Process for purifying oxygenates

Abstract

The present application relates to the field of methanol to olefin by-product oxygen-containing compound post-treatment, and discloses a purification method of oxygen-containing compound. The purification method comprises contacting the oxygen-containing compound solution containing aromatic hydrocarbon with an adsorbent for de-aromatization; wherein the adsorbent comprises silicon oxide, aluminum oxide and a metal component, the metal component comprises Ni and Mo; the mass content of silicon oxide is 50-80% based on the total mass of the adsorbent, the mass content of aluminum oxide is 15-35%, and the mass content of the metal component in terms of elements is 1-15%. The method can efficiently and deeply remove the aromatic hydrocarbon in the oxygen-containing compound solution, which is conducive to the recycling of the oxygen-containing compound.

Description

Technical Field

[0001] This invention relates to the field of post-treatment of oxygen-containing compounds as byproducts of methanol-to-olefins production, and specifically to a method for purifying oxygen-containing compounds. Background Technology

[0002] Ethylene and propylene are important basic organic chemical raw materials. Traditional ethylene and propylene production mainly involves processes such as steam cracking and catalytic cracking using petroleum as feedstock. In recent years, MTO technology, which uses coal-based methanol as feedstock, has developed rapidly. MTO refers to the technology of producing ethylene, propylene, and other low-carbon olefins from methanol under the action of a catalyst.

[0003] The MTO process inevitably produces oxygenated compounds such as aldehydes, ketones, alcohols, and ethers as byproducts, which enter the water system and form oxygenated wastewater. How to effectively utilize these oxygenated compounds and reduce the loss of carbon-based components in the raw materials has gradually become a pressing problem in the conversion of oxygenated compounds. To address the low conversion rate of direct reprocessing of oxygenated compounds in existing technologies, catalysts are used to catalyze the conversion of oxygenated compounds into alcohols, which are then returned to the MTO unit to increase the production of ethylene and propylene. This achieves efficient utilization of oxygenated compounds. However, the aromatics contained in these compounds are easily adsorbed onto the catalyst surface, reducing catalyst activity and significantly shortening catalyst lifespan. Therefore, there is an urgent need to develop a method capable of deeply removing aromatics from oxygenated compounds. Summary of the Invention

[0004] The purpose of this invention is to overcome the problems existing in the prior art and provide a method for purifying oxygen-containing compounds. This method can efficiently and deeply remove aromatic hydrocarbons from oxygen-containing compound solutions, which is beneficial for the subsequent recovery and reuse of the oxygen-containing compounds.

[0005] To achieve the above objectives, the present invention provides a method for purifying oxygen-containing compounds, the method comprising contacting an oxygen-containing compound solution containing aromatic hydrocarbons with an adsorbent to remove aromatic hydrocarbons;

[0006] The adsorbent comprises silicon dioxide, aluminum oxide, and a metal component, wherein the metal component comprises Ni and Mo; based on the total mass of the adsorbent, the mass content of silicon dioxide is 50-80%, the mass content of aluminum oxide is 15-35%, and the mass content of the metal component (based on elemental composition) is 1-15%.

[0007] The beneficial effects of the present invention through the above technical solution include:

[0008] The method provided by this invention uses an adsorbent with a specific composition, which can efficiently reduce the aromatic hydrocarbons in oxygen-containing compound solutions to a low level, which is beneficial for the subsequent recovery and utilization of oxygen-containing compounds.

[0009] Moreover, the adsorbent described in this invention has good stability and still has good activity after 500 hours of continuous operation. Detailed Implementation

[0010] The endpoints and any values ​​of the ranges disclosed herein are not limited to the precise ranges or values, and these ranges or values ​​should be understood to include values ​​close to these ranges or values. For numerical ranges, the endpoint values ​​of the various ranges, the endpoint values ​​of the various ranges and individual point values, and individual point values ​​can be combined with each other to obtain one or more new numerical ranges, which should be considered as specifically disclosed herein.

[0011] The present invention provides a method for purifying oxygen-containing compounds, the method comprising contacting an oxygen-containing compound solution containing aromatic hydrocarbons with an adsorbent to remove aromatic hydrocarbons;

[0012] The adsorbent comprises silicon dioxide, aluminum oxide, and a metal component, wherein the metal component comprises Ni and Mo; based on the total mass of the adsorbent, the mass content of silicon dioxide is 50-80%, the mass content of aluminum oxide is 15-35%, and the mass content of the metal component (based on elemental composition) is 1-15%.

[0013] According to the present invention, preferably, based on the total mass of the adsorbent, the mass content of silicon dioxide is 60-80%, the mass content of aluminum oxide is 15-30%, and the mass content of the metal component (based on elemental composition) is 3-10%. Adsorbents with the specific composition described in this invention exhibit high aromatic hydrocarbon removal rates and operational stability.

[0014] The content of each component in the adsorbent described in this invention was measured using an inductively coupled plasma atomic emission spectrometer (ICP), model Varian725-ES.

[0015] According to the present invention, preferably, the mass ratio of Ni to Mo is 1-6:1, more preferably 2-4:1. This preferred embodiment is beneficial for improving the activity of the adsorbent and achieving a higher aromatic hydrocarbon removal rate.

[0016] The mass ratio of Ni to Mo in the adsorbent of the present invention was measured and calculated using an inductively coupled plasma atomic emission spectrometer (ICP) of model Varian725-ES.

[0017] Characterized by NH3-TPD, the peak temperature of the desorption curve of the adsorbent corresponds to a temperature between 80-160℃, preferably between 80-120℃. Using this preferred embodiment, the adsorbent possesses suitable acid strength, resulting in good adsorption performance for aromatic hydrocarbons.

[0018] The NH3-TPD characterization process described in this invention specifically includes: weighing 0.2g of sample and purging at 300℃ for 1h under a He atmosphere, then cooling to 50℃, introducing a 10% NH3 / He mixed gas for adsorption until saturation, switching to a He atmosphere for purging for 1h to remove physically adsorbed NH3 on the surface. Finally, desorption is performed under a He atmosphere, with the desorption temperature increasing from 100℃ to 500℃, to obtain the NH3-TPD adsorption-desorption curve. In the desorption curve, the temperature corresponding to the peak value of the desorption peak represents the acid strength.

[0019] According to the present invention, preferably, the specific surface area of ​​the adsorbent is 230-450 m². 2 / g, specifically 230m 2 / g、250m 2 / g、300m 2 / g, 350m 2 / g、400m 2 / g、450m 2 / g, and the range of values ​​formed by any two of these point values.

[0020] According to the present invention, preferably, the pore volume of the adsorbent is 0.3-1.2 cm³. 3 / g, specifically 0.3cm 3 / g, 0.4cm 3 / g, 0.5cm 3 / g, 0.6cm 3 / g, 0.7cm 3 / g, 0.8cm 3 / g, 0.9cm 3 / g, 1cm 3 / g, 1.1cm 3 / g, 1.2cm 3 / g, and the range of values ​​formed by any two of these point values.

[0021] According to the present invention, preferably, the average pore size of the adsorbent is 5-50 nm, specifically 5 nm, 10 nm, 15 nm, 20 nm, 25 nm, 30 nm, 35 nm, 40 nm, 45 nm, 50 nm, and a range of any two of these values.

[0022] The average pore size, specific surface area, and pore volume of the adsorbent described in this invention were tested using the static nitrogen adsorption method (BET) on a Micromeritics ASAP-2020 surface area and pore structure analyzer. The method is as follows: the sample (approximately 0.1-0.2 g) was degassed under vacuum at 300 °C for 5 h, and then N2 adsorption and desorption tests were performed at liquid nitrogen temperature (-196 °C). The specific surface area of ​​the sample was obtained by processing the N2 adsorption curve using the BET equation, and the pore volume was calculated using the single-point method.

[0023] This invention does not impose any particular limitation on the preparation method of the adsorbent, as long as an adsorbent with the above-mentioned composition and characteristic parameters can be obtained. To further improve the adsorption performance of the adsorbent, and also to better illustrate the preparation of the adsorbent, this invention also provides a method for preparing the adsorbent.

[0024] According to the present invention, preferably, the method for preparing the adsorbent includes the following steps:

[0025] S1. The silicon-aluminum composite carrier is modified to obtain a modified silicon-aluminum composite carrier; the modifier used in the modification treatment is selected from at least one amino-containing organic compound.

[0026] S2. Metal components are introduced into the modified silicon-aluminum composite carrier obtained in S1 by impregnation.

[0027] The method described in this invention, which involves first modifying the silicon-aluminum composite support and then introducing metal components, is beneficial for enhancing the interaction between the metal components and the composite support, avoiding the loss of metal ions during the adsorption process, and significantly improving the stability of the adsorbent.

[0028] The present invention allows for a wide range of choices for the modifier. Preferably, the modifier is selected from at least one of p-aminobenzoic acid, triethanolamine, ethylenediamine, triethylamine, hexamethylenetetramine, diethanolamine, triethylenediamine, diethylenediamine, and 2-amino-3-hydroxypropionic acid; more preferably, it is selected from at least one of triethanolamine, diethanolamine, triethylenediamine, and ethylenediamine. This preferred embodiment enhances the interaction between metal ions and the support, prevents the loss of metal ions during adsorption, and improves the stability of the adsorbent.

[0029] According to the present invention, preferably, the modifier is provided in solution form.

[0030] According to the present invention, preferably, the concentration of the modifier solution is 1-20 wt%, more preferably 5-15 wt%. In the present invention, controlling the concentration of the modifier solution within the above-mentioned preferred range is more conducive to improving the interaction between the carrier and the metal component.

[0031] According to the present invention, preferably, the solid-liquid mass ratio of the silicon-aluminum composite carrier to the modifier solution is 1:2-6.

[0032] This invention allows for a wide range of solvent choices in the modifier solution, which can be conventional choices in the art. In this embodiment, water is preferably used as the solvent.

[0033] According to the present invention, preferably, the modification process in S1 includes: mixing the silicon-aluminum composite carrier with the modifier solution and performing hydrothermal treatment, followed by drying.

[0034] The mixing process of the above-mentioned silicon-aluminum composite carrier and modifier solution can be carried out by ultrasonication, stirring and other operations to achieve uniform mixing.

[0035] According to the present invention, preferably, the conditions for the hydrothermal treatment include: a temperature of 80-200℃, more preferably 100-160℃; and a time of 4-20h, more preferably 8-16h.

[0036] The present invention does not have any particular limitation on the drying step of the modification process described in S1, and can be carried out with reference to conventional methods in the art. The present invention will not describe it in detail here.

[0037] The modification process described in S1 further includes: performing solid-liquid separation and washing steps before drying the hydrothermal reaction product.

[0038] The present invention does not particularly limit the method of solid-liquid separation, and conventional technical means in the field can be used.

[0039] The present invention does not have any particular limitation on the washing method, and it can be carried out with reference to conventional methods in the art.

[0040] According to a specific embodiment of the present invention, the hydrothermal reaction product is cooled to room temperature, and then solid-liquid separation and washing steps are performed sequentially.

[0041] The present invention does not have any particular limitation on the source of the silicon-aluminum composite carrier. It can be prepared by conventional methods in the art or obtained directly by commercial purchase, with the adsorbent having the above composition and characteristic parameters as the standard.

[0042] The present invention does not particularly limit the method for introducing metal components onto the modified silicon-aluminum composite carrier, and various methods conventionally used in the art can be employed. Preferably, in S2, the metal components are introduced onto the modified silicon-aluminum composite carrier obtained in S1 by impregnation.

[0043] According to the present invention, preferably, the S2 process includes: impregnating the modified silicon-aluminum composite carrier obtained in S1 in an impregnation solution containing a metal component compound, and then drying and calcining it.

[0044] The present invention does not impose any particular limitation on the order of introducing Ni and Mo into the metal component in step S2; they can be introduced together or separately.

[0045] The present invention does not specifically limit the method of impregnation. The method of impregnation can be impregnation with excess liquid or impregnation with equal volume, depending on the amount of impregnation liquid used.

[0046] The present invention does not have a particular limitation on the number of times the immersion is performed; it can be performed once or multiple times, as long as the mass content of the metal component in the adsorbent is within the above-mentioned range.

[0047] This invention does not impose a particular limitation on the impregnation temperature; it can be carried out using conventional methods, such as at room temperature. Similarly, this invention does not impose a particular limitation on the impregnation time, as long as the required amount of metal component is loaded onto the modified silicon-aluminum composite carrier. Once the required impregnation amount and conditions are determined, a suitable impregnation time can be easily selected. This invention does not impose a particular limitation on the impregnation environment; it can be carried out under sealed conditions or in an open environment using conventional methods in the art.

[0048] The present invention allows for a wide range of choices for the types of metal component compounds, which can be conventional choices in the art, as long as they contain a metal component. Preferably, the metal component compound is an oxide of a metal component and / or a soluble salt of a metal component.

[0049] Preferably, the soluble salt of the metal component is selected from at least one of the metal component's nitrate, chloride, and sulfate.

[0050] In this invention, "soluble" means that it can be directly dissolved in a solvent, or dissolved in a solvent with the help of a co-solvent.

[0051] Preferably, in the impregnation solution containing the metal component compound, the molar concentration of Ni is 0.2-3 mol / L and the molar concentration of Mo is 0.02-1 mol / L.

[0052] This invention offers a wide range of solvent options for impregnating compounds containing metal components, representing conventional choices in the field. In this embodiment, water is preferably used as the solvent.

[0053] The drying described in S2 can be carried out using conventional methods in the art, which will not be described in detail here.

[0054] The roasting described in S2 of this invention can be carried out using conventional methods in the art. Preferably, the roasting conditions in S2 include: a temperature of 400-600℃ and a time of 3-10 hours.

[0055] The method described in this invention achieves a high aromatic hydrocarbon removal rate. Preferably, the aromatic hydrocarbon removal process results in an aromatic hydrocarbon removal rate of not less than 99% in the oxygenated compound solution containing aromatic hydrocarbons.

[0056] This invention offers a wide range of operating conditions for the aromatic removal process, which can be appropriately selected based on specific circumstances, ensuring that the aromatic removal rate in the oxygen-containing compound solution is not less than 99%. Preferably, the aromatic removal operating conditions include: a temperature of 80-120℃, a pressure of 0.1-0.6 MPa, and a mass hourly space velocity (HHSV) of 0.5-5 h⁻¹. -1 .

[0057] According to the present invention, preferably, the aromatic hydrocarbon includes at least one selected from toluene, ethylbenzene, trimethylbenzene, tetramethylbenzene, pentamethylbenzene, hexamethylbenzene and methylnaphthalene.

[0058] According to the present invention, preferably, the oxygen-containing compound includes at least one of ketones, aldehydes, ethers and alcohols, more preferably at least one of acetone, butanone, pentanone, hexanone, methanol, ethanol, propanol, isopropanol, acetaldehyde, propionaldehyde, butanone and pentanone.

[0059] According to the present invention, preferably, in the oxygen-containing compound solution, the water content is 20-75% by mass, more preferably 50-70%; the aromatic hydrocarbon content is 0.1-5% by mass, more preferably 1-3%; and the oxygen-containing compound content is 20-75% by mass, more preferably 25-45%.

[0060] The present invention will be described in detail below through embodiments.

[0061] The preparation examples described in this invention are used to illustrate the preparation of adsorbents.

[0062] Preparation Example 1

[0063] Weigh out an average pore size of 10 nm and a specific surface area of ​​260 m². 2 / g, pore volume 0.8cm 3 / g, bulk density is 0.5g / cm³ 3 10g of a spherical silicon-aluminum composite carrier was added to 50ml of a 10wt% ethylenediamine aqueous solution and stirred for 1h. Then it was transferred to a hydrothermal reactor and hydrothermally reacted at 120℃ for 10h. After naturally cooling to room temperature, it was filtered, washed three times with ultrapure water, and dried overnight at 80℃ to obtain the modified silicon-aluminum composite carrier.

[0064] The modified silicon-aluminum composite carrier was immersed in an aqueous solution of nickel nitrate with a nickel ion concentration of 0.8 mol / L and ammonium molybdate with a molybdenum ion concentration of 0.2 mol / L at room temperature for 24 h, then dried at 110 °C for 12 h and calcined at 500 °C for 6 h to obtain the adsorbent. Its composition and characteristic parameters are shown in Table 1.

[0065] Preparation Example 2

[0066] Weigh out an average pore size of 10 nm and a specific surface area of ​​260 m². 2 / g, pore volume 0.8cm 3 / g, bulk density is 0.5g / cm³ 3 10g of a spherical silicon-aluminum composite carrier was added to 50ml of a 5wt% triethylenediamine aqueous solution and stirred for 1 hour. Then, it was transferred to a hydrothermal reactor and reacted at 150℃ for 8 hours. After naturally cooling to room temperature, it was filtered, washed three times with ultrapure water, and dried overnight at 80℃ to obtain the modified silicon-aluminum composite carrier.

[0067] The modified silicon-aluminum composite carrier was immersed in an aqueous solution of nickel nitrate (0.6 mol / L) and ammonium molybdate (0.2 mol / L) at room temperature for 24 h, then dried at 110 °C for 12 h and calcined at 500 °C for 6 h to obtain the adsorbent. Its composition and characteristic parameters are shown in Table 1.

[0068] Preparation Example 3

[0069] Weigh out an average pore size of 10 nm and a specific surface area of ​​260 m². 2 / g, pore volume 0.8cm 3 / g, bulk density is 0.5g / cm³ 3 10g of a spherical silicon-aluminum composite carrier was added to 30ml of a 10wt% triethanolamine aqueous solution and stirred for 1h. Then it was transferred to a hydrothermal reactor and hydrothermally reacted at 130℃ for 12h. After naturally cooling to room temperature, it was filtered, washed three times with ultrapure water, and dried overnight at 80℃ to obtain the modified silicon-aluminum composite carrier.

[0070] The modified silicon-aluminum composite carrier was immersed in an aqueous solution of nickel nitrate with a nickel ion concentration of 0.6 mol / L and ammonium molybdate with a molybdenum ion concentration of 0.5 mol / L at room temperature for 24 h, then dried at 110 °C for 12 h and calcined at 500 °C for 6 h to obtain the adsorbent. Its composition and characteristic parameters are shown in Table 1.

[0071] Preparation Example 4

[0072] Weigh out an average pore size of 10 nm and a specific surface area of ​​260 m². 2 / g, pore volume 0.8cm 3 / g, bulk density is 0.5g / cm³ 3 The spherical silicon-aluminum composite carrier was immersed in an aqueous solution of nickel nitrate with a nickel ion concentration of 0.8 mol / L and ammonium molybdate with a molybdenum ion concentration of 0.2 mol / L at room temperature for 24 h, and then dried at 110 °C for 12 h and calcined at 500 °C for 6 h to obtain the adsorbent. Its composition and characteristic parameters are shown in Table 1.

[0073] Comparative Preparation Example 1

[0074] The preparation method was carried out in accordance with Example 1, except that the modified silicon-aluminum composite carrier was immersed at room temperature in an aqueous solution of nickel nitrate with a nickel ion concentration of 2 mol / L and ammonium molybdate with a molybdenum ion concentration of 1 mol / L.

[0075] The adsorbent was obtained, and its composition and characteristic parameters are shown in Table 1.

[0076] Table 1

[0077]

[0078] Note: A refers to the temperature corresponding to the peak value of the desorption peak in the desorption curve of the adsorbent characterized by NH3-TPD.

[0079] The embodiments described in this invention illustrate a method for purifying oxygen-containing compound solutions.

[0080] Example 1

[0081] The adsorbent prepared in Example 1 was placed in a fixed-bed reactor to conduct adsorption experiments on aromatic hydrocarbons in an oxygen-containing compound solution. The composition of the oxygen-containing compound solution was: water 60 wt%, aromatic hydrocarbons (toluene, ethylbenzene, xylene, trimethylbenzene) 1.5 wt%, acetone 20 wt%, butanone 10 wt%, and acetaldehyde 8.5 wt%. The reactor was operated at a temperature of 100 °C, a pressure of 0.4 MPa, and a mass hourly space velocity (HHSV) of 1 h⁻¹. -1 The adsorption experiment was conducted for 500 hours under the specified conditions, and the adsorption results are shown in Table 2.

[0082] Example 2

[0083] The adsorbent prepared in Example 1 was placed in a fixed-bed reactor to conduct adsorption experiments on aromatic hydrocarbons in an oxygen-containing compound solution. The composition of the oxygen-containing compound solution was: water 65 wt%, aromatic hydrocarbons (toluene, trimethylbenzene, tetramethylbenzene, pentamethylbenzene, methylnaphthalene) 2 wt%, acetone 10 wt%, methanol 15 wt%, butanone 5 wt%, and ethanol 3 wt%. The reactor was operated at a temperature of 110 °C, a pressure of 0.4 MPa, and a mass hourly space velocity (HHSV) of 1.5 h⁻¹. -1 The adsorption experiment was conducted for 500 hours under the specified conditions, and the adsorption results are shown in Table 2.

[0084] Examples 3-5, Comparative Example 1

[0085] The procedure was carried out according to Example 1, except that the adsorbents prepared in Preparation Examples 2-4 and Comparative Preparation Example 1 were used. The adsorption results are shown in Table 2.

[0086] Table 2

[0087] Example number Removal rate of aromatics from oxygen-containing compound solutions, % Example 1 99.8 Example 2 99.3 Example 3 99.5 Example 4 99.7 Example 5 68.5 Comparative Example 1 92.7

[0088] As can be seen from the results in Table 2, the method of the present invention has a significantly better dearomatic effect. Furthermore, the catalyst provided in the embodiments of the present invention still exhibits good activity after 500 hours of continuous operation, indicating that the catalyst described in the present invention has high stability.

[0089] The preferred embodiments of the present invention have been described in detail above; however, the present invention is not limited thereto. Within the scope of the inventive concept, various simple modifications can be made to the technical solutions of the present invention, including combinations of various technical features in any other suitable manner. These simple modifications and combinations should also be considered as the content disclosed in the present invention and are all within the protection scope of the present invention.

Claims

1. A method for purifying oxygen-containing compounds, characterized in that, The purification method includes contacting an oxygen-containing compound solution containing aromatics with an adsorbent to remove aromatics; The adsorbent comprises silicon dioxide, aluminum oxide, and a metal component, wherein the metal component comprises Ni and Mo; based on the total mass of the adsorbent, the mass content of silicon dioxide is 50-80%, the mass content of aluminum oxide is 15-35%, and the mass content of the metal component (based on elemental composition) is 1-15%.

2. The purification method according to claim 1, wherein, Based on the total mass of the adsorbent, the mass content of silicon dioxide is 60-80%, the mass content of aluminum oxide is 15-30%, and the mass content of metal components (calculated as elements) is 3-10%. Preferably, the mass ratio of Ni to Mo is 1-6:1, more preferably 2-4:

1.

3. The purification method according to claim 1 or 2, wherein, Characterized by NH3-TPD, the temperature corresponding to the peak value of the desorption peak in the desorption curve of the adsorbent is between 80-160℃, preferably between 80-120℃. Preferably, the specific surface area of ​​the adsorbent is 230-450 m². 2 / g; Preferably, the pore volume of the adsorbent is 0.3-1.2 cm³. 3 / g; Preferably, the average pore size of the adsorbent is 5-50 nm.

4. The purification method according to any one of claims 1-3, wherein, The method for preparing the adsorbent includes the following steps: S1. The silicon-aluminum composite carrier is modified to obtain a modified silicon-aluminum composite carrier; the modifier used in the modification treatment is selected from at least one amino-containing organic compound. S2. Metal components are introduced into the modified silicon-aluminum composite carrier obtained in S1 by impregnation.

5. The purification method according to claim 4, wherein, The modifier is selected from at least one of p-aminobenzoic acid, triethanolamine, ethylenediamine, triethylamine, hexamethylenetetramine, diethanolamine, triethylenediamine, diethylenediamine and 2-amino-3-hydroxypropionic acid, more preferably selected from at least one of triethanolamine, diethanolamine, triethylenediamine and ethylenediamine.

6. The purification method according to claim 4, wherein, The modifier is provided in solution form; Preferably, the concentration of the modifier solution is 1-20 wt%, more preferably 5-15 wt%. Preferably, the solid-liquid mass ratio of the silicon-aluminum composite carrier to the modifier solution is 1:2-6.

7. The purification method according to claim 6, wherein, The modification process described in S1 includes: mixing the silicon-aluminum composite carrier with the modifier solution and performing hydrothermal treatment, followed by drying; Preferably, the conditions for the hydrothermal treatment include: a temperature of 80-200℃, more preferably 100-160℃; and a time of 4-20h, more preferably 8-16h.

8. The purification method according to any one of claims 1-7, wherein, The aromatic removal process ensures that the aromatic removal rate in the oxygen-containing compound solution is not less than 99%. Preferably, the dearomatics removal operating conditions include: a temperature of 80-120°C, a pressure of 0.1-0.6 MPa, and a mass hourly space velocity of 0.5-5 h⁻¹. -1 .

9. The purification method according to any one of claims 1-8, wherein, The aromatic hydrocarbon includes at least one of toluene, ethylbenzene, trimethylbenzene, tetramethylbenzene, pentamethylbenzene, hexamethylbenzene, and methylnaphthalene; Preferably, the oxygen-containing compound includes at least one of ketones, aldehydes, ethers, and alcohols, and more preferably includes at least one of acetone, butanone, pentanone, hexanone, methanol, ethanol, propanol, isopropanol, acetaldehyde, propionaldehyde, butanone, and pentanone.

10. The purification method according to any one of claims 1-9, wherein, In the oxygen-containing compound solution, the water content is 20-75% by mass, preferably 50-70%; the aromatic hydrocarbon content is 0.1-5% by mass, preferably 1-3%; and the oxygen-containing compound content is 20-75% by mass, preferably 25-45%.

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