CN107537285B - Multi-level recycling system and method for acid-making wastewater from smelting flue gas - Google Patents
Multi-level recycling system and method for acid-making wastewater from smelting flue gas Download PDFInfo
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- CN107537285B CN107537285B CN201710744985.2A CN201710744985A CN107537285B CN 107537285 B CN107537285 B CN 107537285B CN 201710744985 A CN201710744985 A CN 201710744985A CN 107537285 B CN107537285 B CN 107537285B
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- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 65
- 239000003546 flue gas Substances 0.000 title claims abstract description 65
- 239000002351 wastewater Substances 0.000 title claims abstract description 56
- 238000004064 recycling Methods 0.000 title claims abstract description 38
- 238000003723 Smelting Methods 0.000 title claims abstract description 26
- 238000000034 method Methods 0.000 title claims abstract description 19
- 239000002253 acid Substances 0.000 claims abstract description 69
- 238000001816 cooling Methods 0.000 claims abstract description 40
- 230000002378 acidificating effect Effects 0.000 claims abstract description 21
- 238000001914 filtration Methods 0.000 claims abstract description 21
- KRHYYFGTRYWZRS-UHFFFAOYSA-N Fluorane Chemical compound F KRHYYFGTRYWZRS-UHFFFAOYSA-N 0.000 claims abstract description 19
- 239000007789 gas Substances 0.000 claims abstract description 19
- 229910000040 hydrogen fluoride Inorganic materials 0.000 claims abstract description 19
- 238000004519 manufacturing process Methods 0.000 claims abstract description 13
- 238000001035 drying Methods 0.000 claims abstract description 10
- 238000000889 atomisation Methods 0.000 claims abstract description 4
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- 230000005494 condensation Effects 0.000 claims abstract description 4
- 239000007788 liquid Substances 0.000 claims description 73
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 60
- 239000007921 spray Substances 0.000 claims description 52
- 239000000725 suspension Substances 0.000 claims description 40
- 239000002893 slag Substances 0.000 claims description 24
- 238000000746 purification Methods 0.000 claims description 11
- 238000003825 pressing Methods 0.000 claims description 9
- 238000005507 spraying Methods 0.000 claims description 7
- 239000010802 sludge Substances 0.000 claims description 6
- 239000002002 slurry Substances 0.000 claims description 5
- 238000000926 separation method Methods 0.000 claims description 4
- 238000007599 discharging Methods 0.000 claims description 3
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- 241001062472 Stokellia anisodon Species 0.000 claims 1
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- 229910052731 fluorine Inorganic materials 0.000 abstract description 9
- 239000011737 fluorine Substances 0.000 abstract description 9
- 239000000779 smoke Substances 0.000 abstract description 8
- 239000012535 impurity Substances 0.000 abstract description 6
- 239000007787 solid Substances 0.000 abstract description 6
- 238000002156 mixing Methods 0.000 abstract description 4
- 230000000694 effects Effects 0.000 abstract description 3
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 abstract description 2
- 239000000460 chlorine Substances 0.000 abstract description 2
- 229910052801 chlorine Inorganic materials 0.000 abstract description 2
- 230000008021 deposition Effects 0.000 abstract description 2
- 238000004134 energy conservation Methods 0.000 abstract description 2
- 239000000126 substance Substances 0.000 abstract description 2
- PXGOKWXKJXAPGV-UHFFFAOYSA-N Fluorine Chemical compound FF PXGOKWXKJXAPGV-UHFFFAOYSA-N 0.000 abstract 1
- YCKRFDGAMUMZLT-UHFFFAOYSA-N Fluorine atom Chemical compound [F] YCKRFDGAMUMZLT-UHFFFAOYSA-N 0.000 description 8
- CWYNVVGOOAEACU-UHFFFAOYSA-N Fe2+ Chemical compound [Fe+2] CWYNVVGOOAEACU-UHFFFAOYSA-N 0.000 description 2
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- 230000002159 abnormal effect Effects 0.000 description 2
- 238000000151 deposition Methods 0.000 description 2
- 239000002184 metal Substances 0.000 description 2
- 229910052751 metal Inorganic materials 0.000 description 2
- AKEJUJNQAAGONA-UHFFFAOYSA-N sulfur trioxide Chemical compound O=S(=O)=O AKEJUJNQAAGONA-UHFFFAOYSA-N 0.000 description 2
- BUGBHKTXTAQXES-UHFFFAOYSA-N Selenium Chemical compound [Se] BUGBHKTXTAQXES-UHFFFAOYSA-N 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 1
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- 229910052742 iron Inorganic materials 0.000 description 1
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Abstract
The invention discloses a multi-level recycling system and method for acid-making wastewater from smelting flue gas, and belongs to the technical field of chemical industry. Firstly, a multi-level circulating concentration recycling system for purifying the acidic wastewater is formed by utilizing the concentration gradient formed by mixing acid from back to front in the acidic wastewater, and the deposition of smoke dust in the acidic wastewater and the concentration of fluorine, acid and chlorine, and a cooling tower is used for purifying a watershed to ensure that impurities in the smoke gas do not influence the safe and stable operation of a subsequent system; then the acid wastewater is deslimed by coarse and fine filtration, so that the problem of high solid content of the purified and recycled acid wastewater is solved, and the recycling rate of the acid wastewater is improved; in addition, the multi-stage atomization humidification is utilized to dissolve the hydrogen fluoride gas in the flue gas, and the risk that the hydrogen fluoride enters the rear-section drying and converting process is effectively avoided through condensation and electric demisting. The invention has the advantages of low investment, reliable operation, simple operation and remarkable concentration and recycling effects of the acidic wastewater, and achieves the aims of energy conservation, emission reduction and clean production.
Description
Technical Field
The invention belongs to the technical field of chemical industry, relates to wastewater treatment in non-ferrous metal smelting, and particularly relates to a multi-level recycling system and method for acid-making wastewater from smelting flue gas.
Background
In the wet purification and washing process of preparing acid from non-ferrous metal smelting flue gas, a large amount of acidic wastewater can be generated, the existing purification process is single, dust and lead which restrict the purification process are not effectively treated, and the acidic water discharge amount is large and the reuse rate is low. However, if the acid water is forced to circulate and concentrate in the purification system, firstly, the dust in the flue gas can cause serious deposition of acid mud in each purification tower, so that a spraying device and a filler in the tower are blocked, the washing and dedusting effects are further reduced, and the stability of a rear-end acid production system is not facilitated; secondly, dust mud in the system is continuously and circularly enriched, the lead content is increased, and the dust mud subsequently enters the interior of the electric demister, so that mud is accumulated on a cathode wire and an anode tube, lead is hung on the cathode wire and the anode tube, the demisting efficiency is reduced, and potential safety hazards exist; in addition, because smelting flue gas contains a large amount of harmful impurities, especially some gaseous impurities such as metal oxide mine dust with fine granularity, hydrogen fluoride and sulfur trioxide, the harm to a subsequent acid making system is large, acid water is forced to circulate in the original purification system, the concentration of various impurities caused by concentration of the acid water is increased, especially the enrichment of the hydrogen fluoride has large harm to a drying tower and rear-section equipment, and the stable and safe production of the rear-end acid making system is not facilitated.
Disclosure of Invention
The invention aims to provide a multi-level recycling system for acid-making wastewater from smelting flue gas, which improves the recycling rate of the acid-making wastewater from smelting flue gas on the premise of not influencing the stability and safety of a subsequent acid-making system.
The invention also aims to provide a method for recycling the acid-making wastewater from the smelting flue gas by multi-level circulation by using the system.
In order to achieve the purpose, the invention adopts the following technical scheme: a multilevel recycling system for acid-making wastewater from smelting flue gas comprises a turbulent washing tower, a cooling tower, a first-stage electric demister and a second-stage electric demister which are sequentially connected through a flue, wherein a reverse spray pipe humidifying nozzle is arranged on a reverse spray pipe of the turbulent washing tower, a bottom circulation tank of the turbulent washing tower is respectively connected with a spray device in the turbulent washing tower and a power wave nozzle of the reverse spray pipe through a circulating pump of the turbulent washing tower, a bottom settling tank of the turbulent washing tower is connected with an acid water buffer tank through a pipeline, the acid water buffer tank is connected with a suspension filter through an acid water buffer pump, the upper part of the suspension filter is respectively connected with a suspension clear liquid tank and a turbulent washing tower body through pipelines provided with a first valve and a second valve, the bottom of the suspension filter is connected with a slag tank through a pipeline, the suspension clear liquid tank and a slag tank provided with a bottom discharge valve at an outlet are both connected with a pressure filter through a suspension clear liquid buffer pump, the outlet of the clear liquid buffer tank is connected with a clear liquid buffer tank through a pipeline, and the outlet of the clear liquid buffer tank is provided with a third valve and is respectively connected with an overflow weir at the top of the counter-spraying pipe, a counter-spraying pipe humidifying nozzle, a turbulent tower body and an exhaust pipeline through a clear liquid delivery pump; the tower bottom circulating tank of the washing tower is respectively connected with a spray device in the washing tower and the turbulent tower body through a circulating pump of the washing tower; the cooling tower bottom circulating tank is respectively connected with the acid distributing device in the cooling tower and the washing tower body through a cooling tower circulating pump; the gas chamber at the bottom end of the first section of electric demister is connected with the tower body of the cooling tower through a pipeline, a first section of electric fog humidifying spray head is arranged on a flue of the cooling tower and the first section of electric demister, a second section of electric fog humidifying spray head is arranged on a flue between the first section of electric demister and the second section of electric demister, and the second section of electric fog humidifying spray head is connected with a humidifying pump; the outlet at the top of the second-stage electric demister is connected with the drying tower through a pipeline, the air chamber at the bottom end is connected with a second-stage electric fog condensate tank through a pipeline, and the second-stage electric fog condensate tank is connected with a first-stage electric fog humidifying spray head through a condensate water conveying pump.
For standby, the turbulent flow tower circulating pump, the washing tower circulating pump, the cooling tower circulating pump, the slurry pump, the acid water buffer pump, the suspension clear liquid buffer pump and the clear liquid conveying pump are all provided with two groups.
A method for multi-level recycling of acid-making wastewater from smelting flue gas by using the system specifically comprises the following steps:
A. conveying production water to a two-stage electric fog humidifying spray head through a humidifying pump, carrying out countercurrent contact on the atomized production water and the flue gas discharged from a first-stage electric demister, dissolving hydrogen fluoride gas in the flue gas, then, feeding the dissolved hydrogen fluoride gas into the two-stage electric demister for condensation, feeding the condensed hydrogen fluoride gas into a two-stage electric fog condensate water tank for collection, and discharging the fluorine-removed flue gas from an outlet at the top of the two-stage electric demister and feeding the flue gas into a drying tower;
B. the collected condensed water is conveyed to a section of electric fog humidifying spray head through a condensed water conveying pump, is in countercurrent contact with the flue gas discharged out of the cooling tower after being atomized, is condensed through a section of electric demister after dissolving the hydrogen fluoride gas in the flue gas, and flows into the cooling tower to be used as purified make-up water;
C. conveying the acidic wastewater circulated in the cooling tower to a cooling tower acid separation device through a circulating pump part of the cooling tower to wash flue gas, and forcibly adding acid in series to the washing tower; the acid wastewater circulated in the washing tower is partially conveyed to a spraying device of the washing tower through a circulating pump of the washing tower to wash flue gas, and partial acid is forcibly mixed and supplemented to the turbulent washing tower; conveying the acidic wastewater circulated in the turbulent washing tower to a reverse spray pipe power wave spray head and a turbulent washing tower spray device through a turbulent washing tower circulating pump to wash the flue gas, physically settling in a settling tank of the turbulent washing tower, and conveying the acidic wastewater to an acid water buffer tank through a slurry pump, so that the acidic wastewater with the highest impurity concentration after the flue gas is washed in a purification process enters an acid water treatment process in a backward-forward acid mixing mode;
D. conveying the acid wastewater in the acid water buffer tank to a suspension filter through an acid water buffer pump for coarse filtration, allowing clear liquid to flow into a suspension clear liquid tank, and discharging settled acid sludge to a slag tank for temporary storage;
E. conveying the clear liquid in the suspension clear liquid tank to a filter pressure device through a suspension clear liquid buffer pump for fine filtration, conveying the filtered clear liquid into the clear liquid buffer tank, conveying the clear liquid to an overflow weir through a clear liquid conveying pump to be used as overflow weir supplementing water, conveying part of the clear liquid to a reverse spray pipe humidifying nozzle, carrying out countercurrent contact with the flue gas after atomization, dissolving hydrogen fluoride gas in the flue gas, conveying part of the atomized clear liquid to a turbulent flushing tower for continuous circulating concentration, and conveying part of the atomized clear liquid to an exhaust pipeline to enter the next process;
F. e, when the flow of the inlet of the pressure filtering device is reduced to 60 percent of the original flow and the pressure is increased to be more than 0.4Mpa, opening the first valve, closing the second valve, isolating the pressure filtering device, and directly conveying the supernatant in the suspension filter to a purification system; when the liquid level of the suspension clear liquid tank is reduced to the minimum, a bottom discharge valve of the slag tank is quickly opened, a third valve is closed, and the acid sludge temporarily stored in the slag tank is conveyed to a filter-press device through a suspension clear liquid buffer pump for filter-press operation;
G. and F, after the pressure filtration operation is finished, opening the second valve, closing the first valve, opening the third valve and closing the bottom discharge valve of the slag tank in sequence, and recovering the circulating concentration recycling process.
And F, bagging and storing the dry slag obtained by filter pressing operation, wherein the dry slag contains a large amount of valuable elements such as lead, selenium and the like, and can be continuously recycled.
Compared with the prior art, the fluidization magnetization roasting dry-grinding dry-separation process for refractory iron ore has the following advantages:
compared with the prior art, the invention has the following beneficial effects: the invention relates to a multi-level recycling system for acid-making wastewater from smelting flue gas, which mainly comprises a turbulent flow tower, a washing tower, a cooling tower, a first-stage electric demister, a second-stage electric fog condensate water tank, an acid water buffer tank, a suspension filter, a slag tank, a suspension clear liquid tank, a filter pressing device, a clear liquid buffer tank, a reverse spray pipe humidifying nozzle, a first-stage electric fog humidifying nozzle and a second-stage electric fog humidifying nozzle; the method comprises the steps of firstly, forming a multi-level circulating concentration recycling system for purifying the acidic wastewater by utilizing a concentration gradient formed by mixing acid from back to front in the process of purifying the acidic wastewater, and depositing smoke dust in the acidic wastewater and concentrating fluorine, acid and chlorine, and ensuring that impurities in the smoke do not influence the safe and stable operation of a subsequent system by taking a cooling tower as a purification watershed; then the acid wastewater is deslimed by two-stage filtration of coarse filtration and fine filtration, so that the problem of high solid content of the purified and recycled acid wastewater is solved, and the recycling rate of the acid wastewater is improved; in addition, the multi-stage atomization humidification is utilized to dissolve the hydrogen fluoride gas in the flue gas, and the risk that the hydrogen fluoride enters the rear-section drying and converting process is effectively avoided through condensation and electric demisting. The invention has the advantages of low investment, reliable operation, obvious concentration and recycling effects of the acidic wastewater, small occupied area, simple operation and low operation cost, and achieves the aims of energy conservation, emission reduction and clean production.
Drawings
FIG. 1 is a schematic diagram showing the connection relationship between devices in the system of the present invention.
Reference numerals: 1-rushing a tower; 2-a washing tower; 3-a cooling tower; 4-first stage electric demister; 5-two-stage electric demister; 6-two-section electric fog condensate water tank; 7-acid water buffer tank; 8-a suspension filter; 9-a slag pot; 10-a suspension clear solution tank; 11-a filtration and pressure device; 12-clear liquid buffer tank; 13-turbulent tower circulating pump; 14-washing column circulation pump; 15-cooling tower circulation pump; 16-a humidifying pump; 17-a condensate transfer pump; 18-a mud pump; 19-acid water buffer pump; 20-suspension clear liquid buffer pump; 21-clear liquid transfer pump; 22-a weir; 23-a reverse nozzle humidifying nozzle; 24-a section of electric fog humidifying spray head; 25-two-stage electric fog humidifying spray head; 26-an outer discharge pipe; 27-a first valve; 28-a second valve; 29-bottom drain valve; 30-a third valve; 31-drying tower.
Detailed Description
The invention is further described with reference to the following figures and specific examples.
Example 1
As shown in figure 1, a multi-stage recycling system for acid-making wastewater from smelting flue gas comprises a turbulent washing tower 1, a washing tower 2, a cooling tower 3, a first-stage electric demister 4 and a second-stage electric demister 5 which are sequentially connected through a flue, wherein a reverse spray pipe humidifying nozzle 23 is arranged on a reverse spray pipe of the turbulent washing tower 1, a tower bottom circulating tank of the turbulent washing tower 1 is respectively connected with a spray device in the turbulent washing tower 1 and a power wave nozzle of the reverse spray pipe through two groups of turbulent washing tower circulating pumps 13 (one is opened and the other is prepared), a sedimentation tank at the bottom of the turbulent washing tower 1 is connected with an acid water buffer tank 7 through two groups of mud pumps 18 (one is opened and the other is prepared), the acid water buffer tank 7 is connected with a suspension filter 8 through two groups of acid water buffer pumps 19 (one is opened and the other is prepared), the upper part of the suspension filter 8 is respectively connected with a suspension clear liquid tank 10 and a tower body of the turbulent washing tower 1 through a pipeline provided with a first valve 27 and a second valve 28, the, the suspended clear liquid tank 10 and the slag tank 9 are both connected with a filtering and pressing device 11 through two groups of suspended clear liquid buffer pumps 20 (one is opened and one is prepared), a pressure gauge and a flow meter are arranged on a pipeline at the inlet of the filtering and pressing device 11, an outlet is connected with a clear liquid buffer tank 12 through a pipeline, a third valve 30 is arranged at the outlet of the clear liquid buffer tank 12, and the suspended clear liquid tank and the slag tank are respectively connected with an overflow weir 22 at the top of a reverse spray pipe, a reverse spray pipe humidifying nozzle 23, a turbulent tower 1 and an external discharge pipeline 26 through two groups of clear liquid delivery pumps 21 (one is opened; the tower bottom circulating groove of the washing tower 2 is respectively connected with a spraying device in the washing tower 2 and the tower body of the turbulent tower 1 through two groups of washing tower circulating pumps 14 (one is opened and the other is prepared); the tower bottom circulating groove of the cooling tower 3 is respectively connected with an acid separating device in the cooling tower 3 and the tower body of the washing tower 2 through two groups of cooling tower circulating pumps 15 (one is opened and one is prepared); the bottom end air chamber of the first section of electric demister 4 is connected with the tower body of the cooling tower 3 through a pipeline, a first section of electric fog humidifying spray head 24 is arranged on the flue of the cooling tower 3 and the first section of electric demister 4, a second section of electric fog humidifying spray head 25 is arranged on the flue between the first section of electric demister 4 and the second section of electric demister 5, and the second section of electric fog humidifying spray head 25 is connected with the humidifying pump 16; the outlet at the top of the two-section electric demister 5 is connected with the drying tower 31 through a pipeline, the air chamber at the bottom end is connected with the two-section electric fog condensate water tank 6 through a pipeline, and the two-section electric fog condensate water tank 6 is connected with the one-section electric fog humidifying spray head 24 through the condensate water conveying pump 17.
The system is applied to smelting flue gas in normal production (the concentration of HF in the flue gas is 17.43 mg/Nm)3-24.11mg/Nm3Average concentration of 22.42mg/Nm3And the smoke contains dust: less than or equal to 500 mg/Nm3And the smoke amount: 166424Nm3/h-183293Nm3H, average gas amount of 174859Nm3The method specifically comprises the following steps of: the production water is conveyed to a two-stage electric fog humidifying spray head 25 through a humidifying pump 16, and is in countercurrent contact with the flue gas discharged from a first-stage electric demister 4 after being atomized, the hydrogen fluoride gas in the flue gas is dissolved, then is condensed through a second-stage electric demister 5 and flows into a second-stage electric fog condensate water tank 6, and the flue gas after fluorine removal is discharged from an outlet at the top of the second-stage electric demister 5 and enters a drying tower 31; condensed water collected by the second-stage electric fog condensed water tank 6 is conveyed to a first-stage electric fog humidifying spray head 24 through a condensed water conveying pump 17, is in countercurrent contact with the flue gas out of the cooling tower 3 after being atomized, is condensed through the first-stage electric demister 4 after dissolving the hydrogen fluoride gas in the flue gas, and flows into the cooling tower 3 to be used as purified make-up water; the acidic wastewater circulated in the cooling tower 3 is partially conveyed to the acid separation device of the cooling tower 3 through a circulating pump 15 of the cooling tower to wash the flue gas, and partial acid is forcibly mixed and supplemented to the washing tower 2, and the acid is mixed in the washing tower 2The circulating acidic waste water is partially conveyed to a spray device of a washing tower 2 through a circulating pump 14 of the washing tower to wash flue gas, partial acid mixing is forced to be supplemented to a turbulent washing tower 1, the acidic waste water circulating in the turbulent washing tower 1 is conveyed to a reverse spray pipe power wave spray head and the spray device of the turbulent washing tower 1 through a circulating pump 13 of the turbulent washing tower to wash the flue gas, and then the acidic waste water is physically settled in a settling tank of the turbulent washing tower 1 and conveyed to an acid water buffer tank 7 through a slurry pump 18. Through detection, the indexes of the acidic wastewater in the acid water buffer tank 7 are the highest (acidity: 165.6g/L, fluorine content: 3144.43mg/L, solid content: 25.36 g/L, discharge amount: 60 m)3The acid wastewater is conveyed to a suspension filter 8 through an acid water buffer pump 19 for coarse filtration, clear liquid flows into a suspension clear liquid tank 10, and settled acid sludge is discharged to a slag tank 9 for temporary storage; the clear liquid in the suspension clear liquid tank 10 is conveyed to a filter pressure device 11 through a suspension clear liquid buffer pump 20 for fine filtration, the filtered clear liquid flows into a clear liquid buffer tank 12, the clear liquid indexes (acidity: 169.15g/L, fluorine content: 3189.19mg/L, solid content: 0.023 g/L) are detected, part of the clear liquid indexes are conveyed to an overflow weir 22 through a clear liquid conveying pump 21 to be used as the supplement water of the overflow weir 22, part of the clear liquid indexes are conveyed to a reverse spray pipe humidifying nozzle, the atomized clear liquid is in countercurrent contact with the flue gas to dissolve more hydrogen fluoride gas in the flue gas, part of the atomized clear liquid indexes is conveyed to a turbulent flow tower 1 to be continuously circulated and concentrated, the rest part of the clear liquid indexes is conveyed to an exhaust pipeline3H; when the inlet flow of the pressure filter 11 is reduced to 40m3H, when the pressure is increased to be more than 0.4Mpa, the first valve 27 is opened, the second valve 28 is closed, the isolated filter pressure device 11 is closed, and the clear liquid of the suspension filter 8 is directly conveyed to a purification system; and when the liquid level of the suspension clear liquid tank 10 is reduced to the minimum, quickly opening a bottom discharge valve 29 of the slag tank 9, closing a third valve 30, conveying all the acid sludge temporarily stored in the slag tank 9 to a filter-press device 11 for filter-press operation, bagging and storing the filter-pressed dry slag, and continuously recycling the dry slag. In the normal production process, the fluorine content of the flue gas at the outlet of the two-stage electric demister 5 can be controlled to be 0.48-0.85 mg/Nm3In the meantime.
Example 2
The multi-level recycling system for acid-making wastewater from smelting flue gas in the embodiment is the same as that in embodiment 1, and is applied to smelting flue gas with large index fluctuation (flue gas HF concentration: 1).96mg/Nm3-38.92mg/Nm3Average concentration of 27.72mg/Nm3And the smoke contains dust: 860 mg/Nm3And the smoke amount: 171130Nm3/h-205884Nm3H, average gas amount of 188507Nm3In the abnormal production of/h), the procedure was as in example 1. The index of the acid wastewater in the acid water buffer tank 7 is highest (acidity: 214.35g/L, fluorine content: 3672.2mg/L, solid content: 34.57 g/L, discharge amount: 60 m)3H), clear liquid index of filtration pressure equipment 11 (acidity: 221.47g/L, fluorine content: 3519.72mg/L, solid content: 0.036 g/L), the discharge amount can be reduced to 12 m3H is used as the reference value. In the abnormal production process, the fluorine content of the flue gas at the outlet of the two-stage electric demister 5 can be controlled to be 0.68-1.34 mg/Nm3In the meantime.
Claims (10)
1. The utility model provides a smelt flue gas system acid waste water multilevel cycle recycling system which characterized in that: comprises a turbulent washing tower (1), a washing tower (2), a cooling tower (3), a section of electric demister (4) and a section of electric demister (5) which are connected in turn through a flue, a reverse spray pipe humidifying spray head (23) is arranged on a reverse spray pipe of the turbulent washing tower (1), a tower bottom circulating groove of the turbulent washing tower (1) is respectively connected with a spray device in the turbulent washing tower (1) and a power wave spray head of the reverse spray pipe through a turbulent washing tower circulating pump (13), a bottom settling groove of the turbulent washing tower (1) is connected with an acid water buffer tank (7) through a slurry pump (18), the acid water buffer tank (7) is connected with a suspension filter (8) through an acid water buffer pump (19), the upper part of the suspension filter (8) is respectively connected with a suspension clear liquid tank (10) and a tower body of the turbulent washing tower (1) through a pipeline provided with a first valve (27) and a second valve (28), the bottom of the suspension filter (8) is connected with a slag tank (9) provided with a bottom discharge valve (29, the suspension clear liquid tank (10) and the slag tank (9) are both connected with a filtering and pressing device (11) through a suspension clear liquid buffer pump (20), a pressure gauge and a flowmeter are arranged on a pipeline at the inlet of the filtering and pressing device (11), an outlet is connected with a clear liquid buffer tank (12) through a pipeline, a third valve (30) is arranged at the outlet of the clear liquid buffer tank (12), and the third valve is respectively connected with an overflow weir (22) at the top of a counter-spray pipe, a counter-spray pipe humidifying nozzle (23), a turbulent washing tower body (1) and an external discharge pipeline (26) through a clear liquid conveying pump (21); the tower bottom circulating groove of the washing tower (2) is respectively connected with a spraying device in the washing tower (2) and the tower body of the turbulent tower (1) through a washing tower circulating pump (14); the tower bottom circulating groove of the cooling tower (3) is respectively connected with the acid separating device in the cooling tower (3) and the tower body of the washing tower (2) through a cooling tower circulating pump (15); the bottom end air chamber of the first section of electric demister (4) is connected with the tower body of the cooling tower (3) through a pipeline, a first section of electric fog humidifying spray head (24) is arranged on a flue of the cooling tower (3) and the first section of electric demister (4), a second section of electric fog humidifying spray head (25) is arranged on a flue between the first section of electric demister (4) and the second section of electric demister (5), and the second section of electric fog humidifying spray head (25) is connected with a humidifying pump (16); the outlet at the top of the two-section electric demister (5) is connected with the drying tower (31) through a pipeline, the air chamber at the bottom end is connected with the two-section electric fog condensate water tank (6) through a pipeline, and the two-section electric fog condensate water tank (6) is connected with the one-section electric fog humidifying spray head (24) through a condensate water delivery pump (17).
2. The multi-level recycling system for the acid-making wastewater of smelting flue gas as claimed in claim 1, wherein the multi-level recycling system comprises: the turbulent tower circulating pumps (13) are divided into two groups.
3. The multi-level recycling system for the acid-making wastewater of smelting flue gas as claimed in claim 1, wherein the multi-level recycling system comprises: the circulating pumps (14) of the washing tower are divided into two groups.
4. The multi-level recycling system for the acid-making wastewater of smelting flue gas as claimed in claim 1, wherein the multi-level recycling system comprises: the number of the cooling tower circulating pumps (15) is two.
5. The multi-level recycling system for the acid-making wastewater of smelting flue gas as claimed in claim 1, wherein the multi-level recycling system comprises: the mud pumps (18) are divided into two groups.
6. The multi-level recycling system for the acid-making wastewater of smelting flue gas as claimed in claim 1, wherein the multi-level recycling system comprises: the acid water buffer pumps (19) are divided into two groups.
7. The multi-level recycling system for the acid-making wastewater of smelting flue gas as claimed in claim 1, wherein the multi-level recycling system comprises: the suspension liquid buffer pumps (20) are divided into two groups.
8. The multi-level recycling system for the acid-making wastewater of smelting flue gas as claimed in claim 1, wherein the multi-level recycling system comprises: the clear liquid conveying pumps (21) are divided into two groups.
9. The method for recycling the acid-making wastewater from the smelting flue gas by multi-level circulation by using the system as claimed in claim 1, which is characterized by comprising the following steps:
A. conveying production water to a two-stage electric fog humidifying spray head (25) through a humidifying pump (16), carrying out countercurrent contact on the atomized production water and the flue gas discharged from a first-stage electric demister (4), dissolving hydrogen fluoride gas in the flue gas, then feeding the dissolved hydrogen fluoride gas into a second-stage electric demister (5) for condensation, feeding the condensed hydrogen fluoride gas into a second-stage electric fog condensate water tank (6) for collection, and discharging the fluorine-removed flue gas from an outlet at the top of the second-stage electric demister (5) to enter a drying tower (31);
B. condensed water collected by the second-stage electric fog condensed water tank (6) is conveyed to the first-stage electric fog humidifying spray head (24) through a condensed water conveying pump (17), atomized and then in countercurrent contact with flue gas out of the cooling tower (3), hydrogen fluoride gas in the flue gas is dissolved, then condensed through the first-stage electric demister (4), and flows into the cooling tower (3) to be used as purified make-up water;
C. part of the acid wastewater circulated in the cooling tower (3) is conveyed to an acid separation device of the cooling tower (3) through a circulating pump (15) of the cooling tower to wash the flue gas, and part of the acid wastewater is forcibly mixed and supplemented to the washing tower (2); part of the acid wastewater circulated in the washing tower (2) is conveyed to a spraying device of the washing tower (2) through a circulating pump (14) of the washing tower to wash flue gas, and part of the acid wastewater is forcibly mixed and supplemented to the turbulent washing tower (1); acidic wastewater circulating in the turbulent tower (1) is conveyed to a reverse spray pipe power wave spray head and a spray device of the turbulent tower (1) through a turbulent tower circulating pump (13) to wash flue gas, and then physically settled in a settling tank of the turbulent tower (1), and then conveyed to an acidic water buffer tank (7) through a slurry pump (18);
D. acid wastewater in the acid water buffer tank (7) is conveyed to a suspension filter (8) through an acid water buffer pump (19) for coarse filtration, clear liquid flows into a suspension clear liquid tank (10), and settled acid sludge is discharged to a slag tank (9) for temporary storage;
E. clear liquid in a suspended clear liquid tank (10) is conveyed to a filter pressure device (11) through a suspended clear liquid buffer pump (20) for fine filtration, the filtered clear liquid flows into a clear liquid buffer tank (12) from the filter pressure device, and is partially conveyed to an overflow weir (22) through a clear liquid conveying pump (21) to be used as supplementing water for the overflow weir (22), and is partially conveyed to a reverse-jet pipe humidifying nozzle (23), and is in countercurrent contact with flue gas after atomization, hydrogen fluoride gas in the flue gas is dissolved, and is partially conveyed to a turbulent washing tower (1) to continue circulating concentration, and is partially conveyed to an exhaust pipeline (26) to enter a next process;
F. in the step E, when the inlet flow of the pressure filtering device (11) is reduced to 60 percent of the original flow and the pressure is increased to be more than 0.4Mpa, the first valve (27) is opened, the second valve (28) is closed, the pressure filtering device (11) is isolated, and the supernatant in the suspension filter (8) is directly conveyed to a purification system; when the liquid level of the suspension clear liquid tank (10) is reduced to the minimum, a bottom discharge valve (29) of the slag tank (9) is quickly opened, a third valve (30) is closed, and the acid sludge temporarily stored in the slag tank (9) is conveyed to a filter pressing device (11) through a suspension clear liquid buffer pump (20) for filter pressing operation;
G. and F, after the filtration operation is finished, opening the second valve (28), closing the first valve (27), opening the third valve (30) and closing the bottom discharge valve (29) of the slag tank (9) in sequence, and recovering the circulating concentration recycling process.
10. The method for multi-level recycling of acid-making wastewater from smelting flue gas according to claim 9, characterized in that: and F, storing the dry slag obtained by the filter pressing operation in a bag, and recovering valuable elements.
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| CN110354622A (en) * | 2019-07-30 | 2019-10-22 | 易门铜业有限公司 | Flue gas removal of impurities and tail gas cleaning device in a kind of acid manufacturing processes |
| CN110433630B (en) * | 2019-08-15 | 2022-03-01 | 湖南株冶环保科技有限公司 | Deep purification and mercury recovery process for mercury in lead-zinc smelting flue gas |
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| JP2805497B2 (en) * | 1989-05-11 | 1998-09-30 | 千代田化工建設株式会社 | Treatment of wet flue gas desulfurization wastewater |
| CN201015724Y (en) * | 2007-03-01 | 2008-02-06 | 徐全海 | Waste gas processing device |
| CN101274210A (en) * | 2007-12-25 | 2008-10-01 | 金川集团有限公司 | Method for removing fluoride in flue gas during smelting |
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