A catalytic utilization system and catalytic conversion utilization method for carbon monoxide in dry quenching emission gas

Abstract

This invention belongs to the field of industrial energy conservation and environmental protection technology, specifically relating to a catalytic utilization system and method for carbon monoxide in dry quenching exhaust gas. The system includes an interconnected catalytic conversion device and a flue gas cooling device. The catalytic conversion device includes a catalytic conversion component for the catalytic conversion reaction, a heat storage component for collecting heat, and a heat exchange component for cooling. The heat storage component enables cascaded recovery of waste heat. This invention employs a heat storage and heating method with staged catalytic catalysis, eliminating the need for mixing and diluting the flue gas. It satisfies the catalytic ignition temperature of CO, avoids catalyst sintering and deactivation, and retains the high concentration of CO2 in the exhaust gas. It simultaneously achieves deep CO purification, efficient waste heat recovery, and carbon resource utilization. The system has a compact layout, low energy consumption, and can reduce the exhaust gas temperature to below 70°C, combining environmental and economic benefits.

Description

Technical Field

[0001] This invention belongs to the field of industrial energy conservation and environmental protection technology, specifically relating to a catalytic utilization system and catalytic conversion method for carbon monoxide in dry quenching vent gas. Background Technology

[0002] Coke is a core raw material in the iron and steel metallurgy industry. Dry quenching (dry coke quenching) has been widely adopted in the coking industry due to its high quenching efficiency, superior coke quality, and good waste heat recovery. The vast majority of coke ovens are equipped with dry quenching devices. During dry quenching operation, to ensure system safety and prevent the accumulation of combustible gas, it is necessary to continuously release the quenching vent gas. This gas contains a high concentration of carbon monoxide (CO, volume concentration 6-8 vol%), as well as small amounts of SO2 and dust. It is characterized by low oxygen and dryness, thus possessing value in pollution control, energy recovery, and carbon resource utilization.

[0003] With increasingly stringent environmental standards, the coking industry urgently needs to reduce pollution and carbon emissions. CO is a toxic, harmful, and high-calorific-value combustible air pollutant; direct emissions not only pollute the environment but also waste energy. Meanwhile, downstream plants such as methanol and LNG plants using coke oven gas generally suffer from carbon-hydrogen ratio imbalances, necessitating the optimization of reactions with high-purity CO2. However, the CO2 concentration in conventional coke oven flue gas is too low for efficient capture. Therefore, catalytically converting CO in dry quenching vent gas into CO2, while simultaneously recovering waste heat and producing high-concentration CO2, has become a core research direction that balances environmental protection, energy conservation, and resource utilization.

[0004] The technology for treating flammable gases from dry quenching coke is constantly being updated. Early treatment focused on SO2 and dust purification, but direct emissions would cause pollution and waste the energy value of CO. In recent years, the treatment technology has shifted to CO catalytic oxidation and waste heat recovery. Relying on catalysts, CO and O2 can undergo a flameless catalytic reaction to generate CO2 and release heat, thus achieving CO treatment and waste heat recovery. However, this technology has two major drawbacks: first, the catalyst requires an ignition temperature of 240-280℃, which is difficult to meet at the initial temperature of the flammable gas; second, catalyst sintering and deactivation shortens its lifespan and increases operation and maintenance costs.

[0005] To address the challenges of temperature rise and ignition temperature, existing technologies often employ a coke oven flue gas blending and dilution scheme. This involves mixing high-temperature flue gas to raise the temperature, dilute CO to below 1 vol%, and increase the oxygen content to above 6 vol%, thereby controlling the temperature rise and preventing catalyst deactivation. However, this technology has the following drawbacks: First, blending with external flue gas pollutes the vented gas, destroying its low-oxygen, dry, and high-CO2 characteristics, rendering it unusable for subsequent carbon capture and resulting in resource loss. Second, the processing air volume increases dramatically, leading to higher system energy consumption and equipment investment, resulting in high operation and maintenance costs. Third, waste heat recovery efficiency is low; the heat from the diluted flue gas is dispersed, resulting in a small heat exchange temperature difference and insufficient utilization of waste heat.

[0006] In summary, existing technologies for treating CO emissions from dry quenching coke oven gas are insufficient to simultaneously achieve deep CO treatment, efficient waste heat recovery, and high-value carbon resource capture. There is an urgent need for a new treatment solution that features stable temperature control, low energy consumption, and recyclable resources. Summary of the Invention

[0007] Based on the above technical background, the main objective of this invention is to provide a catalytic utilization system and catalytic conversion method for carbon monoxide in dry quenching vent gas, so as to overcome the shortcomings of the prior art.

[0008] To achieve the aforementioned objectives, the technical solution adopted by this invention includes:

[0009] The first aspect of the present invention is to provide a catalytic utilization system for carbon monoxide in dry quenching vent gas, the system comprising a catalytic conversion device and a flue gas cooling device connected to each other; wherein the catalytic conversion device comprises a catalytic conversion component, a heat storage component, and a heat exchange component.

[0010] The catalytic conversion component is used to catalytically oxidize CO in the vent gas, converting it into CO2; The heat storage component is connected to the catalytic conversion component. The heat storage component recovers the heat generated after the catalytic reaction of the purified flammable gas and uses the recovered heat to heat the flammable gas, bringing it to the catalytic reaction initiation temperature. This invention, by incorporating a heat storage component, can recover and utilize the heat generated by the catalytic reaction, offering advantages such as energy saving, environmental protection, and cost reduction.

[0011] The heat exchange component is connected to the catalytic conversion component and is used to exchange heat and cool the vent gas after the catalytic reaction is heated, so as to avoid the catalyst from being deactivated at high temperature due to the catalytic reaction heating. By setting up the heat exchange component, the present invention is beneficial to extending the service life of the catalyst.

[0012] The flue gas cooling device is connected to the catalytic conversion device and is used to catalytically oxidize the residual CO in the purified vent gas into CO2 and cool the purified vent gas so that the purified vent gas is discharged from the system at a lower temperature.

[0013] In this invention, the catalytic conversion assembly includes multiple catalytic reactors arranged sequentially along the direction of vent gas flow. Each catalytic reactor catalytically oxidizes CO in the incoming vent gas. By using multiple catalytic reactors, this invention allows for the batch catalytic oxidation of CO in the vent gas, avoiding excessively high temperatures in a single catalytic oxidation reaction that could lead to catalyst deactivation.

[0014] The multiple catalytic reactors can be arranged in a stacked or sequential manner, preferably in a stacked manner. This stacked arrangement not only saves space, but also allows the purified exhaust gas from the catalytic reaction to naturally flow upwards and into the upper catalytic reactor, thereby reducing the flow resistance of the purified exhaust gas.

[0015] The heat storage component includes two heat storage units, which are respectively located at both ends of the catalytic conversion component. The heat storage unit at the inlet end of the purified vent gas is used to heat the purified vent gas with the heat generated by the catalytic reaction, so that the purified vent gas reaches the starting temperature of the catalytic reaction. The heat storage unit at the outlet end of the purified vent gas is used to collect the heat released by the catalytic reaction and use the heat to heat the purified vent gas, thereby realizing the recovery and utilization of the heat of the catalytic reaction.

[0016] The heat exchange assembly includes multiple heat exchangers, with one heat exchanger installed between each pair of adjacent catalytic reactors. The number of heat exchangers is one less than the number of catalytic reactors. Each heat exchanger is used to exchange heat and cool the purified effluent gas flowing out from the adjacent catalytic reactor. This arrangement ensures that the purified effluent gas heated during each catalytic reaction is cooled by the heat exchangers. By using heat exchangers to cool the purified effluent gas after the catalytic reaction, this invention avoids excessively high temperatures in the purified effluent gas, which could lead to catalyst deactivation at high temperatures, effectively extending the catalyst's lifespan and reducing costs.

[0017] In a preferred embodiment of the present invention, the catalytic conversion assembly includes three catalytic reactors, namely a primary catalytic reactor, a secondary catalytic reactor, and a tertiary catalytic reactor; The heat exchange assembly includes two heat exchangers, namely a primary heat exchanger and a secondary heat exchanger; The heat storage assembly includes a primary heat storage unit and a secondary heat storage unit; The primary heat accumulator, primary catalytic reactor, primary heat exchanger, secondary catalytic reactor, secondary heat exchanger, tertiary catalytic reactor, and secondary heat accumulator are connected in sequence.

[0018] The catalytic conversion device employs regenerative combustion combined with staged catalysis (through the installation of multiple catalytic reactors). This approach not only solves the problem of requiring a specific ignition temperature for high-concentration CO catalytic reactions but also enables segmented temperature and oxygen control, preventing catalyst deactivation at high temperatures. The device utilizes segmented catalytic heat exchange, offering advantages such as a large heat exchange temperature difference, high heat exchange efficiency, small heat exchange area, and low system resistance.

[0019] According to the present invention, the materials of the primary heat accumulator and the secondary heat accumulator are selected from one of alumina ceramic, mullite, high alumina, and corundum.

[0020] Preferably, both the primary and secondary heat accumulators are made of alumina ceramic.

[0021] According to the present invention, the volume of both the primary and secondary heat accumulators is 4–8 m³. 3 .

[0022] Preferably, the volume of both the primary and secondary heat accumulators is 6 m³. 3 .

[0023] Catalysts are provided in the primary, secondary, and tertiary catalytic reactors, with a catalyst volume of 4–12 m³ in each reactor. 3 The catalyst is selected from one or more of the following: Pt-based catalysts, Pt-Ru diatomic catalysts with noble metals such as platinum (Pt), palladium (Pd), rhodium (Rh), and ruthenium (Ru) as active components; copper manganese oxide catalysts, copper cerium oxide catalysts, and copper tin oxide catalysts with transition metal oxides as core active components.

[0024] Preferably, the catalyst is a Pt-based catalyst.

[0025] The space velocity of the catalyst used in each catalytic reactor is 2000–40000 h⁻¹. -1 (The space velocity used should be adjusted according to the type of catalyst.) Preferably, the space velocity used for the catalyst in each catalytic reactor is 20,000 h⁻¹. -1 .

[0026] Catalyst space velocity refers to the volume of gaseous or liquid reactants processed per unit volume of catalyst per unit time, and is an important parameter for measuring the processing capacity of a catalyst.

[0027] According to the present invention, both the primary accumulator and the secondary accumulator are provided with an inlet and an outlet for purified vent gas. This arrangement allows the purified vent gas to enter the catalytic conversion device from the inlet of the primary accumulator or the inlet of the secondary accumulator, and allows the purified vent gas after the catalytic reaction to flow out of the catalytic conversion device from the outlet of the primary accumulator or the outlet of the secondary accumulator.

[0028] According to a preferred embodiment of the present invention, a three-way reversing valve is provided between the inlet of the primary heat accumulator, the inlet of the secondary heat accumulator and the purified vent gas inlet pipe, and a three-way reversing valve is also provided between the outlet of the primary heat accumulator, the outlet of the secondary heat accumulator and the flue gas cooling device.

[0029] The function of the three-way reversing valve in this invention is as follows: When the purified exhaust gas flows in from the inlet of the primary accumulator and out from the outlet of the secondary accumulator, the temperature of the primary accumulator gradually decreases as it continuously heats the purified exhaust gas. When the temperature of the primary accumulator drops to the lower limit of the starting temperature of the catalytic reaction, it can no longer heat the purified exhaust gas to the starting temperature of the catalytic reaction. Simultaneously, the secondary accumulator continuously exchanges heat with the purified exhaust gas that has been heated by the catalytic reaction and flows out from the tertiary catalytic reactor. The secondary accumulator continuously collects the heat released by the catalytic reaction, causing its temperature to rise continuously. When the temperature of the secondary accumulator rises to the same temperature as the purified exhaust gas after the catalytic reaction, it can no longer cool the heated purified exhaust gas. At this point, the two three-way reversing valves can be switched simultaneously, allowing the purified exhaust gas to flow from the inlet of the heated secondary accumulator into the catalytic conversion device. The energy collected by the secondary accumulator, after cooling, flows out of the catalytic converter and into the primary accumulator. This energy is then used to heat the purified exhaust gas to the starting temperature of the catalytic reaction. At this point, the secondary accumulator functions as a device for heating the purified exhaust gas. Simultaneously, the purified exhaust gas, heated by the catalytic reaction, flows into the primary accumulator, which then acts as a device for collecting heat from the purified exhaust gas. The primary accumulator continuously collects heat from the purified exhaust gas after the catalytic reaction, causing its temperature to rise continuously. Meanwhile, the heat collected and stored in the secondary accumulator continuously heats the purified exhaust gas, causing its temperature to drop continuously until the heat from the secondary accumulator can no longer heat the purified exhaust gas to the starting temperature of the catalytic reaction. At this point, the two three-way reversing valves are switched simultaneously, allowing the purified exhaust gas to enter from the heated primary accumulator and exit from the cooled secondary accumulator. This cycle continues, allowing the primary and secondary accumulators to continuously switch roles and fulfill their functions.

[0030] According to a further preferred embodiment of the present invention, the purified vent gas inlets of both the primary and secondary heat accumulators are located on the same side of the heat accumulators, and the purified vent gas outlets of both the primary and secondary heat accumulators are located on the opposite side of the purified vent gas inlets. The inlet flue gas reversing valve and the outlet flue gas reversing valve are respectively located on both sides of the catalytic converter. By arranging the reversing valves and vent gas inlets and outlets in the above manner, the overall layout of the catalytic converter is compact, the pipelines and valves are simple, and the operation is convenient.

[0031] In a further preferred embodiment of the present invention, the primary heat accumulator, the primary catalytic conversion reactor, and the primary heat exchanger are installed on one side of the catalytic conversion device in a stacked manner from low to high, and the secondary heat accumulator, the tertiary catalytic conversion reactor, and the secondary heat exchanger are installed on the other side of the catalytic conversion device in a stacked manner from low to high, and the secondary catalytic conversion reactor is installed on top of the primary heat exchanger and the secondary heat exchanger.

[0032] Specifically, the primary heat accumulator is located on one side of the bottom of the catalytic conversion device, a primary catalytic reactor is set above the primary heat accumulator, a primary heat exchanger is set above the primary catalytic reactor, the secondary heat accumulator is located on the other side of the bottom of the catalytic conversion device, a tertiary catalytic reactor is set above the secondary heat accumulator, a secondary heat exchanger is set above the tertiary catalytic reactor, and a secondary catalytic reactor is set above the primary and secondary heat exchangers.

[0033] The above-described configuration results in a three-dimensional integrated structure for the catalytic converter, with all functional components and devices stacked on top of each other. The vent gas inlet / outlet and the three-way reversing valve are also arranged in this manner, giving the device a compact structure, small footprint, and ease of operation. Furthermore, the stacked arrangement effectively reduces the flow resistance of the purified vent gas.

[0034] According to a preferred embodiment of the present invention, the catalytic conversion device further includes a steam drum assembly, which is connected to a heat exchange assembly and is used to cool the heat exchange assembly.

[0035] In this invention, the steam drum assembly is also connected to a flue gas cooling device. The downcomer at the bottom of the steam drum assembly is connected to the heat exchange tube header of the primary heat exchanger and the secondary heat exchanger. The demineralized water at the bottom of the steam drum assembly flows into the heat exchange tube under gravity. After exchanging heat with the high-temperature vent gas, the demineralized water vaporizes and accumulates at the top of the steam drum assembly, continuously producing steam.

[0036] The heat storage component, heat exchange component, steam drum component, and flue gas cooling device described in this invention adopt deep waste heat recovery technology, which can achieve efficient cooling of flue gas. The flue gas temperature discharged from the system can be reduced to below 70°C, which is beneficial for the deep processing of flue gas in subsequent compression or separation.

[0037] According to a preferred embodiment of the present invention, the flue gas cooling device includes a catalytic reactor, a preheater, a mid-section heat exchanger, and a terminal heat exchanger connected in sequence, according to the flow direction of the purified vent gas.

[0038] The catalytic reactor is connected to a heat accumulator at the outlet of the purified vent gas, and is used to further catalytically oxidize the residual CO in the purified vent gas flowing out of the catalytic conversion unit.

[0039] The preheater, intermediate heat exchanger and terminal heat exchanger are used to cool the purified vent gas flowing out of the catalytic reactor in stages. The present invention can cool the purified vent gas after catalytic conversion to below 70°C by means of staged cooling.

[0040] According to a preferred embodiment of the present invention, a three-way reversing valve is provided between the outlet of the primary heat accumulator, the outlet of the secondary heat accumulator, and the catalytic reactor.

[0041] By setting this three-way reversing valve, the purified vent gas flowing out of the first-stage heat accumulator or the purified vent gas flowing out of the second-stage heat accumulator can be introduced into the catalytic reactor for further catalytic oxidation of CO in the purified vent gas.

[0042] In this invention, the system further includes a boiler feedwater device for pumping circulating water to the flue gas cooling device.

[0043] The boiler feedwater device includes a deaerator, which includes a deaerator tank and a deaerator head installed on top of the deaerator tank.

[0044] The deoxygenated water tank is connected to the front heat exchanger and the middle heat exchanger respectively, and is used to buffer the circulating water entering the system.

[0045] The intermediate heat exchanger uses high-temperature heat exchange, with the outlet water temperature above 95℃. A safety valve, a throttling orifice plate, and a pressure reducing valve are installed sequentially between the heat exchanger outlet and the deaerator head to prevent flashing and cavitation problems caused by a sudden pressure drop after the high-temperature return water enters the deaerator. This stabilizes the flow rate and improves system stability.

[0046] The deoxygenation heads are connected to the intermediate heat exchanger, the terminal heat exchanger, and the steam drum assembly, respectively; they are used to remove dissolved oxygen from the external demineralized water.

[0047] The deaerator is used to pump circulating water into the front heat exchanger, the middle heat exchanger, and the terminal heat exchanger to exchange heat and cool them down. At the same time, it uses hot water pumped from the above heat exchangers to heat up the external demineralized water and remove dissolved oxygen. The deaerator water tank serves as a buffer tank, which can be used to buffer the external demineralized water, the circulating water in the system, and the makeup water going to the steam drum components, thus achieving a three-in-one function.

[0048] According to a preferred embodiment of the present invention, the boiler feedwater device further includes a feedwater pump, a circulating pump, a throttling orifice plate, a pressure reducing valve, and a safety valve.

[0049] The water supply pump is connected between the bottom of the deaerator water tank and the front heat exchanger, and is used to pump the circulating water in the deaerator water tank into the front heat exchanger.

[0050] The circulating pump is connected between the lower part of the deaerated water tank and the middle heat exchanger, and is used to send the pumped circulating water into the middle heat exchanger.

[0051] The orifice plate and pressure reducing valve are connected in sequence between the intermediate heat exchanger and the deaerator. The orifice plate and pressure reducing valve are pressure reducing and reflux devices. By reducing pressure in stages, they can prevent flashing and cavitation problems caused by a sudden drop in pressure after the high-temperature return water enters the deaerator. At the same time, they can stabilize the flow rate and improve the system stability.

[0052] According to a preferred embodiment of the present invention, a circulating water return pipeline is provided between the upper part of the deaerator water tank and the top of the deaerator head, and a safety valve is installed on the circulating water return pipeline. The safety valve ensures the safety of the return water in the return pipeline, and the vent of the safety valve is connected to the lower water tank of the deaerator.

[0053] According to the present invention, the deaerator head of the deaerator is connected to the steam drum assembly, the terminal heat exchanger is connected to an external ambient temperature demineralized water, and the steam drum assembly is connected to the upstream heat exchanger.

[0054] With the above setup, in the boiler feedwater system, external ambient temperature demineralized water (approximately 20°C) from the demineralized water network is first heated by heat exchange in the terminal heat exchanger before entering the deaerator head. In the deaerator, it is heated and deoxygenated by circulating water and steam before falling into the atmospheric pressure deaerator tank at the bottom of the deaerator. A circulating pump is connected to the bottom of the deaerator. Under the action of the circulating pump, circulating water is continuously pumped and sent to the intermediate heat exchanger for heat exchange and heating. Then, after being depressurized by a pressure reducing and reflux device (throttling orifice plate and pressure reducing valve), it returns to the deaerator head, mixes with the replenished fresh external ambient temperature demineralized water, deoxygenates, and falls to the bottom of the deaerator (i.e., the deaerator tank). A safety valve is installed on the circulating water reflux pipeline to ensure the safety of the pressure pipeline. The vent of the safety valve is connected to the lower water tank of the deaerator. A feedwater pump is also connected to the lower part of the deaerator. Under its action, circulating water can be continuously pumped out and sent to the preheater. After heat exchange and heating, it is then fed into the steam drum assembly of the catalytic converter.

[0055] According to the present invention, the system further includes an induced draft fan connected to the terminal heat exchanger; the induced draft fan is installed at the rear end of the catalytic conversion device and the flue gas cooling device to keep the pipeline in the system under negative pressure, so as to facilitate the regulation of the reaction efficiency of each stage of catalytic reaction by controlling the oxygen content.

[0056] A second aspect of the present invention provides a method for catalytically utilizing carbon monoxide in dry quenching vent gas using the carbon monoxide catalytic utilization system described in the first aspect of the present invention, the method comprising the following steps: Step 1: The purified vent gas after desulfurization and dust removal is introduced into the heat storage component. After being heated by the heat storage component, the vent gas flows into the catalytic conversion component, where CO in the purified vent gas is catalytically converted into CO2. After the reaction is completed, the vent gas flows into the heat exchange component for heat exchange and cooling. Step 2: The purified flammable gas after catalytic conversion flows out of the catalytic conversion device through the heat storage component and is introduced into the flue gas cooling device for cooling.

[0057] The steps described above are described in detail below.

[0058] In step 1, the flow rate of the purified vent gas is 15,000–25,000 m³. 3 / h.

[0059] Preferably, the flow rate of the purified vent gas is 20,000 m³ / s. 3 / h.

[0060] The initial temperature of the purified vent gas introduced into the catalytic converter is 120–150°C.

[0061] After being heated by the primary heat accumulator, the temperature of the purified vent gas reaches 380–420℃.

[0062] Preferably, after the purified vent gas is heated by the primary heat accumulator, the temperature of the purified vent gas reaches 400℃.

[0063] After catalytic conversion in the primary catalytic reactor, the gas enters the primary heat exchanger. After heat exchange in the primary heat exchanger, the temperature of the vent gas is cooled to 280-300℃.

[0064] After primary catalytic heat exchange, it enters the secondary catalytic reactor for catalytic conversion, and then is cooled to 280-300℃ by secondary heat exchanger.

[0065] After secondary catalytic heat exchange, the vent gas is introduced into the tertiary catalytic reactor for catalytic conversion. The temperature is raised to 400-450°C through catalysis, and then introduced into the secondary heat accumulator. The temperature of the secondary heat accumulator increases, while the temperature of the vent gas decreases.

[0066] The application space velocity of the catalyst in the primary, secondary, and tertiary catalytic reactors is 2000–40000 h⁻¹. -1 .

[0067] Preferably, the application space velocity of the catalyst is 20,000 h⁻¹. -1 .

[0068] The CO concentration in the dry quenching vent gas is approximately 6-8 vol%. Without considering other combustible gas components, the complete catalytic conversion of CO in the vent gas can result in a temperature rise of approximately 450°C. If a one-step catalytic process is used, with an inlet temperature of 260°C, the outlet temperature will reach 710°C, exceeding the catalyst's tolerance temperature and easily causing sintering and deactivation, thus shortening the catalyst's lifespan. This invention sequentially heats the purified vent gas through a regenerator to reach the initial activation temperature of the catalytic reaction. By controlling the catalyst volume and the vent gas flow rate, a single catalytic reaction is performed, achieving approximately 30%-33% catalysis. The temperature of the purified vent gas increases after catalysis. By controlling the catalyst volume and the purified vent gas flow rate, the temperature of the vent gas can be controlled below 450°C, effectively preventing high-temperature sintering and deactivation of the catalyst.

[0069] The heat exchanger in this invention cools down via heat exchange tubes connected to the steam drum assembly. This cooling process lowers the temperature of the heat exchanger and the vent gas to 260–300°C. The vent gas then undergoes a second catalytic heating in a secondary catalytic reactor, with the heating temperature controlled below 450°C and a catalytic conversion rate of approximately 30%–33%. The purified vent gas, after catalytic heating, is then passed through a secondary heat exchanger to cool down to 260–300°C. After this second cooling, the purified vent gas enters a tertiary catalytic reactor for a third catalytic conversion, also with the temperature controlled below 450°C and a catalytic conversion rate of approximately 30%–33%. The vent gas, after undergoing a third catalytic heating process, enters the secondary accumulator. The secondary accumulator lowers the temperature of the vent gas, and the catalytically heated vent gas heats the secondary accumulator, thus reducing the vent gas's own temperature. When the vent gas exits the catalytic converter, some CO still remains. This residual CO undergoes a final deep catalytic conversion in the catalytic reactor of the flue gas cooling device, completely converting the CO. The converted vent gas is then discharged through the system after three stages of cooling in the flue gas cooling device.

[0070] As the process proceeds, the heat accumulator at the inlet of the purified vent gas gradually decreases in temperature due to the continuous heating of the purified vent gas. When the temperature of the heat accumulator at the inlet of the purified vent gas falls below the lower limit of the catalyst activation temperature, it will be unable to heat the purified vent gas to the activation temperature of the catalytic reaction. At this point, it is necessary to simultaneously switch the three-way reversing valves at the inlet and outlet of the catalytic conversion unit to reverse the flow direction of the purified vent gas. This changes the state of the heat accumulator at the inlet of the purified vent gas from heating to collecting heat, and the state of the heat accumulator at the outlet of the purified vent gas from collecting heat to heating. This allows the two heat accumulators to switch between operating states, and the cycle repeats continuously.

[0071] During the catalytic reaction of the purified vent gas in the catalytic converter, the flow direction of the purified vent gas in the catalytic converter can be adjusted by simultaneously switching the three-way reversing valve at the flue gas inlet and the three-way reversing valve at the flue gas outlet.

[0072] The time interval between switching the three-way reversing valve at the flue gas inlet and the three-way reversing valve at the flue gas outlet is 15 to 45 minutes.

[0073] Preferably, the time interval between switching the three-way reversing valve at the flue gas inlet and the three-way reversing valve at the flue gas outlet is 30 minutes.

[0074] For example, the purified exhaust gas is introduced into the catalytic converter through the bottom flue gas inlet of the primary accumulator. Under the heating of the primary accumulator, the purified exhaust gas reaches the initial activation temperature of the catalytic reaction. Then, it passes upward through the primary catalytic reactor for one catalytic conversion. After that, it passes through the primary heat exchanger for heat exchange and cooling. Then, it passes through the secondary catalytic reactor to reach the top of the catalytic converter for secondary catalytic conversion. Then, it passes downward through the secondary heat exchanger for heat exchange and cooling, and then through the tertiary catalytic reactor for further catalytic conversion. The purified exhaust gas, which has been heated after catalytic conversion, is introduced into the secondary accumulator to heat the secondary accumulator and at the same time lowers its own temperature. Finally, it is led out from the bottom outlet of the secondary accumulator to obtain the purified exhaust gas after catalytic conversion of CO. During the catalytic conversion process, the temperature of the primary accumulator decreases as it continuously heats the vent gas, while the secondary accumulator increases as it is continuously heated by the vent gas. Eventually, the temperature of the primary accumulator falls below the catalyst activation temperature limit, making it impossible to heat the purified vent gas to the activation temperature limit. At this point, the three-way reversing valves at the flue gas inlet and outlet are switched simultaneously to reverse the flow direction of the vent gas in the catalytic conversion device. This allows the purified vent gas to enter the catalytic conversion device through the inlet of the secondary accumulator, then flow upwards through the secondary heat exchanger and the secondary catalytic reactor from the tertiary catalytic reactor, and then downwards through the primary heat exchanger and the primary catalytic reactor, finally exiting through the flue gas outlet of the primary accumulator. This cycle repeats continuously.

[0075] The carbon monoxide catalytic utilization system described in this invention does not require mixing or dilution, has a small flue gas volume, low operating energy consumption, and retains the characteristics of low oxygen, dryness, and relatively high CO2 concentration in the vent gas, creating favorable conditions for subsequent carbon capture and CO2 extraction.

[0076] In step 2, the temperature of the flammable gas after catalytic conversion of CO exiting the catalytic conversion unit is ≥280℃.

[0077] The vent gas after catalytic conversion of CO is fed into a flue gas cooling device. From the inlet of the flue gas cooling device, it passes sequentially through the catalytic reactor, the preheater, the intermediate heat exchanger, and the terminal heat exchanger. After cooling, it is discharged from the system.

[0078] A catalyst is placed in the catalytic reactor, and the application space velocity of the catalyst in the catalytic reactor is 10000 h⁻¹. -1 (Dwell time s = 3600 / airspeed h) -1 ) This invention uses a three-stage flue gas heat exchanger for heat exchange and cooling. The medium-temperature heat exchanger (which handles flue gas at 105 to 99°C) adopts a circulating water pressurization design, which can raise the circulating water temperature by 15 to 17°C and reduce the heat exchange area.

[0079] After three stages of cooling by the flue gas cooling device, the temperature of the flue gas discharged from the system is 50-80℃.

[0080] The beneficial effects of this invention are as follows: (1) The carbon monoxide catalytic utilization system of the present invention includes a catalytic conversion device and a flue gas cooling device. The present invention abandons the flue gas mixing and dilution method, which can avoid the pollution of the vent gas by flue gas mixing, prevent the loss of the utilization value of the vent gas, and avoid post-processing. The present invention can avoid the high-temperature deactivation of the catalyst and improve the service life of the catalyst by setting a heat exchange component in the catalytic conversion device. The heat storage component can collect and utilize the heat released by the catalytic reaction, and use the collected heat to heat and purify the vent gas to the starting temperature of the catalytic reaction, which can effectively reduce the energy consumption of the system operation and has the advantages of being green and environmentally friendly.

[0081] (2) The heat storage component in the catalytic conversion device includes two heat storage units, which can respectively realize the functions of heat storage and heating. The catalytic conversion component includes multiple catalytic reactors along the flow direction of the purified vent gas, which can carry out catalytic reactions on the purified vent gas in stages. The heat exchange component includes multiple heat exchangers, which can exchange heat and cool down the purified vent gas heated by the catalytic reaction in batches. The heat storage component, catalytic conversion component and heat exchange component set in this invention adopt the method of heat storage and heating, staged catalysis and staged heat exchange, which not only meets the CO catalytic ignition temperature requirements, but also controls the temperature of each stage of catalysis below 450°C, avoids catalyst sintering and deactivation, realizes complete CO conversion, and solves the environmental protection problem of vent gas emission in this system.

[0082] (3) The flue gas cooling device includes a catalytic reactor and a three-stage heat exchanger. The catalytic reactor can further catalytically convert the residual CO in the vent gas. The three-stage heat exchanger has the advantages of high heat exchange efficiency and maximum recovery of waste heat through staged heat exchange. It can reduce the temperature of the vent gas discharged from the system to below 70°C. Under standard operating conditions, it can stably produce steam at 0.7-0.9 MPa and 6-10 t / h, converting the chemical energy of CO into high-value steam energy.

[0083] (4) The boiler feed water device adopts an integrated design of atmospheric pressure water tank. The boiler feed water device uses circulating water to preheat external ambient temperature demineralized water, which can significantly reduce the consumption of deoxygenated steam, and at the same time realize the efficient recovery of waste heat from the purified vent gas and deoxygenation energy saving.

[0084] (5) The catalytic conversion device, flue gas cooling device and boiler feed water device in the system described in this invention have the advantages of compact structure, low energy consumption and convenient operation and maintenance. Among them, the catalytic conversion device is a vertical integrated structure with each functional area stacked, which greatly reduces the floor space and effectively reduces the system resistance. The catalytic conversion device adopts negative pressure operation and heat storage of heat storage body circulation, which does not require additional heating and a large amount of mixed flue gas, and the operating energy consumption is significantly reduced. At the same time, a bypass flue is set, which can flexibly adjust the system load, facilitate maintenance, and have high operation and running stability.

[0085] (6) The system and utilization method described in this invention adopts a non-mixed conversion method that allows the flue gas to retain the characteristics of low oxygen, dryness and high CO2 concentration, creating excellent conditions for subsequent carbon capture. The captured CO2 can be supplemented to the coke oven gas to methanol / LNG (liquefied natural gas) unit, effectively solving the problem of carbon-hydrogen ratio imbalance and realizing the resource utilization of CO2. The low oxygen dry flue gas converted by this invention can reduce the difficulty and cost of subsequent compression and separation of flue gas, empowering subsequent carbon capture and resource utilization. Attached Figure Description

[0086] Figure 1 A structural flowchart of the system described in this invention is shown; Figure 2 A schematic diagram of the internal structure of the catalytic conversion device of the present invention is shown; Figure 3 A plan view of the system described in this invention is shown.

[0087] Explanation of icon numbers 100-Catalytic Conversion Unit; 101 - Primary heat accumulator; 102 - Primary catalytic reactor; 103 - Primary heat exchanger; 104 - Secondary catalytic reactor; 105 - Secondary heat exchanger; 106 - Three-stage catalytic reactor; 107 - Secondary heat accumulator; 109 - Steam drum assembly; 200 - Boiler feedwater system; 202 - Deaerator; 203 - Water supply pump; 204-Circulating pump; 205 - Safety valve; 206 - Orifice plate; 207 - Pressure reducing valve; 300-Flue gas cooling device; 301 - Catalytic reactor; 302 - Front heat exchanger; 303 - Mid-section heat exchanger; 304 - Terminal heat exchanger. Detailed Implementation

[0088] The present invention will now be described in detail, and its features and advantages will become clearer and more apparent from these descriptions.

[0089] Example The present invention is further illustrated by specific examples below. These embodiments are only for illustrating the present invention and are not intended to limit the scope of the present invention.

[0090] Example 1 A preferred embodiment of a carbon monoxide catalytic utilization system in dry quenching vent gas, such as Figure 1 As shown, the system includes a catalytic converter 100, a boiler feed water device 200, a flue gas cooling device 300, and an induced draft fan C01. The catalytic converter 100, the boiler feed water device 200, and the flue gas cooling device 300 are interconnected.

[0091] like Figure 1 As shown, the catalytic conversion device 100 includes a primary heat accumulator 101, a primary catalytic reactor 102, a primary heat exchanger 103, a secondary catalytic reactor 104, a secondary heat exchanger 105, a tertiary catalytic reactor 106, a secondary heat accumulator 107, and a steam drum assembly 109. The primary heat accumulator 101, primary catalytic reactor 102, and primary heat exchanger 103 are located on the left side inside the catalytic conversion device 100. The secondary heat exchanger 105, tertiary catalytic reactor 106, and secondary heat accumulator 107 are located on the right side inside the catalytic conversion device 100. The secondary catalytic reactor 104 is located at the top of the catalytic conversion device 100. The catalytic conversion device 100 is a vertical integrated structure with a rectangular cross-section, and the left and right sides of the device are symmetrical.

[0092] The primary heat accumulator 101 is located at the bottom left of the catalytic conversion unit 100. A primary catalytic reactor 102 is positioned above the primary heat accumulator 101, and a primary heat exchanger 103 is positioned above the primary catalytic reactor 102. The secondary heat accumulator 107 is located at the bottom right of the catalytic conversion unit 100. A tertiary catalytic reactor 106 is positioned above the secondary heat accumulator 107, and a secondary heat exchanger 105 is positioned above the tertiary catalytic reactor 106. A secondary catalytic reactor 104 is positioned above the primary heat exchanger 103 and the secondary heat exchanger 105. A steam drum assembly 109 is positioned above the secondary catalytic reactor 104. The downcomer at the bottom of the steam drum assembly 109 is connected to the heat exchanger manifold of the primary heat exchanger 103 and the secondary heat exchanger 105. Figure 1 and Figure 2 As shown.

[0093] The volume of both the primary heat accumulator 101 and the secondary heat accumulator 107 is 6 m³. 3 Catalysts were placed in the primary catalytic reactor 102, the secondary catalytic reactor 104, and the tertiary catalytic reactor 106. The catalysts were Pt-based catalysts, and the catalyst volume was 8 m³. 3 .

[0094] A flue gas inlet A1 is provided on the bottom left side of the primary heat accumulator 101, and a flue gas outlet B1 is provided on the bottom right side of the primary heat accumulator 101. A flue gas inlet A2 is provided on the bottom left side of the secondary heat accumulator 107, and a flue gas outlet B2 is provided on the bottom right side of the secondary heat accumulator 107. Figure 1 As shown.

[0095] An air valve F02 is installed at the top of the secondary catalytic reactor 104. A three-way reversing valve T01 is installed between the purified vent gas, flue gas inlet A1, and flue gas inlet A2. An air valve F01 is installed between the three-way reversing valve T01 and the purified vent gas. The purified vent gas is introduced into the catalytic conversion device 100 through flue gas inlet A1 and flue gas inlet A2. A three-way reversing valve T02 is installed between flue gas outlet B1, flue gas outlet B2, and flue gas cooling device 300. After running for a period of time, the three-way reversing valves T01 and T02 can be switched simultaneously to change the inlet and outlet of the catalytic conversion device, so that the purified vent gas alternately flows in and merges on the left and right sides of the catalytic conversion device, thereby realizing the alternating heat release and heating of the primary and secondary heat accumulators, meeting the temperature requirements of catalytic conversion, and reducing energy consumption.

[0096] The process of introducing purified vent gas is as follows: after desulfurization and dust removal, the purified vent gas enters from the bottom left side of the first-stage heat accumulator 101 through the reversing valve T01, passes upward through the first-stage heat accumulator 101, the first-stage catalytic reactor 102, the first-stage heat exchanger 103, and the second-stage catalytic reactor 104 to reach the top of the catalytic conversion device 100, and then passes downward through the second-stage heat exchanger 105, the third-stage catalytic reactor 106, and the second-stage heat accumulator 107 before being led out from the bottom right side of the second-stage heat accumulator 107 through the flue gas outlet B2. When the three-way reversing valves T01 and T02 are switched simultaneously, the purified vent gas after desulfurization and dust removal enters through the reversing valve T02 from the bottom left side of the secondary heat accumulator 107 at flue gas inlet A2. It then passes upwards sequentially through the secondary heat accumulator 107, the tertiary catalytic reactor 106, the secondary heat exchanger 105, and the secondary catalytic reactor 104 to reach the top of the catalytic conversion device 100. Finally, it passes downwards sequentially through the primary heat exchanger 103, the primary catalytic reactor 102, and the primary heat accumulator 101, and exits from the bottom right side of the primary heat accumulator 101 at flue gas outlet B1. A bypass flue and valve F04 are installed between the three-way reversing valve T01, air valve F01, three-way valve T02, and air valve F03. This bypass flue and valve F04 can adjust the operating load of the catalytic converter and facilitate temporary maintenance, such as... Figure 1 and 3 As shown.

[0097] The flue gas cooling device 300 includes a catalytic reactor 301, a preheater 302, a mid-stage heat exchanger 303, and a terminal heat exchanger 304 connected in sequence. An air valve F03 is installed between the three-way reversing valve T02 and the catalytic reactor 301. The catalyst in the catalytic reactor 301 is the same as that in the primary catalytic reactor 102, the secondary catalytic reactor 104, and the tertiary catalytic reactor 106.

[0098] The catalyst in catalytic reactor 301 is a Pt-based catalyst with a volume of 2 m³. 3 .

[0099] The boiler feedwater device 200 includes a deaerator 202, a water pump 203, a circulating pump 204, a safety valve 205, a throttling orifice plate 206, and a pressure reducing valve 207. The deaerator 202 includes a deaerator water tank and a deaerator head installed on top of the deaerator water tank.

[0100] A water pump 203 is installed between the bottom of the deaerator 202 and the front heat exchanger 302. A circulating pump 204 is installed between the lower part of the deaerator 202 and the middle heat exchanger 303. A throttling orifice plate 206 and a pressure reducing valve 207 are installed between the middle heat exchanger 303 and the deaerator head of the deaerator 202. The deaerator head of the deaerator 202 is connected to the terminal heat exchanger 304. A circulating water return pipeline is installed between the upper part of the deaerator water tank of the deaerator 202 and the top of the deaerator head. A safety valve 205 is installed on the circulating water return pipeline. The deaerator head of the deaerator 202 is connected to the steam drum assembly 109. The terminal heat exchanger 304 is connected to an external ambient temperature demineralized water pipeline network.

[0101] The induced draft fan C01 is located downstream of the catalytic converter 100 and the flue gas cooling device 300, and is connected to the terminal heat exchanger 304. The piping system before the fan operates under negative pressure. By adjusting the opening of air valves F01, F02, and F03, the amount of air drawn into the system can be controlled, thereby controlling the oxygen content and regulating the reaction efficiency of each catalytic reaction.

[0102] After the purified vent gas is converted into CO by the catalytic converter 100, it is introduced into the flue gas cooling device 300 through the flue gas outlet B1 or B2. To ensure the completeness of the catalytic conversion, a set of catalytic reactors 301 is provided at the inlet of the flue gas cooling device 300 for further catalytic conversion of any remaining small amount of CO. Subsequently, the high-temperature vent gas obtained after catalytic conversion is cooled by heat exchange with circulating water from the outlet of the feed water pump 203 through the preheater 302, then by heat exchange with circulating water from the outlet of the circulating pump 204 through the intermediate heat exchanger 303, and finally by deep heat exchange with the external ambient temperature demineralized water of the demineralized water network through the terminal heat exchanger 304 before being discharged from the system described in this invention, completing the heat exchange and cooling conversion. The cooled vent gas is then drawn out from the terminal heat exchanger 304 by the induced draft fan CO1.

[0103] Example 2 Similar to the carbon monoxide catalytic utilization system in dry quenching vent gas described in Example 1, the only difference is that: a flue gas inlet A1 is provided on the bottom right side of the primary accumulator 101, a flue gas outlet B1 is provided on the bottom left side of the primary accumulator 101, a flue gas inlet A2 is provided on the bottom right side of the secondary accumulator 107, and a flue gas outlet B2 is provided on the bottom left side of the secondary accumulator 107.

[0104] Example 3 A method for catalytic utilization of carbon monoxide in dry quenching vent gas using the system described in Example 1: With a standard flow rate of 20,000 m³ 3 Taking the dry quenching gas per hour as an example, the temperature of the purified gas after desulfurization and dust removal is about 120-150℃, the CO concentration is about 6-8 vol%, and the total temperature rise of the flue gas is about 350-470℃.

[0105] The dry quenching gas purified by desulfurization and dust removal is introduced into the system through the bottom flue gas inlet A1 of the primary heat accumulator 101. It passes upward through the primary catalytic reactor 102, the primary heat exchanger 103, and the secondary catalytic reactor 104 to reach the top of the catalytic conversion device 100. Then it passes downward through the secondary heat exchanger 105, the tertiary catalytic reactor 106, and the secondary heat accumulator 107, and is then led out from the bottom flue gas outlet B2 of the secondary heat accumulator 107 to obtain the flammable gas after catalytic conversion of CO. When the primary heat accumulator 101 continuously heats the vent gas, causing its own temperature to drop to near the lower limit of the catalyst activation temperature, and it is unable to heat the purified vent gas to the lower limit of the activation temperature, at this time, the three-way reversing valves T01 and T02 are switched simultaneously to reverse the flow direction of the purified vent gas. The purified vent gas is then introduced into the catalytic conversion device through the inlet A2 of the secondary heat accumulator 107, and then flows upward through the secondary heat exchanger 105 and the secondary catalytic reactor 104 from the tertiary catalytic reactor 106. Subsequently, it flows downward through the primary heat exchanger 103 and the primary catalytic reactor 102 from the secondary catalytic reactor 104, and finally exits through the flue gas outlet B1 of the primary heat accumulator 101. This cycle repeats continuously.

[0106] The time interval between switching three-way reversing valves T01 and T02 is 30 minutes. The residence time of the purified vent gas in the catalytic converter is 7 seconds. The application space velocity of the catalyst is 20,000 h⁻¹ in the first-stage, second-stage, and third-stage catalytic reactors. -1 .

[0107] By adjusting the opening of air valve F01, air valve F02, or air valve F03, the rate of introduction of purified vent gas can be adjusted, thereby controlling the reaction rate.

[0108] The inlet temperature of the catalytic converter 100 is approximately 120–150°C. After being heated by a accumulator, the purified vent gas reaches 400°C (the accumulator gradually cools down to 280°C during the switching cycle). The opening of the air valve is adjusted to control the reaction efficiency, ensuring that the outlet temperature of the first-stage catalytic converter is below 450°C. After the first-stage catalysis, the heat exchanger cools the gas to 280–300°C. A second catalytic reaction follows, followed by another cooling to 280–300°C. A third catalytic reaction raises the temperature to approximately 400–450°C, which is then introduced into the accumulator layer. This accumulator layer is heated from 120–150°C to 400–450°C. The switching cycle duration is adjusted to ensure that the outlet temperature of the catalytic converter is not lower than 280°C.

[0109] The flammable gas after catalytic CO conversion is introduced into a flue gas cooling device 300. From the inlet of the flue gas cooling device 300, it sequentially passes through a catalytic reactor 301, a pre-heat exchanger 302, a mid-stage heat exchanger 303, and a terminal heat exchanger 304. The residual CO in the flammable gas after catalytic CO conversion undergoes further catalytic conversion in the catalytic reactor 301. The residence time of the flammable gas after catalytic CO conversion in the catalytic reactor 301 is 0.36 s, and the application space velocity of the catalyst in the catalytic reactor 301 is 10000 h⁻¹. -1 After CO conversion, the exhaust gas is sequentially fed into the front heat exchanger 302, the middle heat exchanger 303, and the terminal heat exchanger 304. After three stages of heat exchange and cooling, the exhaust gas finally exits the system from the terminal heat exchanger 304 at a temperature of about 60°C, an exhaust steam pressure of about 0.8 MPa, and a gas production rate of about 8 t / h.

[0110] In the description of this invention, it should be noted that the terms "upper", "lower", "inner", "outer", "front", "rear", etc., indicate the orientation or positional relationship based on the orientation or positional relationship in the working state of this invention. They are only for the convenience of describing this invention and simplifying the description, and do not indicate or imply that the device or element referred to must have a specific orientation, or be constructed and operated in a specific orientation. Therefore, they should not be construed as limitations on this invention.

[0111] Furthermore, the terms "first," "second," "third," and "fourth" are used for descriptive purposes only and should not be construed as indicating or implying relative importance. In the description of this invention, it should be noted that, unless otherwise explicitly specified and limited, the terms "installed," "connected," and "linked" should be interpreted broadly. For example, they can refer to a fixed connection, a detachable connection, or an integral connection; they can refer to a mechanical connection or an electrical connection; they can refer to a direct connection or an indirect connection through an intermediate medium; and they can refer to the internal communication between two components. Those skilled in the art can understand the specific meaning of the above terms in this invention based on the specific circumstances.

[0112] The present invention has been described above with reference to preferred embodiments; however, these embodiments are merely exemplary and illustrative. Various substitutions and modifications can be made to the present invention based on these embodiments, all of which fall within the scope of protection of the present invention.

Claims

1. A catalytic utilization system for carbon monoxide in dry quenching vent gas, characterized in that, The system includes a catalytic conversion unit and interconnected flue gas cooling units; wherein... The catalytic conversion device includes a catalytic conversion component, a heat storage component, and a heat exchange component; The catalytic conversion component is used to catalytically oxidize CO in the vent gas, converting it into CO2; The heat storage component is connected to the catalytic conversion component. The heat storage component is used to recover the heat generated by the catalytic reaction to heat the vent gas to the starting temperature of the catalytic reaction. The heat exchange component is connected to the catalytic conversion component and is used to exchange heat and cool the vent gas after the catalytic reaction is heated. The flue gas cooling device is connected to the catalytic conversion device and is used to catalytically oxidize the remaining CO in the vent gas into CO2 and cool the vent gas.

2. The catalytic utilization system for carbon monoxide in dry quenching vent gas according to claim 1, characterized in that, The catalytic conversion assembly includes multiple catalytic reactors, which are stacked along the direction of vent gas flow. Each catalytic reactor catalytically oxidizes CO in the incoming vent gas. The heat storage component includes two heat storage units, which are respectively located at both ends of the catalytic conversion component. The heat storage unit at the inlet end of the purified vent gas is used to heat the purified vent gas with the recovered heat from the catalytic reaction, and the heat storage unit at the outlet end of the purified vent gas is used to recover the heat released by the catalytic reaction. The heat exchange assembly includes multiple heat exchangers, with a heat exchanger installed between each two adjacent catalytic reactors. Each heat exchanger is used to exchange heat and cool the purified vent gas flowing out from the adjacent catalytic reactor.

3. The catalytic utilization system for carbon monoxide in dry quenching vent gas according to claim 2, characterized in that, The catalytic conversion assembly includes three catalytic reactors: a primary catalytic reactor, a secondary catalytic reactor, and a tertiary catalytic reactor. The heat exchange assembly includes two heat exchangers, namely a primary heat exchanger and a secondary heat exchanger; The two heat accumulators are a primary heat accumulator and a secondary heat accumulator; The primary heat accumulator, primary catalytic reactor, primary heat exchanger, secondary catalytic reactor, secondary heat exchanger, tertiary catalytic reactor, and secondary heat accumulator are connected in sequence.

4. The catalytic utilization system for carbon monoxide in dry quenching vent gas according to claim 3, characterized in that, The primary heat accumulator, primary catalytic conversion reactor, and primary heat exchanger are installed sequentially on one side of the catalytic conversion device in a stacked manner from low to high. The secondary heat accumulator, tertiary catalytic conversion reactor, and secondary heat exchanger are installed sequentially on the other side of the catalytic conversion device in a stacked manner from low to high. The secondary catalytic conversion reactor is installed on top of the primary and secondary heat exchangers.

5. The catalytic utilization system for carbon monoxide in dry quenching vent gas according to claim 3, characterized in that, According to the flow direction of the purified vent gas, the flue gas cooling device includes a catalytic reactor, a front heat exchanger, a middle heat exchanger and a terminal heat exchanger connected in sequence. The catalytic reactor is connected to a heat accumulator at the outlet of the purified vent gas, and is used to further catalytically oxidize the residual CO in the vent gas flowing out of the catalytic conversion unit. The front heat exchanger, middle heat exchanger, and terminal heat exchanger are used to cool and reduce the temperature of the purified vent gas flowing out of the catalytic reactor in stages.

6. The catalytic utilization system for carbon monoxide in dry quenching vent gas according to claim 3, characterized in that, The catalytic conversion device also includes a steam drum assembly, which is connected to a heat exchange assembly and is used to cool the heat exchange assembly.

7. The catalytic utilization system for carbon monoxide in dry quenching vent gas according to claim 5 or 6, characterized in that, The system also includes a boiler feedwater system for pumping circulating water to the flue gas cooling device. The boiler feedwater device includes a deaerator, which includes a deaerator water tank and a deaerator head installed on top of the deaerator water tank. The deoxygenated water tank is connected to the front heat exchanger and the middle heat exchanger respectively, and is used to buffer the circulating water entering the system. The intermediate heat exchanger uses high-temperature heat exchange. A safety valve, a throttling orifice plate, and a pressure reducing valve are installed in sequence between the heat exchanger outlet and the deaerator head to prevent flashing and cavitation problems caused by a sudden pressure drop after the high-temperature return water enters the deaerator. This can stabilize the flow rate and improve system stability. The deaerator head is connected to the intermediate heat exchanger, the terminal heat exchanger, and the steam drum assembly, respectively. It uses the hot return water from the intermediate heat exchanger to heat the external demineralized water makeup water, thereby removing dissolved oxygen from the external demineralized water.

8. The catalytic utilization system for carbon monoxide in dry quenching vent gas according to claim 3, characterized in that, A three-way reversing valve is installed between the flue gas inlet of the primary heat accumulator, the flue gas inlet of the secondary heat accumulator, and the purified vent gas inlet pipe; used to switch the flow of purified vent gas into the inlet of the catalytic converter. A three-way reversing valve is also installed between the flue gas outlet of the primary heat accumulator, the flue gas outlet of the secondary heat accumulator, and the flue gas cooling device to switch the purified vent gas out of the catalytic converter outlet.

9. A method for catalytically utilizing carbon monoxide in dry quenching vent gas using the catalytic utilization system for dry quenching vent gas described in any one of claims 1 to 8, characterized in that, The method includes the following steps: Step 1: The purified vent gas after desulfurization and dust removal is introduced into the heat storage component. After being heated by the heat storage component, the vent gas flows into the catalytic conversion component, where CO in the purified vent gas is catalytically converted into CO2. After the reaction is completed, the vent gas flows into the heat exchange component for heat exchange and cooling. Step 2: The purified flammable gas after catalytic conversion flows out of the catalytic conversion device through the heat storage component and is introduced into the flue gas cooling device for cooling.

10. The method according to claim 9, characterized in that, A catalyst is incorporated into the catalytic conversion unit, and the application space velocity of the catalyst in the catalytic conversion device is 2000–40000 h⁻¹. -1 .

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