CN115180748A - Waste acid treatment method - Google Patents
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- CN115180748A CN115180748A CN202211010316.XA CN202211010316A CN115180748A CN 115180748 A CN115180748 A CN 115180748A CN 202211010316 A CN202211010316 A CN 202211010316A CN 115180748 A CN115180748 A CN 115180748A
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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
- C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
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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
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/5236—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents
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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
- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
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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
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/722—Oxidation by peroxides
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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
- C02F2001/007—Processes including a sedimentation step
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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
- C02F2101/103—Arsenic 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
- C02F2101/20—Heavy metals or heavy metal 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
- C02F2301/00—General aspects of water treatment
- C02F2301/08—Multistage treatments, e.g. repetition of the same process step under different conditions
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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
- C02F2305/00—Use of specific compounds during water treatment
- C02F2305/02—Specific form of oxidant
- C02F2305/026—Fenton's reagent
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Abstract
The invention discloses a waste acid treatment method, which comprises the following steps: 1) A first neutralization section: the waste acid water is sent to a section of neutralizing tank, caCO is added 3 Adjusting the pH value to 2.0-3.0, and performing first-stage filter pressing; 2) A second-stage neutralization stage: sending the filtrate into a second-stage neutralizing tank, adding ferrous sulfate and hydrogen peroxide for reaction, adding lime and a flocculating agent for regulating the pH value to be 6-8, automatically flowing to a third-stage thickener after reacting for a period of time, carrying out second-stage filter pressing on the underflow, returning the filtrate to the third-stage thickener, and overflowing the supernatant to the third-stage neutralizing tank; 3) Three-stage neutralization stage: adding lime to adjust the pH value to 11-12, sending to a four-section thickener, carrying out three-section filter pressing on the bottom flow, returning the filtrate to the four-section thickener, and overflowing the supernatant to a four-section neutralizing tank; 4) Four-stage neutralization stage: adding sodium sulfide and auxiliary thallium-removing agent, adjusting pH to 11-12, feeding into five-stage thickener, performing four-stage filter pressing on the bottom flow, and returning the filtrate to five-stage thickenerAnd (4) treating the supernatant to deep water. The method reduces the lime consumption, lowers the waste acid treatment cost and reduces the yield of the environment-friendly slag.
Description
Technical Field
The invention relates to the technical field of waste acid treatment, in particular to a waste acid treatment method.
Background
At present, the non-ferrous metal smelting process in China is mainly a pyrometallurgical process, non-ferrous metal ores mostly exist in a sulfide form, and a large amount of smelting flue gas containing high-concentration sulfur oxides (including sulfur dioxide and sulfur trioxide) and heavy metals is generated in the smelting process. Since wet scrubbing is an important component in the flue gas purification process of nonferrous metal metallurgy, a large amount of scrubbing wastewater containing sulfuric acid and heavy metals is inevitably generated, and the wastewater is often called 'waste acid' in the nonferrous metal metallurgy industry. The waste acid water has high acidity and contains heavy metal ions and sulfate ions, and the like, so the difficulty is high in the actual treatment process.
The common treatment method of the waste acid mainly comprises a physical method and a chemical method. The physical method recovers sulfuric acid and heavy metal with certain concentration by dialysis, osmosis and other treatment means, but has limited treatment capacity and higher energy consumption, and the defects restrict the wide application of the method. The most common of the chemical processes are the sulfidation and lime neutralization processes, such as: the patent CN102115270A discloses a waste acid treatment method for producing acid from metal smelting flue gas, which adopts a sulphite-lime neutralization method to treat waste acid produced by producing acid from metal smelting flue gas, and comprises the steps of vulcanization and neutralization, wherein a neutralizer used in the neutralization step is carbide mud neutralizer slurry prepared from carbide mud. CN103723873A discloses a method for treating waste acid in acid preparation from smelting flue gas, which comprises the following steps: lime is firstly added into polluted acid to neutralize until ph is 2~3, impurities such as calcium sulfate are precipitated, the impurities such as calcium sulfate are filtered, sodium hydroxide is added into filtrate to adjust the ph to 6~7, then 0.5-1 per mill fenton reagent is added, and then microwave radiation is carried out for 25 seconds, the microwave frequency is 915 Mm, and the power is 1 kilowatt. Then filtering once again, adding sodium hydroxide into the obtained filtrate to adjust the pH to 9-9.5, adding 0.5-1 per mill of flocculating agent polyacrylamide, and then performing microwave radiation for 25 seconds, wherein the microwave frequency is 915 million and the power is 1 kilowatt. And discharging the liquid after precipitation to reach the discharge standard. The method adopts the steps of adding carbide slag (taking CaO as a main component) or lime into the heavy metal wastewater to neutralize the contaminated acid, and simultaneously generating insoluble heavy metal hydroxide precipitate and separating by utilizing the reaction of heavy metal ions and hydroxyl ions. The method has the advantages of simple process, cheap raw materials and the like. But has the defects of low processing speed, low lime utilization rate and the like.
The patent application number CN201811307802.1 discloses a method for removing thallium from waste acid water containing high halogen, aiming at waste acid water containing high fluorine, high arsenic and high thallium, calcium carbonate is adopted for defluorination treatment, two sections of oxidation are carried out for arsenic removal after filter pressing, and finally, thallium removal by vulcanization is carried out, so that the waste acid water reaches the standard after treatment. The method can lead the complex waste acid wastewater to reach the standard, but has the defects of long process flow, difficult parameter control, large amount of environment-friendly slag and the like.
Therefore, a new waste acid treatment method is needed to solve the problems of low utilization rate of lime and environment-friendly slag yield in the waste acid treatment process.
Disclosure of Invention
The technical problem to be solved by the invention is as follows: overcomes the defects of the prior art, and provides a waste acid treatment method which has simple process flow, high lime utilization rate and low environmental-friendly slag yield.
The technical scheme adopted by the invention for solving the technical problems is as follows: a waste acid treatment method comprises the following steps:
1) A first neutralization section: the waste acid water is sent into a section of neutralization tank, caCO is added into the section of neutralization tank 3 Adjusting the pH value to 2.0-3.0, having the best arsenic reduction effect within the pH value, and then carrying out first-stage filter pressing;
2) A second-stage neutralization stage: sending the filtrate obtained by the first-stage filter pressing into a second-stage neutralizing tank, adding ferrous sulfate and hydrogen peroxide into the second-stage neutralizing tank for reaction, then adding lime and a flocculating agent to adjust the pH value to 6-8, automatically flowing the solution to a three-stage thickener after reacting for a period of time, overflowing the supernatant to the third-stage neutralizing tank, carrying out second-stage filter pressing on the underflow, returning the filtrate obtained by the second-stage filter pressing to the three-stage thickener, and overflowing the supernatant to the third-stage neutralizing tank;
3) Three-stage neutralization stage: adding ferrous sulfate, hydrogen peroxide and lime into the three-section neutralizing tank to adjust the pH value to 11-12, then pumping to a four-section thickener, overflowing supernatant to the four-section neutralizing tank, carrying out three-section filter pressing on underflow, returning filtrate obtained by the three-section filter pressing to the four-section thickener, and overflowing the supernatant to the four-section neutralizing tank;
4) Four-stage neutralization stage: and adding sodium sulfide and an auxiliary thallium removal agent into the four-section neutralizing tank, adjusting the pH value to 11-12, then pumping to a five-section thickener, carrying out four-section filter pressing on the bottom flow obtained after treatment by the five-section thickener, returning the filtrate to the five-section thickener, and collecting the supernatant obtained after treatment by the five-section thickener to carry out deep water treatment. The waste acid treatment method is divided into four sections, wherein the first section neutralization section mainly adopts CaCO 3 Neutralizing to reduce acidity, and returning the produced neutralized slag to a lead system for batching; the second-stage neutralization section mainly adopts Fenton oxidation and combines a lime milk neutralization method to remove heavy metal ions and most arsenic, and simultaneously, a flocculating agent is added to achieve the effects of flocculating and slag reducing and also remove F ions in the waste acid water; the three-section neutralization section is mainly used for deeply removing arsenic, and the Fenton oxidation method is adopted, so that the step of acid addition and callback is reduced, and the output of slag quantity is reduced; and the four-section neutralization section adopts sodium sulfide and an auxiliary thallium removal agent to remove residual thallium through vulcanization. The method has short process flowThe method not only greatly reduces the using amount of lime and sulfuric acid and reduces the treatment cost of waste acid, but also greatly reduces the yield of environment-friendly slag and lightens the labor intensity.
Further, the pH value of the waste acid and wastewater is 0.5-1.5.
Further, caCO in the step 1) 3 The dosage of the compound is 3 to 5 kg/ton of contaminated acid.
Further, the dosage of the ferrous sulfate in the step 2) is 1 kg/ton of waste acid, and the dosage of the hydrogen peroxide is 2L/ton of waste acid.
Further, the reaction time after adding the ferrous sulfate and the hydrogen peroxide in the step 2) is 40 minutes.
Further, the dosage of the lime in the step 2) is about 8-10kg/ton of contaminated acid. The dosage of the flocculating agent is 0.005 to 0.01kg/ton of waste acid, and the reaction time after the lime and the flocculating agent are added in the step is 30 minutes.
Further, the flocculant is polyaluminium chloride.
Further, the dosage of the lime in the step 3) is about 3 kg/ton of waste acid.
Further, the dosage of the sodium sulfide in the step 4) is 0.3 to 0.4kg/m 3 And the dosage of the auxiliary thallium removal agent is 0.2 kg/ton of contaminated acid, and the reaction time is 40 minutes.
The method for treating the waste acid has the beneficial effects that: the waste acid treatment method is divided into four sections, wherein the first section neutralization section mainly adopts CaCO 3 Neutralizing to reduce acidity, and returning the produced neutralized slag to a lead system for batching; the second-stage neutralization section mainly adopts Fenton oxidation and combines a lime milk neutralization method to remove heavy metal ions and most arsenic; the three-section neutralization section is mainly used for deeply removing arsenic, and the Fenton oxidation method is adopted, so that the step of acid addition and callback is reduced, and the output of slag quantity is reduced; and in the fourth neutralizing stage, sodium sulfide and an auxiliary thallium removing agent are adopted to remove residual thallium through vulcanization. The method has short process flow, not only greatly reduces the use amount of lime and sulfuric acid and reduces the treatment cost of waste acid, but also greatly reduces the yield of environment-friendly slag and lightens the labor intensity.
Drawings
FIG. 1 is a process flow diagram of a waste acid treatment method of the present invention.
Detailed Description
The invention is further illustrated with reference to the following figures and examples, which are not intended to limit the scope of the invention in any way.
Example 1
A method for treating contaminated acid comprises the following steps of treating 7070 tons of contaminated acid wastewater with pH of 0.5-1.5 by the method, wherein a process flow diagram is shown in figure 1:
1) A first neutralization section: sending the waste acid water with pH of 0.5-1.5 into a first-stage neutralization tank, and adding CaCO into the first-stage neutralization tank 3 Adjusting pH to 2.0-3.0, and performing first stage filter pressing with CaCO 3 The addition amount of (A) is 28.5 tons;
2) A second-stage neutralization stage: sending the filtrate obtained by the first-stage filtration into a second-stage neutralization tank, and adding ferrous sulfate and hydrogen peroxide into the second-stage neutralization tank for reaction, wherein the dosages of the ferrous sulfate and the hydrogen peroxide are respectively 7.0 tons and 14m 3 The reaction time is 40 minutes, then lime and polyaluminium chloride are added to adjust the pH value to 6-8, the using amounts of the lime and the flocculating agent are respectively 72.5 tons and 56kg, the mixture flows to a three-section thickener after reacting for 30 minutes, the supernatant fluid overflows to a three-section neutralizing tank, the underflow is subjected to second-section filter pressing, the filtrate obtained by the second-section filter pressing is returned to the three-section thickener, and the supernatant fluid overflows to the three-section neutralizing tank;
3) Three-stage neutralization stage: adding ferrous sulfate, hydrogen peroxide and lime into the three-stage neutralization tank to adjust the pH value to 11-12, wherein the using amount of the lime is 13 tons, and the using amounts of the ferrous sulfate and the hydrogen peroxide are 7.0 tons and 14m respectively 3 Then, the supernatant fluid overflows to a four-section neutralizing tank by using a pump, the underflow carries out three-section filter pressing, the filtrate obtained by the three-section filter pressing returns to the four-section thickener, and the supernatant fluid overflows to the four-section neutralizing tank;
4) Four-stage neutralization stage: adding sodium sulfide and an auxiliary thallium removal agent into the four-section neutralization tank, adjusting the pH to 11-12, wherein the use amounts of the sodium sulfide and the auxiliary thallium removal agent are 2.1 tons and 1.4 tons respectively, then pumping the sodium sulfide and the auxiliary thallium removal agent to a five-section thickener, carrying out four-section filter pressing on the bottom flow obtained after treatment by the five-section thickener, returning the filtrate to the five-section thickener, collecting the supernatant obtained after treatment by the five-section thickener to carry out deep water treatment, and enabling the obtained supernatant to accord with the discharge standard of discharge standards of lead and zinc industrial pollutants (GB 25466-2010).
Example 2
A waste acid treatment method is adopted to treat 6800 tons of waste acid wastewater with pH of 0.5-1.5 monthly, and the process flow chart is shown in figure 1, and the method specifically comprises the following steps:
1) A first neutralization section: sending the waste acid water with pH of 0.5-1.5 into a first-stage neutralization tank, and adding CaCO into the first-stage neutralization tank 3 Adjusting pH to 2.0-3.0, and performing first stage filter pressing with CaCO 3 The addition amount of (A) is 27.4 tons;
2) A second-stage neutralization stage: sending the filtrate obtained by the first-stage filtration into a second-stage neutralization tank, and adding ferrous sulfate and hydrogen peroxide into the second-stage neutralization tank for reaction, wherein the dosages of the ferrous sulfate and the hydrogen peroxide are respectively 6.73 tons and 13.5m 3 The reaction time is 40 minutes, then lime and polyaluminium chloride are added to adjust the pH value to 6-8, the using amounts of the lime and the flocculant are respectively 70.5 tons and 54kg, the mixture flows to a three-section thickener automatically after reacting for 30 minutes, supernatant fluid overflows to a three-section neutralizing tank, underflow is subjected to second-section filter pressing, filtrate obtained by the second-section filter pressing is returned to the three-section thickener, and supernatant fluid overflows to the three-section neutralizing tank;
3) Three-stage neutralization stage: adding ferrous sulfate, hydrogen peroxide and lime into the three-section neutralizing tank to adjust the pH value to 11-12, wherein the using amount of the lime is 12 tons, then pumping the lime to a four-section thickener, overflowing supernatant to the four-section neutralizing tank, carrying out three-section filter pressing on underflow, returning filtrate obtained by the three-section filter pressing to the four-section thickener, and overflowing the supernatant to the four-section neutralizing tank;
4) Four-stage neutralization stage: adding sodium sulfide and an auxiliary thallium removal agent into the four-section neutralization tank, adjusting the pH to 11-12, wherein the use amounts of the sodium sulfide and the auxiliary thallium removal agent are 2.0 tons and 1.3 tons respectively, then pumping the solution to a five-section thickener, carrying out four-section pressure filtration on the bottom flow obtained after treatment by the five-section thickener, returning the filtrate to the five-section thickener, collecting the supernatant obtained after treatment by the five-section thickener to carry out deep water treatment, and obtaining the supernatant compared with the comparative example 1
The comparative example adopts the method of CN102115270A to treat 7070 tons of waste acid and waste water with pH of 0.5-1.5.
Comparative example 2
The comparative example adopts the method of CN102115270A to treat 7070 tons of waste acid and waste water with pH of 0.5-1.5.
Comparative example 3
The comparative example adopts the method of CN201811307802.1 to treat 7070 tons of waste acid and waste water with pH of 0.5-1.5.
The results of the present invention, which were measured on the total weight of the eco-friendly sludge (filter residue after each filtration) obtained after the contaminated acid wastewater was treated by the methods of examples 1 to 2 and comparative examples 1 to 3, and the amount of lime used in the treatment of the contaminated acid wastewater, are shown in the following table:
from the above table, compared with example 1, the weight of the lime used when the method of comparative examples 1 to 3 is used for treating the waste acid wastewater with the same weight and pH as those in example 1 is significantly lower than that in example 1, and the amount of the produced environment-friendly slag is also significantly lower than that in example 1, which shows that the method for treating the waste acid not only can greatly reduce the use amount of the lime, reduce the cost of waste acid treatment, but also greatly reduce the output of the environment-friendly slag.
It should be further noted that the terms "one section," "two section," "three section," "four section," and the like are used herein to describe various steps, but these steps should not be limited by these terms. These terms are only used to distinguish one element from another.
Although the present invention has been described with reference to the preferred embodiments, it will be understood by those skilled in the art that various changes may be made and equivalents may be substituted for elements thereof without departing from the scope of the present invention.
Claims (9)
1. A waste acid treatment method is characterized in that: the method comprises the following steps:
1) A first neutralization section: the waste acid water is sent into a section of neutralization tank, caCO is added into the section of neutralization tank 3 Adjusting the pH value to 2.0-3.0, and then carrying out first-stage filter pressing;
2) A second-stage neutralization stage: sending the filtrate obtained by the first-stage filter pressing into a second-stage neutralizing tank, adding ferrous sulfate and hydrogen peroxide into the second-stage neutralizing tank for reaction, then adding lime and a flocculating agent to adjust the pH value to 6-8, automatically flowing to a third-stage thickener after reacting for a period of time, overflowing the supernatant into the third-stage neutralizing tank, carrying out second-stage filter pressing on the underflow, returning the filtrate obtained by the second-stage filter pressing to the third-stage thickener, and overflowing the supernatant into the third-stage neutralizing tank;
3) Three-stage neutralization stage: adding ferrous sulfate, hydrogen peroxide and lime into the three-section neutralizing tank to adjust the pH value to 11-12, then pumping to a four-section thickener, overflowing supernatant to the four-section neutralizing tank, carrying out three-section filter pressing on underflow, returning filtrate obtained by the three-section filter pressing to the four-section thickener, and overflowing the supernatant to the four-section neutralizing tank;
4) Four-stage neutralization stage: and adding sodium sulfide and an auxiliary thallium removal agent into the four-section neutralizing tank, adjusting the pH value to 11-12, then pumping to a five-section thickener, carrying out four-section filter pressing on the bottom flow obtained after treatment by the five-section thickener, returning the filtrate to the five-section thickener, and collecting the supernatant obtained after treatment by the five-section thickener to carry out deep water treatment.
2. The waste acid treatment method according to claim 1, characterized in that: the pH value of the waste acid and wastewater is 0.5-1.5.
3. The waste acid treatment method according to claim 1, characterized in that: caCO in the step 1) 3 The dosage of the compound is 3 to 5 kg/ton of contaminated acid.
4. The waste acid treatment method according to claim 1, characterized in that: the dosage of the ferrous sulfate in the step 2) is 1 kg/ton of waste acid, and the dosage of the hydrogen peroxide is 2L/ton of waste acid.
5. The waste acid treatment method according to claim 4, characterized in that: the reaction time after adding the ferrous sulfate and the hydrogen peroxide in the step 2) is 40 minutes.
6. The waste acid treatment method according to claim 1, characterized in that: the dosage of lime in the step 2) is about 8 to 10kg/ton of contaminated acid;
the dosage of the flocculating agent is 0.005 to 0.01kg/ton of waste acid, and the reaction time after the lime and the flocculating agent are added in the step is 30 minutes.
7. The waste acid treatment method according to claim 6, wherein: the flocculant is polyaluminium chloride.
8. The waste acid treatment method according to claim 1, characterized in that: the dosage of the lime in the step 3) is about 3 kg/ton of waste acid.
9. The waste acid treatment method according to claim 1, characterized in that: the dosage of the sodium sulfide in the step 4) is 0.3 to 0.4kg/m 3 And the dosage of the auxiliary thallium removal agent is 0.2 kg/ton of contaminated acid, and the reaction time is 40 minutes.
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Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4571264A (en) * | 1984-09-27 | 1986-02-18 | Sherritt Gordon Mines Limited | Recovery of gold from refractory auriferous iron-containing sulphidic ore |
| CN103121763A (en) * | 2012-11-30 | 2013-05-29 | 中南民族大学 | Process for treating high-arsenic and high cadmium waste acid by using three-stage lime-ferric salt method |
| CN113264603A (en) * | 2020-10-27 | 2021-08-17 | 水口山有色金属有限责任公司 | Method for treating acid wastewater with high arsenic and thallium contents in sulfuric acid |
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- 2022-08-23 CN CN202211010316.XA patent/CN115180748A/en active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4571264A (en) * | 1984-09-27 | 1986-02-18 | Sherritt Gordon Mines Limited | Recovery of gold from refractory auriferous iron-containing sulphidic ore |
| CN103121763A (en) * | 2012-11-30 | 2013-05-29 | 中南民族大学 | Process for treating high-arsenic and high cadmium waste acid by using three-stage lime-ferric salt method |
| CN113264603A (en) * | 2020-10-27 | 2021-08-17 | 水口山有色金属有限责任公司 | Method for treating acid wastewater with high arsenic and thallium contents in sulfuric acid |
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