A device for recovering mercury in a copper smelting system

Abstract

This utility model discloses a mercury recovery device in a copper smelting system, comprising a smelting furnace, a smelting waste heat boiler, an adiabatic evaporation tower, a smelting electrostatic precipitator, a spray cooling tower, a bag filter, a smelting high-pressure blower, a high-efficiency scrubber, an inclined plate settling tank, a box filter press, a supernatant storage tank, a high-level water tank, a degassing tower, a waste acid storage tank, an acid sludge packaging station, an acid sludge roasting furnace, a condenser, a mercury receiving container, and a mercury collection tank. Mercury is washed down from the flue gas and fed into the acid sludge. By controlling certain process parameters, such as the roasting furnace temperature and the condenser inlet temperature, the mercury vapor from the roasted acid sludge is condensed and precipitated, with a purity of up to 99.9%. The beneficial effects of this utility model are: it recovers mercury from copper smelting flue gas with a recovery rate of 80%~85%, ensuring that the flue gas meets emission standards, avoiding resource waste, and improving economic efficiency.

Description

Technical Field

[0001] This utility model belongs to the field of non-ferrous metal smelting technology, specifically relating to a mercury recovery device in a copper smelting system. Background Technology

[0002] In copper smelting processes, mercury is concentrated in large quantities in smelting flue gas. This mercury enters the purification section along with the flue gas and adheres to the purified acid sludge, with a content of 5% to 10%. Relevant regulations also have requirements on the emission concentration of mercury and its compounds as pollutants, making mercury recovery difficult. Utility Model Content

[0003] This invention addresses the issue of mercury content in copper smelting flue gas by providing a device for recovering mercury from copper smelting systems.

[0004] To achieve the above objectives, the present invention adopts the following technical solution: A mercury recovery device in a copper smelting system includes a smelting furnace, a smelting waste heat boiler, an adiabatic evaporation tower, a smelting electrostatic precipitator, a spray cooling tower, a bag filter, a smelting high-pressure blower, a high-efficiency scrubber, an inclined plate settling tank, a box filter press, a supernatant storage tank, a high-level water tank, a degassing tower, a waste acid storage tank, an acid sludge packaging station, an acid sludge roasting furnace, a condenser, a mercury receiving container for the condenser, and a mercury collection tank. The smelting furnace, smelting waste heat boiler, adiabatic evaporation tower, smelting electrostatic precipitator, spray cooling tower, bag filter, smelting high-pressure blower, high-efficiency scrubber, and inclined plate settling tank pass through sequentially... The inclined plate settling tank is equipped with an overflow port and a bottom outlet. The overflow port is connected to the supernatant storage tank via a pipe, and the bottom outlet is connected to the chamber filter press via a pipe. The chamber filter press is equipped with a liquid outlet and a solid outlet. The liquid outlet is connected to the supernatant storage tank, and the solid outlet is connected to the acid sludge packaging station. The acid sludge packaging station, acid sludge roasting furnace, condenser, mercury receiving container, and mercury collection tank are connected in sequence via pipes. The bottom outlet of the supernatant storage tank has two branches. One branch is connected to the high-level water tank, and the other branch is connected to the degassing tower. The degassing tower is connected to the waste acid storage tank via a pipe.

[0005] Furthermore, the high-efficiency scrubber includes a primary high-efficiency scrubber and a secondary high-efficiency scrubber connected in series. A gas cooling tower is provided between the primary and secondary high-efficiency scrubbers. The elevated water tank has a bottom outlet and an overflow outlet. The bottom outlet of the elevated water tank is connected to the inlet pipe of the primary high-efficiency scrubber, and the overflow outlet of the elevated water tank is connected to the tower body of the primary high-efficiency scrubber. The primary high-efficiency scrubber has a flue gas outlet and a scrubbing liquid outlet. The flue gas outlet of the primary high-efficiency scrubber is connected to the gas cooling tower through a pipe. The scrubbing liquid outlet of the primary high-efficiency scrubber is connected to the inlet pipe of the primary high-efficiency scrubber through a scrubbing liquid circulation pipe. A scrubbing liquid outlet pipe is branched on the liquid circulation pipe of the primary high-efficiency scrubber and is connected to the inclined plate settling tank. The gas cooling tower has a flue gas outlet and a scrubbing liquid outlet. The flue gas outlet of the gas cooling tower is connected to the secondary high-efficiency scrubber. The scrubbing liquid outlet of the gas cooling tower is connected to the plate heat exchanger through a scrubbing liquid circulation pipe. The scrubbing liquid outlet of the plate heat exchanger is connected to the main spray pipe of the gas cooling tower through a pipe.

[0006] Furthermore, the washing liquid circulation pipeline of the first-stage high-efficiency scrubber is equipped with a first-stage dynamic wave circulation pump, the washing liquid circulation pipeline of the gas cooling tower is equipped with a gas cooling tower circulation pump, the second-stage high-efficiency scrubber is equipped with a flue gas outlet and a washing liquid outlet, the washing liquid outlet of the second-stage high-efficiency scrubber is connected to the inlet pipeline of the second-stage high-efficiency scrubber through the washing liquid circulation pipeline, and the washing liquid circulation pipeline of the second-stage high-efficiency scrubber is equipped with a second-stage dynamic wave circulation pump.

[0007] Furthermore, the condenser consists of a primary condenser and a secondary condenser arranged in series. The primary condenser and the secondary condenser are respectively connected to mercury collection containers via pipes. The mercury collection containers are connected to mercury collection tanks via pipes. The flue gas outlet of the primary condenser is connected to the secondary condenser via a pipe. The secondary condenser is provided with a flue gas outlet.

[0008] Furthermore, a branch is provided on the connecting pipe between the smelting electrostatic precipitator and the spray cooling tower, and the other end of the branch is connected in parallel to the connecting pipe between the bag filter and the smelting high-pressure blower.

[0009] Furthermore, a circulation pump is installed on the main pipeline of the supernatant storage tank, and the supernatant storage tank is equipped with an overflow port, which is connected to the tower body of the first-stage high-efficiency scrubber through a pipeline; the gas cooling tower and the second-stage high-efficiency scrubber are each equipped with an overflow port, the overflow port of the second-stage high-efficiency scrubber is connected to the gas cooling tower through a pipeline, and the overflow port of the gas cooling tower is connected to the first-stage high-efficiency scrubber through a pipeline.

[0010] Furthermore, a filter press pump is installed on the connecting pipe between the inclined plate settling tank and the chamber filter press, and an external discharge pipe is installed on the waste acid storage tank, with an external discharge pump installed on the external discharge pipe.

[0011] Furthermore, the flue gas outlet of the secondary condenser is connected to the flue gas inlet of the primary high-efficiency scrubber via a pipeline, and the slag outlet of the acid sludge roasting furnace is connected to the smelting furnace via a pipeline.

[0012] The method for recovering mercury from a copper smelting system using the aforementioned apparatus is as follows: (1) The high-temperature flue gas generated during normal production of the smelting furnace with a furnace temperature of 1100~1300℃ is cooled to 380℃~420℃ by the smelting waste heat boiler and then enters the smelting electrostatic precipitator. The flue gas temperature entering the smelting electrostatic precipitator is controlled between 270℃~330℃ by the insulated evaporation tower. The inlet and outlet temperature difference of the smelting electrostatic precipitator is controlled between 20℃~40℃ and the resistance of the smelting electrostatic precipitator is less than 300Pa. The flue gas after dust removal by the smelting electrostatic precipitator enters the spray cooling tower for further dust removal and cooling to 150℃~170℃, so that the arsenic trioxide in the flue gas is converted from gaseous to solid particles. Then the flue gas enters the bag dust collector and the pressure drop of the bag dust collector is controlled between 1kPa~1.5kPa to recover and filter the arsenic trioxide particles in the flue gas. The flue gas after dust removal and cooling enters the purification section through the smelting high-temperature fan. (2) The flue gas from the high-temperature blower of the smelting enters the first-stage high-efficiency scrubber in the purification section. The dust, arsenic, fluorine and mercury in the flue gas are washed into the circulating liquid. The flue gas pipeline and flue gas are cooled by the circulating liquid and the overflow liquid of the high-level water tank, so that the flue gas temperature at the outlet of the first-stage high-efficiency scrubber is controlled at ≤78℃. The flue gas exiting the first-stage high-efficiency scrubber enters the gas cooling tower and comes into countercurrent contact with the circulating liquid of the gas cooling tower after being cooled by the plate heat exchanger, so that the flue gas is further dusted and cooled, and the flue gas temperature at the outlet of the gas cooling tower is controlled at <45℃. The cooled flue gas enters the second-stage high-efficiency scrubber for further purification and is sent to the subsequent process. (3) The circulating liquid of the first-stage high-efficiency scrubber enters the inclined plate settling tank through the washing liquid outlet pipe via the first-stage power wave circulation pump. It overflows from the inclined plate settling tank into the supernatant storage tank, and is then sent to the high-level water tank by the first-stage power wave circulation pump. The bottom flow of the high-level water tank enters the flue gas pipe of the first-stage high-efficiency scrubber. The excess circulating liquid is sent to the waste acid storage tank after sulfur dioxide is removed by the degassing tower. It is discharged from the system by the waste acid discharge pump. The circulating liquid is controlled to contain fluorine ≤1000mg / L, arsenic ≤8000mg / L, chlorine ≤1000mg / L, and acid concentration in the first-stage circulating liquid <10wt%; (4) During operation, start the filter press pump for half an hour every hour. When the pressure of the box filter press is ≥0.65MPa, disassemble the box filter press to allow the mercury-containing acid sludge to be pressed out through the box filter press and sent to the acid sludge packaging station. (5) Mercury-containing acid sludge from the acid sludge packaging station is sent to the acid sludge roasting furnace for roasting at a temperature of 850~950℃. After roasting, the mercury vapor enters the first-stage condenser through the flue gas pipe, so that the inlet temperature of the first-stage condenser is controlled at 190~210℃. The mercury vapor entering the first-stage condenser is further cooled by the cooling liquid, and a portion of the mercury is released and enters the mercury receiving container of the first-stage condenser. The mercury vapor coming out of the first-stage condenser enters the second-stage condenser for further mercury release and enters the mercury receiving container of the second-stage condenser. The flue gas pipe of the second-stage condenser is connected to the flue gas pipe of the first-stage high-efficiency scrubber for recycling. The released mercury is sent to the mercury collection tank for storage by the mercury receiving container. The slag of the acid sludge roasting furnace is returned to the smelting furnace.

[0013] Furthermore, the liquid level of the first-stage high-efficiency washer is controlled at 2m~2.2m, so that the high-level water tank and the supernatant tank overflow to the first-stage high-efficiency washer.

[0014] The apparatus described in this application washes mercury down from the flue gas and introduces it into acid sludge. By controlling certain process parameters, such as the roasting furnace temperature and the condenser inlet temperature, the mercury vapor from the roasted acid sludge is condensed and precipitated, with the precipitated mercury reaching a purity of 99.9%. The beneficial effects of this invention are: it recovers mercury from copper smelting flue gas with a recovery rate of 80% to 85%, ensuring that the flue gas meets emission standards, avoiding resource waste, and improving economic efficiency. Attached Figure Description

[0015] Figure 1 This is a schematic diagram of the structure of this utility model; The accompanying drawings are for illustrative purposes only and should not be construed as limiting the scope of this patent. To better illustrate this embodiment, some parts in the drawings may be omitted, enlarged, or reduced, and do not represent the actual dimensions of the product. Detailed Implementation

[0016] The present invention will now be further described with reference to the accompanying drawings.

[0017] Example 1: A device for recovering mercury in a copper smelting system, such as... Figure 1As shown, it includes a smelting furnace (1-1), a smelting waste heat boiler (1-2), an adiabatic evaporation tower (1-7), a smelting electrostatic precipitator (1-3), a spray cooling tower (1-4), a bag filter (1-5), a smelting high-temperature fan (1-6), a primary high-efficiency scrubber (2-1), an inclined plate settling tank (2-3), a chamber filter press (2-5), a supernatant storage tank (2-6), an elevated water tank (2-8), a degassing tower (2-9), a waste acid storage tank (2-10), a gas cooling tower (2-12), a plate heat exchanger (2-14), a secondary high-efficiency scrubber (2-15), an acid sludge packaging station (3-1), an acid sludge roasting furnace (3-2), a primary condenser (3-3), a primary condenser mercury receiving container (3-4), a secondary condenser (3-5), a secondary condenser mercury receiving container (3-6), and a mercury collection tank (3-7).

[0018] The smelting furnace (1-1) and the smelting waste heat boiler (1-2) are connected via a direct-flow flue. The smelting waste heat boiler (1-2) and the smelting electrostatic precipitator (1-3) are connected via a flue. An adiabatic evaporation tower (1-7) is installed on the flue. The smelting electrostatic precipitator (1-4) and the spray cooling tower (1-4) are connected via a flue. The spray cooling tower (1-4) and the bag filter (1-5) are connected via a flue. The bag filter (1-5) and the smelting high-temperature blower (1-6) are connected via a flue. A branch is provided on the connecting pipe between the smelting electrostatic precipitator (1-3) and the spray cooling tower (1-4). The other end of this branch is connected in parallel to the connecting pipe between the bag filter (1-5) and the smelting high-pressure blower (1-6).

[0019] The high-pressure blower (1-6) for smelting is connected to the inlet pipe of the primary high-efficiency scrubber (2-1) via a pipeline. The primary high-efficiency scrubber (2-1), the gas cooling tower (2-12), and the secondary high-efficiency scrubber (2-15) are connected in series via a flue gas pipeline. The high-level water tank (2-8) has a bottom outlet and an overflow outlet. The bottom outlet of the high-level water tank (2-8) is connected to the inlet pipe of the primary high-efficiency scrubber (2-1), and the overflow outlet of the high-level water tank (2-8) is connected to the tower body of the primary high-efficiency scrubber (2-1). The primary high-efficiency scrubber (2-1) has a flue gas outlet and a scrubbing liquid outlet. The flue gas outlet of the primary high-efficiency scrubber (2-1) is connected to the gas cooling tower (2-12) via a pipeline. The scrubbing liquid outlet of the primary high-efficiency scrubber (2-1) is connected to the inlet pipe of the primary high-efficiency scrubber (2-1) via a scrubbing liquid circulation pipeline and a primary power wave circulation pump (2-2) installed on the pipeline. A branch of the liquid circulation pipe of the first-stage high-efficiency scrubber (2-1) is provided with a scrubbing liquid outlet pipe, which is connected to the inclined plate settling tank (2-3). The gas cooling tower (2-12) is provided with a flue gas outlet and a scrubbing liquid outlet. The flue gas outlet of the gas cooling tower (2-12) is connected to the second-stage high-efficiency scrubber (2-15). The scrubbing liquid outlet of the gas cooling tower (2-12) is connected to the plate heat exchanger (2-14) through the scrubbing liquid circulation pipe and the gas cooling tower circulation pump (2-13) installed on the pipe. The scrubbing liquid outlet of the plate heat exchanger (2-14) is connected to the main spray pipe of the gas cooling tower (2-12) through a pipe. The plate heat exchanger (2-14) is connected to the coolant pipe. The secondary high-efficiency scrubber (2-15) is equipped with a flue gas outlet and a scrubbing liquid outlet. The scrubbing liquid outlet of the secondary high-efficiency scrubber (2-15) is connected to the inlet pipe of the secondary high-efficiency scrubber (2-15) through a scrubbing liquid circulation pipe. A secondary power wave circulation pump (2-16) is installed on the scrubbing liquid circulation pipe of the secondary high-efficiency scrubber (2-15).

[0020] The inclined plate settling tank (2-3) is equipped with an overflow port and a bottom flow port. The overflow port is connected to the supernatant storage tank (2-6) via a pipe. The bottom flow port is connected to the chamber filter press (2-5) via a pipe and a filter pump (2-4) mounted on the pipe. The chamber filter press (2-5) is equipped with a liquid outlet and a solid outlet. The liquid outlet is connected to the supernatant storage tank (2-6), and the solid outlet is connected to the acid sludge packaging station (3-1). The acid sludge packaging station (3-1) and the acid sludge roasting furnace (3-2) are connected via a pipe. The supernatant storage tank (2-6) is equipped with an overflow port and a bottom flow port. The overflow port of the supernatant storage tank (2-6) is connected to the tower body of the first-stage high-efficiency scrubber (2-1) through a pipeline. The bottom outlet (2-6) of the supernatant storage tank (2-6) is equipped with a main pipeline. A circulation pump (2-7) is installed on the main pipeline. Two branches are provided at the end of the main pipeline. One branch is connected to the high-level water tank (2-8), and the other branch is connected to the degassing tower (2-9). The degassing tower (2-9) is connected to the waste acid storage tank (2-10) through a pipeline. The waste acid storage tank (2-10) is equipped with an external discharge pipeline, and an external discharge pump (2-11) is installed on the external discharge pipeline.

[0021] The flue gas outlet of the acid mud roasting furnace (3-2) is connected to the primary condenser (3-3) via a flue gas pipe. The mercury inlet container (3-4) of the primary condenser is connected below the primary condenser (3-3) via a pipe. The secondary condenser (3-5) is connected in series with the primary condenser via a flue gas pipe. The mercury inlet container (3-6) of the secondary condenser is connected below the secondary condenser (3-5) via a pipe. The mercury inlet containers (3-4) and (3-6) of the primary and secondary condensers are connected to the mercury collection tank (3-7) via pipes. The primary condenser (3-3) and the secondary condenser (3-5) are respectively connected to the coolant inlet pipe (3-9) and the coolant outlet pipe (3-10). The coolant is circulating cooling water. The secondary condenser is equipped with a flue gas outlet pipe (3-8).

[0022] In this embodiment, the gas cooling tower (2-12) and the secondary high-efficiency scrubber (2-15) are each equipped with an overflow port. The overflow port of the secondary high-efficiency scrubber (2-15) is connected to the gas cooling tower (2-12) via a pipe, and the overflow port of the gas cooling tower (2-12) is connected to the primary high-efficiency scrubber (2-1) via a pipe. The flue gas outlet pipe (3-8) of the secondary condenser (3-5) is connected to the flue gas inlet of the primary high-efficiency scrubber (2-1), and the slag outlet of the acid mud roasting furnace (3-2) is connected to the smelting furnace (1-1) via a pipe.

[0023] The method for recovering mercury using the above-mentioned device is as follows: (1) The high-temperature flue gas generated during normal production of the smelting furnace (1-1) with the furnace temperature controlled at 1200℃ is cooled to 380℃~420℃ by the smelting waste heat boiler (1-2) and then enters the smelting electrostatic precipitator (1-3). The temperature of the flue gas entering the smelting electrostatic precipitator (1-3) is controlled between 270℃~330℃ by the adiabatic evaporation tower (1-7). The temperature difference between the inlet and outlet of the smelting electrostatic precipitator (1-3) is controlled between 20℃~40℃ and the resistance of the smelting electrostatic precipitator (1-3) is less than 300pa. The flue gas after dust removal by the smelting electrostatic precipitator (1-3) enters the spray cooling tower (1-4) for further dust removal and cooling to 150℃~170℃, so that the arsenic trioxide in the flue gas is converted from gaseous to solid particles. Then the flue gas enters the bag filter (1-5) and the pressure drop of the bag filter is controlled between 1kPa~1.5kPa to recover and filter the arsenic trioxide particles in the flue gas. After dust removal and cooling, the flue gas enters the purification section through the high-temperature smelting fan (1-6).

[0024] (2) The flue gas from the high-temperature blower (1-6) of the smelting enters the first-stage high-efficiency scrubber (2-1) of the purification section. The dust, arsenic, fluorine, mercury and other impurities in the flue gas are washed into the circulating liquid, and the mercury element in the flue gas is deeply purified. The flue gas pipeline and flue gas are cooled by the circulating liquid and the high-level water tank (2-8), so that the flue gas temperature at the outlet of the first-stage high-efficiency scrubber (2-1) is controlled at ≤78℃. The flue gas exiting the first-stage high-efficiency scrubber (2-1) enters the gas cooling tower (2-12) and comes into countercurrent contact with the circulating liquid of the gas cooling tower after being cooled by the plate heat exchanger (2-14), so that the flue gas is further dusted and cooled, and the flue gas temperature at the outlet of the gas cooling tower (2-12) is controlled at <45℃. The cooled flue gas enters the second-stage high-efficiency scrubber (2-15) for further purification and is then sent to the subsequent electrostatic precipitator and dry suction process.

[0025] (3) The circulating liquid of the first-stage high-efficiency scrubber (2-1) enters the inclined plate settling tank (2-3) through the first-stage power wave circulating pump (2-2) via a bypass. It overflows from the inclined plate settling tank (2-3) into the supernatant storage tank (2-6), and then is sent to the high-level water tank (2-8) through the circulating pump (2-7). The high-level water tank (2-8) enters the flue gas pipeline of the first-stage high-efficiency scrubber (2-1) through the bottom flow to cool the flue gas and flue gas pipeline. The excess circulating liquid is sent to the waste acid storage tank (2-10) after removing sulfur dioxide through the degassing tower (2-9). It is discharged from the system by the waste acid discharge pump (2-11). The circulating liquid is tested every day to control the fluorine content in the circulating liquid to ≤1000mg / L, the arsenic content to ≤8000mg / L, the chlorine content to ≤1000mg / L, and the acid concentration in the first-stage circulating liquid to <10wt%. If the index is exceeded, add agents such as sodium silicate or increase the waste acid discharge.

[0026] (4) During operation, the liquid levels of the high-level water tank (2-8), the first-stage high-efficiency scrubber (2-1), and the supernatant storage tank (2-6) should be kept in balance. Generally, the liquid in the high-level water tank (2-8) and the supernatant storage tank (2-6) should be slowly overflowed into the first-stage high-efficiency scrubber (2-1), and the liquid level in the first-stage high-efficiency scrubber (2-1) should be controlled at 2m~2.2m.

[0027] (5) During operation, start the filter press pump (2-4) for half an hour every hour. When the pressure of the box filter press (2-5) is ≥0.65MPa, disassemble the box filter press (2-5) to allow the mercury-containing acid sludge to be pressed out through the box filter press (2-5) and sent to the acid sludge packaging station (3-1).

[0028] (6) Mercury-containing acid sludge from the acid sludge packaging station (3-1) is sent to the acid sludge roasting furnace (3-2) for roasting. The roasting temperature is around 900℃ to maximize the mercury recovery rate. The mercury vapor after roasting enters the primary condenser (3-3) through the flue gas pipeline. The flue gas inlet temperature of the primary condenser (3-3) is controlled by the waste heat boiler (not shown in the figure) between the acid sludge roasting furnace (3-2) and the primary condenser (3-3), so that the inlet temperature is controlled at around 200℃. At this temperature, the condensation efficiency of the mercury vapor entering the primary condenser (3-3) is the highest. The mercury vapor entering the primary condenser (3-3) is further cooled and precipitated by the cooling liquid. A portion of the mercury enters the mercury receiving container (3-4) of the primary condenser. The mercury vapor from the primary condenser (3-3) enters the secondary condenser (3-5) for further mercury precipitation, which then enters the mercury receiving container (3-6) of the secondary condenser. After passing through the secondary condenser (3-5), the mercury recovery rate can reach over 80%, and the purity of the precipitated mercury can reach 99.9%. The condensed flue gas is connected to the primary high-efficiency scrubber (2-1) through the flue gas duct (3-8) for recycling. The precipitated mercury is sent from the mercury receiving container to the mercury collection tank (3-7) for storage. The slag from the acid mud roasting furnace (3-2) is returned to the smelting furnace (1-1).

[0029] Finally, it should be noted that the above embodiments are only used to illustrate the technical solutions of the specific implementation of this utility model and not to limit it. Those skilled in the art should understand that any equivalent substitutions or obvious modifications made to the implementation of this utility model without changing its performance or use, without violating the spirit of this utility model, should be covered within the scope of protection claimed by this utility model.

Claims

1. A device for recovering mercury in a copper smelting system, characterized by, The system includes a smelting furnace, a smelting waste heat boiler, an insulated evaporation tower, a smelting electrostatic precipitator, a spray cooling tower, a bag filter, a smelting high-pressure blower, a high-efficiency scrubber, an inclined plate settling tank, a box filter press, a supernatant storage tank, a high-level water tank, a degassing tower, a waste acid storage tank, an acid sludge packaging station, an acid sludge roasting furnace, a condenser, a condenser mercury receiving container, and a mercury collection tank. The smelting furnace, smelting waste heat boiler, insulated evaporation tower, smelting electrostatic precipitator, spray cooling tower, bag filter, smelting high-pressure blower, high-efficiency scrubber, and inclined plate settling tank are connected sequentially by pipelines. The settling tank is equipped with an overflow port and a bottom outlet. The overflow port is connected to the supernatant storage tank via a pipe, and the bottom outlet is connected to the chamber filter press via a pipe. The chamber filter press is equipped with a liquid outlet and a solid outlet. The liquid outlet is connected to the supernatant storage tank, and the solid outlet is connected to the acid sludge packaging station. The acid sludge packaging station, acid sludge roasting furnace, condenser, mercury receiving container, and mercury collection tank are connected in sequence via pipes. The bottom outlet of the supernatant storage tank has two branches. One branch is connected to the high-level water tank, and the other branch is connected to the degassing tower. The degassing tower is connected to the waste acid storage tank via a pipe.

2. The apparatus for recovering mercury from a copper smelting system according to claim 1, wherein The high-efficiency scrubber includes a primary high-efficiency scrubber and a secondary high-efficiency scrubber connected in series. A gas cooling tower is provided between the primary and secondary high-efficiency scrubbers. A high-level water tank has a bottom outlet and an overflow outlet. The bottom outlet of the high-level water tank is connected to the inlet pipe of the primary high-efficiency scrubber, and the overflow outlet of the high-level water tank is connected to the tower body of the primary high-efficiency scrubber. The primary high-efficiency scrubber has a flue gas outlet and a scrubbing liquid outlet. The flue gas outlet of the primary high-efficiency scrubber is connected to the gas cooling tower through a pipe. The scrubbing liquid outlet of the primary high-efficiency scrubber is connected to the inlet pipe of the primary high-efficiency scrubber through a scrubbing liquid circulation pipe. A branch of the liquid circulation pipe of the primary high-efficiency scrubber has a scrubbing liquid outlet pipe, which is connected to an inclined plate settling tank. The gas cooling tower has a flue gas outlet and a scrubbing liquid outlet. The flue gas outlet of the gas cooling tower is connected to the secondary high-efficiency scrubber. The scrubbing liquid outlet of the gas cooling tower is connected to a plate heat exchanger through a scrubbing liquid circulation pipe. The scrubbing liquid outlet of the plate heat exchanger is connected to the main spray pipe of the gas cooling tower through a pipe.

3. The mercury recovery device in the copper smelting system according to claim 2, characterized in that, The first-stage high-efficiency scrubber is equipped with a first-stage dynamic wave circulation pump on its washing liquid circulation pipeline, and a gas cooling tower circulation pump is equipped with a gas cooling tower circulation pipeline on its washing liquid circulation pipeline. The second-stage high-efficiency scrubber is equipped with a flue gas outlet and a washing liquid outlet. The washing liquid outlet of the second-stage high-efficiency scrubber is connected to the inlet pipeline of the second-stage high-efficiency scrubber through a washing liquid circulation pipeline, and a second-stage dynamic wave circulation pump is equipped with a washing liquid circulation pipeline of the second-stage high-efficiency scrubber.

4. The mercury recovery device in the copper smelting system according to claim 1, characterized in that, The condenser consists of a primary condenser and a secondary condenser connected in series. The primary condenser and the secondary condenser are respectively connected to mercury collection containers via pipes. The mercury collection containers of the primary condenser and the secondary condenser are respectively connected to mercury collection tanks via pipes. The flue gas outlet of the primary condenser is connected to the secondary condenser via a pipe. The secondary condenser is provided with a flue gas outlet.

5. The mercury recovery device in the copper smelting system according to claim 1, characterized in that, A branch line is provided on the connecting pipe between the smelting electrostatic precipitator and the spray cooling tower. The other end of the branch line is connected in parallel to the connecting pipe between the bag filter and the smelting high-pressure blower.

6. The mercury recovery device in the copper smelting system according to claim 2, characterized in that, A circulation pump is installed on the main pipeline at the bottom outlet of the supernatant storage tank. The supernatant storage tank is equipped with an overflow port, which is connected to the tower body of the primary high-efficiency scrubber through a pipeline. The gas cooling tower and the secondary high-efficiency scrubber are each equipped with an overflow port. The overflow port of the secondary high-efficiency scrubber is connected to the gas cooling tower through a pipeline, and the overflow port of the gas cooling tower is connected to the primary high-efficiency scrubber through a pipeline.

7. The mercury recovery device in the copper smelting system according to claim 1, characterized in that, A filter press pump is installed on the connecting pipe between the inclined plate settling tank and the chamber filter press, and an external discharge pipe is installed on the waste acid storage tank, with an external discharge pump installed on the external discharge pipe.

8. The mercury recovery device in the copper smelting system according to claim 4, characterized in that, The flue gas outlet of the secondary condenser is connected to the flue gas inlet of the primary high-efficiency scrubber via a pipeline, and the slag outlet of the acid mud roasting furnace is connected to the smelting furnace via a pipeline.

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