Method for preparing acid by dynamically grading high-concentration copper smelting flue gas

Abstract

The invention discloses a dynamic grading acid making method for high-concentration copper smelting flue gas, and belongs to the technical field of smelting flue gas resourceful treatment. 80-85% of the smelting flue gas is supplied to a pre-conversion section, the temperature of an absorption catalyst layer is 560-580 DEG C, the pre-converted flue gas is supplied to a pre-absorption tower, an absorption circulating tank 1 supplies concentrated sulfuric acid into the tower, sulfur trioxide is absorbed and then returns to the absorption circulating tank 1, the pre-absorbed flue gas is mixed with the residual 15-20% of the smelting flue gas, the mixed gas and pressurized oxygen are supplied to a two-conversion two-absorption system, and the mixed gas and pressurized oxygen are supplied to the pre-absorption tower. The concentration of sulfur dioxide in the flue gas is 9.1-9.3%, the concentration of oxygen is 9.1-9.2%, the oxygen-sulfur ratio is 0.8-1, and the absorption circulating tanks 2 and 3 supply concentrated sulfuric acid to the primary absorption tower and the secondary absorption tower respectively during two-conversion and two-absorption treatment. The pre-absorption tower, the primary absorption tower and the secondary absorption tower are respectively connected with the absorption circulating tanks 1, 2 and 3, the three tanks are communicated to dynamically adjust the acid concentration and the acid temperature, and target sulfuric acid is produced in the absorption circulating tank 3. The technical bottleneck that high-concentration flue gas cannot be directly used for preparing acid is solved, and the conversion rate of the high-concentration flue gas reaches 99.8% or above.

Description

Technical Field

[0001] The invention belongs to the technical field of technical treatment of smelting flue gas, and particularly relates to a method for dynamically classifying acid from high-concentration copper smelting flue gas. Background Art

[0002] A copper company in southern China uses an oxygen-enriched bottom-blown molten pool smelting process combined with a converter blowing process. The bottom of the enhanced smelting furnace is blown with oxygen-enriched air at a concentration of 70-72%. 80-85% of the sulfur is burned and removed in this process, producing flue gas with a SO2 concentration of approximately 30% and high-grade matte. The converter blowing process produces flue gas with a SO2 concentration of approximately 12%. After the two are mixed, the SO2 concentration in the dry flue gas reaches 16-19%, and the flue gas volume is 90,000-100,000 Nm 3 / h, far exceeding the 8-10% SO2 concentration and 80,000-100,000 Nm2 applicable to the original acid production system 3 / h flue gas volume range.

[0003] The sulfur dioxide concentration is as high as 16-19%. When the conventional "two-turn, two-absorption" acid production method is used for production, a large amount of air needs to be added to dilute the high-concentration flue gas to achieve a flue gas sulfur dioxide concentration of 8-10%. This treatment will cause the flue gas volume of the acid production system to increase significantly. The addition of a complete sulfuric acid system requires a large area and large equipment investment. In addition, the flue gas concentration is reduced, resulting in an increase in production costs.

[0004] In summary, high flue gas concentration, large fluctuations in gas concentration and volume, and excessive load can easily lead to thermal imbalance in the conversion process, catalyst overburning, high resistance, high gas velocity, and low conversion efficiency (the conversion rate is only 98.5%). Based on this, the present invention aims to provide a method for dynamically fractionating acid production from high-concentration copper smelting flue gas, resolving the technical problem that conventional "two-conversion, two-absorption" acid production technology cannot directly produce acid from high-concentration flue gas, achieving a stable conversion efficiency of over 99.8% for high-concentration flue gas with a fluctuating gas concentration of 13-19%. Summary of the Invention

[0005] The object of the present invention is to provide a method for producing acid from high-concentration copper smelting flue gas using dynamic classification.

[0006] The object of the present invention is achieved by: the method for producing acid by dynamic classification of high-concentration copper smelting flue gas comprises the following steps: Pre-conversion: 80-85% of the smelting flue gas after dust removal and drying is supplied to the pre-conversion section to maintain the temperature of the pre-conversion absorption catalyst layer at 560-580°C; Pre-absorption: The pre-converted flue gas is supplied to the pre-absorption tower. The absorption circulation tank 1 circulates concentrated sulfuric acid into the pre-absorption tower, where it contacts the flue gas in the tower. The concentrated sulfuric acid absorbs sulfur trioxide through gas-liquid contact. The absorbed concentrated sulfuric acid returns to the absorption circulation tank 1. The pre-absorbed flue gas is pressurized and mixed with the remaining 15-20% of the smelting flue gas after dust removal and drying to form the inlet flue gas of the two-conversion and two-absorption sections. Two-transformation and two-absorption: oxygen is pressurized and supplied to the two-transformation and two-absorption system. After oxygen supply, the sulfur dioxide concentration of the flue gas is 9.1-9.3%, the oxygen concentration is 9.1-9.2%, and the oxygen-sulfur ratio is 0.8-1. The flue gas undergoes primary conversion, primary absorption, secondary conversion, and secondary absorption in sequence. Absorption circulation tanks 2 and 3 circulate concentrated sulfuric acid to the primary absorption tower and the secondary absorption tower respectively, contacting the flue gas in the tower. The concentrated sulfuric acid absorbs sulfur trioxide through gas-liquid contact; The pre-absorption tower, primary absorption tower, and secondary absorption tower are connected to absorption circulation tanks 1, 2, and 3, respectively, and the three circulation tanks are interconnected, so that the three circulation tanks can be interconnected while the three systems can operate independently. The sulfuric acid concentration and temperature of each absorption circulation tank and absorption tower are dynamically adjusted, and finally the target sulfuric acid is produced in the absorption circulation tank 3 and the tail gas is discharged.

[0007] The technical solution of the present invention has the following advantages compared with the prior art: 1. The traditional two-transfer and two-absorption acid-making process cannot meet the barrier of high-concentration flue gas acid production. The pre-absorption and pre-conversion links are creatively added. 80-85% of the dried smelting flue gas first enters the pre-conversion section. The catalyst loading amount is controlled by precise calculation, shortening the contact time between the flue gas and the catalyst. The temperature, conversion rate and other parameters of the pre-conversion process are strictly controlled. Then pre-absorption is carried out to reduce the flue gas volume before mixing it with the remaining flue gas and entering the two-transfer and two-absorption system to solve the problem of high-concentration flue gas treatment.

[0008] 2. In order to address the problem of low oxygen-sulfur ratio of the inlet flue gas in the two-transfer and two-absorption section, an oxygen distribution pipeline is installed to pressurize 90% concentration oxygen and introduce it into the two-transfer and two-absorption system, thereby increasing the oxygen-sulfur ratio from 0.58-0.6 to 0.8-1, ensuring efficient conversion of sulfur dioxide in the two-transfer and two-absorption system and steadily improving the conversion rate.

[0009] 3. Changing the traditional absorption model, pre-conversion, primary conversion, and secondary conversion are connected to separate absorption circulation tanks, and the multi-stage absorption circulation tanks are interconnected to build a dynamic absorption system. By adjusting sulfuric acid between the circulation tanks, the imbalance in acid concentration between pre-absorption and primary absorption is resolved, ensuring the final output of qualified sulfuric acid products.

[0010] In summary, the technical solution adds pre-absorption + pre-conversion on the basis of two-turn and two-absorption to ensure that the catalyst is not burned and inactivated due to excessively high temperature. At the same time, the oxygen supply of the two-turn and two-absorption conversion section is supplemented to ensure that the oxygen-sulfur ratio is improved and a high sulfur dioxide conversion rate is achieved. A multi-stage absorption circulation tank is connected to a dynamic absorption acid method to dynamically adjust the pre-absorption and two absorptions of sulfuric acid of different concentrations and temperatures to ensure the output of qualified finished sulfuric acid. BRIEF DESCRIPTION OF THE DRAWINGS

[0011] Figure 1 It is a flow chart of the technical solution of the present invention. DETAILED DESCRIPTION

[0012] The present invention is further described below, but is not intended to limit the present invention in any way. Any changes or substitutions made based on the teachings of the present invention fall within the scope of protection of the present invention.

[0013] The method for producing acid from high-concentration copper smelting flue gas by dynamic classification according to the present invention comprises the following steps: Pre-conversion: 80-85% of the smelting flue gas after dust removal and drying is supplied to the pre-conversion section to maintain the temperature of the pre-conversion absorption catalyst layer at 560-580°C; Pre-absorption: The pre-converted flue gas is supplied to the pre-absorption tower. The absorption circulation tank 1 circulates concentrated sulfuric acid into the pre-absorption tower and contacts the flue gas in the tower. The concentrated sulfuric acid absorbs sulfur trioxide through gas-liquid contact. The absorption process reacts to form SO3+H2O=H2SO4. The absorbed concentrated sulfuric acid returns to the absorption circulation tank 1. The flue gas after pre-absorption is pressurized and mixed with the remaining 15-20% of the smelting flue gas after dust removal and drying to form the inlet flue gas of the two-conversion and two-absorption sections. Two-transformation and two-absorption: oxygen is pressurized and supplied to the two-transformation and two-absorption system. After oxygen supply, the sulfur dioxide concentration of the flue gas is 9.1-9.3%, the oxygen concentration is 9.1-9.2%, and the oxygen-sulfur ratio is 0.8-1. The flue gas undergoes primary conversion, primary absorption, secondary conversion, and secondary absorption in sequence. Absorption circulation tanks 2 and 3 circulate concentrated sulfuric acid to the primary absorption tower and the secondary absorption tower respectively, contacting the flue gas in the tower. The concentrated sulfuric acid absorbs sulfur trioxide through gas-liquid contact; The pre-absorption tower, primary absorption tower, and secondary absorption tower are connected to absorption circulation tanks 1, 2, and 3, respectively, and the three circulation tanks are interconnected, so that the three circulation tanks can be interconnected while the three systems can operate independently. The sulfuric acid concentration and temperature of each absorption circulation tank and absorption tower are dynamically adjusted, and finally the target sulfuric acid is produced in the absorption circulation tank 3 and the tail gas is discharged.

[0014] The smelting flue gas volume after dust removal and drying is 97500~98000Nm 3 / h, sulfur dioxide concentration is 13~19%, and temperature is 35~40℃.

[0015] The inlet flue gas temperature of the pre-conversion section is 390~400℃.

[0016] The height of the catalyst layer is 4.6~4.8cm, and the filling volume is 200~215m 3 .

[0017] The sulfur dioxide concentration of the flue gas after the pre-conversion is 6.4-6.8%, the sulfur trioxide concentration is 13-14%, and the oxygen concentration is 3.5-3.9%.

[0018] The conversion rate after the pre-conversion is 37-39%, and the total conversion rate is 68-70%.

[0019] The amount of flue gas after pre-absorption is reduced to 65-75% of the original amount of flue gas.

[0020] The inlet flue gas volume of the two-stage two-absorption section is 75000~76000Nm 3 / h, the sulfur dioxide concentration is 9~9.5%, the oxygen concentration is 5.5~6%, and the oxygen-sulfur ratio is 0.58~0.6.

[0021] The oxygen concentration is 90%.

[0022] The mixed flue gas volume after oxygen supply is 78000~79000Nm 3 / h.

[0023] After the dynamic adjustment, the sulfuric acid temperature of the pre-absorption tower is 66-68°C, the sulfuric acid temperature of the primary absorption tower is 68-72°C, and the sulfuric acid temperature of the secondary absorption tower is 65-70°C.

[0024] After the dynamic adjustment, the sulfuric acid concentration in the absorption circulation tank 1 is 98.2-98.6%, the sulfuric acid concentration in the absorption circulation tank 2 is 98.2-98.6%; the sulfuric acid concentration output by the absorption circulation tank 3 is 98.3-98.5%.

[0025] During the pre-absorption, primary absorption and secondary absorption, the concentrated sulfuric acid and the flue gas in the absorption tower are in countercurrent contact.

[0026] The method may further include a tail gas treatment step to desulfurize the tail gas to form tail gas emissions that meet standards.

[0027] Example 1

[0028] Pre-conversion: high-concentration smelting flue gas after dust removal and drying, with a flue gas volume of 97500Nm 3 / h, the sulfur dioxide concentration is 13%, the temperature is 37℃. 80% of it is supplied to the pre-conversion section, the temperature of the pre-conversion absorption catalyst layer is 560℃, the height of the catalyst layer is 4.6cm, and the filling volume is 200m 3The inlet flue gas temperature was 390°C. After pre-conversion, the flue gas sulfur dioxide concentration dropped to 6.4%, the sulfur trioxide concentration was 13%, and the oxygen concentration was 3.5%. The conversion rate after pre-conversion was 37%, and the total conversion rate was 68%.

[0029] Pre-absorption: The pre-converted flue gas is fed into the pre-absorption tower. Absorption circulation tank 1 circulates concentrated sulfuric acid into the pre-absorption tower, where it comes into countercurrent contact with the flue gas inside the tower. The concentrated sulfuric acid absorbs sulfur trioxide through gas-liquid contact and then returns to absorption circulation tank 1. The flue gas volume after absorption is reduced to 65% of the original volume. The sulfuric acid in absorption circulation tank 1 has a temperature of 100°C and a concentration of 99%. This absorption circulation tank is connected to absorption circulation tanks 2 and 3 to dynamically adjust the acid concentration and temperature.

[0030] The flue gas after pre-absorption is pressurized by the gas booster and mixed with the remaining 20% ​​of the smelting flue gas after dust removal and drying to form the inlet flue gas of the two-transfer and two-absorption section. The flue gas volume is 75000Nm 3 / h, the sulfur dioxide concentration is 9%, the oxygen concentration is 5.5%, and the oxygen-sulfur ratio is 0.58.

[0031] Two-turn two-suction: When the above-mentioned imported flue gas is supplied to the two-turn two-suction section, 3000m3 of 90% concentration oxygen is supplied through the oxygen pipeline. 3 After being pressurized by the oxygen compressor, it is supplied to the two-turn two-suction system. After oxygen supply, the mixed flue gas volume increases to 78000Nm 3 / h, the sulfur dioxide concentration of the flue gas is 9.1%, the oxygen concentration rises to 9.1%, the oxygen-sulfur ratio increases to 0.8, and the flue gas conversion rate stabilizes at 99.8%.

[0032] The flue gas undergoes primary conversion, primary absorption, secondary conversion, and secondary absorption in sequence. Absorption circulation tanks 2 and 3 circulate concentrated sulfuric acid to the primary and secondary absorption towers, respectively, where it comes into countercurrent contact with the flue gas within the towers. The concentrated sulfuric acid absorbs sulfur trioxide through gas-liquid contact. After two conversions and two absorptions, 97.5% concentrated sulfuric acid is formed in absorption circulation tanks 2 and 3. The inter-tank absorption loop between absorption circulation tanks 1 and 2 is activated, replenishing the 100°C, 99% concentrated sulfuric acid in absorption circulation tank 1 to absorption circulation tank 2. Alternatively, sulfuric acid from absorption circulation tank 2 is diverted back to absorption circulation tank 1.

[0033] Dynamically adjust the sulfuric acid concentration and temperature of each absorption circulation tank and absorption tower. Maintain the sulfuric acid temperature at the pre-absorption tower at 66°C, the primary absorption tower at 68°C, and the secondary absorption tower at 65°C. The sulfuric acid concentration in absorption circulation tank 1 is 98.2%, the sulfuric acid concentration in absorption circulation tank 2 is 98.2%, and the sulfuric acid output from absorption circulation tank 3 is 98.3%.

[0034] Finally, the target sulfuric acid is produced in the absorption circulation tank 3, while ensuring that the flue gas conversion rate stably reaches more than 99.8%. The exhausted exhaust gas is desulfurized to form qualified exhaust gas before being discharged.

[0035] Example 2

[0036] Pre-conversion: high-concentration smelting flue gas after dust removal and drying, with a flue gas volume of 97800Nm 3 / h, the sulfur dioxide concentration is 16%, the temperature is 37℃. 82% of it is supplied to the pre-conversion section, the temperature of the pre-conversion absorption catalyst layer is 570℃, the height of the catalyst layer is 4.7cm, and the filling volume is 210m 3 The inlet flue gas temperature was 395°C. After pre-conversion, the flue gas sulfur dioxide concentration dropped to 6.6%, the sulfur trioxide concentration was 13.5%, and the oxygen concentration was 3.7%. The conversion rate after pre-conversion was 38%, and the total conversion rate was 69%.

[0037] Pre-absorption: The pre-converted flue gas is fed into the pre-absorption tower. Absorption circulation tank 1 circulates concentrated sulfuric acid into the pre-absorption tower, where it comes into countercurrent contact with the flue gas inside the tower. The concentrated sulfuric acid absorbs sulfur trioxide through gas-liquid contact and then returns to absorption circulation tank 1. The flue gas volume after absorption is reduced to 70% of the original volume. The sulfuric acid in absorption circulation tank 1 has a temperature of 105°C and a concentration of 99.2%. This absorption circulation tank is connected to absorption circulation tanks 2 and 3 to dynamically adjust the acid concentration and temperature.

[0038] The flue gas after pre-absorption is pressurized by the gas booster and mixed with the remaining 18% of the smelting flue gas after dust removal and drying to form the inlet flue gas of the two-transfer and two-absorption section. The flue gas volume is 75500Nm 3 / h, the sulfur dioxide concentration is 9.3%, the oxygen concentration is 5.8%, and the oxygen-sulfur ratio is 0.59.

[0039] Two-turn two-suction: When the above-mentioned imported flue gas is supplied to the two-turn two-suction section, 3000m3 of 90% concentration oxygen is supplied through the oxygen pipeline. 3 After being pressurized by the oxygen compressor, it is supplied to the two-turn two-suction system. After oxygen supply, the mixed flue gas volume increases to 78500Nm 3 / h, the sulfur dioxide concentration of the flue gas is 9.2%, the oxygen concentration rises to 9.15%, the oxygen-sulfur ratio increases to 0.9, and the flue gas conversion rate stabilizes at 99.8%.

[0040] The flue gas undergoes primary conversion, primary absorption, secondary conversion, and secondary absorption in sequence. Absorption circulation tanks 2 and 3 circulate concentrated sulfuric acid to the primary and secondary absorption towers, respectively, where it comes into countercurrent contact with the flue gas within the towers. The concentrated sulfuric acid absorbs sulfur trioxide through gas-liquid contact. After two conversions and two absorptions, 97.8% concentrated sulfuric acid is formed in absorption circulation tanks 2 and 3. The inter-tank absorption loop between absorption circulation tanks 1 and 2 is activated, replenishing the highly concentrated sulfuric acid (99.2% acid concentration) in absorption circulation tank 1 with a temperature of 105°C in absorption circulation tank 1 to absorption circulation tank 2. Alternatively, sulfuric acid from absorption circulation tank 2 is diverted back to absorption circulation tank 1.

[0041] Dynamically adjust the sulfuric acid concentration and temperature of each absorption circulation tank and absorption tower. Maintain the sulfuric acid temperature at the pre-absorption tower at 67°C, the primary absorption tower at 70°C, and the secondary absorption tower at 66°C. The sulfuric acid concentration in absorption circulation tank 1 is 98.5%, and that in absorption circulation tank 2 is 98.3%. The sulfuric acid output from absorption circulation tank 3 is 98.4%.

[0042] Finally, the target sulfuric acid is produced in the absorption circulation tank 3, while ensuring that the flue gas conversion rate stably reaches more than 99.8%. The exhausted exhaust gas is desulfurized to form qualified exhaust gas before being discharged.

[0043] Example 3

[0044] Pre-conversion: high-concentration smelting flue gas after dust removal and drying, with a flue gas volume of 98,000 Nm 3 / h, the sulfur dioxide concentration is 19%, the temperature is 37℃. 85% of it is supplied to the pre-conversion section, the temperature of the pre-conversion absorption catalyst layer is 580℃, the height of the catalyst layer is 4.8cm, and the filling volume is 215m 3 The inlet flue gas temperature was 400°C. After pre-conversion, the flue gas sulfur dioxide concentration dropped to 6.8%, the sulfur trioxide concentration was 14%, and the oxygen concentration was 3.9%. The conversion rate after pre-conversion was 39%, and the total conversion rate was 70%.

[0045] Pre-absorption: The pre-converted flue gas is fed to the pre-absorption tower. Absorption circulation tank 1 circulates concentrated sulfuric acid into the pre-absorption tower, where it comes into countercurrent contact with the flue gas inside the tower. The concentrated sulfuric acid absorbs sulfur trioxide through gas-liquid contact and then returns to absorption circulation tank 1. The flue gas volume after absorption is reduced to 75% of the original flue gas volume. The sulfuric acid temperature in absorption circulation tank 1 is 110°C and the concentration is 99.5%. This absorption circulation tank is connected to absorption circulation tanks 2 and 3 to dynamically adjust the acid concentration and temperature.

[0046] The flue gas after pre-absorption is pressurized by the gas booster and mixed with the remaining 15% of the smelting flue gas after dust removal and drying to form the inlet flue gas of the two-transfer and two-absorption section. The flue gas volume is 76000Nm 3 / h, the sulfur dioxide concentration is 9.5%, the oxygen concentration is 6%, and the oxygen-sulfur ratio is 0.6.

[0047] Two-turn two-suction: When the above-mentioned imported flue gas is supplied to the two-turn two-suction section, 3000m3 of 90% concentration oxygen is supplied through the oxygen pipeline. 3 After being pressurized by the oxygen compressor, it is supplied to the two-turn two-suction system. After oxygen supply, the mixed flue gas volume increases to 79000Nm 3 / h, the sulfur dioxide concentration of the flue gas is 9.3%, the oxygen concentration rises to 9.2%, the oxygen-sulfur ratio increases to 1, and the flue gas conversion rate stably reaches 99.8%.

[0048] The flue gas undergoes primary conversion, primary absorption, secondary conversion, and secondary absorption in sequence. Absorption circulation tanks 2 and 3 circulate concentrated sulfuric acid to the primary and secondary absorption towers, respectively, where it comes into countercurrent contact with the flue gas within the towers. The concentrated sulfuric acid absorbs sulfur trioxide through gas-liquid contact. After two conversions and two absorptions, 97.5% concentrated sulfuric acid is formed in absorption circulation tanks 2 and 3. The inter-tank absorption loop between absorption circulation tanks 1 and 2 is activated, replenishing the 110°C, 99.5% concentrated sulfuric acid in absorption circulation tank 1 to absorption circulation tank 2. Alternatively, sulfuric acid from absorption circulation tank 2 is diverted back to absorption circulation tank 1.

[0049] Dynamically adjust the sulfuric acid concentration and temperature of each absorption circulation tank and absorption tower. Maintain the sulfuric acid temperature at the pre-absorption tower at 68°C, the primary absorption tower at 72°C, and the secondary absorption tower at 70°C. The sulfuric acid concentration in absorption circulation tank 1 is 98.6%, the sulfuric acid concentration in absorption circulation tank 2 is 98.6%, and the sulfuric acid output from absorption circulation tank 3 is 98.5%.

[0050] Finally, the target sulfuric acid is produced in the absorption circulation tank 3, while ensuring that the flue gas conversion rate stably reaches more than 99.8%. The exhausted exhaust gas is desulfurized to form qualified exhaust gas before being discharged.

Claims

1. A method for producing acid from high-concentration copper smelting flue gas by dynamic classification, characterized in that: The steps include: Pre-conversion: 80-85% of the smelting flue gas after dust removal and drying is supplied to the pre-conversion section to maintain the temperature of the pre-conversion absorption catalyst layer at 560-580°C; Pre-absorption: The pre-converted flue gas is supplied to the pre-absorption tower. The absorption circulation tank 1 circulates concentrated sulfuric acid into the pre-absorption tower, where it contacts the flue gas in the tower. The concentrated sulfuric acid absorbs sulfur trioxide through gas-liquid contact. The absorbed concentrated sulfuric acid returns to the absorption circulation tank 1. The pre-absorbed flue gas is pressurized and mixed with the remaining 15-20% of the smelting flue gas after dust removal and drying to form the inlet flue gas of the two-conversion and two-absorption sections. Two-transformation and two-absorption: oxygen is pressurized and supplied to the two-transformation and two-absorption system. After oxygen supply, the sulfur dioxide concentration of the flue gas is 9.1-9.3%, the oxygen concentration is 9.1-9.2%, and the oxygen-sulfur ratio is 0.8-1. The flue gas undergoes primary conversion, primary absorption, secondary conversion, and secondary absorption in sequence. Absorption circulation tanks 2 and 3 circulate concentrated sulfuric acid to the primary absorption tower and the secondary absorption tower respectively, contacting the flue gas in the tower. The concentrated sulfuric acid absorbs sulfur trioxide through gas-liquid contact; The pre-absorption tower, primary absorption tower, and secondary absorption tower are connected to absorption circulation tanks 1, 2, and 3, respectively, and the three circulation tanks are interconnected, so that the three circulation tanks can be interconnected while the three systems can operate independently. The sulfuric acid concentration and temperature of each absorption circulation tank and absorption tower are dynamically adjusted, and finally the target sulfuric acid is produced in the absorption circulation tank 3 and the tail gas is discharged.

2. The method for producing acid from high-concentration copper smelting flue gas by dynamic classification according to claim 1, characterized in that: The smelting flue gas volume after dust removal and drying is 97500~98000Nm 3 / h, sulfur dioxide concentration is 13~19%, and temperature is 35~40℃.

3. The method for producing acid from high-concentration copper smelting flue gas by dynamic classification according to claim 1, characterized in that: The inlet flue gas temperature of the pre-conversion section is 390~400℃.

4. The method for producing acid from high-concentration copper smelting flue gas by dynamic classification according to claim 1, characterized in that: The height of the catalyst layer is 4.6~4.8cm, and the filling volume is 200~215m 3 .

5. The method for producing acid from high-concentration copper smelting flue gas by dynamic classification according to claim 1, characterized in that: The sulfur dioxide concentration of the flue gas after the pre-conversion is 6.4-6.8%, the sulfur trioxide concentration is 13-14%, and the oxygen concentration is 3.5-3.9%.

6. The method for producing acid from high-concentration copper smelting flue gas by dynamic classification according to claim 1, characterized in that: The conversion rate after the pre-conversion is 37-39%.

7. The method for producing acid from high-concentration copper smelting flue gas by dynamic classification according to claim 1, characterized in that: The inlet flue gas volume of the two-stage two-absorption section is 75000~76000Nm 3 / h, the sulfur dioxide concentration is 9~9.5%, the oxygen concentration is 5.5~6%, and the oxygen-sulfur ratio is 0.58~0.

6.

8. The method for producing acid from high-concentration copper smelting flue gas by dynamic classification according to claim 1, characterized in that: The mixed flue gas volume after oxygen supply is 78000~79000Nm 3 / h.

9. The method for producing acid from high-concentration copper smelting flue gas by dynamic classification according to claim 1, characterized in that: After the dynamic adjustment, the sulfuric acid temperature of the pre-absorption tower is 66-68°C, the sulfuric acid temperature of the primary absorption tower is 68-72°C, and the sulfuric acid temperature of the secondary absorption tower is 65-70°C.

10. The method for producing acid from high-concentration copper smelting flue gas by dynamic classification according to claim 1, characterized in that: After the dynamic adjustment, the sulfuric acid concentration in the absorption circulation tank 1 is 98.2-98.6%, the sulfuric acid concentration in the absorption circulation tank 2 is 98.2-98.6%; the sulfuric acid concentration output by the absorption circulation tank 3 is 98.3-98.5%.

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