Concentration process of extraction section in hydrogen peroxide production

Abstract

The invention discloses a concentration process for hydrogen peroxide production extraction reaction, and belongs to the technical field of hydrogen peroxide production. The technical problem to be solved is that in an existing extraction process for producing hydrogen peroxide through an anthraquinone method, the concentration of hydrogen peroxide obtained through extraction is low, and the requirement of the market for high-concentration hydrogen peroxide is difficult to meet. According to the technical scheme, the concentration process of the extraction section in hydrogen peroxide production is characterized by comprising the following steps: pumping an acidic pure water extraction agent and a working solution into an extraction tower according to a flow rate ratio of 1: (53-60), carrying out reverse mass transfer extraction separation, and enriching acidic components to obtain hydrogen peroxide; the acidity of the acidic pure water extraction agent is 0.25-0.35 g / L, and the temperature is 50-55 DEG C; the working solution is a mixture of anthraquinone, heavy aromatics and a polar solvent.

Description

TECHNICAL FIELD

[0001] The application belongs to the technical field of hydrogen peroxide production, and particularly relates to a concentration process of an extraction section in hydrogen peroxide production. BACKGROUND

[0002] For understanding the technical content of the present application: As a green chemical product, hydrogen peroxide almost does not cause pollution in the production and use process, and is therefore praised as a model of "clean" chemical products. With excellent oxidation, bleaching, disinfection, deoxidation performance, and unique role as an initiator and crosslinking agent in polymer synthesis, it is widely used in many fields such as chemical industry, papermaking, environmental protection, electronics, food, medicine, textile, mining, and agricultural waste processing, and becomes an indispensable key additive in the production and operation of various industries.

[0003] At present, the production of hydrogen peroxide mainly adopts anthraquinone synthesis process. Compared with the traditional electrolysis method, the anthraquinone method exhibits significant advantages of lower energy consumption and lower cost in the production process, and is easier to realize large-scale industrial production, so it becomes the mainstream technical route.

[0004] Retrieved relevant non-patent literatures: The journal name or book name is "Journal of Ningde Teachers College (Natural Science Edition)", the document name is "Intermediate control analysis in production of hydrogen peroxide by anthraquinone method", the volume number is the 32nd volume, the first issue, and the publication date is March 2020. The literature discloses that the anthraquinone method process mainly includes: dissolving 2-ethylanthraquinone into an organic solution containing heavy aromatic hydrocarbons and tri-octyl phosphate as a working solution, and carrying out hydrogenation treatment in a hydrogenation fixed bed; after filtration and cooling, air is introduced into an oxidation tower to carry out oxidation reaction to generate an oxidation liquid containing anthraquinone and H2O2; the oxidation liquid is subjected to countercurrent extraction in an extraction tower to obtain hydrogen peroxide with a concentration of about 27.5%-35.0%, and finally introduced into a purification tower for purification to obtain the product.

[0005] Retrieved relevant patent literatures: The publication country is China, the publication number is CN114671409A, and the publication date is March 14, 2022. The literature discloses a method for producing hydrogen peroxide in full acidity, which comprises the following steps: a hydrogenation section: hydrogenation reaction of working solution and hydrogen gas under palladium catalysis in a hydrogenation tower to obtain hydrogenation working solution containing hydrogenanthraquinone; an oxidation section: adding phosphoric acid to the hydrogenation working solution obtained in the hydrogenation section and flowing into an oxidation tower, and introducing air into the oxidation tower to generate oxidation reaction to generate hydrogen peroxide and anthraquinone; an extraction section: extracting the reaction product obtained in the oxidation section with water to obtain hydrogen peroxide aqueous solution; a purification section: adding heavy aromatic hydrocarbons to the hydrogen peroxide aqueous solution to obtain hydrogen peroxide.

[0006] The existing technology represented by the literature at least has the following unsolved technical problems or defects: The concentration of hydrogen peroxide produced by the above process is only 27.5%-35.0%, which is difficult to meet the market demand for high-concentration hydrogen peroxide. Therefore, it is particularly urgent and necessary to develop and apply a new concentration process for the extraction section in hydrogen peroxide production in view of the problems existing in the prior art.

[0007] In solving the above problems or overcoming the above defects, the following difficulties and obstacles were encountered: (1) The acidity and temperature of the acidic pure water extractant are the core parameters affecting the stability and mass transfer efficiency of hydrogen peroxide, and there is a complex interaction between them: when the acidity is lower than 0.25 g / L, the acidic environment is not enough to maintain the stability of hydrogen peroxide, which is easy to decompose in the extraction process, and the mass transfer power will be significantly weakened; while the acidity is higher than 0.35 g / L, although the mass transfer effect can be enhanced, excessive acid will accelerate the oxidative decomposition of hydrogen peroxide, which will lead to the decrease of the final concentration. In terms of temperature, if it is lower than 50℃, the molecular movement rate of the two phases is slow, and the mass transfer efficiency is low; if it is higher than 55℃, the thermal stability of hydrogen peroxide will decrease sharply, and the decomposition rate will increase greatly. Therefore, it is necessary to accurately define the synergistic range of acidity (0.25-0.35 g / L) and temperature (50-55℃) to balance the mass transfer efficiency and the stability of hydrogen peroxide, which needs to be verified by a large number of experiments. During the research and development process, the contradictions of "increasing the mass transfer efficiency but increasing the decomposition rate at the same time" or "meeting the stability standard but failing to improve the concentration" occur many times, which is the primary obstacle to be overcome.

[0008] (2) The flow rate ratio of acidic pure water extractant to working fluid (1:53-60) needs to be strictly controlled, which is the key to realizing the high efficiency of reverse mass transfer. If the flow rate ratio is less than 1:53 (i.e. the proportion of extractant is too high), although the extraction amount of hydrogen peroxide can be increased to a certain extent, excessive extractant will cause excessive mixing of the two phases in the tower, which is easy to cause "liquid overflow" phenomenon, i.e. the extractant cannot be clarified in time in the separation section, and forms an emulsion state with the working fluid, which reduces the separation effect, and also increases the energy consumption of the subsequent concentration process; if the flow rate ratio is greater than 1:60 (i.e. the proportion of working fluid is too high), the contact time of the extractant and the working fluid will be insufficient, which will cause the hydrogen peroxide to be unable to fully migrate from the working fluid to the extractant, resulting in the increase of the residual amount of hydrogen peroxide in the raffinate phase, which directly restricts the improvement of the extraction concentration.

[0009] (3) The concentration effect of the present application is not dependent on the optimization of a single parameter, but on the synergistic effect of multiple parameters such as acidity, temperature, flow rate ratio, etc. For example, even if the working fluid composition and flow rate ratio are up to standard, if the temperature of the extractant deviates from the range of 50-55℃, it will still lead to a decrease in the concentration of hydrogen peroxide. In the early stage of research and development, due to the lack of understanding of the correlation between parameters, only a single parameter is adjusted (such as simply increasing the acidity), resulting in large fluctuations in the overall effect, and even the case of "local parameter optimization but overall concentration not improved". Therefore, a large number of experiments are required to finally realize the synergistic regulation of multiple parameters, which is a time-consuming process and a key difficulty to be overcome. SUMMARY

[0010] The present application aims to provide: A concentration process for the extraction section in hydrogen peroxide production, and related technologies, to solve the technical problems or their combinations in the existing anthraquinone method for producing hydrogen peroxide, such as the low concentration of hydrogen peroxide extracted, which is difficult to meet the market demand for high-concentration hydrogen peroxide.

[0011] Term explanation: Unless otherwise defined, all technical terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which the subject matter of the claims belongs. Unless otherwise indicated, all patents, patent applications, publications, and other references cited herein are incorporated by reference in their entirety. If there is a plurality of definitions for a term herein, the definition in this section prevails.

[0012] It should be understood that the above brief summary and the following detailed description are exemplary and are intended to explain, but not limit, the subject matter of the present application. In the present application, the singular also includes the plural unless specifically stated otherwise. It should also be noted that "or" is used as "and / or" unless otherwise indicated. In addition, the term "comprise" and other forms such as "comprises" and "comprising" are not limiting.

[0013] The definition of standard chemical terms can be found in the reference "Hydrogen Peroxide Production Technology", Chemical Industry Press, January 2012, 1st edition.

[0014] Unless otherwise specified, conventional methods within the scope of the art are used, such as methods for detecting extraction concentration.

[0015] Unless a specific definition is provided, the use of each type of commercially available product used herein is in accordance with standard techniques. For example, the manufacturer's instructions for the use of a kit or according to well-known methods in the art or the instructions of the present application can be used. In general, the above-mentioned techniques and methods can be carried out according to conventional methods well known in the art, according to the description in the multiple summary and more specific literature cited and discussed in the present specification.

[0016] The term "optionally" or "optionally" means that the event or circumstance subsequently described can or can not occur, and the description includes the occurrence of the event or circumstance and the non-occurrence of the event or circumstance. For example, according to the definition below: "the anthraquinone includes any one or more of 2-ethyl anthraquinone, 2-butyl anthraquinone, 2-pentyl anthraquinone" means "the anthraquinone is 2-ethyl anthraquinone"; or "the anthraquinone is 2-butyl anthraquinone"; or "the anthraquinone is a mixture of 2-ethyl anthraquinone and 2-butyl anthraquinone"; or "the anthraquinone is a mixture of 2-ethyl anthraquinone, 2-butyl anthraquinone and 2-pentyl anthraquinone".

[0017] The term "hydrogen peroxide" used herein, also known as hydrogen peroxide or H2O2, refers to: a green chemical product, with the performance of oxidation, bleaching, disinfection, etc., widely used in many fields, is the target product of the process of the invention.

[0018] The term "reverse mass transfer extraction separation" used herein refers to: the acid pure water extractant and the working liquid are pumped into the extraction tower at a certain flow rate ratio, and flow in opposite directions, and material transfer is realized in the contact process, so that hydrogen peroxide is transferred from the working liquid to the extractant.

[0019] The term "flow rate ratio" used herein refers to: the flow rate ratio of the acid pure water extractant and the working liquid, which is 1:53-60 in the invention.

[0020] The term "acid regulator" used herein refers to: a substance used to adjust the acidity of pure water to prepare an acid pure water extractant.

[0021] The term "heavy aromatic hydrocarbon" used herein refers to: a class of organic compounds composed of multiple benzene rings, whose molecular structure usually contains benzene rings and other carbon-hydrogen groups. The molecular formula of heavy aromatic hydrocarbon is usually represented as CnH (2n-6), where n represents the number of benzene rings.

[0022] The term "polar solvent" used herein refers to: a polar solvent refers to a solvent containing a polar group.

[0023] The term "extraction tower" used herein refers to: the equipment for realizing the extraction of hydrogen peroxide, which is internally provided with 56 layers of stainless steel sieve plates (3-5 mesh aperture per layer) to provide a place for two-phase reverse mass transfer.

[0024] The term "flood" used herein refers to: when the flow rate ratio of the extractant and the working liquid is not appropriate (such as the extractant accounts for a high proportion), the two phases are excessively mixed in the extraction tower and cannot be normally separated.

[0025] In the first aspect, the present application provides a concentration process for an extraction section in hydrogen peroxide production, the concentration process comprising the following steps: pumping an acidic pure water extractant and a working liquid into an extraction tower at a flow rate ratio of 1:53-60, countercurrent mass transfer extraction separation, and enrichment of acidic components to obtain hydrogen peroxide.

[0026] Among them, the technical features include: acidic pure water extractant, working liquid, flow rate ratio, extraction tower, etc.

[0027] Among them, the acidity of the technical feature acidic pure water extractant is 0.25-0.35 g / L.

[0028] Among them, the acidity of the technical feature acidic pure water extractant is preferably 0.25-0.26 g / L, 0.26-0.27 g / L, 0.27-0.28 g / L, 0.28-0.29 g / L, 0.29-0.30 g / L, 0.30-0.31 g / L, 0.31-0.32 g / L, 0.32-0.33 g / L, 0.33-0.34 g / L or 0.34-0.35 g / L.

[0029] Among them, the acidity of the technical feature acidic pure water extractant is further preferably 0.30-0.31 g / L, 0.31-0.32 g / L, 0.32-0.33 g / L, 0.33-0.34 g / L or 0.34-0.35 g / L.

[0030] Among them, the acidity of the technical feature acidic pure water extractant is still further preferably 0.30 g / L.

[0031] Among them, the temperature of the technical feature acidic pure water extractant is 50-55°C.

[0032] Among them, the temperature of the technical feature acidic pure water extractant is preferably 50-51°C, 51-52°C, 52-53°C, 53-54°C or 54-55°C.

[0033] Among them, the temperature of the technical feature acidic pure water extractant is further preferably 52-53°C, 53-54°C or 54-55°C.

[0034] Among them, the temperature of the technical feature acidic pure water extractant is still further preferably 55°C.

[0035] Among them, the preparation method of the technical feature acidic pure water extractant is to add an acidic regulator to pure water and heat to obtain an acidic pure water extractant.

[0036] Among them, the technical feature pure water is pure water with an electrical conductivity of ≤1 μS / cm.

[0037] Among them, the technical feature acidic regulator is phosphoric acid.

[0038] wherein the technical feature acid regulator is further preferably phosphoric acid at 20-40% v / v.

[0039] wherein the technical feature acid regulator is further preferably phosphoric acid at 30% v / v.

[0040] wherein the technical feature working solution is a mixture of anthraquinone, heavy aromatic hydrocarbon and polar solvent.

[0041] wherein the technical feature anthraquinone includes but is not limited to any one or more of 2-ethylanthraquinone, 2-butylanthraquinone, 2-pentylanthraquinone.

[0042] wherein the technical feature anthraquinone is preferably 2-ethylanthraquinone.

[0043] wherein the technical feature heavy aromatic hydrocarbon includes but is not limited to any one or more of cumene, n-propylbenzene, ethyltoluene, mesitylene, cymene, o-cymene, tetramethylbenzene, naphthalene, methylnaphthalene.

[0044] wherein the technical feature heavy aromatic hydrocarbon is preferably mesitylene.

[0045] wherein the technical feature polar solvent includes but is not limited to any one or more of trioctyl phosphate, 2-methylcyclohexyl acetate, acetic acid ester, tetrabutyl urea, diisobutyl carbinol.

[0046] wherein the technical feature polar solvent is preferably trioctyl phosphate and acetic acid ester.

[0047] wherein the technical feature working solution is preferably a mixture of 2-ethylanthraquinone, mesitylene, trioctyl phosphate and acetic acid ester.

[0048] wherein the technical feature preparation method of the working solution comprises: S1, mixing mesitylene, trioctyl phosphate and acetic acid ester according to a volume ratio to obtain a mixed solvent; S2, adding 2-ethylanthraquinone into the mixed solvent and mixing to obtain the working solution.

[0049] wherein the volume ratio of mesitylene, trioctyl phosphate and acetic acid ester in step S1 is 70-80: 10-15: 10-15.

[0050] wherein the volume ratio of mesitylene, trioctyl phosphate and acetic acid ester in step S1 is preferably 70-71, 71-72, 72-73, 73-74, 74-75, 75-76, 76-77, 77-78, 78-79 or 79-80: 10-11, 11-12, 12-13, 13-14 or 14-15: 10-11, 11-12, 12-13, 13-14 or 14-15.

[0051] The volume ratio of the mesitylene, the trioctyl phosphate, and the acetic acid ester in step S1 is further preferably 80:10:10.

[0052] The ratio of the 2-ethylanthraquinone to the mixed solvent in step S2 is 125-135 g:1 L.

[0053] The ratio of the 2-ethylanthraquinone to the mixed solvent in step S2 is preferably 125-126 g:1 L, 126-127 g:1 L, 127-128 g:1 L, 128-129 g:1 L, 129-130 g:1 L, 130-131 g:1 L, 131-132 g:1 L, 132-133 g:1 L, 133-134 g:1 L, or 134-135 g:1 L.

[0054] The ratio of the 2-ethylanthraquinone to the mixed solvent in step S2 is further preferably 130 g:1 L.

[0055] The ratio of the 2-ethylanthraquinone to the mixed solvent in step S2 is further preferably 130 g:1 L.

[0056] The ratio of the 2-ethylanthraquinone to the mixed solvent in step S2 is further preferably 130 g:1 L.

[0057] The ratio of the 2-ethylanthraquinone to the mixed solvent in step S2 is further preferably 130 g:1 L. 3

[0058] The ratio of the 2-ethylanthraquinone to the mixed solvent in step S2 is further preferably 130 g:1 L. 3 3 3 3

[0059] The ratio of the 2-ethylanthraquinone to the mixed solvent in step S2 is further preferably 130 g:1 L. 3

[0060] The ratio of the 2-ethylanthraquinone to the mixed solvent in step S2 is further preferably 130 g:1 L. 3

[0061] The ratio of the 2-ethylanthraquinone to the mixed solvent in step S2 is further preferably 130 g:1 L. 3 3 3 ​​​​​​​​​ / h, 830-840 m 3 / h, 840-850 m 3 / h, 850-860 m 3 / h, 860-870 m 3 / h, 870-880 m 3 / h, 880-8900 m 3 / h or 890-900 m 3 / h.

[0062] wherein the flow rate of the technical feature working fluid is further preferably 850 m 3 / h.

[0063] wherein the technical feature extraction column is provided with 56 layers of stainless steel sieve plates, and each layer of sieve plate is distributed with 3-5 mesh apertures.

[0064] Based on further solving or simultaneously solving multiple technical problems of the technical problems of the present application, in the technical solution provided in the first aspect of the present application, the preferred scheme comprises: The first preferred scheme: the acidity of the acidic pure water extractant is 0.30-0.31 g / L, 0.31-0.32 g / L, 0.32-0.33 g / L, 0.33-0.34 g / L or 0.34-0.35 g / L. Based on solving the technical problem "the concentration of hydrogen peroxide extracted in the existing extraction process for producing hydrogen peroxide by anthraquinone method is low, which is difficult to meet the market demand for high-concentration hydrogen peroxide", the technical solution further solves the technical problem "the lack of acidic environment leads to poor stability and easy decomposition of hydrogen peroxide during extraction, and weak mass transfer power, which affects the extraction efficiency".

[0065] The second preferred scheme: the temperature of the acidic pure water extractant is 52-53℃, 53-54℃ or 54-55℃. Based on solving the technical problem "the concentration of hydrogen peroxide extracted in the existing extraction process for producing hydrogen peroxide by anthraquinone method is low, which is difficult to meet the market demand for high-concentration hydrogen peroxide", the technical solution further solves the technical problem "unsuitable temperature leads to slow molecular motion rate and low mass transfer efficiency, or hydrogen peroxide thermal stability decreases and decomposition rate increases".

[0066] The third priority scheme: the flow rate ratio of the acidic pure water extractant and the working liquid is 1:53-54, 1:54-55, 1:55-56, 1:56-57, 1:57-58, 1:58-59 or 1:59-60. On the basis of solving the technical problem that the concentration of the extracted hydrogen peroxide is low in the existing extraction process for producing hydrogen peroxide by the anthraquinone method, and it is difficult to meet the market demand for high-concentration hydrogen peroxide, the technical problem that the improper flow rate ratio causes the "liquid overflow" phenomenon, the separation effect is reduced, the energy consumption of the subsequent concentration process is increased, or the contact time between the extractant and the working liquid is insufficient, resulting in high residual hydrogen peroxide, is further solved.

[0067] Examples 1-3 in the present application at least support the protection scope of claim 1.

[0068] For claim 1: The technical feature "the acidity of the acidic pure water extractant is 0.25-0.35 g / L" is generalized from the aforementioned explanations and / or the corresponding technical features 0.35 g / L, 0.25 g / L, 0.30 g / L, etc. in examples 1-3 through the common feature "0.25-0.35 g / L". Therefore, a person skilled in the art can reasonably infer that the technical feature "the acidity of the acidic pure water extractant is 0.25-0.35 g / L", the lower concept of "the acidity of the acidic pure water extractant is 0.25-0.35 g / L", the basically equivalent technical means of "the acidity of the acidic pure water extractant is 0.25-0.35 g / L", and the technical means of "the acidity of the acidic pure water extractant is 0.25-0.35 g / L" that can be replaced within the conventional technical means and common knowledge based on the existing technical level, should all belong to the protection scope of claim 1, for example, the acidity of the acidic pure water extractant is 0.26 g / L, 0.27 g / L, etc. under the condition that other technical features remain unchanged, which still belongs to the protection scope of claim 1 of the present application.

[0069] The technical feature "the temperature of the acidic pure water extractant is 50-55℃" is generalized from the aforementioned explanations and / or the corresponding technical features 52℃, 50℃, 55℃, etc. in examples 1-3 through the common feature "50-55℃". Therefore, a person skilled in the art can reasonably infer that the technical feature "the temperature of the acidic pure water extractant is 50-55℃", the lower concept of "the temperature of the acidic pure water extractant is 50-55℃", the basically equivalent technical means of "the temperature of the acidic pure water extractant is 50-55℃", and the technical means of "the temperature of the acidic pure water extractant is 50-55℃" that can be replaced within the conventional technical means and common knowledge based on the existing technical level, should all belong to the protection scope of claim 1, for example, the temperature of the acidic pure water extractant is 51℃, 53℃, 54℃, etc. under the condition that other technical features remain unchanged, which still belongs to the protection scope of claim 1 of the present application.

[0070] The technical feature "working liquid is a mixture of anthraquinone, heavy aromatic hydrocarbon and polar solvent" is summarized by the common feature "anthraquinone, heavy aromatic hydrocarbon and polar solvent are mixed according to the volume ratio" from the aforementioned explanation and / or the corresponding technical features of the preparation of working liquid in Examples 1-3. Therefore, the person skilled in the art can reasonably infer that the lower concept of the technical feature "working liquid is a mixture of anthraquinone, heavy aromatic hydrocarbon and polar solvent", the basic equivalent technical means of the technical feature "working liquid is a mixture of anthraquinone, heavy aromatic hydrocarbon and polar solvent", and the replaceable technical means of the technical feature "working liquid is a mixture of anthraquinone, heavy aromatic hydrocarbon and polar solvent" based on the existing technical level within the conventional technical means and common knowledge should all belong to the protection scope of claim 1, for example, the working liquid is mixed according to the volume ratio of methyl naphthalene, tetrabutyl urea, etc. instead of mesitylene, trioctyl phosphate, acetic acid ester, which still belongs to the protection scope of claim 1 of the present application.

[0071] The technical feature "acidic pure water extractant and working liquid are pumped into the extraction tower at a flow rate ratio of 1:53-60" is summarized by the common feature "acidic pure water extractant and working liquid are pumped into the extraction tower at a flow rate ratio of 1:53-60" from the aforementioned explanation and / or the corresponding technical features of the acidic pure water extractant and working liquid in Examples 1-3. Therefore, the person skilled in the art can reasonably infer that the lower concept of the technical feature "acidic pure water extractant and working liquid", the basic equivalent technical means of the technical feature "acidic pure water extractant and working liquid pumped into the extraction tower at a flow rate ratio of 1:53-60", and the replaceable technical means of the technical feature "acidic pure water extractant and working liquid pumped into the extraction tower at a flow rate ratio of 1:53-60" based on the existing technical level within the conventional technical means and common knowledge should all belong to the protection scope of claim 1, for example, the acidic pure water extractant and working liquid are pumped into the extraction tower at a flow rate ratio of 1:58 instead of 1:53-60, which still belongs to the protection scope of claim 1 of the present application.

[0072] Examples 1 and 3 in the present application at least support the protection scope of claim 2.

[0073] The technical feature "the acidity of the acidic pure water extractant is 0.30-0.35 g / L" is generalized from the corresponding technical features 0.35 g / L, 0.30 g / L, etc. in the foregoing explanations and / or Examples 1 and 3 by the common feature "0.30-0.35 g / L". Therefore, according to a reasonable presumption of a person skilled in the art, it can be determined that the technical feature "the acidity of the acidic pure water extractant is 0.30-0.35 g / L", the lower concept of the acidity of the acidic pure water extractant being 0.30-0.35 g / L, the substantially equivalent technical means of the acidity of the acidic pure water extractant being 0.30-0.35 g / L, and the technical means of the acidity of the acidic pure water extractant being 0.30-0.35 g / L which can be replaced within the conventional technical means and common general knowledge based on the existing technical level, should all belong to the protection scope of claim 2, for example, the acidity of the acidic pure water extractant being 0.30-0.35 g / L is replaced by 0.31 g / L, 0.32 g / L, etc. without changing other technical features, which still belongs to the protection scope of claim 2 of the present application.

[0074] The technical feature "the temperature of the acidic pure water extractant is 52-55 ℃" is generalized from the corresponding technical features 52 ℃, 55 ℃, etc. in the foregoing explanations and / or Examples 1 and 3 by the common feature "52-55 ℃". Therefore, according to a reasonable presumption of a person skilled in the art, it can be determined that the technical feature "the temperature of the acidic pure water extractant is 52-55 ℃", the lower concept of the temperature of the acidic pure water extractant being 52-55 ℃, the substantially equivalent technical means of the temperature of the acidic pure water extractant being 52-55 ℃, and the technical means of the temperature of the acidic pure water extractant being 52-55 ℃ which can be replaced within the conventional technical means and common general knowledge based on the existing technical level, should all belong to the protection scope of claim 2, for example, the temperature of the acidic pure water extractant being 52-55 ℃ is replaced by 53 ℃, 54 ℃, etc. without changing other technical features, which still belongs to the protection scope of claim 22 of the present application.

[0075] Examples 1-3 in the present application at least support the protection scope of claim 3.

[0076] For claim 3: The technical feature "the flow rate of the acidic pure water extractant is 14-16 m 3 / h" is generalized from the corresponding technical features 14 m 3 / h, 15 m 3 / h, 16 m 3 / h, etc. in the foregoing explanations and / or Examples 1-3 by the common feature "14-16 m 3 / h". Therefore, according to a reasonable presumption of a person skilled in the art, it can be determined that the technical feature "the flow rate of the acidic pure water extractant is 14-16 m 3 / h, the flow rate of the acidic pure water extractant is 14-16 m 3 / h, the flow rate of the acidic pure water extractant is 14-16 m 3 / h, the flow rate of the acidic pure water extractant is 14-16 m 3 / h, the flow rate of the acidic pure water extractant is 14-16 m 3 / h is replaced by 14.5 m 3 / h, 15.6 m 3 / h, etc. still belong to the protection scope of claim 3 of the present application.

[0077] The technical feature "the flow rate of the working liquid is 800-900 m 3 / h" is summarized by the aforementioned explanations and / or the corresponding technical features 800 m 3 / h, 900 m 3 / h, 850 m 3 / h, etc. by the common feature "800-900 m 3 / h". Therefore, the skilled in the art can reasonably infer that the technical feature "the flow rate of the working liquid is 800-900 m 3 / h, the flow rate of the working liquid is 800-900 m 3 / h, the flow rate of the working liquid is 800-900 m 3 / h, the flow rate of the working liquid is 800-900 m 3 / h, the flow rate of the working liquid is 800-900 m 3 / h is replaced by 830 m 3 / h, 870 m 3 / h, etc. still belong to the protection scope of claim 3 of the present application.

[0078] The embodiments 1-3 in the present application at least support the protection scope of claim 4.

[0079] For the claim 4: The technical feature "the preparation method of the acidic pure water extractant is: adding an acidic regulator to pure water and heating to obtain an acidic pure water extractant" is generalized by the common feature "adding an acidic regulator to pure water and heating to obtain an acidic pure water extractant" from the aforementioned explanation and / or the corresponding technical feature in Examples 1-3, i.e., the preparation of an acidic pure water extractant: pure water with an electrical conductivity of ≤1 μS / cm is prepared with 30% v / v phosphoric acid. Therefore, a person skilled in the art can reasonably infer that the technical feature "the preparation method of the acidic pure water extractant is: adding an acidic regulator to pure water and heating to obtain an acidic pure water extractant", the subordinate concept of "the preparation method of the acidic pure water extractant is: adding an acidic regulator to pure water and heating to obtain an acidic pure water extractant", the substantially equivalent technical means of "the preparation method of the acidic pure water extractant is: adding an acidic regulator to pure water and heating to obtain an acidic pure water extractant", and the technical means of "the preparation method of the acidic pure water extractant is: adding an acidic regulator to pure water and heating to obtain an acidic pure water extractant" that can be replaced within the conventional technical means and common knowledge based on the existing technical level, all should be within the protection scope of claim 4, for example, the technical feature "the preparation method of the acidic pure water extractant is: adding an acidic regulator to pure water and heating to obtain an acidic pure water extractant" is replaced by "the preparation method of the acidic pure water extractant is: adding carbonic acid to pure water and heating to obtain an acidic pure water extractant", and the like, which still belongs to the protection scope of claim 4 of the present application.

[0080] Examples 1-3 in the present application at least support the protection scope of claim 5.

[0081] The technical feature "the acidic regulator is 30% v / v phosphoric acid" is generalized by the common feature "30% v / v phosphoric acid" from the aforementioned explanation and / or the corresponding technical feature in Examples 1-3, i.e., 30% v / v phosphoric acid. Therefore, a person skilled in the art can reasonably infer that the technical feature "the acidic regulator is 30% v / v phosphoric acid", the subordinate concept of "the acidic regulator is 30% v / v phosphoric acid", the substantially equivalent technical means of "the acidic regulator is 30% v / v phosphoric acid", and the technical means of "the acidic regulator is 30% v / v phosphoric acid" that can be replaced within the conventional technical means and common knowledge based on the existing technical level, all should be within the protection scope of claim 5.

[0082] Examples 1-3 in the present application at least support the protection scope of claim 6.

[0083] The technical feature "anthraquinone" is generalized from the aforementioned explanation herein and / or the corresponding technical feature 2-ethylanthraquinone in Examples 1-3 via the common feature "anthraquinone". Therefore, the anthraquinone described in the technical feature, the lower concept of anthraquinone, the substantially equivalent technical means of anthraquinone, and the technical means of anthraquinone that can be replaced within the conventional technical means and common knowledge based on the existing technical level, should all belong to the protection scope of claim 6, for example, 2-ethylanthraquinone is replaced by any one or more of 2-ethylanthraquinone, 2-butylanthraquinone, 2-pentylanthraquinone, etc., which still belongs to the protection scope of claim 6 of the present application.

[0084] Examples 1-3 in the present application at least support the protection scope of claim 7.

[0085] The technical feature "anthraquinone is 2-ethylanthraquinone" is generalized from the aforementioned explanation herein and / or the corresponding technical feature 2-ethylanthraquinone in Examples 1-3 via the common feature "2-ethylanthraquinone". Therefore, the anthraquinone described in the technical feature, the lower concept of anthraquinone, the substantially equivalent technical means of anthraquinone, and the technical means of anthraquinone that can be replaced within the conventional technical means and common knowledge based on the existing technical level, should all belong to the protection scope of claim 7.

[0086] Examples 1-3 in the present application at least support the protection scope of claim 8.

[0087] The technical feature "heavy aromatic hydrocarbon" is generalized from the aforementioned explanation herein and / or the corresponding technical feature mesitylene in Examples 1-3 via the common feature "heavy aromatic hydrocarbon". Therefore, the heavy aromatic hydrocarbon described in the technical feature, the lower concept of heavy aromatic hydrocarbon, the substantially equivalent technical means of heavy aromatic hydrocarbon, and the technical means of heavy aromatic hydrocarbon that can be replaced within the conventional technical means and common knowledge based on the existing technical level, should all belong to the protection scope of claim 8, for example, mesitylene is replaced by any one or more of cumene, n-propylbenzene, ethyltoluene, mesitylene, m-cymene, o-cymene, p-cymene, naphthalene, methylnaphthalene, etc., which still belongs to the protection scope of claim 8 of the present application.

[0088] Examples 1-3 in the present application at least support the protection scope of claim 9.

[0089] The technical feature "mesitylene" is generalized from the technical features "mesitylene" and / or "mesitylene" in the foregoing explanations and / or embodiments 1-3 by the common feature "mesitylene". Therefore, the skilled person can reasonably conclude that the mesitylene described in the technical feature, the subgeneric concept of mesitylene, the substantially equivalent technical means of mesitylene, and the technical means of mesitylene that can be replaced within the conventional technical means and common general knowledge based on the existing technical level, should all fall within the protection scope of claim 9.

[0090] The embodiments 1-3 in the present application at least support the protection scope of claim 10.

[0091] The technical feature "polar solvent" is generalized from the technical features "trioctyl phosphate" and "acetate" in the foregoing explanations and / or embodiments 1-3 by the common feature "polar solvent". Therefore, the skilled person can reasonably conclude that the polar solvent described in the technical feature, the subgeneric concept of polar solvent, the substantially equivalent technical means of polar solvent, and the technical means of polar solvent that can be replaced within the conventional technical means and common general knowledge based on the existing technical level, should all fall within the protection scope of claim 10, for example, replacing "trioctyl phosphate" and "acetate" with any one or more of "trioctyl phosphate", "2-methylcyclohexyl acetate", "acetate", "tetrabutyl urea", "diisobutyl carbinol", etc., while other technical features remain unchanged, still falls within the protection scope of claim 10 of the present application.

[0092] The embodiments 1-3 in the present application at least support the protection scope of claim 11.

[0093] The technical feature "trioctyl phosphate and acetate" is generalized from the technical features "trioctyl phosphate" and "acetate" in the foregoing explanations and / or embodiments 1-3 by the common feature "trioctyl phosphate and acetate". Therefore, the skilled person can reasonably conclude that the trioctyl phosphate and acetate described in the technical feature, the subgeneric concept of trioctyl phosphate and acetate, the substantially equivalent technical means of trioctyl phosphate and acetate, and the technical means of trioctyl phosphate and acetate that can be replaced within the conventional technical means and common general knowledge based on the existing technical level, should all fall within the protection scope of claim 11.

[0094] The embodiments 1-3 in the present application at least support the protection scope of claim 12.

[0095] The technical feature "the working solution is a mixture of 2-ethylanthraquinone, mesitylene, trioctyl phosphate and acetic acid ester" is summarized by the common feature "the working solution is a mixture of 2-ethylanthraquinone, mesitylene, trioctyl phosphate and acetic acid ester" through the aforementioned explanation and / or the corresponding technical features of mesitylene, trioctyl phosphate and acetic acid ester in examples 1-3 mixed according to the volume ratio to obtain a mixed solvent. Therefore, the skilled person in the art can reasonably infer that the working solution described in the technical feature, the sub-concept of the working solution being a mixture of 2-ethylanthraquinone, mesitylene, trioctyl phosphate and acetic acid ester, the basic equivalent technical means of the working solution being a mixture of 2-ethylanthraquinone, mesitylene, trioctyl phosphate and acetic acid ester, the technical means of replacing the polar solvent based on the existing technical level within the conventional technical means and common knowledge should all belong to the protection scope of claim 12.

[0096] Examples 1-3 in the present application at least support the protection scope of claim 13.

[0097] The technical feature "the preparation method of the working solution" is summarized by the common feature "the preparation method of the working solution" through the aforementioned explanation and / or the corresponding technical features of the preparation of the working solution in examples 1-3: mesitylene, trioctyl phosphate and acetic acid ester are mixed according to the volume ratio to obtain a mixed solvent; 2-ethylanthraquinone is added to the mixed solvent and mixed to obtain the working solution. Therefore, the skilled person in the art can reasonably infer that the sub-concept of the preparation method of the working solution described in the technical feature, the basic equivalent technical means of the preparation method of the working solution, the technical means of replacing the preparation method of the working solution based on the existing technical level within the conventional technical means and common knowledge should all belong to the protection scope of claim 13.

[0098] Examples 1-3 in the present application at least support the protection scope of claim 14.

[0099] The technical feature "volume ratio of mesitylene, trioctyl phosphate, acetic acid ester is 70-80:10-15:10-15" is generalized from the aforementioned explanations and / or the corresponding technical features in embodiments 1-3, i.e. "volume ratio of mesitylene, trioctyl phosphate, acetic acid ester is 70:15:15", "volume ratio of mesitylene, trioctyl phosphate, acetic acid ester is 70:15:15", "volume ratio of mesitylene, trioctyl phosphate, acetic acid ester is 80:10:10". Therefore, according to the reasonable presumption, the technical feature "volume ratio of mesitylene, trioctyl phosphate, acetic acid ester is 70-80:10-15:10-15", the subordinate concept of "volume ratio of mesitylene, trioctyl phosphate, acetic acid ester is 70-80:10-15:10-15", the substantially equivalent technical means of "volume ratio of mesitylene, trioctyl phosphate, acetic acid ester is 70-80:10-15:10-15", and the technical means of the preparation method of "volume ratio of mesitylene, trioctyl phosphate, acetic acid ester is 70-80:10-15:10-15" based on the existing technical level within the conventional technical means and common knowledge, should all belong to the protection scope of claim 14, for example, replacing "volume ratio of mesitylene, trioctyl phosphate, acetic acid ester is 70-80:10-15:10-15" with "volume ratio of mesitylene, trioctyl phosphate, acetic acid ester is 78:10:12" and the like, which still belongs to the protection scope of claim 14 of the present application.

[0100] Embodiments 1-3 in the present application at least support the protection scope of claims 15-16.

[0101] The technical feature "the ratio of 2-ethylanthraquinone to mixed solvent is 125-135 g: 1 L" is summarized by the common feature "125-135 g: 1 L" from the aforementioned explanations and / or the ratio of 2-ethylanthraquinone to mixed solvent in the corresponding technical features in Embodiments 1-3, which is 130 g: 1 L, etc. Therefore, according to a reasonable presumption, the person skilled in the art can determine that the technical feature "the ratio of 2-ethylanthraquinone to mixed solvent is 125-135 g: 1 L", the lower concept of "the ratio of 2-ethylanthraquinone to mixed solvent is 125-135 g: 1 L", the substantially equivalent technical means of "the ratio of 2-ethylanthraquinone to mixed solvent is 125-135 g: 1 L", and the technical means of "the ratio of 2-ethylanthraquinone to mixed solvent is 125-135 g: 1 L" that can be replaced within the conventional technical means and common knowledge based on the prior art level, should all belong to the protection scope of claims 15-16, for example, the flow rate of the working solution is replaced by the ratio of 2-ethylanthraquinone to mixed solvent of 131 g: 1 L, etc., while other technical features remain unchanged, which still belongs to the protection scope of claims 15-16 of the present application.

[0102] The basic embodiment 1 in the present application supports at least the protection scope of claim 17.

[0103] The present application has the following beneficial effects: The present application has at least the following beneficial effects: Compared with the prior art, the present application has better technical effects in improving the extraction concentration of hydrogen peroxide. According to experimental tests, the present application improves the extraction concentration of hydrogen peroxide from 27.5%-35.0% in the prior art to 38.17%-38.94%.

[0104] In addition, based on the present application: Based on the comparison between Embodiment 1 and Comparative Examples 1-5, the present application adopts the technical means of specific acidity of acidic pure water extractant, specific temperature of acidic pure water extractant, and the combination of specific flow rate of acidic pure water extractant and working solution, which achieves the new technical effect of improving the extraction concentration of hydrogen peroxide. The technical effect after combination is more superior than the sum of the effects of each technical means. BRIEF DESCRIPTION OF DRAWINGS

[0105] Figure 1 The extraction concentration process flowchart in the production of hydrogen peroxide described in the present application. DETAILED DESCRIPTION

[0106] The following non-limiting examples can make the ordinary skilled in the art more comprehensive understanding of the present application, but not in any way limit the present application. The following content is only an exemplary description of the scope of the present application, those skilled in the art can make various changes and modifications to the present application according to the disclosed content, and it should also belong to the scope of the present application claimed.

[0107] The present application is further described below in the manner of specific examples. The various instruments, devices, equipment, reagents, products, etc. used in the embodiments of the present application, such as no special description are obtained by conventional commercial channels.

[0108] Basic embodiment 1 The extraction column used in the present application is the equipment for realizing the extraction of hydrogen peroxide, which is internally provided with 56 layers of stainless steel sieve plates (3-5 mesh aperture per layer) to provide a place for two-phase reverse mass transfer.

[0109] Embodiment 1 A concentration process for the extraction section in hydrogen peroxide production, comprising the following steps: S1, preparation of working solution: mixing mesitylene, trioctyl phosphate, and acetate according to a volume ratio of 70:15:15 to obtain a mixed solvent; adding 2-ethylanthraquinone to the mixed solvent and mixing to obtain a working solution; the ratio of 2-ethylanthraquinone to the mixed solvent is 130 g:1 L.

[0110] S2, preparation of acidic pure water extractant: pure water with an electrical conductivity of ≤1 μS / cm is prepared with 30% v / v phosphoric acid, and the volume ratio of pure water to phosphoric acid is 1:0.05, to obtain an acidic pure water extractant with an acidity of 0.35 g / L and a temperature of 52°C.

[0111] S3, the working solution of the oxidation liquid tank is pumped into the extraction column at a speed of 800 m 3 / h; the acidic pure water extractant is pumped into the extraction column at a speed of 14 m 3 / h; the acidic pure water extractant and the working solution in the extraction column are reversely mass transferred and separated at a flow rate ratio of 1:57.14, and the acidic components are enriched to obtain hydrogen peroxide.

[0112] Embodiment 2 A concentration process for the extraction section in hydrogen peroxide production, comprising the following steps: S1, preparation of working solution: mixing mesitylene, trioctyl phosphate, and acetate according to a volume ratio of 70:15:15 to obtain a mixed solvent; adding 2-ethylanthraquinone to the mixed solvent and mixing to obtain a working solution; the ratio of 2-ethylanthraquinone to the mixed solvent is 130 g:1 L.

[0113] S2. Preparation of acidic pure water extractant: Pure water with a conductivity ≤1μS / cm is mixed with 30% v / v phosphoric acid, and the volume ratio of pure water to phosphoric acid is 1:0.03 to obtain an acidic pure water extractant with an acidity of 0.25g / L and a temperature of 50℃.

[0114] S3, the working fluid in the oxidation tank is 900m 3 The acidic pure water extractant is pumped into the extraction tower at a rate of / h; 3 The acidic pure water extractant is pumped into the extraction tower at a rate of / h; the acidic pure water extractant and the working liquid in the extraction tower are separated by countercurrent mass transfer at a flow rate ratio of 1:60, and the acidic components are enriched to obtain hydrogen peroxide.

[0115] Example 3 A concentration process in the extraction stage of hydrogen peroxide production includes the following steps: S1. Preparation of working solution: Trimethylbenzene, trioctyl phosphate, and acetate are mixed in a volume ratio of 80:10:10 to obtain a mixed solvent; 2-ethylanthraquinone is added to the mixed solvent and mixed well to obtain the working solution; the ratio of 2-ethylanthraquinone to the mixed solvent is 130g:1L.

[0116] S2. Preparation of acidic pure water extractant: Pure water with a conductivity ≤1μS / cm is mixed with 30% v / v phosphoric acid, with a volume ratio of pure water to phosphoric acid of 1:0.04, to obtain an acidic pure water extractant with an acidity of 0.30g / L and a temperature of 55℃.

[0117] S3, the working fluid in the oxidation tank is 850m 3 The acidic pure water extractant is pumped into the extraction tower at a rate of / h; 3 The acidic pure water extractant is pumped into the extraction tower at a rate of / h; the acidic pure water extractant and the working liquid in the extraction tower are separated by countercurrent mass transfer at a flow rate ratio of 1:53, and the acidic components are enriched to obtain hydrogen peroxide.

[0118] Comparative Example 1 A concentration process in the extraction stage of hydrogen peroxide production differs from Example 1 only in that step S2 is different. The specific steps are as follows: S2. Preparation of acidic pure water extractant: Pure water with a conductivity ≤1μS / cm is mixed with 30% v / v phosphoric acid, and the volume ratio of pure water to phosphoric acid is 1:0.02 to obtain an acidic pure water extractant with an acidity of 0.20g / L and a temperature of 52℃.

[0119] Comparative Example 2 A concentration process in the extraction stage of hydrogen peroxide production differs from Example 1 only in that step S2 is different. The specific steps are as follows: S2. Preparation of acidic pure water extractant: Pure water with a conductivity ≤1μS / cm is mixed with 30% v / v phosphoric acid, and the volume ratio of pure water to phosphoric acid is 1:0.08 to obtain an acidic pure water extractant with an acidity of 0.50g / L and a temperature of 52℃.

[0120] Comparative Example 3 A concentration process in the extraction stage of hydrogen peroxide production differs from Example 1 only in that step S2 is different. The specific steps are as follows: S2. Preparation of acidic pure water extractant: Pure water with a conductivity ≤1μS / cm is mixed with 30% v / v phosphoric acid, and the volume ratio of pure water to phosphoric acid is 1:0.05 to obtain an acidic pure water extractant with an acidity of 0.35g / L and a temperature of 45℃.

[0121] Comparative Example 4 A concentration process in the extraction stage of hydrogen peroxide production differs from Example 1 only in that step S2 is different. The specific steps are as follows: S2. Preparation of acidic pure water extractant: Pure water with a conductivity ≤1μS / cm is mixed with 30% v / v phosphoric acid, with a volume ratio of pure water to phosphoric acid of 1:0.05, to obtain an acidic pure water extractant with an acidity of 0.35g / L and a temperature of 60℃.

[0122] Comparative Example 5 A concentration process in the extraction stage of hydrogen peroxide production differs from Example 1 only in that step S2 is different. The specific steps are as follows: S2. Preparation of acidic pure water extractant: Pure water with a conductivity ≤1μS / cm is mixed with 30% v / v phosphoric acid, and the volume ratio of pure water to phosphoric acid is 1:0.04 to obtain an acidic pure water extractant with an acidity of 0.50g / L and a temperature of 60℃.

[0123] Comparative Example 6 A concentration process in the extraction stage of hydrogen peroxide production differs from Example 1 only in that step S3 is different. The specific steps are as follows: S3, the working fluid in the oxidation tank is 900m 3 The acidic pure water extractant is pumped into the extraction tower at a rate of / h; 3 The acidic pure water extractant is pumped into the extraction tower at a rate of / h; the acidic pure water extractant and the working liquid in the extraction tower are separated by countercurrent mass transfer at a flow rate ratio of 1:65, and the acidic components are enriched to obtain hydrogen peroxide.

[0124] Comparative Example 7 A concentration process in the extraction stage of hydrogen peroxide production differs from Example 1 only in that step S3 is different. The specific steps are as follows: S3, the working fluid in the oxidation tank is 700m 3The acidic pure water extractant is pumped into the extraction tower at a rate of / h; 3 The acidic pure water extractant is pumped into the extraction tower at a rate of / h; the acidic pure water extractant and the working liquid in the extraction tower are separated by countercurrent mass transfer at a flow rate ratio of 1:50, and the acidic components are enriched to obtain hydrogen peroxide.

[0125] Comparative Example 8 A concentration process in the extraction stage of hydrogen peroxide production differs from Example 1 only in that steps S2 and S3 are different. The specific steps are as follows: S2. Preparation of acidic pure water extractant: Pure water with a conductivity ≤1μS / cm is mixed with 30% v / v phosphoric acid, and the volume ratio of pure water to phosphoric acid is 1:0.08 to obtain an acidic pure water extractant with an acidity of 0.50g / L and a temperature of 60℃.

[0126] S3, the working fluid in the oxidation tank is 700m 3 The acidic pure water extractant is pumped into the extraction tower at a rate of / h; 3 The acidic pure water extractant is pumped into the extraction tower at a rate of / h; the acidic pure water extractant and the working liquid in the extraction tower are separated by countercurrent mass transfer at a flow rate ratio of 1:50, and the acidic components are enriched to obtain hydrogen peroxide.

[0127] Experimental Example 1 The hydrogen peroxide prepared in step S4 of Examples 1-3 and Comparative Examples 1-8 was tested for extraction concentration, and the results are shown in Table 1 below: Table 1

[0128] The above detailed description is a specific illustration of one feasible embodiment of the present invention, and this embodiment is not intended to limit the patent scope of the present invention. It should be noted that all equivalent implementations or modifications made without departing from the present invention should be included within the scope of the technical solution of the present invention. Therefore, the protection scope of the present invention should be determined by the appended claims.

Claims

1. A concentration process in the extraction stage of hydrogen peroxide production, characterized in that, The concentration process includes the following steps: acidic pure water extractant and working solution are pumped into the extraction tower at a flow rate ratio of 1:53-60, and the acidic components are enriched by reverse mass transfer extraction to obtain hydrogen peroxide. The acidic pure water extractant has an acidity of 0.25-0.35 g / L and a temperature of 50-55℃; the working solution is a mixture of anthraquinone, heavy aromatic hydrocarbons, and a polar solvent.

2. The concentration process according to claim 1, characterized in that, The acidic pure water extractant has an acidity of 0.30-0.35 g / L and a temperature of 52-55℃.

3. The extraction process according to claim 1, characterized in that, The flow rate of the acidic pure water extractant is 14-16 m / s. 3 / h; the flow rate of the working fluid is 800-900m / h. 3 / h.

4. The extraction process according to claim 1, characterized in that, The method for preparing the acidic pure water extractant is as follows: add an acid regulator to pure water and then heat it to obtain the acidic pure water extractant.

5. The extraction process according to claim 4, characterized in that, The acid regulator is 30% v / v phosphoric acid.

6. The extraction process according to claim 1, characterized in that, The anthraquinones mentioned include any one or more of 2-ethylanthraquinone, 2-butylanthraquinone, and 2-pentylanthraquinone.

7. The extraction process according to claim 6, characterized in that, The anthraquinone mentioned is 2-ethylanthraquinone.

8. The extraction process according to claim 1, characterized in that, The heavy aromatic hydrocarbons include any one or more of cumene, n-propylbenzene, ethyltoluene, mesitylene, pseudotrimethylbenzene, o-trimethylbenzene, tetramethylbenzene, naphthalene, and methylnaphthalene.

9. The extraction process according to claim 8, characterized in that, The heavy aromatic hydrocarbon mentioned is mesitylene.

10. The extraction process according to claim 1, characterized in that, The polar solvents include any one or more of trioctyl phosphate, 2-methylcyclohexyl acetate, acetate, tetrabutylurea, and diisobutylmethanol.

11. The extraction process according to claim 10, characterized in that, The polar solvents are trioctyl phosphate and acetate.

12. The extraction process according to claim 1, characterized in that, The working solution is a mixture of 2-ethylanthraquinone, mesitylene, trioctyl phosphate and acetate.

13. The extraction process according to claim 12, characterized in that, The method for preparing the working fluid includes: S1. Mix mesitylene, trioctyl phosphate, and acetate in a volume ratio to obtain a mixed solvent; S2. Add 2-ethylanthraquinone to the mixed solvent and mix well to obtain the working solution.

14. The extraction process according to claim 13, characterized in that, The volume ratio of mesitylene, trioctyl phosphate, and acetate in step S1 is 70-80:10-15:10-15.

15. The extraction process according to claim 13, characterized in that, The ratio of 2-ethylanthraquinone to the mixed solvent in step S2 is 125-135 g: 1 L.

16. The extraction process according to claim 14, characterized in that, The ratio of 2-ethylanthraquinone to the mixed solvent in step S2 is 130 g: 1 L.

17. The extraction process according to claim 1, characterized in that, The extraction tower is equipped with 56 layers of stainless steel sieves, each layer having a pore size of 3-5 mesh.

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