Reactor and reaction system for low-temperature catalytic decomposition of sulfur oxides
By using a combination of spherical reactors and catalysts under low-temperature conditions, the problem of low decomposition efficiency of sulfur oxides at low temperatures was solved, achieving efficient and low-energy decomposition and recovery of sulfur oxides and eliminating secondary pollution.
Patent Information
- Authority / Receiving Office
- CN · China
- Patent Type
- Utility models(China)
- Current Assignee / Owner
- 北京贞吉环保科技有限公司
- Filing Date
- 2025-05-14
- Publication Date
- 2026-05-15
AI Technical Summary
Existing desulfurization technologies have low efficiency in catalytic decomposition of sulfur oxides at low temperatures of 100 to 130 degrees Celsius, high energy consumption, and secondary pollution problems.
A spherical reactor with a diameter greater than 15 mm is used, with macropores and mesopores distributed on the surface and inside. The catalyst is loaded to form a mesoporous reaction unit. Combined with catalysts such as Cu, Fe and their sulfates, a low-temperature catalytic decomposition system is constructed, including a desulfurization tower and bed structure, to achieve low-temperature catalytic decomposition of SO2.
The decomposition efficiency of sulfur oxides was significantly improved at temperatures between 100 and 130 degrees Celsius, reducing energy consumption and costs, eliminating secondary pollution, and the generated elemental sulfur can be recycled.
Smart Images
Figure CN224236531U_ABST
Abstract
Description
Technical Field
[0001] This utility model relates to the field of flue gas desulfurization technology, and in particular to a reactor and reaction system for low-temperature catalytic decomposition of sulfur oxides. Background Technology
[0002] With the acceleration of industrialization, sulfur oxide emissions have become a significant factor in environmental pollution. This is especially true for coal-fired power plants, metallurgy, and chemical industries, whose flue gas contains large amounts of sulfur dioxide and other sulfur oxides. These pollutants not only cause serious damage to the atmospheric environment but may also trigger environmental disasters such as acid rain.
[0003] Existing desulfurization technologies, such as wet desulfurization and solar desulfurization, can remove sulfur oxides to some extent, but they often require high temperatures, are costly, involve complex equipment, consume a lot of energy, and cause serious secondary pollution. Furthermore, the efficiency of catalytic decomposition of sulfur oxides at low temperatures of 100°C to 130°C is very low. Therefore, how to improve the reaction efficiency of catalytic decomposition of sulfur oxides at these low temperatures, and reduce the energy consumption and cost of flue gas desulfurization, has become an urgent technical challenge. Utility Model Content
[0004] The purpose of this invention is to provide a reactor and reaction system for low-temperature catalytic decomposition of sulfur oxides, which improves the reaction efficiency of catalytic decomposition of sulfur oxides under low-temperature conditions of 100°C to 130°C, reduces the energy consumption and cost of flue gas desulfurization, and completely eliminates secondary pollution.
[0005] To achieve the above objectives, this utility model provides the following solution:
[0006] This invention provides a reactor for the low-temperature catalytic decomposition of sulfur oxides:
[0007] The reactor is a spherical reactor with a diameter greater than 15 mm. The surface and interior of the reactor are covered with macropores and mesopores. Both macropores and mesopores are connected to the outside of the reactor and are loaded with catalyst.
[0008] Furthermore, the diameter of the reactor is 20–40 mm.
[0009] Furthermore, the specific surface area of the reactor is 1.00–2.00 m². 2 / g.
[0010] Furthermore, the number of large holes is 1.00 × 10⁻⁶. 11 ~2.00×10 11 indivual.
[0011] Furthermore, the diameter of the macropore is 1600–1900 nm.
[0012] Furthermore, the macropores contain mesopores, and the number of mesopores is 3.00 × 10⁻⁶. 5 ~4.0×10 5 Each has a diameter of 20.00–30.00 nm.
[0013] This invention also provides a reaction system for the low-temperature catalytic decomposition of sulfur oxides, comprising:
[0014] A desulfurization tower, wherein the desulfurization tower is provided with at least one bed for low-temperature catalytic decomposition of sulfur oxides, the bed being formed by a plurality of the above-mentioned reactors being closely stacked;
[0015] The flue gas inlet pipe has an inlet for introducing the flue gas to be treated, and the outlet pipe is connected to the inlet at the top of the desulfurization tower.
[0016] The flue gas outlet is connected to the outlet at the bottom of the desulfurization tower, and the outlet of the flue gas outlet is used to connect to the chimney.
[0017] Furthermore, it also includes:
[0018] An induced draft fan is connected between the smoke outlet end of the smoke outlet pipe and the chimney;
[0019] A chimney direct discharge bypass pipe, with its two ends connected to the inlet pipe and the outlet pipe, respectively;
[0020] A shut-off valve is installed on the flue gas inlet pipe, the flue gas outlet pipe, and the chimney bypass pipe; the shut-off valve on the flue gas inlet pipe is located downstream of the connection point between the flue gas inlet pipe and the chimney bypass pipe, the shut-off valve on the flue gas outlet pipe is located upstream of the connection point between the flue gas outlet pipe and the chimney bypass pipe, and the shut-off valve on the chimney bypass pipe is located at both ends of the chimney bypass pipe.
[0021] Furthermore, the desulfurization tower is provided with three bed layers.
[0022] Furthermore, the total void volume of the bed layer is ≥60%.
[0023] Furthermore, the main active components of the catalyst are Cu, Fe and their sulfates as the main active acidic body materials, and the co-active materials of the catalyst are one or more metal oxides selected from CeO2, Fe2SO3, NiO, ZrO, TiO2, and Nb2O5.
[0024] The present invention achieves the following technical advantages over the prior art:
[0025] This invention discloses a reactor and reaction system for low-temperature catalytic decomposition of sulfur oxides. The spherical reactors are tightly packed within a desulfurization tower, forming a bed within the tower. During the reaction, the temperature inside the tower is raised to 100–130 degrees Celsius. A completely inelastic collision, adsorption, and catalytic integrated mesoporous reaction unit is established within the mesopores of the reactor. This structure increases the pre-factor of the sulfide decomposition reaction and reduces the bond breaking energy, lowering the activation energy for SO2 decomposition to 100–130 KJ / mol. This provides the kinetic conditions for catalytic reaction to achieve SO2 decomposition and removal at 100–130 degrees Celsius. The synergistic effect of the catalyst and the porous structure of the spherical reactor enables the decomposition and removal of SO2 at a low temperature of 100°C to 130°C. In the reactor, SO2 in the flue gas undergoes a catalytic decomposition reaction to generate S and O2. O2 is discharged into the air through the flue, while elemental S diffuses into the air with the flue gas. After cooling, it aggregates into 8-atom sulfur aggregates, which fall into the soil or are recycled and reused to produce sulfur and other industrial raw materials. No harmful by-products are generated, which significantly improves desulfurization efficiency, reduces energy consumption, lowers the cost of flue gas desulfurization, and eliminates secondary pollution. Attached Figure Description
[0026] To more clearly illustrate the technical solutions in the embodiments of this utility model or the prior art, the drawings used in the embodiments will be briefly introduced below. Obviously, the drawings described below are only some embodiments of this utility model. For those skilled in the art, other drawings can be obtained based on these drawings without creative effort.
[0027] Figure 1 A schematic diagram of the reactor provided for an embodiment of this utility model;
[0028] Figure 2 A schematic diagram of the reaction system provided for an embodiment of this utility model;
[0029] Figure 3 A schematic diagram of a desulfurization tower provided for an embodiment of this utility model;
[0030] The components include: 1. Reactor; 2. Macropore; 3. Desulfurization tower; 4. Inlet pipe; 5. Outlet pipe; 6. Exhaust fan; and 7. Chimney direct discharge bypass pipe. Detailed Implementation
[0031] The technical solutions of the present utility model will be clearly and completely described below with reference to the accompanying drawings of the embodiments. Obviously, the described embodiments are only some embodiments of the present utility model, and not all embodiments. Based on the embodiments of the present utility model, all other embodiments obtained by those of ordinary skill in the art without creative effort are within the protection scope of the present utility model.
[0032] The purpose of this invention is to provide a reactor for low-temperature catalytic decomposition of sulfur oxides, which improves the reaction efficiency of catalytic decomposition of sulfur oxides under low-temperature conditions of 100°C to 130°C, reduces the energy consumption and cost of flue gas desulfurization, and completely eliminates secondary pollution.
[0033] To make the above-mentioned objectives, features and advantages of this utility model more apparent and understandable, the utility model will be further described in detail below with reference to the accompanying drawings and specific embodiments.
[0034] Secondary pollution refers to harmful byproducts generated by desulfurization methods such as wet desulfurization and solar desulfurization, which are well known to those skilled in the art and can cause secondary pollution to the environment.
[0035] like Figure 1 As shown, this utility model provides a reactor for low-temperature catalytic decomposition of sulfur oxides. The reactor 1 is a spherical reactor 1 with a diameter greater than 15 mm. The surface of the reactor 1 is distributed with macropores 2 and mesopores, and the interior of the reactor 1 is also distributed with macropores 2 and mesopores. Both macropores 2 and mesopores are connected to the outside of the reactor 1 and are loaded with catalyst.
[0036] Within reactor 1, a fully inelastic collision, adsorption, and catalytic integrated mesoporous reaction unit is established within the mesopores. This structure increases the pre-factor of the sulfide decomposition reaction and reduces the bond breaking energy, lowering the activation energy for SO2 decomposition to 100-130 KJ / mol. This provides the kinetic conditions for catalytic reaction to achieve SO2 decomposition and removal at 100-130°C. The catalyst, through the porous structure of the spherical reactor 1, improves the efficiency of SO2 decomposition and removal at the low temperature of 100-130°C. In the reactor, SO2 in the flue gas undergoes catalytic decomposition, generating S and O2. O2 is discharged through the flue, while elemental S diffuses into the air with the flue gas. After cooling, it aggregates into 8-atom sulfur aggregates, which fall into the soil or are recycled for use in sulfur and other industrial raw materials. No harmful byproducts are generated, reducing the energy consumption and cost of flue gas desulfurization and eliminating secondary pollution.
[0037] The matrix material of reactor 1 can be composed of a ceramic material mainly composed of MgO-SiO2-Al2O3, configured in a weight ratio of 20:50:30; the matrix material also contains a support material for supporting the catalyst. ，The support material is mainly a combination of one or more of the porous materials with a large specific surface area, such as SiO2, Al2O3, and C; the main active component of the catalyst is an acidic material that can generate dual active sites, such as Cu, Fe, and their sulfates, and the co-active material of the catalyst is mainly one or more metal oxides selected from CeO2, Fe2SO3, NiO, ZrO, TiO2, and Nb2O5.
[0038] As a feasible example, reactor 1 has a diameter of 20–40 mm, which facilitates better mass and heat transfer channels in the bed structure of reactor 1 and avoids excessive pressure drop; wherein the specific surface area of reactor 1 is 1.00–2.00 m². 2 / g, the number of macropores 2 is 1.00×10 11 ~2.00×10 11 There are 2 macropores, with a diameter of 1600–1900 nm. Macropores 2 contain mesopores, with a number of 3.00 × 10⁻⁶. 5 ~4.0×10 5 Each device, with a diameter of 20.00–30.00 nm, effectively increases the contact area between reactor 1 and sulfur oxides, thereby enhancing the activity and efficiency of catalytic decomposition of sulfur oxides.
[0039] This invention also provides a reaction system for the low-temperature catalytic decomposition of sulfur oxides, such as... Figures 2-3 As shown, it includes: desulfurization tower 3, flue gas inlet pipe 4, and flue gas outlet pipe 5;
[0040] The desulfurization tower 3 is equipped with at least one bed for low-temperature catalytic decomposition of sulfur oxides, and the bed is composed of multiple reactors 1 tightly stacked. The inlet of the flue gas inlet pipe 4 is used to introduce the flue gas to be treated, and the outlet of the flue gas inlet pipe 4 is connected to the inlet at the top of the desulfurization tower 3. The inlet of the flue gas outlet pipe 5 is connected to the outlet at the bottom of the desulfurization tower 3, and the outlet of the flue gas outlet pipe 5 is used to connect to the chimney. The flue gas enters the desulfurization tower 3 from the flue gas inlet pipe 4, and desulfurizes by contacting and reacting with the flue gas in the reactor 1 inside the desulfurization tower 3. The flue gas that meets the standards is discharged from the flue gas outlet pipe 5.
[0041] As an example of an implementable approach, such as Figure 2 As shown, it also includes an induced draft fan 6, a chimney direct discharge bypass pipe 7, and a shut-off valve;
[0042] The induced draft fan 6 is used to connect the flue gas outlet end of the flue gas pipe 5 to the chimney, thereby enhancing the flow of flue gas and enabling the flue gas to undergo sufficient catalytic decomposition reaction in the desulfurization tower 3, thus improving the catalytic efficiency.
[0043] The two ends of the chimney direct discharge bypass pipe 7 are connected to the inlet pipe 4 and the outlet pipe 5, respectively.
[0044] The shut-off valves are installed on the inlet pipe 4, the outlet pipe 5, and the chimney bypass pipe 7. The shut-off valve on the inlet pipe 4 is located downstream of the connection point between the inlet pipe 4 and the chimney bypass pipe 7, and the shut-off valve on the outlet pipe 5 is located upstream of the connection point between the outlet pipe 5 and the chimney bypass pipe 7. The shut-off valves on the chimney bypass pipe 7 are located at both ends of the chimney bypass pipe 7. When the flue gas meets the emission standards and does not require desulfurization, the shut-off valves on the inlet pipe 4 and the outlet pipe 5 can be closed, and the shut-off valve on the chimney bypass pipe 7 can be opened to directly discharge the flue gas into the atmosphere. When the flue gas requires desulfurization, the shut-off valves on the inlet pipe 4 and the outlet pipe 5 can be opened, and the shut-off valve on the chimney bypass pipe 7 can be closed to allow the flue gas to be introduced into the desulfurization tower 3 for desulfurization. By controlling the opening and closing of the shut-off valves, it is convenient to inspect, regenerate, or replace the catalyst in the desulfurization tower without affecting the flue gas discharge.
[0045] As an example of implementation, the desulfurization tower 3 is equipped with three bed layers to ensure the flue gas flow rate of the desulfurization tower 3 while effectively desulfurizing the flue gas; the total void volume of the bed layer is ≥60%, that is, the total void volume in the bed layer accounts for ≥60% of the entire bed volume, which can ensure that the gas is fully contacted and reacted in each reactor 1, increase the contact area between the catalyst and sulfur oxides, ensure smooth flue gas flow, avoid flue gas stagnation, and improve the overall reaction efficiency of the reaction system.
[0046] This utility model uses specific examples to illustrate its principles and implementation methods. The above description of the embodiments is only for the purpose of helping to understand the core idea of this utility model. At the same time, for those skilled in the art, there will be changes in the specific implementation methods and application scope based on the idea of this utility model. Therefore, the content of this specification should not be construed as a limitation of this utility model.
Claims
1. A reactor for low-temperature catalytic decomposition of sulfur oxides, characterized in that: The reactor is a spherical reactor with a diameter greater than 15 mm. The surface and interior of the reactor are covered with macropores and mesopores. Both macropores and mesopores are connected to the outside of the reactor and are loaded with catalyst.
2. The reactor for low-temperature catalytic decomposition of sulfur oxides according to claim 1, characterized in that: The diameter of the reactor is 20-40 mm.
3. The reactor for low-temperature catalytic decomposition of sulfur oxides according to claim 1, characterized in that: The specific surface area of the reactor is 1.00–2.00 m². 2 / g.
4. The reactor for low-temperature catalytic decomposition of sulfur oxides according to any one of claims 1 to 3, characterized in that: The number of large holes is 1.00 × 10 11 ~2.00×10 11 indivual.
5. The reactor for low-temperature catalytic decomposition of sulfur oxides according to claim 4, characterized in that: The diameter of the macropore is 1600–1900 nm.
6. The reactor for low-temperature catalytic decomposition of sulfur oxides according to claim 4, characterized in that: The macropores contain mesopores, and the number of mesopores is 3.00 × 10⁻⁶. 5 ~4.0×10 5 Each has a diameter of 20.00–30.00 nm.
7. A reaction system for the low-temperature catalytic decomposition of sulfur oxides, characterized in that, include: A desulfurization tower, wherein the desulfurization tower is provided with at least one bed for low-temperature catalytic decomposition of sulfur oxides, the bed being formed by closely stacking multiple reactors as described in any one of claims 1-6; The flue gas inlet pipe has an inlet for introducing the flue gas to be treated, and the outlet pipe is connected to the inlet at the top of the desulfurization tower. The flue gas outlet is connected to the outlet at the bottom of the desulfurization tower, and the outlet of the flue gas outlet is used to connect to the chimney.
8. The low-temperature catalytic decomposition reaction system for sulfur oxides according to claim 7, characterized in that, Also includes: An induced draft fan is connected between the smoke outlet end of the smoke outlet pipe and the chimney; A chimney direct discharge bypass pipe, with its two ends connected to the inlet pipe and the outlet pipe, respectively; A shut-off valve is installed on the flue gas inlet pipe, the flue gas outlet pipe, and the chimney bypass pipe; the shut-off valve on the flue gas inlet pipe is located downstream of the connection point between the flue gas inlet pipe and the chimney bypass pipe, the shut-off valve on the flue gas outlet pipe is located upstream of the connection point between the flue gas outlet pipe and the chimney bypass pipe, and the shut-off valve on the chimney bypass pipe is located at both ends of the chimney bypass pipe.
9. The reaction system for low-temperature catalytic decomposition of sulfur oxides according to claim 7, characterized in that: The desulfurization tower is equipped with three bed layers.
10. The reaction system for low-temperature catalytic decomposition of sulfur oxides according to claim 7, characterized in that: The total void volume of the bed layer is ≥60%.