KR20020042397A - Process for preparing 1,3-alkanediol from 3-hydroxyester compounds - Google Patents

Abstract

PURPOSE: Provided is a process for producing 1,3-alkanediol from a 3-hydroxy ester compound by using a hydrogenation catalyst having high activity and high selectivity. CONSTITUTION: The 1,3-alkanediol is produced by hydrogenating the 3-hydroxy ester compound such as 3-hydroxy methyl propanoate in the presence of the catalyst in a mixed solvent comprising an alcohol solvent and a solvent having a higher boiling point than the 1,3-alkanediol by a liquid-gas phase method, wherein the catalyst is produced by adding an alkali precipitant, such as an alkali carbonate or sodium hydroxide, to a water solution of copper salts to produce particles and then aging by adding colloidal silica. The catalyst has a weight ratio of copper oxide(CuO) and silica(SiO2) being 9:1-5:5.

Description

Process for preparing 1,3-alkanediol from 3-hydroxyester compound

The present invention relates to a method for preparing 1,3-alkanediol from 3-hydroxyester compound, and more particularly to a hydrogenation catalyst for preparing 1,3-alkanediol from high yield of 3-hydroxyester compound. And a method for hydrogenating a 3-hydroxyester compound under this catalyst.

1,3-alkanediol is not only a synthetic raw material of polyester but also used as a coating or as an intermediate of organic synthesis.It has various uses.Hydroformylation of epoxide compounds has been carried out. Synthesis of 3-hydroxyaldehyde derivative and hydrogenation thereof to synthesize 1,3-alkanediol (US Pat. Nos. 5,770,776, 5,723,389, 5,731,478, 5,777,182) and hydration of acrolein to 3-hydroxypropanal Synthesis and hydrogenation thereof (European Patent 577,972, U.S. Patent No. 5,093,537), and a method for producing 1,3-alkanediol by biological method from glycerol (European Patent 361,082, German Patent 3,734,764) and the like are known, The process of synthesize | combining 3-hydroxypropanal by the hydroformylation reaction of ethylene oxide and hydrogenating it by Shell company It has been commercialized during production. However, in the synthesis method using 3-hydroxypropanal as an intermediate, the aldehyde itself is unstable and oligomers are formed or hydrogenation does not proceed completely with desired 1,3-propanediol due to the formation of by-product acetal or the quality of the final product. It is known that this problem is reduced.

In another method, a 3-hydroxyester compound is synthesized by a carboesterification reaction in which an epoxide compound is reacted with carbon monoxide and an alcohol, and the ester group of the compound is hydrogenated to produce a 1,3-alkanediol compound. It is possible to make it, but the process for producing 1,3-alkanediol by this method has not yet been industrialized. This is because the 3-hydroxyester compound reacts very non-selectively on hydrogenation catalysts of conventional ester groups such as copper-chromium oxide catalysts or copper-zinc oxides or Raney Ni.

On the other hand, the corresponding monoalcohol, 1,4-butanediol, 1,4-cyclohexane from a general ester compound, a carbonyl compound, or a C ₄ or more dicarboxylic acid ester compound such as alkyl maleate or cyclohexanedicarboxylic acid ester A heterogeneous hydrogenation catalyst for gaseous or liquid phase processes for producing dimethanol is known and industrially useful. U. S. Patent No. 5,406, 004 discloses a hydrogenation catalytic process of a typical ester group used in the reaction. For example, Cu-Al ₂ O ₃ with a copper-containing catalyst, reduced CuO / ZnO (Cu: Zn = 0.4: 1 to 2: 1), and reduced copper-chromite (Cu: Cr = 0.1: 1 to 4: 1) type catalyst, and the CuO / ZnO catalyst or the copper-chromite catalyst is in the range of 0.1 to 15 wt% based on barium, manganese, rare earth metals (lanthanum, samarium, thorium, cerium, yttrium, etc.) or elements such as magnesium and calcium. A catalyst improved in the above is known, and in some cases, a catalyst using a support such as alumina or zirconia may be used. The catalysts mentioned above are commercially available catalysts. Others include Pd-Zn (US Pat. No. 5,185,476), Cu-TiO ₂ (US Pat. No. 4,929,777), Re-Cu-Zn (European Patent 373,946), Zn-Ru (US Pat. No. 4,443,639) and Pd, Pt, Ru containing catalysts are known.

Although many copper-containing catalysts and precious metal catalysts have been developed as described above to prepare corresponding alcohols from carbonyl group-containing compounds, in particular ester compounds, as in the substrate compounds of the present invention, hydroxyl groups in particular at the β-position are contained. A catalytic process which is useful for the preparation of 1,3-alkanediols from 3-hydroxyester compounds is rarely proposed, and WO 00/18712 describes the preparation of 1,3-propanediol from methyl 3-hydroxypropanoates. Cu / ZnO-based catalysts are the only known catalysts, but they do not show industrially meaningful performance.

A catalyst for the preparation of 1,2,4-butanetriol from malic acid or malic ester, which is a similar compound substituted with a hydroxyl group at the β-position. In US Pat. No. 4,973,769, a Cu-Al ₂ O ₃ based catalyst WO 99/38613 proposes a Ru-Re-based catalyst, but in the above process, a high pressure of about 100 to 300 atmospheres is required as a reaction condition for preparing a triol compound. It is unreasonable to apply it to the process for manufacturing.

In addition, WO 00/18712 proposes a reaction under an alcoholic solvent such as methanol in the reduction of methyl 3-hydroxypropanoate on a Cu / ZnO hydrogenation catalyst. Alcohol is expected to have a positive effect of inhibiting the lactonation of the reactant 3-hydroxyester compound itself and the decomposition of the ester group, but the alcohol having a low boiling point under the hydrogen gas flow in the fixed-phase catalytic reactor is high in the gas phase under the reaction conditions. It does not help to maintain high selectivity in conversion or to ensure long-term reaction stability of the catalyst. In the embodiment of the invention there is a significant decrease in selectivity at high conversion rates. In addition, since the 3-hydroxyester compound and the product 1,3-alkanediol, which are reactants, do not have a large difference in chemical properties or break point, it is difficult to separate and purify the reactants and products when the conversion rate is low.

The problem of the hydrogenation catalyst / process of the 3-hydroxyester compound in which the β-position is substituted with a hydroxyl group compared to the hydrogenation reaction of the general ester compound is that the reactant is very unstable chemically and thermally so that the hydroxyl at the β-position Easily dehydrated, the resultant unsaturated ester compound is reduced to easily sidereact with a saturated ester compound or a corresponding monoalcohol with reduced ester group. In addition, the β-lactone compound, an intramolecular reaction product of the 3-hydroxyester compound, is thermally unstable to become a decomposed or polymerized lactone polymer, and the intermolecular reaction or other hydrogenation product of 1,3-alkanediol compound. Condensation reaction with and side reactions with various esterates or lactone compounds. Since the degree of side reaction is sensitive to the reaction temperature, there is a limit in controlling the reaction rate by increasing the reaction temperature, and maintaining a high pressure to maintain proper activity at a low reaction temperature is an industrial problem.

An object of the present invention is to solve the problems of the prior art as described above, to prepare 1,3-alkanediol from a 3-hydroxyester compound using a novel hydrogenation catalyst showing high activity and high selectivity even under mild reaction conditions. To provide a way.

That is, according to the present invention, an alkaline precipitant such as an alkali carbonate or sodium hydroxide is added to an aqueous copper salt solution to generate particles, and then hydrogenated to a 3-hydroxyester compound on a catalyst prepared by adding colloidal silica to aged. It is to provide a method for producing 1,3-alkanediol in high yield.

Hereinafter, the present invention will be described in more detail.

In the present invention, a silica stabilized copper catalyst is applied to a hydrogenation process for preparing 1,3-alkanediol from 3-hydroxyester compound. The main component of the catalyst is copper in an oxide state, the content of which is 20 to 99% by weight, preferably 50 to 95% by weight, and the content of silica contained in the catalyst is 1 to 80% by weight, preferably 5 to 50%. Weight percent. The copper oxide catalyst stabilized with silica may be represented by CuO-SiO ₂ , but a method of supporting copper on a conventional silica carrier may not produce a catalyst expressing a target performance of the present invention, and 10 nm. The following fine copper oxide precursor particles are prepared by a special method of stabilizing with silica to exhibit high activity. More specifically, it is prepared by adding an alkaline precipitant such as an alkali carbonate or sodium hydroxide to the copper salt solution to generate particles, and adding the colloidal silica to this to mature. Therefore, the silica included in the catalyst of the present invention is distinguished from the carrier normally used as an essential component.

As a method of shaping the catalyst, an extrusion method, a tableting method, or a method of supporting the refractory carrier may be used. The molded catalyst is calcined at 200 to 800 ° C., preferably at 300 to 700 ° C., for 2 to 10 hours.

The calcined oxide catalyst is preferably used after being activated for about 1 to 20 hours at 150 to 450 ° C. using hydrogen or a hydrogen-containing gas. In general, this activation process is carried out by filling a calcined oxide catalyst in the reactor and flowing a gas diluted with hydrogen or a hydrogen-containing gas with nitrogen or argon, and by the heat generated during the reduction of the catalyst. Adjust the hydrogen concentration, gas flow rate, temperature increase rate, etc. so as not to cause deterioration.

The hydrogenation catalyst may be used in combination of at least one component or more promoter to enhance the hydrogenation activity or selectivity. Useful accelerator components include rhenium (Re), ruthenium (Ru), palladium (Pd), platinum (Pt), rhodium (Rh), silver (Ag), selenium (Se), tellurium (Te), molybdenum (Mo) and Manganese (Mn) and the like, and the amount of use is preferably 0.001 to 10 mol%, preferably 0.003 to 7 mol% relative to copper.

The hydrogenation catalyst may be modified by using an alkylsilane compound in order to improve activity or selectivity. In this case, the hydroxyl group of the silica is masked by the alkylsilane compound, and the catalyst exhibits hydrophobicity in hydrophilicity. Alkylsilane compounds used include trialkoxy monoalkylsilanes, dialkoxydialkylsilanes or monoalkoxytrialkylsilane compounds. The silane compound preferably has an alkyl group having 1 to 30 carbon atoms and an alkoxy group having a C ₅ or less linear or nonlinear alkoxy group, more preferably a methoxy or ethoxy group. Examples of such compounds include trimethoxypropylsilane, trimethoxyoctylsilane, dimethoxydimethylsilane, dimethoxymethylpropylsilane, dimethoxymethyloctylsilane, methoxytrimethylsilane, methoxydimethylpropylsilane, methoxydimethyloctylsilane Etc.

The 3-hydroxyester compound used in the hydrogenation reaction of the present invention is represented by the following formula (1) or (2).

R ₁ , R _2, and R in Formulas 1 and 2 each independently represent a hydrogen atom, a C ₁ to C ₂₀ saturated branched aliphatic hydrocarbon, branched aliphatic hydrocarbon, saturated cyclized hydrocarbon, and a ring. Or a hydrocarbon in which at least one hydrogen in the carbon chain is substituted with an ester, a hydroxyl group, an alkoxy group, or the like.

R in the formulas (1) and (2) is preferably methyl, ethyl, n-propyl, isopropyl, n-butane, isobutane, t-butane, cyclohexane, cyclohexanemethyl and the like.

Preferred examples of the 3-hydroxyester compound include methyl (or ethyl) 3-hydroxypropionate, 3-hydroxybutyl acid ester, 3-hydroxypentanoic acid ester, 3-hydroxyheptanoic acid ester, 3- Hydroxyoctanoic acid ester, 3-hydroxynonanoic acid ester, 3-hydroxydecanoic acid ester, 2-methyl-3-hydroxypropanoic acid ester, 2-methyl-3-hydroxybutanoic acid ester, 2-methyl- 3-hydroxypentanoic acid ester, 2-methyl-3-hydroxyhexanoic acid ester, 2-methyl-3-hydroxyheptanoic acid ester, 2-methyl-3-hydroxyoctanoic acid ester, 2-methyl-3- Hydroxynonanoic acid ester, 2-methyl-3-hydroxydecanoic acid ester, 2-ethyl-3-hydroxybutanoic acid ester, 2-ethyl-3-hydroxypentanoic acid ester, 2-ethyl-3-hydroxy Hexanoic acid ester, 2-ethyl-3-hydroxyhexanoic acid ester, 2-ethyl-3-hydroxyheptanoic acid ester, 2-methyl-3-hydroxyoctanoic acid ester, 2-ethyl-3-hydroxynonanoic acid ester, 2-ethyl-3-hydroxydecanoic acid ester, etc. are mentioned.

As a method for producing 1,3-alkanediol from the 3-hydroxyester compound using the hydrogenation catalyst as described above, a liquid slurry method, a liquid-gas method, or a gas phase method may be applied.

In the method for preparing 1,3-alkanediol from the 3-hydroxyester compound of the present invention, only 3-hydroxyester can be reacted by supplying the catalyst with hydrogen gas on the catalyst, but the 3-hydroxyester reactant itself or the reactant To suppress side reactions due to lactonation and condensation reaction between the product and the product, and to adjust the concentration of the reactants in contact with the catalyst during the reaction to enhance the reaction activity and selectivity, and to mitigate the sharp decrease in selectivity under high conversion Depending on the type of hydrogenation reaction, the 3-hydroxyester compound may be dissolved in an alcohol solvent or a mixed solvent of a high boiling point solvent having a higher breaking point than the reactant or product.

In the case of hydrogenation of the 3-hydroxyester compound by liquid-gas method, the 3-hydroxyester compound is added in a dissolved state of a mixed solvent of alcohol and a high boiling point solvent, wherein the alcohol and the high boiling point solvent are 5:95. ˜90: 10 (w / w), preferably 10:90 to 70:30 (w / w), and the concentration of the 3-hydroxyester compound is 2 to 95% by weight in the total solution, preferably Preferably 5 to 90% by weight.

In the liquid-phase reaction method, a catalyst is charged into a reactor and a relatively low partial pressure of hydrogen gas and a 3-hydroxyester-containing solution are introduced under the same direction of flow to react between hydrogen in the gas phase and 3-hydroxyester compound in the liquid phase. This method has the advantage that the residence time can be smoothly controlled.

Appropriate reaction conditions for the synthesis of 1,3-alkanediol from 3-hydroxyester compound in liquid-phase flow reaction are reaction temperature of 100 to 250 ° C, preferably 120 to 200 ° C, and reaction pressure of 50 to 3,000 psig, preferably 150 to 2,000 psig. 3-hydroxy ester is adjusted so that the feed rate of 3-hydroxy ester compound based solely on the LHSV is 0.01 ~ 5hr ^-1, preferably in the range of 0.03 ~ 3hr ^-1 when calculating the solution, and hydrogen consumption is platoon 3 The molar ratio of the hydroxyester compound is adjusted to be in the range of 10 to 300: 1, preferably 20 to 200: 1.

On the other hand, when the 3-hydroxyester compound is hydrogenated by gas phase method, the 3-hydroxyester compound is added in a dissolved state in an alcohol solvent, and the mixing ratio of the 3-hydroxyester compound and the alcohol is 10:90. 90:10 (w / w), Preferably it is 30: 70-70: 30 (w / w).

In the gas phase reaction method, a catalyst is charged to a reactor and a relatively high partial pressure of hydrogen gas and a 3-hydroxyester-containing solution are introduced under the same direction of flow, and the 3-hydroxyester compound reacts with hydrogen gas in a vaporized state. do.

Suitable reaction conditions for synthesizing 1,3-alkanediol from 3-hydroxyester compound in gas phase reaction are 130-200 ° C, preferably 140-200 ° C, and reaction pressure 100-3,000 psig, preferably Preferably from 200 to 1500 psig. Adjusted to 3-hydroxy ester in the feed rate in the range of LHSV is 0.02 ~ 1.0hr ^-1, preferably 0.05 ~ 0.20hr ^-1 when calculating, based only the 3-hydroxy ester compound of the solution, and hydrogen consumption is The molar ratio of the large 3-hydroxyester compound is adjusted to be in the range of 300 to 3,000: 1, preferably 500 to 1,500: 1. By carrying out the gas phase reaction under such conditions, it is possible to achieve high conversions of up to 99% or more without reducing the selectivity.

The alcohol usable above is not particularly limited, but C ₅ or less linear or nonlinear alcohols such as methanol, ethanol, propanol, isopropanol, n-butanol, isobutanol and t-butanol are used to facilitate separation and purification after the reaction. Good to do. In particular, when the gas phase method is adopted, it is preferable to use a low boiling alcohol, preferably methanol, having a lower boiling point than 1,3-alkanediol.

High boiling point solvents are well mixed with 3-hydroxyester compounds and have a high break point, and any difference can be used as long as the break point with the resulting 1,3-alkanediol is large and there is no problem in separation and purification. Tetra (ethylene glycol) dimethyl ether: hereinafter, TEGDME], pentaethylene glycol dimethyl ether, or sulfolane (ether compound) such as sulfolane is preferable.

Under the hydrogenation catalyst according to the present invention, in the preparation of 1,3-alkanediol from 3-hydroxyester compound within the range of the reaction conditions described above, the one-time per pass conversion is 30 to 99%, preferably 60 to 98 The reaction conditions are adjusted to fall within the range of%, more preferably within the range from 80 to 98%. If the reaction conditions are severe in order to maintain the conversion rate above 99%, the selectivity is poor. In order to increase the conversion rate of the 3-hydroxyester compound, a part of the product is separated and recycled without being purified, or after the separation and purification, the unreacted 3-hydroxyester compound and the condensation reaction by-product are recycled together. You can choose how to make it.

The invention can be more clearly understood by the following examples, the following examples are merely for the purpose of illustrating the invention, and are not intended to limit the scope of the invention.

Example 1 :

(1) Preparation of Hydrogenation Catalyst CuO (70 wt.%)-SiO ₂ (30 wt.%)

60.0 g of copper nitrate [Cu (NO ₃ ) ₂ .3H ₂ O] was dissolved in 400 ml of distilled water, and 124 ml of 16 wt% aqueous sodium hydroxide solution was added to precipitate. 21.2 g of colloidal silica aqueous solution Ludox AS-40 (stable ammonium, containing 40% by weight of silica) was added to the precipitated solution, and then aged at 70-80 ° C. for 4 hours. The precipitated slurry solution was washed with distilled water and dried at 120 ° C. for 12 hours, and the powder was compacted by pressing and fractionated to a size of 20-40 mesh after crushing. This was baked at 450 degreeC and air atmosphere for 6 hours. The calcined catalyst oxide was analyzed by XRD (XRD line broading method) and the crystal size of copper oxide was 4.5 nm and the BET specific surface area was 172 m ² / g.

(2) catalytic reduction

3.0 g of the calcined oxide catalyst was charged in a tubular reactor (1.27 cm outer diameter, 25 cm long), and gradually heated up while flowing a 5% H ₂ / N ₂ mixed gas, and reduced at 300 ° C. for 6 hours.

(3) Hydrogenation of methyl 3-hydroxypropanoate

After reducing activation of the catalyst as described above, the reactor temperature was adjusted to 150 ° C. and the pressure was adjusted to 900 psig using hydrogen gas. After adjusting the flow rate of the hydrogen gas to 90ml / min and flowing into the reactor, the reaction mixture of methyl 3-hydroxypropanoate (HPM), methanol and TEGDME 20:20:20 (w / w / w) HPLC The reaction was performed by injecting in the same direction as the flow of hydrogen gas at 0.015 ml / min using a pump. The product was collected by 10C under the same pressure and analyzed by GC. 50 hours after the start of the reaction, the conversion was 90.26% and the selectivity of 1,3-propanediol was 88.51%.

Comparative Example 1 :

Except for injecting a reactant mixed with 3-hydroxypropanoate (HPM) and methanol at 20:80 (w / w) at a rate of 0.016 ml / min without mixing the high boiling solvent TEGDME in the reaction. The hydrogenation reaction was carried out in the same manner as in (3). As a result, the conversion rate of HPM was 81.21%, and the selectivity of 1,3-propanediol was 74.60%.

Example 2 :

A catalyst of CuO (80 wt.%)-SiO ₂ (20 wt.%) Was prepared in the same manner as in Example (1). A solution in which 0.163 g of Re ₂ O ₇ was dissolved in acetone was added to 10.0 g of the catalyst powder calcined at 450 ° C., and ball milling. After ball milling acetone was blown off at room temperature and dried at 120 ° C. The catalyst was prepared by press molding the dried catalyst powder, crushing and classifying into 20-40 mesh size. 3.0 g of the prepared catalyst was charged to a reactor and reduced at a temperature below 200 ° C. in the same manner as in Example (2), and then activated under pressure using only hydrogen. The hydrogenation reaction was carried out under the same conditions as in Table 1 using the prepared catalyst. The reaction results are shown in Table 1.

Example 3-8 :

In the same manner as in Example 1 (1), a CuO (80 wt%)-SiO ₂ (20 wt%) catalyst was prepared and first calcined at 300 ° C. Pd, Ru, Ag, Se, Te and Mo components were added thereto to prepare a catalyst in the same manner as in Example 3. In this case, Pd was used as a precursor compound by dissolving palladium nitrate (Pd (NO ₃ ) ₂ 2.5H ₂ O) in water, and Ru was used by dissolving ruthenium carbonyl compound (Ru ₃ (CO) ₁₂ ) in ethanol. , Se and Te are silver nitrate (AgNO ₃ ), ammonium selenate ((NH ₄ ) ₂ SeO ₄ ), ammonium tellurium ((NH ₄ ) ₂ TeO ₄ ) and ammonium molybdate ((NH ₄ ) ₆ Mo ₇ O _24. 4H ₂ O) was used after dissolving in water. After drying at 120 ° C. and calcining at 450 ° C. for 6 hours, reduction was carried out as in Example 1 (2), and then hydrogenated under the same conditions as in Table 1. The reaction results are shown in Table 1.

Example 9 :

Hydroxide in an aqueous solution in which copper nitrate and manganese nitrate [Mn (NO ₃ ) ₂ .6H ₂ O] were dissolved in place of an aqueous solution in which only copper nitrate [Cu (NO ₃ ) ₂ ㆍ 3H ₂ O] was dissolved in Example 1 (1). A Mn _0.61 Cu ₁₀ SiO ₂ catalyst was prepared in the same manner as in (1) of Example 1, except that the aqueous solution was precipitated by addition of aqueous sodium solution. The catalyst thus prepared was reduced in the same manner as in Example (2), and then hydrogenated under the same conditions as in Table 1. The reaction results are shown in Table 1.

Catalyst ¹⁾ Reaction conditions % Conversion % Selectivity Temperature (℃) Pressure (psi) H ₂ feed rate (ml / min) Reactant feed rate ²⁾ (ml / min) Example 2 Re _0.067 Cu ₁₀ SiO ₂ 150 900 90 0.015 94.1 88.12 Example 3 Pd _0.040 Cu ₁₀ SiO ₂ 150155 1,0001,000 9090 0.0150.020 94.8691.97 89.6388.36 Example 4 Ru _0.038 Cu ₁₀ SiO ₂ 150155155 1,0001,0001,000 909090 0.0150.0200.025 97.0692.9885.42 85.7287.3788.08 Example 5 Ag _0.022 Cu ₁₀ SiO ₂ 155 900 90 0.015 96.70 84.28 Example 6 Se _0.018 Cu ₁₀ SiO ₂ 150 1,000 90 0.015 92.03 87.04 Example 7 Te _0.067 Cu ₁₀ SiO ₂ 150 1,000 90 0.015 94.81 87.33 Example 8 Mo _0.07 Cu ₁₀ SiO ₂ 150155 1,0001,000 9090 0.01750.0175 92.5597.92 88.0185.43 Example 9 Mn _0.61 Cu ₁₀ SiO ₂ 150145 1,0001,000 9090 0.01750.0175 96.6982.90 88.7887.70

1) Display only atomic ratio of Cu and accelerator

2) HPM: MeOH: TEGDME = 20:20:60 (w / w / w)

Example 10 :

A CuO (80 wt.%)-SiO ₂ (20 wt.%) Catalyst was prepared in the same manner as in Example (1). 10.0 g of the catalyst powder calcined at 450 ° C. for 6 hours was dried in an argon gas atmosphere, dispersed in toluene, 1.5 g of trimethoxyoctylsilane was added thereto, and reacted for 2 hours under reflux of toluene, followed by toluene at room temperature. Washed and dried. After crushing and fractionating to a size of 20-40 mesh after pressurization and molding, 3.0 g of the catalyst was charged into the reactor and firstly reduced to 5% H ₂ / N ₂ mixed gas while slowly raising the temperature to 200 ° C. Thereafter, the mixture was pressurized to 900 psig using only hydrogen, the reactor temperature was adjusted to 150 ° C., and hydrogenation reaction was performed under the same conditions as in Example 1. The reaction results are shown in Table 2.

Reaction conditions HPM Conversion Rate (%) PDO Selectivity (%) Reactant feed rate ¹⁾ (ml / min) Hydrogen supply rate (ml / min) Temperature (℃) Pressure (psig) 0.015 90 150 950 97.41 87.50 0.017 90 150 1,000 98.29 87.15 0.0185 90 150 1,000 94.72 88.86 0.0225 90 155 1,000 98.24 86.26 0.025 90 155 1,000 95.39 86.23

1) HPM: MeOH: TEGDME = 20:20:60 (w / w / w)

Example 11 :

After preparing CuO (80% by weight) -SiO ₂ (20% by weight) catalyst in the same manner as in Example 1 (1), 3.0 g of catalyst was charged to the reactor and activated in the same manner as in (2) of Example 1 I was. Hydrogen gas at a flow rate of 90 ml / min at a reaction condition of 155 ° C and 1000 psig, and 0.015 ml / min of a reactant mixed with 3-hydroxybutyrate, methanol and TEGDME at 20:20:60 (w / w / w) The reaction was carried out while flowing in the same direction at the flow rate. The conversion of methyl 3-hydroxybutyrate was 82.85% and the selectivity to 1,3-butanediol was 74.35%.

Example 12 :

After the CuO-Mn-SiO ₂ catalyst was prepared and reduced in the same manner as in Example 9, a table was introduced while introducing a reactant containing methyl 3-hydroxypropanoate and 40:60 (w / w) into the reactor. Gas phase hydrogenation was carried out under the same conditions as in step 3. The reaction results are shown in Table 3.

Reaction condition HPM Conversion Rate (%) % Selectivity Temperature (℃) Pressure (psig) LHSV (hr ^-1 ) H ₂ / HPM (mol / mol) PDO 1-propanol Methyl propionate Etc 155 600 0.096 900 98.77 88.79 7.23 2.29 1.69 155 600 0.107 810 97.46 89.12 6.04 2.32 2.52 153 750 0.107 850 99.13 89.07 6.61 2.80 1.52 153 750 0.096 950 99.35 89.06 6.74 2.55 1.11 160 450 0.129 670 95.08 85.98 7.71 3.72 2.59 160 600 0.129 670 97.94 86.07 8.0 3.54 2.39

In the process for producing 1.3-alkanediols by hydrogenating 3-hydroxyester compounds, it is possible to produce 1.3-alkanediols with high activity and high selectivity under the catalyst and reaction system of the present invention.

Claims (16)

A method of producing 1,3-alkanediol by hydrogenating a 3-hydroxyester compound on a catalyst prepared by adding an alkaline precipitant to an aqueous copper salt solution, followed by aging by adding colloidal silica. The method of claim 1 wherein the alkaline precipitant is an alkali carbonate or sodium hydroxide. The method of claim 1, wherein the catalyst has a weight ratio of copper oxide (CuO) to silica (SiO ₂ ) in the range of 9: 1 to 5: 5. According to claim 1, wherein the catalyst is rhenium (Re), palladium (Pd), ruthenium (Ru), platinum (Pt), rhodium (Rh), silver (Ag), selenium (Se), tellurium (Te), Method for using at least one element selected from the group consisting of molybdenum (Mo) and manganese (Mn) containing 0.001 to 10 mol% compared to copper. The catalyst according to claim 1, wherein the catalyst is modified with a trialkoxy monoalkylsilane, dialkoxydialkylsilane or monoalkoxytrialkylsilane compound wherein the alkyl group has a carbon number ranging from C ₁ to C ₃₀ and the alkoxy group is a methoxy or ethoxy group. How to use. The method according to any one of claims 1 to 5, wherein the 3-hydroxyester compound is methyl 3-hydroxypropanoate. The method according to any one of claims 1 to 5, wherein the hydrogenation reaction is carried out by a liquid-based method under a mixed solvent of an alcohol solvent and a high boiling point solvent having a boiling point higher than that of 1,3-alkanediol. The method of claim 7, wherein tetra (ethylene glycol) dimethyl ether, pentaethylene glycol dimethyl ether or sulfolane is used as the high boiling point solvent, and the ratio of the alcohol to the high boiling point solvent is from 5:95 to 9. 90:10 (w / w). The method according to claim 7, wherein the 3-hydroxyester compound is dissolved in the mixed solvent at a concentration of 2 to 95% by weight. The method of claim 7, wherein the hydrogenation reaction is carried out using a fixed bed reactor at a reaction temperature of 100 ° C. to 250 ° C. and a reaction pressure of 50 to 3,000 psig. The process according to claim 10, wherein the molar ratio of hydrogen and 3-hydroxyester compound introduced into the hydrogenation reaction is 10: 1 to 300: 1. The method according to any one of claims 1 to 5, wherein the hydrogenation reaction is carried out by a gas phase method under a low boiling alcohol solvent having a boiling point lower than that of 1,3-alkanediol. 13. The method of claim 12, wherein the low boiling alcohol solvent is methanol. 13. The method of claim 12, wherein the ratio of alcohol solvent to 3-hydroxyester compound is from 10:90 to 90:10 (w / w). The method of claim 12, wherein the hydrogenation reaction is carried out using a fixed bed reactor at a reaction temperature of 130 ° C. to 200 ° C. and a reaction pressure of 100 to 3,000 psig. The process according to claim 15, wherein the molar ratio of hydrogen and 3-hydroxyester compound introduced into the hydrogenation reaction is 300: 1 to 3,000: 1.