Method and system for preparing electronic grade isopropanol by hydrogenation of acetone

Abstract

The present invention provides a process for preparing isopropanol by hydrogenating acetone, comprising the steps of: (1) introducing an acetone feedstock into an acetone pre-oxidation treater to pre-oxidize impurities and obtain a pre-oxidized acetone feedstock; and (2) introducing the acetone feedstock after pre-oxidation and any intermediate treatments into an acetone hydrogenation reactor to carry out a hydrogenation reaction and obtain a crude isopropanol product.

Description

[Technical Field]

[0001] The present invention relates to the technical field of chemical feedstock preparation, and in particular to a process and system for hydrogenating acetone to prepare electronic grade isopropanol. [Background technology]

[0002] As the semiconductor industry's transition to tertiary industry accelerated in the 21st century, China's integrated circuit market has expanded year by year. Ultra-high-purity reagents (wet electronic chemicals) are important basic functional chemicals in the IC manufacturing process, primarily used for chip cleaning and etching. Their purity and cleanliness have a crucial impact on the yield and reliability of integrated circuits, and the narrower the linewidth of integrated circuits, the higher the quality requirements become. Currently, G3 to G4 grade wet electronic chemicals are used in 8-inch wafer production. However, with the change in processing methods for 12-inch wafers, the amount of wet electronic chemicals used has increased significantly, leading to higher requirements for wet electronic chemical grades, generally G4 to G5 grades.

[0003] Isopropanol is the most widely used organic solvent in wet electronic chemicals, primarily used for cleaning and drying. Isopropanol for integrated circuits has strict requirements regarding trace organic impurity content, metal cation impurity content, particle size and particle number, and anion impurity content. With the continuous breakthrough of advanced integrated circuit process nodes, the demand for high-grade G4 to G5 isopropanol is gradually increasing.

[0004] CN111675598A discloses a production system for preparing electronic-grade isopropanol by hydrogenating acetone, where the electronic-grade isopropanol product is obtained through an acetone hydrogenation unit, a variable-pressure adsorption unit, a distillation unit, and an adsorption filtration unit. However, because this method employs a variable-pressure adsorption separation process, the method is complicated and the measured trace organic impurities in the resulting isopropanol product are not effectively removed, failing to meet the requirements of high-end wafer manufacturing (line width ≤ 90 nm).

[0005] CN102898275A discloses a process for preparing high-purity isopropanol, which involves molecular sieve dehydration, resin dehydration, reverse osmosis, high-temperature distillation, ion exchange, and cyclic adsorption filtration. However, this process does not address the removal of trace organic impurities and cannot meet the cleanliness requirements of wet electronic chemicals used in high-end wafer manufacturing (line widths ≤ 90 nm). Summary of the Invention

[0006] Therefore, one objective of the present invention is to provide a process and system for producing electronic-grade isopropanol by hydrogenating acetone to overcome the problem of ineffective removal of reducing organic impurities in the isopropanol obtained from the production process, which cannot meet the requirements for high-end wafer manufacturing (line width ≦ 90 nm). The organic impurity content of the isopropanol product obtained by this process is low, at 5 ppm or less, and the anion and cation, particle content, water content, etc. can all meet the requirements for high-end wafer manufacturing (line width ≦ 90 nm).

[0007] To this end, the present inventors have conducted extensive research and found that for some specific feedstocks, including acetone feedstocks for the production of electronic-grade isopropanol, particularly when the feedstocks contain specific impurities such as reducing impurities, a specific oxygen-containing metal complex can be used as a pre-oxidant to pretreat the feedstock, which is particularly beneficial for reducing the content of organic impurities in the desired product and meeting various requirements, such as anion and cation content, particle content, and water content.

[0008] In order to achieve the above object, the present invention provides, in one aspect, a process for preparing isopropanol by hydrogenating acetone, characterized in that the process comprises the following steps: (1) introducing the acetone raw material into an acetone pre-oxidation treatment device and pre-oxidizing reducible impurities to obtain a pre-oxidized acetone raw material; (2) introducing the acetone feed into an acetone hydrogenation reactor for hydrogenation reaction to obtain a crude isopropanol product; wherein the acetone feed is the pre-oxidized acetone feed obtained from step (1) or a purified acetone feed obtained by any intermediate treatment (1-2) of the pre-oxidized acetone feed.

[0009] In another aspect, the present invention provides a system for preparing electronic grade isopropanol by hydrogenating acetone, the system comprising: an acetone pre-oxidation processor used to perform step (1) of the process of the present invention to obtain a pre-oxidized acetone feedstock; and an acetone hydrogenation unit used to carry out step (2) of the process of the present invention to obtain a crude isopropanol product; and optionally An acetone dehydration unit and an acetone purification unit used to carry out the intermediate treatment (1-2) of the process according to any one of the preceding claims.

[0010] Compared with the prior art, the present invention has at least the following beneficial effects: (1) The content of organic reducing impurities in the isopropanol product obtained by the present invention is as low as 5 ppm or less, and the anion and cation, particle content, water content, etc. can all meet the requirements for high-end wafer manufacturing (line width ≦ 90 nm); (1-2) The raw material used in the present invention is acetone, which is inexpensive and readily available. Electronic-grade isopropanol can be produced through an acetone purification unit, an acetone hydrogenation unit, and an isopropanol purification unit. The entire process is simple and has high added value. (2) The acetone purification unit used in the present invention has mild reaction conditions and good oxidation effect, with almost no loss of raw acetone, complete removal of reducing impurities, and little by-product generation; (3) The present invention is cleverly designed to remove organic impurities that are difficult to separate from isopropanol in the acetone purification unit, thereby avoiding the difficulty of separation from isopropanol and the large energy consumption in the subsequent stages. [Brief explanation of the drawings]

[0011] [Figure 1] 1 is a system for hydrogenating acetone to produce electronic grade isopropanol, in accordance with a preferred embodiment of the present invention. DETAILED DESCRIPTION OF THE INVENTION

[0012] [Table 1]

[0013] The range endpoints and any values ​​disclosed herein are not intended to be limited to the exact ranges or values, and these ranges or values ​​should be understood to include values ​​close to these ranges or values. For numerical ranges, the range endpoints, range endpoints, and individual point values ​​can be combined with each other to create one or more new numerical ranges, which should be considered specifically disclosed herein.

[0014] The "acetone feedstock" of the present invention includes the target substance (acetone) and impurities. For further processing or application, it is necessary to carry out appropriate treatment such as purification to improve the purity of the target feedstock and / or to facilitate further processing or application of the target feedstock. In the present invention, the acetone feedstock particularly refers to the acetone feedstock used for hydrogenation to produce isopropanol (particularly electronic grade isopropanol).

[0015] In one aspect, the present invention provides a process for preparing isopropanol by hydrogenating acetone, the process being characterized in that it comprises: (1) introducing the acetone raw material into an acetone pre-oxidation treatment vessel to pre-oxidize reducing impurities to obtain a pre-oxidized acetone raw material; (2) introducing the acetone feed into an acetone hydrogenation reactor for hydrogenation reaction to obtain a crude isopropanol product; wherein the acetone feed is the pre-oxidized acetone feed obtained from step (1), or the pre-oxidized acetone feed is optionally subjected to intermediate treatment (1-2) to obtain a purified acetone feed.

[0016] According to an exemplary embodiment of the present invention, an intermediate treatment (1-2) is performed between step (1) and step (2), and the intermediate treatment (1-2) includes sequentially introducing the pre-oxidized acetone feedstock into an acetone dehydration device and an acetone purification device to dehydrate the acetone and purify the acetone to obtain a purified acetone feedstock.

[0017] According to an exemplary embodiment of the present invention, the process of the present invention further includes a step (3) of post-treating the crude isopropanol product: passing the crude isopropanol product sequentially through an isopropanol dehydration unit, an isopropanol purification unit, and an adsorption filtration unit to perform isopropanol dehydration, isopropanol purification, and at least one type of isopropanol adsorption filtration to obtain electronic-grade isopropanol.

[0018] Thus, for example, as shown in FIG. 1, in one aspect, the present invention provides a process for preparing electronic grade isopropanol by hydrogenating acetone, the process comprising: (1) introducing the acetone raw material into an acetone pre-oxidation treatment unit R1 and pre-oxidizing reducible impurities to obtain a pre-oxidized acetone raw material; (1-2) introducing the pre-oxidized acetone into an acetone dehydration device and an acetone purification device in sequence to dehydrate and purify the acetone, thereby obtaining a purified acetone raw material; (2) introducing the purified acetone raw material as an acetone feed into an acetone hydrogenation reactor R2 for hydrogenation reaction to obtain a crude isopropanol product; (3) Passing the crude isopropanol product through an isopropanol dehydration unit, an isopropanol purification unit, and an adsorption filtration unit in sequence to perform isopropanol dehydration, isopropanol purification, and at least one type of isopropanol adsorption filtration to obtain electronic grade isopropanol.

[0019] According to the present invention, a purified acetone feedstock can be obtained by pre-oxidizing an inexpensive and readily available acetone feedstock, dehydrating the acetone, and purifying the acetone. This purified acetone feedstock can then be used in a hydrogenation reaction to produce a crude isopropanol product. The crude isopropanol product can then be subjected to simple dehydration, purification, and at least one adsorption filtration to produce an isopropanol product with an organic reducing impurity content of 5 ppm or less, and with anions, cations, particle content, and water content that meet the requirements for high-end wafer manufacturing (line widths ≤ 90 nm). The present invention removes organic impurities from the acetone feedstock that are difficult to separate from isopropanol, thereby avoiding the drawbacks of difficult separation from isopropanol and the resulting high energy consumption in downstream processes.

[0020] According to the present invention, the form of the pre-oxidation is not limited as long as the object of the present invention can be achieved. In some preferred embodiments, pre-oxidation is carried out by contacting the acetone raw material with a pre-oxidizing agent in step (1). By adopting the above embodiment, reducing impurities in acetone can be effectively removed.

[0021] According to the present invention, there are no limitations on the pre-oxidation conditions as long as the object of the present invention can be achieved. In some embodiments, the pre-oxidation conditions in step (1) include adding a pre-oxidizing agent in an amount of 0.01 to 0.1% by weight of the acetone feedstock, for example, 0.01%, 0.02%, 0.03%, 0.04%, 0.05%, 0.08%, or 0.1%. By employing the above embodiment, reducing impurities in the acetone feedstock can be removed.

[0022] In some embodiments of the present invention, the pre-oxidation conditions include room temperature and atmospheric pressure, which allows for mild pre-oxidation conditions, good oxidation effect, little loss of raw material acetone, complete removal of reducing impurities, and minimal by-products.

[0023] In the present invention, room temperature refers to a temperature of 10 to 30°C.

[0024] According to the present invention, the type of pre-oxidant is not limited as long as the objectives of the present invention can be achieved. In some preferred embodiments, the pre-oxidant comprises an oxygen-containing metal complex; more preferably, the oxygen-containing metal complex has a transition metal element as a central atom and an oxygen-containing heterocyclic organic compound containing a substituent as a ligand. By employing the above-mentioned embodiment, reducing impurities in acetone can be effectively removed, thereby reducing the generation of excess impurities in the subsequent isopropanol preparation process.

[0025] According to the present invention, the type of transition metal element is not limited as long as the object of the present invention can be achieved. In some embodiments, the transition metal element is selected from one or more of chromium, molybdenum, tungsten, iron, cobalt, nickel, ruthenium, rhodium, palladium, platinum, manganese, technetium, and rhenium, and preferably one or more of manganese, cobalt, and molybdenum.

[0026] According to the present invention, in some preferred embodiments, the ligand is a compound having the structure shown in formula (I): [ka] In Formula (I), n is an integer from 0 to 5 (e.g., 0, 1, 2, 3, 4, or 5), A is —CH(R5)—; and R1, R2, R3, R4, and R5 are each independently selected from H, C1-C8 alkyl, phenylC1-C8 alkyl, and C1-C8 alkylphenyl.

[0027] According to a preferred embodiment of the present invention, R1, R2, R3, R4 and R (5) are each independently selected from H, C1-C5 alkyl, phenyl C1-C5 alkyl, and C1-C5 alkyl-substituted phenyl, preferably each independently selected from H, C1-C4 alkyl, benzyl, and C1-C3 alkyl-substituted phenyl.

[0028] By adopting the above-described preferred embodiment, it is possible to remove organic impurities that are difficult to separate from isopropanol in the acetone raw material, and to avoid the drawback of the difficulty in separating from isopropanol and the resulting large energy consumption in the downstream stage.

[0029] According to the present invention, when n is 0, A is absent and in that case, formula (I) is a 5-membered ring structure; when n is 1, formula (I) is a 6-membered ring structure, R5 is selected from H, C1-C8 alkyl, phenylC1-C8 alkyl and C1-C8 alkylphenyl, or preferably selected from H, C1-C5 alkyl, benzyl, C1-C3 alkyl-substituted phenyl; when n is 2, A = -CH(R5)-CH(R5), formula (I) is a 7-membered ring structure, and each occurrence of R5 is independently selected from H, C1-C8 alkyl, phenylC1-C8 alkyl and C1-C8 alkylphenyl, or preferably selected from H, C1-C5 alkyl, benzyl, C1-C3 alkyl-substituted phenyl. Similarly, for example: When n is 0, R1 is methyl, R2 is methyl, R3 is H, and R4 is H, the ligand is 2,2-dimethyl-1,3-dioxolane-4,5-dimethanol; When n is 1, R1 is methyl, R2 is H, R3 is H, R4 is H, and R5 is methyl, the ligand is 2,2-dimethyl-1,3-dioxane-4,6-dimethanol; When n is 0, R1 is ethyl, R2 is ethyl, R3 is H, and R4 is H, the ligand is 2,2-diethyl-1,3-dioxolane-4,5-dimethanol.

[0030] Similarly, compounds of formula (I) useful in the present invention also include 2,2-dimethyl-1,3-dioxolane-4,5-di-1-ethanol, 2,2-dimethyl-1,3-dioxolane-4,5-dibenzyl alcohol, and 2,2-dimethyl-1,3-dioxolane-4,5-di-p-methylbenzyl alcohol.

[0031] According to the present invention, in some preferred embodiments, in formula (I), n is an integer of 0 to 3; in some preferred embodiments, R1, R2, R3, and R4 are each independently selected from H, C1-C3 alkyl, benzyl, and methyl-substituted phenyl; in some preferred embodiments, A=CH(R5), and R5 is H or C1-C3 alkyl.

[0032] According to the present invention, the process for preparing an oxygen-containing metal complex is not limited as long as the object of the present invention can be achieved. The oxygen-containing metal complex can be obtained by appropriately selecting a ligand solution containing the ligand of the present invention and a metal salt solution containing the transition metal of the present invention and performing a complex formation reaction. The conditions required for the complex formation reaction are not particularly limited and can be selected appropriately. In some embodiments, the process for preparing an oxygen-containing metal complex includes adding a ligand solution and a metal salt solution in equimolar amounts of the ligand and transition metal under an anhydrous, oxygen-free, nitrogen atmosphere, and stirring at room temperature for 1 to 10 hours to perform the complex formation reaction; in some optional embodiments, the solvent is evaporated after the complex formation reaction.

[0033] According to the present invention, the ligand solution refers to a solution formed by dissolving a ligand in a solvent, generally an organic solvent. The metal salt solution refers to a solution formed by dissolving a metal salt in a solvent, generally water. Since the present invention is not particularly limited, the metal salt solution will not be described in detail in this specification.

[0034] According to the present invention, ligands of different specific structures can be commercially purchased or prepared as needed. For example, in Formula (I), when n is 0, R1 is methyl, R2 is methyl, R3 is H, and R4 is H, the ligand is 2,2-dimethyl-1,3-dioxolane-4,5-dimethanol. The ligand preparation process includes the following: 2,2-dimethoxypropane, dimethyl 2,3-dihydroxysuccinate, p-toluenesulfonic acid, and anhydrous dichloromethane are added sequentially under an anhydrous and oxygen-free nitrogen atmosphere, reacted at 20-100°C for 2-10 hours, and then allowed to cool and evaporate the solvent; under a nitrogen atmosphere, anhydrous methanol and sodium borohydride are added, stirred at room temperature for 5-24 hours, diluted with water, and then the organic solvent is evaporated. The residual liquid is extracted and dried, the organic solvent is filtered and evaporated, and the residue is recrystallized to obtain the ligand.

[0035] The present invention does not go into detail about the source of the ligand. The ligand in the present invention can be purchased commercially as needed, or can be prepared by the same preparation process as 2,2-dimethyl-1,3-dioxolane-4,5-dimethanol, for ligands with different specific structures, which involves changing the raw materials 2-dimethoxypropane and dimethyl 2,3-dihydroxysuccinate, selecting the raw materials to prepare the required ligand, reacting them under the action of p-toluenesulfonic acid, and then carrying out a reduction reaction.

[0036] According to the present invention, in order to increase the activity of the oxygen-containing metal complex, in some embodiments, the pre-oxidant is oxidized with an oxidizing agent prior to the pre-oxidation in step (1).

[0037] According to the present invention, in some preferred embodiments, the oxidizing agent is selected from one or more of oxygen, hydrogen peroxide, cumene peroxide, peracetic acid, perchlorate, permanganate, and dichromate.

[0038] According to the present invention, after the complex formation reaction for preparing an oxygen-containing metal complex is completed, the pre-oxidant can be oxidized by directly adding an oxidizing agent to carry out the oxidation reaction. For example, in some embodiments, a ligand solution and a metal salt solution are added in equimolar amounts of the ligand and the transition metal in an anhydrous and oxygen-free nitrogen atmosphere, and the mixture is stirred at room temperature for 1 to 10 hours to carry out the complex formation reaction. Then, an appropriate amount of an oxidizing agent is added thereto and the mixture is stirred for 1 to 10 hours to carry out the oxidation treatment. The solvent is then evaporated to obtain the oxidized pre-oxidant.

[0039] According to the present invention, in another embodiment, the pre-oxidant can be oxidized by subjecting an oxygen-containing metal complex to an oxidation reaction with an oxidizing agent under oxidizing conditions in the presence of a solvent, followed by evaporation of the solvent to obtain the oxidized pre-oxidant.

[0040] According to the present invention, those skilled in the art can select appropriate oxidation treatment conditions depending on the type of oxidizing agent, and the present invention is not particularly limited thereto.

[0041] According to the present invention, the type of reducing impurity is not limited as long as the objectives of the present invention can be achieved. In some embodiments, the reducing impurity includes at least one of alcohols, aldehydes, ketones, esters, ethers, and olefins. Generally, reducing impurities that can be treated by the process of the present invention are selected from saturated or unsaturated C1-C4 primary or secondary alcohols, such as methanol, ethanol, isopropanol, propenol, and propargyl alcohol; C1-C4 aldehydes, such as formaldehyde, acetaldehyde, and propionaldehyde; C1-C4 alkyl formates, such as methyl formate and ethyl formate; C2-C4 olefins or alkynes, such as ethylene and propylene; and C1-C4 alkyl-substituted phenols, such as C1-C4 alkyl-substituted aniline, phenol, and alkyl-substituted compounds thereof.

[0042] The pre-oxidation of the present invention can efficiently remove reducing impurities such as alcohols, aldehydes, ketones, esters, ethers, and olefins, ultimately obtaining isopropanol whose anion and cation content, particle content, and water content meet the requirements of high-end wafer manufacturing (line width ≦ 90 nm).

[0043] According to the present invention, the source of the acetone raw material is not limited as long as the objectives of the present invention can be achieved. In some embodiments, the acetone raw material includes one or more of industrial grade acetone, analytical grade acetone, and electronic grade acetone.

[0044] According to the present invention, according to the standards in this field, the purity of industrial grade acetone is 95-99.5%, the purity of analytical grade acetone is 99.5-99.9%, and the purity of electronic grade acetone is above 99.9%.

[0045] In the present invention, unless otherwise specified, purity and content refer to purity and content by weight.

[0046] According to some embodiments of the present invention, the dehydration materials used in the dehydration of acetone in step (1-2) and the dehydration of isopropanol in step (3) each include one or more of molecular sieves, silica gel, membranes, resins, and salts capable of forming crystalline hydrates. By employing the above-described embodiments, the water content of the final isopropanol product can meet the requirements for ultra-high purity isopropanol used in the integrated circuit industry.

[0047] According to the present invention, the dehydration material can be selected as needed, and the types of dehydration material will not be detailed herein.

[0048] According to some embodiments of the present invention, in step (1-2), acetone is purified in a plate distillation column or a packed distillation column.

[0049] According to the present invention, there are no limitations on the acetone purification conditions as long as the objectives of the present invention can be achieved. In some embodiments, the acetone purification conditions include an operating reflux ratio of 0.5 to 10; an operating pressure of -0.5 to 10 bar; and an overhead operating temperature of 30 to 70°C.

[0050] According to some preferred embodiments of the present invention, the acetone purification conditions include an operating reflux ratio of 0.5 to 5; an operating pressure of 0.5 to 1 bar; and an overhead operating temperature of 35 to 65° C. By employing the above embodiments, high-boiling impurities in acetone can be removed.

[0051] According to the present invention, there is no limitation on the manner and conditions of the hydrogenation reaction as long as the object of the present invention can be achieved. In some embodiments, the hydrogenation catalyst used in the hydrogenation reaction includes one or more of a Cu-based catalyst, a Ni-based catalyst, and a Mn-based catalyst.

[0052] According to the present invention, "Cu-based" refers to a hydrogenation catalyst in which Cu is supported on a carrier as an active component; "Mn-based" refers to a hydrogenation catalyst in which Mn is supported on a carrier as an active component; the type of carrier can be selected as needed, and examples include, but are not limited to, SiO2 carriers, molecular sieve carriers, and Al2O3 carriers.

[0053] According to the present invention, there are no limitations on the hydrogenation reaction conditions as long as the objectives of the present invention can be achieved. In some embodiments, the hydrogenation reaction conditions include a reaction inlet temperature of 70 to 140°C (e.g., 70°C, 80°C, 90°C, 110°C, 120°C, 130°C, or 140°C); a reaction pressure of 2 to 8 MPaG (e.g., 2 MPaG, 4 MPaG, 5 MPaG, 7 MPaG, or 8 MPaG); and a hydrogen to acetone molar ratio of 4 to 40:1 (e.g., 4:1, 8:1, 12:1, 16:1, 20:1, 21:1, 23:1, 30:1, 32:1, 35:1, or 40:1). In some embodiments, the hydrogenation reaction conditions include a reaction time of 0.6 to 3 h. -1 Acetone space velocity (e.g., 0.6 h -1 , 1h -1 , 1.6h -1 , 2h -1 , 2.5h -1 or 3h -1 ).

[0054] According to the present invention, in order to more effectively remove light and heavy impurity components from isopropanol, in some embodiments, a de-light separation is performed using a plate distillation column or a packed distillation column to separate the light impurity components, and the de-light separation conditions include the following: an operating reflux ratio of 2 to 20 (e.g., 2, 4, 5, 8, 10, 12, 15, or 20), preferably 5 to 15.

[0055] According to the present invention, in some embodiments, the conditions for de-lightening include an operating pressure of −0.5 to 10 bar (e.g., −0.5 bar, 0.25 bar, 1 bar, 1.5 bar, 2.0 bar, 5.0 bar, 8.0 bar, or 10 bar), preferably 0.25 to 1.0 bar.

[0056] According to the present invention, in some embodiments, the conditions for de-lightening separation include: a bottom operating temperature of 40 to 95°C (e.g., 40°C, 50°C, 60°C, 75°C, 85°C, or 95°C), preferably 50 to 85°C.

[0057] According to some embodiments of the present invention, to separate heavy impurity components, deheavying separation is carried out using a plate distillation column or a packed distillation column, and the deheavying separation conditions include the following: an operating reflux ratio of 1 to 10 (e.g., 1, 2, 4, 6, 8, or 10), preferably 2 to 8.

[0058] According to the present invention, in some embodiments, the conditions for deheavy separation include: an operating pressure of −0.5 to 10 bar (e.g., −0.5 bar, 0.5 bar, 1.0 bar, 2.0 bar, 4.0 bar, 6.0 bar, or 10 bar), preferably 0.5 to 1 bar.

[0059] According to the present invention, in some embodiments, the conditions for deheavy separation include: a column overhead operating temperature of 50 to 90°C (e.g., 50°C, 60°C, 65°C, 75°C, 85°C, or 90°C), preferably 65 to 85°C.

[0060] According to the present invention, "at least one isopropanol adsorption filtration" means that the adsorption filtration operation can be repeated one or more times as necessary.

[0061] According to the present invention, in some embodiments, the adsorbent material used in isopropanol adsorptive filtration to remove anions and cations in isopropanol comprises one or more of anion exchange resin and cation exchange resin.

[0062] According to the present invention, those skilled in the art can use anion exchange resin or cation exchange resin alone as the adsorption material as needed, or can select a mixed resin of anion exchange resin and cation exchange resin as the adsorption material as needed, which will not be described in detail in this specification.

[0063] According to the present invention, in some embodiments, the filter material used in isopropanol adsorptive filtration to remove particles in isopropanol includes one or more of a polymer membrane, a ceramic membrane, and a metal membrane.

[0064] By adopting the above-described embodiment, it is possible to avoid the influence on the purity of isopropanol caused by the elution of metal ions and particles that may be present in the materials of the components of the preliminary process section.

[0065] In another aspect, the present invention provides a system for preparing electronic grade isopropanol by hydrogenating acetone, the system comprising: an acetone purification unit, which is used to purify acetone raw material to obtain acetone feed; an acetone hydrogenation unit used to hydrogenate acetone feed to obtain a crude isopropanol product; an isopropanol purification unit, which is used to purify crude isopropanol to obtain electronic grade isopropanol; Here, the acetone purification unit includes an acetone pre-oxidation treatment device, an acetone dehydration device, and an acetone purification device, which are connected in sequence; the acetone hydrogenation unit includes an acetone hydrogenation reactor; and the isopropanol purification unit includes an isopropanol dehydration device, an isopropanol purification device, and an adsorption filtration device, which are connected in sequence.

[0066] In the present invention, the acetone pre-oxidation treatment unit can be selected as a tubular reactor or a kettle reactor as needed. The specific structures of the tubular reactor, the kettle reactor and the acetone hydrogenation reactor are those commonly used in the art.

[0067] According to the present invention, organic impurities that are difficult to separate from isopropanol are removed in the acetone purification unit, thereby avoiding the drawbacks of difficulty in separating them from isopropanol and large energy consumption in the subsequent stage.

[0068] According to the present invention, in some embodiments, the acetone dehydration unit comprises an acetone dehydration tower.

[0069] According to the present invention, in some embodiments, the acetone purification unit comprises an acetone purification column.

[0070] According to the present invention, in some embodiments, the isopropanol dehydration unit comprises an isopropanol dehydration tower.

[0071] According to some embodiments of the present invention, the isopropanol purification apparatus includes an isopropanol delightening column for removing light impurity components having a boiling point lower than that of isopropanol, and an isopropanol deheavying column for removing heavy impurity components having a boiling point higher than that of isopropanol, which are connected in series.

[0072] According to some embodiments of the present invention, the isopropanol delightening column is a plate distillation column or a packed distillation column, and the isopropanol deheavying column is a plate distillation column or a packed distillation column.

[0073] In the present invention, the structures of the acetone dehydration column, plate distillation column and packed distillation column are those commonly used in the art and will not be described in detail in this specification.

[0074] According to the present invention, in some embodiments, the adsorptive filtration facility comprises an adsorptive filtration facility.

[0075] In the system according to the present invention, a raw material pump, inlets and outlets for raw materials and products, etc. may be provided as required.

[0076] A preferred embodiment of the process and system of the present invention will now be described in conjunction with FIG.

[0077] As shown in Figure 1, The acetone raw material (1) is pressurized by a raw material pump and introduced into an acetone pre-oxidation treatment unit R1 filled with an oxidized pre-oxidant to perform pre-oxidation, thereby obtaining pre-oxidized acetone (2); the pre-oxidized acetone (2) is dehydrated in an acetone dehydration tower C1 filled with a dehydration material to obtain dehydrated acetone (3); the dehydrated acetone (3) is introduced into an acetone purification tower T1 to obtain a purified acetone feed (4), and heavy components (5) are discharged; the purified acetone feed (4) is introduced into an acetone hydrogenation reactor R2 filled with a hydrogenation catalyst to perform a hydrogenation reaction, thereby obtaining a crude isopropanol product (6); the crude isopropanol product (6) is then dehydrated in an acetone dehydration tower C1 filled with a dehydration material. The dehydrated isopropanol (7) is obtained by dehydrating the isopropanol (7) in the isopropanol delightening column T2, where light impurity components (8) are removed, and a light isopropanol product (9) is obtained. The light isopropanol product (9) is then fed to the isopropanol deheavying column T3, where heavy impurity components (11) are removed, and a primary isopropanol product (10) is obtained. The primary isopropanol product (10) is then fed to the adsorption filtration equipment C3, where anions, cations, and particles are removed, and electronic grade isopropanol (12) is obtained. [Example]

[0078] The present invention will be described in detail below with reference to examples. In the following examples and comparative examples: Moisture content was measured with a Karl Fischer Moisture Meter; Single metal cation concentrations were measured by ICP-MS; Anion concentrations were measured by ion chromatography; The particle number (≥50 nm) was measured by an online particle size analyzer; Unless otherwise specified, various materials are commercially available.

[0079] Example 1 Oxidation treatment of pre-oxidant: Equimolar amounts of 2,2-dimethyl-1,3-dioxolane-4,5-dimethanol and manganese chloride salt were taken, and in an anhydrous and oxygen-free nitrogen atmosphere, a 2,2-dimethyl-1,3-dioxolane-4,5-dimethanol solution containing 2,2-dimethyl-1,3-dioxolane-4,5-dimethanol and a manganese chloride solution containing manganese chloride were added, followed by stirring at room temperature for 6 hours; potassium permanganate was added thereto, and the reaction was continued for 3 hours, after which the solvent was evaporated to obtain an oxidized pre-oxidant; As shown in FIG. 1, the acetone raw material (1) (industrial acetone, purity 98%) is pressurized by a raw material pump and introduced into the acetone pre-oxidation treatment unit R1 filled with an oxidizing pre-oxidant at a rate of 0.6 mL / min for pre-oxidation to obtain pre-oxidized acetone (2). This pre-oxidized acetone (2) is dehydrated in the acetone dehydration column C1 filled with a dehydrating material (4A molecular sieve) to obtain dehydrated acetone (3). The dehydrated acetone is introduced into the acetone purification column T1 (plate distillation column) for purification to obtain purified acetone feed (4). Heavy components (5) are discharged. The purified acetone feed is introduced into the acetone hydrogenation reactor R2 filled with a hydrogenation catalyst (5 wt.% Cu / SiO2 catalyst) for hydrogenation to obtain crude isopropanol product (6). The isopropanol product (6) is dehydrated in an isopropanol dehydration column C2 packed with a dehydrating material (4A molecular sieve) to obtain dehydrated isopropanol (7); the dehydrated isopropanol (7) is introduced into an isopropanol light removal column T2 (packed column) to separate light components and remove light impurities (8) to obtain a dehydrated isopropanol product (9); the dehydrated isopropanol product (9) is passed through an isopropanol heavy impurity removal column T3 (packed column) to separate heavy components and remove heavy impurities (11) to obtain a primary isopropanol product (10); the primary isopropanol product (10) is then passed through an adsorption filtration unit C3 to remove anions, cations, and particles to obtain electronic grade isopropanol (12); The pre-oxidation conditions include: normal temperature and pressure, the amount of pre-oxidant added is 0.03 wt% of the acetone raw material; Operating reflux ratio 0.5, operating pressure 1 bar, top operating temperature 56°C; The hydrogenation reaction conditions included: reaction inlet temperature 100°C, reaction pressure 4 MPa, hydrogen to acetone molar ratio 8:1, acetone space velocity 1.0 h -1 ; The conditions for de-light separation include: operating reflux ratio 5, operating pressure 0.75 bar, and controlling the column bottom operating temperature to 75°C; The conditions for deheavy separation include: operating reflux ratio 5, operating pressure 1 bar, and controlling the column top operating temperature to 82°C; The adsorption filtration equipment C3 was filled with a mixed resin of cation exchange resin and anion exchange resin and a polymer filtration membrane.

[0080] The purity, water content, single metal cation concentration, anion concentration, and particle number (≥50 nm) of electronic grade isopropanol (12) are shown in Table 1.

[0081] Example 2 The procedure of Example 1 was followed with the following exceptions: Oxidation treatment of pre-oxidant: Equimolar amounts of 2,2-dimethyl-1,3-dioxane-4,6-dimethanol and cobalt acetate were taken, and in an anhydrous, oxygen-free, nitrogen atmosphere, a 2,2-dimethyl-1,3-dioxane-4,6-dimethanol solution containing 2,2-dimethyl-1,3-dioxane-4,6-dimethanol and a cobalt acetate solution containing cobalt acetate were added, potassium permanganate was added thereto, and the mixture was reacted for 3 hours, after which the solvent was evaporated to obtain an oxidized pre-oxidant.

[0082] The purity, water content, single metal cation concentration, anion concentration, and particle number (≥50 nm) of electronic grade isopropanol (12) are shown in Table 1.

[0083] Example 3 The procedure of Example 1 was followed with the following exceptions: Oxidation treatment of pre-oxidant: Equimolar amounts of 2,2-dimethyl-1,3-dioxane-4,6-dimethanol and cobalt acetate were taken, and in an anhydrous, oxygen-free, nitrogen atmosphere, a 2,2-dimethyl-1,3-dioxane-4,6-dimethanol solution containing 2,2-dimethyl-1,3-dioxane-4,6-dimethanol and a cobalt acetate solution containing cobalt acetate were added, potassium permanganate was added thereto, and the mixture was reacted for 3 hours, and then the solvent was evaporated to obtain an oxidized pre-oxidant; Dehydration material (composite bed layer of 4A molecular sieve and anhydrous potassium carbonate, volume ratio 50%-50%); Acetone purification column T1 (packed distillation column); Hydrogenation catalyst (Ni / SiO2 catalyst); Here, the acetone purification conditions include: operating reflux ratio 2, operating pressure 1.5 bar, and column top operating temperature controlled at 64°C.

[0084] The hydrogenation reaction conditions included: reaction inlet temperature 90°C, reaction pressure 4 MPa, hydrogen / acetone molar ratio 8:1, acetone space velocity 1.0 h -1 .

[0085] The conditions for de-light separation include: operating reflux ratio 5, operating pressure 0.5 bar, and column bottom operating temperature controlled at 65°C.

[0086] The conditions for deheavy separation include: operating reflux ratio 5, operating pressure 1.5 bar, and controlling the column top operating temperature to 90°C.

[0087] The purity, water content, single metal cation concentration, anion concentration, and particle number (≥50 nm) of electronic grade isopropanol (12) are shown in Table 1.

[0088] Example 4 The procedure of Example 1 was followed with the following exceptions: Oxidation treatment of pre-oxidant: Equimolar amounts of 2,2-diethyl-1,3-dioxolane-4,5-dimethanol and manganese chloride were taken, and in an anhydrous, oxygen-free, nitrogen atmosphere, a manganese chloride solution containing 2,2-diethyl-1,3-dioxolane-4,5-dimethanol and manganese chloride was added, and the mixture was stirred at room temperature for 6 hours; potassium permanganate was added thereto, and the mixture was reacted for 3 hours, after which the solvent was evaporated to obtain the oxidized pre-oxidant.

[0089] The hydrogenation reaction conditions included: reaction inlet temperature 70°C, reaction pressure 2 MPaG, hydrogen and acetone molar ratio 4:1, acetone space velocity 0.8 h -1 ; The conditions for de-light separation include: operating reflux ratio 15, operating pressure 1 bar, and controlling the column bottom operating temperature to 85°C.

[0090] The conditions for deheavy separation include: operating reflux ratio 7, operating pressure 1 bar, and controlling the column top operating temperature to 85°C.

[0091] The adsorption filtration equipment C3 was filled with mixed resin and ceramic filtration membrane.

[0092] The purity, water content, single metal cation concentration, anion concentration, and particle number (≥50 nm) of electronic grade isopropanol (12) are shown in Table 1.

[0093] Example 5 The procedure of Example 3 was followed with the following exceptions: Here, the acetone purification conditions include: operating reflux ratio 2, operating pressure 0.5 bar; controlling the column top operating temperature at 47°C; The conditions for de-light separation include: operating reflux ratio 5, operating pressure 1.5 bar, and controlling the column bottom operating temperature to 90°C; The conditions for deheavy separation include: operating reflux ratio 5, operating pressure 0.5 bar, and controlling the overhead operating temperature to 65°C.

[0094] The purity, water content, single metal cation concentration, anion concentration, and particle number (≥50 nm) of electronic grade isopropanol (12) are shown in Table 1.

[0095] Example 6 The procedure of Example 3 was followed with the following exceptions: Oxidation treatment of pre-oxidant: Equimolar amounts of 2,2-dimethyl-1,3-dioxolane-4,5-dimethanol and molybdenum chloride were taken, and in an anhydrous, oxygen-free, nitrogen atmosphere, a 2,2-dimethyl-1,3-dioxolane-4,5-dimethanol solution containing 2,2-dimethyl-1,3-dioxolane-4,5-dimethanol and a molybdenum chloride solution containing molybdenum chloride were added, and the mixture was stirred at room temperature for 6 hours; potassium permanganate was added thereto, and the mixture was reacted for 3 hours, after which the solvent was evaporated to obtain the oxidized pre-oxidant.

[0096] The purity, water content, single metal cation concentration, anion concentration, and particle number (≥50 nm) of electronic grade isopropanol (12) are shown in Table 1.

[0097] Example 7 The procedure of Example 1 was followed with the following exceptions: Pretreatment of oxidant: Equimolar amounts of 2,2-dimethyl-1,3-dioxolane-4,5-dimethanol and cupric chloride were taken, and in an anhydrous, oxygen-free, nitrogen atmosphere, a 2,2-dimethyl-1,3-dioxolane-4,5-dimethanol solution containing 2,2-dimethyl-1,3-dioxolane-4,5-dimethanol and a cupric chloride solution containing cupric chloride were added, and the mixture was stirred at room temperature for 6 hours; potassium permanganate was added, and the mixture was reacted for 3 hours, after which the solvent was evaporated to obtain the oxidized pre-oxidant.

[0098] The purity, water content, single metal cation concentration, anion concentration, and particle number (≥50 nm) of electronic grade isopropanol (12) are shown in Table 1.

[0099] Example 8 The procedure of Example 1 was followed with the following exceptions: The oxidized pre-oxidant was replaced with the oxidizing metal salt KMnO4.

[0100] The purity, water content, single metal cation concentration, anion concentration, and particle number (≥50 nm) of electronic grade isopropanol (12) are shown in Table 1.

[0101] Example 9 The procedure of Example 1 was followed with the following exceptions: The oxidized pre-oxidant was replaced with 10 wt% Co oxide / SiO2 supported catalyst.

[0102] The purity, water content, single metal cation concentration, anion concentration, and particle number (≥50 nm) of electronic grade isopropanol (12) are shown in Table 1.

[0103] Example 10 The procedure of Example 1 was followed with the following exceptions: Oxidation treatment of pre-oxidant: Equimolar amounts of 2,2-dimethyl-1,3-dioxolane-4,5-di-1-ethanol and manganese chloride salt were taken, and in an anhydrous, oxygen-free, nitrogen atmosphere, a 2,2-dimethyl-1,3-dioxolane-4,5-di-1-ethanol solution containing 2,2-dimethyl-1,3-dioxolane-4,5-di-1-ethanol and a manganese chloride solution containing manganese chloride were added, and the mixture was stirred at room temperature for 6 hours; potassium permanganate was added thereto, and the mixture was reacted for 3 hours, after which the solvent was evaporated to obtain the oxidized pre-oxidant.

[0104] The results are shown in Table 1.

[0105] Example 11 The procedure of Example 1 was followed with the following exceptions: Oxidation treatment of pre-oxidant: Equimolar amounts of 2,2-dimethyl-1,3-dioxolane-4,5-dibenzyl alcohol and manganese chloride salt were taken, and in an anhydrous, oxygen-free, nitrogen atmosphere, a 2,2-dimethyl-1,3-dioxolane-4,5-dibenzyl alcohol solution containing 2,2-dimethyl-1,3-dioxolane-4,5-dibenzyl alcohol and a manganese chloride solution containing manganese chloride were added, and the mixture was stirred at room temperature for 6 hours; potassium permanganate was added thereto, and the mixture was reacted for 3 hours, after which the solvent was evaporated to obtain the oxidized pre-oxidant.

[0106] The results are shown in Table 1.

[0107] Example 12 The procedure of Example 1 was followed with the following exceptions: Oxidation treatment of pre-oxidant: Equimolar amounts of 2,2-dimethyl-1,3-dioxolane-4,5-di-p-methylbenzyl alcohol and manganese chloride salt were taken, and in an anhydrous, oxygen-free, nitrogen atmosphere, a 2,2-dimethyl-1,3-dioxolane-4,5-di-p-methylbenzyl alcohol solution containing 2,2-dimethyl-1,3-dioxolane-4,5-di-p-methylbenzyl alcohol and a manganese chloride solution containing manganese chloride were added, and the mixture was stirred at room temperature for 6 hours; potassium permanganate was added thereto, and the mixture was reacted for 3 hours, after which the solvent was evaporated to obtain the oxidized pre-oxidant.

[0108] The results are shown in Table 1.

[0109] Example 13 The procedure of Example 1 was followed with the following exceptions: Oxidation treatment of pre-oxidant: Equimolar amounts of 2,2-diphenyl-1,3-dioxolane-4,5-dimethanol and manganese chloride salt were taken, and in an anhydrous, oxygen-free, nitrogen atmosphere, a 2,2-diphenyl-1,3-dioxolane-4,5-dimethanol solution containing 2,2-diphenyl-1,3-dioxolane-4,5-dimethanol and a manganese chloride solution containing manganese chloride were added, and the mixture was stirred at room temperature for 6 hours. Potassium permanganate was added thereto, and the mixture was reacted for 3 hours. The solvent was then evaporated to obtain an oxidized pre-oxidant; The results are shown in Table 1.

[0110] Comparative Example 1 The procedure of Example 1 was followed with the following exceptions: The acetone raw material (1) was not subjected to a preliminary oxidation treatment. In other words, the acetone raw material (1) was directly pressurized by a raw material pump and introduced into an acetone dehydration column C1 filled with a dehydrating material to remove water, thereby obtaining dehydrated acetone (3). This dehydrated acetone (3) was then treated according to the post-process of Example 1 until isopropanol was obtained.

[0111] The purity, water content, single metal cation concentration, anion concentration, and particle number (≧50 nm) of isopropanol are shown in Table 1.

[0112] Comparative Example 2 The procedure of Example 1 was followed with the following exceptions: The pre-oxidized acetone (2) was not passed through the acetone dehydrating column C1 packed with a dehydrating material (4A molecular sieve) to remove water, but was directly introduced into an acetone purifying column T1 (plate distillation column) for purification to obtain a purified acetone feed (4). This acetone feed (4) was treated according to the post-process of Example 1 until isopropanol was obtained.

[0113] The purity, water content, single metal cation concentration, anion concentration, and particle number (≧50 nm) of isopropanol are shown in Table 1.

[0114] [Table 2]

[0115] The results in Table 1 demonstrate that the overall process of Examples 1-13, which combines acetone dehydration, acetone purification, isopropanol dehydration, isopropanol purification, and at least one type of isopropanol adsorption filtration, involves introducing acetone feedstock into an acetone pre-oxidation reactor to pre-oxidize impurities and obtain pre-oxidized acetone. The organic impurity content of the resulting isopropanol product is low, at 5 ppm or less, and the anion and anion, particle content, and water content meet the requirements for high-end wafer manufacturing (linewidth ≦90 nm).

[0116] Although the preferred embodiments of the present invention have been described in detail above, the present invention is not limited thereto. Within the technical concept of the present invention, the technical solutions of the present invention may undergo various simple modifications, including the combination of various technical features in any other suitable manner, and these simple modifications and combinations shall also be considered as the contents disclosed by the present invention and fall within the protection scope of the present invention.

Claims

1. 1. A process for hydrogenating an acetone feedstock to prepare isopropanol, the process comprising the steps of: (1) introducing the acetone feedstock into an acetone pre-oxidation reactor to pre-oxidize reducing impurities to obtain a pre-oxidized acetone feedstock; and (2) introducing an acetone feed into an acetone hydrogenation reactor for hydrogenation reaction to obtain a crude isopropanol product; wherein the acetone feed is the pre-oxidized acetone feedstock obtained from step (1) or a purified acetone feedstock obtained by any intermediate treatment (1-2) of the pre-oxidized acetone feedstock.

2. 2. The process of claim 1, wherein the intermediate treatment (1-2) is carried out between step (1) and step (2), and the intermediate treatment (1-2) comprises sequentially introducing the pre-oxidized acetone feedstock into an acetone dehydration unit and an acetone purification unit to dehydrate and purify acetone, thereby obtaining a purified acetone feedstock.

3. 3. The process of claim 1 or 2, further comprising a step (3) of post-treating the crude isopropanol product: passing the crude isopropanol product sequentially through an isopropanol dehydration unit, an isopropanol purification unit, and an adsorption filtration unit to perform isopropanol dehydration, isopropanol purification, and at least one round of isopropanol adsorption filtration to obtain electronic-grade isopropanol.

4. In step (1), the pre-oxidation conditions are as follows: the amount of pre-oxidizer added being 0.01 to 0.1 wt. % of the acetone feedstock; and At normal temperature and pressure; The process according to any one of claims 1 to 3, comprising:

5. The pre-oxidation is carried out by using an oxygen-containing metal complex as a pre-oxidizing agent; wherein the oxygen-containing metal complex uses a transition metal element as a central atom and uses an oxygen-containing heterocyclic organic compound having a substituent as a ligand; and the ligand is a compound having a structure represented by formula (I), 【Chemical 1】 In formula (I), n is an integer from 0 to 5, and A is —CH(R ５ )- and; R １ , R ２ , R ３ , R ４ and R ５ is each independently selected from H, C1-C8 alkyl, phenyl C1-C8 alkyl, and C1-C8 alkylphenyl.

6. In formula (I), R at each occurrence １ , R ２ , R ３ , R ４ and R ５ are each independently selected from H, C1-C5 alkyl, phenyl C1-C5 alkyl, and C1-C5 alkyl-substituted phenyl, preferably each independently selected from H, C1-C4 alkyl, benzyl, and C1-C3 alkyl-substituted phenyl.

7. 6. The process of claim 5, wherein the transition metal element is selected from one or more of chromium, molybdenum, tungsten, iron, cobalt, nickel, ruthenium, rhodium, palladium, platinum, manganese, technetium, and rhenium.

8. In formula (I), n is an integer from 0 to 3; R １ , R ２ , R ３ , and R ４ are each independently selected from H, C1-C3 alkyl, benzyl, and methyl-substituted phenyl; and A is -CH(R ５ )- and R ５ is H or C1-C3 alkyl; Preferably, in formula (I), n is an integer from 0 to 3; and / or R １ and R ２ are each independently selected from H, C1-C3 alkyl, and R ３ and R ４ are each independently selected from H, C1-C3 alkyl, benzyl, and methyl-substituted phenyl; and / or R ５ is H or C1-C3 alkyl; Also preferably, in formula (I), n is 0 or 1; and R １ and R ２ are each independently selected from C1-C3 alkyl; R ３ and R ４ are each independently selected from H, C1-C3 alkyl, benzyl, and methyl-substituted phenyl; R ５ The process of any one of claims 5 to 7, wherein is H.

9. 9. The process according to any one of claims 5 to 8, wherein the oxygen-containing metal complex is prepared by the following steps: adding a ligand solution and a metal salt solution according to an equimolar ratio of ligand to transition metal under anhydrous, oxygen-free, nitrogen atmosphere, stirring at room temperature for 1 to 10 hours to carry out the coordination reaction, and optionally evaporating the solvent after the coordination reaction.

10. In step (1), prior to pre-oxidizing the pre-oxidant, the pre-oxidant is oxidized using an oxidizing agent; Preferably, the oxidizing agent is selected from one or more of oxygen, hydrogen peroxide, cumene peroxide, peracetic acid, perchlorates, permanganates, and dichromates; 10. The process of claim 1, wherein in step (1), the acetone source comprises one or more of technical grade acetone, analytical grade acetone, and electronic grade acetone.

11. 4. The process of claim 2 or 3, wherein the dehydration materials used in the dehydration of acetone in step (1-2) and the dehydration of isopropanol in step (3) each independently comprise one or more of molecular sieves, silica gel, membranes, resins, and salts capable of forming crystalline hydrates.

12. 12. The process according to any one of claims 1 to 11, wherein in step (2), the hydrogenation catalyst used in the hydrogenation reaction comprises one or more of a Cu-based catalyst, a Ni-based catalyst, and a Mn-based catalyst.

13. 4. The process of claim 3, wherein in step (3), the purification of isopropanol comprises the steps of: Delight separation, which is used to remove light impurity components with a boiling point lower than that of isopropanol; and Deheavy separation is used to remove heavy impurity components with a boiling point higher than that of isopropanol.

14. 14. The process of any one of claims 1 to 13, wherein the reducing impurities are selected from alcohols, aldehydes, ketones, esters, ethers and olefins, preferably the reducing impurities are selected from saturated or unsaturated C1-C4 primary or secondary alcohols, C1 to C4 aldehydes, C1 to C4 alkyl formates, C2 to C4 olefins, anilines optionally substituted with C1 to C4 alkyl and phenols optionally substituted with C1 to C4 alkyl.

15. 15. A system for preparing electronic grade isopropanol by carrying out the hydrogenation of acetone of the process of any one of claims 1 to 14, characterized in that the system comprises: An acetone pre-oxidation processor used to perform step (1) of the process according to any one of claims 1 to 14 to obtain a pre-oxidized acetone feedstock; and an acetone hydrogenation unit used to carry out step (2) of the process according to any one of claims 1 to 14 to obtain a crude isopropanol product; and optionally An acetone dehydration unit and an acetone purification unit used to carry out the intermediate treatment (1-2) of the process according to any one of claims 1 to 14.

16. Plus: an isopropanol purification unit used to purify the crude isopropanol to obtain electronic grade isopropanol; Preferably, the isopropanol purification unit includes an isopropanol dehydration device, an isopropanol purification device, and an adsorption filtration device connected in sequence.

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