Reduction device and system for resource treatment of smelting flue gas

Abstract

The utility model discloses a reduction device which is characterized in that the reduction device comprises a reduction tower and an in-tower heat exchanger, the reduction tower is provided with a first reaction space and a second reaction space, and catalyst layers are arranged in the first reaction space and the second reaction space; the in-tower heat exchanger is provided with a first heat exchange channel and a second heat exchange channel capable of exchanging heat with the first heat exchange channel; the output end of the first heat exchange channel is communicated with the inlet of the first reaction space, and the outlet of the catalyst layer in the first reaction space is communicated with the input end of the second heat exchange channel; the output end of the second heat exchange channel is communicated with the inlet of the second reaction space. By adopting the reduction device, the in-tower heat exchanger is arranged in the reduction tower, and the integrated design is adopted, so that the occupied area and the flue gas pipeline are saved, the equipment cost is reduced, meanwhile, the shortening of the flue gas pipeline reduces the heat loss, and the energy utilization rate is improved. The utility model further discloses a system for resource treatment of the smelting flue gas.

Description

Technical Field

[0001] This application belongs to the field of smelting flue gas treatment technology, specifically relating to a reduction device and a system for resource-based treatment of smelting flue gas. Background Technology

[0002] Currently, the mainstream method for treating sulfur dioxide-containing flue gas from smelters is to first convert the sulfur dioxide in the flue gas into concentrated sulfuric acid, and then perform flue gas desulfurization treatment on the remaining flue gas. Concentrated sulfuric acid, as a highly corrosive and toxic liquid, faces numerous challenges in its transportation and storage. For enterprises in remote areas or those without sulfuric acid users within a few hundred kilometers, the high cost of transporting and storing concentrated sulfuric acid directly restricts their development.

[0003] In recent years, many domestic enterprises have developed technologies for the resource-based treatment of smelting flue gas, especially the technology of preparing sulfur from sulfur dioxide in smelting flue gas. For example, utility model patent CN105502302A discloses a method and system for preparing sulfur from smelting flue gas. First, the smelting flue gas is purified to obtain high-purity sulfur dioxide gas. The pure sulfur dioxide gas and hydrogen sulfide gas are then introduced into three series-connected fixed-bed reactors to react and generate sulfur. Before the three series-connected fixed-bed reactors, an additional fixed-bed reactor is set up to react a portion of the prepared sulfur product with water gas, coal, and other substances to generate hydrogen sulfide gas. The four fixed-bed reactors connected in series result in complex process pipelines, require corresponding heat exchangers, and occupy a large area. Utility Model Content

[0004] Therefore, in view of the problem that the existing flue gas to sulfur production system has a large equipment footprint, it is necessary to provide a reduction device and a system for resource-based treatment of smelting flue gas that can treat flue gas containing sulfur dioxide with a small equipment footprint.

[0005] The technical solution proposed in this application is as follows:

[0006] A reduction apparatus, characterized in that it comprises:

[0007] The reduction tower has a first reaction space and a second reaction space, and both the first reaction space and the second reaction space are provided with a catalyst layer;

[0008] The heat exchanger inside the tower has a first heat exchange channel and a second heat exchange channel capable of exchanging heat with the first heat exchange channel;

[0009] The output end of the first heat exchange channel is connected to the inlet of the first reaction space, the outlet of the catalyst layer in the first reaction space is connected to the input end of the second heat exchange channel, and the output end of the second heat exchange channel is connected to the inlet of the second reaction space.

[0010] By adopting the above-mentioned reduction device, the heat exchanger is built into the reduction tower in an integrated design, which saves floor space and flue gas ducts, reduces equipment costs, and at the same time, the shortening of the flue gas duct reduces heat loss and improves energy utilization.

[0011] Furthermore, the reacted gas mixture can exchange heat with the newly introduced gas mixture in the first heat exchange channel in the second heat exchange channel, raising the temperature of the newly introduced gas mixture to meet the reaction requirements. Simultaneously, the reacted gas mixture cools down after passing through the heat exchanger inside the tower, ensuring its temperature meets the requirements of the second-stage redox reaction. This allows for the reuse of heat from the reacted gas, improving energy efficiency and reducing costs. By subjecting the mixed gas to a two-stage catalytic redox reaction, the conversion rate of sulfur dioxide can be effectively improved.

[0012] Furthermore, the second heat exchange channel includes a first sub-channel and a second sub-channel; the catalyst layer includes a first catalyst layer, a second catalyst layer, and a third catalyst layer, the first catalyst layer and the second catalyst layer are arranged alternately within the first reaction space, and the output end of the first heat exchange channel is connected to the inlet of the first catalyst layer, the outlet of the first catalyst layer is connected to the input end of the first sub-channel, the output end of the first sub-channel is connected to the inlet of the second catalyst layer, the outlet of the second catalyst layer is connected to the input end of the second sub-channel, and the output end of the second sub-channel is connected to the second reaction space; the third catalyst layer is disposed within the second reaction space;

[0013] In this process, the gas in the first heat exchange channel is transported along a first direction, and the first sub-channel and the second sub-channel are arranged sequentially along a second direction opposite to the first direction.

[0014] Furthermore, it also includes an external heat exchanger, the output end of the second sub-channel is connected to the input end of the external heat exchanger, and the output end of the external heat exchanger is connected to the inlet of the second reaction space.

[0015] Furthermore, the reduction tower also has a connecting space, the output end of the second sub-channel is connected to the inlet of the connecting space, and the outlet of the connecting space is connected to the input end of the heat exchanger outside the tower.

[0016] Furthermore, the reduction tower is provided with a first partition and a second partition. The first partition and the second partition are arranged vertically at intervals in the reduction tower. The first partition cooperates with the heat exchanger in the tower to separate the first reaction space in the reduction tower. The second partition can separate the second reaction space in the reduction tower. The first partition, the heat exchanger in the tower and the second partition enclose the communicating space in the reduction tower.

[0017] Furthermore, the reduction tower is provided with an air inlet, a first air outlet, a reflux outlet and a second air outlet. The first air outlet is connected to the communicating space, and the reflux outlet and the second air outlet are both connected to the second reaction space.

[0018] The reduction device further includes a connecting pipe for connecting the air inlet and the input end of the first heat exchange channel. The input end of the external heat exchanger is connected to the first air outlet, and the output end of the external heat exchanger is connected to the reflux port.

[0019] A system for the resource-based treatment of smelting flue gas includes a reduction device as described above.

[0020] Furthermore, it also includes a condenser, which is connected to the outlet of the second reaction space.

[0021] Furthermore, it also includes a liquid storage tank and a production line, wherein the liquid storage tank is connected to the liquid phase output end of the condenser, and the production line is connected to the liquid storage tank.

[0022] Furthermore, it also includes a purification device, a deoxygenation device, a gas supply device, and a gas delivery assembly. The purification device is used to purify the gas containing sulfur dioxide and input the purified gas into the deoxygenation device. The deoxygenation device is used to remove oxygen from the gas and input the deoxygenated gas into the gas delivery assembly. The gas supply device is used to input reducing gas into the gas delivery assembly. The gas delivery assembly is connected to the input end of the first heat exchange channel.

[0023] In summary, the system for resource-based treatment of smelting flue gas provided in this application has at least the following advantages:

[0024] 1. The smelting flue gas is first purified and deoxygenated before further treatment. Sulfur is prepared by using high concentration of sulfur dioxide, which reduces the amount of gas to be processed in the reduction unit, reduces the equipment size, and reduces investment costs. At the same time, no high-temperature dust removal is required afterward, which avoids dust entering the sulfur and improves the quality of the sulfur.

[0025] 2. The catalytic reaction temperature is low, the operating conditions are mild, and continuous production can be achieved;

[0026] 3. The heat exchanger is built into the reduction tower in an integrated design, which saves floor space and flue gas ducts, reduces equipment costs, and at the same time reduces heat loss and improves energy utilization. Attached Figure Description

[0027] The accompanying drawings are provided to further understand this application and form part of the specification. They are used together with the embodiments of this application to explain this application and do not constitute a limitation thereof.

[0028] Figure 1 This is a schematic diagram of a system for the resource-based treatment of smelting flue gas provided in an embodiment of this application;

[0029] Figure 2 for Figure 1 The diagram shows the structure of the reduction unit in the system for the resource-based treatment of smelting flue gas.

[0030] Label Explanation:

[0031] 110. Gas supply assembly; 120. Purification device; 130. Gas supply device; 140. Deoxygenation device; 150. Exhaust mechanism; 200. Reduction device; 210. Reduction tower; 211. First reaction space; 212. Second reaction space; 213. Connecting space; 214. First partition; 215. Second partition; 220. Heat exchanger inside the tower; 221. First heat exchange channel; 222. First sub-channel; 223. Second sub-channel; 230. Preheater; 241. First catalytic layer; 242. Second catalytic layer; 243. Third catalytic layer; 250. Heat exchanger outside the tower; 260. Connecting pipe; 310. Condenser; 320. Incinerator; 330. Storage tank; 340. Granulator; 350. Conveying device; 360. Packaging machine. Detailed Implementation

[0032] The technical solutions of the embodiments of this application will be clearly and completely described below with reference to the accompanying drawings. Obviously, the described embodiments are only some embodiments of this application, and not all embodiments. Based on the embodiments of this application, all other embodiments obtained by those of ordinary skill in the art without creative effort are within the scope of protection of this application.

[0033] In the description of this application, it should be understood that the terms "center", "longitudinal", "lateral", "length", "width", "thickness", "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", "clockwise", "counterclockwise", etc., indicate the orientation or positional relationship based on the orientation or positional relationship shown in the accompanying drawings. They are used only for the convenience of describing this application and simplifying the description, and do not indicate or imply that the equipment 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 application.

[0034] On the one hand, this application provides a system for the resource-based treatment of smelting flue gas, which can treat smelting flue gas in a resource-based manner and at a low cost.

[0035] like Figure 1As shown, in one embodiment, the system for resource-based treatment of smelting flue gas includes a gas supply assembly 110, a reduction device 200, and a condenser 310. The gas supply assembly 110 is capable of supplying a mixed gas comprising sulfur dioxide and a reducing gas, wherein the sulfur dioxide originates from the smelting flue gas, and the reducing gas can be one or more of natural gas, carbon monoxide, hydrogen sulfide, and hydrogen. It is also certain that the mixed gas will contain at least other impurities, such as impurities in the smelting flue gas other than sulfur dioxide.

[0036] The reduction unit 200 is connected to the gas supply assembly 110 to react the reducing gas with sulfur dioxide to produce gaseous sulfur. The condenser 310 is connected to the reduction unit 200 to obtain and condense the gaseous sulfur. Compared to concentrated sulfuric acid, sulfur is less hazardous, resulting in lower transportation and storage costs.

[0037] The system described above for the resource-based treatment of smelting flue gas mixes sulfur dioxide-containing gas with reducing gas and then enters the reduction unit 200 for reduction to generate gaseous sulfur. The gaseous sulfur is then condensed in the condenser 310. Compared to concentrated sulfuric acid, sulfur is easier to transport and store, thus effectively reducing transportation and storage costs while also improving safety.

[0038] In one embodiment, the system for resource-based treatment of smelting flue gas further includes a purification device 120 and a gas supply device 130. Both the purification device 120 and the gas supply device 130 are connected to the gas delivery assembly 110. The purification device 120 is able to acquire and purify gas containing sulfur dioxide, and then input the purified gas into the gas delivery assembly 110. The gas supply device 130 is used to input reducing gas into the gas delivery assembly 110 so that the purified gas and the reducing gas are mixed in the gas delivery assembly 110, and then the mixed gas including sulfur dioxide and reducing gas is input into the reduction device 200 through the gas delivery assembly 110.

[0039] In one embodiment, the purification device 120 includes a scrubbing tower, a cooling tower, and an electrostatic precipitator. The scrubbing tower can contain defluorinating agents, mercury-removing agents, and other reagents. The appropriate reagent can be added based on the impurities in the smelting flue gas to remove non-metallic impurities such as fluorine and arsenic, as well as metallic impurities such as copper and mercury. The cooling tower is located downstream of the scrubbing tower to cool the scrubbed gas. The electrostatic precipitator is located downstream of the cooling tower to remove acid mist from the cooled gas, thereby completing the purification of the smelting flue gas.

[0040] In one embodiment, the system for resource-based treatment of smelting flue gas further includes a deoxygenation device 140. The deoxygenation device 140 is disposed between the purification device 120 and the gas supply assembly 110, and is used to remove oxygen from the mixed gas, then input the oxygen-removed mixed gas into the gas supply assembly 110. It should be noted that the main component of the deoxygenated gas is sulfur dioxide, and it may also contain small amounts of water, nitrogen, oxygen, and carbon dioxide, but the oxygen concentration is less than 1%.

[0041] In one embodiment, the gas supply assembly 110 includes a delivery pipe and a fan. One end of the delivery pipe is connected to the deoxygenation device 140, and the other end is connected to the reduction device 200. The gas supply device 130 is connected to the delivery pipe and is used to input reducing gas into the delivery pipe so that the gas containing sulfur dioxide and the reducing gas are mixed in the delivery pipe. The fan is installed in the delivery pipe to guide the mixed gas into the reduction device 200.

[0042] Please also refer to Figure 2 Furthermore, the reduction device 200 includes a reduction tower 210 and an in-tower heat exchanger 220, with the in-tower heat exchanger 220 disposed within the reduction tower 210. The reduction tower 210 has a first reaction space 211 and a second reaction space 212, and both the first reaction space 211 and the second reaction space 212 are provided with a catalytic layer. The in-tower heat exchanger 220 has a first heat exchange channel 221 and a second heat exchange channel capable of exchanging heat with the first heat exchange channel 221. The gas supply assembly 110 is connected to the input end of the first heat exchange channel 221 to input the mixed gas into the first heat exchange channel 221.

[0043] The output of the first heat exchange channel 221 is connected to the inlet of the first reaction space 211 to introduce the mixed gas into the first reaction space 211, where a first-stage redox reaction occurs under the action of the catalytic layer. The outlet of the catalytic layer in the first reaction space 211 is connected to the inlet of the second heat exchange channel to introduce the mixed gas that has undergone the redox reaction into the second heat exchange channel and exchange heat with the newly introduced mixed gas in the first heat exchange channel 221. The output of the second heat exchange channel is connected to the inlet of the second reaction space 212 to introduce the heat-exchanged mixed gas into the second reaction space 212, where a second-stage redox reaction occurs under the action of the catalytic layer. The outlet of the second reaction space 212 is connected to the condenser 310 to introduce the mixed gas into the condenser 310.

[0044] In the above embodiment, the gas supply assembly 110 inputs the mixed gas into the first heat exchange channel 221. The mixed gas then enters the first reaction space 211 through the first heat exchange channel 221, where a first-stage oxidation-reduction reaction occurs under the action of the catalytic layer. Part of the sulfur dioxide is converted into gaseous sulfur, and the temperature of the mixed gas rises. Subsequently, the mixed gas enters the second heat exchange channel, where it exchanges heat with the gas in the first heat exchange channel 221. That is, the mixed gas in the second heat exchange channel cools down, while the mixed gas in the first heat exchange channel 221 heats up, thus utilizing the heat from the reacted mixed gas and reducing energy consumption. The cooled mixed gas is then input into the second reaction space 212, where a second-stage oxidation-reduction reaction occurs under the action of the catalytic layer, further converting sulfur dioxide into gaseous sulfur. Finally, the gas is input into the condenser 310, where the gaseous sulfur is condensed.

[0045] It should be noted that, as an example, the aforementioned catalytic layer is a catalyst layer, and the catalyst can be an iron-cobalt or iron-molybdenum series composite catalyst. It should also be explained that, in this embodiment, the temperature of the catalytic reaction is 400-700℃, while the temperature of the mixed gas input into the first heat exchange channel 221 is relatively low, and the temperature of the mixed gas after the catalytic reaction is relatively high. Therefore, the heat exchanger 220 inside the tower achieves heat exchange between the mixed gas after the reaction and the newly input mixed gas, ensuring that the temperature of the newly input mixed gas meets the requirements of the catalytic reaction.

[0046] It needs further explanation that, taking natural gas as an example, the reaction principle between sulfur dioxide and natural gas is shown in the following reaction equation:

[0047] 2SO2+CH4 2S + CO2 + 2H2O

[0048] Therefore, the gas mixture after the reaction will contain at least gaseous sulfur, carbon dioxide, and water vapor. Other sulfur-containing components may also be present in the gas mixture after the reaction, but this is not a limitation.

[0049] By employing the aforementioned reduction device 200, the reacted mixed gas can exchange heat with the newly input mixed gas in the first heat exchange channel 221 in the second heat exchange channel, thereby raising the temperature of the newly input mixed gas to meet the reaction requirements. Simultaneously, the reacted mixed gas cools down after passing through the heat exchanger 220 in the tower, ensuring its temperature meets the reaction requirements of the second-stage redox reaction. Thus, the reduction device 200 enables the reuse of heat from the reacted gas, improving energy efficiency and reducing costs. By subjecting the mixed gas to a two-stage catalytic redox reaction, the conversion rate of sulfur dioxide can be effectively improved.

[0050] In addition, the heat exchanger 220 is built into the reduction tower 210, which is an integrated design that saves floor space and flue gas ducts, reduces equipment costs, and at the same time, the shortened flue gas duct reduces heat loss and improves energy utilization.

[0051] It should be explained that, during initial use, a preheater 230 can be installed before the reduction tower 210. The preheater 230 heats the mixed gas initially input into the first heat exchange channel 221, ensuring that the temperature of the initially input mixed gas meets the reaction requirements. After running for a period of time, the reacted mixed gas can exchange heat with the newly input mixed gas. At this point, the preheater 230 can be turned off or its load reduced, thus reducing energy consumption.

[0052] In one embodiment, the second heat exchange channel includes a first sub-channel 222 and a second sub-channel 223, and the catalyst layer includes a first catalyst layer 241, a second catalyst layer 242 and a third catalyst layer 243. The first catalyst layer 241 and the second catalyst layer 242 are arranged at intervals in the first reaction space 211, and the third catalyst layer 243 is disposed in the second reaction space 212.

[0053] The output end of the first heat exchange channel 221 is connected to the inlet of the first catalyst layer 241 to transport the newly input mixed gas to the first catalyst layer 241 and allow it to undergo a first-stage redox reaction under the action of the first catalyst layer 241; the outlet of the first catalyst layer 241 is connected to the inlet of the first sub-channel 222 to input the reacted mixed gas into the first sub-channel 222 and exchange heat with the mixed gas in the first heat exchange channel 221; the output end of the first sub-channel 222 is connected to the inlet of the second catalyst layer 242 to allow the heat-exchanged mixed gas to pass through the first sub-channel 222. The gas is fed into the second catalyst layer 242, where the first stage of the redox reaction continues under its action. The outlet of the second catalyst layer 242 is connected to the inlet of the second sub-channel 223, allowing the reacted mixed gas to exchange heat with the mixed gas in the first heat exchange channel 221. The outlet of the second sub-channel 223 is connected to the second reaction space 212, allowing the heat-exchanged mixed gas to be fed into the second reaction space 212, where the second stage of the redox reaction occurs under the action of the third catalyst layer 243. This process improves both the conversion rate of sulfur dioxide and the heat exchange effect.

[0054] Furthermore, the gas in the first heat exchange channel 221 is transported along a first direction, and the first sub-channel 222 and the second sub-channel 223 are arranged sequentially along a second direction opposite to the first direction. In this way, the mixed gas in the second sub-channel 223 can exchange heat with the mixed gas upstream of the first heat exchange channel 221, and the mixed gas in the first sub-channel 222 can exchange heat with the mixed gas downstream of the first heat exchange channel 221, achieving gradual heating of the mixed gas in the first heat exchange channel 221 and improving the heating effect. Specifically... Figure 2 In the embodiment shown, the first direction is the vertically upward direction, and the second direction is the vertically downward direction.

[0055] It should be explained that among the first catalyst layer 241, the second catalyst layer 242, and the third catalyst layer 243, the first catalyst layer 241 has the highest reaction efficiency, therefore the temperature of the mixed gas output from the first reaction space 211 is the highest. The second catalyst layer 242 has the second highest reaction efficiency, therefore the temperature of the mixed gas passing through the second catalyst layer 242 is lower than the temperature of the mixed gas passing through the first catalyst layer 241, but both are higher than the required catalytic reaction temperature. Thus, by preheating the newly input mixed gas with the mixed gas passing through the second catalyst layer 242, and then reheating the newly input mixed gas with the mixed gas passing through the first catalyst layer 241, the heating effect can be improved to ensure that the temperature of the newly input mixed gas meets the reaction requirements.

[0056] In one embodiment, the reduction device 200 further includes an external heat exchanger, the output end of the second sub-channel 223 being connected to the input end of the external heat exchanger, and the output end of the external heat exchanger being connected to the inlet of the second reaction space 212. Optionally, the external heat exchanger may be a waste heat boiler or other equipment capable of heat reuse, which is not limited herein.

[0057] It should be noted that most of the heat from the mixed gas passing through the first catalytic layer 241 is transferred to the newly input mixed gas to ensure that the temperature of the newly input mixed gas meets the reaction requirements. The mixed gas passing through the second catalytic layer 242 is used to preheat the newly input mixed gas. Therefore, the mixed gas passing through the second catalytic layer 242 can also reuse its heat through the external heat exchanger. It is only necessary to ensure that the temperature of the mixed gas after heat exchange in the external heat exchanger meets the reaction requirements.

[0058] Specifically Figure 2In the illustrated embodiment, the reduction tower 210 also includes a connecting space 213. The first reaction space 211, the connecting space 213, and the second reaction space 212 are arranged vertically from top to bottom. Gas in the first heat exchange channel 221 is transported from bottom to top, and the first sub-channel 222 and the second sub-channel 223 are arranged alternately from top to bottom, with gas inside both transported from top to bottom. The output end of the second sub-channel 223 is connected to the inlet of the connecting space 213, and the outlet of the connecting space 213 is connected to the input end of the external heat exchanger. It can be determined that the first reaction space 211, the second reaction space 212, and the connecting space 213 in the reduction tower 210 are isolated from each other and maintained connected through heat exchange channels or an external heat exchanger, so that the gas input into the reduction tower 210 follows a preset path (e.g., Figure 2 (As indicated by the arrow). The gas flow direction of the first heat exchange channel 221, the first sub-channel 222, and the second sub-channel 223 is as shown by the arrow, but the arrows in the figure do not limit the specific locations of the first heat exchange channel 221, the first sub-channel 222, and the second sub-channel 223.

[0059] Understandably, the connection space 213 is designed to facilitate the connection between the heat exchange channel and the external heat exchanger.

[0060] In one embodiment, the reduction tower 210 is further provided with a first partition 214 and a second partition 215. The first partition 214 and the second partition 215 are arranged vertically at intervals within the reduction tower 210. The first partition 214, in conjunction with the heat exchanger 220 within the tower, separates a first reaction space 211 within the reduction tower 210. The second partition 215 can separate a second reaction space 212 within the reduction tower 210. The first partition 214, the heat exchanger 220, and the second partition 215 together form a communicating space 213 within the reduction tower 210. In other words, the first partition 214 and the second partition 215 can separate the first reaction space 211, the communicating space 213, and the second reaction space 212 within the reduction tower 210. Specifically... Figure 2 In the middle of the reduction tower 210, the heat exchanger 220 is located in the middle of the reduction tower 210. The first partition 214 includes two layers. The two layers of the first partition 214 are arranged vertically between the heat exchanger 220 and the inner wall of the reduction tower 210 to separate the first catalyst layer 241 and the second catalyst layer 242.

[0061] In one embodiment, the reduction tower 210 has an air inlet, a first air outlet, a reflux outlet, and a second air outlet. The air supply assembly 110 is connected to the air inlet. The reduction tower 210 is provided with a connecting pipe 260 that connects the air inlet and the input end of the first heat exchange channel 221. The first air outlet is the outlet of the connecting space 213, and the input end of the heat exchanger outside the tower is connected to the first air outlet. The reflux outlet is the inlet of the second reaction space 212, and the second air outlet is the outlet of the second reaction space 212.

[0062] In one embodiment, the system for resource-based treatment of smelting flue gas further includes an incinerator 320, which is connected to the gas phase output end of the condenser 310. Thus, the sulfur-containing components in the remaining gas can be re-burned into sulfur dioxide through the incinerator 320, achieving the reuse of the sulfur-containing components and improving the sulfur conversion rate.

[0063] In one embodiment, the system for resource-based treatment of smelting flue gas further includes a storage tank 330 and a production line. The storage tank 330 is connected to the liquid phase output end of the condenser 310 to receive liquid sulfur condensed by the condenser 310. The production line is connected to the storage tank 330 to obtain liquid sulfur and prepare the liquid sulfur into related products, such as solid sulfur.

[0064] Furthermore, the production line includes a granulator 340, a conveying device 350, and a packaging machine 360. The granulator 340 is connected to a storage tank 330 to obtain liquid sulfur from the storage tank 330. The granulator 340 can solidify the liquid sulfur to form granular sulfur. The conveying device 350 can transport the granular sulfur prepared by the granulator 340 to the packaging machine 360, which is used to package the granular sulfur. In this embodiment, the granulator 340 is a belt granulator 340, and a low-temperature circulating water cooling mechanism is used. Of course, in other embodiments, if the production line is of other types, the condenser 310 can also directly condense gaseous sulfur into solid sulfur, which is not limited here.

[0065] Furthermore, the conveying device 350 includes a conveyor belt, a bucket elevator, and a hopper. The conveyor belt is located downstream of the granulator 340 and is used to convey granular sulfur to the bucket elevator. The hopper is located above the packaging machine 360, and the bucket elevator is used to lift the granular sulfur into the hopper, and then convey the granular sulfur to the packaging machine 360 ​​through the hopper.

[0066] To further understand the technical solution of this application, this document combines... Figure 1 and Figure 2 The process flow of the resource-based treatment system for smelting flue gas in the above embodiments is illustrated with a specific example:

[0067] The temperature of the smelting flue gas is 300℃, and the sulfur dioxide concentration is 12%. After passing through a scrubbing tower, a cooling tower, and an electrostatic precipitator, the temperature of the smelting flue gas is reduced to 35℃. Next, it is deoxygenated by a deoxygenation device 140. The temperature of the deoxygenated gas is 50℃, and its main components are sulfur dioxide (concentration of 92.4%) and water (concentration of 7.6%). The deoxygenated gas then enters the gas supply assembly 110, mixes with natural gas, and is fed into the reduction tower 210.

[0068] The gas flow rate within the reduction tower 210 is 0.5-1.5 m / s, preferably 0.9 m / s, to ensure both efficiency and reaction effectiveness. The reaction temperature requirements for the first catalyst layer 241, the second catalyst layer 242, and the third catalyst layer 243 are 550-650℃. The mixed gas enters the first reaction space 211 through the first heat exchange channel 221, where it reacts under the catalytic action of the first catalyst layer 241 to generate gaseous sulfur. The reacted mixed gas then enters the first sub-channel 222, where it exchanges heat with the newly input mixed gas, bringing the temperature of the newly input mixed gas to the required reaction temperature while simultaneously lowering the temperature of the mixed gas within the first sub-channel 222. The cooled mixed gas then enters the second catalyst layer 242 and reacts again under its catalytic action. The mixed gas after the second reaction enters the second sub-channel 223, where it exchanges heat with the newly input mixed gas, preheating the newly input mixed gas. The mixed gas then enters the connecting space 213 and from the connecting space 213 enters the external heat exchanger of the tower.

[0069] The mixed gas, after heat exchange in the external heat exchanger, enters the second reaction space 212, where it undergoes a second-stage redox reaction under the catalysis of the third catalytic layer 243. The resulting mixed gas then enters the condenser 310. The condenser 310 condenses the gaseous sulfur into liquid sulfur, which is stored in the storage tank 330. The remaining gas is fed into the incinerator 320, where the sulfur-containing components are burned into sulfur dioxide.

[0070] Liquid sulfur in storage tank 330 can be pumped to granulator 340 by a transfer pump. Granulator 340 cools and solidifies the liquid sulfur to form granular sulfur. Then, the granular sulfur at a temperature of 20-40℃ is conveyed to packaging machine 360 ​​by conveying device 350 for packaging.

[0071] It should be noted that the heat exchanger 220 in the above embodiment can be a single heat exchanger that includes all the heat exchange channels mentioned above; or it can include two heat exchangers arranged vertically, with the upper heat exchanger having a first sub-channel 222 and the lower heat exchanger having a second sub-channel 223, and the two heat exchangers having a directly connected channel in the middle to form the first heat exchange channel 221 mentioned above.

[0072] In summary, the system for resource-based treatment of smelting flue gas provided in this application has at least the following advantages:

[0073] 1. The smelting flue gas is first purified and deoxygenated before subsequent treatment. Sulfur is prepared by using high concentration of sulfur dioxide, which reduces the gas volume of the reduction unit 200, reduces the equipment size, and reduces investment costs. At the same time, no high-temperature dust removal is required afterward, which avoids dust entering the sulfur and improves the quality of sulfur.

[0074] 2. The catalytic reaction temperature is low, the operating conditions are mild, and continuous production can be achieved;

[0075] 3. The heat exchanger 220 is built into the reduction tower 210. The integrated design saves floor space and flue gas ducts, reduces equipment costs, and at the same time, the shortened flue gas duct reduces heat loss and improves energy utilization.

[0076] Although embodiments of this application have been shown and described, it will be understood by those skilled in the art that various changes, modifications, substitutions and variations can be made to these embodiments without departing from the principles and spirit of this application, the scope of which is defined by the appended claims and their equivalents.

Claims

1. A reduction apparatus, characterized in that, include: The reduction tower has a first reaction space and a second reaction space, and both the first reaction space and the second reaction space are provided with a catalyst layer; The heat exchanger inside the tower has a first heat exchange channel and a second heat exchange channel capable of exchanging heat with the first heat exchange channel; The output end of the first heat exchange channel is connected to the inlet of the first reaction space, the outlet of the catalyst layer in the first reaction space is connected to the input end of the second heat exchange channel, and the output end of the second heat exchange channel is connected to the inlet of the second reaction space.

2. The reduction apparatus according to claim 1, characterized in that, The second heat exchange channel includes a first sub-channel and a second sub-channel; the catalyst layer includes a first catalyst layer, a second catalyst layer, and a third catalyst layer. The first catalyst layer and the second catalyst layer are arranged alternately within the first reaction space. The output end of the first heat exchange channel is connected to the inlet of the first catalyst layer, the outlet of the first catalyst layer is connected to the input end of the first sub-channel, the output end of the first sub-channel is connected to the inlet of the second catalyst layer, the outlet of the second catalyst layer is connected to the input end of the second sub-channel, and the output end of the second sub-channel is connected to the second reaction space; the third catalyst layer is disposed within the second reaction space. In this process, the gas in the first heat exchange channel is transported along a first direction, and the first sub-channel and the second sub-channel are arranged sequentially along a second direction opposite to the first direction.

3. The reduction apparatus according to claim 2, characterized in that, It also includes an external heat exchanger, the output end of the second sub-channel is connected to the input end of the external heat exchanger, and the output end of the external heat exchanger is connected to the inlet of the second reaction space.

4. The reduction apparatus according to claim 3, characterized in that, The reduction tower also has a connecting space, the output end of the second sub-channel is connected to the inlet of the connecting space, and the outlet of the connecting space is connected to the input end of the heat exchanger outside the tower.

5. The reduction apparatus according to claim 4, characterized in that, The reduction tower is provided with a first partition and a second partition. The first partition and the second partition are arranged vertically at intervals in the reduction tower. The first partition cooperates with the heat exchanger in the tower to separate the first reaction space in the reduction tower. The second partition can separate the second reaction space in the reduction tower. The first partition, the heat exchanger in the tower and the second partition enclose the communicating space in the reduction tower.

6. The reduction apparatus according to claim 4, characterized in that, The reduction tower is provided with an inlet, a first outlet, a reflux outlet and a second outlet. The first outlet is connected to the communicating space, and the reflux outlet and the second outlet are both connected to the second reaction space. The reduction device further includes a connecting pipe for connecting the air inlet and the input end of the first heat exchange channel. The input end of the external heat exchanger is connected to the first air outlet, and the output end of the external heat exchanger is connected to the reflux port.

7. A system for the resource-based treatment of smelting flue gas, characterized in that, Includes the reduction apparatus as described in any one of claims 1-6.

8. The system for resource-based treatment of smelting flue gas according to claim 7, characterized in that, It also includes a condenser, which is connected to the outlet of the second reaction space.

9. The system for resource-based treatment of smelting flue gas according to claim 8, characterized in that, It also includes a liquid storage tank and a production line, wherein the liquid storage tank is connected to the liquid phase output end of the condenser, and the production line is connected to the liquid storage tank.

10. The system for resource-based treatment of smelting flue gas according to claim 7, characterized in that, It also includes a purification device, a deoxygenation device, a gas supply device, and a gas delivery assembly. The purification device is used to purify the gas containing sulfur dioxide and input the purified gas into the deoxygenation device. The deoxygenation device is used to remove oxygen from the gas and input the deoxygenated gas into the gas delivery assembly. The gas supply device is used to input reducing gas into the gas delivery assembly. The gas delivery assembly is connected to the input end of the first heat exchange channel.

Images