CN113754166B

CN113754166B - Treatment method of photo-initiator TPO production wastewater

Info

Publication number: CN113754166B
Application number: CN202111062687.8A
Authority: CN
Inventors: 杨宏伟; 胡忠华; 史政伟
Original assignee: Shenyang Huiyu Chemical Environmental Protection Technology Co ltd
Current assignee: Shenyang Huiyu Chemical Environmental Protection Technology Co ltd
Priority date: 2021-09-10
Filing date: 2021-09-10
Publication date: 2023-07-14
Anticipated expiration: 2041-09-10
Also published as: CN113754166A

Abstract

The invention relates to a complexing agent composition, which comprises the following components in percentage by volume: 10% -50% of complexing agent, 5% -25% of cosolvent and the balance of diluent; the complexing agent is one or more of N, N-dialkyl acetamide, trialkyl phosphate and tertiary amine. The complexing agent composition can extract and separate toxic pollutants such as phosphorus-containing organic matters and organic acids without phosphorus in TPO production wastewater, the COD of the wastewater after complexing extraction is low, the removal rate of the pollutants is higher than that of the prior art, and the water after complexing extraction can be recycled for the production process. The invention also relates to a method for treating the waste water in the production of the photo-initiator TPO by using the complexing agent composition, which can remarkably reduce the COD of the waste water, has high pollutant removal rate, low treatment cost and simple process, can realize serialization and has wide application prospect.

Description

Treatment method of photo-initiator TPO production wastewater

Technical Field

The invention relates to the field of fine chemical wastewater treatment, in particular to a method for treating wastewater produced by a photoinitiator TPO.

Background

TPO is a high-efficiency free radical (I) type photoinitiator, the chemical name is 2,4, 6-trimethylbenzoyl-diphenyl phosphine oxide, the structural formula is shown as follows, the effective absorption peak value is 350-400nm, and the TPO can be absorbed until about 420nm, so that the TPO is not only suitable for mercury lamp systems, but also widely applied to mercury lamp systems.

The photoinitiator TPO adopts phosphorus trichloride, benzene and aluminum trichloride with low cost as raw materials to start reaction, after the reaction, diphenyl phosphine oxide is synthesized through one-step reaction of decomplexing and hydrolysis, then the reaction is carried out with 2,4, 6-trimethyl benzaldehyde to carry out addition reaction, and further oxidation is carried out to generate 2,4, 6-trimethyl benzoyl-diphenyl phosphine oxide, and the synthesis method is completed in 4 steps. A large amount of high-concentration organic wastewater is generated in the production process.

The wastewater has complex components, high organic matter concentration and contains organic phosphorus compounds. Most of organic substances in water are raw materials with incomplete reaction and byproducts produced by synthesis reaction, including 2,4, 6-trimethyl benzoic acid, diphenyl phosphonic acid, phenylphosphonic acid, diphenyl phosphine oxide and the like, which are difficult to biochemically degrade and belong to biological toxic substances. In addition, the production process has neutralization steps such as acid-base regulation and the like, and a large amount of sodium chloride salt is generated, and the salt content is more than 20%. The characteristics of the wastewater determine that the wastewater can not be treated by the traditional methods such as coagulating sedimentation, biochemistry and the like, so the treatment difficulty is very high.

At present, the following methods are mainly adopted for treating the wastewater containing the organic phosphorus.

CN104609665a discloses a Fenton oxidation method, wherein organic phosphorus in water is oxidized into inorganic phosphorus, and then the inorganic phosphorus is removed in the form of water-insoluble phosphorus salt through flocculation precipitation. The process has the defects that a large amount of ferrous sulfate and hydrogen peroxide are required to be added, so that the cost is increased and a large amount of solid waste is generated.

CN208717118U discloses an evaporation method, which uses the characteristic that the boiling point of the organic phosphorus is higher than that of water, and leaves the organic phosphorus in the residue by adopting the evaporation method; the water is distilled out in a gas phase form, and the condensed water almost contains no organic phosphorus or has low organic phosphorus content. The disadvantage of this process is the high operating costs and the considerable amount of hazardous waste generated by the kettle residues.

For this purpose, the present invention is proposed.

Disclosure of Invention

The first aim of the invention is to provide a complexing agent composition for treating photo-initiator TPO production wastewater, which can extract and separate phosphorus-containing organic matters and phosphorus-free organic acids and other toxic pollutants in the TPO production wastewater, has low COD of the wastewater after complexing extraction, has higher removal rate of pollutants than the prior art, and can recycle the water after complexing extraction for production process.

The second aim of the invention is to provide a method for treating waste water in the production of photo-initiator TPO by using the complexing agent composition, which can remarkably reduce COD in the waste water, has high pollutant removal rate, low treatment cost and simple process, can realize serialization and has wide application prospect.

In order to achieve the above object, the present invention provides the following technical solutions.

A complexing agent composition comprising, in percent by volume: 10% -50% of complexing agent, 5% -25% of cosolvent and the balance of diluent;

the complexing agent is one or more of N, N-dialkyl acetamide, trialkyl phosphate and tertiary amine.

The complexing agent composition provided by the invention can be used for treating the wastewater generated in the production of the photoinitiator TPO.

The complexing agent composition of the present invention is a complexing agent that reacts with the organic contaminant under acidic conditions. When the wastewater treatment agent is used for treating the photo-initiator TPO production wastewater, the TPO production wastewater is regulated to be acidic, preferably the pH value is regulated to be 2-4, and organic pollutants are separated and extracted in an organic phase, so that the wastewater is purified, and the COD is reduced.

The N, N-dialkylacetamide may be one or more of N, N-diheptylacetamide, N-dioctylacetamide and N, N-dinonylacetamide. The heptyl, octyl or nonyl radicals are each independently of the other a straight-chain alkyl or branched alkyl radical.

The trialkyl phosphate may be trimethyl phosphate, triethyl phosphate, tripropyl phosphate, tributyl phosphate, tripentyl phosphate or trihexyl phosphate, preferably tripropyl phosphate or tributyl phosphate, most preferably tributyl phosphate.

The tertiary amine may be a trialkylamine, such as a tri (C) ₇ -C ₁₀ Alkyl) amines or trioctylamines, and the like.

Preferably, the complexing agent is two or more of N, N-dialkylacetamide, trialkyl phosphate and tertiary amine.

More preferably, the complexing agent is a mixture of one or both of N, N-dialkylacetamide and tertiary amine with trialkyl phosphate.

Particularly preferably, the complexing agent is a mixture of N, N-dialkylacetamide and trialkyl phosphate, or a mixture of tertiary amine and trialkyl phosphate.

In some embodiments, the complexing agent is a mixture of tributyl phosphate with one or more of N, N-diheptylacetamide, N-dioctylacetamide, and N, N-dinonylacetamide, such as a mixture of N, N-diheptylacetamide, N-dioctylacetamide, N-dinonylacetamide, and tributyl phosphate.

In some embodiments, the complexing agent is a mixture of trioctylamine and tributyl phosphate.

Unexpectedly, the inventors have found that the use of a nitrogen-containing complexing agent in combination with tributyl phosphate can significantly improve contaminant removal compared to the use of either a nitrogen-containing compound or tributyl phosphate alone as the complexing agent.

Organic materials separated using the complexing agent compositions of the present invention include phosphorus-containing organic materials and phosphorus-free organic acids and other toxic contaminants including, for example, diphenyl phosphonic acid, phenylphosphonic acid, diphenyl phosphine oxide, 2,4, 6-trimethylbenzoic acid.

In some embodiments, the complexing agent is present in an amount of 15% to 35% by volume. In other embodiments, the complexing agent is present in an amount of 18% to 32% by volume. The proper complexing agent content can improve the removal rate of toxic pollutants on one hand and control the treatment cost in a lower range on the other hand.

The cosolvent may be one or more of the isomeric alcohols having 8-18 carbon atoms, and may be, for example, isodecanol, isononanol, isooctanol, isoundecanol, isododecanol, isotridecanol, or a mixture thereof. The cosolvent is favorable for uniform dispersion of the complexing agent, so that the utilization rate of the complexing agent is improved, and the reaction rate is also improved.

In some embodiments, the co-solvent is present in an amount of 8% to 20% by volume. In other embodiments, the co-solvent is present in an amount of 9.5% to 18.5% by volume.

The diluent is used to dissolve the complexing agent. In order to improve the solubility of the complexing agent and promote the complex extraction reaction, the diluent can be one or more of alkanes with 8-20 carbon atoms. The alkane having 8 to 20 carbon atoms may be, for example, a C8 alkane, a C9 alkane, a C10 alkane, a C11 alkane, a C12 alkane, a C13 alkane, a C14 alkane, a C15 alkane, a C16 alkane, a C17 alkane, a C18 alkane, a C19 alkane or a C20 alkane, and may be a straight chain alkane or a branched alkane, taking the solubility of the complexing agent as a main consideration.

In some embodiments, the diluent comprises a C10 alkane and a C18 alkane. In other embodiments, the diluent comprises a C8 alkane and a C16 alkane. These alkanes may be straight chain alkanes or branched alkanes.

In addition, the diluent may vary depending on the complexing agent, for example where the complexing agent is a single complexing agent, it is preferred to employ a single type of alkane, if a mixed complexing agent, preferably a mixed alkane.

The invention also provides a method for treating the waste water generated in the production of the photo-initiator TPO by utilizing the complexing agent composition, which comprises the following steps:

regulating the pH of the photo-initiator TPO production wastewater to 2-4, adding the complexing agent composition, mixing, reacting, standing for layering to obtain an upper extraction phase and a lower aqueous phase;

adjusting the pH of the water phase to 6-10, adding a catalyst and introducing ozone to perform oxidation reaction to obtain oxidized effluent; and

adding a flocculating agent into the oxidized effluent, regulating the pH to 4-10, and removing sediment by filtration or standing sedimentation to obtain clear liquid.

Preferably, the volume ratio of the complexing agent composition to TPO process wastewater is 1 (3-15), preferably 1 (3-9).

The amount of the complexing agent composition used is primarily related to its concentration and is preferably arbitrarily adjusted within the ranges provided above. To increase the reaction rate, various means of mixed mass transfer may be employed including, but not limited to, stirring, sonication, vibration, and the like.

The complexation extraction step of the invention can be carried out in a normal environment without high temperature, high pressure and complex equipment, so the investment cost is very low, and the burden of enterprises can be reduced.

Preferably, the concentration of ozone in the aqueous phase after ozone is introduced is 100-300mg/L, preferably 150-250mg/L, more preferably 150-200mg/L. The oxidation reaction time may be 30-120min. Air may be introduced for 10-30min after the reaction is completed to discharge unreacted ozone.

The catalyst comprises a carrier and an active component, wherein the carrier can be one or more of alumina, silica and zeolite, and the active component can be one of copper, cobalt, silver and copper oxide.

Preferably, the flocculant is an inorganic flocculant or a combination of an inorganic flocculant and an organic flocculant. The inorganic flocculant can be ferric trichloride, polyferric chloride, polyaluminum chloride or aluminum trichloride. The organic flocculant may be Polyacrylamide (PAM).

In some embodiments, an inorganic flocculant is added to the oxidized effluent first, after adjusting the pH to 4-10, a small amount of an organic flocculant is added, and then the precipitate is removed by filtration or settling.

Preferably, after removal of the precipitate, the resulting supernatant is concentrated by evaporation to yield distilled water and salt.

In some embodiments, an alkaline solution is added to the extract phase, and after mixing, the mixture is allowed to stand to separate into layers, with the upper layer being the regenerated complexing agent composition and the lower layer being an organic-containing salt solution. The regenerated complexing agent composition can be recycled for the next complexation extraction, and the cycle is repeated, so that the cost is saved. The alkaline solution can be sodium hydroxide solution, potassium hydroxide solution, ammonia water solution or the like. The volume ratio of the alkaline solution to the extract phase may be 1 (4-10).

The treatment method firstly utilizes the principle of complexation extraction to extract and separate the toxic pollutants such as phosphorus-containing organic matters and non-phosphorus-containing organic acids in the TPO production wastewater, thereby greatly reducing the COD of the wastewater; then the residual organic phosphorus and other toxic organic pollutants are oxidized and decomposed by utilizing the principle of ozone catalytic oxidation, so that the organic phosphorus is completely removed, and the COD of the wastewater is further reduced; after ozone catalytic oxidation, most of organic phosphorus in the wastewater is converted into inorganic phosphorus, and the inorganic phosphorus is removed through flocculation precipitation; the treated wastewater can be evaporated for desalting, and the evaporated water is nontoxic and has good biodegradability; meanwhile, white byproduct salt sodium chloride can be obtained, so that harmlessness and recycling of salt are realized; after the treatment by the process, the distilled water can be recycled for the production process.

Compared with the prior art, the invention has the beneficial effects that:

1. the complexing agent composition can extract and separate phosphorus-containing organic matters and phosphorus-free organic acids and other toxic pollutants in TPO production wastewater, and the wastewater after complexing extraction has low COD, has higher COD removal rate than the prior art, and can be recycled for production process after complexing extraction.

2. The treatment method adopts the complex extraction, ozone oxidation and flocculation dephosphorization combined technology to treat TPO production wastewater, can remarkably reduce the COD of the wastewater, has high pollutant removal rate, and has the total phosphorus removal rate of 95-99.8 percent and the COD removal rate of 85-90 percent; and the treatment cost is low, the process is simple, the continuity can be realized, and the method has wide application prospect. Evaporating to remove salt after flocculating and dephosphorizing, and obtaining distilled water which is colorless and nontoxic and has good biodegradability; meanwhile, byproduct salt sodium chloride can be obtained, so that the harmlessness and recycling of salt are realized.

Detailed Description

In order to make the contents of the present invention more easily understood, the technical scheme of the present invention will be further described with reference to the specific embodiments, but the present invention is not limited thereto. All techniques implemented based on the above description of the invention are intended to be included within the scope of the invention. Unless otherwise indicated, the raw materials and reagents used in the examples were all commercially available. The reagents, instruments or procedures not described herein are those routinely determinable by one of ordinary skill in the art.

Example 1

The wastewater used in this example was the production wastewater of photoinitiator TPO from some chemical plant in Shandong province, and the water quality conditions are shown in Table 1:

TABLE 1 Water quality Condition of photo initiator TPO production wastewater

(1) 200mL of A101 (mixture of N, N-diheptylacetamide, N-dioctyl acetamide and N, N-dinonylacetamide, purchased from Tianjin Dike technology Co., ltd.), 50mL of tributyl phosphate, 150mL of isodecyl alcohol, 600mL of mixed alkane with 10 and 18 carbon atoms (volume ratio 1:1) are taken respectively, uniformly mixed, transparent and uniform in whole, and the complexing agent composition is prepared. Then 1800mL of the photo-initiator TPO production wastewater is measured, the pH is regulated to 2, stirring is started, 200mL of complexing agent composition is added into the wastewater, liquid-liquid mass transfer is carried out for 40min, and standing and layering are carried out. The upper layer extract phase is regenerated; the lower layer is the extracted wastewater.

(2) Neutralizing the wastewater in the step (1) by using 32% NaOH solution, adjusting the pH to about 6, and obtaining clear liquid after neutralization for the next working procedure; selecting a reaction device made of polyethylene, adopting zeolite as a catalyst carrier and copper as a catalyst active ingredient, transferring the wastewater into a gas-liquid reactor, introducing ozone for 120min, introducing air for 30min after the reaction is finished, and removing residual ozone.

(3) And (3) adding 20mL of 10 wt% ferric trichloride solution into the wastewater in the step (2), starting stirring, adjusting the pH value to 8-9 by using 32% NaOH solution, adding a small amount of PAM solution after 5min, slowly stirring for reaction, carrying out suction filtration after reacting for 1h, and filtering out residues to obtain clear liquid.

Detecting and analyzing, wherein the effluent is colorless; COD:1280mg/L, and the removal rate is 88.6%; total phosphorus: 0.2mg/L, and the removal rate is 99.8%. The effluent is desalted by evaporation, and the distilled water B/C=0.42 has good biodegradability; and white byproduct sodium chloride is obtained.

Adding 40mL of 20 wt% sodium hydroxide solution into the extract phase obtained in the step (1), stirring, reacting for 20min, standing for layering for 1h, and recovering the regenerated complexing agent composition as the upper layer for the next complexation extraction, and repeating the cycle. The lower layer is a salt solution containing organic matters.

Example 2

The wastewater used in this example was the same as in example 1, and the specific steps were as follows:

(1) 150mL of N235 (purchased from Shanghai Qihai chemical Co., ltd.), 50mL of tributyl phosphate, 100mL of isodecyl alcohol and 650mL of (1:1) mixed alkane with the carbon number of 8 and 16 are respectively taken, uniformly mixed, and the whole is transparent and uniform, and the complexing agent composition is prepared. Then 1800mL of the photo-initiator TPO production wastewater is measured, alkali is added to adjust the pH to 4, stirring is started, 500mL of complexing agent composition is added to the wastewater, liquid-liquid mass transfer is carried out for 20min, and standing and layering are carried out. The upper layer extract phase is regenerated; the lower layer is the extracted wastewater.

(2) Neutralizing the wastewater in the step (1) by using 32% NaOH solution, adjusting the pH to about 9, and obtaining clear liquid after neutralization for the next working procedure; the method comprises the steps of selecting a polyethylene filler device as a reaction device, adopting silicon dioxide as a catalyst carrier and copper oxide as a catalyst active ingredient, transferring the wastewater into a gas-liquid reactor, and introducing ozone for 90min, wherein the ozone concentration is 150mg/L. And introducing air for 30min after the reaction is finished.

(3) 36mL of 10 wt% polyiron solution is added into the wastewater in the step (2), stirring is started, a small amount of PAM solution is added after pH=6 and 5min, the reaction is slowly stirred, and natural sedimentation is carried out after the reaction for 1h, so that clear liquid is obtained.

Detecting and analyzing, wherein the effluent is colorless; COD:1567mg/L, and the removal rate is 86.1 percent; total phosphorus: 0.15mg/L, and the removal rate is 99.9%. The effluent is desalted by evaporation, and the distilled water B/C=0.46 has good biodegradability; and white byproduct sodium chloride is obtained.

Adding 60mL of 15 wt% sodium hydroxide solution into the extract phase obtained in the step (1), stirring, reacting for 30min, standing for layering for 1h, and recovering the regenerated complexing agent composition as the upper layer for the next complexation extraction, and repeating the cycle. The lower layer is a salt solution containing organic matters.

Example 3

The wastewater used in this example was the production wastewater of photoinitiator TPO from inner Mongolia chemical plant, and the water quality conditions are shown in Table 2:

TABLE 2 Water quality Condition of photo initiator TPO Process wastewater

(1) 250mL of A101, 80mL of tributyl phosphate, 100mL of isodecyl alcohol and 600mL of (1:1) mixed alkane with the carbon atoms of 10 and 18 are respectively taken and uniformly mixed, the whole is transparent and uniform, and the complexing agent composition is prepared. Then 1800mL of the photo-initiator TPO production wastewater is measured, the pH is regulated to 2, stirring is started, 300mL of complexing agent composition is added into the wastewater, liquid-liquid mass transfer is carried out for 30min, and standing and layering are carried out. The upper layer extract phase is regenerated; the lower layer is the extracted wastewater.

(2) Neutralizing the wastewater in the step (1) by using 32% NaOH solution, adjusting the pH value to about 10, and obtaining clear liquid after neutralization for the next working procedure; selecting a reaction device made of polyethylene, adopting ceramic as a catalyst carrier, adopting cobalt as a catalyst active ingredient, transferring the wastewater into a gas-liquid reactor, introducing ozone for 150min, introducing air for 30min after the reaction is finished, and removing residual ozone.

(3) And (3) adding 40mL of 10 wt% polyaluminium chloride solution into the wastewater in the step (2), starting stirring, adjusting the pH value to be 6-7 by using 32% NaOH solution, adding a small amount of PAM solution after 5min, slowly stirring for reaction, carrying out suction filtration after reacting for 1h, and filtering out residues to obtain clear liquid.

Detecting and analyzing, wherein the effluent is colorless; COD:1440mg/L, the removal rate is 89.9%; total phosphorus: 0.4mg/L, and the removal rate is 99.8%. The effluent is desalted by evaporation, and the distilled water B/C=0.45 has good biodegradability; and white byproduct sodium chloride is obtained.

Adding 50mL of 18 wt% sodium hydroxide solution into the extract phase in the step (1), stirring, reacting for 30min, standing for layering for 1h, and recovering the regenerated complexing agent composition as the upper layer for the next complexation extraction and repeating the cycle. The lower layer is a salt solution containing organic matters.

Example 4

The wastewater used in this example was the same as in example 3, and the specific steps were as follows:

(1) 100mL of trioctylamine, 80mL of tributyl phosphate, 150mL of isodecyl alcohol and 650mL of (1:1) mixed alkane with the carbon atoms of 8 and 16 are respectively taken and uniformly mixed, the whole is transparent and uniform, and the complexing agent composition is prepared. Then 1800mL of the photo-initiator TPO production wastewater is measured, alkali is added to adjust the pH to 3, stirring is started, 400mL of complexing agent composition is added to the wastewater, liquid-liquid mass transfer is carried out for 20min, and standing and layering are carried out. The upper layer extract phase is regenerated; the lower layer is the extracted wastewater.

(2) Neutralizing the wastewater in the step (1) by using 32% NaOH solution, adjusting the pH value to about 4, and obtaining clear liquid after neutralization for the next working procedure; the method comprises the steps of selecting a polyethylene filler device as a reaction device, adopting aluminum oxide as a catalyst carrier and silver as a catalyst active ingredient, transferring the wastewater into a gas-liquid reactor, and introducing ozone for 100min, wherein the ozone concentration is 150mg/L. And introducing air for 30min after the reaction is finished.

(3) And (3) adding 40mL of 10 wt% aluminum trichloride solution into the wastewater in the step (2), starting stirring, adjusting the pH=7-8, adding a small amount of PAM solution after 5min, slowly stirring for reaction, and settling after reacting for 1h to obtain clear liquid.

Detecting and analyzing, wherein the effluent is colorless; COD:1763mg/L, the removal rate is 87.7%; the total phosphorus content is 0.3mg/L, and the removal rate is 99.8%. The effluent is desalted by evaporation, and the distilled water B/C=0.45 has good biodegradability; and white byproduct sodium chloride is obtained.

Adding 80mL of 10 wt% sodium hydroxide solution into the extract phase in the step (1), stirring, reacting for 30min, standing for layering for 1h, and recovering the regenerated complexing agent composition as the upper layer for the next complexation extraction and repeating the cycle. The lower layer is a salt solution containing organic matters.

Comparative example 1

The wastewater used in this comparative example was the same as that used in example 1, and the test was conducted without tributyl phosphate to examine the change of COD and total phosphorus in the effluent, and the specific steps were as follows:

(1) 200mL of A101, 150mL of isodecyl alcohol and 600mL of mixed alkane with the carbon number of 10 and 18 (volume ratio of 1:1) are respectively taken and uniformly mixed, the whole is transparent and uniform, and the complexing agent composition is prepared. Then 1800mL of the photo-initiator TPO production wastewater is measured, the pH is regulated to 2, stirring is started, 200mL of complexing agent composition is added into the wastewater, liquid-liquid mass transfer is carried out for 40min, and standing and layering are carried out. The upper layer extract phase is regenerated; the lower layer is the extracted wastewater.

Detecting and analyzing, wherein the effluent is colorless; COD:3392mg/L, and the removal rate is 69.9%; total phosphorus: 57mg/L and the removal rate is 65 percent. The effluent is desalted by evaporation, and the B/C=0.21 of the effluent has poor biochemical property; and white sodium chloride containing organic phosphorus is obtained.

As can be seen from a comparison of example 1 and comparative example 1, example 1 used both a nitrogen-containing complexing agent and tributyl phosphate, whereas comparative example 1 used only a nitrogen-containing complexing agent, the removal rate of example 1 was significantly higher than that of comparative example 1.

The present invention is not limited to the above-mentioned embodiments, and any changes or substitutions that can be easily understood by those skilled in the art within the technical scope of the present invention are intended to be included in the scope of the present invention. Therefore, the protection scope of the present invention shall be subject to the protection scope of the claims.

Claims

1. A method for treating wastewater from the production of a photoinitiator TPO using a complexing agent composition comprising:

regulating the pH of the photo-initiator TPO production wastewater to 2-4, adding a complexing agent composition, mixing and reacting, standing for layering to obtain an upper extract phase and a lower aqueous phase;

adding a flocculating agent into the oxidized effluent, regulating the pH to 4-10, and removing sediment by filtering or standing and settling to obtain clear liquid;

wherein the complexing agent composition comprises the following components in percentage by volume: 10% -50% of complexing agent, 5% -25% of cosolvent and the balance of diluent;

the complexing agent is a mixture of N, N-dialkyl acetamide and trialkyl phosphate or a mixture of tertiary amine and trialkyl phosphate;

the N, N-dialkyl acetamide is one or more of N, N-diheptyl acetamide, N-dioctyl acetamide and N, N-dinonyl acetamide;

the trialkyl phosphate is trimethyl phosphate, triethyl phosphate, tripropyl phosphate, tributyl phosphate, tripentyl phosphate or trihexyl phosphate;

the tertiary amine is triheptanamine, trioctylamine or trinonamine.

2. The method as recited in claim 1, further comprising: after removing the precipitate, the resulting clear liquid was concentrated by evaporation to obtain distilled water and a salt.

3. The method according to claim 1 or 2, further comprising: adding alkaline solution into the extraction phase, mixing, standing for layering, wherein the upper layer is regenerated complexing agent composition, and the lower layer is organic matter-containing salt solution.

4. The process according to claim 1 or 2, wherein the volume ratio of complexing agent composition to TPO process wastewater is 1 (3-15).

5. The method according to claim 1 or 2, characterized in that the concentration of ozone in the aqueous phase after ozone is introduced is 100-300mg/L.

6. The method according to claim 1 or 2, wherein the cosolvent is one or more of isomeric alcohols having 8 to 18 carbon atoms.

7. The method according to claim 1 or 2, wherein the diluent is one or more of alkanes having 8 to 20 carbon atoms.