maximizes the recovery and utilization of combustible byproducts generated inside the system and significantly reduces dependence on external fossil fuels such as natural gas and fuel oil.

[0123] (4) High industrialization potential: This invention innovatively couples the two core units of pyrolysis and gasification. The pyrolysis unit efficiently converts biomass to obtain pyrolysis oil and gas and pyrolysis char; the gasification unit performs deep activation treatment on the pyrolysis char and produces fuel gas as a byproduct. It realizes the full-scale, high-value utilization of biomass components (such as bamboo waste), and produces high-yield bio-oil + high specific surface area activated biochar.

[0124] This document presents a description of various embodiments of the invention for illustrative purposes only and is not intended to be exhaustive or limited to the disclosed embodiments. Many modifications and variations will be apparent to those skilled in the art without departing from the scope and spirit of the described embodiments. The terminology used herein has been chosen to best explain the principles, practical applications, or technological advancements of the embodiments, or to enable others skilled in the art to understand the embodiments disclosed herein, compared to technologies found in the market.

[0125] In this document, various embodiments of the invention may be presented in the form of a scope. It should be understood that the scope description is merely for convenience and brevity and should not be construed as a hard limitation on the scope of the invention. Therefore, the scope description should be considered to specifically disclose all possible sub-scopes and individual numerical values ​​within that scope. For example, a description of a scope such as 1 to 6 should be considered to specifically disclose sub-scopes, such as 1 to 3, 1 to 4, 1 to 5, 2 to 4, 2 to 6, 3 to 6, etc., and individual numerical values ​​within that scope, such as 1, 2, 3, 4, 5, 6, regardless of the width of the scope.

[0126] It should be understood that, for clarity, certain features of the invention described in the context of a single embodiment may also be provided in combination in a single embodiment. Conversely, for brevity, various features of the invention described in the context of a single embodiment may also be provided individually or in any suitable sub-combination, or, where appropriate, in any other described embodiment of the invention. Unless the embodiment does not function without those features, certain features described in the context of various embodiments are not considered essential features of those embodiments.

Claims

1. A self-sustained biomass pyrolysis-gasification poly-generation system, characterized in that: The pyrolysis unit, the gasification unit and the pyrolysis oil collection unit are connected in series. The pyrolysis unit comprises a rotary kiln reactor (6) having a first feeding port, a first heat supply port (47), a rotary kiln flue gas outlet (48), a rotary kiln reaction cavity, a pyrolysis carbon discharge port (8) and a pyrolysis oil gas outlet (29), a first feeding mechanism connected with the first feeding port, and an external heat source connected with the first heat supply port (47). The gasification unit comprises a gasifier reactor (20) having a second feeding port connected with the pyrolysis carbon discharge port (8), a second heat supply port (19) connected with the external heat source, and a gasifier flue gas outlet (25), a gasifier reaction cavity, a biochar outlet (18) and a gasification gas outlet (26). The pyrolysis oil collection unit has a pyrolysis oil gas inlet connected with the pyrolysis oil gas outlet (29), a bio-oil outlet and a non-condensable gas outlet. The external heat source is a burner (46) having a fuel inlet (45) connected with the gasification gas outlet (26) and the non-condensable gas outlet respectively to receive the gasification gas and the non-condensable gas as fuel. The gasifier reaction cavity is provided with a material guiding mechanism and a driving mechanism; the material guiding mechanism comprises two sets of material guiding plates, each set of material guiding plates comprising at least two material guiding plates (21) arranged obliquely downward and hinged at the upper end to the cavity wall of the gasifier reaction cavity; the material guiding plates (21) in the two sets of material guiding plates are staggered in the height direction of the gasifier reaction cavity and are drivingly connected with the driving mechanism; the driving mechanism can drive the material guiding plates (21) to swing up and down about the hinged part at the upper end and always maintain an oblique downward state.

2. The self-heating biomass pyrolysis-gasification poly-generation system according to claim 1, wherein: The first feeding mechanism comprises a first screw conveyor (2) provided with a first feeding motor (1), and a material bin (54) connected with the feeding port of the first screw conveyor (2) through a second discharge gas lock (55). The first feeding port is in communication with the front end of the rotary kiln reaction cavity, the pyrolysis carbon discharge port (8) is in communication with the lower part of the rear end of the rotary kiln reaction cavity, and the pyrolysis oil gas outlet (29) is in communication with the rear end of the rotary kiln reaction cavity. The cavity wall of the rotary kiln reaction cavity is provided with a rotary kiln heating cavity (5), the first heat supply port (47) is in communication with the rear part of the rotary kiln heating cavity (5), and the rotary kiln flue gas outlet (48) is in communication with the front part of the rotary kiln heating cavity (5).

3. The self-heating biomass pyrolysis-gasification poly-generation system according to claim 1, wherein: The rotary kiln reaction cavity is provided with a cylindrical inner member (56), and the inner wall of the inner member (56) is provided with a material lifting structure; the material lifting structure comprises at least three rows of material lifting plate groups distributed along the circumference of the inner member (56), each material lifting plate group comprises at least two material lifting plates (57) distributed along the axial direction of the inner member (56), and the material lifting plates (57) in any two adjacent material lifting plate groups are distributed in a staggered manner.

4. The self-heating biomass pyrolysis-gasification poly-generation system according to claim 3, wherein: The front surface of the material lifting plate (57) is provided with an inner side protrusion (58), and the back surface of the material lifting plate (57) is provided with an outer side protrusion (59). And / or, one end of the material lifting plate (57) is connected with the inner wall of the inner member (56), and the other end is provided with a material lifting hook bent to one side, the bending direction of the material lifting hook is the same as the rotating direction of the rotary kiln reactor (6); along the radial direction of the rotary kiln reactor (6), the size length of the material lifting plate (57) is 1 / 10-1 / 5 of the radius of the rotary kiln reactor (6).

5. The self-heating biomass pyrolysis-gasification poly-generation system according to claim 1, wherein: The second feeding port is communicated with the upper part of the gasification furnace reaction cavity, the biochar outlet (18) is communicated with the bottom of the gasification furnace reaction cavity, and the gasification gas outlet (26) is communicated with the top of the gasification furnace reaction cavity. A gasification furnace heating cavity (22) is arranged in the cavity wall of the gasification furnace reaction cavity, the second heat supply port (19) is communicated with the lower part of the gasification furnace heating cavity (22), and the gasification furnace flue gas outlet (25) is communicated with the upper part of the gasification furnace heating cavity (22). The gasification unit further comprises a carbon tank (17), and the carbon tank (17) is connected with the biochar outlet (18).

6. The self-heating biomass pyrolysis-gasification poly-generation system according to claim 1, wherein: The second feeding port is connected with the pyrolysis carbon discharge port (8) through a second feeding mechanism; The second feeding mechanism comprises a second screw conveyor (27) provided with a second feeding motor (28); The driving mechanism comprises a crank arranged at the upper part of the gasification furnace reaction cavity and in transmission connection with the second feeding motor (28), and a positioning shaft (23) arranged along the height direction of the gasification furnace reaction cavity and in movable connection with each guide plate (21) respectively; the positioning shaft (23) is in transmission connection with the driving end of the crank. The upper side of the guide plate (21) is provided with scattering teeth (24), and the scattering teeth (24) are at least three and are arranged in sequence along the inclined direction of the guide plate (21).

7. The self-heating biomass pyrolysis-gasification poly-generation system according to claim 1, wherein: The pyrolysis oil collecting unit comprises a spray tower (31), a heavy oil collecting tank (33), a first condensing tank (38), a second condensing tank (41) and a light oil collecting tank (34); The spray tower (31) has a spray tower inlet (30) as a pyrolysis oil gas inlet, a spray tower condensing oil outlet (32) and a spray tower non-condensable oil gas outlet (35); The heavy oil collecting tank (33) is connected with the spray tower condensing oil outlet (32); The first condensing tank (38) has a first condensing tank gas inlet (37) connected with the spray tower non-condensable oil gas outlet (35), and a first condensing tank oil outlet (36) and a first condensing tank gas outlet (39); The second condensing tank (41) has a second condensing tank gas inlet (40) connected with the first condensing tank gas outlet (39), and a second condensing tank gas outlet (42) and a second condensing tank oil outlet (43); The light oil collecting tank (34) is connected with the first condensing tank oil outlet (36) and the second condensing tank oil outlet (43) respectively; The spray tower condensing oil outlet (32), the first condensing tank oil outlet (36) and the second condensing tank oil outlet (43) are all bio-oil outlets, and the second condensing tank gas outlet (42) is a non-condensable gas outlet, which is connected with a fuel inlet (45) through a second induced draft fan (44).

8. The self-heating biomass pyrolysis-gasification poly-generation system according to any one of claims 1 to 7, characterized in that: Further comprising a heat exchange unit, the heat exchange unit comprises a first heat exchanger (10) and a second heat exchanger (50); The gasifier reactor (20) also has a gasifier reaction cavity lower communicating gasifier adding port; the first heat exchanger (10) has a gasifier inlet (11), a gasifier outlet (12) connected with the gasifier adding port, a first heat exchanger flue gas inlet connected with the rotary kiln flue gas outlet (48) and / or the gasifier flue gas outlet (25), and a first heat exchanger flue gas outlet; The second heat exchanger (50) has an oxygen supply inlet (52), an oxygen supply outlet (49) connected with the fuel inlet (45), a second heat exchanger flue gas inlet connected with the rotary kiln flue gas outlet (48) and / or the gasifier flue gas outlet (25), and a second heat exchanger flue gas outlet (51).

9. The self-heating biomass pyrolysis-gasification poly-generation system according to claim 8, wherein: The heat exchange unit also includes a flue gas processor (14), a first air blower (16) and a blast fan (53); The flue gas processor (14) has a flue gas processor gas inlet (13) connected with the first heat exchanger flue gas outlet, and a flue gas processor gas outlet (15); The first air blower (16) is connected with the flue gas processor gas outlet (15); The blast fan (53) is connected with the oxygen supply inlet (52).

10. A self-sustained biomass pyrolysis-gasification poly-generation process, characterized in that: Biomass particles with a particle size of 2-30 mm are used as raw materials to prepare bio-oil and biochar by using the self-heat supply type biomass pyrolysis-gasification multi-production system according to any one of claims 1-9; During the preparation process, the rotary speed of the rotary kiln reactor (6) is 1-2 r / min, the pyrolysis temperature is 550-600℃, the pyrolysis time is 35-45 min, the gasification temperature is 800-900℃, and the gasification time is 55-65 min.

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