Double-oxidant thallium removal reagent combination for water treatment and water treatment method

Abstract

The invention provides a double-oxidant thallium removal reagent combination for water treatment and a water treatment method. The double-oxidant thallium removal reagent combination comprises a sodium hypochlorite solution, a potassium ferrate solution, a manganese chloride solution, a PH regulator, a coagulant and a flocculant. The concentration of the sodium hypochlorite solution is 15-30% by mass, the concentration of the potassium ferrate solution is 8-10% by mass, and the concentration of the manganese chloride solution is 12-18% by mass. When the double-oxidant thallium removal reagent combination is used for executing a water treatment process, manganese chloride serving as an aid can improve the oxidized competitiveness of Tl < + >, so that Tl < + > in wastewater can be effectively oxidized into Tl < 3 + >, other pollutants in the wastewater can be oxidized, the agent adding cost is reduced, and introduction of other pollutants is avoided.

Description

Technical Field

[0001] The invention belongs to the technical field of water treatment, and in particular relates to a double oxidant thallium removal reagent combination for water treatment and a water treatment method. Background Art

[0002] Sintering and desulfurization are inevitable processes in steel production, and sintering wastewater and desulfurization wastewater contain a large number of pollutants, such as heavy metal ions, nitrides, sulfides, etc. Among them, thallium is a typical heavy metal pollutant. If it is directly discharged, it will cause potential harm to the environment and human health. Therefore, the discharge of thallium-containing wastewater in the steel industry needs to be effectively controlled.

[0003] In order to effectively control and direct the thallium pollution in the steel industry wastewater, the government departments of my country have promulgated a series of relevant laws and regulations. For example, the "Industrial Wastewater Thallium Pollutant Emission Standard" (DB43 / 968-2014) issued by Hunan Province stipulates that the emission limit of thallium pollutants in industrial wastewater involving heavy metal thallium is 0.005mg / L; for another example, the "Industrial Wastewater Thallium Pollutant Emission Standard" (DB44 / 1989-2017) issued by Guangdong Province stipulates that the emission limit of total thallium is: 0.005mg / L for existing enterprises and 0.002mg / L for newly built enterprises. / L, the special emission limit is 0.001mg / L; for example, Jiangsu Province has clarified the emission standard DB32 / 3431-2018 for thallium pollutants in steel industry wastewater, which stipulates that the emission limit of thallium pollutants in steel industry wastewater at the wastewater discharge outlet of workshops or production facilities is 0.002mg / L ((direct emission and indirect emission). With the attention paid to thallium pollutants and the further implementation of ultra-low emission standards, in 2020, the Ministry of Ecology and Environment added an emission limit for total thallium in the Amendment to the "Steel Industry Wastewater Discharge Standard" (Draft for Comments), requiring it to be 0.05mg / L.

[0004] The thallium removal process in industrial wastewater mainly adopts the method of adding reagents and coagulation and precipitation. The type of reagents has an impact on the process of water treatment, and the price difference of different reagents is large. In the past, when complex high-salt wastewater was treated for thallium removal, inorganic sulfur reagents such as sodium sulfide were usually used to capture and precipitate thallium. This method has the advantage of low cost. However, sodium sulfide has a peculiar smell. When the thallium content in the wastewater is high, the amount of sodium sulfide that needs to be added is large, resulting in a large peculiar smell at the water treatment site. When the drug is manually dosed, the peculiar smell causes the inefficiency of manual operation and high labor costs. At the same time, impurities such as suspended matter in the wastewater cannot be removed. In addition, when using inorganic sulfur reagents to remove thallium, if slaked lime is used as a pH regulator, there is a problem of excessive mud in the entire treatment process. If a liquid pH regulator is used to adjust the pH, there is a problem of not being able to ensure that the thallium content of the effluent meets the standard. In this regard, a slaked lime enhanced sodium sulfide coagulation technology has been proposed in the prior art. Although it can ensure a stable thallium removal efficiency, it is difficult to synergistically remove pollutants such as ammonia nitrogen and COD in the water. Summary of the invention

[0005] The purpose of the present invention is to provide a double oxidant thallium removal reagent combination for water treatment and a water treatment method, so as to effectively remove thallium ions in wastewater while also simultaneously removing pollutants such as ammonia nitrogen and COD, and reduce the cost of reagents and the introduction of new pollutants.

[0006] To achieve the above object, the present invention provides a dual oxidant thallium removal reagent combination for water treatment, comprising: sodium hypochlorite solution, potassium ferrate solution, manganese chloride solution, pH regulator, coagulant, and flocculant;

[0007] Calculated in mass percentage, the concentration of the sodium hypochlorite solution is 15% to 30%, the concentration of the potassium ferrate solution is 8% to 10%, and the concentration of the manganese chloride solution is 12% to 18%.

[0008] Optionally, the coagulant is a polyaluminium chloride solution, and the mass percentage of the polyaluminium chloride solution is 30%.

[0009] Optionally, the coagulant is polyacid ferric.

[0010] Optionally, the flocculant is a polyacrylamide solution, and the mass percentage of the polyacrylamide solution is 1‰ to 3‰.

[0011] Optionally, the pH adjuster includes a first pH adjuster and a second pH adjuster, the first pH adjuster includes an alkaline compound, and the second pH adjuster includes an acidic compound.

[0012] The embodiment of the present invention also provides a water treatment method, comprising:

[0013] Step S1, using a pH regulator to adjust the pH of the wastewater so that the pH of the wastewater at room temperature is 10.5-11.5;

[0014] Step S2, adding sodium hypochlorite solution to the wastewater treated in step S1 and stirring, wherein the mass percentage of the sodium hypochlorite solution is 15% to 30%;

[0015] Step S3, adding potassium ferrate solution and manganese chloride solution to the wastewater treated in step S2 and stirring, wherein the mass percentage of potassium ferrate solution is 8% to 10%, and the mass percentage of manganese chloride solution is 12% to 18%;

[0016] Step S4, using a pH regulator to adjust the pH of the wastewater treated in step S3 so that the pH of the wastewater at room temperature is 8.5 to 9.5;

[0017] Step S5, adding coagulant and flocculant to the wastewater treated in step S4.

[0018] Optionally, the step S1, the step S2, the step S3, the step S4, and the step S5 are performed in different containers.

[0019] Optionally, the pH of the wastewater adjusted in step S1 at room temperature is 11, and the pH of the wastewater adjusted in step S4 at room temperature is 9.

[0020] Optionally, the stirring speed in step S2 is 300 rpm to 500 rpm, and the reaction time is 15 min to 20 min; the stirring speed in step S3 is 300 rpm to 500 rpm, and the reaction time is 20 min to 25 min.

[0021] Optionally, assuming that the thallium content in the wastewater is 1500 μg / L and the volume of the wastewater is 1 L, the volume of the sodium hypochlorite solution added in step S2 is 20 mL to 40 mL, the volume of the potassium ferrate solution added in step S3 is 8 mL to 14 mL, and the volume of the manganese chloride solution is 2 mL to 4 mL.

[0022] Compared with the prior art, the dual oxidant thallium removal reagent combination for water treatment of the present invention has the following advantages:

[0023] The aforementioned double oxidant thallium removal reagent combination for water treatment includes sodium hypochlorite solution, potassium ferrate solution, manganese chloride solution, pH regulator, coagulant, and flocculant; in terms of mass percentage, the concentration of sodium hypochlorite solution is 15% to 30%, the concentration of potassium ferrate solution is 8% to 10%, and the concentration of manganese chloride solution is 12% to 18%. The process of using the double oxidant thallium removal reagent combination to perform a water treatment process is as follows: first, the pH of the wastewater is adjusted using a pH regulator so that the pH of the wastewater at room temperature is 10.5 to 11.5; then, sodium hypochlorite solution is added to the wastewater and stirred; then, potassium ferrate solution and manganese chloride solution are added to the wastewater and stirred; then, the pH of the wastewater is adjusted using a pH regulator so that the pH of the wastewater at room temperature is 8.5 to 9.5; finally, a coagulant and a flocculant are added to the wastewater. In this process, sodium hypochlorite and potassium ferrate are used to oxidize the wastewater under alkaline conditions, and manganese chloride is used as an auxiliary agent to increase Tl + The competitive oxidation of Tl in wastewater can be effectively + Oxidized to Tl 3+ On the one hand, it also oxidizes other pollutants in the wastewater, on the other hand, it reduces the amount of expensive reagents used and reduces the cost of adding reagents, and on the other hand, it will not introduce other pollutants due to the addition of reagents. DETAILED DESCRIPTION

[0024] The following describes the embodiments of the present invention through specific examples, and those skilled in the art can easily understand other advantages and effects of the present invention from the contents disclosed in this specification. The present invention can also be implemented or applied through other different specific embodiments, and the details in this specification can also be modified or changed in various ways based on different viewpoints and applications without departing from the spirit of the present invention.

[0025] In addition, each embodiment of the following description has one or more technical features, but this does not mean that the user of the present invention must implement all the technical features in any embodiment at the same time, or can only implement part or all of the technical features in different embodiments separately. In other words, under the premise that implementation is possible, those skilled in the art can selectively implement part or all of the technical features in any embodiment according to the disclosure of the present invention and according to the design specifications or implementation requirements, or selectively implement a combination of part or all of the technical features in multiple embodiments, thereby increasing the flexibility of the implementation of the present invention.

[0026] As used in this specification, the singular forms "a", "an", and "the" include plural objects, and the plural form "a plurality" includes more than two objects, unless the context clearly indicates otherwise. As used in this specification, the term "or" is generally used to include the meaning of "and / or", unless the context clearly indicates otherwise. For those of ordinary skill in the art, the specific meanings of the above terms in the present invention can be understood according to specific circumstances.

[0027] The purpose of the present invention is to provide a double oxidant thallium removal reagent combination for water treatment and a water treatment method, so as to remove pollutants such as ammonia nitrogen and COD while removing thallium, reduce the dosage of the reagent, and save the cost of adding the reagent.

[0028] The dual oxidant thallium removal reagent combination for water treatment comprises a sodium hypochlorite solution, a potassium ferrate solution, a manganese chloride solution, a pH regulator, a coagulant, and a flocculant. In terms of mass percentage, the concentration of the sodium hypochlorite solution is 15% to 30%, the concentration of the potassium ferrate solution is 8% to 10%, and the concentration of the manganese chloride solution is 12% to 18%.

[0029] The process of treating thallium-containing wastewater using the dual oxidant thallium removal reagent combination is as follows:

[0030] First, step S1 is performed: the pH of the wastewater is adjusted using a pH regulator so that the pH of the wastewater at room temperature is 10.5-11.5.

[0031] Then, step S2 is performed: adding sodium hypochlorite solution to the wastewater treated in step S1 and stirring, wherein the mass percentage of the sodium hypochlorite solution is 15% to 30%.

[0032] Then, step S3 is performed: adding potassium ferrate solution and manganese chloride solution to the wastewater treated in step S2 and stirring, wherein the mass percentage of potassium ferrate solution is 8% to 10%, and the mass percentage of manganese chloride solution is 12% to 18%.

[0033] Then, step S4 is performed: using a pH regulator to adjust the pH of the wastewater treated in step S3 so that the pH of the wastewater at room temperature is 8.5 to 9.5.

[0034] Then, step S5 is performed: adding coagulant and flocculant to the wastewater treated in step S4.

[0035] The priority of reducing substances in wastewater in consuming oxidants is different. Generally speaking, small molecular organic matter in ammonia nitrogen and COD is easier to be oxidized, while large molecular organic matter is more difficult to be oxidized. + It is more difficult to be oxidized than ammonia nitrogen and COD. Therefore, Tl is present in general water treatment processes. +In the solution provided by the present invention, potassium ferrate and sodium hypochlorite are used as two oxidants, and manganese chloride is also used as an auxiliary agent to reduce Tl + The oxidation difficulty can be reduced, and the dosage of potassium ferrate can be reduced to reduce the cost of adding reagents.

[0036] Specifically, by adding relatively cheap sodium hypochlorite in step S2, ammonia nitrogen and small organic molecules in COD can be oxidized and reduced by sodium hypochlorite, and the cost of dosing is relatively low compared to directly adding a relatively expensive potassium ferrate solution to make ammonia nitrogen and small organic molecules in COD react with potassium ferrate. When performing step S3, manganese chloride solution is used as an auxiliary agent, so that manganese chloride and potassium ferrate produce a synergistic effect to enhance Tl + Thus, in step S3, even if the oxidant concentration in the wastewater is slightly low, the oxidation of Tl can be achieved. + The oxidation of Tl is carried out to reduce the dosage of potassium ferrate and the cost of adding the reagent. In addition, in the step S3, the concentration of the oxidant in the wastewater is first oxidized to + , and then oxidize the macromolecular organic matter in ammonia nitrogen and COD, so that after executing step S5, the metal thallium in the wastewater can be effectively removed. It can be understood that in Tl + After the oxidation is completed, as long as there is a sufficient amount of oxidant in the wastewater, the macromolecular organic matter in the ammonia nitrogen and COD can also be oxidized and removed. It should be noted that after the execution of step S2, some sodium hypochlorite may still exist in the wastewater. Therefore, the oxidant in step S3 includes at least potassium ferrate and may also include sodium hypochlorite.

[0037] It should be noted that the mass percentage of the sodium hypochlorite solution used in the embodiment of the present invention is within the range of 15% to 30% because a sodium hypochlorite solution with a mass percentage higher than 30% is prone to cause safety accidents, and a sodium hypochlorite solution with a mass percentage lower than 15% has a poor oxidation effect. The mass percentage of potassium ferrate is within the range of 8% to 10% because, on the one hand, the dissolution rate of potassium ferrate is considered, and on the other hand, the oxidation effect of potassium ferrate is considered.

[0038] Optionally, the pH regulator includes a first pH regulator and a second pH regulator, wherein the first pH regulator includes an alkaline compound and the second pH regulator includes an acidic compound. More specifically, the first pH regulator includes but is not limited to at least one of slaked lime and sodium hydroxide, and the second pH regulator includes but is not limited to a hydrochloric acid solution. Thus, a suitable pH regulator can be selected as needed to adjust the acidity and alkalinity of the wastewater.

[0039] Alternatively, the coagulant may be a conventional coagulant, such as a polyaluminium chloride solution. Alternatively, the coagulant may also be polyferric sulfate.

[0040] Optionally, the flocculant may be a conventional flocculant, such as a polyacrylamide solution.

[0041] Furthermore, an embodiment of the present invention also provides a water treatment method, which includes steps S1 to S5 as above.

[0042] The normal temperature refers to 20°C to 30°C.

[0043] It can be understood that the step S1 uses the first pH regulator to adjust the pH of the wastewater, and preferably adjusts the pH of the wastewater to 11 at room temperature. The step S4 uses the second pH regulator to adjust the pH of the wastewater, and preferably adjusts the pH of the wastewater to 9 at room temperature.

[0044] Further, each step in the water treatment process is performed in a different container. Specifically in the embodiment of the present invention, step S1 is performed in a regulating tank, step S2 is performed in a first reaction tank, step S3 is performed in a second reaction tank, step S4 is performed in an equalizing tank, and step S5 is performed in an inclined plate sedimentation tank.

[0045] Furthermore, the amount of the sodium hypochlorite solution added in step S2 and the amount of the potassium ferrate solution and the manganese chloride solution added in step S3 should be reasonable. Too much addition will cause waste, and too little addition will not fully oxidize ammonia nitrogen, COD, and Tl + After repeated tests, it was determined that for 1L of sewage with a thallium content of 1500μg / L, the volume of the sodium hypochlorite solution added in step S2 is 20mL-40mL, the volume of the potassium ferrate solution added in step S3 is 8mL-14mL, and the amount of the manganese chloride solution added is 2mL-4mL.

[0046] In addition, in the step S2, the residence time of the wastewater in the first reaction tank is 15min to 20min, and the wastewater in the first reaction tank is preferably stirred by a first mechanical stirring device at a stirring speed of 300rpm to 500rpm. In the step S3, the residence time of the wastewater in the second reaction tank is 20min to 25min, and the wastewater in the second reaction tank is preferably stirred by a second mechanical stirring device at a stirring speed of 300rpm to 500rpm.

[0047] In step S5, the coagulant and the flocculant are added in conventional amounts. In addition, when polyaluminium chloride solution is used as the coagulant, the mass percentage of the polyaluminium chloride solution can be 30%. The mass percentage of the polyacrylamide solution used as the flocculant can be 1‰ to 3‰.

[0048] In order to make the objects, advantages and features of the present invention more clear, the present invention is further described in detail below in conjunction with specific embodiments.

[0049] <Example 1>

[0050] The treatment object is the desulfurization wastewater of a power plant with a daily water output of 12t / d. The pH of the desulfurization wastewater at room temperature is about 6.2, the thallium content is about 130μg / L, and the ammonia nitrogen content is about 87mg / L.

[0051] The Environmental Protection Bureau in the area where the power plant is located requires that the thallium content in the workshop drainage outlet be controlled so that the thallium content in the resulting water is kept below 5μg / L and the ammonia nitrogen content is below 30mg / L.

[0052] The wastewater treatment process is as follows:

[0053] Step S1, allowing the wastewater to enter the regulating tank, and using sodium hydroxide solution to adjust the pH of the wastewater to 11 at room temperature.

[0054] Step S2: the wastewater treated in step S1 is heated to 2.5 m 3 / h flow rate into the first reaction tank, and make the mass percentage of 20% sodium hypochlorite solution according to 0.005m 3 / h flow rate into the first reaction tank, and at the same time, the first mechanical stirring device is controlled to operate at a speed of 350rpm for stirring. In this step, the residence time of the wastewater in the first reaction tank is 20min, that is, the reaction time of this step is about 20min.

[0055] Step S3: the wastewater treated in step S2 is heated to 2.5 m 3 / h flow rate into the second reaction tank, and the mass percentage of 9% potassium ferrate solution at 0.002m 3 / h flow rate into the second reaction tank, so that the mass percentage of 15% manganese chloride solution according to 0.0008m 3 / h flow rate into the second reaction tank, and at the same time, the second mechanical stirring device is controlled to operate at a speed of 350rpm for stirring. In this step, the wastewater stays in the second reaction tank for 20 minutes, that is, the reaction time of this step is about 20 minutes.

[0056] Step S4: the wastewater treated in step S3 is heated to 2.5 m 3 / h flow rate into the equalization tank, and hydrochloric acid is added to the equalization tank to adjust the pH of the wastewater to about 9.5 at room temperature.

[0057] Step S5: subjecting the wastewater treated in step S4 to a temperature of 2.5 m 3 / h flow into the inclined plate sedimentation tank, and add polyaluminium chloride solution and polyacrylamide solution into the wastewater. The mass percentage of the polyaluminium chloride solution used in this step is 30%, and the mass percentage of the polyacrylamide solution is 2‰.

[0058] After the above treatment, the thallium content in the power plant's effluent was stabilized at around 4μg / L, and the ammonia nitrogen content dropped to around 23mg / L, meeting local environmental protection requirements.

[0059] <Example 2>

[0060] The treatment object is the sintering wastewater of a steel plant, which produces 21t / d of water per day. The pH of the sintering wastewater at room temperature is about 1.2, the thallium content is about 2588μg / L, and the COD content is about 370mg / L.

[0061] The Environmental Protection Bureau in the area where the steel plant is located requires that the thallium content in the water discharged from the workshop outlet should be less than 5μg / L, and the COD content should be less than 250mg / L.

[0062] The wastewater treatment process is as follows:

[0063] Step S1, allowing the wastewater to enter the regulating tank, and using sodium hydroxide solution to adjust the pH of the wastewater to 11.5 at room temperature.

[0064] Step S2: subjecting the wastewater treated in step S1 to a temperature of 5 m 3 / h flow rate into the first reaction tank, and make the mass percentage of 15% sodium hypochlorite solution according to 0.3m 3 / h flow rate into the first reaction tank, and at the same time, the first mechanical stirring device is controlled to operate at a speed of 300rpm for stirring. In this step, the residence time of the wastewater in the first reaction tank is 20min, so that the reaction time of this step is about 20min.

[0065] Step S3: subjecting the wastewater treated in step S2 to a temperature of 5 m 3 / h flow rate into the second reaction tank, and the mass percentage of 8% potassium ferrate solution at 0.11m 3 / h flow rate into the second reaction tank, so that the mass percentage of 18% manganese chloride solution according to 0.02m3 / h flow rate into the second reaction tank, and at the same time, the second mechanical stirring device is controlled to operate at a speed of 400rpm for stirring. In this step, the wastewater stays in the second reaction tank for 25min, that is, the reaction time of this step is about 25min.

[0066] Step S4: the wastewater treated in step S3 is heated to 2.5 m 3 / h flow rate into the equalization tank, and hydrochloric acid is added to the equalization tank to adjust the pH of the wastewater to about 9 at room temperature.

[0067] Step S5: subjecting the wastewater treated in step S4 to a temperature of 5 m 3 / h flow into the inclined plate sedimentation tank, and add polyaluminium chloride solution and polyacrylamide solution into the wastewater. The mass percentage of the polyaluminium chloride solution used in this step is 30%, and the mass percentage of the polyacrylamide solution is 1‰.

[0068] After the above treatment, the pH value of the effluent from the power plant at room temperature fluctuates between 9 and 10, the average thallium content in the effluent is about 3.7 μg / L, and the average COD content is about 220 mg / L, which meets the local environmental protection requirements.

[0069] <Example 3>

[0070] The treatment object is the sintering wastewater of a steel plant, which produces 75t / d of water per day. The pH of the sintering wastewater at room temperature is about 3.4, and the thallium content is 5225μg / L.

[0071] The Environmental Protection Bureau in the area where the steel plant is located requires that the thallium content in the water discharged from the workshop outlet shall not exceed 2μg / L.

[0072] The wastewater treatment process is as follows:

[0073] Step S1, allowing the wastewater to enter the regulating tank, and using sodium hydroxide solution to adjust the pH of the wastewater to 10.5 at room temperature.

[0074] Step S2: the wastewater treated in step S1 is heated to 7m 3 / h flow rate into the first reaction tank, and make the mass percentage of 30% sodium hypochlorite solution according to 0.95m 3 / h flow rate into the first reaction tank, and at the same time, the first mechanical stirring device is controlled to operate at a speed of 500rpm for stirring. In this step, the residence time of the wastewater in the first reaction tank is 15min, so that the reaction time of this step is about 15min.

[0075] Step S3: the wastewater treated in step S2 is heated to 7m 3 / h flow rate into the second reaction tank, and the mass percentage of 10% potassium ferrate solution at 0.3m 3 / h flow rate into the second reaction tank, so that the mass percentage of 12% manganese chloride solution according to 0.92m 3 / h flow rate into the second reaction tank, and at the same time, the second mechanical stirring device is controlled to operate at a speed of 480rpm for stirring. In this step, the wastewater stays in the second reaction tank for 25min, that is, the reaction time of this step is about 25min.

[0076] Step S4: the wastewater treated in step S3 is heated to 2.5 m 3 / h flow rate into the equalization tank, and hydrochloric acid is added to the equalization tank to adjust the pH of the wastewater to about 8.5 at room temperature.

[0077] Step S5: subjecting the wastewater treated in step S4 to 7m 3 / h flow into the inclined plate sedimentation tank, and add polyaluminium chloride solution and polyacrylamide solution into the wastewater. The mass percentage of the polyaluminium chloride solution used in this step is 30%, and the mass percentage of the polyacrylamide solution is 3‰.

[0078] After the above treatment, the pH value of the effluent from the power plant at room temperature fluctuates between 9 and 10, and the average thallium content in the effluent is about 1.2 μg / L, which meets local environmental protection requirements.

[0079] Although the present invention is disclosed as above, it is not limited thereto. Those skilled in the art may make various changes and modifications to the present invention without departing from the spirit and scope of the present invention. Thus, if these modifications and variations of the present invention fall within the scope of the claims of the present invention and their equivalents, the present invention is also intended to include these modifications and variations.

Claims

1. A dual oxidant thallium removal reagent combination for water treatment, characterized in that: include: Sodium hypochlorite solution, potassium ferrate solution, manganese chloride solution, pH adjuster, coagulant, and flocculant; Calculated in mass percentage, the concentration of the sodium hypochlorite solution is 15% to 30%, the concentration of the potassium ferrate solution is 8% to 10%, and the concentration of the manganese chloride solution is 12% to 18%.

2. The double oxidant thallium removal reagent combination for water treatment according to claim 1, characterized in that: The coagulant is a polyaluminium chloride solution, and the mass percentage of the polyaluminium chloride solution is 30%.

3. The double oxidant thallium removal reagent combination for water treatment according to claim 1, characterized in that: The coagulant is polyacid ferric.

4. The double oxidant thallium removal reagent combination for water treatment according to claim 1, characterized in that: The flocculant is a polyacrylamide solution, and the mass percentage of the polyacrylamide solution is 1‰ to 3‰.

5. The double oxidant thallium removal reagent combination for water treatment according to claim 1, characterized in that: The pH adjuster includes a first pH adjuster and a second pH adjuster, wherein the first pH adjuster includes an alkaline compound and the second pH adjuster includes an acidic compound.

6. A water treatment method, characterized in that: include: Step S1, using a pH regulator to adjust the pH of the wastewater so that the pH of the wastewater at room temperature is 10.5-11.5; Step S2, adding sodium hypochlorite solution to the wastewater treated in step S1 and stirring, wherein the mass percentage of the sodium hypochlorite solution is 15% to 30%; Step S3, adding potassium ferrate solution and manganese chloride solution to the wastewater treated in step S2 and stirring, wherein the mass percentage of potassium ferrate solution is 8% to 10%, and the mass percentage of manganese chloride solution is 12% to 18%; Step S4, using a pH regulator to adjust the pH of the wastewater treated in step S3 so that the pH of the wastewater at room temperature is 8.5 to 9.5; Step S5, adding coagulant and flocculant to the wastewater treated in step S4.

7. The water treatment method according to claim 6, characterized in that: The step S1, the step S2, the step S3, the step S4 and the step S5 are performed in different containers.

8. The water treatment method according to claim 6 or 7, characterized in that: The pH of the wastewater adjusted in step S1 at room temperature is 11, and the pH of the wastewater adjusted in step S4 at room temperature is 9.

9. The water treatment method according to claim 6, characterized in that: The stirring speed in step S2 is 300 rpm to 500 rpm, and the reaction time is 15 min to 20 min; the stirring speed in step S3 is 300 rpm to 500 rpm, and the reaction time is 20 min to 25 min.

10. The water treatment method according to claim 6, characterized in that: Assuming that the thallium content in the wastewater is 1500 μg / L and the volume of the wastewater is 1 L, the volume of the sodium hypochlorite solution added in step S2 is 20 mL to 40 mL, the volume of the potassium ferrate solution added in step S3 is 8 mL to 14 mL, and the volume of the manganese chloride solution is 2 mL to 4 mL.