Gas-solid sensible heat recovery integrated device and recovery method of by-product superheated steam

Abstract

The application discloses a gas-solid sensible heat recovery integrated device with by-product superheated steam and a recovery method, and belongs to the technical field of industrial waste heat recovery. The application solves the technical problem of sensible heat waste in the treatment mode of all or part of quenching of a large amount of sensible heat carried by crude synthesis gas and high-temperature ash slag. The upper part of the outer cylinder membrane type wall is connected and sealed with a pressure-bearing shell. Gas inlets are arranged on the upper parts of two sides of the pressure-bearing shell and are communicated with the outer cylinder membrane type wall. The inner cylinder membrane type wall is connected and sealed with the upper part of the outer cylinder membrane type wall. The upper end and the lower end of the inner cavity of the inner cylinder water cooling wall are both arranged as open. A superheater and low-temperature evaporation pipe bundles are arranged in the inner cylinder membrane type wall. The superheater is located below the low-temperature evaporation pipe bundles. An ash slag cooling chamber is located below the outer cylinder membrane type wall. The upper end of the ash slag cooling chamber is connected and sealed with the lower end of the outer cylinder membrane type wall. The bottom of the pressure-bearing shell is provided with an ash outlet. The lower end of the ash slag cooling chamber is connected and sealed with the ash outlet. The energy raw material utilization rate is high. The application is used for industrial waste heat recovery.

Description

TECHNICAL FIELD

[0001] The present application relates to a kind of gas-solid sensible heat recovery integrated device and recovery method of by-product superheated steam, belong to industrial waste heat recovery technical field. BACKGROUND

[0002] Coal, biomass, petroleum coke, domestic waste and other carbon-containing raw materials are used for heat conversion and utilization by gasification technology, which is an important basic technology for modern coal chemical industry, green methanol and large-scale industrial production of aviation oil. The crude synthesis gas and high-temperature ash produced in the gasification process carry a large amount of sensible heat. The traditional technology uses all or part of the cooling method to cool down, which causes waste of high-quality sensible heat and generates a large amount of black water that needs to be treated. The black water circulation also causes equipment and pipeline wear and blockage problems. The cost of filter cake ash treatment is relatively high, which further increases the overall energy consumption of the device and the operating cost of the enterprise.

[0003] The existing technology has the technical problem of sensible heat waste by using all or part of the cooling method to treat the large amount of sensible heat carried by the crude synthesis gas and high-temperature ash. SUMMARY

[0004] The present application is to solve the technical problem of sensible heat waste by using all or part of the cooling method to treat the large amount of sensible heat carried by the crude synthesis gas and high-temperature ash in the existing technology, and further provides a gas-solid sensible heat recovery integrated device and recovery method for by-product superheated steam.

[0005] The technical solution of the present application is a gas-solid sensible heat recovery integrated device for by-product superheated steam, which includes a pressure-containing shell, an outer cylinder membrane wall, an inner cylinder membrane wall, a superheater, a low-temperature evaporation tube bundle and an ash cooling chamber arranged coaxially inside the pressure-containing shell.

[0006] The outer diameter of the outer cylinder membrane wall is smaller than the inner diameter of the pressure-containing shell, and the upper part of the outer cylinder membrane wall is connected and sealed with the pressure-containing shell. The gas inlet is arranged on both sides of the upper part of the pressure-containing shell, and the gas inlet is communicated with the outer cylinder membrane wall.

[0007] The inner cylinder membrane wall is placed in the outer cylinder membrane wall, the outer diameter of the inner cylinder membrane wall is smaller than the inner diameter of the outer cylinder membrane wall, the inner cylinder membrane wall is connected and sealed with the upper part of the outer cylinder membrane wall, and the upper end and the lower end of the inner cylinder water-cooled wall are both arranged as open.

[0008] The superheater and the low-temperature evaporation tube bundle are placed in the inner cylinder membrane wall, the superheater is located below the low-temperature evaporation tube bundle, the lower end of the superheater is not lower than the lower end of the inner cylinder membrane wall, and the upper end of the low-temperature evaporation tube bundle is not higher than the upper end of the inner cylinder membrane wall.

[0009] The ash cooling chamber is located below the outer membrane wall, and the upper end of the ash cooling chamber is connected and sealed to the lower end of the outer membrane wall; the top of the pressure shell is provided with an air outlet, and the bottom of the pressure shell is provided with an ash outlet, and the lower end of the ash cooling chamber is connected and sealed to the ash outlet.

[0010] As another improvement of the present invention, the pressure-bearing shell is a rotating body structure with an upper end cap, a middle cylindrical body, and a lower end cap coaxially. Two to six air inlets are evenly arranged on the upper side wall of the cylindrical body; an air outlet is provided in the middle of the upper end cap, and an ash outlet is provided in the middle of the lower end cap.

[0011] As another improvement of the present invention, the inner diameter of the air outlet is 1.5 to 4 times the inner diameter of the air inlet.

[0012] As another improvement of the present invention, both the outer cylinder membrane wall and the inner cylinder membrane wall are composed of tubular water-cooled walls; the lower part of the outer cylinder water-cooled wall has a conical constriction structure; the upper part of the inner cylinder water-cooled wall has a conical flaring structure, and the outer diameter of the conical flaring at the upper part of the inner cylinder water-cooled wall is not greater than the inner diameter of the outer cylinder water-cooled wall.

[0013] As another improvement of the present invention, the superheater is a structure of multiple sets of serpentine tube bundles arranged in a uniform manner, and the maximum distance between the superheater and the inner wall of the inner cylinder water-cooled wall does not exceed the distance between adjacent tube bundles of the superheater.

[0014] As another improvement of the present invention, the low-temperature evaporation tube bundle is a uniformly arranged tube bundle structure, and the maximum distance between the low-temperature evaporation tube bundle and the inner wall of the inner cylinder water-cooled wall does not exceed the distance between adjacent tube bundles of the low-temperature evaporation tube bundle.

[0015] As another improvement of the present invention, the outer cylindrical membrane wall, the inner cylindrical membrane wall, the superheater and the low-temperature evaporation tube bundle are all provided with independent inlet distribution boxes and independent outlet collection boxes. The outer cylindrical membrane wall, the inner cylindrical membrane wall, the superheater and the low-temperature evaporation tube bundle are all connected to the external system through independent water vapor inlet pipes and independent water vapor outlet pipes.

[0016] As another improvement of the present invention, the ash cooling chamber is composed of 2 to 6 uniformly arranged fluidizing air inlets, 2 to 6 uniformly arranged jet air inlets, and an air distribution device.

[0017] The fluidizing air outlet is located on the lower end cap of the pressure shell or the ash removal port, and the fluidizing air outlet is connected to the annular space between the pressure shell and the air distribution device.

[0018] The jet nozzle is located on the lower end cap or ash removal port of the pressure shell, and the jet nozzle is connected to the internal space of the air distribution device;

[0019] The air distribution device has a gyro-shaped hollow structure. The upper part of the air distribution device is connected and communicates with the lower part of the outer cylinder water-cooled wall, with a smooth transition at the connection. The maximum outer diameter of the air distribution device is smaller than the inner diameter of the pressure-bearing shell, and the air distribution device is sealed to the inner wall of the pressure-bearing shell. The maximum outer diameter of the bottom of the air distribution device is smaller than the inner diameter of the ash outlet, and the air distribution device is sealed to the inner wall of the ash outlet. The lower conical part of the air distribution device has multiple small holes with a diameter ranging from 0.5 to 20 mm. The spacing between the small holes increases gradually from bottom to top in a stepped or linear manner.

[0020] A gas-solid sensible heat recovery method for by-product superheated steam, characterized by the following treatment steps for high-temperature, high-dust process gas and solid particles using an integrated gas-solid sensible heat recovery device for by-product superheated steam:

[0021] S1. High-temperature and high-dust process gas and solid particles enter the device through the air inlet and descend in the annular space formed by the outer and inner membrane walls, while exchanging heat with the water-cooled walls on both sides of the annular cavity.

[0022] S2. High-temperature and high-dust process gas and solid particles naturally separate into process gas and ash particles at the lower end of the annular cavity under the action of gravity.

[0023] S21. The process gas flows upward along the inner cavity of the inner cylinder membrane wall, during which it exchanges heat with the superheater and the low-temperature evaporator tube bundle. The cooled process gas leaves the device through the outlet at the top of the pressure shell.

[0024] S22. Ash particles fall into the inner cavity of the ash cooling chamber connected to the outer cylinder through the lower conical opening of the outer cylinder membrane wall.

[0025] The outer cylinder membrane wall, inner cylinder membrane wall, and low-temperature evaporator tube bundle heating surface all adopt the bottom-in, top-out mode. In the bottom-in, top-out mode, boiler water enters from the bottom and generates steam during the heat exchange process to form a steam-water mixture. The steam-water mixture leaves the device from the top and goes to the steam drum.

[0026] The ash and slag that settle down at the lower conical end of the outer membrane wall enter the ash and slag cooling chamber and accumulate; fluidizing air is introduced into the annular cavity between the ash and slag cooling chamber and the pressure shell through the fluidizing air inlet, and the fluidizing air enters the inner cavity of the ash and slag cooling chamber through the small hole opened in the lower conical part of the air distribution device; jet air is introduced into the inner cavity of the ash and slag cooling chamber through the jet air inlet.

[0027] The jetting air and fluidizing air come into contact with the high-temperature ash particles for heat exchange. The cooled ash particles are discharged from the ash outlet under gravity. The heated fluidizing air and jetting air mix with the process gas, enter the inner cylinder membrane wall and exchange heat with the superheater and low-temperature evaporator tube bundle before leaving the device.

[0028] As another improvement of the present invention, in step S1, the operating pressure of the high-temperature and high-dust process gas received by the air inlet is 0.1 to 12 MPaG, the operating temperature is 300 to 1300°C, and the particle size range of the solid particles contained in the high-temperature and high-dust process gas is 0.01 to 100 mm.

[0029] The beneficial effects of this invention are:

[0030] 1. The gas-solid sensible heat recovery integrated device for by-product superheated steam of the present invention is applicable to the thermal conversion and utilization technology of carbon-containing raw materials such as coal, biomass, and waste. By coupling the main process of process gas heat recovery with the secondary process of ash particle fluidized cooling, the gas-solid sensible heat recovery is integrated, reducing the ash discharge temperature and realizing dry ash discharge.

[0031] 2. This invention produces high-quality superheated steam as a byproduct in the gas-solid coupling recovery of sensible heat, avoiding the additional investment, operation, and maintenance costs of wet ash removal. It has high energy and raw material utilization, good economic benefits, and significantly improves the energy efficiency of the process technology. Attached Figure Description

[0032] Figure 1 This is a schematic diagram of the structure of an integrated gas-solid sensible heat recovery device for by-product superheated steam according to the present invention.

[0033] Figure 2 This is a schematic diagram of the ash cooling chamber. Detailed Implementation

[0034] Specific implementation method one: Combining Figure 1 This embodiment describes an integrated gas-solid sensible heat recovery device for by-product superheated steam, comprising a pressure-bearing shell 1 and an outer cylindrical membrane wall 2, an inner cylindrical membrane wall 3, a superheater 4, a low-temperature evaporation tube bundle 5, and an ash and slag cooling chamber 6, coaxially arranged inside the pressure-bearing shell 1.

[0035] The outer diameter of the outer membrane wall 2 is smaller than the inner diameter of the pressure shell 1, and the upper part of the outer membrane wall 2 is connected and sealed to the pressure shell 1; the air inlet 11 is provided on both sides of the upper part of the pressure shell 1, and the air inlet 11 is connected to the outer membrane wall 2.

[0036] The inner cylinder membrane wall 3 is placed inside the outer cylinder membrane wall 2. The outer diameter of the inner cylinder membrane wall 3 is smaller than the inner diameter of the outer cylinder membrane wall 2. The inner cylinder membrane wall 3 is connected and sealed to the upper part of the outer cylinder membrane wall 2 to form an annular cavity space A01 with a one-way opening on the lower side. One or more air inlets are opened on the upper side wall of the outer cylinder membrane wall 2. The process gas and the ash particles it carries enter the annular cavity space A01 through the air inlet. The upper and lower ends of the inner cylinder water-cooled wall 3 are both set as open.

[0037] The superheater 4 and the low-temperature evaporator tube bundle 5 are placed inside the inner cylinder film wall 3. The superheater 4 is located below the low-temperature evaporator tube bundle 5. The lower end of the superheater 4 is not lower than the lower end of the inner cylinder film wall 3, and the upper end of the low-temperature evaporator tube bundle 5 is not higher than the upper end of the inner cylinder film wall 3.

[0038] The ash cooling chamber 6 is located below the outer membrane wall 2, and the upper end of the ash cooling chamber 6 is connected and sealed to the lower end of the outer membrane wall 2; the top of the pressure shell 1 is provided with an air outlet 12, and the bottom of the pressure shell 1 is provided with an ash outlet 13, and the lower end of the ash cooling chamber 6 is connected and sealed to the ash outlet 13. The superheater 4 and the low-temperature evaporator tube bundle 5 are both heat-receiving surfaces with gaps. The inner cylinder membrane wall 3, together with the superheater 4 and the low-temperature evaporator tube bundle 5, forms an inner cavity space A02, which allows the process gas and some ash particles to flow upward under the pressure difference between the inlet 11 and the outlet 12. The upper part of the ash cooling chamber 6 is connected to the lower part of the outer cylinder membrane wall 2 to form a bottom space A03. The annular cavity space A01, the inner cavity space A02, and the bottom space A03 are the flow spaces for high-temperature process gas and the ash particles it carries. As the process gas flows through the annular cavity space A01 and the inner cavity space A02 in sequence, it is cooled and its temperature gradually decreases. The ash particles fall into the bottom space A03 under the action of gravity at the junction of A01 and A02.

[0039] Both the outer cylindrical membrane wall 2 and the inner cylindrical membrane wall 3 are membrane water-cooled wall structures composed of heat exchange tubes and their connectors. The medium flowing through the outer cylindrical tube space B01 and the inner cylindrical tube space B02 is water or a steam-water mixture. The superheater 4 is a multi-winding tube bundle structure composed of serpentine or spiral tubes. The medium flowing through the superheater tube space B03 is saturated or superheated steam. The low-temperature evaporator tube bundle 5 is a shell-and-tube bare tube bundle, a tube clamp connected tube bundle, or a multi-screen heating surface structure. The medium flowing through the low-temperature evaporator tube space B04 is water or a steam-water mixture. The steam-water flow of B01, B02, and B04 is designed in parallel. The generated steam-water mixture flows into a unified steam drum device. The saturated steam separated from the steam drum enters the B03 space, is heated to form superheated steam, and leaves the device.

[0040] This invention relates to an integrated gas-solid sensible heat recovery device for by-product superheated steam, applicable to the thermal conversion and utilization of carbonaceous raw materials such as coal, biomass, and waste. By coupling the main process gas heat recovery flow with the fluidized cooling sub-flow of ash particles, the gas-solid sensible heat recovery is integrated, reducing the ash discharge temperature and achieving dry ash discharge. High-quality superheated steam is produced as a by-product during the gas-solid coupled sensible heat recovery process, avoiding the additional investment, operation, and maintenance costs of wet ash discharge. This results in high energy and raw material utilization, good economic benefits, and a significant improvement in the energy efficiency of the process technology. The device employs inner and outer cylindrical membrane walls, a serpentine tube superheater, and a low-temperature evaporator tube bundle for sensible heat recovery through evaporation and superheating. The process design achieves natural separation of ash and solid particles, while jet fluidization cools the ash particles and recovers sensible heat. All these functions are achieved by fully utilizing the same pressure-bearing shell space, resulting in high technological integration and excellent overall benefits.

[0041] Specific Implementation Method Two: Combining Figure 1 This embodiment differs from specific embodiment one in that the pressure-bearing shell 1 is a rotating structure with an upper end cap, a middle cylindrical body, and a lower end cap coaxially. Two to six air inlets 11 are evenly arranged on the upper side wall of the cylindrical body; one air outlet 12 is provided in the middle of the upper end cap, and one ash outlet 13 is provided in the middle of the lower end cap. The even arrangement of two to six air inlets 11 improves air intake efficiency. Other components and connection methods are the same as in specific embodiment one.

[0042] Specific implementation method three: Combining Figure 1 This embodiment differs from specific embodiment one in that the inner diameter of the air outlet 12 is 1.5 to 4 times the inner diameter of the air inlet 11. This design aims to ensure the stability of the device's operation. Other components and connections are the same as in specific embodiment one or two.

[0043] Specific implementation method four: Combination Figure 1 This embodiment differs from specific embodiment one in that both the outer cylindrical membrane wall 2 and the inner cylindrical membrane wall 3 are composed of tubular water-cooled walls; the lower part of the outer cylindrical water-cooled wall 2 has a tapered constriction structure; the upper part of the inner cylindrical water-cooled wall 3 has a tapered flare structure, and the outer diameter of the tapered flare at the upper part of the inner cylindrical water-cooled wall 3 is not greater than the inner diameter of the outer cylindrical water-cooled wall 2. This design ensures stable heat exchange and improves heat exchange efficiency. Other components and connection methods are the same as in any one of specific embodiments one to three.

[0044] Specific Implementation Method Five: Combining Figure 1This embodiment differs from specific embodiment one in that the superheater 4 is a uniformly arranged multi-group serpentine tube bundle structure, and the maximum distance between the superheater 4 and the inner wall of the inner cylinder water-cooled wall 3 does not exceed the distance between adjacent tube bundles of the superheater 4. Its function is to improve heat exchange efficiency. Other components and connection methods are the same as any one of specific embodiments one to four.

[0045] Specific Implementation Method Six: Combination Figure 1 This embodiment differs from specific embodiment one in that the low-temperature evaporator tube bundle 5 is a uniformly arranged tube bundle structure, and the maximum distance between the low-temperature evaporator tube bundle 5 and the inner wall of the inner cylinder water-cooled wall 3 does not exceed the distance between adjacent tube bundles of the low-temperature evaporator tube bundle 5. Its function is to improve heat exchange efficiency. Other components and connection methods are the same as any one of specific embodiments one to five.

[0046] Specific implementation method seven: Combining Figure 1 This embodiment differs from specific embodiment one in that the outer membrane wall 2, inner membrane wall 3, superheater 4, and low-temperature evaporator tube bundle 5 are all equipped with independent inlet distribution boxes and independent outlet collection boxes. The outer membrane wall 2, inner membrane wall 3, superheater 4, and low-temperature evaporator tube bundle 5 are all connected to the external system via independent inlet steam pipes and independent outlet steam pipes. Other components and connection methods are the same as in any one of specific embodiments one through six.

[0047] Specific implementation method eight: Combination Figure 1 and Figure 2 This embodiment differs from specific embodiment one in that the ash cooling chamber 6 is composed of 2 to 6 uniformly arranged fluidizing air inlets 61, 2 to 6 uniformly arranged jet air inlets 62, and an air distribution device 63.

[0048] Fluidizing air outlet 61 is installed on the lower end cap of the pressure shell 1 or the ash removal port 13, and the fluidizing air outlet 61 is connected to the annular cavity space between the pressure shell 1 and the air distribution device 63.

[0049] The jet nozzle 62 is installed on the lower end cap of the pressure shell 1 or the ash removal port 13, and the jet nozzle 62 is connected to the internal space of the air distribution device 63.

[0050] The air distribution device 63 has a gyro-shaped hollow structure. The upper part of the air distribution device 63 is connected and communicates with the lower part of the outer cylinder water-cooled wall 2, with a smooth transition at the connection. The maximum outer diameter of the air distribution device 63 is smaller than the inner diameter of the pressure-bearing shell 1, and the air distribution device 63 is sealed to the inner wall of the pressure-bearing shell 1. The maximum outer diameter of the bottom of the air distribution device 63 is smaller than the inner diameter of the ash outlet 13, and the air distribution device 63 is sealed to the inner wall of the ash outlet 13. Preferably, a heat insulation layer 64 is arranged between the upper part of the inner wall of the air distribution device 63 and the outer cylinder membrane wall. The heat insulation layer 64 can improve the heat exchange efficiency. The lower conical part of the air distribution device 63 has multiple small holes with a diameter range of 0.5 to 20 mm. The spacing between the small holes increases gradually from bottom to top in a stepped or linear manner. The ash particles enter the bottom space A03 from the lower section of the outer membrane wall 2 at the top. Under the influence of the jet air supplied by the jet air inlet 62, the ash particles churn. Simultaneously, the fluidizing air supplied by the fluidizing air inlet 61, after being regulated by the flow field C01 of the air distribution device, enters the bottom space A03. The churning ash particles fully contact and exchange heat. The jet air and fluidizing air are heated by the ash particles and rise, merging into the process gas flow. The cooled ash particles are discharged from the bottom ash outlet 13. The pressure in the ash cooling chamber is P0, the fluidizing air pressure is P1, and the jet air pressure is P2, where P0 < P1 < P2; the ash particle temperature is T0, the fluidizing air temperature is T1, and the jet air temperature is T2, where T0 > T1 ≈ T2; the fluidizing air and jet air can be steam, CO2, process gas, etc.

[0051] Specific Implementation Method Nine: Combining Figure 1 and Figure 2 This embodiment describes a gas-solid sensible heat recovery method for by-product superheated steam. The method employs the integrated gas-solid sensible heat recovery device for by-product superheated steam described in Embodiment Eight to perform the following treatment steps on the high-temperature, high-dust process gas and solid particles.

[0052] S1. High-temperature and high-dust process gas and solid particles enter the device through the air inlet 11 and descend in the annular space formed by the outer cylindrical membrane wall 2 and the inner cylindrical membrane wall 3, while exchanging heat with the water-cooled walls on both sides of the annular cavity.

[0053] S2. High-temperature and high-dust process gas and solid particles naturally separate into process gas and ash particles at the lower end of the annular cavity under the action of gravity.

[0054] S21. The process gas flows upward along the inner cavity of the inner cylinder membrane wall 3, and exchanges heat with the superheater 4 and the low-temperature evaporator tube bundle 5 during this period. The cooled process gas leaves the device through the outlet 12 at the top of the pressure shell 1.

[0055] S22, ash particles fall into the inner cavity of the ash cooling chamber 6 connected to the outer cylinder membrane wall 2 through the lower conical constriction.

[0056] The outer cylinder membrane wall 2, the inner cylinder membrane wall 3, and the low-temperature evaporator tube bundle 5 all adopt a bottom-in, top-out mode for their heating surfaces. In the bottom-in, top-out mode, boiler water enters from the bottom and generates steam during the heat exchange process to form a steam-water mixture. The steam-water mixture leaves the device from the top and goes to the steam drum. The superheater 4 serpentine tube heating surface adopts a top-in, bottom-out or bottom-in, top-out mode. Saturated steam from the steam drum enters the superheater 4 for heat exchange and forms superheated steam that leaves the device.

[0057] The ash and slag that settle down at the lower conical end of the outer membrane wall 2 enter the ash and slag cooling chamber 6 and accumulate there; fluidizing air is sent into the annular cavity between the ash and slag cooling chamber 6 and the pressure shell 1 through the fluidizing air inlet 61, and the fluidizing air enters the inner cavity of the ash and slag cooling chamber 6 through the small hole opened in the lower conical part of the air distribution device 63; jet air is sent into the inner cavity of the ash and slag cooling chamber 6 through the jet air inlet 62;

[0058] The jetting air and fluidizing air come into contact with the high-temperature ash particles for heat exchange. The cooled ash particles are discharged from the ash outlet 13 under the action of gravity. The heated fluidizing air and jetting air mix with the process gas and enter the inner cylinder membrane wall 3 to exchange heat with the superheater 4 and the low-temperature evaporation tube bundle 5 before leaving the device.

[0059] Specific Implementation Method Ten: Combining Figure 1 This embodiment differs from specific embodiment nine in that, in step S1, the operating pressure of the high-temperature, high-dust process gas received by the air inlet 11 is 0.1–12 MPaG, the operating temperature is 300–1300°C, and the particle size range of the solid particles contained in the high-temperature, high-dust process gas is 0.01–100 mm. Using the above-mentioned operating pressure and temperature provides better treatment effect for high-temperature, high-dust process gas with a particle size range of 0.01–100 mm.

[0060] The above embodiments are only used to illustrate the technical solutions of the present invention, and are not intended to limit it. 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. Such modifications or substitutions do not cause the essence of the corresponding technical solutions to deviate from the spirit and scope of the technical solutions of the embodiments of the present invention.

Claims

1. An integrated gas-solid sensible heat recovery device for by-product superheated steam, characterized in that: It includes a pressure-bearing shell (1) and an outer cylindrical membrane wall (2), an inner cylindrical membrane wall (3), a superheater (4), a low-temperature evaporator tube bundle (5), and an ash and slag cooling chamber (6) arranged coaxially inside the pressure-bearing shell (1). The outer diameter of the outer membrane wall (2) is smaller than the inner diameter of the pressure shell (1), and the upper part of the outer membrane wall (2) is connected and sealed to the pressure shell (1); the air inlet (11) is located on both sides of the upper part of the pressure shell (1), and the air inlet (11) is connected to the outer membrane wall (2); The inner cylindrical membrane wall (3) is placed inside the outer cylindrical membrane wall (2). The outer diameter of the inner cylindrical membrane wall (3) is smaller than the inner diameter of the outer cylindrical membrane wall (2). The inner cylindrical membrane wall (3) is connected and sealed to the upper part of the outer cylindrical membrane wall (2). The upper and lower ends of the inner cavity of the inner cylindrical membrane wall (3) are both set as open openings. The superheater (4) and the low-temperature evaporation tube bundle (5) are placed inside the inner cylinder membrane wall (3). The superheater (4) is located below the low-temperature evaporation tube bundle (5). The lower end of the superheater (4) is not lower than the lower end of the inner cylinder membrane wall (3), and the upper end of the low-temperature evaporation tube bundle (5) is not higher than the upper end of the inner cylinder membrane wall (3). The ash cooling chamber (6) is located below the outer cylinder membrane wall (2), and the upper end of the ash cooling chamber (6) is connected and sealed to the lower end of the outer cylinder membrane wall (2); the top of the pressure shell (1) is provided with an air outlet (12), and the bottom of the pressure shell (1) is provided with an ash outlet (13), and the lower end of the ash cooling chamber (6) is connected and sealed to the ash outlet (13); The ash cooling chamber (6) consists of 2 to 6 uniformly arranged fluidizing air inlets (61), 2 to 6 uniformly arranged jet air inlets (62), and an air distribution device (63); The fluidizing air outlet (61) is located on the lower end cap or ash outlet (13) of the pressure shell (1), and the fluidizing air outlet (61) is connected to the annular space between the pressure shell (1) and the air distribution device (63); The jet nozzle (62) is installed on the lower end cap or ash outlet (13) of the pressure shell (1), and the jet nozzle (62) is connected to the internal space of the air distribution device (63); The air distribution device (63) is a gyroscope-shaped hollow structure. The upper part of the air distribution device (63) is connected and communicates with the lower part of the outer cylindrical membrane wall (2), and the connection is smooth. The maximum outer diameter of the air distribution device (63) is smaller than the inner diameter of the pressure shell (1), and the air distribution device (63) is connected and sealed to the inner wall of the pressure shell (1). The maximum outer diameter of the bottom of the air distribution device (63) is smaller than the inner diameter of the ash outlet (13), and the air distribution device (63) is connected and sealed to the inner wall of the ash outlet (13). The lower conical part of the air distribution device (63) has multiple small holes with a diameter range of 0.5 to 20 mm. The spacing between the small holes increases gradually from bottom to top in a stepped or linear manner.

2. The integrated gas-solid sensible heat recovery device for by-product superheated steam according to claim 1, characterized in that: The pressure-bearing shell (1) is a rotating body structure with an upper end cap, a middle cylindrical body, and a lower end cap coaxially. Two to six air inlets (11) are evenly arranged on the upper side wall of the cylindrical body. An air outlet (12) is set in the middle of the upper end cap, and an ash outlet (13) is set in the middle of the lower end cap.

3. The integrated gas-solid sensible heat recovery device for by-product superheated steam according to claim 2, characterized in that: The inner diameter of the air outlet (12) is 1.5 to 4 times that of the inner diameter of the air inlet (11).

4. The integrated gas-solid sensible heat recovery device for by-product superheated steam according to claim 1, characterized in that: The outer cylindrical membrane wall (2) and the inner cylindrical membrane wall (3) are both composed of tubular water-cooled walls; the lower part of the outer cylindrical membrane wall (2) is a conical constriction structure; the upper part of the inner cylindrical membrane wall (3) is a conical flaring structure, and the outer diameter of the conical flaring at the upper part of the inner cylindrical membrane wall (3) is not greater than the inner diameter of the outer cylindrical membrane wall (2).

5. The integrated gas-solid sensible heat recovery device for by-product superheated steam according to any one of claims 1-4, characterized in that: The superheater (4) is a structure of multiple serpentine tube bundles arranged uniformly. The maximum distance between the superheater (4) and the inner wall of the inner cylinder membrane wall (3) does not exceed the distance between adjacent tube bundles of the superheater (4).

6. The integrated gas-solid sensible heat recovery device for by-product superheated steam according to any one of claims 1-4, characterized in that: The low-temperature evaporation tube bundle (5) is a uniformly arranged tube bundle structure, and the maximum distance between the low-temperature evaporation tube bundle (5) and the inner wall of the inner cylinder membrane wall (3) does not exceed the distance between adjacent tube bundles of the low-temperature evaporation tube bundle (5).

7. An integrated gas-solid sensible heat recovery device for by-product superheated steam according to any one of claims 1-4, characterized in that: The outer cylindrical membrane wall (2), inner cylindrical membrane wall (3), superheater (4) and low-temperature evaporation tube bundle (5) are each equipped with an independent inlet distribution box and an independent outlet collection box. The outer cylindrical membrane wall (2), inner cylindrical membrane wall (3), superheater (4) and low-temperature evaporation tube bundle (5) are all connected to the external system through independent water vapor inlet pipes and independent water vapor outlet pipes.

8. A gas-solid sensible heat recovery method for by-product superheated steam, characterized in that: The integrated gas-solid sensible heat recovery device for by-product superheated steam as described in claim 1 performs the following treatment steps on high-temperature, high-dust process gas and solid particles: S1. High-temperature and high-dust process gas and solid particles enter the device through the air inlet (11) and descend in the annular space formed by the outer cylindrical membrane wall (2) and the inner cylindrical membrane wall (3), while exchanging heat with the water-cooled walls on both sides of the annular cavity. S2. High-temperature and high-dust process gas and solid particles naturally separate into process gas and ash particles at the lower end of the annular cavity under the action of gravity. S21. The process gas flows upward along the inner cavity of the inner cylinder membrane wall (3), and exchanges heat with the superheater (4) and the low temperature evaporator tube bundle (5) during the process. The cooled process gas leaves the device through the outlet (12) at the top of the pressure shell (1). S22, ash particles fall into the inner cavity of the ash cooling chamber (6) connected to it through the lower conical opening of the outer cylinder membrane wall (2); The outer cylinder membrane wall (2), the inner cylinder membrane wall (3), and the low-temperature evaporation tube bundle (5) all adopt the bottom-in and top-out mode. The bottom-in and top-out mode means that the boiler water enters from the bottom and generates steam during the heat exchange process to form a steam-water mixture. The steam-water mixture leaves the device from the top and goes to the steam drum. The ash and slag that settle down at the lower conical end of the outer membrane wall (2) enter the ash and slag cooling chamber (6) and accumulate; fluidizing air is sent into the annular cavity between the ash and slag cooling chamber (6) and the pressure shell (1) through the fluidizing air inlet (61), and the fluidizing air enters the inner cavity of the ash and slag cooling chamber (6) through the small hole opened in the lower conical part of the air distribution device (63); jetting air is sent into the inner cavity of the ash and slag cooling chamber (6) through the jetting air inlet (62); The jetting air and fluidizing air come into contact with the high-temperature ash particles for heat exchange. The cooled ash particles are discharged from the ash outlet (13) under gravity. The heated fluidizing air and jetting air mix with the process gas and enter the inner cylinder membrane wall (3) to exchange heat with the superheater (4) and the low-temperature evaporation tube bundle (5) before leaving the device.

9. A gas-solid sensible heat recovery method for by-product superheated steam according to claim 8, characterized in that: In step S1, the high-temperature and high-dust process gas received by the air inlet (11) has an operating pressure of 0.1 to 12 MPaG, an operating temperature of 300 to 1300℃, and a particle size range of 0.01 to 100 mm for solid particles contained in the high-temperature and high-dust process gas.

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