Coal and solid waste co-pyrolysis gasification reaction device and method and application

Abstract

The present invention relates to a coal and solid waste co-pyrolysis and gasification reaction device, method, and application. The device comprises a pyrolysis furnace, a stripping furnace, and a gasifier connected in sequence. Raw materials containing coal and solid waste enter the pyrolysis furnace to produce products including crude pyrolysis gas and crude semi-coke. The crude semi-coke enters the stripping furnace to produce replacement gas and activated semi-coke. The activated semi-coke enters the gasifier to produce synthesis gas, high-temperature semi-coke, and crude slag. Part of the high-temperature semi-coke is returned to the bottom of the pyrolysis furnace, and part of the synthesis gas is returned to the pyrolysis furnace as circulating synthesis gas. The reaction device and method of the present invention can be applied to the field of co-utilization of coal and solid waste, improving the carbon conversion rate and effective gas content. The carbon conversion rate reaches over 98%, effectively improving the tar yield and quality.

Description

Technical Field

[0001] The present invention relates to the technical field of co-pyrolysis and gasification, and more specifically to a coal and solid waste co-pyrolysis and gasification reaction device, a reaction method and applications thereof. Background Art

[0002] Solid waste treatment involves reducing its volume and accelerating its natural purification through physical means (such as crushing, compression, drying, evaporation, and incineration), biochemical processes (such as oxidation, digestion, decomposition, and absorption), and chemical processes such as pyrolysis and gasification. This generally refers to solid and muddy materials discarded by people in production and daily life, including waste plastics, waste rubber, and dry garbage. Pyrolysis and gasification are highly regarded for their harmlessness, volume reduction, and resource recycling.

[0003] Pyrolysis of solid waste is a technical measure that involves heating solid waste in the absence or anoxic conditions to decompose it, converting it into storable and easily transportable energy sources such as gaseous fuel and fuel oil, or recovering resource products (such as liquid pyrolysis products as chemical raw materials). Because pyrolysis occurs in the absence or anoxic conditions, its exhaust volume is less than that of incineration. It is primarily used in the treatment and utilization of municipal solid waste, sewage sludge, waste plastics, waste rubber, and other wastes. The co-resource utilization of organic solid waste and coal, as it does not require additional equipment investment, can save coal resources, and can also solve the problem of waste resource utilization, making it a new approach to implementing the energy diversification strategy.

[0004] At present, the treatment of co-pyrolysis of coal and solid waste is still limited to the stage of coke oven dry distillation and laboratory exploratory research, and there are even fewer reports on co-pyrolysis and co-gasification of coal and solid waste. Patent CN104232129A proposes a method for co-pyrolysis of organic waste and coal to produce semi-coke and tar. The organic waste is first mixed with coal in a vertical dry distillation furnace for drying and preheating. The preheated materials are then subjected to low-temperature dry distillation and medium-temperature dry distillation in turn to obtain low-volatile semi-coke and coal gas. The semi-coke and tar are then recovered, and finally the coal gas is purified. Patent CN107057730A discloses a method for co-pyrolysis of solid waste and coal. After drying, the solid waste and coal are subjected to dry distillation and pyrolysis reaction in a horizontal rotary kiln furnace. After separation, semi-coke, tar and coal gas are obtained, of which part of the coal gas is used as a heat source for pyrolysis of the mixture. However, existing devices and methods such as retorts, rotary kilns and fixed beds that commonly handle the co-pyrolysis and gasification reaction of coal and solid waste have disadvantages such as uneven mixing, poor heat and mass transfer, and slow reaction rate, which lead to problems such as low tar yield, low conversion rate and small processing volume. Therefore, we have proposed improvements to the above problems. Summary of the Invention

[0005] In view of the problems existing in the above-mentioned prior art such as difficulty in utilizing solid waste, low tar yield, and low carbon conversion rate, one of the purposes of the present invention is to provide a coal and solid waste co-pyrolysis and gasification reaction device, which adopts a combination of a pyrolysis furnace, a steam stripping furnace and a gasification furnace to better solve the above-mentioned problems and can be applied to the field of co-utilization of coal and solid waste.

[0006] To achieve the above object, the technical solution adopted by the present invention is as follows:

[0007] A coal and solid waste co-pyrolysis and gasification reaction device comprises a pyrolysis furnace, a stripping furnace and a gasification furnace connected in sequence; raw materials containing coal and solid waste enter the pyrolysis furnace to obtain products containing crude pyrolysis gas and crude semi-coke, the crude semi-coke enters the stripping furnace to obtain replacement gas and activated semi-coke, the activated semi-coke enters the gasification furnace to obtain synthesis gas, high-temperature semi-coke and crude slag, part of the high-temperature semi-coke returns to the bottom of the pyrolysis furnace, and part of the synthesis gas returns to the pyrolysis furnace as circulating synthesis gas.

[0008] Further preferably:

[0009] In the above technical solution, the top of the pyrolysis furnace is provided with a raw material inlet and a product outlet, and the bottom is provided with a high-temperature semi-coke return inlet and a circulating synthesis gas inlet; the top of the stripping furnace is provided with a replacement gas outlet, the middle and upper part is provided with a coarse semi-coke return inlet, and the bottom is provided with an activated semi-coke outlet; the top of the gasification furnace is provided with a gas outlet, the middle and upper part is provided with a high-temperature semi-coke outlet, the middle and lower part is provided with an activated semi-coke return inlet, and the bottom is provided with an ash outlet and a gasifying agent inlet.

[0010] In the above technical solution, a pyrolysis furnace cyclone separator is provided at the product outlet of the pyrolysis furnace, a coarse pyrolysis gas outlet is provided above the pyrolysis furnace cyclone separator, a coarse semi-coke outlet is provided below the pyrolysis furnace cyclone separator, and is connected to the coarse semi-coke return inlet of the stripping furnace through a coarse semi-coke return device.

[0011] In the above technical solution, the activated semi-coke outlet at the bottom of the stripping furnace is provided with an activated semi-coke return device, and is connected to the activated semi-coke return inlet of the gasifier through the activated semi-coke return device.

[0012] In the above technical solution, the gas outlet at the top of the gasifier is connected to the gasifier cyclone separator. The top of the gasifier cyclone separator is provided with a syngas outlet, which is connected to the circulating syngas inlet below the pyrolysis furnace through a syngas splitter. The bottom of the gasifier cyclone separator is provided with a gasified semi-coke outlet, which is connected to the gasified semi-coke return inlet located on the side wall of the gasifier through a gasified semi-coke return device. The gasified semi-coke return device can be a conventional return device, generally a U-shaped return valve.

[0013] In the above technical solution, the high-temperature semi-coke outlet of the gasifier is provided with a high-temperature semi-coke return device, which is connected to the high-temperature semi-coke return inlet at the bottom of the pyrolysis furnace through the high-temperature semi-coke return device. The high-temperature semi-coke return device can be a conventional return device, generally a J-type return valve.

[0014] In the above technical solution, the coarse semi-coke return device and / or activated semi-coke return device is an inner and outer double-cylindrical structure, the outer outer cylinder is provided with a through hole at the top and an air inlet at the bottom, preferably a porous structure; the inner inner cylinder is provided with a gap at the bottom, preferably a grid-type gap structure; the top is provided with a feed port communicating with the coarse semi-coke outlet or the activated semi-coke outlet, the feed port passes through the through hole at the top of the outer cylinder and its outer wall is connected to the inner wall of the through hole at the top of the outer cylinder, preferably a sealed fixed connection; the inner cylinder divides the return device into an inner cylinder space and an outer cylinder space, and a space is left between the bottom of the inner cylinder and the bottom end of the outer cylinder to form a horizontal channel, and the height of the horizontal channel is preferably 1 / 5 to 3 / 5 of the height of the outer cylinder of the return device; the upper side wall of the outer cylinder is provided with a plurality of, preferably 2 to 6, return pipes, which are connected to the coarse semi-coke return inlet of the stripping furnace or the activated semi-coke return inlet of the gasification furnace. The air inlet at the bottom of the outer cylinder is used to admit loosening air, which causes particles of the coarse or activated semi-coke return material to move and flip, reaching the desired location within the return device. Preferably, the linear velocity of the loosening air is specified, with the linear velocity of the loosening air inlet corresponding to the inner cylinder area being different from the linear velocity of the loosening air inlet corresponding to the annular area between the outer and inner cylinders, and the air intake of each of these different areas is independently controlled. Furthermore, the loosening air comprises at least one of nitrogen, an inert gas, and water vapor.

[0015] In the above technical solution, the crude semi-coke return inlet of the stripping furnace corresponds to the return pipe of the crude semi-coke return device, and multiple, preferably 2-6, crude semi-coke return inlets are arranged at equal intervals along the circumference of the cross-section of the stripping furnace; and / or, the activated semi-coke return inlet of the gasifier corresponds to the return pipe of the activated semi-coke return device, and multiple, preferably 2-6, activated semi-coke return inlets are arranged at equal intervals along the circumference of the cross-section of the gasifier.

[0016] In the above technical solution, a guide tube is arranged in the pyrolysis furnace, preferably a coaxial guide tube; the guide tube is a cylindrical structure with open ends, the upper port of the guide tube is connected to the top of the pyrolysis furnace, and the lower port of the guide tube is placed in the pyrolysis furnace; the guide tube divides the pyrolysis furnace into an inner pyrolysis tube and an outer pyrolysis tube, the raw material inlet of the pyrolysis furnace is located at the upper port of the inner pyrolysis tube of the guide tube, and the product outlet of the pyrolysis furnace is arranged on the outer pyrolysis tube, and communicates with the space between the inner pyrolysis tube and the outer pyrolysis tube.

[0017] In the above technical solution, the inner wall of the guide tube is provided with multiple rows, preferably 2 to 4 rows of triangular prisms, and the triangular prisms preferably occupy 1 / 4 to 1 / 2 of the circumference of the inner wall of the guide tube. The triangular prisms of different rows are preferably staggered at different heights along the guide tube.

[0018] In the above technical solution, the height of the guide tube is 1 / 10 to 9 / 10 of the height of the pyrolysis furnace.

[0019] In the above technical solution, the inner diameter of the guide tube is 1 / 5 to 3 / 5 of the inner diameter of the pyrolysis furnace.

[0020] In the above technical solution, a pyrolysis furnace gas distributor is horizontally arranged at the bottom of the pyrolysis furnace, and preferably: the pyrolysis furnace gas distributor is a circular flat plate structure, the outer periphery of which is fixedly connected to the inner wall of the bottom of the pyrolysis furnace, and air holes are provided on the circular plane, and the air holes are evenly arranged along the circumference and in the radial direction; when a guide tube is provided inside the pyrolysis furnace, the circular flat plate is divided into an inner ring and an outer ring, the outer diameter of the inner ring corresponds to the inner diameter of the guide tube, the porosity of the inner ring flat plate is 3-5%, and the porosity of the outer ring flat plate is 0.5-3%; more preferably, the inner ring is provided with 10-50 circles of inner ring air holes, each circle is provided with 20-50 inner ring air holes, and the inner ring air hole diameter is 5-10 mm; the outer ring is provided with 10-50 circles of outer ring air holes, each circle is provided with 50-100 outer ring air holes, and the outer ring air hole diameter is 0.5-3 mm.

[0021] In the above technical solution, 1 to 5 layers of stripping furnace baffles are provided in the stripping furnace, and each layer of stripping furnace baffles includes supporting ribs that cross the same axis and are connected to the inner wall of the stripping furnace at both ends, and baffles connecting adjacent supporting ribs; each baffle is provided with a plurality of pairs of triangular sawtooth structures that are opposite to each other on both sides, and the top angles of the triangular sawtooth structures are all facing the bottom of the stripping furnace, the triangular sawtooth structure on one side is inclined outward, and the triangular sawtooth structure on the other side is inclined inward; a gap is left between the inward-inclined triangular sawtooth structures and the outward-inclined triangular sawtooth structures between adjacent baffles.

[0022] In the above technical solution, the support ribs evenly divide the cross section of the stripping furnace;

[0023] The number of the supporting ribs is 2 or more, preferably 3 to 6;

[0024] The number of the stop bars is more than 1, preferably 4 to 10, along the radial direction of the support ribs;

[0025] Each of the said bars is provided with 1 to 10 pairs of triangular sawtooth structures;

[0026] Each layer of the stripping furnace baffle includes 50 to 200 pairs of triangular sawtooth structures.

[0027] In the above technical solution, multiple, preferably 2-3, stripping gas distributors are arranged in sequence from top to bottom at the lower part of the stripping furnace. The stripping gas distributor includes a ventilation main pipe and horizontal circular tubes connected to the ventilation main pipe, which are nested from large to small; the circular tubes are preferably 4 to 10; one end of the ventilation main pipe is provided with an air inlet connected to the air inlet pipe outside the stripping furnace, and 20 to 100 air holes are evenly arranged on the circular tube, and the air holes are arranged at equal intervals along the circle, the air hole diameter is 1 to 10 mm, and the gas outlets are all arranged downward.

[0028] In the above technical solution, a gasifier gas distributor is provided at the bottom of the gasifier, and the gasifier gas distributor includes a support plate and a gas nozzle provided on the support plate; the support plate is a funnel-shaped structure provided on the bottom plate of the gasifier, and the maximum outer edge of the upper end of the funnel-shaped structure is fixedly connected to the inner wall of the gasifier; the lower end of the funnel-shaped structure is connected to an ash channel which is connected to the ash outlet at the bottom of the gasifier; the gasifying agent inlet of the gasifier is connected to the space formed between the funnel-shaped structure of the gasifier gas distributor and the inner wall of the gasifier.

[0029] In the above technical solution, the funnel structure of the gasifier gas distributor support plate has a funnel cone surface with a horizontal axis that forms an angle less than or equal to 60°, preferably 15° to 45°;

[0030] The gas nozzles of the gasifier gas distributor support plate are all distributed in concentric circles on the support plate funnel cone surface, which are radially arranged with the same axis as the gasifier; preferably, the funnel cone surface of the gasifier gas distributor support plate is divided into an inner ring and an outer ring, the outer ring is provided with a vertical nozzle, and the outer ring has an opening rate of 1-5%; the inner ring is provided with a rotating nozzle, and the inner ring has an opening rate of 3-5%;

[0031] More preferably, the spacing between nozzles in each circle is the same, and the vertical nozzles on the outer circle are preferably arranged in 1 to 10 circles, with preferably 50 to 100 nozzles in each circle; the rotating nozzles on the inner circle are preferably rotated at an angle of 5 to 45° along the axial direction, and the rotating nozzles are preferably arranged in 10 to 50 circles, with preferably 10 to 150 rotating nozzles in each circle.

[0032] The above technical solution also includes a cooling and separation unit, which is connected to the pyrolysis furnace and / or stripping furnace pipeline; preferably, the pyrolysis gas outlet of the pyrolysis furnace cyclone separator and / or the replacement gas outlet of the stripping furnace are respectively connected to the air inlet of the cooling and separation unit, and the crude pyrolysis gas from the pyrolysis furnace cyclone separator and / or the replacement gas from the stripping furnace are passed through the cooling and separation unit to obtain tar and pyrolysis gas.

[0033] The second object of the present invention is to provide a method for treating the co-pyrolysis and gasification reaction of coal and solid waste, comprising: the raw materials enter the pyrolysis furnace and contact with the circulating synthesis gas to undergo a co-pyrolysis reaction to produce crude pyrolysis gas and crude semi-coke, the crude semi-coke enters the stripping furnace for stripping and activation to obtain displacement gas and activated semi-coke, and the crude pyrolysis gas and displacement gas are separated to obtain oil products and pyrolysis gas; the activated semi-coke enters the gasification furnace and undergoes incomplete combustion and gasification reaction with the gasifying agent from the gasification furnace to generate synthesis gas, high-temperature semi-coke and coarse slag; part of the high-temperature semi-coke returns to the bottom of the pyrolysis furnace, and part of the synthesis gas returns to the pyrolysis furnace as circulating synthesis gas.

[0034] Preferably,

[0035] In the above technical solution, the reaction temperature of the pyrolysis furnace is 400-700°C, the gas phase linear velocity of the pyrolysis inner cylinder is 0.1-0.5 m / s, the gas phase linear velocity of the pyrolysis outer cylinder is 0.5-2.0 m / s, and the average density of the pyrolysis outer cylinder reactant bed is 150-300 kg / m 3 ;

[0036] The stripping furnace reaction temperature is 350-550°C, the gas phase linear velocity is 0.1-1m / s, and the average bed density is 250-600kg / m 3 ;

[0037] The reaction temperature of the gasifier is 700-1200°C, the gas phase linear velocity is 0.2-2m / s, and the average bed density is 150-450kg / m 3 ;

[0038] The system reaction pressure ranges from 0.1 to 10.0 MPa, wherein the system pressure refers to the reaction pressure of the entire co-pyrolysis and gasification reaction device system.

[0039] In the above technical solution, the gas velocity at the outlet of the inner circle pores of the pyrolysis furnace gas distributor is 5-20 m / s, and the gas velocity at the outlet of the outer circle pores is 10-50 m / s; and / or,

[0040] Specifically, the gas outlet speeds of the inner and outer rings of the pyrolysis furnace gas distributor are controlled by separate gas supply from the two zones. The linear velocity of the loose gas at the bottom of the inner cylinder space of the coarse coke return device and the activated coke return device is 0.05-0.2 m / s, and the linear velocity of the loose gas at the bottom of the outer cylinder space is 0.02-0.4 m / s.

[0041] Water vapor is introduced into the stripping gas distributor, the water vapor temperature is 200-500°C, and the gas velocity at the outlet of the stripping gas distributor hole is 2-20m / s;

[0042] The gas velocity at the vertical nozzle outlet of the gasifier gas distributor is 10-50 m / s, and the gas velocity at the rotary nozzle outlet is 2-20 m / s;

[0043] Specifically, the gas outlet speeds of the vertical nozzle and the rotary nozzle of the gas distributor are controlled by separate gas supply to the two areas.

[0044] The gasifying agent comprises one of an oxygen-containing gas, a mixture of an oxygen-containing gas and water vapor, or a mixture of an oxygen-containing gas, water vapor, and CO2, and the oxygen-containing gas preferably comprises oxygen, air, oxygen-enriched air, or a mixture thereof; more preferably, the molar ratio of oxygen in the gasifying agent to carbon in the semi-coke in the gasifier is 0.5 to 1.0 mol / mol, and the molar ratio of water vapor in the gasifying agent to carbon in the semi-coke in the gasifier is 0.5 to 5.0 mol / mol; and / or,

[0045] The temperature of the gasifying agent is 200-800°C.

[0046] In the above technical solution, the weight ratio of solid waste to coal in the raw materials is (3-10):100.

[0047] The third object of the present invention is to provide a coal and solid waste co-pyrolysis and gasification reaction device or the application of the described method in the coal and solid waste co-pyrolysis and gasification reaction, wherein the coal preferably includes at least one of lignite, bituminous coal, anthracite and peat, and the solid waste preferably includes at least one of waste plastic, waste rubber and dry garbage.

[0048] Beneficial effects of the present invention:

[0049] 1) The co-pyrolysis of coal and solid waste has a synergistic effect, effectively improving the tar yield and quality. By setting up a guide tube and a guide baffle, the raw coal and solid waste can be preheated in the guide tube, and the contact area and residence time are increased under the action of the guide baffle, further promoting the uniform mixing of coal and solid waste, and solving the problem of uneven solid-solid mixing. The setting of different apertures in the inner and outer rings of the pyrolysis furnace gas distributor ensures a smooth transition of the material from the downward flow of the inner tube to the upward flow of the outer tube, smoothly realizes the flow pattern change, and makes the fluidization and mixing of the outer tube area uniform.

[0050] 2) The coarse coke return device and the activated coke return device are configured to be cylindrical and have a multi-channel return system with multiple return pipes, which can achieve a large circulation rate of material circulation, meet the requirements of the pyrolysis and stripping processes for the particle circulation volume, and enter the next reactor through multiple return pipes, achieving radial uniformity of solid particle feeding.

[0051] 3) The stripping furnace displaces oil and gas trapped between coarse coke particles and adsorbed within their pores. It also opens up the pores of the coke, further activating the coke and enhancing its gasification reactivity. The stripping furnace baffles within the furnace disperse large bubbles in the high-density zone, enhancing homogeneous gas-solid mixing within the furnace and improving heat and mass transfer between the steam and the coarse coke particles, resulting in a significant stripping effect.

[0052] 4) The outer vertical nozzles in the gasifier gas distributor reduce the wall effect to a certain extent, and the inner rotating nozzles promote uniform radial distribution of the material, extend the residence time of the gasifier and particles in the furnace, and improve the carbon conversion rate and effective gas content. BRIEF DESCRIPTION OF THE DRAWINGS

[0053] Figure 1 This is a schematic diagram of the coal and solid waste co-pyrolysis and gasification reaction device and process flow diagram of the present invention;

[0054] Figure 2-1 It is a side view schematic diagram of the guide tube (the guide tube with two rows of triangular prisms);

[0055] Figure 2-2 This is a perspective front view of a guide tube (a guide tube with two rows of triangular prisms);

[0056] Figure 2-3 This is a cross-sectional view of the guide tube (a guide tube with two rows of triangular prisms);

[0057] Figure 3-1 It is a perspective diagram of the structure of the coarse coke return device and the activated coke return device;

[0058] Figure 3-2 It is a three-dimensional schematic diagram of the coarse semi-coke return device and the activated semi-coke return device;

[0059] Figure 4 This is a schematic diagram of the gas distributor for the pyrolysis furnace;

[0060] Figure 5-1 It is a top view schematic diagram of the stripping furnace baffle;

[0061] Figure 5-2 This is a schematic diagram of the cross-sectional structure of the stripping furnace baffle;

[0062] Figure 6 This is a top view of the gas distributor of the gasifier.

[0063] Reference numerals:

[0064] 1 is the raw material inlet, 2 is the guide tube; 3 is the guide plate; 4 is the pyrolysis furnace; 5 is the pyrolysis furnace gas distributor; 6 is the pyrolysis furnace cyclone separator; 7 is the coarse semi-coke return device; 8 is the coarse semi-coke return inlet; 9 is the stripping furnace; 10 is the built-in cyclone separator; 11 is the stripping furnace baffle; 12-13 are the stripping gas distributor; 14 is the activated semi-coke return device; 15 is the activated semi-coke return inlet; 16 is the gasifier; 17 is the gasifier gas distributor; 18 is the gasifying agent inlet; 19 is the gasifier cyclone separator; 20 is the gasified semi-coke return device; 21 is the gasified semi-coke return inlet; 22 is the ash outlet; 23 is the synthesis gas splitter; 24 is the high-temperature semi-coke return device; 25 is the high-temperature semi-coke return inlet; 26 is the circulating synthesis gas inlet; 27 is the cooling and separation unit;

[0065] A is coal; B is solid waste; C is tar; D is pyrolysis gas; E is water vapor and oxygen-containing gas; F is gasification agent; G is coarse slag; H is product synthesis gas; I is recycled synthesis gas; and J is loose gas. DETAILED DESCRIPTION

[0066] The present invention will be described in detail below with reference to specific embodiments. It is necessary to point out that the following embodiments are only used to further illustrate the present invention and are not to be construed as limiting the scope of protection of the present invention. Non-essential improvements and adjustments made by those skilled in the art to the present invention based on the contents of the present invention still fall within the scope of protection of the present invention.

[0067] Example 1

[0068] A coal and solid waste co-pyrolysis and gasification reaction device comprises a pyrolysis furnace 4, a stripping furnace 9 and a gasification furnace 16 connected in sequence; raw materials containing coal and solid waste enter the pyrolysis furnace to obtain products containing crude pyrolysis gas and crude semi-coke, the crude semi-coke enters the stripping furnace to obtain replacement gas and activated semi-coke, the activated semi-coke enters the gasification furnace to obtain synthesis gas, high-temperature semi-coke and crude slag, part of the high-temperature semi-coke returns to the bottom of the pyrolysis furnace, and part of the synthesis gas returns to the pyrolysis furnace as circulating synthesis gas.

[0069] The pyrolysis furnace 4 is provided with a raw material inlet 1 and a product outlet at the top, and a high-temperature semi-coke return inlet 25 and a circulating synthesis gas inlet 26 at the bottom; the stripping furnace is provided with a replacement gas outlet at the top, a coarse semi-coke return inlet 8 at the middle and upper part, and an activated semi-coke outlet at the bottom; the gasification furnace is provided with a gas outlet at the top, a high-temperature semi-coke outlet at the middle and upper part, an activated semi-coke return inlet 15 at the middle and lower part, and an ash outlet 22 and a gasifying agent inlet 18 at the bottom.

[0070] The product outlet of the pyrolysis furnace 4 is provided with a pyrolysis furnace cyclone separator 6, a coarse pyrolysis gas outlet is provided above the pyrolysis furnace cyclone separator 6, and a coarse semi-coke outlet is provided below the pyrolysis furnace cyclone separator 6, which is connected to the coarse semi-coke return inlet 8 of the stripping furnace through a coarse semi-coke return device 7;

[0071] The activated semi-coke outlet at the bottom of the stripping furnace 9 is provided with an activated semi-coke return device 14, and is connected to the activated semi-coke return inlet 15 of the gasifier through the activated semi-coke return device 14;

[0072] The gas outlet at the top of the gasifier 16 is connected to the gasifier cyclone separator 19, and the top of the gasifier cyclone separator 19 is provided with a synthesis gas outlet and is connected to the circulating synthesis gas inlet 26 below the pyrolysis furnace 4 through a synthesis gas diversion device; the bottom of the gasifier cyclone separator is provided with a gasified semi-coke outlet, and is connected to the gasified semi-coke return inlet 21 provided on the side wall of the gasifier through a gasified semi-coke return device 20; the gasified semi-coke return device 20 is a U-shaped return valve.

[0073] The high-temperature semi-coke outlet of the gasification furnace 16 is provided with a high-temperature semi-coke return device 24, which is connected to the high-temperature semi-coke return inlet 25 at the bottom of the pyrolysis furnace 4 through the high-temperature semi-coke return device 24. The high-temperature semi-coke return device 24 is a J-type return valve.

[0074] A draft tube 2 is provided within the pyrolysis furnace 4. The raw material inlet 1 is located above the inner pyrolysis tube of the draft tube 2. The height of the draft tube 2 is 7 / 10 of the height of the pyrolysis furnace 4, and the inner diameter of the draft tube 2 is 1 / 2 of the inner diameter of the pyrolysis furnace 4. Two rows of triangular prisms are provided within the draft tube 2, and the triangular prisms occupy 1 / 4 of the circumference of the inner wall of the draft tube 2. A pyrolysis furnace gas distributor 5 is provided horizontally at the bottom of the pyrolysis furnace 4. The pyrolysis furnace gas distributor 5 is a circular flat plate structure with air holes provided on the circular plane. The inner diameter of the draft tube divides the circular plane into an inner ring and an outer ring. The inner ring is provided with 20 inner ring air holes, each ring has 20 inner ring air holes, the inner ring air hole diameter is 10mm, and the inner ring flat plate has an open area ratio of 5%. The outer ring is provided with 10 outer ring air holes, each ring has 50 outer ring air holes, the outer ring air hole diameter is 1mm, and the outer ring flat plate has an open area ratio of 1%. The coarse semi-coke return device 7 and the activated semi-coke return device 14 are both double-cylindrical structures, with a through hole provided at the top of the outer cylinder and a porous structure at the bottom; a grid-type gap is provided at the bottom of the inner cylinder; the height of the horizontal channel at the bottom of the inner cylinder of the coarse semi-coke return device 7 and the activated semi-coke return device 14 is 1 / 5 of the height of the outer cylinder of the return device, and 4 return pipes are provided along the circumferential side wall of the upper part of the outer cylinder.

[0075] The upper portion of the stripping furnace corresponds to the coarse coke return pipe, and is provided with four coarse coke return inlets at equal intervals around the circumference; the lower portion of the gasifier corresponds to the activated coke return pipe, and is provided with four activated coke return inlets at equal intervals around the circumference. Two layers of stripping furnace baffles 11 are provided in the stripping furnace 9, and the triangular serrations of the stripping furnace baffles 11 are arranged along the circumference with six supporting ribs. The funnel cone surface of the gasifier gas distributor 17 forms an angle of 45° with the horizontal axis. The outer circle is provided with three circles of vertical nozzles with an opening rate of 2%, and the inner circle is provided with 20 circles of rotating nozzles with a rotation angle of 30° and an opening rate of 3%. The lower portion of the stripping furnace is provided with a first-level stripping gas distributor 12 and a second-level stripping gas distributor 13 from top to bottom. The stripping gas distributor includes a ventilation main pipe and three horizontal circular tubes connected to the ventilation main pipe, which are arranged in descending order. One end of the ventilation main pipe is provided with an air inlet that communicates with the air inlet pipe outside the stripping furnace. The circular tube is evenly provided with 20 air holes, which are arranged at equal intervals along the ring. The air holes have an aperture of 1mm, and the gas outlets are all downwardly facing. A gasifier gas distributor is provided at the bottom of the gasifier, and an ash outlet is provided in the middle of the bottom of the gasifier. The gasifier gas distributor includes a support plate and a gas nozzle provided on the support plate. The support plate is a funnel-shaped structure provided on the bottom plate of the gasifier, and the maximum outer edge of the upper end of the funnel-shaped structure is fixedly connected to the inner wall of the gasifier. The lower end of the funnel-shaped structure is connected to an ash channel that communicates with the ash outlet at the bottom of the gasifier.

[0076] A mixture of Inner Mongolia lignite and 5% waste plastics is added from the raw material inlet 1, mixed evenly under the action of the guide plate 3, and then falls into the bottom of the pyrolysis furnace 4, where it is mixed with the circulating synthesis gas I from the pyrolysis furnace gas distributor 5. Then, it flows in the outer tube of the guide tube 2 in parallel, at 500℃, 1.0m / s gas phase linear velocity in the pyrolysis outer tube, and 200kg / m3 average density of the bed layer in the pyrolysis outer tube. 3 Under these conditions, co-pyrolysis, tar cracking and other reactions are carried out to produce crude pyrolysis gas and crude semi-coke. The crude pyrolysis gas and crude semi-coke are discharged from the top outlet of the pyrolysis furnace 4 and enter the pyrolysis furnace cyclone separator 6. The crude pyrolysis gas is separated from the top outlet of the pyrolysis furnace cyclone separator 6 and enters the cooling and separation unit 27. The crude semi-coke is separated from the pyrolysis furnace cyclone separator 6 and enters the stripping furnace 9 through the crude semi-coke return device 7 (nitrogen enters the bottom end of the outer cylinder of the crude semi-coke return device 7, and the nitrogen inlet linear velocity corresponding to the inner cylinder area is 0.1m / s; the nitrogen inlet linear velocity corresponding to the annular area between the outer cylinder and the inner cylinder is 0.2m / s), the crude semi-coke return pipe and the crude semi-coke return inlet 8, and is mixed with the water vapor E from the first stripping gas distributor 12 and the second stripping gas distributor 13. At 500°C, a gas phase linear velocity of 0.2m / s, and an average bed density of 520kg / m 3Under the above conditions, during the stripping and activation process, the oil and gas entrained between the coarse coal coke particles and adsorbed in the coarse coal coke pores are displaced, and the pores of the coal coke are opened to obtain displacement gas and activated semi-coke. The displacement gas enters the cooling and separation unit 27 through the built-in cyclone separator 10, and the crude pyrolysis gas and the displacement gas pass through the cooling and separation unit 27 to obtain oil product C and pyrolysis gas D, wherein the oil product yield is 21%. The activated semi-coke passes through the activated semi-coke return device 14 (nitrogen enters the bottom end of the outer cylinder of the activated semi-coke return device 14, corresponding to the nitrogen inlet linear velocity of the inner cylinder area of ​​0.1m / s; corresponding to the nitrogen inlet linear velocity of the annular area between the outer cylinder and the inner cylinder of 0.2m / s) and the activated semi-coke return pipe and the activated semi-coke return inlet 15 into the bottom of the gasifier 16, at 1000℃, gas phase linear velocity of 1.0m / s, and bed average density of 300kg / m 3 Under the above conditions, the incomplete combustion and gasification reaction with the water vapor and oxygen from the gasifier gas distributor 17 is carried out to generate synthesis gas, high-temperature semi-coke and coarse slag. The coarse slag is discharged from the ash outlet at the bottom of the gasifier 16, and the carbon conversion rate reaches 98.0%. After the semi-coke is separated by the cyclone separator 17 of the gasifier, the synthesis gas enters the synthesis gas diversion device 23. The separated high-temperature semi-coke is then circulated back to the middle and lower part of the gasifier 16 through the gasification semi-coke return device 20 and the gasification semi-coke return inlet 21. Part of the high-temperature semi-coke enters the bottom of the pyrolysis furnace 4 through the high-temperature semi-coke return device 24 to provide heat for the pyrolysis furnace. The synthesis gas entering the synthesis gas diversion device 23 is divided into product synthesis gas H and circulating synthesis gas I, of which the circulating synthesis gas I is then introduced into the circulating synthesis gas inlet at the bottom of the pyrolysis furnace to provide heat, pyrolysis atmosphere and fluidizing gas for the pyrolysis furnace.

[0077] Example 2

[0078] A coal and solid waste co-pyrolysis and gasification reaction device, the differences between the device settings and Example 1 are listed in Table 1, and the settings of other parts not listed are the same.

[0079] A mixture of Inner Mongolia lignite and 5% waste plastics is added from the raw material inlet and mixed evenly under the action of the guide plate. After falling into the bottom of the pyrolysis furnace, it is mixed with the circulating synthesis gas I from the pyrolysis furnace distributor and then flows in the outer tube of the guide tube in parallel. At 500℃, the gas phase linear velocity of the pyrolysis outer tube is 1.0m / s, and the average density of the pyrolysis outer tube bed is 200kg / m 3Under these conditions, co-pyrolysis, tar cracking and other reactions are carried out to produce crude pyrolysis gas and crude semi-coke. The crude pyrolysis gas and crude semi-coke are discharged from the top outlet of the pyrolysis furnace and enter the pyrolysis furnace cyclone separator. The crude pyrolysis gas is separated from the top outlet of the pyrolysis furnace cyclone separator and enters the cooling and separation unit. The crude semi-coke is separated from the pyrolysis furnace cyclone separator and enters the stripping furnace through the crude semi-coke return device, the crude semi-coke return pipe and the crude semi-coke return inlet. It is mixed with the water vapor E from the first and second stripping gas distributors and is heated at 500°C, a gas phase linear velocity of 0.2m / s and an average bed density of 520kg / m 3 Under the conditions, during the stripping and activation process, the oil and gas entrained between the coarse coal coke particles and adsorbed in the coarse coal coke pores are displaced, and the pores of the coal coke are opened to obtain displacement gas and activated semi-coke. The displacement gas enters the cooling and separation unit through the built-in cyclone separator, and the crude pyrolysis gas and displacement gas pass through the cooling and separation unit to obtain oil product C and pyrolysis gas D, of which the oil product yield is 23%. The activated semi-coke enters the bottom of the gasifier through the activated semi-coke return device, the activated semi-coke return pipe and the activated semi-coke return inlet. At 1000℃, the gas phase linear velocity is 1.0m / s, and the average bed density is 300kg / m 3 Under these conditions, incomplete combustion and gasification reactions occur with water vapor and oxygen from the gasifier gas distributor to produce synthesis gas, high-temperature semi-coke, and coarse slag. The coarse slag is discharged from the ash outlet at the bottom of the gasifier, and the carbon conversion rate reaches 98.0%. After the semi-coke is separated by the cyclone separator of the gasifier, the synthesis gas enters the synthesis gas diversion device. The separated high-temperature semi-coke is then circulated back to the middle and lower part of the gasifier through the gasification semi-coke return device and the gasification semi-coke return inlet. Part of the high-temperature semi-coke enters the bottom of the pyrolysis furnace through the high-temperature semi-coke return device to provide heat for the pyrolysis furnace. The synthesis gas entering the synthesis gas diversion device is divided into product synthesis gas H and circulating synthesis gas I, of which the circulating synthesis gas I is then introduced into the circulating synthesis gas inlet at the bottom of the pyrolysis furnace to provide heat, pyrolysis atmosphere, and fluidizing gas for the pyrolysis furnace.

[0080] Example 3

[0081] A coal and solid waste co-pyrolysis and gasification reaction device, the differences between the device settings and Example 1 are listed in Table 1, and the settings of other parts not listed are the same.

[0082] A mixture of Inner Mongolia lignite and 5% waste plastics is added from the raw material inlet and mixed evenly under the action of the guide plate. After falling into the bottom of the pyrolysis furnace, it is mixed with the circulating synthesis gas I from the pyrolysis furnace distributor and then flows in the outer tube of the guide tube in parallel. At 500℃, the gas phase linear velocity of the pyrolysis outer tube is 1.0m / s, and the average density of the pyrolysis outer tube bed is 200kg / m 3Under these conditions, co-pyrolysis, tar cracking and other reactions are carried out to produce crude pyrolysis gas and crude semi-coke. The crude pyrolysis gas and crude semi-coke are discharged from the top outlet of the pyrolysis furnace and enter the pyrolysis furnace cyclone separator. The crude pyrolysis gas is separated from the top outlet of the pyrolysis furnace cyclone separator and enters the cooling and separation unit. The crude semi-coke is separated from the pyrolysis furnace cyclone separator and enters the stripping furnace through the crude semi-coke return device, the crude semi-coke return pipe and the crude semi-coke return inlet. It is mixed with the water vapor E from the first and second stripping gas distributors and is heated at 500°C, a gas phase linear velocity of 0.2m / s and an average bed density of 520kg / m 3 Under the conditions, during the stripping and activation process, the oil and gas entrained between the coarse coal coke particles and adsorbed in the coarse coal coke pores are displaced, and the pores of the coal coke are opened to obtain displacement gas and activated semi-coke. The displacement gas enters the cooling and separation unit through the built-in cyclone separator, and the crude pyrolysis gas and displacement gas pass through the cooling and separation unit to obtain oil product C and pyrolysis gas D, of which the oil product yield is 24%. The activated semi-coke enters the bottom of the gasifier through the activated semi-coke return device, the activated semi-coke return pipe and the activated semi-coke return inlet. At 1000℃, the gas phase linear velocity is 1.0m / s, and the average bed density is 300kg / m 3 Under these conditions, incomplete combustion and gasification reactions occur with water vapor and oxygen from the gasifier gas distributor to produce synthesis gas, high-temperature semi-coke, and coarse slag. The coarse slag is discharged from the ash outlet at the bottom of the gasifier, and the carbon conversion rate reaches 98.0%. After the semi-coke is separated by the cyclone separator of the gasifier, the synthesis gas enters the synthesis gas diversion device. The separated high-temperature semi-coke is then circulated back to the middle and lower part of the gasifier through the gasification semi-coke return device and the gasification semi-coke return inlet. Part of the high-temperature semi-coke enters the bottom of the pyrolysis furnace through the high-temperature semi-coke return device to provide heat for the pyrolysis furnace. The synthesis gas entering the synthesis gas diversion device is divided into product synthesis gas H and circulating synthesis gas I, of which the circulating synthesis gas I is then introduced into the circulating synthesis gas inlet at the bottom of the pyrolysis furnace to provide heat, pyrolysis atmosphere, and fluidizing gas for the pyrolysis furnace.

[0083] Example 4

[0084] A coal and solid waste co-pyrolysis and gasification reaction device, the differences between the device settings and Example 1 are listed in Table 1, and the settings of other parts not listed are the same.

[0085] A mixture of Inner Mongolia lignite and 5% waste plastics is added from the raw material inlet and mixed evenly under the action of the guide plate. After falling into the bottom of the pyrolysis furnace, it is mixed with the circulating synthesis gas I from the pyrolysis furnace distributor and then flows in the outer tube of the guide tube in parallel. At 500℃, the gas phase linear velocity of the pyrolysis outer tube is 1.0m / s, and the average density of the pyrolysis outer tube bed is 200kg / m 3Under these conditions, co-pyrolysis, tar cracking and other reactions are carried out to produce crude pyrolysis gas and crude semi-coke. The crude pyrolysis gas and crude semi-coke are discharged from the top outlet of the pyrolysis furnace and enter the pyrolysis furnace cyclone separator. The crude pyrolysis gas is separated from the top outlet of the pyrolysis furnace cyclone separator and enters the cooling and separation unit. The crude semi-coke is separated from the pyrolysis furnace cyclone separator and enters the stripping furnace through the crude semi-coke return device, the crude semi-coke return pipe and the crude semi-coke return inlet. It is mixed with the water vapor E from the first and second stripping gas distributors and is heated at 500°C, a gas phase linear velocity of 0.2m / s and an average bed density of 520kg / m 3 Under the conditions, during the stripping and activation process, the oil and gas entrained between the coarse coal coke particles and adsorbed in the coarse coal coke pores are displaced, and the pores of the coal coke are opened to obtain displacement gas and activated semi-coke. The displacement gas enters the cooling and separation unit through the built-in cyclone separator, and the crude pyrolysis gas and displacement gas pass through the cooling and separation unit to obtain oil product C and pyrolysis gas D, of which the oil product yield is 23%. The activated semi-coke enters the bottom of the gasifier through the activated semi-coke return device, the activated semi-coke return pipe and the activated semi-coke return inlet. At 1000℃, the gas phase linear velocity is 1.0m / s, and the average bed density is 300kg / m 3 Under these conditions, incomplete combustion and gasification reactions occur with water vapor and oxygen from the gasifier gas distributor to produce synthesis gas, high-temperature semi-coke, and coarse slag. The coarse slag is discharged from the ash outlet at the bottom of the gasifier, and the carbon conversion rate reaches 98.5%. After the semi-coke is separated by the cyclone separator of the gasifier, the synthesis gas enters the synthesis gas diversion device. The separated high-temperature semi-coke is then circulated back to the middle and lower part of the gasifier through the gasification semi-coke return device and the gasification semi-coke return inlet. Part of the high-temperature semi-coke enters the bottom of the pyrolysis furnace through the high-temperature semi-coke return device to provide heat for the pyrolysis furnace. The synthesis gas entering the synthesis gas diversion device is divided into product synthesis gas H and circulating synthesis gas I, of which the circulating synthesis gas I is then introduced into the circulating synthesis gas inlet at the bottom of the pyrolysis furnace to provide heat, pyrolysis atmosphere, and fluidizing gas for the pyrolysis furnace.

[0086] Example 5

[0087] A coal and solid waste co-pyrolysis and gasification reaction device, the differences between the device settings and Example 1 are listed in Table 1, and the settings of other parts not listed are the same.

[0088] A mixture of Inner Mongolia lignite and 5% waste plastics is added from the raw material inlet and mixed evenly under the action of the guide plate. After falling into the bottom of the pyrolysis furnace, it is mixed with the circulating synthesis gas I from the pyrolysis furnace distributor and then flows in the outer tube of the guide tube in parallel. At 500℃, the gas phase linear velocity of the pyrolysis outer tube is 1.0m / s, and the average density of the pyrolysis outer tube bed is 200kg / m 3Under these conditions, co-pyrolysis, tar cracking and other reactions are carried out to produce crude pyrolysis gas and crude semi-coke. The crude pyrolysis gas and crude semi-coke are discharged from the top outlet of the pyrolysis furnace and enter the pyrolysis furnace cyclone separator. The crude pyrolysis gas is separated from the top outlet of the pyrolysis furnace cyclone separator and enters the cooling and separation unit. The crude semi-coke is separated from the pyrolysis furnace cyclone separator and enters the stripping furnace through the crude semi-coke return device, the crude semi-coke return pipe and the crude semi-coke return inlet. It is mixed with the water vapor E from the first and second stripping gas distributors and is heated at 500°C, a gas phase linear velocity of 0.2m / s and an average bed density of 520kg / m 3 Under the conditions, during the stripping and activation process, the oil and gas entrained between the coarse coal coke particles and adsorbed in the coarse coal coke pores are displaced, and the pores of the coal coke are opened to obtain displacement gas and activated semi-coke. The displacement gas enters the cooling and separation unit through the built-in cyclone separator, and the crude pyrolysis gas and displacement gas pass through the cooling and separation unit to obtain oil product C and pyrolysis gas D, of which the oil product yield is 21%. The activated semi-coke enters the bottom of the gasifier through the activated semi-coke return device, the activated semi-coke return pipe and the activated semi-coke return inlet. At 1000℃, the gas phase linear velocity is 1.0m / s, and the average bed density is 300kg / m 3 Under these conditions, incomplete combustion and gasification reactions occur with water vapor and oxygen from the gasifier gas distributor to produce synthesis gas, high-temperature semi-coke, and coarse slag. The coarse slag is discharged from the ash outlet at the bottom of the gasifier, and the carbon conversion rate reaches 99.0%. After the semi-coke is separated by the cyclone separator of the gasifier, the synthesis gas enters the synthesis gas diversion device. The separated high-temperature semi-coke is then circulated back to the middle and lower part of the gasifier through the gasification semi-coke return device and the gasification semi-coke return inlet. Part of the high-temperature semi-coke enters the bottom of the pyrolysis furnace through the high-temperature semi-coke return device to provide heat for the pyrolysis furnace. The synthesis gas entering the synthesis gas diversion device is divided into product synthesis gas H and circulating synthesis gas I, of which the circulating synthesis gas I is then introduced into the circulating synthesis gas inlet at the bottom of the pyrolysis furnace to provide heat, pyrolysis atmosphere, and fluidizing gas for the pyrolysis furnace.

[0089] Example 6

[0090] A coal and solid waste co-pyrolysis and gasification reaction device, the differences between the device settings and Example 1 are listed in Table 1, and the settings of other parts not listed are the same.

[0091] A mixture of Inner Mongolia lignite and 5% waste plastics is added from the raw material inlet and mixed evenly under the action of the guide plate. After falling into the bottom of the pyrolysis furnace, it is mixed with the circulating synthesis gas I from the pyrolysis furnace distributor and then flows in the outer tube of the guide tube in parallel. At 600℃, the gas phase linear velocity of the pyrolysis outer tube is 1.0m / s, and the average density of the pyrolysis outer tube bed is 200kg / m 3Under these conditions, co-pyrolysis, tar cracking and other reactions are carried out to produce crude pyrolysis gas and crude semi-coke. The crude pyrolysis gas and crude semi-coke are discharged from the top outlet of the pyrolysis furnace and enter the pyrolysis furnace cyclone separator. The crude pyrolysis gas is separated from the top outlet of the pyrolysis furnace cyclone separator and enters the cooling and separation unit. The crude semi-coke is separated from the pyrolysis furnace cyclone separator and enters the stripping furnace through the crude semi-coke return device, the crude semi-coke return pipe and the crude semi-coke return inlet. It is mixed with the water vapor E from the first and second stripping gas distributors and is heated at 500°C, a gas phase linear velocity of 0.2m / s and an average bed density of 520kg / m 3 Under the conditions, during the stripping and activation process, the oil and gas entrained between the coarse coal coke particles and adsorbed in the coarse coal coke pores are displaced, and the pores of the coal coke are opened to obtain displacement gas and activated semi-coke. The displacement gas enters the cooling and separation unit through the built-in cyclone separator, and the crude pyrolysis gas and displacement gas pass through the cooling and separation unit to obtain oil product C and pyrolysis gas D, of which the oil product yield is 17%. The activated semi-coke enters the bottom of the gasifier through the activated semi-coke return device, the activated semi-coke return pipe and the activated semi-coke return inlet. At 1000℃, the gas phase linear velocity is 1.0m / s, and the average bed density is 300kg / m 3 Under these conditions, incomplete combustion and gasification reactions occur with water vapor and oxygen from the gasifier gas distributor to produce synthesis gas, high-temperature semi-coke, and coarse slag. The coarse slag is discharged from the ash outlet at the bottom of the gasifier, and the carbon conversion rate reaches 98.0%. After the semi-coke is separated by the cyclone separator of the gasifier, the synthesis gas enters the synthesis gas diversion device. The separated high-temperature semi-coke is then circulated back to the middle and lower part of the gasifier through the gasification semi-coke return device and the gasification semi-coke return inlet. Part of the high-temperature semi-coke enters the bottom of the pyrolysis furnace through the high-temperature semi-coke return device to provide heat for the pyrolysis furnace. The synthesis gas entering the synthesis gas diversion device is divided into product synthesis gas H and circulating synthesis gas I, of which the circulating synthesis gas I is then introduced into the circulating synthesis gas inlet at the bottom of the pyrolysis furnace to provide heat, pyrolysis atmosphere, and fluidizing gas for the pyrolysis furnace.

[0092] Example 7

[0093] A coal and solid waste co-pyrolysis and gasification reaction device, the differences between the device settings and Example 1 are listed in Table 1, and the settings of other parts not listed are the same.

[0094] A mixture of Inner Mongolia lignite and 5% waste plastics is added from the raw material inlet and mixed evenly under the action of the guide plate. After falling into the bottom of the pyrolysis furnace, it is mixed with the circulating synthesis gas I from the pyrolysis furnace distributor and then flows in the outer tube of the guide tube in parallel. At 500℃, the gas phase linear velocity of the pyrolysis outer tube is 1.0m / s, and the average density of the pyrolysis outer tube bed is 200kg / m 3Under these conditions, co-pyrolysis, tar cracking and other reactions are carried out to produce crude pyrolysis gas and crude semi-coke. The crude pyrolysis gas and crude semi-coke are discharged from the top outlet of the pyrolysis furnace and enter the pyrolysis furnace cyclone separator. The crude pyrolysis gas is separated from the top outlet of the pyrolysis furnace cyclone separator and enters the cooling and separation unit. The crude semi-coke is separated from the pyrolysis furnace cyclone separator and enters the stripping furnace through the crude semi-coke return device, the crude semi-coke return pipe and the crude semi-coke return inlet. It is mixed with the water vapor E from the first and second stripping gas distributors and is heated at 500°C, a gas phase linear velocity of 0.3m / s and an average bed density of 500kg / m 3 Under the conditions, during the stripping and activation process, the oil and gas entrained between the coarse coal coke particles and adsorbed in the coarse coal coke pores are displaced, and the pores of the coal coke are opened to obtain displacement gas and activated semi-coke. The displacement gas enters the cooling and separation unit through the built-in cyclone separator, and the crude pyrolysis gas and displacement gas pass through the cooling and separation unit to obtain oil product C and pyrolysis gas D, of which the oil product yield is 24%. The activated semi-coke enters the bottom of the gasifier through the activated semi-coke return device, the activated semi-coke return pipe and the activated semi-coke return inlet. At 1000℃, the gas phase linear velocity is 1.0m / s, and the average bed density is 300kg / m 3 Under these conditions, incomplete combustion and gasification reactions occur with water vapor and oxygen from the gasifier gas distributor to produce synthesis gas, high-temperature semi-coke, and coarse slag. The coarse slag is discharged from the ash outlet at the bottom of the gasifier, and the carbon conversion rate reaches 98.9%. After the semi-coke is separated by the cyclone separator of the gasifier, the synthesis gas enters the synthesis gas diversion device. The separated high-temperature semi-coke is then circulated back to the middle and lower part of the gasifier through the gasification semi-coke return device and the gasification semi-coke return inlet. Part of the high-temperature semi-coke enters the bottom of the pyrolysis furnace through the high-temperature semi-coke return device to provide heat for the pyrolysis furnace. The synthesis gas entering the synthesis gas diversion device is divided into product synthesis gas H and circulating synthesis gas I, of which the circulating synthesis gas I is then introduced into the circulating synthesis gas inlet at the bottom of the pyrolysis furnace to provide heat, pyrolysis atmosphere, and fluidizing gas for the pyrolysis furnace.

[0095] Example 8

[0096] A coal and solid waste co-pyrolysis and gasification reaction device, the differences between the device settings and Example 1 are listed in Table 1, and the settings of other parts not listed are the same.

[0097] A mixture of Inner Mongolia lignite and 5% waste plastics is added from the raw material inlet and mixed evenly under the action of the guide plate. After falling into the bottom of the pyrolysis furnace, it is mixed with the circulating synthesis gas I from the pyrolysis furnace distributor and then flows in the outer tube of the guide tube in parallel. At 500℃, the gas phase linear velocity of the pyrolysis outer tube is 1.0m / s, and the average density of the pyrolysis outer tube bed is 200kg / m 3Under these conditions, co-pyrolysis, tar cracking and other reactions are carried out to produce crude pyrolysis gas and crude semi-coke. The crude pyrolysis gas and crude semi-coke are discharged from the top outlet of the pyrolysis furnace and enter the pyrolysis furnace cyclone separator. The crude pyrolysis gas is separated from the top outlet of the pyrolysis furnace cyclone separator and enters the cooling and separation unit. The crude semi-coke is separated from the pyrolysis furnace cyclone separator and enters the stripping furnace through the crude semi-coke return device, the crude semi-coke return pipe and the crude semi-coke return inlet. It is mixed with the water vapor E from the first and second stripping gas distributors and is heated at 500°C, a gas phase linear velocity of 0.2m / s and an average bed density of 520kg / m 3 Under the conditions, during the stripping and activation process, the oil and gas entrained between the coarse coal coke particles and adsorbed in the coarse coal coke pores are displaced, and the pores of the coal coke are opened to obtain displacement gas and activated semi-coke. The displacement gas enters the cooling and separation unit through the built-in cyclone separator, and the crude pyrolysis gas and displacement gas pass through the cooling and separation unit to obtain oil product C and pyrolysis gas D, of which the oil product yield is 21%. The activated semi-coke enters the bottom of the gasifier through the activated semi-coke return device, the activated semi-coke return pipe and the activated semi-coke return inlet. At 1100℃, the gas phase linear velocity is 1.0m / s, and the average bed density is 300kg / m 3 Under these conditions, incomplete combustion and gasification reactions occur with water vapor and oxygen from the gas distributor of the gasifier to produce synthesis gas, high-temperature semi-coke and coarse slag. The coarse slag is discharged from the ash outlet at the bottom of the gasifier, and the carbon conversion rate reaches 99.5%. After the semi-coke is separated by the cyclone separator of the gasifier, the synthesis gas enters the synthesis gas diversion device. The separated high-temperature semi-coke is then circulated back to the middle and lower part of the gasifier through the gasification semi-coke return device and the gasification semi-coke return inlet. Part of the high-temperature semi-coke enters the bottom of the pyrolysis furnace through the high-temperature semi-coke return device to provide heat for the pyrolysis furnace. The synthesis gas entering the synthesis gas diversion device is divided into product synthesis gas H and circulating synthesis gas I, of which the circulating synthesis gas I is then introduced into the circulating synthesis gas inlet at the bottom of the pyrolysis furnace to provide heat, pyrolysis atmosphere and fluidizing gas for the pyrolysis furnace.

[0098] Specific example parameters and product data are shown in Table 1 and Table 2.

[0099] Table 1

[0100]

[0101]

[0102] Table 2

[0103]

[0104] Due to the long residence time of the coal and solid waste within the pyrolysis furnace, they are fully pyrolyzed in the syngas atmosphere. The stripping action displaces oil and gas trapped between the coarse semi-coke particles and adsorbed within the pores of the coarse semi-coke, achieving a high tar yield exceeding 20%. The pyrolysis gas is rich in H2 and CH4. Activated semi-coke significantly enhances its reactivity. Driven by the wall jets and central swirling flow within the gasifier, it reacts with the gasifying agent to produce syngas rich in CO and H2. This significantly increases the carbon conversion rate to over 98%.

[0105] Comparative Example 1

[0106] Coal and waste plastics were co-pyrolyzed in a coke oven at a pyrolysis temperature of 800°C. The products were semi-coke, pyrolysis gas and tar. The co-pyrolysis yield of tar oil was 11.1%, the semi-coke yield was 68.5%, and the pyrolysis gas contained 61.44% H2, 13.53% CH4, 8.55% CO, 2.48 CO2, and the rest N2.

[0107] Compared with the examples in this application, the examples of this application use the aforementioned coal and solid waste co-pyrolysis gasification reaction device to treat a mixture of Inner Mongolia lignite and 5% waste plastics for co-pyrolysis to obtain a tar yield of more than 17% (the yield in Example 6 is the lowest, at 17%, so it is best to change it to more than 17% here). Most of the pyrolysis gas can reach H2: 59%, CH4: 27%, CO: 9%, CO2: 5%, and the tar yield and pyrolysis gas quality are greatly increased. Most of the synthesis gas obtained by activated semi-coke gasification can reach H2: 35%, CO: 56%, CO2: 8%, CH4: 1%, and the carbon conversion rate reaches more than 98%.

Claims

1. A coal and solid waste co-pyrolysis and gasification reaction device, comprising a pyrolysis furnace, a stripping furnace, and a gasifier connected in sequence; raw materials comprising coal and solid waste enter the pyrolysis furnace to produce products comprising crude pyrolysis gas and crude semi-coke; the crude semi-coke enters the stripping furnace to produce displacement gas and activated semi-coke; the activated semi-coke enters the gasifier to produce synthesis gas, high-temperature semi-coke, and crude slag; a portion of the high-temperature semi-coke is returned to the bottom of the pyrolysis furnace, and a portion of the synthesis gas is returned to the pyrolysis furnace as recycled synthesis gas; The stripping furnace is provided with a coarse semi-coke return material inlet at the upper middle part, and an activated semi-coke outlet at the bottom; the pyrolysis furnace is provided with a raw material inlet and a product outlet at the top, and a high-temperature semi-coke return material inlet and a circulating synthesis gas inlet at the bottom; a guide tube is provided in the pyrolysis furnace, and the guide tube is a cylindrical structure with open ends, the upper port of the guide tube is connected to the top of the pyrolysis furnace, and the lower port of the guide tube is placed in the pyrolysis furnace; the guide tube divides the pyrolysis furnace into an inner pyrolysis tube and an outer pyrolysis tube; the inner wall of the guide tube is provided with multiple rows of triangular prisms; a pyrolysis furnace gas distributor is provided horizontally at the bottom of the pyrolysis furnace, and the pyrolysis furnace gas distributor is used for the transition of materials from the inner pyrolysis tube to the outer pyrolysis tube and for the pyrolysis furnace to pass through the pyrolysis tube. The outer cylinder area is fluidized and mixed uniformly; the raw material inlet of the pyrolysis furnace is located at the upper port of the pyrolysis inner cylinder of the guide cylinder, and the product outlet of the pyrolysis furnace is arranged on the pyrolysis outer cylinder, and is communicated with the space between the pyrolysis inner cylinder and the pyrolysis outer cylinder; the product outlet of the pyrolysis furnace is provided with a pyrolysis furnace cyclone separator, and a coarse semi-coke outlet is provided below the pyrolysis furnace cyclone separator, and is connected to the coarse semi-coke return inlet of the stripping furnace through a coarse semi-coke return device; the activated semi-coke outlet at the bottom of the stripping furnace is provided with an activated semi-coke return device, and the middle and lower part of the gasifier is provided with an activated semi-coke return inlet, and the activated semi-coke outlet is connected to the activated semi-coke return inlet of the gasifier through the activated semi-coke return device; The coarse semi-coke return device and / or activated semi-coke return device is an inner and outer double-cylindrical structure, and an air inlet is provided at the bottom end of the outer cylinder; a plurality of return pipes are provided on the upper side wall of the outer cylinder, which are connected to the coarse semi-coke return inlet of the stripping furnace or the activated semi-coke return inlet of the gasification furnace; a plurality of coarse semi-coke return inlets are provided along the circumference of the cross section of the stripping furnace, corresponding to the return pipes of the coarse semi-coke return device; a plurality of activated semi-coke return inlets are provided along the circumference of the cross section of the gasification furnace, corresponding to the return pipes of the activated semi-coke return device.

2. The device according to claim 1, characterized in that The stripping furnace is provided with a replacement gas outlet at the top; the gasification furnace is provided with a gas outlet at the top, a high-temperature semi-coke outlet at the middle and upper part, and an ash outlet and a gasifying agent inlet at the bottom.

3. The device according to claim 1, characterized in that A coarse pyrolysis gas outlet is provided above the pyrolysis furnace cyclone separator; and / or, The gas outlet at the top of the gasifier is connected to the gasifier cyclone separator, the top of the gasifier cyclone separator is provided with a synthesis gas outlet and is connected to the circulating synthesis gas inlet below the pyrolysis furnace through a synthesis gas splitter; the bottom of the gasifier cyclone separator is provided with a gasified semi-coke outlet and is connected to the gasified semi-coke return inlet provided on the side wall of the gasifier through a gasified semi-coke return device; and / or, The high-temperature semi-coke outlet of the gasification furnace is provided with a high-temperature semi-coke return device, and is connected to the high-temperature semi-coke return inlet at the bottom of the pyrolysis furnace through the high-temperature semi-coke return device.

4. The device according to claim 3, characterized in that The top of the outer cylinder of the coarse coke return device and / or the activated coke return device is provided with a through hole; the bottom of the inner cylinder of the coarse coke return device and / or the activated coke return device is provided with a gap, and the top is provided with a feed port connected to the coarse coke outlet or the activated coke outlet, the feed port passes through the top through hole of the outer cylinder and the outer wall thereof is connected with the inner wall of the top through hole of the outer cylinder; the inner cylinder divides the return device into an inner cylinder space and an outer cylinder space, and a space is left between the bottom of the inner cylinder and the bottom end of the outer cylinder to form a horizontal channel; and / or, The upper side wall of the outer cylinder is provided with 2 to 6 return pipes, which are connected to the raw coke return inlet of the stripping furnace or the activated coke return inlet of the gasification furnace.

5. The device according to claim 4, characterized in that The outer wall of the feed port at the top end of the inner cylinder of the coarse semi-coke returning device and / or the activated semi-coke returning device is sealed and fixedly connected to the inner wall of the through hole at the top end of the outer cylinder.

6. The device according to claim 4, characterized in that The height of the horizontal channel is 1 / 5 to 3 / 5 of the height of the outer cylinder of the return device.

7. The device according to claim 4, characterized in that The coarse coke return inlet of the stripping furnace corresponds to the return pipe of the coarse coke return device, and 2 to 6 coarse coke return inlets are arranged at equal intervals along the circumference of the cross section of the stripping furnace; and / or, The activated semi-coke return inlet of the gasifier corresponds to the return pipe of the activated semi-coke return device, and 2 to 6 activated semi-coke return inlets are arranged at equal intervals along the circumference of the gasifier cross section.

8. The device according to claim 1, characterized in that The guide tube is a coaxial guide tube.

9. The device according to claim 8, characterized in that The inner wall of the guide tube is provided with 2 to 4 rows of triangular prisms; and / or, The height of the guide tube is 1 / 10 to 9 / 10 of the height of the pyrolysis furnace; and / or, The inner diameter of the guide tube is 1 / 5 to 3 / 5 of the inner diameter of the pyrolysis furnace.

10. The device according to claim 9, characterized in that The triangular prism occupies 1 / 4 to 1 / 2 of the circumference of the inner wall of the guide tube.

11. The device according to claim 9, characterized in that Different rows of triangular prisms are staggered at different heights along the guide tube.

12. The device according to claim 1, characterized in that The pyrolysis furnace gas distributor is a circular flat plate structure, the outer circumference of which is fixedly connected to the inner wall of the bottom of the pyrolysis furnace. The circular flat plate is provided with air holes, which are evenly arranged along the circumference and in the radial direction. When a guide tube is provided inside the pyrolysis furnace, the circular flat plate is divided into an inner ring and an outer ring, the outer diameter of the inner ring corresponds to the inner diameter of the guide tube, the opening rate of the inner ring flat plate is 3-5%, and the opening rate of the outer ring flat plate is 0.5-3%.

13. The device according to claim 12, characterized in that The inner ring is provided with 10 to 50 circles of inner ring air holes, each circle is provided with 20 to 50 inner ring air holes, and the inner ring air holes have an aperture of 5 to 10 mm; the outer ring is provided with 10 to 50 circles of outer ring air holes, each circle is provided with 50 to 100 outer ring air holes, and the outer ring air holes have an aperture of 0.5 to 3 mm.

14. The device according to claim 1, characterized in that The stripping furnace is provided with 1 to 5 layers of stripping furnace baffles, each layer of stripping furnace baffles includes coaxially crossed supporting ribs and both ends of which are connected to the inner wall of the stripping furnace, and baffles connecting adjacent supporting ribs; each baffle is provided with a plurality of pairs of triangular sawtooth structures facing each other on both sides, the top angles of the triangular sawtooth structures are all facing the bottom of the stripping furnace, the triangular sawtooth structure on one side is inclined outward, and the triangular sawtooth structure on the other side is inclined inward; a gap is left between the inward-inclined triangular sawtooth structures and the outward-inclined triangular sawtooth structures between adjacent baffles.

15. The device according to claim 14, characterized in that The support ribs evenly divide the cross section of the stripping furnace; and / or, There are more than two supporting ribs; and / or, The barrier strips are provided at least one along the radial direction of the support rib; and / or, Each of the baffles is provided with 1 to 10 pairs of triangular sawtooth structures; and / or, Each layer of the stripping furnace baffle includes 50 to 200 pairs of triangular sawtooth structures.

16. The device according to claim 15, characterized in that The number of the supporting ribs is 3 to 6; and / or, The number of the blocking bars is 4 to 10 along the radial direction of the supporting rib.

17. The device according to claim 1, characterized in that A plurality of stripping gas distributors are sequentially arranged at the lower part of the stripping furnace from top to bottom, and the stripping gas distributors include a ventilation main pipe and horizontal circular ring pipes connected to the ventilation main pipe and arranged in descending order; an air inlet is provided at one end of the ventilation main pipe and communicates with the air inlet pipe outside the stripping furnace; 20 to 100 air holes are evenly arranged on the circular pipe, and the air holes are arranged at equal intervals along the circular ring, with an air hole diameter of 1 to 10 mm, and the gas outlets are all arranged downward.

18. The device according to claim 17, characterized in that The lower part of the stripping furnace is provided with 2 to 3 stripping gas distributors in sequence from top to bottom.

19. The device according to claim 17, characterized in that There are 4 to 10 circular tubes.

20. The device according to claim 1, wherein A gasifier gas distributor is provided at the bottom of the gasifier, and the gasifier gas distributor includes a support plate and a gas nozzle provided on the support plate; the support plate is a funnel-shaped structure provided on the bottom plate of the gasifier, and the maximum outer edge of the upper end of the funnel-shaped structure is fixedly connected to the inner wall of the gasifier; the lower end of the funnel-shaped structure is connected to an ash channel which is connected to the ash outlet at the bottom of the gasifier; the gasifying agent inlet of the gasifier is connected to the space formed between the funnel-shaped structure of the gasifier gas distributor and the inner wall of the gasifier.

21. The device according to claim 20, characterized in that The gasifier gas distributor is a funnel structure of a support plate, and the funnel cone forms an angle of less than or equal to 60° with the horizontal axis; and / or, The gas nozzles of the gasifier gas distributor support plate are all distributed in concentric circles on the support plate funnel cone surface that are radially arranged with the same axis as the gasifier.

22. The device according to claim 21, characterized in that The funnel cone surface of the funnel structure of the gasifier gas distributor forms an angle of 15° to 45° with the horizontal axis.

23. The device according to claim 21, characterized in that The funnel cone surface of the gasifier gas distributor support plate is divided into an inner ring and an outer ring. A vertical nozzle is arranged on the outer ring. The opening rate of the outer ring is 1-5%; the opening rate of the inner ring is 3-5%.

24. The device according to claim 23, characterized in that The nozzle spacing in each circle is the same.

25. The device according to claim 23, characterized in that The outer ring is provided with 1 to 10 circles of vertical nozzles; and / or each circle has 50 to 100 nozzles.

26. The device according to any one of claims 1 to 25, characterized in that It also includes a cooling and separation unit connected to the pyrolysis furnace and / or stripping furnace pipeline.

27. The device according to claim 26, characterized in that The pyrolysis gas outlet of the pyrolysis furnace cyclone separator and / or the replacement gas outlet of the stripping furnace are respectively connected to the air inlet of the cooling and separation unit. The crude pyrolysis gas from the pyrolysis furnace cyclone separator and / or the replacement gas from the stripping furnace pass through the cooling and separation unit to obtain tar and pyrolysis gas.

28. A method for treating a co-pyrolysis and gasification reaction of coal and solid waste using the device according to any one of claims 1 to 27, comprising: The raw materials enter the pyrolysis furnace and are evenly mixed under the action of multiple rows of triangular prisms. After falling into the bottom of the pyrolysis furnace, they are mixed and contacted with the circulating synthesis gas, and then flow upward in the outer tube of the guide tube to produce co-pyrolysis reaction to generate crude pyrolysis gas and crude semi-coke. The crude semi-coke passes through the pyrolysis furnace cyclone separator, the crude semi-coke return device, the crude semi-coke return pipe and the crude semi-coke return inlet in sequence to enter the stripping furnace for stripping and activation to obtain replacement gas and activated semi-coke. The crude pyrolysis gas and the replacement gas are separated to obtain oil products and pyrolysis gas; the activated semi-coke passes through the activated semi-coke return device, the activated semi-coke return pipe and the activated semi-coke return inlet in sequence to enter the gasification furnace for incomplete combustion and gasification reaction with the gasifying agent from the gasification furnace to generate synthesis gas, high-temperature semi-coke and coarse slag; part of the high-temperature semi-coke returns to the bottom of the pyrolysis furnace, and part of the synthesis gas returns to the pyrolysis furnace as circulating synthesis gas.

29. The method according to claim 28, characterized in that The reaction temperature of the pyrolysis furnace is 400-700°C, the gas phase linear velocity of the pyrolysis inner cylinder is 0.1-0.5 m / s, the gas phase linear velocity of the pyrolysis outer cylinder is 0.5-2.0 m / s, and the average density of the reactant bed of the pyrolysis outer cylinder is 150-300 kg / m 3 and / or, The stripping furnace reaction temperature is 350-550°C, the gas phase linear velocity is 0.1-1m / s, and the average bed density is 250-600kg / m 3 and / or, The reaction temperature of the gasifier is 700-1200°C, the gas phase linear velocity is 0.2-2m / s, and the average bed density is 150-450kg / m 3 and / or, The system reaction pressure range of the co-pyrolysis and gasification reaction device is 0.1 to 10.0 MPa.

30. The method according to claim 28, wherein The gas velocity at the outlet of the inner circle pores of the pyrolysis furnace gas distributor is 5-20 m / s, and the gas velocity at the outlet of the outer circle pores is 10-50 m / s; and / or, The linear velocity of the loosening gas corresponding to the bottom of the inner cylinder space of the coarse coke returning device and the activated coke returning device is 0.05-0.2 m / s, and the linear velocity of the loosening gas corresponding to the bottom of the outer cylinder space is 0.02-0.4 m / s; and / or, Water vapor is introduced into the stripping gas distributor, the water vapor temperature is 200-500° C., and the gas velocity at the stripping gas distributor pore outlet is 2-20 m / s; and / or, The gas velocity at the outlet of the vertical nozzle of the gasifier gas distributor is 10 to 50 m / s; and / or, The gasifying agent comprises one of an oxygen-containing gas, a mixture of an oxygen-containing gas and water vapor, or a mixture of an oxygen-containing gas, water vapor and CO2; and / or, The temperature of the gasifying agent is 200-800°C.

31. The method according to claim 30, wherein The oxygen-containing gas includes oxygen, air or a mixture thereof.

32. The method according to claim 31, characterized in that The molar ratio of oxygen in the gasifying agent to carbon in the semi-coke in the gasifier is 0.5-1.0 mol / mol, and the molar ratio of water vapor in the gasifying agent to carbon in the semi-coke in the gasifier is 0.5-5.0 mol / mol.

33. The method according to any one of claims 28 to 32, characterized in that The weight ratio of solid waste to coal in the raw materials is (3-10):

100.

34. Use of the coal and solid waste co-pyrolysis and gasification reaction device according to any one of claims 1 to 27 or the method according to any one of claims 28 to 33 in a coal and solid waste co-pyrolysis and gasification reaction.

35. The use according to claim 34, characterized in that The coal includes at least one of lignite, bituminous coal, anthracite and peat, and the solid waste includes at least one of waste plastic and waste rubber.

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