CN113979574A - Waste water treatment method - Google Patents
Waste water treatment method Download PDFInfo
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- CN113979574A CN113979574A CN202111164303.3A CN202111164303A CN113979574A CN 113979574 A CN113979574 A CN 113979574A CN 202111164303 A CN202111164303 A CN 202111164303A CN 113979574 A CN113979574 A CN 113979574A
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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
- C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
- C02F1/461—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis
- C02F1/463—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis by electrocoagulation
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- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/24—Treatment of water, waste water, or sewage by flotation
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
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- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
- C02F1/461—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis
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- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
- C02F1/461—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis
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- C—CHEMISTRY; METALLURGY
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- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
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Abstract
The application relates to the technical field of wastewater treatment, and provides a wastewater treatment method, which comprises the following steps: performing electric flocculation treatment on the wastewater to obtain primary purified water; and (3) preparing the primary purified water and the raw ore into ore pulp, and performing flotation treatment on the ore pulp to obtain a flotation product and flotation water. According to the flotation method provided by the application, on one hand, the COD value of the wastewater is reduced by performing electric flocculation treatment on the wastewater to obtain flotation water, and the flotation water and the raw ore are prepared into slurry for flotation treatment, so that the aim of reasonably utilizing the wastewater is achieved, and a path is provided for utilizing the wastewater.
Description
Technical Field
The application belongs to the technical field of wastewater treatment, and particularly relates to a wastewater treatment method.
Background
Lead and zinc in lead-zinc ores mainly exist in galena and sphalerite, and main process flows are optimized along with the change of ore properties. In the ore dressing process, different flotation reagents are added in different sorting operations in order to effectively sort useful metals. In a high-alkali medium, the collecting capacity of low-dosage ethionine to monomer lead is stronger than that of butyl xanthate, and for a symbiont, the collecting capacity of xanthate is stronger. The main inhibitors used in the lead-zinc ore beneficiation flow comprise lime and sodium humate; the activating agent mainly comprises copper sulfate and sulfuric acid. In addition, the sulfur separation operation also uses a collecting agent of etihuang. The lead-zinc ore dressing plant produces a large amount of dressing wastewater every year, and the dressing reagents are remained in the discharged dressing wastewater. In addition, the wastewater includes a part of suspended matter, various metal ions, decomposed substances of various beneficiation chemicals, and the like. Various organic and inorganic agents remained in the mineral processing wastewater cause higher COD value of the wastewater.
Lime has long been used as a suppressant for pyrite, and when a large amount of lime is added, the system is strongly alkaline, and Ca (OH) is formed on the surface of pyrite2、CaSO4And covering the layer to make the surface hydrophilic. Therefore, for the special high-sulfur lead-zinc ore, such as the lead-zinc ore, the pyrite can be effectively inhibited under the condition of high alkali, and the pH value of the mixed wastewater of the lead-zinc ore is higher because a large amount of lime inhibitors are used in the ore dressing process.
How to treat the beneficiation wastewater is a major problem which needs to be solved by each beneficiation plant, so that how to economically and effectively realize the recycling of the beneficiation wastewater and how to ensure the production index of the beneficiation plants to the greatest extent is very important.
Disclosure of Invention
An object of this application is to provide a waste water treatment takes precautions against, aims at solving the problem that prior art ore dressing waste water recycled.
In order to achieve the purpose of the application, the technical scheme adopted by the application is as follows:
the application provides a wastewater treatment method, which comprises the following steps:
performing electric flocculation treatment on the wastewater to obtain primary purified water;
and preparing the primary purified water and the raw ore into ore pulp, and performing flotation treatment on the ore pulp to obtain a flotation product and the flotation water.
The application provides a flotation method, on the one hand, carry out waste water through the electric flocculation treatment, reduce the COD value of waste water, obtain the primary purification water, and configure primary purification water and raw ore into the thick liquids and carry out the flotation treatment, reached the mesh of rational utilization waste water, for the utilization of waste water provides a way, on the other hand, adopt waste water and the raw ore configuration thick liquids that this application was handled to carry out the flotation treatment, compare with directly carrying out the flotation with waste water, the rate of recovery change of raw ore is high.
Drawings
FIG. 1 an embodiment of the present invention provides an electrocoagulation treatment apparatus;
FIG. 2 shows the flotation results of lead concentrate from different water samples of Van-Kote lead-zinc ores provided in the embodiment of the present invention;
FIG. 3 shows the flotation results of zinc concentrate from different water samples of Van-Korea lead-zinc ore provided in the embodiment of the present invention.
Detailed Description
In order to make the technical problems, technical solutions and advantageous effects to be solved by the present application more clearly apparent, the present application is further described in detail below with reference to the embodiments. It should be understood that the specific embodiments described herein are merely illustrative of the present application and are not intended to limit the present application.
In this application, the term "and/or" describes an association relationship of associated objects, meaning that three relationships may exist, for example, a and/or B, may mean: a is present alone, A and B are present simultaneously, and B is present alone. Wherein A and B can be singular or plural. The character "/" generally indicates that the former and latter associated objects are in an "or" relationship.
In the present application, "at least one" means one or more, "a plurality" means two or more. "at least one of the following" or similar expressions refer to any combination of these items, including any combination of the singular or plural items. For example, "at least one (a), b, or c", or "at least one (a), b, and c", may each represent: a, b, c, a-b (i.e., a and b), a-c, b-c, or a-b-c, wherein a, b, and c may be single or plural, respectively.
It should be understood that, in various embodiments of the present application, the sequence numbers of the above-mentioned processes do not mean the execution sequence, and some or all of the steps may be executed in parallel or executed sequentially, and the execution sequence of each process should be determined by its function and inherent logic, and should not constitute any limitation to the implementation process of the embodiments of the present application.
The terminology used in the embodiments of the present application is for the purpose of describing particular embodiments only and is not intended to be limiting of the application. As used in the examples of this application and the appended claims, the singular forms "a", "an", and "the" are intended to include the plural forms as well, unless the context clearly indicates otherwise.
The weight of the related components mentioned in the description of the embodiments of the present application may not only refer to the specific content of each component, but also represent the proportional relationship of the weight among the components, and therefore, the content of the related components is scaled up or down within the scope disclosed in the description of the embodiments of the present application as long as it is scaled up or down according to the description of the embodiments of the present application. Specifically, the mass described in the specification of the embodiments of the present application may be a mass unit known in the chemical industry field such as μ g, mg, g, kg, etc.
The terms "first" and "second" are used for descriptive purposes only and are used for distinguishing purposes such as substances from one another, and are not to be construed as indicating or implying relative importance or implying any number of technical features indicated. For example, a first XX may also be referred to as a second XX, and similarly, a second XX may also be referred to as a first XX, without departing from the scope of embodiments of the present application. Thus, features defined as "first" and "second" may explicitly or implicitly include one or more of the features.
The embodiment of the application provides a wastewater treatment method, which comprises the following steps:
s1, a wastewater treatment step, namely performing electric flocculation treatment on the wastewater to obtain primary purified water;
s2, a flotation treatment step, namely preparing the COD value reduced water and the raw ore into ore pulp, and carrying out flotation treatment on the ore pulp to obtain a flotation product and flotation water.
The flotation method provided by the embodiment of the application adopts an electric flocculation method to carry out primary purification treatment on wastewater, reduces the COD value of the wastewater, obtains primary purified water, and configures the primary purified water and raw ore into slurry to carry out flotation treatment on the slurry, thereby achieving the purpose of reasonably utilizing the wastewater, and providing a way for utilizing the wastewater.
In the step of S1 wastewater treatment, the wastewater includes flotation wastewater, industrial wastewater and domestic wastewater, wherein the flotation wastewater includes a flotation reagent, the flotation reagent includes at least one of a capture agent, an alkaline agent, an inhibitor and a foaming agent, and the flotation reagent includes at least one of butyl xanthate, ethionine, copper sulfate, sulfuric acid, lime, sodium humate, 2# oil and ethidium xanthate.
In some embodiments, researchers have conducted research on the plumbum-zincium ore wastewater, wherein the research shows that the plumbum-zincium ore wastewater accounts for about 70% of the total water amount, the wastewater is lead-zinc separation mixed wastewater, the properties of the mixed beneficiation wastewater are mainly determined by the wastewater, and the pH value and the COD value of the mixed beneficiation wastewater are relatively close to those of the wastewater. The mixed wastewater of lead-zinc ore is high pH value wastewaterThe pH value is above 11.8, and the COD value is about 425mg.L-1In addition, the chemical composition of the mixed wastewater of lead-zinc ore is as follows: na (Na)>53.231mg.L-1K is 26.131mg.L-1，Ca>13.738mg.L-1，S>104.857mg.L-1Ba is 0.124mg.L-1And the Mg content is 6.197mg.L-1Sr is 1.062mg.L-1Li of 0.055mg.L-1Pb 7.662mg.L-1After the wastewater treatment and flotation method of the embodiment of the application is adopted, compared with the flotation treatment directly adopting mixed wastewater of Van's lead-zinc ore, the flotation recovery rate of the raw ore is higher.
In some embodiments, in order to further reduce the COD value of the wastewater, in the step of the electrocoagulation treatment, the anode plate comprises one of Fe electrode and Al electrode, and the cathode plate is stainless steel, and the wastewater can be treated.
In some embodiments, the anode plate comprises one of an Fe electrode and an Al electrode, wherein the Fe electrode has a better wastewater treatment effect than the Al electrode.
Furthermore, the negative plate is made of stainless steel, the pH value is 7.1, and the current density is 13.74mA/cm2And under the condition of 50min of electrolysis, the anode plate comprises one of an Fe electrode and an Al electrode, wherein the wastewater treatment effect is better than that of the Al electrode when the Fe electrode is used, and the wastewater treatment effect is better.
In some embodiments, in order to further reduce the COD value of the wastewater, the electrode plate spacing in the step of the electrocoagulation treatment is 10-20 mm, the wastewater can be treated, and the smaller the electrode plate spacing is, the smaller the required electrolysis voltage is, and the lower the energy consumption is, but the COD removal rate is relatively low.
In some embodiments, the plate spacing is 10mm, 20 mm.
Furthermore, the anode plate is Fe, the cathode plate is stainless steel, and the current density is 19.23mA/cm2The wastewater treatment effect is better than that of the polar plate spacing of 10mm when the polar plate spacing of 20mm is under the conditions that the pH value is 8.5 and the electrolysis time is 70 min.
In some embodiments, to further reduce the COD value of the wastewater, in the electrocoagulation treatment stepResearch results show that the current density is 8.24-24.73 mA/cm2The electrolytic voltage is 10-35V, and the wastewater can be treated.
Furthermore, under the conditions that the anode plate is an Fe electrode, the cathode plate is stainless steel, the experimental pH value is 7.1, and the electrolysis time is 50min, the current density can be 8.24mA/cm2、10.99mA/cm2、16.48 mA/cm2、19.23mA/cm2、24.73mA/cm2And 30.22mA/cm2Wherein, the COD removing effect is gradually enhanced along with the increase of the current density, and when the current density is 8.24mA/cm2When the current density was increased to 19.23mA/cm, the COD removal rate was only 49.41%2In this case, the COD removal rate was increased to 73.1%.
In some embodiments, in order to further reduce the COD value of the wastewater, before the electrocoagulation treatment, the method further comprises the step of adding a pH reagent into the wastewater, and adjusting the pH value of the wastewater to 3-11.
Furthermore, the anode plate is Fe electrode, the cathode plate is stainless steel, and the current density is 19.23mA/cm2And the pH value of the wastewater can be 3.0, 5.0, 7.0, 9.0 and 11.0 under the condition of electrolysis time of 50 min. The electrocoagulation method has good treatment effect on the mixed wastewater of the lead-zinc ore in a wider pH value range (3.0 to 9.0), wherein the COD removal rate is about 74.0 percent in the pH value range, and the electrocoagulation effect is approximate; when the electrolysis pH continued to rise to 11.0, there was a significant decrease in COD removal, at which point the COD removal was 71.08%. Therefore, the electric flocculation method for treating the mineral processing wastewater of the minite needs to use acid (5 percent sulfuric acid is adopted in the experiment) to adjust the pH value to 9.0 or below.
In some embodiments, before the step of electrocoagulation, the step of adding activated carbon to the wastewater is further included, and the concentration of the activated carbon in the wastewater is 0.59-6.47 g.L-1。
Furthermore, the anode plate is Fe electrode, the cathode plate is stainless steel, and the current density is 19.23mA/cm2pH value of 8.5 during electrolysisThe addition amount of active carbon can be 0.1g, 0.3g, 0.5g, 0.7g, 0.9g, 1.1g under the condition of interval of 70min and electrode plate interval of 20 mm. The effect of singly using the active carbon on treating the wastewater is not good, and the adding amount of the active carbon is from 0.59g.L-1Gradually increased to 6.47g.L-1The COD removal rate is only about 20 percent. When activated carbon is added in the electric flocculation process, the COD removal rate can be further improved, and when the adding amount of the activated carbon is 5.29g.L-1When the COD removal rate reaches 85.11%, the COD value of the wastewater treated under the condition is 63.3mg.L-1。
In some embodiments, the step of electroflocculation treatment is preceded by the addition of H to the wastewater2O2And said H is2O2The concentration of the wastewater is 600-938.85 mg.L-1H is added in the electric flocculation process2O2Can improve the removal rate of COD.
Furthermore, the anode plate is Fe electrode, the cathode plate is stainless steel, and the current density is 19.23mA/cm2Adding H under the conditions of pH value of 3.0, electrolysis time of 70min and electrode plate spacing of 20mm2O2The dosage can be 187.77mg.L-1、375.54mg.L-1、563.31mg.L-1、751.08mg.L-1And 938.85mg.L-1And H is added in the electric flocculation process2O2Has great influence on the removal rate of COD when H2O2The addition amount is less than 500mg.L-1The removal rate of COD is dependent on H2O2The increase of the dosage is in a descending trend; continuously increasing H2O2The dosage and the COD removal rate are in a rapid rising trend when H is2O2The addition amount is 938.85mg.L-1When the COD removal rate is 84.47%, the COD value of the treated wastewater is 66.7mg.L-1. From the effect of the electrocoagulation treatment, it can be seen that the muddy water boundary after the standing sedimentation also shows an overall tendency of descending first and then ascending.
In some embodiments, the duration of the electric flocculation treatment is 10-110 min, so that the treatment effect on the wastewater can be improved.
Furthermore, the anode plate is an Fe electrode, and the cathode plate is a cathodeThe polar plate is made of stainless steel and has a current density of 19.23mA/cm2Under the condition of pH value of 8.5, the duration of the electric flocculation treatment can be 10min, 30min, 50min, 70min, 90min and 110 min. When the electrolysis time is gradually increased from 10min to 110min, the COD removal rate is gradually increased along with the increase of the electrolysis time and then becomes stable. When the electrolysis time is 10min, the COD removal rate is only 23.58 percent; when the electrolysis time was increased to 70min, the COD removal rate was increased to 79.62%, and then the electrolysis time was continued to be extended, and the COD removal rate was not greatly changed. The electrolysis time is 70min, and the treatment effect on the wastewater can be improved.
S2 flotation processing step, in the embodiment, the raw ore includes lead-zinc ore, the processed waste water can be prepared into slurry with the lead-zinc ore, and the lead-zinc ore is processed by flotation.
In some embodiments, the raw ore comprises lead-zinc ore, and the water with reduced COD value and the lead-zinc ore are prepared into slurry according to the mass ratio of 8: 2-1: 1.
In some embodiments, the raw ore is crushed and ground to a particle size of less than 0.074 mm.
Further, crushing the raw ore to below-3 mm by using a laboratory conical ball mill
And carrying out grinding fineness test research, wherein the ore dosage is 800 g/time, the coarse grinding time is determined to be 5min 30s, and the granularity of the raw ore after ball milling is less than-0.074 mm.
In the embodiment, the process of treating the ore pulp by flotation comprises the steps of lead roughing, lead concentrating, zinc roughing and zinc concentrating.
In some embodiments, the lead roughing comprises a first lead roughing and a second lead roughing, and the lead concentration comprises a first lead concentrating, a second lead concentrating and a third lead concentrating, and the recovery rate of lead-zinc ore can be improved, wherein the lead roughing and the zinc roughing adopt a 1.5L single-groove flotation machine; the first lead concentration operation of the lead concentration process adopts a 0.75L single-groove flotation machine, and the second lead concentration and the third lead concentration adopt 0.5L single-groove flotation machines; the zinc concentration operation adopts a 0.5L single-groove flotation machine.
The zinc beneficiation comprises a first zinc beneficiation and a second zinc beneficiation.
In an embodiment, the first lead roughing, the second lead roughing, the first lead concentrating, the second lead concentrating, the third lead concentrating, the zinc roughing, the first zinc concentrating, and the second zinc concentrating may respectively include the following steps:
primary lead roughing: mixing the primary purified water and the raw ore to obtain ore pulp, adding No. 2 oil according to the concentration of 25g/t, adding calcium oxide according to the concentration of 6000g/t, adding butyl xanthate and ethidium and nitrogen (the weight ratio is 1:1) according to the concentration of 100g/t into the first slurry, and mixing to obtain first lead coarse slurry and first lead dressing tailings.
And (3) secondary lead roughing: and preparing the first lead tailings into second slurry, adding the butyl xanthate and ethidium and nitrogen (the weight ratio is 1:1) into the second slurry according to the concentration of 10g/t, and mixing to obtain second lead coarse slurry and second lead tailings (K1).
First lead concentration: and adding calcium oxide (lime) into the second lead coarse slurry in a 0.5L single-groove flotation machine according to a concentration of 2000g/t for mixing treatment, adding copper sulfate according to a concentration of 400g/t for mixing treatment, adding xanthate according to a concentration of 20g/t for mixing treatment, adding 2# oil according to a concentration of 15g/t for mixing treatment, and stirring for 6-7 min to obtain first lead concentrate slurry and third middling (N1).
And (3) second lead concentration: in a 0.5L single-groove flotation machine, calcium oxide (lime) is added into the first lead concentrate slurry according to the concentration of 2000g/t for mixing treatment, and a mixture of butyl xanthate and ethyl sulfur nitrogen is added according to the concentration of 20g/t for mixing treatment, so that second lead concentrate slurry and fourth middling (N2) are obtained.
And (3) third lead concentration: and adding calcium oxide (lime) into the second lead concentrate slurry in a 0.5L single-groove flotation machine according to the concentration of 500g/t for mixing treatment, adding DS according to the concentration of 100g/t for mixing treatment, adding a mixture of xanthate and ethidium and nitrogen according to the concentration of 0-5 g/t for mixing treatment, and obtaining third lead concentrate slurry (K-Pb) and fifth middling (N3).
Roughing zinc: preparing a second slurry from lead tailings of a preset grade in a 0.75L single-groove flotation machine, adding calcium oxide (lime) into the second slurry according to a concentration of 2000g/t for mixing treatment, adding butyl xanthate according to a concentration of 100g/t for mixing treatment, and adding No. 2 oil according to a concentration of 15g/t to obtain zinc coarse slurry and zinc tailings.
First zinc concentration: in a 0.5L single-groove flotation machine, calcium oxide (lime) is added into the zinc crude slurry according to the concentration of 100g/t for mixing treatment, and butyl xanthate is added according to the concentration of 30g/t for mixing treatment, so that a first zinc concentrate (N-Zn1) and a sixth middling are obtained.
And (3) second zinc concentration: and preparing the first zinc concentrate ore into third slurry in a 0.5L single-groove flotation machine, adding calcium oxide (lime) into the third slurry according to the concentration of 500g/t, and mixing to obtain a second zinc concentrate ore (K-Zn) and a seventh middling ore (N-Zn 2).
And adding butyl xanthate into the zinc tailings according to the concentration of 25g/t for mixing treatment to obtain eighth middling (X) and zinc tailings (K2).
In some embodiments, the method further comprises step S3 of recycling, returning the flotation water to the electrolytic cell as a part of the wastewater, inserting the two electrode plates into the electrolytic cell under the wastewater level at intervals, setting the voltage of the steady-current power supply, and electrifying to perform the electrocoagulation treatment on the wastewater.
Example 1
The following experimental procedure, please refer to fig. 1, is adopted to perform open-circuit flotation experimental study on the actual ore of the minite by using clean water, wastewater after electric flocculation treatment and mineral processing wastewater without any treatment. The influence of the electrolytic flocculation treatment on the flotation indexes of the lead-zinc ore wastewater is mainly researched. The COD value of the mixed wastewater subjected to the electrocoagulation experiment treatment is 74.6mgL-1The water sample is subjected to a flotation test.
The roughing of the laboratory flotation experimental study adopts a 1.5L single-groove flotation machine; in the lead separation process, a 0.75L single-groove flotation machine is adopted in the first lead separation operation, and a 0.5L single-groove flotation machine is adopted in the second and third separation operations; the zinc fine-selection operation adopts a 0.5L single-groove flotation machine. The test equipment used in the flotation test is shown in table 1 below, and the specific flotation test results are shown in the following test indexes.
TABLE 1 flotation test instrumentation
Fig. 1 provides an electric flocculation treatment device, which comprises a magnetic stirrer 1, two electrode plates 2, an electrolytic tank 3 and a current-stabilizing power supply 4, wherein the two electrode plates 2 are respectively connected with the positive electrode and the negative electrode of the current-stabilizing power supply 4 through leads, the two electrode plates 2 are oppositely arranged under the liquid level in the electrolytic tank 3 in the positive direction, and the electric flocculation method is used for treating the waste water of the lead-zinc ore, and the following experimental conditions are specifically adopted:
an anode plate: fe electrode
A negative plate of the negative plate: stainless steel
Current density: 19.23mA/cm2
pH value: 8.5
Electrolysis time 50min
The COD removal rate of the minium lead-zinc ore wastewater treated by the device is about 73.18 percent.
A laboratory conical ball mill XMQ-phi 240 x 90 is adopted to carry out grinding fineness test research, the ore consumption is 800 g/time, the coarse grinding time is determined to be 5min 30s, and the raw ore with the granularity of-0.074 mm accounts for 83.15% after ball milling.
Primary lead roughing: and mixing the flotation water and the raw ore in a 0.75L single-groove flotation machine to obtain ore pulp, adding No. 2 oil at a concentration of 25g/t, calcium oxide at a concentration of 6000g/t, and butyl xanthate and ethidium nitrate (in a weight ratio of 1:1) at a concentration of 100g/t into the first slurry, and mixing to obtain first lead coarse slurry and first lead tailings.
And (3) secondary lead roughing: and preparing the first lead tailings into second slurry, adding the butyl xanthate and ethidium and nitrogen (the weight ratio is 1:1) into the second slurry according to the concentration of 10g/t, and mixing to obtain second lead coarse slurry and second lead tailings (K1).
First lead concentration: and adding calcium oxide (lime) into the second lead coarse slurry in a 0.5L single-groove flotation machine according to a concentration of 2000g/t for mixing treatment, adding copper sulfate according to a concentration of 400g/t for mixing treatment, adding xanthate according to a concentration of 20g/t for mixing treatment, adding 2# oil according to a concentration of 15g/t for mixing treatment, and stirring for 6-7 min to obtain first lead concentrate slurry and third middling (N1).
And (3) second lead concentration: in a 0.5L single-groove flotation machine, calcium oxide (lime) is added into the first lead concentrate slurry according to the concentration of 2000g/t for mixing treatment, and a mixture of butyl xanthate and ethyl sulfur nitrogen is added according to the concentration of 20g/t for mixing treatment, so that second lead concentrate slurry and fourth middling (N2) are obtained.
And (3) third lead concentration: and adding calcium oxide (lime) into the second lead concentrate slurry in a 0.5L single-groove flotation machine according to the concentration of 500g/t for mixing treatment, adding DS according to the concentration of 100g/t for mixing treatment, adding a mixture of xanthate and ethidium and nitrogen according to the concentration of 0-5 g/t for mixing treatment, and obtaining third lead concentrate slurry (K-Pb) and fifth middling (N3).
Roughing zinc: preparing a second slurry from lead tailings of a preset grade in a 0.75L single-groove flotation machine, adding calcium oxide (lime) into the second slurry according to a concentration of 2000g/t for mixing treatment, adding butyl xanthate according to a concentration of 100g/t for mixing treatment, and adding No. 2 oil according to a concentration of 15g/t to obtain zinc coarse slurry and zinc tailings.
First zinc concentration: in a 0.5L single-groove flotation machine, calcium oxide (lime) is added into the zinc crude slurry according to the concentration of 100g/t for mixing treatment, and butyl xanthate is added according to the concentration of 30g/t for mixing treatment, so that a first zinc concentrate (N-Zn1) and a sixth middling are obtained.
And (3) second zinc concentration: and preparing the first zinc concentrate ore into third slurry in a 0.5L single-groove flotation machine, adding calcium oxide (lime) into the third slurry according to the concentration of 500g/t, and mixing to obtain a second zinc concentrate ore (K-Zn) and a seventh middling ore (N-Zn 2).
And adding butyl xanthate into the zinc tailings according to the concentration of 25g/t for mixing treatment to obtain eighth middling (X) and zinc tailings (K2).
As shown in table 2, the experimental results are explained, wherein: (i) the third lead concentration ore slurry (K-Pb),: (ii) the fifth middling (N3), (iii) the fourth middling (N2), (iv) the third middling (N1), (v) the second lead concentration tailings (K1), (K-Zn) the second zinc concentration (K-Zn), (c) the seventh middling (N-Zn2), and (iii) the first zinc concentration, and (iv-Zn 1), (X) the eighth middling (X), and (iv) the zinc concentration tailings (K2).
TABLE 2 flotation test results of wastewater from electroflocculation of lead-zinc ore
Wherein, the flotation test is carried out by adopting the water sample of the mixed wastewater of the minium lead-zinc ore after the electrocoagulation treatment. The yield of the open-circuit flotation lead concentrate is 2.82%, the lead grade is 51.91%, and the lead recovery rate is 36.06%. The yield of the zinc concentrate is 8.36 percent, and the grade of the zinc concentrate is 56.33 percent. The flotation final tailing yield is 62.88 percent, and the lead grade and the zinc grade are 0.22 percent and 0.58 percent respectively.
Comparative example 1
The flotation experiment was carried out in the same manner as in example 1, except that the flotation water was pure paradoxical lead-zinc ore. The result of the flotation test is shown in table 3, and explained below, the third lead concentrate slurry (K-Pb), the fifth middling (N3), the fourth middling (N2), the third middling (N1), the second lead concentrate tailings (K1), the second zinc concentrate (K-Zn), the seventh middling (N-Zn2), the first zinc concentrate (r), the eighth middling (X) (N-Zn1), and the zinc concentrate tailings (K2) (c).
TABLE 3 test results of the clean water flotation of the minite
Wherein, the yield of the open-circuit flotation lead concentrate is 1.80 percent, the lead grade is 71.73 percent, and the lead recovery rate is 30.54 percent. The yield of the zinc concentrate is 8.60 percent, and the grade of the zinc concentrate is 56.96 percent. The flotation final tailing yield is 62.24%, and the lead and zinc grade is 0.22% and 0.32% respectively.
Comparative example 2
The flotation experiment was carried out in the same manner as in example 1, except that the flotation water was mixed beneficiation wastewater from untreated paradox lead-zinc ore. The results of the flotation tests are shown in table 4, wherein it is to be explained that (i) the third lead concentrate slurry (K-Pb), the fifth middling (N3), the fourth middling (N2), the third middling (N1), the second lead concentrate tailings (K1), the second zinc concentrate (K-Zn), the seventh middling (N-Zn2), the first zinc concentrate (Zn), the ninth middling (N-Zn1), the eighth middling (X), and the zinc concentrate tailings (K2) are indicated.
TABLE 4 flotation test results for untreated wastewater from Van-Korea lead-zinc ores
Wherein, the yield of the open-circuit flotation lead concentrate is 1.83 percent, the lead grade is 57.62 percent, and the lead recovery rate is 25.01 percent. The yield of the zinc concentrate is 4.56%, and the grade of the zinc concentrate is 56.96%. The flotation final tailing yield is 7.56 percent, and the lead and zinc grade is 0.22 percent and 0.63 percent respectively.
Referring to fig. 2 to 3, the arrangement shows the main flotation indexes of the open-circuit flotation test of the lead-zinc ore sample by using different water samples. Mainly presents the difference between flotation test indexes and clear water flotation indexes before and after the wastewater of the dressing plant is treated by an electrocoagulation test, and researches the influence of the wastewater reuse on the dressing indexes and the feasibility of the wastewater reuse after the electrocoagulation treatment.
It can be obviously seen that the recovery rate and grade of the lead concentrate are lower than the flotation indexes of clear water when the mixed wastewater is adopted to carry out the flotation test of the Van-Kou lead-zinc ore. And performing a flotation test on the mixed wastewater after the electrocoagulation treatment, wherein the grade of the lead concentrate is lower than the flotation index of the clear water, and the recovery rate is higher than the flotation index of the clear water. The wastewater is adopted for a flotation test, and the influence on the recovery rate of lead concentrate is the greatest. The wastewater after the electric flocculation treatment is adopted for a flotation test, the lead concentrate level is reduced, but the lead concentrate recovery rate is improved.
The flotation test result in fig. 3 shows that the flotation test is carried out by adopting the clean water, the mixed wastewater and the water sample after the electric flocculation treatment, the obtained zinc concentrate has similar grade, and the three water samples have almost no influence on the zinc concentrate grade. In the aspect of zinc concentrate recovery rate, the recovery rate of the zinc concentrate by adopting clear water flotation is highest, and the recovery rate by adopting waste water direct flotation is lowest.
The lead grades of flotation tailings obtained by the three water samples are equal, and the recovery rates of the tailings are almost the same. The zinc grade and recovery rate of tailings obtained by wastewater flotation are highest, the water sample obtained after the electric flocculation treatment is second, and the clear water flotation is lowest.
The present invention is not intended to be limited to the particular embodiments shown, but is to be accorded the widest scope consistent with the principles and spirit of the present invention.
Claims (10)
1. A wastewater treatment method is characterized by comprising the following steps:
performing electric flocculation treatment on the wastewater to obtain primary purified water;
and preparing the primary purified water and the raw ore into ore pulp, and performing flotation treatment on the ore pulp to obtain a flotation product and the flotation water.
2. The wastewater treatment method according to claim 1, wherein in the step of electrocoagulation treatment, the anode plate comprises one of an Fe electrode and an Al electrode, and the cathode plate comprises a stainless steel electrode.
3. The wastewater treatment method according to claim 2, wherein in the step of the electrocoagulation treatment, the distance between the anode plate and the cathode plate is 10-20 mm.
4. The wastewater treatment method according to any one of claims 1 to 3, wherein in the electrocoagulation treatment step, the current density is 8.24 to 24.73mA/cm2The electrolytic voltage is 10-35V.
5. The wastewater treatment method according to any one of claims 1 to 3, further comprising a step of adding a pH reagent to the wastewater to adjust the pH of the wastewater to 3 to 11 before the electrocoagulation treatment.
6. The wastewater treatment method according to any one of claims 1 to 3, further comprising a step of adding activated carbon to the wastewater before the step of electroflocculation, and the concentration of the activated carbon in the wastewater is 0.59 to 6.47g.L-1。
7. The wastewater treatment method according to any one of claims 1 to 3, further comprising adding H to the wastewater before the step of electroflocculation2O2And said H is2O2The concentration of the wastewater is 600-938.85 mg.L-1。
8. The method for treating wastewater according to any one of claims 1 to 3, wherein the duration of the electrocoagulation treatment is 50 to 70 min.
9. A method for treating wastewater according to any of claims 1 to 3, wherein the raw ore is crushed and ground to have a particle size of less than 0.074 mm.
10. The wastewater treatment method according to any one of claims 1 to 3, wherein the raw ore comprises lead-zinc ore, and the COD value-reduced water and the lead-zinc ore are formulated into a slurry at a mass ratio of 8:2 to 1: 1.
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