Energy-saving straw charcoal and coke mixed fuel preparation equipment

Abstract

The invention discloses energy-saving straw charcoal and coke mixed fuel preparation equipment which comprises a coke condensation reaction tank, a pyrolysis and carbonization reaction tank, a condensation mechanism, a nitrogen gas cylinder, a heating device and a waste heat insulation device, and the interior of the pyrolysis and carbonization reaction tank is divided into a semi-coking area and a coking area; the heating device is arranged to be capable of heating the coking zone to generate tar synthesis gas, and the waste heat insulation device is arranged to be capable of heating the semi-coking zone and is matched with the flow regulating valve to regulate the flow of the tar-containing synthesis gas, so that straw placed on a semi-coking bed layer is subjected to semi-coking, and the tar-containing synthesis gas is generated; according to the reactor designed by the invention, a single-section heating device is taken as a core heat source, and synchronous preparation of three products of charcoal, semi-coke straws and tar adsorption straws can be realized in the same reactor through graded temperature control of a coking zone, a semi-coking zone and a coke condensing tank; the problems of single product of traditional equipment and inconsistent quality caused by multi-equipment step-by-step processing are solved.

Description

TECHNICAL FIELD

[0001] The present application relates to the technical field of biomass pyrolysis equipment, in particular to an energy-saving straw charcoal and coke mixed fuel preparation equipment. BACKGROUND

[0002] Pyrolysis technology can convert biomass such as straw into high-value-added products such as biochar, tar, and synthesis gas, which can be used as high-calorie fuel. It is an important way to realize the resource utilization of agricultural waste, which can not only reduce environmental pollution caused by straw burning, but also replace fossil resources, and has good ecological and economic value.

[0003] If the biochar, tar and synthesis gas produced in the process of straw biomass pyrolysis are fully utilized, the economic efficiency can be improved and the environmental pollution can be reduced. The straw pyrolysis equipment plays a key role in the pyrolysis process, which can promote the efficient progress of the pyrolysis carbonization reaction and improve the yield and quality of biochar. However, in the prior art, a single reactor cannot simultaneously produce differentiated products, and the comprehensive utilization of biochar, tar and synthesis gas cannot be realized. Multiple equipment in series is often required for processing, which has a complex process and high energy consumption. Moreover, the tar, synthesis gas and waste heat generated by pyrolysis lack integrated recovery mechanisms, resulting in energy waste and the underutilization of the added value of by-products (waste heat, synthesis gas, etc.).

[0004] Therefore, there is an urgent need for a new energy-saving straw charcoal and coke mixed fuel preparation equipment to solve the above technical problems. SUMMARY

[0005] The present application aims to solve the above technical problems, i.e., to solve the problem that the existing straw pyrolysis equipment often requires multiple equipment in series for processing when producing multiple products, which is difficult to simultaneously produce differentiated products, has a complex process and high energy consumption, and the tar, synthesis gas and waste heat generated by pyrolysis lack integrated recovery mechanisms, resulting in energy waste and the underutilization of the added value of by-products.

[0006] To this end, the present invention provides an energy-saving straw-coke mixed fuel preparation device, comprising a coking reactor, a pyrolysis carbonization reactor, a condensation mechanism, a nitrogen cylinder, a heating device, and a waste heat preservation device. The pyrolysis carbonization reactor is internally divided into a semi-coking zone and a coking zone from top to bottom. A flow regulating valve is installed in the pyrolysis reactor between the semi-coking zone and the coking zone. Multiple coking beds for placing straw are installed in the coking zone. The heating device is configured to heat the coking zone to form coke and tar-containing syngas from the straw placed on the coking beds. The semi-coking zone contains semi-coking beds. The waste heat preservation device is configured to heat the semi-coking zone and, in conjunction with the flow regulating valve, regulate the flow rate of tar-containing syngas to semi-coke the straw placed in the semi-coking bed and generate tar-containing syngas. The coking reaction tank is located at the top of the pyrolysis carbonization reaction tank and is interconnected with it. The coking reaction tank contains multiple layers of coking beds arranged vertically. The condensing mechanism is configured to cool the tar-containing syngas in the coking reaction tank to liquefy the tar. The top of the coking reaction tank is provided with a syngas exhaust port, and the outlet of the nitrogen cylinder is connected to the bottom of the pyrolysis carbonization reaction tank.

[0007] In a specific embodiment of the above-mentioned energy-saving straw-coke mixed fuel preparation equipment, the bottom end of the coking reaction tank is provided with a tank inlet for connecting to the top of the pyrolysis carbonization reaction tank. The tank inlet is funnel-shaped. A porous gas distribution plate is fixed at the bottom of the coking reaction tank, and the coking bed is located above the porous gas distribution plate.

[0008] In a specific embodiment of the above-mentioned energy-saving straw-coke mixed fuel preparation equipment, the energy-saving straw-coke mixed fuel preparation equipment further includes a tar collection tank, a guide pipe, and a tar collection box. The tar collection tank is annular in shape and fixed on the inner peripheral wall of the coking reaction tank, and one end of the tar collection tank is in close contact with the inner side wall of the coking reaction tank. The tar collection box is fixed on the bottom outer wall of the coking reaction tank. The guide pipe passes through the coking reaction tank and one end of it is connected to the tar collection tank, and the other end is connected to the tar collection box.

[0009] In the specific embodiment of the above-mentioned energy-saving straw-coke mixed fuel preparation equipment, the semi-coking bed, coking bed and condensing bed have the same structure. The coking bed has a cylindrical structure. The top of the coking bed is provided with a groove for placing straw. The bottom of the coking bed is provided with multiple ventilation holes communicating with the inside of the groove. The bottom of the pyrolysis carbonization reaction tank is fixed with a material isolation plate. The material isolation plate is located below the coking bed and has multiple evenly distributed gas flow holes on it.

[0010] In a specific embodiment of the above-mentioned energy-saving straw-coke mixed fuel preparation equipment, the energy-saving straw-coke mixed fuel preparation equipment further includes a sealed box, a drawer-type compartment, and a sliding drive mechanism. The sealed box penetrates radially through the pyrolysis carbonization reactor corresponding to the semi-coking zone and divides it into an upper semi-coking zone and a lower semi-coking zone. A drawer-type compartment with an open top is placed inside the sealed box. Two sets of semi-coking bed layers arranged in parallel at intervals are arranged inside the drawer-type compartment. Each set of semi-coking bed layers includes at least two semi-coking bed layers arranged vertically. A flow port is provided on the bottom wall of the drawer-type compartment for the passage of syngas. The sliding drive mechanism is set on the sealed box and connected to the drawer-type compartment to drive the drawer-type compartment to perform reciprocating linear motion so that the two sets of semi-coking bed layers inside the drawer-type compartment are alternately aligned with the inside of the pyrolysis carbonization reactor, thereby connecting the upper semi-coking zone and the lower semi-coking zone.

[0011] In a specific embodiment of the above-mentioned energy-saving straw-coke mixed fuel preparation equipment, the energy-saving straw-coke mixed fuel preparation equipment further includes an air cylinder and a syngas storage tank. The air inlet of the syngas storage tank is connected to the syngas exhaust port to collect the syngas discharged from the coking reaction tank. The heating device includes a gas-fired heater and an electric heater. The air inlet of the gas-fired heater is connected to the air cylinder and the syngas storage tank. The gas-fired heater is located at the bottom of the pyrolysis carbonization reaction tank and can heat it. The electric heater is a resistance wire heater. The resistance wire of the resistance wire heater is embedded in the side wall of the pyrolysis carbonization reaction tank corresponding to the coking zone in a spiral winding manner.

[0012] In a specific embodiment of the above-mentioned energy-saving straw-coke mixed fuel preparation equipment, the waste heat insulation device includes a waste heat exchanger and a heating coil. The heating coil is embedded in the side wall of the pyrolysis carbonization reaction tank corresponding to the semi-coking zone in a spiral winding manner. The two ends of the heating coil are respectively connected to the fluid inlet and fluid outlet of the waste heat exchanger to form a closed fluid circulation. The waste heat inlet of the waste heat exchanger is connected to the exhaust gas outlet of the gas heating furnace to exchange heat with the fluid in the waste heat exchanger.

[0013] In a specific embodiment of the above-mentioned energy-saving straw-coke mixed fuel preparation equipment, the energy-saving straw-coke mixed fuel preparation equipment further includes a nitrogen recovery tank and a filtration and washing mechanism. The recovery inlet of the filtration and washing mechanism is connected to the waste heat exhaust port of the waste heat exchanger, and the recovery exhaust port of the filtration and washing mechanism is connected to the nitrogen recovery tank. The filtration and washing mechanism is configured to remove solid particles, impurities and miscellaneous gases from the waste gas.

[0014] In a specific embodiment of the above-mentioned energy-saving straw-coke mixed fuel preparation equipment, the top of the coking reactor is provided with a syngas discharge pipe. The side wall of the syngas discharge pipe has a hollow structure. The syngas discharge pipe is connected to the inside of the coking reactor, and the top of the syngas discharge pipe forms a syngas outlet. The condensation mechanism includes a condenser and a cooling coil. The cooling coil is embedded in the side wall, top wall, and inside the syngas discharge pipe of the coking reactor in a spiral winding manner. The cooling coil is located above the lowest coking bed in the coking reactor. The spiral spacing of the cooling coil located at the top of the coking reactor and inside the syngas discharge pipe is smaller than the spiral spacing of the cooling coil located inside the side wall of the coking reactor. The coolant outlet of the condenser is connected to one end of the cooling coil, and the coolant recovery port of the condenser is connected to the other end of the cooling coil.

[0015] In a specific embodiment of the above-mentioned energy-saving straw-coke mixed fuel preparation equipment, a tank support frame is fixed at the top of the sealed box, the tank support frame is fixedly connected to the coking reaction tank, the bottom of the coking reaction tank is provided with a tank air inlet, the top of the pyrolysis carbonization reaction tank is provided with a tank air outlet, the tank air inlet and the tank air outlet are connected and sealed by a sealing ring, a tank fixing frame is fixed on the outer wall of the pyrolysis carbonization reaction tank for support and fixation, and the gas heating furnace is fixed inside the tank fixing frame.

[0016] Compared with the prior art, the beneficial effects of the present invention are:

[0017] 1. The reactor designed in this invention adopts an integrated vertical structure, relying on a single-stage heating device as the core heat source. Through graded temperature control in the coking zone, semi-coking zone, and coking tank, a gradient temperature zone design is formed, thereby creating different generation conditions for different products. It can simultaneously prepare three products—biochar, semi-coke straw, and tar-adsorbed straw—within the same reactor. At the same time, it specifically addresses the pain points of traditional equipment, such as the difficulty in collecting tar and low added value. Specifically, by using the funnel-shaped air inlet of the coking tank to reduce the air velocity, the porous air distribution plate to even out the flow, and the gradient cooling design, the high-energy-density tar generated by pyrolysis is fully condensed and adheres to the surface of the straw. This avoids tar waste and allows the tar-adsorbed straw and semi-coke straw to directly form a high-calorific-value mixed fuel. It not only solves the problem of inconsistent quality caused by the single product and multi-stage processing of traditional equipment, but also further enhances the economic value of straw products. Moreover, each temperature zone can be independently controlled, flexibly adapting to the characteristics of different straw raw materials, and even other biomass, with strong raw material adaptability.

[0018] 2. The heat carried by the pyrolysis gas in the coking zone is directly used for heating the semi-coke zone. The tar is condensed and collected in the coking tank. After the syngas is collected, it is burned in a gas-fired heater to provide heat and works in conjunction with an electric heater to regulate the temperature of the coking zone for pyrolysis. Instead of relying solely on external heating energy, this method not only makes full use of the generated syngas, improving resource utilization, but also saves external heating energy and reduces overall production costs. The waste heat from the combustion of the gas-fired heater is recovered through a waste heat exchanger and used for auxiliary heating and insulation of the semi-coke zone. At the same time, the nitrogen in the purified waste gas can be recycled, significantly reducing dependence on external energy. This method enables energy cascade utilization and efficient recovery and utilization of by-products, solving the problems of waste heat loss, synthesis by-product and nitrogen waste in traditional equipment.

[0019] 3. The drawer-type chamber designed in this invention can reciprocate linearly along the sealed box. Two sets of semi-coking bed layers are set in the drawer-type chamber for placing straw. Driven by the sliding drive mechanism, the semi-coking bed layers can be replaced in a sealed state to achieve material replacement, so that the raw materials will not break the sealed environment in a continuous reaction state.

[0020] 4. The air inlet at the bottom of the coking reactor is designed as a funnel shape. After the tar synthesis gas enters the bottom of the coking reactor, the flow rate decreases, reducing the impact condensation phenomenon of large tar molecules at the air inlet. After entering, it passes through a porous gas distribution plate for forced gas distribution, which forces the airflow to be evenly distributed through the coking bed, ensuring that the tar synthesis gas has sufficient residence time for adhesion, improving the tar collection rate and reducing the difficulty of tar collection. Attached Figure Description

[0021] The preferred embodiments of the present invention are described below with reference to the accompanying drawings, in which:

[0022] Figure 1 This is a schematic diagram of the overall structure of the energy-saving straw-coke mixed fuel preparation equipment provided by the present invention;

[0023] Figure 2 yes Figure 1 Schematic diagram of the internal structure of the intermediate pyrolysis carbonization reactor;

[0024] Figure 3 yes Figure 1 Top view of the sealed box and drawer-type compartment;

[0025] Figure 4 yes Figure 1 Schematic diagram of the internal structure of the coking reactor and condensation mechanism;

[0026] Figure 5 yes Figure 4 Enlarged view of the structure of the medium tar collection tank and tar collection box installed on the coking reaction vessel;

[0027] Figure 6 yes Figure 1 Schematic diagram of the structure of a gas-fired heating furnace;

[0028] Figure 7 This is a schematic diagram of the waste heat exchanger and the gas filtration and washing mechanism in Path 1.

[0029] List of reference numerals in the attached diagram:

[0030] 1. Coking reactor; 101. Syngas outlet; 102. Syngas discharge pipe; 103. Sealing ring; 104. Cooling coil; 105. Tank inlet; 106. Coking bed; 107. Perforated gas distribution plate; 2. Operating door; 3. Tank support frame; 4. Tar collection box; 5. Syngas storage tank; 6. Pyrolysis carbonization reactor; 601. Coking bed; 602. Material isolation plate; 603. Semi-coking bed; 604. Tank outlet; 7. Sealed box; 8. Drawer-type compartment; 801. Handle; 9. Tank fixing frame; 10. Gas-fired heater; 1001. Exhaust gas outlet; 1002. Mixed gas combustion chamber; 1003. Gas mixing chamber; 1004. Syngas inlet port; 1005. Mixed gas flow valve; 1006. Air inlet port; 11. 12. Air cylinder; 13. Nitrogen cylinder; 14. Nitrogen recovery tank; 15. Filter and scrubbing mechanism; 16. Filter; 17. Scrubbing assembly; 18. Waste heat exchanger; 19. Fluid inlet; 10. Fluid outlet; 11. Flow pump; 12. Waste heat inlet; 13. Waste heat exhaust port; 14. Pallet; 15. Flow regulating valve; 16. Electric drawer slide rail; 17. Temperature sensor; 28. Condenser; 29. ​​Coolant storage tank; 20. Condensing coil; 20. First inlet pipe; 20. Coolant transfer pump; 21. Tar collection tank; 22. Guide pipe; 23. Insulation cotton; 24. Bed fixing frame; 25. Resistance wire; 26. Slide rail controller; 27. Heating coil; 28. Coking zone; 29. ​​Semi-coking zone. Detailed Implementation

[0031] To make the objectives, technical solutions, and advantages of this invention clearer, the technical solutions of this invention will be clearly and completely described below with reference to the accompanying drawings. Obviously, the described embodiments are only some, not all, of the embodiments of this invention. All other embodiments obtained by those skilled in the art based on the embodiments of this invention without creative effort are within the scope of protection of this invention.

[0032] In the description of this invention, it should be noted that the terms "upper," "lower," "inner," and "outer," etc., indicate the orientation or positional relationship based on the orientation or positional relationship shown in the accompanying drawings. They are used only for the convenience of describing the invention and for simplifying the description, and do not indicate or imply that the system 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 the invention. Furthermore, the terms "first," "second," etc., used to define components are merely for the convenience of distinguishing the aforementioned components. Unless otherwise stated, these terms have no special meaning and should not be construed as indicating or implying relative importance.

[0033] In the description of this invention, it should be noted that, unless otherwise explicitly specified and limited, the terms "installation," "setting," and "connection" should be interpreted broadly. For example, they can refer to a fixed connection, a detachable connection, or an integral connection; they can refer to a mechanical connection or an electrical connection; they can refer to a direct connection or an indirect connection through an intermediate medium; and they can refer to the internal connection of two components. Those skilled in the art can understand the specific meaning of the above terms in this invention based on the specific circumstances.

[0034] This invention relates to the field of biomass pyrolysis equipment technology, and in particular to an energy-saving straw-char-coke mixed fuel preparation device. The aim is to solve the problems of existing straw pyrolysis equipment, which often requires multiple devices to be processed in series when producing multiple products, making it difficult to simultaneously produce differentiated products, resulting in complex processes, high energy consumption, and a lack of integrated recovery mechanisms for tar, syngas, and waste heat generated during pyrolysis, leading to energy waste and underutilization of the added value of by-products. To this end, the present invention provides an energy-saving straw-coke mixed fuel preparation device, comprising a coking reactor, a pyrolysis-carbonization reactor, a condensation mechanism, a nitrogen cylinder, a heating device, and a waste heat preservation device. The pyrolysis-carbonization reactor is internally divided into a semi-coking zone and a coking zone from top to bottom. A flow regulating valve is installed in the pyrolysis reactor between the semi-coking zone and the coking zone. Multiple coking beds for placing straw are installed in the coking zone. The heating device is configured to heat the coking zone to form coke and tar-containing syngas from the straw placed on the coking beds. A semi-coking bed is installed in the semi-coking zone. The waste heat preservation device is configured to heat the semi-coking zone and, in conjunction with the flow regulating valve, regulate the flow rate of the tar-containing syngas to semi-coke the straw placed in the semi-coking bed and generate tar-containing syngas. The coking reactor is configured to... The reactor is designed with an integrated vertical structure, relying on a single-stage heating device as the core heat source. Through graded temperature control of the coking zone, semi-coking zone, and coking tank, different generation conditions are formed for the production of different products. It can simultaneously produce three products in the same reactor: biochar, semi-coke straw, and adsorbed tar straw. This solves the problem of inconsistent quality caused by single product and multi-stage processing in traditional equipment. Moreover, each temperature zone can be independently controlled, flexibly adapting to the characteristics of different straw raw materials, and even other biomass, with strong raw material adaptability.

[0035] The energy-saving straw-coke mixed fuel preparation equipment provided in the embodiments of the present invention will now be described in detail with reference to the accompanying drawings.

[0036] See Figures 1-2 and Figure 4This invention provides an energy-saving straw-coke mixed fuel preparation device, including a coking reactor 1, a pyrolysis-carbonization reactor 6, a condensation mechanism, a nitrogen cylinder 12, a heating device, and a waste heat preservation device. The interior of the pyrolysis-carbonization reactor 6 is divided into a semi-coking zone 29 and a coking zone 28 from top to bottom. A flow regulating valve 17 is installed in the pyrolysis reactor between the semi-coking zone 29 and the coking zone 28. Multiple coking beds 601 for placing straw are installed in the coking zone 28. The heating device is configured to heat the coking zone 28 so that the straw placed on the coking beds forms coke and tar-containing syngas. The semi-coking zone 29 is equipped with a semi-coking bed 603. The waste heat insulation device is configured to heat the semi-coking zone 29 and, in conjunction with the flow regulating valve 17, regulate the flow of tar-containing syngas so that the straw placed in the semi-coking bed 603 can be semi-coked and tar-containing syngas can be generated. The coking reaction tank 1 is located at the top of the pyrolysis carbonization reaction tank 6 and is connected to it. The coking reaction tank 1 is equipped with multiple layers of coking beds 106 arranged vertically. The condensing mechanism is configured to cool the tar-containing syngas in the coking reaction tank 1 so that the tar can be liquefied. The top of the coking reaction tank 1 is equipped with a syngas exhaust port.

[0037] Specifically, the coking zone 28 and the semi-coking zone 29 are divided by the installation position of the flow regulating valve 17. The semi-coking zone 29 is above the flow regulating valve 17, and the coking zone 28 is below the flow regulating valve 17. The flow regulating valve 17 controls the hot synthesis gas flow from the coking zone 28 by controlling the opening and closing angle. The semi-coking zone 29 uses the waste heat insulation device and the flow rate regulation of the hot synthesis gas from the coking zone 28 to adjust the heating and insulation effect, and controls the temperature at about 300°C, so that the straw biomass undergoes a semi-coking reaction and continues to produce syngas. The new syngas, carrying the hot synthesis gas from the coking zone 28 and the waste heat, enters the coking reaction tank 1 through the tank body connecting gas port.

[0038] More specifically, multiple bed fixing frames 24 arranged vertically are fixed on the inner wall of the pyrolysis carbonization reactor 6 corresponding to the coking zone 28 and the inner wall of the coking reactor 1. The coking bed 106 and the long coking bed are installed in the tank body through the corresponding bed fixing frames 24. A material isolation plate 602 is fixed at the bottom of the pyrolysis carbonization reactor 6 to isolate the material. The material isolation plate 602 is located below the coking bed 601 and has multiple evenly distributed gas flow holes.

[0039] Both the coking reactor 1 and the pyrolysis carbonization reactor 6 are cylindrical, with double walls and a cavity between them filled with insulating cotton 23. Temperature sensors 19 are installed inside the coking reactor 1, in the semi-coking zone 29, and in the coking zone 28. Display instruments corresponding to the temperature sensors 19 are installed on the outer walls of both reactors to display the temperature. Operating doors 2, which can be opened or closed, are installed on the side walls of the coking reactor 1, the pyrolysis carbonization reactor 6 corresponding to the coking zone 28, and the pyrolysis carbonization reactor 6 corresponding to the semi-coking zone 29. These doors allow for the addition of straw to the reactor bed and other operations such as maintenance.

[0040] In the above embodiments, preferably, see [reference needed]. Figure 1 The energy-saving straw-coke blended fuel preparation equipment also includes a nitrogen cylinder 12, the outlet of which is connected to the bottom of the pyrolysis carbonization reaction tank 6. Before the reaction, nitrogen cylinder 12 is opened to introduce nitrogen gas to purge air from the coking reaction tank 1 and the pyrolysis carbonization reaction tank 6, preventing oxidation. During the reaction, the introduced nitrogen gas can carry the tar synthesis gas produced in the coking zone 28 and the waste heat to the semi-coking zone 29.

[0041] In one embodiment, see Figures 1-3 The energy-saving straw-coke blended fuel preparation equipment also includes a sealed box 7, a drawer-type compartment 8, and a sliding drive mechanism. The sealed box 7 penetrates radially through the pyrolysis carbonization reactor 6 corresponding to the semi-coking zone 29 and divides it into an upper semi-coking zone 29 and a lower semi-coking zone 29. The sealed box 7 contains a drawer-type compartment 8 with an open top. The drawer-type compartment 8 contains two sets of semi-coking bed layers arranged in parallel at intervals. Each set of semi-coking bed layers includes at least two semi-coking bed layers 603 arranged vertically. The bottom wall of the drawer-type compartment 8 is provided with a flow port for passing syngas. The sliding drive mechanism is set on the sealed box 7 and connected to the drawer-type compartment 8 to drive the drawer-type compartment 8 to perform reciprocating linear motion so that the two semi-coking bed layers inside the drawer-type compartment 8 are alternately aligned with the inside of the pyrolysis carbonization reactor 6, so that the upper semi-coking zone 29 and the lower semi-coking zone 29 are connected.

[0042] Specifically, the pyrolysis carbonization reactor 6 corresponding to the upper coking zone 28 is fixed to the top of the sealed box 7 and communicates with the interior of the sealed box 7, while the pyrolysis carbonization reactor 6 corresponding to the lower coking zone 28 is fixed to the bottom of the sealed box 7 and communicates with the interior of the sealed box 7. The top wall of the semi-coking bed assembly is flush with the top wall of the drawer-type compartment 8, and insulation cotton 23 is filled between the semi-coking bed assembly and the surrounding inner wall of the drawer-type compartment 8. Two bed positioning frames are fixed inside the drawer-type compartment. Each bed positioning frame includes two clamping plates 16 arranged side by side along the drawer-type compartment's pull-out direction. A set of semi-coking bed assemblies is placed between the two clamping plates 16. The opposite sidewalls of the two clamping plates 16 are arc-shaped for the semi-coking bed assemblies to fit together, thus restricting the lateral and longitudinal positions of the semi-coking bed assemblies, allowing only vertical movement, and thus positioning the semi-coking bed assemblies. The height of the clamping plates is set according to the height of the semi-coking bed assembly.

[0043] Preferably, the drawer-type compartment 8 has an elongated oval shape, and the curvature of both ends of the drawer-type compartment is the same as the curvature of the tank wall of the pyrolysis carbonization reactor. This ensures that when one group of semi-coking beds is aligned with the pyrolysis carbonization reactor, the curved end of the drawer-type compartment adjacent to that semi-coking bed is aligned with the outer wall of the pyrolysis carbonization reactor. Figure 3 As shown. In addition, when a set of semi-coking bed layers of the drawer-type compartment is inserted into the pyrolysis carbonization reactor, the top and bottom walls of the drawer-type compartment fit into the pyrolysis carbonization reactor, thus supporting the drawer-type compartment.

[0044] The sealed box 7 has openings on both side walls, and each opening has a sealing door at its edge. The sealing door is used to seal or open the opening, and the drawer-type compartment 8 can be pulled out or pushed into the sealed box 7 from the opening. Pulling the drawer-type compartment 8 out from the opening can be used to place straw on the semi-coking bed 603 or to remove the semi-coking straw.

[0045] In the above embodiment, preferably, handles 801 are fixed on the side walls of both ends of the drawer-type compartment 8, and the sliding drive mechanism is an electric drawer slide rail 18. The electric drawer slide rail 18 is located on one side of the operating door 2 corresponding to the semi-coking zone 29, so as not to affect the opening and closing of the operating door 2. A slide rail controller 26 is installed on the outer side wall of the sealed box 7. The slide rail controller 26 is connected to the electric drawer slide rail 18. A button is installed on the slide rail controller 26 to control the movement of the electric drawer slide rail 18. The electric drawer slide rail 18 can automatically control the drawer-type compartment 8 to perform reciprocating linear movement so that one of the semi-coking bed groups corresponds to the pyrolysis carbonization reaction tank 6. At the same time, the drawer-type compartment 8 can also be manually pulled by the handles 801 to perform reciprocating linear movement.

[0046] It should be noted that the electric drawer slide 18 is a commercially available product, and its specific structure is common knowledge to those skilled in the art, so it will not be described in detail here.

[0047] In the above embodiment, the electric drawer slide rail 18 can drive the drawer-type compartment 8 to slide within the sealed box 7. When the straw in one of the semi-coking bed groups has finished coking or is about to be carbonized, the drawer-type compartment 8 is controlled to slide by controlling the slide rail controller 26, so that the other semi-coking bed group is aligned with the pyrolysis carbonization reactor to achieve the purpose of switching the other semi-coking bed 603 and proceeding to the next drawer-type compartment 8 for reaction. By switching, the straw in the semi-coking zone 29 can be replaced during the sealed reaction process, without having to frequently stop the reactor to replace the straw in the semi-coking bed 603. This ensures that the raw materials do not break the sealed environment 103 during continuous reaction, thus improving production efficiency.

[0048] See Figure 1 The top of the sealed box 7 is fixed with a tank support frame 3, which is fixedly connected to the coking reaction tank 1. The bottom of the coking reaction tank 1 is provided with a tank air inlet 105, and the top of the pyrolysis carbonization reaction tank 6 is provided with a tank air outlet 604. The tank air inlet 105 and the tank air outlet 604 are connected and sealed by a sealing ring 103. The outer wall of the pyrolysis carbonization reaction tank 6 is fixed with a tank fixing frame 9 for support and fixation.

[0049] In the above embodiments, preferably, see [reference needed]. Figure 2 and Figure 4 The air inlet 105 at the bottom of the coking reaction tank 1 is funnel-shaped. A porous air distribution plate 107 is fixed at the bottom of the coking reaction tank 1. The coking bed 106 is located above the porous air distribution plate 107. The semi-coking bed 603, the coking bed 601 and the coking bed 106 have the same structure. The coking bed 601 has a cylindrical structure. The top of the coking bed 601 is provided with a groove for placing straw. The bottom of the coking bed 601 is provided with multiple air holes that communicate with the inside of the groove.

[0050] The tar synthesis gas in the pyrolysis carbonization reactor 6 enters the coking reactor 1 through a funnel-shaped inlet. Forced gas distribution via the porous gas distribution plate 107 ensures the gas flow is evenly distributed across the coking bed 106, guaranteeing sufficient residence time for the tar synthesis gas to adhere. As the temperature decreases, the large tar molecules in the tar synthesis gas slowly condense into a liquid state and are adsorbed onto the straw raw material in the coking bed 106.

[0051] In the above embodiments, this application utilizes the funnel-shaped air inlet of the coking tank to reduce speed, the porous air distribution plate to even out flow, and the gradient cooling design to fully condense the high energy density tar generated by pyrolysis and attach it to the surface of the straw. This not only avoids tar waste, but also allows the straw that has absorbed tar and the semi-coke straw to directly form a high-calorific-value mixed fuel, specifically solving the pain points of difficult tar collection and low added value in traditional equipment.

[0052] In the above embodiments, preferably, see [reference needed]. Figures 1-2 and Figure 7 The energy-saving straw charcoal mixed fuel preparation equipment also includes an air cylinder 11 and a syngas storage tank 5. The air inlet of the syngas storage tank 5 is connected to the syngas exhaust port to collect the syngas discharged from the coking reaction tank 1. The heating device includes a gas heater 10 and an electric heater. The air inlet of the gas heater 10 is connected to the air cylinder 11 and the syngas storage tank 5. The gas heater 10 is set at the bottom of the pyrolysis carbonization reaction tank 6 and can heat it. The electric heater is a resistance wire 25 heater. The resistance wire 25 of the resistance wire 25 heater is embedded in the side wall of the pyrolysis carbonization reaction tank 6 corresponding to the coking zone 28 in a spiral winding manner, that is, embedded in the cavity between the double walls.

[0053] Specifically, the resistance wire 25 is wound around the outer wall of the inner wall of the pyrolysis carbonization reactor 6. The gas-fired heating furnace 10 is fixed inside the tank body fixing frame 9. The gas-fired combustion furnace is equipped with a mixed gas combustion chamber 1002 and a gas mixing chamber 1003. The bottom of the pyrolysis carbonization reactor 6 is inserted into the mixed gas combustion chamber 1002. The overall heating of the pyrolysis carbonization reactor 6 is achieved by heating the bottom. The mixed gas combustion chamber 1002 is equipped with a waste gas outlet 1001 for discharging combustion waste gas. The gas mixing chamber 1003 is located below the mixed gas combustion chamber 1002. The gas mixing chamber 1003 is equipped with an air input port 1006 for connecting to the air cylinder 11 and a syngas input port 1004 for connecting to the syngas storage tank 5. The air input port 1006 and the syngas input port 1004 are connected to a mixed gas flow valve 1005. The mixing ratio of air and syngas can be adjusted through the mixed gas flow valve 1005 to achieve the combustion requirements. After passing through the mixed gas flow valve 1005, the gas enters the gas mixing chamber 1003 for mixing. After mixing, the two gases enter the mixed gas combustion chamber 1002 for combustion and are supplied to the coking zone 28 for pyrolysis and carbonization reaction. The generated combustion exhaust gas, carrying waste heat and nitrogen, enters the waste heat exchanger 15 through the exhaust port and the inlet of the waste heat exchanger 15 described below for waste heat recovery and utilization.

[0054] At the start of production, the heating resistance wire 25 is turned on to heat the straw biomass in the coking bed 601 for pyrolysis. After normal operation (meaning after the set operating time, ensuring that syngas has been collected in the syngas storage tank 5), the gas-fired heater 10 is turned on for auxiliary heating. The temperature is monitored in real time by the temperature sensor 19, and the temperature of the heating resistance wire 25 is adjusted according to the temperature to control the pyrolysis temperature of the coking zone 28 within the set temperature range. The tar syngas produced by the pyrolysis and carbonization reaction of the straw biomass is guided by nitrogen, carrying residual heat, and enters the semi-coking zone 29 through the flow regulating valve 17.

[0055] The gas-fired furnace 10 burns the syngas collected in the syngas storage tank 5. During the pyrolysis process, the temperature of the coking zone 28 can be adjusted by the gas-fired furnace 10 and the electric heater to carry out the pyrolysis operation, instead of simply relying on external heating energy. This invention not only makes full use of the generated syngas and improves resource utilization, but also saves external heating energy and reduces overall production costs.

[0056] In the above embodiments, preferably, see [reference needed]. Figure 2 The waste heat insulation device includes a waste heat exchanger 15 and a heating coil 27. The heating coil 27 is embedded in the side wall of the pyrolysis carbonization reaction tank 6 corresponding to the semi-coking zone 29 in a spiral winding manner. The two ends of the heating coil 27 are respectively connected to the fluid inlet and fluid outlet 1502 of the waste heat exchanger 15 to form a closed fluid circulation. The waste heat inlet 1504 of the waste heat exchanger 15 is connected to the exhaust gas outlet of the gas-fired heating furnace 10 to exchange heat with the fluid in the waste heat exchanger 15.

[0057] Specifically, the heating coil 27 is wrapped around the outer wall of the inner wall of the pyrolysis carbonization reactor corresponding to the semi-coking zone 29, and the heating coil 27 is wrapped to the gas outlet of the tank near the top of the pyrolysis carbonization reaction tank 6. The outer wall of the pyrolysis carbonization reaction tank 6 is provided with a heat exchange inlet and a heat exchange outlet. One end of the heating tube is connected to the heat exchange inlet, and the other end of the heating tube is connected to the heat exchange outlet. The waste heat exchanger 15 has a fluid inlet 1501 and a fluid outlet 1502 at its top. The fluid inlet 1501 is connected to the heat exchange outlet through a pipeline, and the fluid outlet 1502 is connected to the heat exchange inlet through a pipeline. The waste heat exchanger 15 has a waste heat inlet 1504 and a waste heat outlet 1505 on its side wall. A fluid heat exchange tube is installed inside the waste heat exchanger 15. The two ends of the fluid heat exchange tube are connected to the fluid inlet and the fluid outlet 1502, respectively. A flow pump 1503 is installed on the fluid heat exchange tube to control the flow rate of the fluid in the fluid heat exchange tube. The exhaust gas generated by combustion enters the waste heat exchanger 15 through the waste heat inlet 1504 and exchanges heat with the fluid in the fluid heat exchange tube to realize the recycling of waste heat. The mixed gas of the exhaust gas and nitrogen after heat exchange flows into the filter and scrubbing mechanism 14 described below through the waste heat outlet 1505.

[0058] The tar syngas produced in coking zone 28 enters semi-coking zone 29 through flow regulating valve 17. The flow regulating valve 17 controls the gas flow rate into semi-coking zone 29 by adjusting its opening angle. After the straw biomass is laid in the semi-coking bed, the opening of flow regulating valve 17 is expanded from its minimum to its maximum, allowing the tar syngas to carry residual heat into semi-coking zone 29. The waste heat exchanger 15 is then activated, allowing the waste heat fluid to enter the heating coil 27 through the fluid outlet 1502 of the waste heat exchanger 15 to heat semi-coking zone 29. The tar syngas in coking zone 28, carrying residual heat, passes through the semi-coking bed, causing the straw within the bed to undergo a coking reaction. Temperature in the semi-coking zone 29 is monitored in real time by temperature sensor 19. The flow rate of the waste heat exchanger 15 is controlled by the flow pump 1503, and the opening angle of the flow regulating valve 17 is also controlled to regulate the temperature of the semi-coking zone 29, ensuring that the straw cokes but does not reach the carbonization temperature. When the straw coking is complete or about to carbonize, the electric drawer slide rail 18 moves the drawer-type compartment 8, switching the semi-coking bed layers within the drawer-type compartment 8 so that another semi-coking bed group is aligned with the pyrolysis carbonization reactor 6 for the next semi-coking bed layer 603 reaction. Waste heat fluid flows within the heating coil 27 and enters the fluid heat exchange tube from the fluid inlet of the waste heat exchanger 15 to achieve waste heat circulation. By controlling the opening of the waste heat exchanger 15 and the flow regulating valve 17 to reach the desired set temperature, the waste heat recovery and utilization function is realized.

[0059] In one embodiment, see Figure 7 The energy-saving straw charcoal mixed fuel preparation equipment also includes a nitrogen recovery tank 13 and a filter and scrubbing mechanism 14. The recovery inlet of the filter and scrubbing mechanism 14 is connected to the waste heat exhaust port 1505 of the waste heat exchanger 15, and the recovery exhaust port of the filter and scrubbing mechanism 14 is connected to the nitrogen recovery tank 13. The filter and scrubbing mechanism 14 is configured to remove solid particles, impurities (tar particles and dust) and miscellaneous gases (acidic gases and water vapor) from the exhaust gas.

[0060] Specifically, the air scrubbing mechanism 14 includes a housing, an air scrubbing assembly 1402 installed inside the housing, and a filter 1401. The side wall of the housing is provided with a recovery air inlet and a recovery exhaust outlet. The waste heat exhaust outlet 1505 of the waste heat exchanger 15 is connected to the recovery air inlet. The recovery outlet of the nitrogen recovery tank 13 is connected to the recovery exhaust outlet. The air scrubbing assembly 1402 is connected to the recovery air inlet to remove impurities from the waste gas. The exhaust outlet of the air scrubbing assembly 1402 is connected to the air inlet of the filter 1401 to filter out solid particles and impurities in the waste gas. The exhaust outlet of the filter 1401 is connected to the recovery exhaust outlet.

[0061] More specifically, the gas scrubbing assembly 1402 includes multiple filter bottles arranged side by side, each filter bottle being sealed. One part of the filter bottles contains sodium hydroxide solution to remove acidic gases, and another part of the filter bottles contains anhydrous calcium chloride to remove water vapor. Adjacent filter bottles are connected by a first guide pipe. The recovery air inlet is connected to the filter bottle at the beginning of a second guide pipe, and the filter bottle at the end is connected to the air inlet of the filter 1401 by a third guide pipe. One end of the third guide pipe is inserted into the corresponding filter bottle, and the other end is the exhaust port.

[0062] The filter 1401 includes a vacuum filtration flask, a Buchner funnel, and an ethanol solution bottle. The vacuum filtration flask is connected to a vacuum pump. The Buchner funnel is installed on the vacuum filtration flask and contains filter paper. The output port of the vacuum pump is connected to the ethanol solution bottle through a fourth guide tube. The ethanol solution bottle contains ethanol solution, and the outlet of the ethanol solution bottle is connected to the outlet of the filter 1401 through a fifth guide tube. The gas extracted by the vacuum pump enters the ethanol solution to remove tar, and then enters the nitrogen recovery tank 13 through the outlet of the filter 1401 for preliminary recovery. The gas in the nitrogen recovery tank 13 can be further processed to separate nitrogen for reuse.

[0063] In one embodiment, see Figure 4 The top of the coking reactor 1 is provided with a syngas discharge pipe 102. The side wall of the syngas discharge pipe 102 has a hollow structure. The syngas discharge pipe 102 is connected to the inside of the coking reactor 1, and the top of the syngas discharge pipe 102 forms a syngas outlet 101. The condensation mechanism includes a condenser 20 and a cooling coil 104. The cooling coil 104 is embedded in the side wall, top wall and syngas discharge pipe 102 of the coking reactor 1 in a spiral winding manner, and the cooling coil 104 is located in the lowest coking bed 1 inside the coking reactor 1. Above 06, the spiral spacing of the cooling coils 104 located at the top of the coking reactor 1 and inside the syngas discharge pipe 102 is smaller than that of the cooling coils 104 located inside the side wall of the coking reactor 1. This makes the cooling coils 104 on the coking reactor 1 more densely distributed as they go up, resulting in a better cooling effect. The coolant outlet of the condenser 20 is connected to one end of the cooling coil 104 through the first liquid delivery pipe 2003, and the coolant recovery port of the condenser 20 is connected to the other end of the cooling coil 104 through the second liquid delivery pipe.

[0064] Specifically, the cooling coil 104 is wrapped tightly around the outer wall of the inner wall of the coking reaction tank 1. The condenser 20 is equipped with a cooler and a condensing coil 2002. The cooler cools the coolant in the condensing coil 2002. The two ends of the condensing coil 2002 are connected to the coolant outlet and the coolant recovery port, respectively. A coolant transfer pump 2004 is installed on the condensing coil 2002, which realizes the circulation of coolant in the cooling coil 104 and the condensing coil 2002.

[0065] More specifically, a coolant storage tank 2001 is installed between the second infusion pipe and the coolant recovery port to store a portion of the coolant.

[0066] In one embodiment, see Figures 4-5 The energy-saving straw-coke blended fuel preparation equipment also includes a tar collection tank 21, a guide pipe 22, and a tar collection box 4. The tar collection tank 21 is annular in shape and fixed to the inner circumferential wall of the coking reaction tank 1, with one end of the tar collection tank 21 in close contact with the inner sidewall of the coking reaction tank 1. The cross-section of the tar collection tank may, but is not limited to, be arc-shaped. The tar collection box 4 is fixed to the bottom outer wall of the coking reaction tank 1. The guide pipe passes through the coking reaction tank 1, with one end connected to the tar collection tank 21 and the other end connected to the tar collection box 4. There is at least one guide pipe 22.

[0067] The tar synthesis gas from coking zone 28 enters the coking reactor 1 through flow regulating valve 17, passes through porous gas distribution plate 107 to ensure uniform gas distribution and upward flow, and passes through coking bed 106. The condensing mechanism is activated to supply coolant to the cooling coil 104 through the first liquid delivery pipe 2003 to cool the coking reactor 1. The temperature is monitored in real time by temperature sensor 19, and the output power of coolant delivery pump 2004 in condenser 20 is controlled accordingly to regulate the temperature. After the tar syngas is cooled, the large tar molecules in it condense and liquefy, adsorbing onto the straw biomass. The cooled syngas undergoes a second cooling process through the syngas discharge pipe 102, and the tar further condenses and falls back into the coking bed 106. The remaining nitrogen and syngas are transported to the syngas storage tank 5 for storage. The coolant flows in the cooling coil 104 and flows back to the condensing coil 2002 for the next condensation cycle. The tar that is not adsorbed onto the straw biomass (i.e., the tar adsorbed on the inner wall of the coking reactor 1) is collected through the tar collection tank and guided to the tar collection box 4 through the guide pipe for collection.

[0068] In the above embodiments, the energy-saving straw-coke mixed fuel preparation equipment also includes a central control system. Temperature sensor 19, flow regulating valve 17, electric drawer slide rail 18, waste heat exchanger 15, electric heater and condenser 20 are all connected to the central control system, and the central control system realizes automatic temperature regulation and display.

[0069] Combination Figures 1-7 The above embodiments are described in detail.

[0070] Step 1: Crush the straw raw material to about five mesh, open the operating door 2 on the coking reaction tank 1 and the pyrolysis carbonization reaction tank 6, and spread the straw raw material flat on the coking bed 106, the coking bed 601 and the semi-coking bed 603 respectively, and then close the operating door 2.

[0071] Step 2: Open nitrogen cylinder 12, allowing nitrogen to enter the coking zone 28 from the bottom of the pyrolysis carbonization reactor 6 through the outlet of nitrogen cylinder 12. Introduce nitrogen at a high flow rate of 10 L / min for 30 minutes. The nitrogen then enters the semi-coking zone 29 through the flow regulating valve 17, and then enters the coking tank 1 through the top of the pyrolysis carbonization reactor 6, purging all oxygen from the tanks to prevent oxidation. Finally, the nitrogen in the coking tank 1 is discharged into the syngas storage tank 5 through the syngas exhaust port for temporary storage. After purging, reduce the nitrogen flow rate of nitrogen cylinder 12 to 2 L / min. Turn on the electric heater and set the pyrolysis temperature to 500℃±50℃. The coking zone 28 of the pyrolysis carbonization reactor 6 is equipped with a temperature sensor 19 for real-time temperature monitoring to prevent overheating or underheating. The reaction time in the coking zone 28 is 90-120 minutes.

[0072] Step 3: The straw raw material in the coking bed 601 undergoes a pyrolysis and carbonization reaction to produce tar syngas. Nitrogen gas entering from the nitrogen inlet, carrying the tar syngas and residual heat from the electric heater, enters the semi-coking zone 29 through the flow regulating valve 17. This causes the straw biomass on the semi-coking bed 603 to undergo an incomplete pyrolysis and carbonization reaction (semi-coking reaction) and produce tar syngas. The semi-coking zone 29 of the pyrolysis and carbonization reactor 6 is also equipped with a temperature sensor 19 for temperature monitoring. The flow rate of the syngas is controlled by adjusting the opening of the flow regulating valve 17, indirectly controlling the heat brought in. At the same time, heating coils 27 are arranged on the periphery. When the heat brought in by the syngas is insufficient (temperature <250℃), the waste heat exchanger 15 is activated, allowing the waste heat fluid to circulate into the heating coils 27 to supplement the heat of the semi-coking zone 29. Simultaneously, the opening of the flow regulating valve 17 is increased; when the temperature in the semi-coking zone 29 is too high (temperature > 350℃), the waste heat exchanger 15 is shut off, and the opening of the flow regulating valve 17 is reduced. The temperature in the semi-coking zone 29 is maintained at 300±50℃ by controlling the opening of the waste heat exchanger 15 and the flow regulating valve 17. The reaction time in the semi-coking zone 29 is 30-60 minutes. When the straw biomass reaction in the semi-coking bed 603 of one semi-coking bed group ends, the drawer-type chamber 8 is moved by operating the slide rail controller 26 to switch to another semi-coking bed group and align with the pyrolysis carbonization reaction tank 6 to continue the reaction.

[0073] Step 4: Nitrogen gas, carrying residual heat and newly generated tar synthesis gas, continues to enter the coking reactor 1 through the top of the pyrolysis carbonization reactor 6. The condenser 20 is turned on, and the flow rate of the coolant is controlled by the coolant delivery pump 2004, delivering the coolant to the cooling coil 104. This maintains the temperature in the lower part of the coking reactor 1 at 200-150℃, and the temperature in the upper part at 100-150℃, decreasing from bottom to top. A heating coil 27 is wrapped around the gas outlet near the top of the pyrolysis carbonization reactor 6 to control the inlet temperature difference at 15℃-25℃ to prevent tar condensation. The gas inlet 105 at the bottom of the coking reactor 1 is funnel-shaped; the flow rate of the tar synthesis gas decreases after entering, reducing the impact condensation phenomenon of large tar molecules at this inlet. After passing through the inlet at the bottom of the coking reactor 1, the syngas encounters a porous gas distribution plate 107. The porous gas distribution plate 107 forces the gas to be evenly distributed through the coking bed 106, ensuring sufficient residence time for the tar-rich syngas to adhere. As the temperature decreases, the large tar molecules in the syngas slowly condense into a liquid state and are adsorbed onto the straw raw material in the coking bed 106. The coking reactor 1 is also equipped with a temperature sensor 19 to monitor the internal temperature. A tar collection box 4 at the bottom directs the liquefied tar adsorbed on the inner wall of the coking reactor 1 to a tar collection tank, and then into the tar collection box 4 through a guide pipe. The syngas that has lost tar enters the syngas storage tank 5 through the syngas exhaust port. Tar that is not completely liquefied during its passage through the syngas exhaust port is further condensed and liquefied by the cooling coil 104 and flows back into the coking reactor 1. The coolant that has completed the cooling and condensation process in cooling coil 104 is returned to condensing coil 2002 via coolant transfer pump 2004, thus achieving a cooling cycle. The adsorption and condensation reaction time in the condensing tank is 60-120 minutes.

[0074] Step 5: During the reaction, the nitrogen recovery tank 13, syngas storage tank 5, and air cylinder 11 are opened. The syngas in the syngas storage tank 5 flows into the gas heater 10 through the syngas inlet. The air cylinder 11 flows into the gas heater 10 through the air inlet. After the mixing ratio is adjusted by the mixed gas flow valve 1005, it is injected into the gas mixing chamber 1003 and ignited in the mixed gas combustion chamber 1002, supplying the pyrolysis carbonization reaction tank 6 for the pyrolysis carbonization reaction. The exhaust gas after combustion enters the waste heat exchanger 15 through the exhaust port for heat exchange. After heat exchange, the exhaust gas enters the filtration and washing mechanism 14 through the recovery inlet. After being washed by the washing component 1402 and filtered by the filter 1401, it flows into the nitrogen recovery tank 13. After further purification and drying, the nitrogen can be recycled.

[0075] The reactor designed in this invention adopts an integrated vertical structure, relying on a single-stage heating device as the core heat source. Through staged temperature control in the coking zone, semi-coking zone, and coking tank, a gradient temperature zone design is formed, creating different generation conditions for different products. This allows for the simultaneous preparation of three products—biochar, semi-coke straw, and adsorbed tar straw—within the same reactor, reducing process steps and procedures. Each reaction zone operates independently without interference, minimizing variable influences and improving process stability. It overcomes the shortcomings of traditional equipment, such as complex product preparation and pyrolysis separation processes. Simultaneously, it utilizes a waste heat exchanger, a gas-fired heater, and a filtration and washing mechanism to achieve the recycling of waste heat, syngas, and nitrogen. Multi-stage heat source utilization improves energy recovery rate, reduces external energy consumption, and addresses the waste heat and low resource utilization of traditional equipment. Furthermore, the equipment has a compact structure, occupies little space, and is easy to disassemble and process, reducing manufacturing costs and solving the problem of large footprint in traditional charcoal production equipment.

[0076] Finally, it should be noted that the above embodiments are only used to illustrate the technical solutions of the present invention, and not to limit them; although the present invention has been described in detail with reference to the foregoing embodiments, those skilled in the art should understand that modifications can still be made to the technical solutions described in the foregoing embodiments, or equivalent substitutions can be made to some of the technical features; and these modifications or substitutions do not cause the essence of the corresponding technical solutions to deviate from the protection scope of the technical solutions of the embodiments of the present invention.

Claims

1. An energy-saving straw-coke blended fuel preparation device, characterized in that, The system includes a coking reactor, a pyrolysis carbonization reactor, a condensation mechanism, a nitrogen cylinder, a heating device, and a waste heat preservation device. The pyrolysis carbonization reactor is internally divided into a semi-coking zone and a coking zone from top to bottom. A flow regulating valve is installed in the pyrolysis reactor between the semi-coking zone and the coking zone. Multiple coking beds for placing straw are installed in the coking zone. The heating device is configured to heat the coking zone to form coke and tar-containing syngas from the straw placed on the coking beds. A semi-coking bed is installed in the semi-coking zone. The waste heat preservation device is configured to... The semi-coking zone is heated, and the flow regulating valve regulates the flow of tar-containing syngas to semi-coke the straw placed in the semi-coking bed and generate tar-containing syngas. The coking reaction tank is located at the top of the pyrolysis carbonization reaction tank and is interconnected with it. The coking reaction tank has multiple layers of coking beds arranged vertically. The condensing mechanism is configured to cool the tar-containing syngas in the coking reaction tank to liquefy the tar. The top of the coking reaction tank is provided with a syngas exhaust port, and the outlet of the nitrogen cylinder is connected to the bottom of the pyrolysis carbonization reaction tank.

2. The energy-saving straw-coke blended fuel preparation equipment according to claim 1, characterized in that, The bottom of the coking reaction vessel is provided with a tank inlet for connection to the top of the pyrolysis carbonization reaction vessel. The tank inlet is funnel-shaped. A porous gas distribution plate is fixed at the bottom of the coking reaction vessel, and the coking bed is located above the porous gas distribution plate.

3. The energy-saving straw-coke blended fuel preparation equipment according to claim 1, characterized in that, The energy-saving straw-coke blended fuel preparation equipment also includes a tar collection tank, a guide pipe, and a tar collection box. The tar collection tank is annular in shape and fixed on the inner circumferential wall inside the coking reaction tank, with one end of the tar collection tank in close contact with the inner side wall of the coking reaction tank. The tar collection box is fixed on the bottom outer wall of the coking reaction tank. The guide pipe passes through the coking reaction tank, with one end connected to the tar collection tank and the other end connected to the tar collection box.

4. The energy-saving straw-coke blended fuel preparation equipment according to claim 1, characterized in that, The semi-coking bed, coking bed, and coking bed have the same structure. The coking bed is a cylindrical structure. The top of the coking bed is provided with a groove for placing straw. The bottom of the coking bed is provided with multiple ventilation holes communicating with the inside of the groove. The bottom of the pyrolysis carbonization reaction tank is fixed with a material isolation plate. The material isolation plate is located below the coking bed and has multiple evenly distributed gas flow holes on it.

5. The energy-saving straw-coke blended fuel preparation equipment according to claim 1, characterized in that, The energy-saving straw-coke blended fuel preparation equipment also includes a sealed box, a drawer-type compartment, and a sliding drive mechanism. The sealed box penetrates radially through the pyrolysis carbonization reactor corresponding to the semi-coking zone and divides it into an upper semi-coking zone and a lower semi-coking zone. A drawer-type compartment with an open top is placed inside the sealed box. Two sets of semi-coking bed layers are arranged side by side at intervals inside the drawer-type compartment. Each set of semi-coking bed layers includes at least two semi-coking bed layers arranged vertically. A flow port is provided on the bottom wall of the drawer-type compartment for the passage of syngas. The sliding drive mechanism is set on the sealed box and connected to the drawer-type compartment to drive the drawer-type compartment to perform reciprocating linear motion so that the two sets of semi-coking bed layers inside the drawer-type compartment alternately align with the inside of the pyrolysis carbonization reactor, thereby connecting the upper and lower semi-coking zones.

6. The energy-saving straw-coke blended fuel preparation equipment according to claim 1, characterized in that, The energy-saving straw-coke mixed fuel preparation equipment also includes an air cylinder and a syngas storage tank. The air inlet of the syngas storage tank is connected to the syngas exhaust port to collect the syngas discharged from the coking reaction tank. The heating device includes a gas-fired heater and an electric heater. The air inlet of the gas-fired heater is connected to the air cylinder and the syngas storage tank. The gas-fired heater is located at the bottom of the pyrolysis carbonization reaction tank and can heat it. The electric heater is a resistance wire heater. The resistance wire of the resistance wire heater is embedded in the side wall of the pyrolysis carbonization reaction tank corresponding to the coking zone in a spiral winding manner.

7. The energy-saving straw-coke blended fuel preparation equipment according to claim 1, characterized in that, The waste heat insulation device includes a waste heat exchanger and a heating coil. The heating coil is embedded in the side wall of the pyrolysis carbonization reaction tank corresponding to the semi-coking zone in a spiral winding manner. The two ends of the heating coil are respectively connected to the fluid inlet and fluid outlet of the waste heat exchanger to form a closed fluid circulation. The waste heat inlet of the waste heat exchanger is connected to the exhaust gas outlet of the gas-fired heating furnace to exchange heat with the fluid in the waste heat exchanger.

8. The energy-saving straw-coke blended fuel preparation equipment according to claim 7, characterized in that, The energy-saving straw-coke mixed fuel preparation equipment also includes a nitrogen recovery tank and a filtration and washing mechanism. The recovery inlet of the filtration and washing mechanism is connected to the waste heat exhaust port of the waste heat exchanger, and the recovery exhaust port of the filtration and washing mechanism is connected to the nitrogen recovery tank. The filtration and washing mechanism is configured to remove solid particles, impurities and miscellaneous gases from the waste gas.

9. The energy-saving straw-coke blended fuel preparation equipment according to claim 1, characterized in that, The coking reactor is equipped with a syngas discharge pipe at its top. The sidewall of the syngas discharge pipe has a hollow structure. The syngas discharge pipe is connected to the inside of the coking reactor, and the top of the syngas discharge pipe forms a syngas outlet. The condensation mechanism includes a condenser and a cooling coil. The cooling coil is embedded in the sidewall, top wall, and inside the syngas discharge pipe of the coking reactor in a spiral winding manner. The cooling coil is located above the lowest coking bed in the coking reactor. The spiral spacing of the cooling coils located at the top of the coking reactor and inside the syngas discharge pipe is smaller than the spiral spacing of the cooling coils located inside the sidewall of the coking reactor. The coolant outlet of the condenser is connected to one end of the cooling coil, and the coolant recovery port of the condenser is connected to the other end of the cooling coil.

10. The energy-saving straw-coke mixed fuel preparation equipment according to claim 6, characterized in that, The top of the sealed box is fixed with a tank support frame, which is fixedly connected to the coking reaction tank. The top of the pyrolysis carbonization reaction tank is provided with a tank outlet. The tank inlet and the tank outlet are connected and sealed by a sealing ring. A tank fixing frame is fixed on the outer wall of the pyrolysis carbonization reaction tank for support and fixation. The gas heating furnace is fixed inside the tank fixing frame.

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