Device for concentrating and deoxidizing SO2 in non-ferrous metal smelting flue gas

Abstract

The utility model relates to a non-ferrous metal smelting flue gas SO2 concentration and deoxidization device which comprises a primary deaerator (1), a secondary deaerator (2), a material preheater (3), a dust removal unit (4), a waste heat recovery unit (5), a deep dust removal unit (6) and a washing unit (7) which are sequentially communicated through pipelines, a branch pipeline communicated with a solid material outlet of the secondary deaerator (2) is also arranged on a flue gas inlet pipeline of the primary deaerator (1), a solid material outlet pipeline respectively connected with the material preheater (3) and the dust removal unit (4) is also arranged on a flue gas inlet pipeline of the secondary deaerator (2), and the material preheater (3) is also connected with a deoxidant source. Compared with the prior art, SO2 in the smelting flue gas can be effectively removed, so that the concentration of SO2 is increased, and oxygen is effectively removed.

Description

Technical Field

[0001] The utility model relates to the fields of metallurgy, chemical industry and environmental protection, in particular to a device for concentrating SO2 and removing oxygen from flue gas in non-ferrous metal smelting. Background Art

[0002] The non-ferrous metal smelting industry occupies a pivotal position in China. At present, China's output of non-ferrous metals ranks first in the world. However, the pollutants generated during the smelting process have also caused serious environmental pollution problems. The pollutants generated during non-ferrous metal smelting mainly include dust, SO2, SO3 and heavy metals, etc. Non-ferrous metal smelting includes two smelting processes: pyrometallurgy and hydrometallurgy. Among them, the pyrometallurgy process is to roast metal oxides into metal vapor at high temperature, and then form metal ingots by cooling. Since the smelting raw materials contain a large amount of metal sulfide ores, a large amount of SO2 will be generated during this process. The amount of SO2 generated by the smelting industry accounts for 30% of the total industrial output, which is the main industrial SO2 emission source. Therefore, the recovery and utilization of sulfur resources in the non-ferrous metal smelting industry has always been an important research direction in the field of flue gas purification of smelting.

[0003] At present, the main methods for treating SO2 in smelting flue gas are dry desulfurization and wet desulfurization. For high-concentration SO2, acid production treatment is generally adopted. However, due to the low added value of industrial sulfuric acid products, the high content of heavy metals, and the high risk coefficient during transportation, resulting in a small transportation radius, it cannot be effectively transported, which is likely to cause inventory backlogs and even affect the safe production of smelting enterprises. Therefore, the effective recovery and utilization of high-concentration SO2 is an important research direction for sulfur resource utilization in non-ferrous metal smelting flue gas. For high-concentration SO2, the method of catalytic reduction to convert it into sulfur is a relatively popular sulfur resource recovery method at present. Elemental sulfur has high economic value, is convenient for storage and transportation, and has its unique advantages. The reducing agents used in this method can be carbon (C), hydrogen (H2), carbon monoxide (CO) and hydrocarbons, etc. Different reducing agents require different reaction conditions and the reaction products are also different. However, due to the residual oxygen with a certain concentration in the smelting flue gas, the consumption of reducing agents increases during the reduction reaction process. Chinese Patent CN115430288A discloses a chemical looping deoxygenation method for power plant flue gas. By introducing the power plant flue gas into a reactor fixed with a reduced oxygen carrier, the oxygen in the flue gas is removed through an oxidation reaction, and the oxidized oxygen carrier and deoxygenated flue gas are obtained, so as to realize the continuous and deep deoxygenation of the power plant flue gas. However, this method has a high cost and may require modifications to existing equipment. Summary of the Invention

[0004] The purpose of the utility model is to overcome the defects of the above-mentioned existing technologies and provide a device for concentrating SO2 and removing oxygen from non-ferrous metal smelting flue gas, which can effectively remove SO2 from the smelting flue gas, so as to realize the concentration improvement of SO2 and the effective removal of oxygen.

[0005] The object of the present utility model can be achieved by the following technical solutions: A device for concentrating SO2 and removing oxygen from the flue gas in non-ferrous metal smelting, comprising a primary deaerator (1), a secondary deaerator (2), a material preheater (3), a dust removal unit (4), a waste heat recovery unit (5), a deep dust removal unit (6) and a washing unit (7) connected in sequence through pipelines. A branch pipeline connecting the solid material outlet of the secondary deaerator (2) is further provided on the flue gas inlet pipeline of the primary deaerator (1). Solid material outlet pipelines respectively connecting the material preheater (3) and the dust removal unit (4) are further provided on the flue gas inlet pipeline of the secondary deaerator (2). The material preheater (3) is further connected to an oxygen scavenger source, and an oxygen scavenger made of metallurgical sulfide ore and coke is used to remove oxygen from the flue gas and increase the concentration of SO2 in the flue gas.

[0006] Further, both the primary deaerator and the secondary deaerator are of a cyclone dust removal structure, and the internal reaction temperature is 800 - 1200 °C.

[0007] Further, the material preheater (3) is of a cyclone dust removal structure, and is provided with an oxygen scavenger material inlet, a solid material outlet, a flue gas inlet and a flue gas outlet. The oxygen scavenger material inlet is connected to the oxygen scavenger source, the solid material outlet is connected to the flue gas inlet of the secondary deaerator (2), the flue gas inlet is connected to the flue gas outlet of the secondary deaerator (2), and the flue gas outlet is connected to the dust removal unit (4).

[0008] Further, a nitrogen protection layer is further provided at the oxygen scavenger material inlet of the material preheater (3) to prevent the introduction of new air.

[0009] Further, the metallurgical flue gas includes high-concentration SO2 flue gas generated by copper smelting, lead smelting, zinc smelting or molybdenum smelting, with an SO2 concentration of 5% - 35%, an oxygen concentration of 1% - 15%, and a flue gas temperature of 700 - 1300 °C.

[0010] Further, the oxygen scavenger source is a storage tank for storing the oxygen scavenger. The oxygen scavenger is one or a combination of copper, lead, zinc, iron or molybdenum metal sulfide powder, coke, semi-coke or pulverized coal, with a powder particle size of 0.01 - 5 mm, and the addition amount is 10 - 1000 g added per 1 m 3 of flue gas.

[0011] Further, the dust removal unit is a two-stage cyclone dust removal device, and the dust concentration in the flue gas after dust removal is < 10 g / m 3 ;

[0012] The waste heat recovery unit is of a shell-and-tube structure, and the flue gas outlet temperature of the waste heat recovery unit is 200 - 300 °C.

[0013] Further, the deep dust removal unit is a high-temperature filtration dust removal structure. A seal is also provided at the outlet of the deep dust removal unit (6) to prevent air from being inhaled during dust cleaning. The flue gas dust concentration at the outlet of the deep dust removal unit is < 30 mg / m 3 , and the airtightness of the system is ensured to prevent air from being inhaled during dust cleaning;

[0014] The washing unit is a spray washing structure. The spray layer is 1 - 3 layers. The spray washing liquid is clean water or dilute acid water. The SO2 content in the flue gas at the outlet of the washing unit is 10 - 40%, and the oxygen content is < 0.5%.

[0015] The present utility model provides a device for concentrating SO2 and efficiently removing oxygen from smelting flue gas, that is, an oxygen remover and a waste heat recovery unit with a gas-solid swirling contact effect are arranged at the high-temperature flue gas outlet of the smelting furnace. Under such conditions, the high-temperature flue gas first passes through the primary oxygen remover and contacts the high-temperature sulfide ore and coke that have been fully preheated in the secondary oxygen remover, so that part of the sulfide ore and coke react rapidly with the oxygen in the flue gas. Then the high-temperature flue gas enters the secondary oxygen remover and contacts the sulfide ore and coke that have been preheated in the material preheater to fully remove the oxygen again. This device can effectively remove SO2 from the smelting flue gas, thereby realizing the concentration increase of SO2 and the effective removal of oxygen.

[0016] Compared with the prior art, the present utility model has the following beneficial effects:

[0017] (1) The present utility model is provided with two-stage oxygen remover units, and a material preheater is also provided and connected to the oxygen remover source. Using metallurgical raw materials such as sulfide ore powder / coke as the oxygen remover, the oxygen in the high-oxygen and high-concentration SO2 flue gas is efficiently removed, and the SO2 concentration in the flue gas is increased.

[0018] (2) While using the two-stage oxygen remover units to remove oxygen from the flue gas, the present utility model technology uses metallurgical sulfide ore raw materials as the oxygen remover to remove the oxygen in the flue gas, while realizing pre-desulfurization treatment by itself, preheating the metallurgical raw materials, and recovering part of the heat in the flue gas.

[0019] (3) The low-oxygen and high-concentration SO2 flue gas obtained by the present utility model technology can be used to produce sulfur, thereby reducing the consumption of reducing agents. This technology has a simple structure, fully utilizes the energy of each link, and has a low operating cost.

[0020] (4) The device of the present utility model enables the high-oxygen and high-concentration SO2 flue gas to pass through the primary oxygen remover, the secondary oxygen remover, and the material preheater in sequence to complete the oxygen removal of the flue gas and the concentration increase of SO2 in the flue gas. And there is a flue gas circulation process after pipelines are arranged between the three devices, thereby increasing the treatment effect on the flue gas. Description of the Drawings

[0021] Figure 1Schematic diagram of the device for concentrating SO2 and removing oxygen from the flue gas in non-ferrous metal smelting according to the present utility model.

[0022] The labels in the figure are as follows:

[0023] 1 - Primary deaerator, 2 - Secondary deaerator, 3 - Material preheater, 4 - Dust removal unit, 5 - Waste heat recovery unit, 6 - Deep dust removal unit, 7 - Washing unit. Specific implementation manners

[0024] The present utility model will be described in detail below with reference to the accompanying drawings and specific embodiments. This embodiment is implemented on the premise of the technical solution of the present utility model, and detailed implementation manners and specific operation processes are given, but the protection scope of the present utility model is not limited to the following embodiments.

[0025] It should be noted that: Similar reference numerals and letters denote similar items in the following drawings. Therefore, once an item is defined in one drawing, it does not need to be further defined and explained in subsequent drawings.

[0026] Some implementation manners of the present utility model will be described in detail below with reference to the accompanying drawings. Without conflict, the following embodiments and the features in the embodiments can be combined with each other.

[0027] In the following embodiments, unless otherwise specified for raw materials or treatment techniques, it means that they are all conventional commercially available raw material products or conventional treatment techniques in the art. Unless otherwise specified for functional components or structures, it means that they are all conventional components or conventional structures adopted in the art to achieve the corresponding functions.

[0028] Embodiment 1

[0029] A device for concentrating SO2 and removing oxygen from the flue gas in non-ferrous metal smelting, as Figure 1 shown, includes: a primary deaerator 1, a secondary deaerator 2, a material preheater 3, a dust removal unit 4, a waste heat recovery unit 5, a deep dust removal unit 6, and a washing unit 7. The gas outlet of the primary deaerator 1 is connected to the secondary deaerator 2, the gas outlet of the secondary deaerator 2 is connected to the material preheater 3, and the solid material outlet (i.e., the solid materials such as sulfide ore and coke as deoxidizers are discharged from the bottom) is connected to the material inlet of the primary deaerator 1; the material inlet of the material preheater 3 is also connected to a deoxidizer source (i.e., a sulfide ore powder / coke source), its gas outlet is connected to the dust removal unit 4, and the solid material outlet is connected to the material inlet of the secondary deaerator 2. The gas outlet of the dust removal unit 4 is connected to the waste heat recovery unit 5, and the solid material outlet is connected to the material inlet of the secondary deaerator 2. The waste heat recovery unit 5 is sequentially connected to the deep dust removal unit 6 and the washing unit 7.

[0030] Among them, the primary deaerator 1 and the secondary deaerator 2 are both cyclone dust removal structures, and the reaction temperature inside the deaerator is 800 - 1200 °C. The material preheater 3 is a cyclone dust removal structure. After the material is preheated, the flue gas outlet temperature of the material preheater 3 is 600 - 800 °C. The inlet of the deoxidizer material is protected by nitrogen to prevent the introduction of new air. The dust removal unit 4 is a two-stage cyclone dust removal device, and the dust concentration in the flue gas after dust removal is < 10 g / m 3 . The deep dust removal unit 6 is a high-temperature filtration dust removal structure, and the dust concentration of the flue gas at the outlet of the deep dust removal unit 6 is < 30 mg / m 3 , and the airtightness of the system is ensured to prevent the inhalation of air during dust cleaning. The washing unit 7 is a spray washing structure, the spray layer is 1 - 3 layers, the spray washing liquid is clean water or dilute acid water, etc., and the SO2 content in the flue gas at the outlet of the washing unit 7 is 10 - 40%, and the oxygen content is < 0.5%.

[0031] During use:

[0032] The high-temperature metallurgical flue gas flowing out from the high-temperature furnace (generally flue gas with high oxygen content and high concentration of SO2) first enters the primary deaerator 1. By reacting with the deoxidizer (sulfide ore and coke, etc.) that has been fully preheated in the secondary deaerator 2, the sulfide ore is desulfurized to a certain extent, and the coke is partially burned to provide heat, generating SO2 and CO2, thereby removing the oxygen in the flue gas. The separated solid material enters the metallurgical furnace for full smelting. The high-temperature flue gas flowing out from the primary deaerator 1 then enters the secondary deaerator 2, and reacts preliminarily with the sulfide ore and coke in the material preheater 3, causing the coke to be partially burned to generate CO2, thereby fully removing the oxygen in the flue gas. The separated solid material enters the primary deaerator 1 for re-reaction. The high-temperature flue gas flowing out from the secondary deaerator 2 then enters the material preheater 3. By mixing with the newly added sulfide ore and coke, the solid material is preheated and the flue gas is cooled to a certain extent. The separated solid material enters the secondary deaerator 2 for re-reaction, and the flue gas enters the subsequent dust removal unit 4. The collected dust returns to the secondary deaerator 2 through the pipeline at the bottom of the material preheater 3. The flue gas flowing out of the dust removal unit 4 is further purified through the waste heat recovery unit 5, the deep dust removal unit 6 and the washing unit 7 to obtain low-oxygen and high-concentration SO2 flue gas, which can be used for the preparation of sulfur, etc.

[0033] Applying the device of Example 1 to treat specific smelting flue gas has obtained good technical effects. The application examples are as follows:

[0034] Application Example 1:

[0035] The volume flow rate is 10 m 31000 °C copper smelting flue gas with a volume flow rate of [[[ID=]]] / h (where the SO2 concentration is 25% and the oxygen concentration is 10%) The high-temperature metallurgical flue gas flowing out of the high-temperature furnace first enters the primary deaerator 1. By reacting with the deoxidizer (a mixture of 1 kg of coke powder and coal powder with a particle size of 0.01 - 5 mm) that has been fully preheated in the secondary deaerator 2, the high-temperature flue gas flowing out of the primary deaerator 1 (with an internal reaction temperature of 900 °C) then enters the secondary deaerator 2 (with an internal reaction temperature of 800 °C). The high-temperature flue gas flowing out of the secondary deaerator 2 then enters the material preheater 3 (with an internal reaction temperature of 700 °C). The separated solid material enters the secondary deaerator 2 for further reaction, and the flue gas enters the subsequent dust removal unit 4. The collected dust is returned to the secondary deaerator 2 through the pipeline at the bottom of the material preheater 3. The flue gas flowing out of the dust removal unit 4 is further purified through the waste heat recovery unit 5, the deep dust removal unit 6, and the washing unit 7. The final outlet flue gas has an SO2 content of 31% and an oxygen content of 0.3%.

[0036] Application Example 2:

[0037] Volume flow rate of 10 m 3 1000 °C copper smelting flue gas with a volume flow rate of [[[ID=]]] / h (where the SO2 concentration is 25% and the oxygen concentration is 10%) The high-temperature metallurgical flue gas flowing out of the high-temperature furnace first enters the primary deaerator 1. By reacting with the deoxidizer (a mixture of 5 kg of coke powder and coal powder with a particle size of 0.01 - 5 mm) that has been fully preheated in the secondary deaerator 2, the high-temperature flue gas flowing out of the primary deaerator (with an internal reaction temperature of 900 °C) then enters the secondary deaerator (with an internal reaction temperature of 800 °C). The high-temperature flue gas flowing out of the secondary deaerator then enters the material preheater (with an internal reaction temperature of 650 °C). The separated solid material enters the secondary deaerator for further reaction, and the flue gas enters the subsequent dust removal unit. The collected dust is returned to the secondary deaerator through the pipeline at the bottom of the material preheater. The flue gas flowing out of the dust removal unit is further purified through the waste heat recovery unit, the deep dust removal unit, and the washing unit. The final outlet flue gas has an SO2 content of 33% and an oxygen content of 0.1%.

[0038] Application Example 3:

[0039] Volume flow rate of 10 m 3 / h 1000℃ copper smelting flue gas (with SO2 concentration of 30% and oxygen concentration of 15%) flowing out of the high-temperature furnace first enters the primary deaerator 1, and reacts with the deoxidizer (5kg coke powder and coal powder mixture, powder particle size of 0.01-5mm) that has been fully preheated in the secondary deaerator 2. The high-temperature flue gas flowing out of the primary deaerator (internal reaction temperature of 900℃) enters the secondary deaerator (internal reaction temperature of 800℃), and the high-temperature flue gas flowing out of the secondary deaerator enters the material preheater (internal reaction temperature of 650℃). The separated solid material enters the secondary deaerator for further reaction, and the flue gas enters the subsequent dust removal unit, and the collected dust returns to the secondary deaerator through the pipeline at the bottom of the material preheater. The flue gas flowing out of the dust removal unit is purified by the waste heat recovery unit, the deep dust removal unit and the washing unit, and the final outlet flue gas has a SO2 content of 35% and an oxygen content of 0.3%.

[0040] Application Example 4:

[0041] Volume flow rate is 10m 3 / h 1000℃ copper smelting flue gas (with SO2 concentration of 25% and oxygen concentration of 10%) flowing out of the high-temperature furnace first enters the primary deaerator 1, and reacts with the deoxidizer (5kg coke powder and coal powder mixture, powder particle size of 0.01-5mm) that has been fully preheated in the secondary deaerator 2. The high-temperature flue gas flowing out of the primary deaerator (internal reaction temperature of 900℃) then enters the secondary deaerator (internal reaction temperature of 800℃), and the high-temperature flue gas flowing out of the secondary deaerator then enters the material preheater (internal reaction temperature of 650℃), the separated solid material enters the secondary deaerator for further reaction, and the flue gas enters the subsequent dust removal unit, and the collected dust returns to the secondary deaerator through the pipeline at the bottom of the material preheater. The flue gas flowing out of the dust removal unit is purified by the waste heat recovery unit, the deep dust removal unit and the washing unit, and the final outlet flue gas has a SO2 content of 30% and an oxygen content of 0.1%.

[0042] Application Example 5:

[0043] Volume flow rate is 10m 31000 °C copper smelting flue gas with a volume flow rate of 10 m³ / h (where the SO₂ concentration is 30% and the oxygen concentration is 15%) flows out of the high-temperature furnace. The high-temperature metallurgical flue gas first enters the primary deoxidizer 1 and reacts with the deoxidizer (a mixture of 5 kg of coke powder and pulverized coal with a powder particle size of 0.01 - 5 mm) that has been fully preheated in the secondary deoxidizer 2. The high-temperature flue gas flowing out of the primary deoxidizer (with an internal reaction temperature of 900 °C) then enters the secondary deoxidizer (with an internal reaction temperature of 800 °C). The high-temperature flue gas flowing out of the secondary deoxidizer then enters the material preheater (with an internal reaction temperature of 650 °C). The separated solid material enters the secondary deoxidizer for re-reaction, and the flue gas enters the subsequent dust removal unit. The collected dust returns to the secondary deoxidizer through the pipeline at the bottom of the material preheater. The flue gas flowing out of the dust removal unit is further purified through a waste heat recovery unit, a deep dust removal unit, and a washing unit. The final outlet flue gas has an SO₂ content of 34% and an oxygen content of 0.1%.

[0044] Application Comparative Example 1:

[0045] 10 m 3 1000 °C copper smelting flue gas with a volume flow rate of 10 m³ / h (where the SO₂ concentration is 25% and the oxygen concentration is 10%) flows out of the high-temperature furnace. The high-temperature metallurgical flue gas only enters the primary deoxidizer 1 and reacts with the deoxidizer (a mixture of 1 kg of coke powder and pulverized coal with a powder particle size of 0.01 - 5 mm) with the temperature in the secondary deoxidizer 2 turned off and fully preheated. The high-temperature flue gas flowing out of the primary deoxidizer 1 (with an internal reaction temperature of 900 °C) then enters the material preheater 3 (with an internal reaction temperature of 700 °C). The separated solid material enters the secondary deoxidizer 1 for re-reaction, and the flue gas enters the subsequent dust removal unit 4. The collected dust returns to the primary deoxidizer through the pipeline at the bottom of the material preheater 3. The flue gas flowing out of the dust removal unit 4 is further purified through a waste heat recovery unit 5, a deep dust removal unit 6, and a washing unit 7. The final outlet flue gas has an SO₂ content of 31% and an oxygen content of 5.5%. It can be seen that when only the primary deoxidizer is used, the oxygen content in the final product is too high.

[0046] Application Comparative Example 2:

[0047] 10 m 31000 °C copper smelting flue gas at a rate of / h (with a SO₂ concentration of 25% and an oxygen concentration of 10%) directly enters the secondary deoxidizer 2 from the high-temperature metallurgical flue gas flowing out of the high-temperature furnace and reacts with the fully preheated deoxidizer (a mixture of 1 kg of coke powder and coal powder, with a powder particle size of 0.01 - 5 mm). The temperature is not set inside the primary deoxidizer 1 and is at room temperature. The high-temperature flue gas flowing out of the secondary deoxidizer 2 then enters the material preheater 3 (with an internal reaction temperature of 700 °C). The separated solid materials enter the secondary deoxidizer 2 for further reaction, while the flue gas enters the subsequent dust removal unit 4. The collected dust returns to the secondary deoxidizer 2 through the pipeline at the bottom of the material preheater 3. The flue gas flowing out of the dust removal unit 4 is further purified through the waste heat recovery unit 5, the deep dust removal unit 6, and the washing unit 7. The SO₂ content in the final outlet flue gas is 31% and the oxygen content is 6.3%. It can be seen that when only using the primary deoxidizer, the oxygen content in the final product is too high.

[0048] The above description of the embodiments is for the convenience of those of ordinary skill in the art to understand and use the invention. It is obvious that those skilled in the art can easily make various modifications to these embodiments and apply the general principles described herein to other embodiments without creative efforts. Therefore, the present utility model is not limited to the above embodiments, and the improvements and modifications made by those skilled in the art without departing from the scope of the present utility model according to the disclosure of the present utility model should be within the protection scope of the present utility model.

Claims

1. A device for concentrating SO2 and removing oxygen from the flue gas in non-ferrous metal smelting, characterized in that, It includes a primary deaerator (1), a secondary deaerator (2), a material preheater (3), a dust removal unit (4), a waste heat recovery unit (5), a deep dust removal unit (6) and a washing unit (7) that are connected in sequence through pipelines. A branch pipeline connecting the solid material outlet of the secondary deaerator (2) is also provided on the flue gas inlet pipeline of the primary deaerator (1). Solid material outlet pipelines respectively connecting the material preheater (3) and the dust removal unit (4) are also provided on the flue gas inlet pipeline of the secondary deaerator (2). The material preheater (3) is also connected to an oxygen scavenger source.

2. The device for concentrating SO2 and removing oxygen from the flue gas in non-ferrous metal smelting according to claim 1, characterized in that, Both the primary deaerator (1) and the secondary deaerator (2) are cyclone dust removal structures.

3. The device for concentrating SO2 and removing oxygen from the flue gas in non-ferrous metal smelting according to claim 1, wherein The material preheater (3) is a cyclone dust removal structure, which is provided with an oxygen scavenger material inlet, a solid material outlet, a flue gas inlet and a flue gas outlet. Among them, the oxygen scavenger material inlet is connected to the oxygen scavenger source, the solid material outlet is connected to the flue gas inlet of the secondary deaerator (2), the flue gas inlet is connected to the flue gas outlet of the secondary deaerator (2), and the flue gas outlet is connected to the dust removal unit (4).

4. A device for concentrating SO2 and removing oxygen from the flue gas in non-ferrous metal smelting according to claim 1, characterized in that, A nitrogen protection layer is also provided at the oxygen scavenger material inlet of the material preheater (3).

5. A device for concentrating SO2 and removing oxygen from the flue gas in non-ferrous metal smelting according to claim 1, characterized in that, The oxygen scavenger source is a storage tank for storing oxygen scavenger.

6. The device for concentrating SO2 and removing oxygen from the flue gas in non-ferrous metal smelting according to claim 1, characterized in that, The dust removal unit (4) is a two-stage cyclone dust removal device.

7. The device for concentrating SO2 and removing oxygen from the flue gas in non-ferrous metal smelting according to claim 1, characterized in that, The waste heat recovery unit (5) is of a shell-and-tube structure.

8. A device for concentrating SO2 and removing oxygen from flue gas in non-ferrous metal smelting according to claim 1, characterized in that, The deep dust removal unit (6) is a high-temperature filtration dust removal structure, and a seal for preventing air from being inhaled during dust cleaning is also provided at the outlet of the deep dust removal unit (6).

9. The device for concentrating SO2 and removing oxygen from the flue gas in non-ferrous metal smelting according to claim 1, characterized in that, The washing unit (7) is a spray washing structure, the spray layer is 1 - 3 layers, and the spray washing liquid is clean water or dilute acid water.

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