CN108862807B - Device and method for removing fluorine and chlorine by evaporation and concentration of strengthened copper smelting waste acid - Google Patents
Device and method for removing fluorine and chlorine by evaporation and concentration of strengthened copper smelting waste acid Download PDFInfo
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- CN108862807B CN108862807B CN201810547746.2A CN201810547746A CN108862807B CN 108862807 B CN108862807 B CN 108862807B CN 201810547746 A CN201810547746 A CN 201810547746A CN 108862807 B CN108862807 B CN 108862807B
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/48—Treatment of water, waste water, or sewage with magnetic or electric fields
- C02F1/481—Treatment of water, waste water, or sewage with magnetic or electric fields using permanent magnets
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/58—Treatment of water, waste water, or sewage by removing specified dissolved compounds
- C02F1/583—Treatment of water, waste water, or sewage by removing specified dissolved compounds by removing fluoride or fluorine compounds
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/12—Halogens or halogen-containing compounds
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/12—Halogens or halogen-containing compounds
- C02F2101/14—Fluorine or fluorine-containing compounds
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/16—Nature of the water, waste water, sewage or sludge to be treated from metallurgical processes, i.e. from the production, refining or treatment of metals, e.g. galvanic wastes
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Abstract
The invention discloses a device and a method for removing fluorine and chlorine by evaporation concentration of waste acid in reinforced copper smelting, belongs to the field of copper smelting, and solves the problem that a large amount of dangerous waste which is difficult to treat is generated in the prior art. The device comprises an evaporation concentration device and a circulating device, wherein the circulating device comprises a valve, a flowmeter, a circulating pump, a magnet and a pipeline, and the valve, the flowmeter, the circulating pump, the magnet and a heating groove in the evaporation concentration device are connected in series on the pipeline to form a circulating loop. The method of the invention comprises the following steps: starting a circulating pump and a heating device to perform evaporation concentration under the condition that the magnetic induction intensity is 1-3T; removing the crystals; performing a defluorination process under the condition that the magnetic induction intensity is 0.2-0.8T; the dechlorination process is carried out under the condition that the magnetic induction intensity is 0.2-0.8T. The invention has the beneficial effects that: the efficiency of removing fluorine and chlorine by evaporating and concentrating the copper smelting waste acid is improved; no environmental pollution.
Description
Technical Field
The invention belongs to the field of copper smelting, and particularly relates to a device and a method for removing fluorine and chlorine by evaporation and concentration of waste acid generated in copper smelting.
Background
The waste acid generated by copper smelting mainly refers to high-arsenic high-acid waste liquid discharged by a copper pyrometallurgical flue gas acid making system and associated rare and noble metal extraction production. The waste acid solution system is very complex, has multiple components and high concentration, mainly contains high-concentration arsenic ions, sulfate ions, fluoride ions and chloride ions, and also contains various metals such as copper, zinc, lead, cadmium and the like, thereby being refractory mining and metallurgy industrial wastewater.
For waste acid generated in copper smelting, a vulcanization precipitation-neutralization iron salt treatment method is generally adopted at present, and the method has the problems of high treatment cost, generation of a large amount of dangerous waste which is difficult to treat, failure in resource recovery of various valuable substances in the waste acid, difficulty in meeting the recycling requirement of effluent water quality and the like.
Disclosure of Invention
The invention aims to provide a device for removing fluorine and chlorine by evaporation concentration of enhanced copper smelting waste acid, which aims to solve the problems that a large amount of dangerous waste which is difficult to treat is generated and various valuable substances in the waste acid are not recycled when the copper smelting waste acid is treated by the prior art.
The invention also aims to provide a method for removing fluorine and chlorine by enhancing the evaporation concentration of the copper smelting waste acid.
The technical scheme of the invention is as follows:
the utility model provides a device that dirty sour evaporative concentration of intensive copper smelting removed fluorine and chlorine, includes the evaporative concentration device, the evaporative concentration device includes heating tank, heating device, condensing equipment and collection device, still includes circulating device, and circulating device includes valve, flowmeter, circulating pump, magnet and pipeline, and valve, flowmeter, circulating pump and magnet concatenate on the pipeline, and the heating tank both ends are equipped with the interface, and the heating tank passes through the interface and links to each other with the pipeline and forms circulation circuit.
As a further improvement of the invention, the number of the magnets is at least two, and the magnetic field directions are alternately distributed upwards and downwards, so that the magnetization efficiency can be enhanced.
As a further improvement of the invention, the interfaces are positioned in the middle or upper parts of the two ends of the heating tank so as to avoid the liquid flow from impacting crystals at the bottom of the heating tank.
A method for removing fluorine and chlorine by evaporation concentration of waste acid from copper smelting is enhanced, and comprises the following steps:
firstly, pouring waste acid into a heating tank, setting the magnetic induction intensity of a magnet to be 1-3T, starting a circulating pump and a heating device, setting the flow velocity of the waste acid through a valve and a flowmeter, carrying out evaporation concentration, and recycling evaporated gas to a collecting device through a condensing device to form condensate;
step two, after the waste acid is evaporated, removing crystals so as to recover other valuable elements in the next step;
step three, pouring the condensate recovered in the step one back to a heating tank, adjusting the magnetic induction intensity to 0.2-0.8T, starting a circulating pump and a heating device, setting the flow rate of the waste acid, controlling the pH to be 11-12, and adding CaO and Ca (OH)2And CaCl2After reacting for 20-30 min, closing the circulating pump and the heating device, standing for 50-80 min, and then completing the defluorination process;
step four, taking clear supernatant of the condensate subjected to fluorine removal in the step three, placing the clear supernatant in a heating tank, adjusting the magnetic induction intensity to 0.2-0.8T, starting a circulating pump and a heating device, setting the flow rate of the waste acid, controlling the pH to be 12.8-13, and adding Ca (OH)2And NaAlO2And completing the dechlorination process after reacting for 50-70 min.
As a further improvement of the invention, in the first step, the third step and the fourth step, the flow velocity of the waste acid is 0.2-1 m/s, and the magnetizing effect can be influenced by too large or too small flow velocity.
As a further improvement of the invention, in the step one, the evaporation concentration multiple is 6-7 times. Too low a concentration by evaporation leads to F-And Cl-Too small a concentration is not conducive to crystallization.
As a further improvement of the invention, in the first step, the temperature of the heating device is 120-140 ℃. Low temperature, low evaporation, long evaporation time, high temperature, F-And Cl-And also evaporated, damaging the equipment.
As a further improvement of the invention, in the third step, the temperature of the heating device is 120-140 ℃, and CaO and Ca (OH) are added2And CaCl2The molar ratio of calcium to fluorine is 1.2-1.5: 1.
As a further improvement of the present invention,in the fourth step, the temperature of the heating device is 35-45 ℃, and Ca (OH) is added2And NaAlO2The molar ratio of calcium to aluminum to chlorine is 10-10.5: 4-4.5: 1.
Preferably, in step one, the magnetic induction is 2T, and in step three and step four, the magnetic induction is 0.5T.
The invention adds a circulating system on the original device, and arranges a magnet on the circulating system to make the waste acid in a circulating state and perform chemical reaction under the action of a magnetic field, and has the following beneficial effects:
1. the magnetic field can reduce the surface tension of the solution, thereby improving the efficiency of evaporating, concentrating and removing fluorine and chlorine from the copper smelting waste acid;
2. the invention does not cause pollution to the environment and has obvious environmental benefit;
3. the invention does not need to add a flocculating agent, can improve the use efficiency of the medicament, shortens the reaction time, greatly reduces the cost and has obvious economic benefit;
4. the invention can increase the evaporation concentration rate and the sedimentation rate, so crystals with poor natural sedimentation performance can be quickly settled in a short time.
Drawings
FIG. 1 is a schematic view of the structure of the apparatus used in the present invention.
In the figure, 1-valve; 2-a flow meter; 3-a circulating pump; 4-an adjustable permanent magnet; 5-heating a tank; 6-interface; 7-a pipeline; 8-a heating device; 9-a condensing unit; 10-a collecting device.
Detailed Description
The following examples further illustrate the invention but are not intended to limit the invention in any way.
The utility model provides a device that dirty sour evaporative concentration of intensive copper smelting removed fluorine and chlorine, as shown in figure 1, includes the evaporative concentration device, the evaporative concentration device includes heating tank 5, heating device 8, condensing equipment 9 and collection device 10, still includes circulating device, and circulating device includes valve 1, flowmeter 2, circulating pump 3, magnet 4 and pipeline 7, valve 1, flowmeter 2, circulating pump 3 and magnet 4 concatenate on pipeline 7, and 5 both ends in heating tank are equipped with interface 6, and heating tank 5 links to each other with pipeline 7 through interface 6 and forms circulation circuit.
The number of the magnets 4 is at least two, and the magnetic field directions are distributed alternately upwards and downwards.
The interfaces 6 are located at the middle or upper portions of both ends of the heating bath 5.
The copper smelting waste acid in the following three examples is taken from a copper smelting plant, wherein the concentration of fluorine and chlorine in the stock solution is 10g/L and 15g/L respectively.
Examples 1,
In the embodiment, 5 magnets 4 are arranged, and the magnetic field directions are alternately distributed upwards and downwards.
Firstly, pouring waste acid into a heating tank 5, setting the magnetic induction intensity of a magnet 4 to be 1T, starting a circulating pump 3 and a heating device 8, setting the temperature of the heating device 8 to be 120 ℃, setting the flow rate of the waste acid to be 0.2m/s by using a valve 1 and a flowmeter 2, carrying out evaporation concentration, wherein the concentration multiple is 6 times, and recovering the evaporated gas to a collecting device 10 through a condensing device 9 to form condensate;
step two, after the waste acid is evaporated, removing crystals so as to recover other valuable elements in the next step;
step three, pouring the condensate recovered in the step one back to a heating tank 5, adjusting the magnetic induction intensity to 0.2T, starting a circulating pump 3 and a heating device 8, setting the temperature of the heating device 8 to 120 ℃, setting the flow rate of the waste acid to 0.2m/s, controlling the pH to be 11-12, and then respectively adding CaO and Ca (OH) according to the calcium-fluorine molar ratio of 1.2:12And CaCl2After 20min, the circulating pump 3 and the heating device 8 are closed, and the defluorination process is completed after standing for 50 min;
step four, placing the clarified supernatant of the condensate subjected to defluorination in the step three in a heating tank 5, adjusting the magnetic induction intensity to 0.2T, starting a circulating pump 3 and a heating device 8, setting the temperature of the heating device 8 to 35 ℃, setting the flow rate of waste acid to 0.2m/s, controlling the pH to 12.8-13, and adding Ca (OH) according to the molar ratio of calcium to aluminum to chlorine of 10:4:12And NaAlO2And the dechlorination process is completed after the reaction time is 50 min.
In the embodiment, after the defluorination process is finished, the supernatant of the condensate is measured, wherein the concentration of fluorine ions is 6.5mg/L, the removal rate is over 99 percent, and the condensate meets the national standard; after the dechlorination process is finished, standing the condensate for a period of time until the supernatant is clear, taking part of the supernatant to measure the chloride ion concentration to be 4.9mg/L, wherein the removal rate reaches more than 99 percent and meets the national standard.
Examples 2,
In the embodiment, 8 magnets 4 are arranged, and the magnetic field directions are alternately distributed upwards and downwards.
Firstly, pouring waste acid into a heating tank 5, setting the magnetic induction intensity of a magnet 4 to be 2T, starting a circulating pump 3 and a heating device 8, setting the temperature of the heating device 8 to be 130 ℃, setting the flow rate of the waste acid to be 0.4m/s by using a valve 1 and a flowmeter 2, carrying out evaporation concentration, wherein the concentration multiple is 7 times, and recovering the evaporated gas to a collecting device 10 through a condensing device 9 to form condensate;
step two, after the waste acid is evaporated, removing crystals so as to recover other valuable elements in the next step;
step three, pouring the condensate recovered in the step one back to a heating tank 5, adjusting the magnetic induction intensity to 0.5T, starting a circulating pump 3 and a heating device 8, setting the temperature of the heating device 8 to 130 ℃, setting the flow rate of the waste acid to 0.4m/s, controlling the pH to be 11-12, and then respectively adding CaO and Ca (OH) according to the calcium-fluorine molar ratio of 1.2:12And CaCl2After 20min, the circulating pump 3 and the heating device 8 are closed, and the defluorination process is finished after standing for 60 min;
step four, placing the clarified supernatant of the condensate subjected to defluorination in the step three in a heating tank 5, adjusting the magnetic induction intensity to 0.5T, starting a circulating pump 3 and a heating device 8, setting the temperature of the heating device 8 to 40 ℃, setting the flow rate of waste acid to 0.4m/s, controlling the pH to 12.8-13, and adding Ca (OH) according to the molar ratio of calcium to aluminum to chlorine of 10:4:12And NaAlO2And the dechlorination process is finished after the reaction time is 60 min.
In the embodiment, after the defluorination process is finished, the supernatant of the condensate is measured, wherein the concentration of fluorine ions is 2.5mg/L, the removal rate is more than 99 percent, and the national standard is met; after the dechlorination process is finished, standing the condensate for a period of time until the supernatant is clear, taking part of the supernatant to measure the chloride ion concentration to be 1.9mg/L, wherein the removal rate reaches more than 99 percent and meets the national standard.
Examples 3,
In the embodiment, 2 magnets 4 are arranged, and the magnetic field directions are alternately distributed upwards and downwards.
Firstly, pouring waste acid into a heating tank 5, setting the magnetic induction intensity of a magnet 4 to be 3T, starting a circulating pump 3 and a heating device 8, setting the temperature of the heating device 8 to be 140 ℃, setting the flow rate of the waste acid to be 1m/s by using a valve 1 and a flowmeter 2, carrying out evaporation concentration, wherein the concentration multiple is 7 times, and recovering the evaporated gas to a collecting device 10 through a condensing device 9 to form condensate;
step two, after the waste acid is evaporated, removing crystals so as to recover other valuable elements in the next step;
step three, pouring the condensate recovered in the step one back to a heating tank 5, adjusting the magnetic induction intensity to 0.8T, starting a circulating pump 3 and a heating device 8, setting the temperature of the heating device 8 to 140 ℃, setting the flow rate of the waste acid to 1m/s, controlling the pH to be 11-12, and then respectively adding CaO and Ca (OH) according to the calcium-fluorine molar ratio of 1.5:12And CaCl2After 30min, the circulating pump 3 and the heating device 8 are closed, and the defluorination process is completed after standing for 80 min;
step four, taking the clarified supernatant of the condensate subjected to defluorination in the step three, placing the clarified supernatant in a heating tank 5, adjusting the magnetic induction intensity to 0.8T, starting a circulating pump 3 and a heating device 8, setting the temperature of the heating device 8 to 45 ℃, setting the flow rate of waste acid to be 1m/s, controlling the pH to be 12.8-13, and adding Ca (OH) according to the molar ratio of calcium to aluminum to chlorine of 10.5:4.5:12And NaAlO2And the dechlorination process is finished after the reaction time is 70 min.
In the embodiment, after the defluorination process is finished, the supernatant of the condensate is measured, wherein the concentration of fluorine ions is 4.5mg/L, the removal rate is more than 99 percent, and the national standard is met; after the dechlorination process is finished, standing the condensate for a period of time until the supernatant is clear, taking part of the supernatant to measure the chloride ion concentration to be 3.6mg/L, wherein the removal rate reaches more than 99 percent and meets the national standard.
Claims (9)
1. The utility model provides a strengthen device that sour evaporative concentration of copper smelting removed fluorine and chlorine, includes the evaporative concentration device, the evaporative concentration device includes heating bath, heating device, condensing equipment and collection device, its characterized in that: the circulating device comprises a valve (1), a flowmeter (2), a circulating pump (3), a magnet (4) and a pipeline (7), wherein the valve (1), the flowmeter (2), the circulating pump (3) and the magnet (4) are connected in series on the pipeline (7), connectors (6) are arranged at two ends of a heating groove (5), and the heating groove (5) is connected with the pipeline (7) through the connectors (6) to form a circulating loop; the number of the magnets (4) is at least two, and the directions of the magnetic fields are alternately distributed upwards and downwards.
2. The device for strengthening the evaporation concentration and fluorine and chlorine removal of the copper smelting waste acid according to claim 1, characterized in that: the interface (6) is positioned in the middle or the upper part of the two ends of the heating groove (5).
3. A method for strengthening the fluorine and chlorine removal by evaporation concentration of copper smelting waste acid, which utilizes the device for strengthening the fluorine and chlorine removal by evaporation concentration of copper smelting waste acid as claimed in claim 1 or 2, and comprises the following steps:
firstly, pouring waste acid into a heating tank (5), setting the magnetic induction intensity of a magnet (4) to be 1-3T, starting a circulating pump (3) and a heating device (8), setting the flow rate of the waste acid through a valve (1) and a flowmeter (2), carrying out evaporation concentration, and recycling evaporated gas to a collecting device (10) through a condensing device (9) to form condensate;
step two, after the waste acid is evaporated, removing crystals so as to recover other valuable elements in the next step;
step three, pouring the condensate recovered in the step one back to a heating tank (5), adjusting the magnetic induction intensity to 0.2-0.8T, starting a circulating pump (3) and a heating device (8), setting the flow rate of the waste acid, controlling the pH to be 11-12, and adding CaO and Ca (OH)2And CaCl2And closing after reacting for 20-30 minClosing the circulating pump (3) and the heating device (8), standing for 50-80 min, and finishing the defluorination process;
step four, taking the clarified supernatant of the condensate subjected to fluorine removal in the step three, placing the clarified supernatant in a heating tank (5), adjusting the magnetic induction intensity to 0.2-0.8T, starting a circulating pump (3) and a heating device (8), setting the flow rate of the waste acid, controlling the pH to be 12.8-13, and adding Ca (OH)2And NaAlO2And completing the dechlorination process after reacting for 50-70 min.
4. The method for removing fluorine and chlorine by enhancing copper smelting waste acid evaporation concentration according to claim 3, characterized by comprising the following steps: in the first step, the third step and the fourth step, the flow velocity of the waste acid is 0.2-1 m/s.
5. The method for removing fluorine and chlorine by enhancing copper smelting waste acid evaporation concentration according to claim 4, characterized by comprising the following steps: in the first step, the evaporation concentration multiple is 6-7 times.
6. The method for removing fluorine and chlorine by enhancing copper smelting waste acid evaporation concentration according to claim 5, characterized by comprising the following steps: in the first step, the temperature of the heating device (8) is 120-140 ℃.
7. The method for removing fluorine and chlorine by enhancing copper smelting waste acid evaporation concentration according to claim 6, characterized by comprising the following steps: in the third step, the temperature of the heating device (8) is 120-140 ℃, and CaO and Ca (OH) are added2And CaCl2The molar ratio of total calcium in the copper smelting waste acid to fluorine in the copper smelting waste acid is 1.2-1.5: 1.
8. The method for removing fluorine and chlorine by enhancing copper smelting waste acid evaporation concentration according to claim 7, characterized by comprising the following steps: in the fourth step, the temperature of the heating device (8) is 35-45 ℃, and Ca (OH) is added2And NaAlO2The molar ratio of calcium to aluminum to chlorine in the copper smelting waste acid is 10-10.5: 4-4.5: 1.
9. The method for removing fluorine and chlorine by enhancing copper smelting waste acid evaporation concentration according to claim 8, characterized by comprising the following steps: in the first step, the magnetic induction is 2T, and in the third step and the fourth step, the magnetic induction is 0.5T.
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Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105439356A (en) * | 2015-12-28 | 2016-03-30 | 中南大学 | Method and device for synchronously recycling sulfuric acid and fluorine and chlorine from polluted acid |
| CN105776703A (en) * | 2016-04-08 | 2016-07-20 | 南通三圣石墨设备科技股份有限公司 | Method for processing smelting waste acid |
| CN206089139U (en) * | 2016-10-17 | 2017-04-12 | 苏州宁红健康科技有限公司 | Multistage multichannel circulation water magnetizing device |
| CN107555698A (en) * | 2017-10-26 | 2018-01-09 | 上海辨洁环保科技有限公司 | Flash evaporator system and method for high concentration concentrate |
-
2018
- 2018-05-31 CN CN201810547746.2A patent/CN108862807B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105439356A (en) * | 2015-12-28 | 2016-03-30 | 中南大学 | Method and device for synchronously recycling sulfuric acid and fluorine and chlorine from polluted acid |
| CN105776703A (en) * | 2016-04-08 | 2016-07-20 | 南通三圣石墨设备科技股份有限公司 | Method for processing smelting waste acid |
| CN206089139U (en) * | 2016-10-17 | 2017-04-12 | 苏州宁红健康科技有限公司 | Multistage multichannel circulation water magnetizing device |
| CN107555698A (en) * | 2017-10-26 | 2018-01-09 | 上海辨洁环保科技有限公司 | Flash evaporator system and method for high concentration concentrate |
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