Carbosulfan high-salinity wastewater treatment method and application thereof

Abstract

The invention discloses a carbosulfan high-salinity wastewater treatment method and application thereof, and relates to the technical field of wastewater treatment. The treatment method comprises the following steps: reacting modified carbon with the carbosulfan high-salt wastewater in an ABR reaction device; the preparation method of the modified carbon comprises the following steps: performing pyrolysis, alkali washing, acid washing and aluminum salt dipping treatment on a biomass material in sequence. By means of the treatment method, the COD removal rate can be remarkably increased under the high-salt condition, degradation of furanphenol and triethylamine is promoted, and the biodegradability of wastewater is improved.

Description

Technical Field

[0001] This invention relates to the field of wastewater treatment technology, and in particular to a method for treating high-salinity wastewater containing thiocarbamate and its application. Background Technology

[0002] Thiocarbofuran is a carbamate insecticide, acaricide, and nematicide. Its synthesis generates wastewater with high COD and difficulty in biochemical degradation. Therefore, it is necessary to treat the high-salinity wastewater from thiocarbofuran to reduce the dual environmental and economic pressure it imposes.

[0003] In related technologies, high-salinity wastewater containing thiocarbofuran is generally treated using extraction, Fenton oxidation, and flocculation. However, extraction methods suffer from drawbacks such as high operating costs, poor subsequent biodegradability, and complex operation. Fenton oxidation cannot effectively remove characteristic pollutants such as triethylamine from the wastewater, and the treated wastewater has poor biodegradability. Flocculation cannot effectively remove furanophenol from the wastewater, and because the wastewater is highly alkaline, it requires a large amount of hydrochloric acid to adjust the pH, and the COD of the treated wastewater remains high. Therefore, a method for treating high-salinity thiocarbofuran wastewater is still needed. Summary of the Invention

[0004] The present invention aims to at least solve one of the technical problems existing in the prior art. To this end, the present invention proposes a method for treating high-salinity wastewater containing thiocarbamate.

[0005] The present invention also provides applications of the above-described processing method.

[0006] A method for treating high-salinity wastewater containing thiocarbamate according to a first aspect of the present invention includes the following steps: The modified charcoal and the high-salt wastewater containing thiocarbamate were reacted in an ABR reactor. The method for preparing the modified carbon includes the following steps: The biomass materials were subjected to pyrolysis, alkali washing, acid washing, and aluminum salt impregnation in sequence.

[0007] The processing method according to embodiments of the present invention has at least the following beneficial effects: The treatment method described in this embodiment is simple to operate, low in cost, and low in energy consumption. It can significantly improve the COD removal rate under high salinity conditions, promote the degradation of furanol and triethylamine, and improve the biodegradability of wastewater. It has a promising application prospect in the recycling and treatment of high salinity wastewater containing thiocarbofuran.

[0008] According to some embodiments of the present invention, the biomass material includes at least one of coconut shell, rice husk, walnut shell, straw, and tea leaves.

[0009] According to some embodiments of the present invention, the pyrolysis temperature is 600℃-900℃. For example, it can be 600℃, 610℃, 620℃, 630℃, 640℃, 650℃, 660℃, 670℃, 680℃, 690℃, 700℃, 710℃, 720℃, 730℃, 740℃, 750℃, 760℃, 770℃, 780℃, 790℃, 800℃, 810℃, 820℃, 830℃, 840℃, 850℃, 860℃, 870℃, 880℃, 890℃, or 900℃. According to some embodiments of the present invention, the pyrolysis time is 1 h to 3 h. For example, it can be 1 h, 1.1 h, 1.2 h, 1.3 h, 1.4 h, 1.5 h, 1.6 h, 1.7 h, 1.8 h, 1.9 h, 2 h, 2.1 h, 2.2 h, 2.3 h, 2.4 h, 2.5 h, 2.6 h, 2.7 h, 2.8 h, 2.9 h, or 3 h.

[0010] According to some embodiments of the present invention, the atmosphere for pyrolysis is a nitrogen atmosphere or an inert gas atmosphere.

[0011] According to some embodiments of the present invention, the inert gas includes at least one of argon, xenon, and krypton.

[0012] According to some embodiments of the present invention, the alkaline washing includes the following steps: A mixture of pyrolytic carbon (after pyrolysis treatment) and alkaline solution is prepared, and the reaction is carried out.

[0013] According to some embodiments of the present invention, the reaction time for alkaline washing is 10 min to 60 min. For example, it can be 10 min, 15 min, 20 min, 25 min, 30 min, 35 min, 40 min, 45 min, 50 min, 55 min or 60 min.

[0014] According to some embodiments of the present invention, the reaction temperature for alkaline washing is 40℃-70℃. For example, it can be 40℃, 41℃, 42℃, 43℃, 44℃, 45℃, 46℃, 47℃, 48℃, 49℃, 50℃, 51℃, 52℃, 53℃, 54℃, 55℃, 56℃, 57℃, 58℃, 59℃, 60℃, 61℃, 62℃, 63℃, 64℃, 65℃, 66℃, 67℃, 68℃, 69℃, or 70℃.

[0015] According to some embodiments of the present invention, the mass-to-volume ratio of the pyrolytic char to the alkaline solution is (8 g-12 g):1 L. For example, it can be 8 g: 1 L, 8.2 g: 1 L, 8.4 g: 1 L, 8.6 g: 1 L, 8.8 g: 1 L, 9 g: 1 L, 9.2 g: 1 L, 9.4 g: 1 L, 9.6 g: 1 L, 9.8 g: 1 L, 10 g: 1 L, 10.2 g: 1 L, 10.4 g: 1 L, 10.6 g: 1 L, 10.8 g: 1 L, 11 g: 1 L, 11.2 g: 1 L, 11.4 g: 1 L, 11.6 g: 1 L, 11.8 g: 1 L, or 12 g: 1 L.

[0016] According to some embodiments of the present invention, the concentration of alkali in the alkaline solution is 2 mol / L to 4 mol / L. For example, it can be 2 mol / L, 2.1 mol / L, 2.2 mol / L, 2.3 mol / L, 2.4 mol / L, 2.5 mol / L, 2.6 mol / L, 2.7 mol / L, 2.8 mol / L, 2.9 mol / L, 3 mol / L, 3.1 mol / L, 3.2 mol / L, 3.3 mol / L, 3.4 mol / L, 3.5 mol / L, 3.6 mol / L, 3.7 mol / L, 3.8 mol / L, 3.9 mol / L, or 4 mol / L.

[0017] According to some embodiments of the present invention, the alkali is a strong alkali. The balance is water.

[0018] According to some embodiments of the present invention, the alkali includes at least one of NaOH, KOH, and Ca(OH)2.

[0019] According to some embodiments of the present invention, the pickling includes the following steps: A mixture of alkali-washed charcoal and acid solution was prepared and reacted.

[0020] According to some embodiments of the present invention, the pickling reaction time is 10 min to 60 min. For example, it can be 10 min, 15 min, 20 min, 25 min, 30 min, 35 min, 40 min, 45 min, 50 min, 55 min or 60 min.

[0021] According to some embodiments of the present invention, the pickling reaction temperature is 40℃-70℃. For example, it can be 40℃, 41℃, 42℃, 43℃, 44℃, 45℃, 46℃, 47℃, 48℃, 49℃, 50℃, 51℃, 52℃, 53℃, 54℃, 55℃, 56℃, 57℃, 58℃, 59℃, 60℃, 61℃, 62℃, 63℃, 64℃, 65℃, 66℃, 67℃, 68℃, 69℃, or 70℃.

[0022] According to some embodiments of the present invention, the mass-to-volume ratio of the alkaline washing char to the acid solution is (8 g-12 g):1 L. For example, it can be 8 g: 1 L, 8.2 g: 1 L, 8.4 g: 1 L, 8.6 g: 1 L, 8.8 g: 1 L, 9 g: 1 L, 9.2 g: 1 L, 9.4 g: 1 L, 9.6 g: 1 L, 9.8 g: 1 L, 10 g: 1 L, 10.2 g: 1 L, 10.4 g: 1 L, 10.6 g: 1 L, 10.8 g: 1 L, 11 g: 1 L, 11.2 g: 1 L, 11.4 g: 1 L, 11.6 g: 1 L, 11.8 g: 1 L, or 12 g: 1 L.

[0023] According to some embodiments of the present invention, the concentration of acid in the acid solution is 2 mol / L to 4 mol / L. For example, it can be 2 mol / L, 2.1 mol / L, 2.2 mol / L, 2.3 mol / L, 2.4 mol / L, 2.5 mol / L, 2.6 mol / L, 2.7 mol / L, 2.8 mol / L, 2.9 mol / L, 3 mol / L, 3.1 mol / L, 3.2 mol / L, 3.3 mol / L, 3.4 mol / L, 3.5 mol / L, 3.6 mol / L, 3.7 mol / L, 3.8 mol / L, 3.9 mol / L, or 4 mol / L.

[0024] According to some embodiments of the present invention, the acid is a strong acid. The balance is water.

[0025] According to some embodiments of the present invention, the acid includes at least one of HCl, H2SO4, and HNO3.

[0026] According to some embodiments of the present invention, the aluminum salt impregnation treatment includes the following steps: A mixture of acid-washed carbon and aluminum salt solution was prepared and reacted.

[0027] According to some embodiments of the present invention, the reaction time for the aluminum salt impregnation treatment is 1 h to 3 h. For example, it can be 1 h, 1.1 h, 1.2 h, 1.3 h, 1.4 h, 1.5 h, 1.6 h, 1.7 h, 1.8 h, 1.9 h, 2 h, 2.1 h, 2.2 h, 2.3 h, 2.4 h, 2.5 h, 2.6 h, 2.7 h, 2.8 h, 2.9 h, or 3 h.

[0028] According to some embodiments of the present invention, the reaction temperature of the aluminum salt impregnation treatment is 40℃-70℃. For example, it can be 40℃, 41℃, 42℃, 43℃, 44℃, 45℃, 46℃, 47℃, 48℃, 49℃, 50℃, 51℃, 52℃, 53℃, 54℃, 55℃, 56℃, 57℃, 58℃, 59℃, 60℃, 61℃, 62℃, 63℃, 64℃, 65℃, 66℃, 67℃, 68℃, 69℃, or 70℃.

[0029] According to some embodiments of the present invention, the mass-to-volume ratio of the pickled carbon and the aluminum salt solution is (8 g-12 g):1 L. For example: it can be... According to some embodiments of the present invention, the aluminum salt in the aluminum salt solution includes at least one of aluminum chloride, aluminum nitrate, and aluminum sulfate.

[0030] According to some embodiments of the present invention, the concentration of aluminum salt in the aluminum salt solution is 0.2 mol / L to 1 mol / L. For example, it can be 0.2 mol / L, 0.25 mol / L, 0.3 mol / L, 0.35 mol / L, 0.4 mol / L, 0.45 mol / L, 0.5 mol / L, 0.55 mol / L, 0.6 mol / L, 0.65 mol / L, 0.7 mol / L, 0.75 mol / L, 0.8 mol / L, 0.85 mol / L, 0.9 mol / L, 0.95 mol / L, or 1 mol / L.

[0031] According to some embodiments of the present invention, the bacteria in the ABR reactor include bacteria that have a degradation effect on at least one of triethylamine, n-hexane, and furanol.

[0032] According to some embodiments of the present invention, the bacteria in the ABR reactor include ECM strains.

[0033] According to some embodiments of the present invention, the ECM strain is ECM-200 from Jiangsu Yuanjie Environmental Technology Co., Ltd.

[0034] According to some embodiments of the present invention, the pH of the thiocarbamate high-salinity wastewater is 7-8. For example, it can be 7, 7.1, 7.2, 7.3, 7.4, 7.5, 7.6, 7.7, 7.8, 7.9 or 8.

[0035] According to some embodiments of the present invention, the COD of the thiocarbofuran high-salt wastewater is 10,000 mg / L-20,000 mg / L. For example, it can be 10,000 mg / L, 11,000 mg / L, 12,000 mg / L, 13,000 mg / L, 14,000 mg / L, 15,000 mg / L, 16,000 mg / L, 17,000 mg / L, 18,000 mg / L, 19,000 mg / L, or 20,000 mg / L.

[0036] According to some embodiments of the present invention, the salt concentration of the thiocarbofuran high-salt wastewater is 0-20000 mg / L. For example, it can be 1000 mg / L, 2000 mg / L, 3000 mg / L, 4000 mg / L, 5000 mg / L, 6000 mg / L, 7000 mg / L, 8000 mg / L, 9000 mg / L, 10000 mg / L, 11000 mg / L, 12000 mg / L, 13000 mg / L, 14000 mg / L, 15000 mg / L, 16000 mg / L, 17000 mg / L, 18000 mg / L, 19000 mg / L, or 20000 mg / L.

[0037] According to some embodiments of the present invention, the furanol concentration in the thiocarbofuran high-salt wastewater is 0-3000 mg / L. For example: it can be 100 mg / L, 200 mg / L, 300 mg / L, 400 mg / L, 500 mg / L, 600 mg / L, 700 mg / L, 800 mg / L, 900 mg / L, 1000 mg / L, 1100 mg / L, 1200 mg / L, 1300 mg / L, 1400 mg / L, 1500 mg / L, 1600 mg / L, 1700 mg / L, 1800 mg / L, 1900 mg / L, 2000 mg / L, 2100 mg / L, 2200 mg / L, 2300mg / L, 2400 mg / L, 2500 mg / L, 2600 mg / L, 2700 mg / L, 2800 mg / L, 2900 mg / L or 3000 mg / L.

[0038] According to some embodiments of the present invention, the triethylamine concentration in the thiocarbamate high-salt wastewater is 0-3500 mg / L. For example: it can be 100 mg / L, 200 mg / L, 300 mg / L, 400 mg / L, 500 mg / L, 600 mg / L, 700 mg / L, 800 mg / L, 900 mg / L, 1000 mg / L, 1100 mg / L, 1200 mg / L, 1300 mg / L, 1400 mg / L, 1500 mg / L, 1600 mg / L, 1700 mg / L, 1800 mg / L, 1900 mg / L, 2000 mg / L, 2100 mg / L, 2200 mg / L, 2300mg / L, 2400 mg / L, 2500 mg / L, 2600 mg / L, 2700 mg / L, 2800 mg / L, 2900 mg / L, 3000 mg / L, 3100 mg / L, 3200 mg / L, 3300 mg / L, 3400 mg / L or 3500 mg / L.

[0039] According to some embodiments of the present invention, the reaction temperature in the ABR reactor is 30°C-40°C. For example, it can be 30°C, 31°C, 32°C, 33°C, 34°C, 35°C, 36°C, 37°C, 38°C, 39°C, or 40°C.

[0040] According to some embodiments of the present invention, the reaction time in the ABR reactor is 8-20 days. For example, it can be 8, 9, 10, 11, 12, 13, 14, 15, 16, 17, 18, 19 or 20 days.

[0041] The application of the treatment method described in the first aspect embodiment of the second aspect of the present invention in the treatment and recovery of high-salinity wastewater containing thiocarbamate.

[0042] Other features and advantages of the invention will be set forth in the description which follows, and will be apparent in part from the description, or may be learned by practicing the invention. Detailed Implementation

[0043] The following will describe the concept and technical effects of the present invention clearly and completely with reference to the embodiments, so as to fully understand the purpose, features and effects of the present invention. Obviously, the described embodiments are only some embodiments of the present invention, not all embodiments. Other embodiments obtained by those skilled in the art based on the embodiments of the present invention without creative effort are all within the scope of protection of the present invention.

[0044] Unless otherwise specified in the examples, the procedures should be performed under standard conditions or conditions recommended by the manufacturer. Reagents or instruments whose manufacturers are not specified are all commercially available products.

[0045] When a numerical range is disclosed herein, the range is considered continuous and includes the minimum and maximum values ​​of the range, as well as every value between the minimum and maximum values. Furthermore, when the range refers to integers, it includes every integer between the minimum and maximum values ​​of the range. Additionally, when multiple ranges are provided to describe a feature or characteristic, the ranges may be combined. In other words, unless otherwise specified, all ranges disclosed herein should be understood to include any and all subranges to which they are incorporated.

[0046] The high-salt wastewater from the production of thiocarbofuran contains furanol at a concentration of 2382 mg / L, triethylamine at a concentration of 2974 mg / L, pH = 13.2, salt content of 15000 mg / L, COD = 14000 mg / L, and BOD5 / COD = 0.07.

[0047] Preparation Example 1 This example provides a method for preparing modified carbon, the steps of which are as follows: (1) After crushing the coconut shell, wash it three times with deionized water, dry it overnight at 80°C, and sieve it to obtain coconut shell powder with a particle size of 60 mesh.

[0048] (2) Place coconut shell powder in a tube furnace and pyrolyze it at 800°C under a nitrogen atmosphere for 2 hours. After cooling to room temperature, pyrolyzed char is obtained.

[0049] (3) Pyrolytic carbon was mixed with 3 mol / L NaOH aqueous solution at a mass-volume ratio of 10 g: 1 mL, reacted at 55℃ for 30 min, filtered, washed twice with anhydrous ethanol, then washed twice with deionized water, and dried at 80℃ to constant weight to obtain alkali-washed carbon.

[0050] (4) Mix the alkaline-washed carbon with 3 mol / L hydrochloric acid aqueous solution at a mass-volume ratio of 10 g: 1 mL, react at 55℃ for 30 min, filter, wash twice with anhydrous ethanol, then wash twice with deionized water, and dry at 80℃ to constant weight to obtain acid-washed carbon.

[0051] (5) Mix the acid-washed carbon with 0.5 mol / L AlCl3 aqueous solution at a mass-volume ratio of 10 g: 1 mL, soak at 55℃ for 2 h, filter, wash twice with anhydrous ethanol, then wash twice with deionized water, and dry at 80℃ to constant weight to obtain modified carbon.

[0052] Preparation of Comparative Example 1 This example provides a method for preparing modified carbon, which is basically the same as the method in Example 1, except that step (5) is omitted. The details are as follows: (1) After crushing the coconut shell, wash it three times with deionized water, dry it overnight at 80°C, and sieve it to obtain coconut shell powder with a particle size of 60 mesh.

[0053] (2) Place coconut shell powder in a tube furnace and pyrolyze it at 800°C under a nitrogen atmosphere for 2 hours. After cooling to room temperature, pyrolyzed char is obtained.

[0054] (3) Pyrolytic carbon was mixed with 3 mol / L NaOH aqueous solution at a mass-volume ratio of 10 g: 1 mL, reacted at 55℃ for 30 min, filtered, washed twice with anhydrous ethanol, then washed twice with deionized water, and dried at 80℃ to constant weight to obtain alkali-washed carbon.

[0055] (4) Mix the alkaline-washed carbon with 3 mol / L hydrochloric acid aqueous solution at a mass-volume ratio of 10 g: 1 mL, react at 55℃ for 30 min, filter, wash twice with anhydrous ethanol, then wash twice with deionized water, and dry at 80℃ to constant weight to obtain modified carbon.

[0056] Preparation of Comparative Example 2 This example provides a method for preparing modified carbon, which is basically the same as the method in Example 1, except that step (4) is omitted. Specifically: (1) After crushing the coconut shell, wash it three times with deionized water, dry it overnight at 80°C, and sieve it to obtain coconut shell powder with a particle size of 60 mesh.

[0057] (2) Place coconut shell powder in a tube furnace and pyrolyze it at 800°C under a nitrogen atmosphere for 2 hours. After cooling to room temperature, pyrolyzed char is obtained.

[0058] (3) Pyrolytic carbon was mixed with 3 mol / L NaOH aqueous solution at a mass-volume ratio of 10 g: 1 mL, reacted at 55℃ for 30 min, filtered, washed twice with anhydrous ethanol, then washed twice with deionized water, and dried at 80℃ to constant weight to obtain alkali-washed carbon.

[0059] (4) Mix the alkaline washed carbon with 0.5 mol / L AlCl3 aqueous solution at a mass-volume ratio of 10 g: 1 mL, soak at 55℃ for 2 h, filter, wash twice with anhydrous ethanol, then wash twice with deionized water, and dry at 80℃ to constant weight to obtain modified carbon.

[0060] Example 1 This example provides a method for treating high-salinity wastewater containing thiocarbamate, with the following steps: 50 kg of the modified carbon prepared in Example 1 and 10 kg of ECM bacteria (ECM-200, purchased from Jiangsu Yuanjie Environmental Technology Co., Ltd.) were added to the ABR tank. The pH of 200 L of high-salinity wastewater containing thiocarbamate was adjusted to 7.5 and then transferred to the ABR tank at a temperature of 32℃ for a retention time of 10 days.

[0061] Comparative Example 1 This example provides a method for treating high-salinity wastewater containing thiocarbamate, which is basically the same as the previous example, except that the modified char prepared in Preparation Example 1 is replaced with an equal mass of the modified char prepared in Comparative Example 1. The steps are as follows: 50 kg of the modified carbon prepared in Comparative Example 1 and 10 kg of ECM bacteria were added to the ABR tank. The pH of 200 L of high-salt wastewater containing thiocarbamate was adjusted to 7.5 and then transferred to the ABR tank. The temperature was 32℃ and the retention time was 10 days.

[0062] Comparative Example 2 This example provides a method for treating high-salinity wastewater containing thiocarbamate, which is basically the same as the previous example, except that the modified carbon obtained in Preparation Example 1 is replaced with an equal mass of the modified carbon obtained in Comparative Example 2. The steps are as follows: 50 kg of the modified carbon prepared in Comparative Example 2 and 10 kg of ECM bacteria were added to the ABR tank. The pH of 200 L of high-salt wastewater containing thiocarbamate was adjusted to 7.5 and then transferred to the ABR tank. The temperature was 32℃ and the retention time was 10 days.

[0063] Comparative Example 3 This example provides a method for treating high-salinity wastewater containing thiocarbamate, which is basically the same as the previous example, except that the modified carbon obtained in Preparation Example 1 is replaced with an equal mass of columnar activated carbon (1 mm particle size, purchased from Henan Youji New Material Technology Co., Ltd.). The steps are as follows: Add 50 kg of columnar activated carbon and 10 kg of ECM bacteria to the ABR tank. Adjust the pH of 200 L of high-salt wastewater containing thiocarbamate to 7.5, transfer it to the ABR tank, maintain the temperature at 32℃, and allow it to remain for 10 days.

[0064] Detection example The parameters of the high-salt wastewater containing thiocarbamate after treatment using the methods of Example 1 and Comparative Examples 1-3 were measured.

[0065] Table 1

[0066] As shown in Table 1, the modified carbon prepared in Example 1 significantly improved COD removal rate, promoted the degradation of furanol and triethylamine, and improved the biodegradability of wastewater. Using the modified carbon prepared in Comparative Examples 1 or 2, as well as commercially available activated carbon, resulted in significantly poorer performance. This may be because acid washing effectively increases the porosity and specific surface area of ​​the material, and combined with aluminum salt impregnation, it alters the composition of active groups on the material surface, thereby promoting good contact between the modified carbon surface and pollutants, enhancing the material's adsorption capacity, and improving the colonization of degrading bacteria on the modified carbon surface, thus increasing degradation efficiency.

[0067] The embodiments of the present invention have been described in detail above with reference to the examples. However, the present invention is not limited to the above embodiments. Within the scope of knowledge possessed by those skilled in the art, various changes can be made without departing from the spirit of the present invention.

Claims

1. A method for treating high-salinity wastewater containing thiocarbamate, characterized in that, Includes the following steps: The modified charcoal and the high-salt wastewater containing thiocarbamate were reacted in an ABR reactor. The method for preparing the modified carbon includes the following steps: The biomass materials were subjected to pyrolysis, alkali washing, acid washing, and aluminum salt impregnation in sequence.

2. The processing method according to claim 1, characterized in that, The pyrolysis temperature is 600℃-900℃; and / or the pyrolysis time is 1 h-3 h; and / or the pyrolysis atmosphere is a nitrogen atmosphere or an inert gas atmosphere.

3. The processing method according to claim 1, characterized in that, The alkaline washing includes the following steps: A mixture of pyrolytic carbon (after pyrolysis treatment) and alkaline solution is prepared, and the reaction is carried out.

4. The processing method according to claim 3, characterized in that, The alkaline washing reaction time is 10 min-60 min; and / or the alkaline washing reaction temperature is 40℃-70℃.

5. The processing method according to claim 1, characterized in that, The pickling process includes the following steps: A mixture of alkali-washed charcoal and acid solution was prepared and reacted.

6. The processing method according to claim 5, characterized in that, The pickling reaction time is 10 min-60 min; and / or the pickling reaction temperature is 40℃-70℃.

7. The processing method according to claim 1, characterized in that, The aluminum salt impregnation treatment includes the following steps: A mixture of acid-washed carbon and aluminum salt solution was prepared and reacted.

8. The processing method according to claim 7, characterized in that, The reaction time for the aluminum salt impregnation treatment is 1 h to 3 h; and / or the reaction temperature for the aluminum salt impregnation treatment is 40℃ to 70℃.

9. The processing method according to claim 7, characterized in that, The aluminum salt in the aluminum salt solution includes at least one of aluminum chloride, aluminum nitrate, and aluminum sulfate.

10. The application of the treatment method according to any one of claims 1-9 in the treatment and recovery of high-salinity wastewater containing thiocarbamate.

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