A gas desulfurization and hydrolysis composite tank and blast furnace gas fine desulfurization system

Abstract

The invention discloses a gas decontamination and hydrolysis composite tank and a blast furnace gas fine desulfurization system, comprising a reaction tank body, wherein a gas inlet and a gas outlet are radially arranged on the reaction tank body, three mesh partitions are arranged inside the reaction tank body, the mesh partitions are arranged parallel to the center line of the reaction tank, and the gas flows radially along the tank body. The mesh partitions divide the interior of the reaction tank body into a gas distribution chamber, a decontamination chamber, a catalytic hydrolysis chamber and a gas collecting chamber. The gas inlet is arranged on the gas distribution chamber side of the reaction tank body, and the gas outlet is arranged on the gas collecting chamber side of the reaction tank body. A decontamination agent is placed in the decontamination chamber, and an organic catalytic converter is placed in the catalytic hydrolysis chamber. The gas enters the gas distribution chamber from the gas inlet, flows uniformly toward the decontamination chamber and the catalytic hydrolysis chamber, and is discharged through the outlet after merging in the gas collecting chamber. The gas has low resistance along the gas flow and low pressure loss, and can meet the requirements of removing harmful impurities in blast furnace flue gas and catalytically hydrolyzing organic sulfides.

Description

Technical Field

[0001] The invention belongs to the technical field of blast furnace gas fine desulfurization, and in particular relates to a gas desulfurization and hydrolysis composite tank and a blast furnace gas fine desulfurization system. Background Art

[0002] At present, blast furnace gas is only purified by bag dust collector to remove dust in the gas, so that the dust content of the gas is less than 10mg / m 3 Or lower, to meet the requirements of the subsequent process. However, the chemical composition of the gas does not change at all. The chemical composition determines the composition of the flue gas after combustion, that is, the sulfur content of the blast furnace gas determines the SO2 content of the flue gas.

[0003] Blast furnace gas production is high and has many end users. Using flue gas desulfurization (SO2) has many disadvantages, including multiple processing points, high investment, large land area, and high labor requirements. Therefore, fine desulfurization is a more optimal treatment option for blast furnace gas, especially for newly built integrated steel enterprises.

[0004] Different blast furnaces use different raw material conditions and operating methods, resulting in varying total sulfur contents in their gas. This content is primarily determined by the sulfur content of the raw materials, with 10-20% of the raw material sulfur typically entering the top gas. Sulfur in blast furnace gas primarily exists as COS, along with some H2S, and smaller amounts of CS2 and R-SH. While H2S can be directly removed using established adsorption or alkaline washing methods, organic sulfur compounds like COS cannot be directly removed using current technologies. Therefore, COS and other organic sulfur compounds must be converted to H2S through catalytic hydrolysis under specific conditions. After the hydrolyzed hydrogen sulfide-containing blast furnace gas is passed through a turbine for power generation, the hydrogen sulfide is removed through adsorption or alkaline washing, reducing the total sulfur content of the reformed blast furnace gas. This ensures that flue gas emissions from each blast furnace gas combustion point meet local ultra-low emission requirements.

[0005] However, at present, blast furnace gas enters the residual pressure turbine power generation device after the catalytic hydrolysis process. The greater the gas pressure entering the residual pressure turbine power generation device, the greater the power generation through the residual pressure turbine power generation device. The current pressure loss of the existing blast furnace gas after the catalytic hydrolysis process is still somewhat too large, and the gas resistance along the way is large, resulting in the gas pressure entering the residual pressure turbine power generation device not reaching the ideal state. Summary of the Invention

[0006] In response to the above-mentioned problems of the prior art, the present invention provides a gas desulfurization and hydrolysis composite tank and a blast furnace gas fine desulfurization system. The gas desulfurization and hydrolysis composite tank adopts radial gas flow, with small gas resistance along the flow and small pressure loss, and can meet the requirements of removing harmful impurities in blast furnace flue gas and catalytically hydrolyzing organic sulfides.

[0007] To achieve the above object, the technical solution of the present invention is:

[0008] A gas decontamination and hydrolysis composite tank comprises a reaction tank body, wherein the reaction tank body is radially provided with a gas inlet and a gas outlet, at least three mesh partitions are arranged inside the reaction tank body, the mesh partitions are arranged parallel to or at an acute angle to the center line of the reaction tank, and the gas flows radially along the tank body. The mesh partitions divide the interior of the reaction tank body into a gas distribution chamber, a decontamination chamber, a catalytic hydrolysis chamber and a gas collecting chamber. The gas inlet is arranged on the peripheral side of the reaction tank body close to the gas distribution chamber, and the gas outlet is arranged on the peripheral side of the reaction tank body close to the gas collecting chamber. A decontamination agent is placed in the decontamination chamber, and an organic catalytic converter is placed in the catalytic hydrolysis chamber. The gas enters the distribution chamber from the gas inlet, flows evenly distributed to the decontamination chamber and the catalytic hydrolysis chamber, and is discharged through the gas outlet after merging in the gas collecting chamber.

[0009] The present invention changes the gas flow direction from the usual axial flow to the radial flow, sets a gas inlet and a gas outlet on the peripheral side of the tank body of the reaction tank body, and then installs at least three mesh partitions in the reaction tank body. From the direction of gas flow, the mesh partitions divide the interior of the reaction tank body into a gas distribution chamber, a de-impurity chamber, a catalytic hydrolysis chamber and a gas collection chamber. A de-impurity agent for removing impurities harmful to the organic catalytic converter is placed in the de-impurity chamber, and an organic catalytic converter for converting organic sulfides in the gas into hydrogen sulfide is placed in the catalytic hydrolysis chamber. The mesh partitions limit the positions of solid materials such as the de-impurity agent and the organic catalytic converter, while maintaining the gas flow area. The gas enters the gas distribution chamber from the gas inlet, flows evenly toward the de-impurity chamber and the catalytic hydrolysis chamber, and is discharged through the gas outlet after merging in the gas collection chamber. When the gas passes through the de-impurity and hydrolysis composite tank of the present invention, the gas resistance along the way is small, the pressure loss is reduced, thereby increasing the gas pressure entering the residual pressure turbine power generation device, and also meeting the requirements of removing impurities in the gas and catalytic hydrolysis.

[0010] In a preferred embodiment, the mesh partition is arranged parallel to the center line of the reaction tank body.

[0011] In a preferred embodiment, a feeding hopper is provided on the top of the reaction tank body, the feeding hopper is connected to the decontamination chamber and the catalytic hydrolysis chamber respectively, a first blind plate valve is provided between the feeding hopper and the reaction tank body, and the feeding hopper realizes the function of feeding the decontamination chamber and the catalytic hydrolysis chamber.

[0012] In a preferred embodiment, a buffer hopper and an impeller feeder are provided at the bottom of the reaction tank body, the buffer hopper is connected to the de-impurity chamber and the catalytic hydrolysis chamber respectively, a second blind plate valve is provided between the buffer hopper and the reaction tank body, and an impeller feeder is provided at the bottom to facilitate discharge of materials for the de-impurity chamber and the catalytic hydrolysis chamber. The buffer hopper is provided to facilitate multiple discharges.

[0013] In a preferred embodiment, a plurality of supporting plates are axially arranged in the de-impurity chamber and the catalytic hydrolysis chamber, the supporting plates are arranged at an angle to the center line of the reaction tank body, the supporting plates are fixedly connected to the mesh partitions, and a gap is left between the supporting plates and the tank wall of the reaction tank body; or the supporting plates are fixedly connected to the tank wall of the reaction tank body, and a gap is left between the supporting plates and the mesh partitions.

[0014] Generally, the reaction tank is set very high, and the de-impurity agent and organic catalytic converter are added from the top of the reaction tank to the de-impurity chamber and catalytic hydrolysis chamber. Taking the de-impurity agent as an example, since the de-impurity agent must be piled up in the entire de-impurity chamber, the de-impurity agent at the bottom may be crushed by the de-impurity agent on the upper part, thereby losing the removal effect. Therefore, a number of supporting plates are set along the axial direction from top to bottom, and the supporting plates are set at an angle. The inclination angle of the supporting plates to the center line is determined according to the stacking angle of the material (de-impurity agent or organic catalytic converter) to be placed. The supporting plates are spaced apart from the mesh partition or the tank wall of the reaction tank body to reduce the vertical pressure of the material, thereby preventing the de-impurity agent at the bottom from being broken. The height of adjacent supporting plates is determined according to the compressive strength of the de-impurity agent or organic catalytic converter.

[0015] In a preferred embodiment, the supporting plate is fixedly connected to the mesh partition plate, and a gap is left between the supporting plate and the tank wall of the reaction tank body.

[0016] In a preferred embodiment, guide plates are provided in both the de-impurity chamber and the catalytic hydrolysis chamber. The guide plates are fixedly connected to the tank wall of the reaction tank body at an angle and are provided at the tank wall position at the end of the supporting plate. There is a gap channel between the supporting plate and the guide plates.

[0017] When the impurity-removing agent falls into the next supporting plate from the gap between the supporting plate and the tank wall of the reaction tank body, it flows into the next supporting plate from the inclined surface of the guide plate, which has the effect of guiding flow and also reduces the pressure of the impurity-removing agent. The inclination angle of the guide plate and the tank wall of the reaction tank body is determined according to the natural stacking angle of the impurity-removing agent or organic catalytic converter.

[0018] In a preferred embodiment, the supporting plate is perpendicular to the guide surface of the guide plate, which has a better guide effect.

[0019] To prevent the formation of dead corners where the gas does not contact the de-impurity agent or the organic catalytic converter, in a preferred embodiment, the guide plate and the tank wall of the reaction tank body form a closed area.

[0020] In a preferred embodiment, the supporting plate, guide plate and mesh partition are all made of corrosion-resistant stainless steel.

[0021] In a preferred embodiment, a heat-insulating layer is provided outside the tank body of the reaction tank.

[0022] The present invention also provides a blast furnace gas fine desulfurization system, including the gas desulfurization and hydrolysis composite tank, bag dust collector and residual pressure turbine power generation device of all the above embodiments, the flue gas outlet of the bag dust collector is connected to the gas inlet of the gas desulfurization and hydrolysis composite tank, the gas outlet of the gas desulfurization and hydrolysis composite tank is connected to the residual pressure turbine power generation device, the blast furnace flue gas is dedusted by the bag dust collector, and then enters the desulfurization and hydrolysis composite tank to convert organic sulfide into easily removable hydrogen sulfide with small pressure loss, and then the high-pressure blast furnace gas containing hydrogen sulfide is used to generate electricity through the residual pressure turbine power generation device.

[0023] Due to the adoption of the above technical solution, the present invention has the following advantages and positive effects compared with the prior art:

[0024] The present invention changes the gas flow direction from the usual axial flow to radial flow, sets a gas inlet and a gas outlet on the peripheral side of the tank body of the reaction tank, and then installs at least three mesh partitions in the reaction tank body. From the direction of gas flow, the mesh partitions divide the interior of the reaction tank body into a gas distribution chamber, a decontamination chamber, a catalytic hydrolysis chamber and a gas collection chamber. A decontamination agent for removing impurities harmful to the organic catalytic converter is placed in the decontamination chamber, and an organic catalytic converter for converting organic sulfides in the gas into hydrogen sulfide is placed in the catalytic hydrolysis chamber. The mesh partitions limit the positions of solid materials such as the decontamination agent and the organic catalytic converter, while maintaining the gas flow area. The gas enters the gas distribution chamber from the gas inlet, flows evenly toward the decontamination chamber and the catalytic hydrolysis chamber, and is discharged through the gas outlet after merging in the gas collection chamber. The gas resistance along the way is small, which reduces the pressure loss, thereby increasing the gas pressure entering the residual pressure turbine power generation device, and also meets the requirements of removing impurities in the gas and catalytic hydrolysis.

[0025] In a preferred embodiment of the present invention, supporting plates are provided in the decontamination chamber and the catalytic hydrolysis chamber. Since the decontamination agent and the organic catalytic converter need to be added to the decontamination chamber and the catalytic hydrolysis chamber from the top of the reaction tank, taking the decontamination agent as an example, since the decontamination agent needs to be piled up in the entire decontamination chamber, the decontamination agent at the bottom may be crushed by the decontamination agent at the top. Firstly, it may be carried into another compartment through the mesh partition by the gas, and secondly, the removal effect is poor. Therefore, a plurality of supporting plates are provided axially from top to bottom, and the supporting plates are arranged at an angle and spaced from the mesh partition or the tank wall of the reaction tank body to reduce the vertical pressure of the material, thereby preventing the decontamination agent at the bottom from being broken. The height of adjacent supporting plates is determined according to the compressive strength of the decontamination agent or the organic catalytic converter.

[0026] Another preferred embodiment of the present invention includes guide plates in both the decontamination chamber and the catalytic hydrolysis chamber. The guide plates are fixedly connected at an angle to the wall of the reactor body and positioned at the ends of the support plates. For example, when the decontamination agent falls through the gap between the support plate and the reactor body wall onto the next support plate, it flows from the guide plate's inclined surface onto the next support plate, providing a diversion effect while also reducing the pressure on the decontamination agent. To achieve a more effective diversion effect, the support plate and the guide plate's guide surface are positioned perpendicularly, and the angle of inclination between the guide plate and the reactor body wall is determined based on the natural stacking angle of the decontamination agent or organic catalytic converter. BRIEF DESCRIPTION OF THE DRAWINGS

[0027] Figure 1 Schematic diagram of a gas decontamination and hydrolysis composite tank according to Example 1 of the present invention;

[0028] Figure 2 This is a schematic transverse cross-sectional view of a gas decontamination and hydrolysis composite tank according to Example 1 of the present invention;

[0029] Figure 3 Schematic diagram of the interior of the decontamination chamber or catalytic hydrolysis chamber of Example 1 of the present invention.

[0030] Explanation of the reference numerals: 1-reaction tank body; 2-gas distribution chamber; 3-de-impurity chamber; 4-catalytic hydrolysis chamber; 5-gas collecting chamber; 6-gas inlet; 7-gas outlet; 8-feeding hopper; 9-first blind plate valve; 10-impeller feeder; 11-buffer hopper; 12-second blind plate valve; 13-support plate; 14-guide plate; 15-insulation layer; 16-mesh partition; 161-non-porous partition; 162-grid-shaped partition; 17-triangular enclosed area. DETAILED DESCRIPTION

[0031] The advantages and features of the present invention will become more apparent from the following description and claims.

[0032] Example 1

[0033] See Figure 1 and Figure 2, a gas desulfurization and hydrolysis composite tank, which is used for the fine desulfurization of blast furnace flue gas in this embodiment, and can of course also be used for other gases, includes a reaction tank body 1, the reaction tank body 1 is radially provided with a gas inlet 6 and a gas outlet 7, three mesh partitions 16 are arranged inside the reaction tank body 1, the mesh partitions 16 are arranged parallel to the center line of the reaction tank, and along the direction of radial gas flow, the mesh partitions 16 divide the interior of the reaction tank body 1 into a gas distribution chamber 2, a desulfurization chamber 3, a catalytic hydrolysis chamber 4 and a gas collecting chamber 5, the gas inlet 6 is arranged on the peripheral side of the reaction tank body 1 near the gas distribution chamber 2, the gas outlet 7 is arranged on the peripheral side of the reaction tank body 1 near the gas collecting chamber 5, a desulfurization agent is placed in the desulfurization chamber 3, and an organic catalytic converter is placed in the catalytic hydrolysis chamber 4.

[0034] In this embodiment, the gas flow direction is designed to be radial flow instead of the usual axial flow. A gas inlet 6 and a gas outlet 7 are provided on the peripheral side of the reactor body 1. Then, three mesh partitions 16 are installed in the reactor body 1. From the direction of gas flow, the mesh partitions 16 divide the interior of the reactor body 1 into a decontamination chamber 3 and a catalytic hydrolysis chamber 4. A decontamination agent for removing impurities harmful to the organic catalytic converter is placed in the decontamination chamber 3, and an organic catalytic converter for converting organic sulfides in the gas into hydrogen sulfide is placed in the catalytic hydrolysis chamber 4. The gas enters the gas distribution chamber 2 from the gas inlet 6, flows evenly toward the decontamination chamber 3 and the catalytic hydrolysis chamber 4, and is discharged through the gas outlet 7 after merging in the gas collecting chamber 5. The gas has low resistance along the way, which reduces pressure loss, thereby increasing the gas pressure entering the residual pressure turbine power generation device, while also meeting the requirements of removing impurities in the gas and catalytic hydrolysis.

[0035] The mesh partition 16 limits the position of solid materials such as the impurity remover and the organic catalytic converter, while maintaining the gas flow area. Preferably, the mesh partition 16 is designed as a non-porous partition 161 at the top position of the reaction tank body 1, and the grid-shaped partition 162 is directly connected to the bottom of the tank. The purpose of this is that when the material (impurity remover and organic catalytic converter) collapses slightly, the material on the top can be replenished accordingly, and no gas flow short circuit will occur. Figure 3 shown.

[0036] The reaction tank body adopts a pressure-resistant tank body, and a heat-insulating layer 15 is provided on the outside of the tank body.

[0037] In addition, a feeding hopper 8 is provided on the top of the reaction tank body 1 , and the feeding hopper 8 is connected to the de-impurity chamber 3 and the catalytic hydrolysis chamber 4 respectively. A first blind plate valve 9 is provided between the feeding hopper 8 and the reaction tank body 1 to realize the feeding function for the de-impurity chamber 3 and the catalytic hydrolysis chamber 4 .

[0038] A buffer hopper 11 and an impeller feeder 10 are provided at the bottom of the reaction tank body 1. The buffer hopper 11 is respectively connected to the de-impurity chamber 3 and the catalytic hydrolysis chamber 4. A second blind plate valve 12 is provided between the buffer hopper 11 and the reaction tank body 1. An impeller feeder 10 is provided at the bottom to facilitate discharge of the de-impurity chamber 3 and the catalytic hydrolysis chamber 4. The buffer hopper 11 is provided to facilitate multiple discharges.

[0039] Generally, the reaction tank is set very high. The impurity remover and the organic catalytic converter are added from the top of the reaction tank to the impurity remover chamber 3 and the catalytic hydrolysis chamber 4. Taking the impurity remover as an example, since the impurity remover is piled up in the entire impurity remover chamber 3, the impurity remover at the bottom may be crushed by the impurity remover at the top, thereby losing the removal effect. In order to prevent the impurity remover from being crushed and losing the removal effect, see Figure 3 Several supporting plates 13 are arranged axially from top to bottom in the de-impurity chamber 3 and the catalytic hydrolysis chamber 4. The supporting plates 13 are arranged at an angle to the center line of the reaction tank body 1. The supporting plates 13 are fixedly connected to the mesh partition 16, and a gap channel is left between the supporting plates 13 and the tank wall of the reaction tank body 1.

[0040] A plurality of supporting plates 13 are arranged axially from top to bottom, and the supporting plates 13 are arranged obliquely and spaced apart from the tank wall of the reaction tank body 1. Each supporting plate 13 bears part of the pressure and transmits it to the tank body 1, thereby preventing the de-doping agent at the bottom from breaking. The height of adjacent supporting plates 13 is determined according to the compressive strength of the de-doping agent or organic catalytic converter.

[0041] Guide plates 14 are provided in both the impurity removal chamber 3 and the catalytic hydrolysis chamber 4. The guide plates 14 are fixedly connected to the tank wall of the reaction tank body 1 at an angle and are provided at the tank wall position at the end of the supporting plate 13. No guide plates 14 are required at the end of the supporting plate 13 at the highest position and the end of the supporting plate 13 at the lowest position.

[0042] When the impurity-removing agent falls into the next supporting plate 13 from the gap between the supporting plate 13 and the tank wall of the reaction tank body 1, it flows into the next supporting plate 13 from the inclined surface of the guide plate 14, which plays a guiding effect and also has a vertical continuous effect of reducing the pressure of the impurity-removing agent. The inclination angle of the guide plate 14 and the tank wall of the reaction tank body 1 is determined according to the natural stacking angle of the impurity-removing agent or the organic catalytic converter.

[0043] In a preferred embodiment, the supporting plate 13 is perpendicular to the plane of the guide plate 14, which has a better guiding effect.

[0044] To prevent the formation of a dead corner where the gas does not contact the de-doping agent or the organic catalytic converter, the guide plate 14 and the tank wall of the reaction tank body 1 preferably form a triangular closed area 17 .

[0045] The supporting plate 13, the guide plate 14 and the mesh partition plate 16 are all made of corrosion-resistant stainless steel.

[0046] Example 2

[0047] like Figure 1 A blast furnace gas fine desulfurization system includes the gas desulfurization and hydrolysis composite tank, a bag dust collector and a residual pressure turbine power generation device (TRT) of the above-mentioned embodiment 1. The flue gas outlet of the bag dust collector is connected to the gas inlet 6 of the gas desulfurization and hydrolysis composite tank, and the gas outlet 7 of the gas desulfurization and hydrolysis composite tank is connected to the residual pressure turbine power generation device. The blast furnace flue gas is dedusted by the bag dust collector and then enters the trisulfurization and hydrolysis composite tank to convert organic sulfide into easily removable hydrogen sulfide with low pressure loss. Then, the high-pressure blast furnace gas containing hydrogen sulfide is used to generate electricity through the residual pressure turbine power generation device.

[0048] The embodiments of the present invention have been described in detail above with reference to the accompanying drawings, but the present invention is not limited to the above embodiments. Even if various changes are made to the present invention, if these changes fall within the scope of the claims of the present invention and their equivalents, they still fall within the scope of protection of the present invention.

Claims

1. A gas decontamination and hydrolysis composite tank, comprising a reaction tank body, wherein the reaction tank body is radially provided with a gas inlet and a gas outlet, at least three mesh partitions are provided inside the reaction tank body, the mesh partitions are arranged parallel to the center line of the reaction tank, and gas flows radially along the tank body, the mesh partitions divide the interior of the reaction tank body into a gas distribution chamber, a decontamination chamber, a catalytic hydrolysis chamber, and a gas collection chamber, the gas inlet is provided on the peripheral side of the reaction tank body near the gas distribution chamber, the gas outlet is provided on the peripheral side of the reaction tank body near the gas collection chamber, a decontamination agent is placed in the decontamination chamber, and an organic catalytic converter is placed in the catalytic hydrolysis chamber; The mesh partition is designed as a non-porous partition at the top of the reaction tank body, and the partition with a grid form directly passes through the bottom of the reaction tank body; A feeding hopper is provided on the top of the reaction tank body, the feeding hopper is communicated with the impurity removal chamber and the catalytic hydrolysis chamber respectively, and a first blind plate valve is provided between the feeding hopper and the reaction tank body; A plurality of supporting plates are axially arranged in the de-impurity chamber and the catalytic hydrolysis chamber. The supporting plates are arranged at an angle to the center line of the reaction tank body. The supporting plates are fixedly connected to the mesh partitions, and a gap is left between the supporting plates and the tank wall of the reaction tank body; or the supporting plates are fixedly connected to the tank wall of the reaction tank body, and a gap is left between the supporting plates and the mesh partitions.

2. The gas decontamination and hydrolysis composite tank according to claim 1, characterized in that: A buffer hopper and an impeller feeder are provided at the bottom of the reaction tank body. The buffer hopper is communicated with the impurity removal chamber and the catalytic hydrolysis chamber respectively. A second blind plate valve is provided between the buffer hopper and the reaction tank body.

3. The gas decontamination and hydrolysis composite tank according to claim 1, characterized in that: The supporting plate is fixedly connected to the mesh partition plate, and a gap is left between the supporting plate and the tank wall of the reaction tank body.

4. The gas decontamination and hydrolysis composite tank according to claim 3, characterized in that: Guide plates are provided in both the de-impurity chamber and the catalytic hydrolysis chamber. The guide plates are fixedly connected to the tank wall of the reaction tank body at an angle and are provided at the tank wall position at the end of the supporting plate. A gap channel is formed between the supporting plate and the guide plates.

5. The gas decontamination and hydrolysis composite tank according to claim 4, characterized in that: The supporting plate is perpendicular to the guide surface of the guide plate.

6. The gas decontamination and hydrolysis composite tank according to claim 4, characterized in that: The guide plate and the tank wall of the reaction tank body form a closed area.

7. The gas decontamination and hydrolysis composite tank according to claim 4, characterized in that: The supporting plate, guide plate and mesh partition plate are all made of stainless steel.

8. The gas decontamination and hydrolysis composite tank according to any one of claims 1 to 7, characterized in that: A heat-insulating layer is provided outside the tank body of the reaction tank body.

9. A blast furnace gas fine desulfurization system, characterized in that: It comprises the gas decontamination and hydrolysis composite tank, bag dust collector and residual pressure turbine power generation device as described in any one of claims 1 to 8, the flue gas outlet of the bag dust collector is connected to the gas inlet of the gas decontamination and hydrolysis composite tank, and the gas outlet of the gas decontamination and hydrolysis composite tank is connected to the residual pressure turbine power generation device.

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