CO isothermal transformation system and process of pulverized coal pressurized gasification device

Abstract

The invention relates to the technical field of coal chemical industry, and particularly discloses a CO isothermal conversion system and process of a pulverized coal pressurized gasification device. First-order conversion gas discharged from a first isothermal conversion furnace is used as a heat source to perform heat exchange and temperature rise on raw gas from a gasification unit; mixing the raw gas subjected to heat exchange and temperature rise with part of steam from a byproduct of a first isothermal transformation furnace, and introducing the mixed raw gas into the first isothermal transformation furnace to carry out isothermal change reaction; first-order shift gas discharged from the first isothermal shift converter is subjected to secondary cooling and then mixed with steam, the mixed gas is introduced into a second isothermal shift converter for isothermal change reaction, second-order shift gas discharged from the first isothermal shift converter is introduced into a boiler feed water preheater and a waste heat recovery section heat exchanger in sequence for cooling and liquid separation, and then desulfurization and decarburization are performed; the conversion process flow disclosed by the invention is relatively simple, the process flow is shortened, the number of equipment in the system is reduced, the temperature of a catalyst bed layer is reduced, and long-period stable operation of the catalyst is ensured.

Description

Technical Field

[0001] The present invention relates to the technical field of coal chemical industry, and specifically discloses a CO isothermal conversion system and process for a pulverized coal pressurized gasification device. Background Art

[0002] The CO conversion principle of the pulverized coal pressurized gasification device is to chemically react the CO from the gasified semi-water gas with water vapor under high temperature and pressure conditions with the help of cobalt-molybdenum catalysts to generate CO2 and H2, and produce H2 conversion gas that meets the needs of downstream production processes.

[0003] The CO conversion process is divided into an adiabatic conversion process and an isothermal conversion process. The adiabatic conversion process requires the use of multiple adiabatic reactors to meet the requirements of the CO concentration at the system outlet. Generally, four adiabatic conversion furnaces are connected in series, and seven steam generators are used to recover the heat energy of the conversion reaction. The process route is long and complex, with many equipment and pipelines, high investment costs, and high subsequent maintenance costs. There are also problems such as complex operation and control, long start-up time, unstable start-up, easy overheating of the first and second conversion furnaces, short catalyst life, and large pressure drop before and after the system. In addition, the heat recovery rate is low and the self-produced steam is small. In order to control the CO content at the system outlet to meet the process index requirements and improve the steam-to-gas ratio, a certain amount of steam needs to be added before the first and second conversion furnaces, resulting in a large amount of separated condensate in the latter stage and a large steam consumption.

[0004] The invention patent with application number 201911014621.4 discloses an isothermal conversion hydrogen production method and an isothermal conversion furnace for matching pulverized coal gasification equipment. The raw coal gas from the pulverized coal gasification equipment is separated into two streams after condensate is separated, preheated, and detoxified; the first stream is sent to the adiabatic conversion furnace for conversion reaction after adjusting the water / dry gas ratio, and the primary adiabatic conversion gas is humidified and heat recovered before being mixed with the second stream of raw coal gas. After the water / dry gas ratio of the mixed gas is adjusted, it enters the first reaction chamber of the isothermal conversion furnace for medium-temperature CO conversion reaction, and at the same time, medium-pressure saturated steam is produced as a by-product. After heat exchange, the primary isothermal conversion gas enters the second reaction chamber for low-temperature CO conversion reaction, and at the same time, low-pressure saturated steam is produced as a by-product to generate secondary isothermal conversion gas; the secondary isothermal conversion gas is sent downstream as raw hydrogen after heat recovery. The isothermal conversion hydrogen production method disclosed in this patent is actually a process that combines adiabatic conversion and isothermal conversion. Compared with the adiabatic conversion process with transmission, the number of equipment units can be reduced, and the saturated steam produced as a by-product of the isothermal conversion furnace can be mixed with the reaction gas as a raw material, reducing steam consumption. However, this process still has some shortcomings: First, the process requires the raw coal gas to be divided into two streams. One stream first undergoes a conversion reaction in the adiabatic conversion furnace, and then is mixed with the second stream and passed into the adiabatic reaction furnace after the reaction. The flow distribution process requires that the two raw gas streams be mixed with steam according to the amount, resulting in a complicated operation process. Second, the adiabatic conversion furnace is used as a startup furnace, and its internal temperature is still prone to overheating, resulting in a short catalyst life. In addition, the heat inside the adiabatic conversion furnace cannot be effectively utilized. Therefore, in response to the shortcomings of the traditional adiabatic conversion process and the isothermal conversion hydrogen production method disclosed in this patent, this application proposes a CO isothermal conversion system and process for a pulverized coal pressurized gasification device that can effectively solve the above problems. Summary of the Invention

[0005] The purpose of the present invention is to provide a CO isothermal conversion system and process for a pulverized coal pressurized gasification device to solve the problems in the prior art such as the relatively complex conversion process, the easy overheating inside the adiabatic conversion furnace, resulting in a short catalyst life, and the inability to effectively utilize the heat inside the adiabatic conversion furnace.

[0006] The present invention is achieved through the following technical solutions: A CO isothermal shift process for a pulverized coal pressurized gasification device comprises the following steps: 1) The first-stage shift gas discharged from the first isothermal shift furnace is used as a heat source and is heated by heat exchange with the raw coal gas from the gasification unit through a feed heat exchanger; 2) The raw coal gas after heat exchange and temperature increase is mixed with part of the steam produced as a by-product from the first isothermal shift furnace. After the mixture is introduced into the first isothermal shift furnace, CO and water vapor undergo an isothermal shift reaction under the action of a shift catalyst, reducing the CO dry basis content to between 5.0±0.5%; 3) The first-stage shifted gas discharged from the first isothermal shift furnace is cooled in a feed heat exchanger and then passed into a condensate heater for heat exchange and cooling. After the second cooling, it is mixed with part of the steam by-product from the first isothermal shift furnace and then passed into the second isothermal shift furnace. The CO and water vapor undergo an isothermal shift reaction over a shift catalyst, reducing the CO content on a dry basis to below 0.4%. 4) The second-stage shift gas discharged from the second isothermal shift furnace is successively passed into the boiler feed water preheater and the subsequent waste heat recovery section heat exchanger for cooling and liquid separation, and finally sent to the desulfurization and decarbonization unit for treatment.

[0007] As a further configuration of the above scheme, in step 1, the gauge pressure of the raw coal gas from the gasification unit is 3.26±0.30 MPa (G), the temperature is 193±5°C, and the temperature of the raw coal gas after heat exchange and heating is 220±5°C.

[0008] As a further configuration of the above scheme, the raw coal gas from the gasification unit in step 1 first enters a gas-liquid separator to separate water before entering the feed heat exchanger.

[0009] As a further configuration of the above scheme, the raw coal gas after heat exchange and temperature increase in step 2 is first sent to a detoxification tank to remove components harmful to the conversion catalyst before being mixed with steam.

[0010] As a further configuration of the above scheme, the temperature of the first-stage conversion gas after heat exchange and cooling by the condensate heater in step 3 is controlled at 210±5°C.

[0011] As a further arrangement of the above scheme, the by-product saturated steam in the first isothermal conversion furnace is introduced into the first steam drum, and the saturated steam in the first steam drum is divided into three routes, one route is mixed with the detoxified raw coal gas, the second route is fed into the process pipeline in front of the second isothermal conversion furnace, and the remaining saturated steam is used as the third route and sent to the external steam network after being decompressed; the by-product saturated steam in the second isothermal conversion furnace is introduced into the second steam drum, and the saturated steam in the second steam drum is all sent to the external steam network after being decompressed.

[0012] The present invention also discloses a CO isothermal conversion system based on the CO isothermal conversion process of the pulverized coal pressurized gasification device, comprising a first isothermal conversion furnace, a second isothermal conversion furnace, a first steam drum, a second steam drum, a gas-liquid separator, a feed heat exchanger, a detoxification tank, a condensate heater and an external steam pipe network, wherein one end of the gas-liquid separator is connected to a raw coal gas pipeline from a gasification unit, and the other end is connected to a heat exchange medium inlet of the feed heat exchanger, a heat exchange medium outlet of the feed heat exchanger is connected to the detoxification tank, the other end of the detoxification tank is connected to an air inlet of the first isothermal conversion furnace, an air outlet of the first isothermal conversion furnace is connected to a heat source inlet of the feed heat exchanger, a heat source outlet of the feed heat exchanger is connected to one end of a condensate heater, the other end of the condensate heater is connected to an air inlet of the second isothermal conversion furnace, and an air outlet of the second isothermal conversion furnace is sequentially connected to a boiler feed water preheater, a subsequent waste heat recovery section heat exchanger and a desulfurization and decarbonization unit through a pipeline; The drain outlet of the first steam drum is connected to the water chamber in the first isothermal conversion furnace, the steam inlet of the first steam drum is connected to the steam chamber in the first isothermal conversion furnace, the steam outlet of the first steam drum is divided into three routes, one route is connected to the gas pipeline between the detoxification tank and the first isothermal conversion furnace, the second route is connected to the gas pipeline between the condensate heater and the second isothermal conversion furnace, and the third route is connected to the external steam pipeline network. The drain outlet of the second steam drum is connected to the water chamber in the second isothermal conversion furnace, the steam inlet of the second steam drum is connected to the steam chamber in the second isothermal conversion furnace, and the steam outlet of the second steam drum is connected to the external steam pipeline network.

[0013] As a further configuration of the above scheme, the first isothermal conversion furnace and the second isothermal conversion furnace have the same structure and both include a concentrically arranged outer cylinder and a radial hole frame. The interior of the radial hole frame is provided with a central tube extending downward from the outer cylinder, and a conversion catalyst is filled between the intermediate tube and the radial hole frame. An upper tube plate and a lower tube plate are provided at the upper end of the inner cavity of the outer cylinder, a steam chamber is formed between the upper tube plate and the lower tube plate, and a water chamber is formed between the upper tube plate and the top of the outer cylinder. A heat exchange outer sleeve is provided on the lower tube plate and extends into the conversion catalyst, and the bottom of the heat exchange outer sleeve is sealed. A heat exchange inner sleeve is provided on the upper tube plate and extends into the heat exchange outer sleeve, and the bottom of the heat exchange inner sleeve is connected to the heat exchange outer sleeve.

[0014] Compared with the prior art, the present invention has the following beneficial effects: The conversion process disclosed in the present invention is relatively simple. The raw coal gas only needs to be dehumidified, heated, and detoxified before being mixed with steam and introduced into a first isothermal conversion furnace for a first-order conversion reaction. After the first-order conversion reaction is completed, the gas is cooled by utilizing waste heat and then mixed with steam for a second-order conversion reaction. This allows the CO dry basis content of the converted gas after the reaction to be controlled within a corresponding range. This not only shortens the process flow and reduces the number of devices in the system, but also makes the entire conversion process simple to control and easy to operate. It also effectively reduces equipment investment costs and saves land occupation.

[0015] The conversion process disclosed in the present invention has a small number of equipment units and a simple pipeline route, which shortens the start-up time of the entire system, ensures smooth start-up, and effectively reduces production costs. At the same time, due to the short process route and the small number of equipment and pipelines, there are fewer corrosion points and the operating temperature is low, which reduces thermal stress corrosion and avoids leakage and fire accidents.

[0016] The first isothermal change furnace and the second isothermal change furnace in the present invention both utilize heat transfer water pipe bundles distributed inside the catalyst bed to directly convert the reaction heat energy of the catalyst bed into high-grade steam, thereby improving the energy utilization efficiency of the reaction heat energy; at the same time, since the bed reaction heat can be continuously and promptly removed, the catalyst bed temperature is reduced, ensuring that the catalyst bed temperature is controllable, fundamentally solving the problem of overheating of the catalyst bed in the "double high" raw coal gas conversion reaction, giving full play to the low-temperature activity of the catalyst, and ensuring the long-term stable operation of the catalyst. BRIEF DESCRIPTION OF THE DRAWINGS

[0017] In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the following briefly introduces the drawings required for describing the embodiments. Obviously, the drawings described below are only some embodiments of the present invention. For ordinary technicians in this field, other drawings can be obtained based on these drawings without creative work.

[0018] Figure 1 This is a schematic diagram showing the connections of the various components of the CO isothermal conversion system of the pulverized coal pressurized gasification device of the present invention; Figure 2 It is a schematic diagram of the internal planar structure of the first isothermal conversion furnace or the second isothermal conversion furnace in the present invention. DETAILED DESCRIPTION

[0019] In order to enable those skilled in the art to better understand the present invention, the following will clearly and completely describe the technical solutions in the embodiments of the present invention in conjunction with the drawings in the embodiments of the present invention. Obviously, the described embodiments are only part of the embodiments of the present invention, not all of the embodiments. Based on the embodiments in the present invention, all other embodiments obtained by ordinary technicians in this field without making creative efforts should fall within the scope of protection of this application.

[0020] It should be noted that, in the absence of conflict, the embodiments and features in the embodiments of this application can be combined with each other. Figure 1 and attached Figure 2 , and describes the application in detail with reference to embodiments. Example 1

[0021] Example 1 discloses a CO isothermal conversion system for a pulverized coal pressurized gasification device. Figure 1-2 The system includes a first isothermal shift furnace 4, a first steam drum 5, a second isothermal shift furnace 4', a second steam drum 5', a gas-liquid separator 1, a feed heat exchanger 2, a detoxification tank 3, a condensate heater 6 and an external steam pipe network 7.

[0022] The gas-liquid separator 1's air inlet is connected to the crude gas pipeline from the gasification unit, and its air outlet is connected to the heat exchange medium air inlet of the feed heat exchanger 2. The heat exchange medium air outlet of the feed heat exchanger 2 is connected to the air inlet of the detoxification tank 3. The air outlet of the detoxification tank 3 is connected to the air inlet of the first isothermal shift furnace 4 via a pipeline. Simultaneously, a steam pipeline on the first steam drum 5 is connected to the pipeline after the air outlet of the detoxification tank 3 to ensure thorough mixing of the detoxified crude gas and steam. The air outlet of the first isothermal shift furnace 4 is connected to the heat medium air inlet of the feed heat exchanger 2, which in turn is connected to the air inlet of the condensate heater 6. The air outlet of the condensate heater 6 is connected to the second steam pipeline on the first steam drum 5 via a pipeline. After mixing, it is connected to the air inlet of the second isothermal shift furnace 4'. The gas outlet of the second isothermal conversion furnace 4' is first connected to the boiler feed water preheater (not shown) through a pipeline, then to the subsequent waste heat recovery section heat exchanger (not shown), and finally to the desulfurization and decarbonization unit.

[0023] Furthermore, the heat source removed from the first isothermal shift furnace 4 is connected to the first steam drum 5 via a pipe, while the heat source removed from the second isothermal shift furnace 4' is connected to the second steam drum 5' via a pipe. The first steam drum 5 is equipped with three steam pipes: one connected to the gas pipeline from the rear of the detoxification tank 3 (i.e., connected to the detoxified raw coal gas); a second connected to the pipe at the outlet of the condensate heater 6; and a third connected directly to the external steam network 7. Finally, the second steam drum 5' is equipped with only a single steam pipe, which is directly connected to the external steam network 7.

[0024] The first isothermal conversion furnace 4 and the second isothermal conversion furnace 4' in this embodiment 1 have basically the same structure, both including an outer cylinder 401, a radial hole frame 402 is concentrically arranged inside the outer cylinder 401, a central tube 403 extending downward from the outer cylinder 401 is arranged at the center of the radial hole frame 402, and a conversion catalyst is filled in the annular cavity formed by the radial hole frame 402 and the central tube 403.

[0025] An upper tube sheet 404 and a lower tube sheet 405 are located at the upper end of the inner cavity of the outer cylinder 401. The space within the outer cylinder 401 above the upper tube sheet 404 serves as a water chamber for receiving hot water discharged from the first steam drum 5 or the second steam drum 5'. The space between the upper tube sheet 404 and the lower tube sheet 405 serves as a steam chamber for collecting the high-temperature steam generated by the reaction heat, which is then piped to the first steam drum 5 or the second steam drum 5'. The first steam drum 5 or the second steam drum 5' is also equipped with corresponding water supply pipes and steam discharge pipes.

[0026] Multiple heat exchange outer sleeves 406, with sealed lower ends, are evenly distributed on the lower tube sheet 405. These outer sleeves extend into the inner cavity filled with the shift catalyst. On the upper tube sheet 404, inner heat exchange sleeves 407 are aligned vertically with each outer heat exchange sleeve 406 and extend concentrically into the outer heat exchange sleeve 406. A certain gap is maintained between the lower end of each inner heat exchange sleeve 407 and the bottom of the outer heat exchange sleeve 406, allowing hot water in the water chamber to flow downward along the inner heat exchange sleeves 407, enter the bottom of the outer heat exchange sleeve 406, and then flow upward. During this upward flow, it absorbs the heat of the shift reaction to generate steam. The resulting steam enters the steam chamber and is then transported via pipelines to the first steam drum 5 or the second steam drum 5'.

[0027] Finally, a mixed gas inlet end is provided on the outer wall of the lower end of the outer cylinder 401. After the mixed gas to be reacted enters the inner part of the outer cylinder 401, it will flow upward along the annular gap between the outer cylinder 401 and the radial hole frame 402, and then pass through the radial hole frame 402 to contact with the conversion catalyst to realize the reaction. After the reaction, it enters the top of the central tube 403 and is then discharged from the lower end by the central tube 403. Example 2

[0028] Example 2 discloses a CO isothermal shift process based on the isothermal shift system in Example 1, which includes the following steps: S1: The raw coal gas at 3.26±0.30MPa (G) and 193±5℃ from the gasification unit is passed into the gas-liquid separator 1. After the water is separated, it is passed into the feed heat exchanger 2 for heat exchange with the conversion gas from the outlet of the first isothermal conversion furnace 4. The temperature of the raw coal gas after heat exchange is 220±5℃.

[0029] S2: The raw coal gas after heat exchange and temperature increase is introduced into the detoxification tank 3 to remove Cl- , oxygen, solid particles and other harmful components to the conversion catalyst are removed and then fully mixed with the steam from the first steam drum 5. After mixing, it is introduced into the first isothermal conversion furnace 4 for isothermal conversion reaction to reduce the CO dry content to between 5.0±0.5%. The reaction heat in the first isothermal conversion furnace 4 is transferred out of the bed through the internal heat exchange sleeve, and 4.2MPaG saturated steam is produced as a by-product. The saturated steam produced as a by-product is divided into three routes. One route is mixed with the detoxified raw coal gas as a first-order reaction raw material, the second route is fed into the process pipeline in front of the second isothermal conversion furnace 4' as a second-order reaction raw material, and the remaining saturated steam is sent as the third route to the external steam network 7 after decompression.

[0030] S3: The first-stage shifted gas discharged from the first isothermal shift furnace 4 is first passed into the feed heat exchanger 2 to preheat the raw coal gas. It then enters the condensate heater 6 to heat the condensate, controlling its temperature after exiting the condensate heater 6 to between 210±5°C. The gas is then thoroughly mixed with steam from the first steam drum 5 before entering the second isothermal shift furnace 4' for a second-stage shift reaction, reducing the CO content on a dry basis to below 0.4%. The reaction heat in the second isothermal shift furnace 4' is removed from the bed via internal heat exchanger tubing, producing low-pressure saturated steam at 0.85±0.15 MPaG as a byproduct. This saturated steam is then depressurized and fed to the external steam network 7.

[0031] S4: The second-stage conversion gas discharged from the second isothermal conversion furnace 4' is first introduced into the boiler feed water preheater to heat the boiler feed water, and then the boiler heats the feed water in one step and serves as the supplementary water source for the first steam drum 5 and the second steam drum 5'. The conversion gas discharged from the boiler feed water preheater is then cooled and separated in the subsequent waste heat recovery section heat exchanger, and finally sent to the desulfurization and decarbonization unit for treatment.

[0032] The above are only preferred embodiments of the present invention and are not intended to limit the present invention. Any modifications, equivalent substitutions and improvements made within the spirit and principles of the present invention should be included in the scope of protection of the present invention.

Claims

1. A CO isothermal shift process for a pulverized coal pressurized gasification device, characterized in that: The steps include: The first-stage shifted gas discharged from the first isothermal shift furnace is used as a heat source and is heated by heat exchange with the raw coal gas from the gasification unit through the feed heat exchanger; The raw coal gas after heat exchange and temperature increase is mixed with part of the steam produced as a by-product from the first isothermal shift furnace. After mixing, it is passed into the first isothermal shift furnace. CO and water vapor undergo an isothermal shift reaction under the action of a shift catalyst, reducing the CO dry basis content to between 5.0±0.5%. The first-stage shift gas discharged from the first isothermal shift furnace is cooled in a feed heat exchanger and then passed into a condensate heater for heat exchange and cooling. After the second cooling, it is mixed with part of the steam by-product from the first isothermal shift furnace and then passed into the second isothermal shift furnace. The CO and water vapor undergo an isothermal shift reaction over a shift catalyst, reducing the CO dry content to below 0.4%. The second-stage conversion gas discharged from the second isothermal conversion furnace is successively passed into the boiler feed water preheater and the subsequent waste heat recovery section heat exchanger for cooling and liquid separation, and finally sent to the desulfurization and decarbonization unit for treatment.

2. The CO isothermal shift process of the pulverized coal pressurized gasification device according to claim 1, characterized in that: In the step 1, the gauge pressure of the raw coal gas from the gasification unit is 3.26±0.30 MPa (G), and the temperature is 193±5° C. The temperature of the raw coal gas after heat exchange and temperature increase is 220±5° C.

3. The CO isothermal shift process of the pulverized coal pressurized gasification device according to claim 1, characterized in that: In step 1, the raw coal gas from the gasification unit first enters the gas-liquid separator to separate water before entering the feed heat exchanger.

4. The CO isothermal shift process of the pulverized coal pressurized gasification device according to claim 1, characterized in that: The raw coal gas after heat exchange and temperature increase in step 2 enters the detoxification tank to remove the Shift Catalyst Harmful ingredients.

5. The CO isothermal shift process of the pulverized coal pressurized gasification device according to claim 1, characterized in that: In step 3, the temperature of the first-stage conversion gas after heat exchange and cooling by the condensate heater is controlled at 210±5°C.

6. The CO isothermal shift process of the pulverized coal pressurized gasification device according to claim 1, characterized in that: The by-product saturated steam in the first isothermal conversion furnace is introduced into the first steam drum. The saturated steam in the first steam drum is divided into three routes. One route is mixed with the detoxified raw coal gas, the second route is fed into the process pipeline in front of the second isothermal conversion furnace, and the remaining saturated steam is used as the third route and sent to the external steam network after being decompressed; the by-product saturated steam in the second isothermal conversion furnace is introduced into the second steam drum, and the saturated steam in the second steam drum is all sent to the external steam network after being decompressed.

7. A CO isothermal conversion system based on the CO isothermal conversion process of the pulverized coal pressurized gasification device according to any one of claims 1 to 6, characterized in that: It includes a first isothermal conversion furnace, a second isothermal conversion furnace, a first steam drum, a second steam drum, a gas-liquid separator, a feed heat exchanger, a detoxification tank, a condensate heater and an external steam network, one end of the gas-liquid separator is connected to the raw gas pipeline from the gasification unit, and the other end is connected to the heat exchange medium inlet of the feed heat exchanger, the heat exchange medium outlet of the feed heat exchanger is connected to the detoxification tank, the other end of the detoxification tank is connected to the air inlet of the first isothermal conversion furnace, the air outlet of the first isothermal conversion furnace is connected to the heat source inlet of the feed heat exchanger, the heat source outlet of the feed heat exchanger is connected to one end of the condensate heater, the other end of the condensate heater is connected to the air inlet of the second isothermal conversion furnace, the air outlet of the second isothermal conversion furnace is connected to the boiler feed water preheater, the subsequent waste heat recovery section heat exchanger and the desulfurization and decarbonization unit in sequence through pipelines; The drain outlet of the first steam drum is connected to the water chamber in the first isothermal conversion furnace, the steam inlet of the first steam drum is connected to the steam chamber in the first isothermal conversion furnace, the steam outlet of the first steam drum is divided into three routes, one route is connected to the gas pipeline between the detoxification tank and the first isothermal conversion furnace, the second route is connected to the gas pipeline between the condensate heater and the second isothermal conversion furnace, and the third route is connected to the external steam pipeline network. The drain outlet of the second steam drum is connected to the water chamber in the second isothermal conversion furnace, the steam inlet of the second steam drum is connected to the steam chamber in the second isothermal conversion furnace, and the steam outlet of the second steam drum is connected to the external steam pipeline network.

8. The CO isothermal conversion system of the pulverized coal pressurized gasification device according to claim 7, characterized in that: The first isothermal conversion furnace and the second isothermal conversion furnace have the same structure, both including a concentrically arranged outer cylinder and a radial hole frame, a central tube extending downward from the outer cylinder is provided inside the radial hole frame, and a conversion catalyst is filled between the intermediate tube and the radial hole frame, an upper tube plate and a lower tube plate are provided at the upper end of the inner cavity of the outer cylinder, a steam chamber is formed between the upper tube plate and the lower tube plate, and a water chamber is formed between the upper tube plate and the top of the outer cylinder, a heat exchange outer sleeve is provided on the lower tube plate and extends into the conversion catalyst, and the bottom of the heat exchange outer sleeve is sealed, a heat exchange inner sleeve is provided on the upper tube plate and extends into the heat exchange outer sleeve, and the bottom of the heat exchange inner sleeve is connected to the heat exchange outer sleeve.

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