Treatment method of glycidyl methacrylate byproduct tar

Abstract

The invention relates to a preparation method of a cobalt oxide modified supported rhodium-carbon catalyst and a treatment method of glycidyl methacrylate byproduct tar. Through the novel cobalt oxide modified rhodium-carbon catalyst, rhodium metal and cobalt metal are supported on a carrier, so that the activity of the catalyst is improved; the catalyst is applied to hydrogenation reaction in glycidyl methacrylate byproduct tar, and the selectivity of converting 2-oxopropionic acid glycidyl ester into 2-hydracrylic acid glycidyl ester reaches 99% or above.

Description

Technical Field

[0001] The invention relates to the field of tar post-processing, and in particular to a method for processing tar produced as a by-product of glycidyl methacrylate. Background Art

[0002] Glycidyl methacrylate contains vinyl and epoxy rings, which can undergo different reactions: using free radicals to catalyze the opening of double bonds, generating linear polymers containing epoxy rings with other acrylic monomers; epoxy rings cross-link with carboxylic acids in the system under acid or amine catalysis, so this monomer has a wide range of uses. It is mainly used in powder coatings, adhesives, antistatic agents and other fields.

[0003] Glycidyl methacrylate is mainly obtained by condensation reaction of sodium methacrylate and epichlorohydrin, and then separated by distillation tower. During the high-temperature distillation process, glycidyl methacrylate will produce tar containing polyglycidyl methacrylate. The tar components are complex and have a high boiling point. Conventional distillation is difficult to separate and reuse the components. In industry, it is generally incinerated as waste tar, resulting in great waste.

[0004] How to realize the reuse of tar and improve the added value of the process is an urgent problem that needs to be solved in the industry. Summary of the invention

[0005] The purpose of the present invention is to provide a method for treating tar produced as a by-product of glycidyl methacrylate, which uses ozone oxidation, hydrogenation and the like to break the carbon-carbon double bonds of a glycidyl methacrylate polymer to generate high value-added products such as 2-oxopropionic acid glycidyl ester and 2-hydroxypropionic acid glycidyl ester, thereby greatly reducing the amount of tar produced and increasing the added value of the products.

[0006] In order to achieve the above object, the technical solution adopted by the present invention is as follows:

[0007] A method for treating tar produced as a by-product of glycidyl methacrylate comprises the following steps:

[0008] a. introducing ozone-oxygen mixed gas into tar for reaction;

[0009] b. After the reaction is completed, stop introducing the ozone-oxygen mixed gas and replace it with a reaction inert gas;

[0010] c. The reaction liquid after ozone oxidation is reacted with hydrogen in the presence of a catalyst.

[0011] Preferably, the tar is a tar containing polyglycidyl methacrylate produced by condensing sodium methacrylate and epichlorohydrin and then distilling through a distillation tower.

[0012] Preferably, in step a, the tar is first dissolved in a solvent and then the mixed gas is introduced, the solvent is one or more of n-hexane, cyclohexane, n-heptane, n-octane or n-decane, and the mass ratio of the solvent to the tar is 2-10:1, preferably 3-8:1.

[0013] Preferably, in step a, in the ozone-oxygen mixed gas, the volume fraction of ozone is 2-16%, and the volume fraction of oxygen is 84-98%; the reaction can be carried out under normal pressure, and the reaction temperature is 10-50°C.

[0014] Preferably, in step b, a reaction inert gas is continuously introduced into the solution to perform replacement until ozone and formaldehyde are no longer detected in the tail gas, thus completing the replacement;

[0015] Preferably, the reaction inert gas is nitrogen.

[0016] Preferably, the catalyst is a supported rhodium-carbon catalyst modified with cobalt oxide.

[0017] In the catalyst, the content of rhodium accounts for 2-8wt% of the mass of the catalyst, preferably 4-6wt%; the content of cobalt accounts for 5-40wt% of the mass of the catalyst, preferably 12-30wt%.

[0018] Preferably, the method for preparing the catalyst comprises the following steps:

[0019] (1) adding activated carbon, a rhodium precursor, and a cobalt precursor into water to obtain an activated carbon dispersion, a rhodium precursor aqueous solution, and a cobalt precursor aqueous solution, respectively;

[0020] (2) mixing the rhodium precursor aqueous solution and the cobalt precursor aqueous solution obtained in step (1) for co-impregnation, wherein the mass ratio of the rhodium precursor to the cobalt precursor is 1:3-7, and co-impregnation is performed;

[0021] (3) adding the mixed solution obtained in step (2) to an activated carbon dispersion for aging, drying and grinding to obtain a solid;

[0022] (4) calcining the solid obtained in step (3) under a nitrogen atmosphere;

[0023] (5) The calcined catalyst obtained in step (4) is reduced by introducing hydrogen under a nitrogen atmosphere to obtain a shaped cobalt oxide-modified supported rhodium-carbon catalyst.

[0024] The rhodium precursor is RhCl 3 , the cobalt precursor is selected from one or more of cobalt nitrate, cobalt sulfate, and cobalt hydroxide;

[0025] More preferably, the cobalt precursor is a mixture of cobalt sulfate, cobalt nitrate and cobalt hydroxide, wherein the molar ratio of cobalt sulfate, cobalt nitrate and cobalt hydroxide is (1-3): (0.5-1.5): (0.5-1.5);

[0026] Preferably, in step (2), the co-impregnation can be carried out under ultrasonic conditions.

[0027] Preferably, in step (3), aging is carried out at 20-50° C. for 10-20 h, preferably under stirring.

[0028] Preferably, in step (3), the mixed solution is slowly added to the activated carbon dispersion over a period of 20-40 minutes.

[0029] Preferably, in step (4) and / or step (5), the purity of nitrogen is greater than 99.5%.

[0030] Preferably, in step (4), the calcination temperature is 400-700°C, preferably 500-550°C; the calcination time is 1-5h, preferably 2-3h. Preferably, in step (5), the hydrogen reduction temperature is 400-700°C, preferably 500-550°C; the hydrogen reduction time is 1-5h, preferably 2-3h.

[0031] In the step c, the reaction temperature is 20-80°C, preferably 30-60°C;

[0032] In the step c, the reaction pressure is 2-20 MPaG; preferably 5-15 MPaG;

[0033] In step c, the feed mass space velocity of the reaction solution is 0.1-1h -1 .

[0034] In step c, the hydrogen is added in the form of a mixture of hydrogen and nitrogen, and the volume space velocity of the mixture of hydrogen and nitrogen is 10-50h -1 , the volume fraction of hydrogen in the mixed gas is 30-60%.

[0035] In the present invention, the solvent can be removed by distillation of the reaction solution, and further distillation is performed to obtain pure products of 2-oxopropionic acid glycidyl ester and 2-hydroxypropionic acid glycidyl ester.

[0036] The beneficial effects of the present invention are:

[0037] The invention solves the problem that the by-product waste tar in the production of glycidyl methacrylate cannot be utilized. About 60%-80% of the tar can be converted into high-value-added 2-oxopropionic acid glycidyl ester and 2-hydroxypropionic acid glycidyl ester through steps such as ozonation and hydrogenation, with a high tar recovery rate, economic and environmental protection.

[0038] The present invention prepares a novel rhodium-carbon catalyst modified with cobalt oxide, whose activity is greatly improved. The modified rhodium-carbon catalyst is applied to the hydrogenation unit in the treatment process of by-product waste tar in the production of glycidyl methacrylate, and the selectivity of the target product 2-hydroxypropionic acid glycidyl reaches more than 99%, realizing a highly selective catalytic reaction process. DETAILED DESCRIPTION

[0039] The present invention is further described below by way of examples, which are not limited to the following examples. The present invention extends to any new features or any new combination disclosed in the specification, and any new method or process steps or any new combination disclosed.

[0040] 1. Sources of main raw materials in the examples:

[0041] 1. Waste tar: The pilot plant of glycidyl methacrylate of Wanhua Chemical Group Co., Ltd. is a tar containing polyglycidyl methacrylate produced during the condensation reaction of sodium methacrylate and epichlorohydrin and then distilled through a distillation tower.

[0042] 2. Rhodium precursor (rhodium chloride trihydrate): Jiangsu Jinwo New Materials Co., Ltd., analytical grade;

[0043] 3. Cobalt nitrate hexahydrate: Jicheng Xinchuang Nonferrous Metal Products Co., Ltd., analytical grade;

[0044] 4. Cobalt sulfate heptahydrate: Jicheng Xinchuang Nonferrous Metal Products Co., Ltd., analytical grade;

[0045] 5. Cobalt hydroxide: Jicheng Xinchuang Nonferrous Metal Products Co., Ltd., analytical grade;

[0046] 6. Activated carbon: Henan Chengying Environmental Protection Technology Co., Ltd., analytical grade;

[0047] 7. n-Hexane: Xilong Scientific Co., Ltd., analytical grade;

[0048] 8. Cyclohexane: Xilong Scientific Co., Ltd., analytical grade;

[0049] 9. n-Octane: Inokai Technology Co., Ltd., analytical grade;

[0050] 10. Ozone is oxygen produced by an ozone generator;

[0051] 2. Product analysis method in the embodiment:

[0052] 1. Gas chromatography is used to analyze the components and contents of the reaction solution and products using the correction factor method. Instrument manufacturer and model: Shimadzu 1020-plus.

[0053] 2. Inductively coupled plasma optical emission spectrometer is used to analyze the metal element content in the catalyst. Instrument manufacturer and model: Agilent 720-OES.

[0054] Example 1 (Catalyst Preparation - Cobalt Loading)

[0055] (1) Place 5 g of activated carbon in a 100 ml round-bottom flask, add deionized water at a solid-liquid mass ratio of 1:10, and stir ultrasonically at 25 °C for 30 min to obtain an activated carbon dispersion; take 0.26 g of rhodium precursor RhCl 3 ·3H 2 O solid, according to the solid-liquid mass ratio of 1:10, added to deionized water, at 25 ° C, ultrasonic stirring for 30 minutes; 0.78g of cobalt precursor (0.34g of cobalt sulfate heptahydrate, 0.33g of cobalt nitrate hexahydrate, 0.11g of cobalt hydroxide) was added to deionized water at a solid-liquid mass ratio of 1:10, at 25 ° C, ultrasonic stirring for 30 minutes;

[0056] (2) The prepared rhodium precursor aqueous solution and cobalt precursor aqueous solution are added dropwise to each other and mixed by co-impregnation method, and then ultrasonicated at a temperature of 25° C. for 30 minutes;

[0057] (3) Put the activated carbon dispersion into a round-bottom flask, stir ultrasonically at 25° C. for 30 min, then stir in a water bath at 25° C. at a speed of 800 rpm, add the cobalt precursor and rhodium precursor mixed solution prepared by the co-impregnation method in step (2) dropwise into the round-bottom flask under stirring, and age at 25° C. for 10 h under stirring (speed of 800 rpm), dry the resulting solution at 115° C. overnight for 14 h, and grind it into powder with a mortar after drying;

[0058] (4) The obtained powdered solid was placed in a vacuum calcination furnace, high-purity nitrogen was introduced, the temperature was raised to 500° C. and calcined for 2 h to obtain a formed catalyst, recorded as Rh-CoOx-C, with a rhodium content of 4.5 wt% and a cobalt content of 12.3 wt%.

[0059] Example 2 (Catalyst Preparation - Cobalt Loading)

[0060] (1) Place 5 g of activated carbon in a 100 ml round-bottom flask, add deionized water at a solid-liquid mass ratio of 1:10, and stir ultrasonically at 25 °C for 30 min to obtain an activated carbon dispersion; take 0.26 g of rhodium precursor RhCl 3 ·3H 2O solid, according to the solid-liquid mass ratio of 1:10, added to deionized water, at 25 ° C, ultrasonic stirring for 30 minutes; 1.82g of cobalt precursor (0.8g of cobalt sulfate heptahydrate, 0.77g of cobalt nitrate hexahydrate, 0.25g of cobalt hydroxide) was added to deionized water at a solid-liquid mass ratio of 1:10, at 25 ° C, ultrasonic stirring for 30 minutes;

[0061] (2) The prepared rhodium precursor aqueous solution and cobalt precursor aqueous solution are added dropwise to each other and mixed by co-impregnation method, and then ultrasonicated at a temperature of 25° C. for 30 minutes;

[0062] (3) Put the activated carbon dispersion into a round-bottom flask, stir ultrasonically at 25° C. for 40 min, then stir in a water bath at 25° C. at a speed of 800 rpm, add the cobalt precursor and rhodium precursor mixed solution prepared by the co-impregnation method in step (2) dropwise into the round-bottom flask under stirring, and age at 25° C. for 20 h under stirring (800 rpm), dry the resulting solution at 115° C. overnight for 14 h, and grind it into powder with a mortar after drying;

[0063] (4) The obtained powdered solid was placed in a vacuum calcination furnace, high-purity nitrogen was introduced, the temperature was raised to 550° C. and calcined for 3 h to obtain a formed catalyst, recorded as Rh-CoOx-C, with a rhodium content of 4.5 wt% and a cobalt content of 28.6 wt%.

[0064] Example 3 (Catalyst Preparation - Cobalt Loading)

[0065] (1) Place 5 g of activated carbon in a 100 ml round-bottom flask, add deionized water at a solid-liquid mass ratio of 1:10, and stir ultrasonically at 25 °C for 30 min to obtain an activated carbon dispersion; take 0.26 g of rhodium precursor RhCl 3 ·3H 2 O solid, according to the solid-liquid mass ratio of 1:10, added to deionized water, at 25 ° C, ultrasonic stirring for 30 minutes; 1.30g of cobalt precursor (0.57g of cobalt sulfate heptahydrate, 0.55g of cobalt nitrate hexahydrate, 0.18g of cobalt hydroxide) was added to deionized water at a solid-liquid mass ratio of 1:10, at 25 ° C, ultrasonic stirring for 30 minutes;

[0066] (2) The prepared rhodium precursor aqueous solution and cobalt precursor aqueous solution are added dropwise to each other and mixed by co-impregnation method, and then ultrasonicated at a temperature of 25° C. for 40 min;

[0067] (3) Put the activated carbon dispersion into a round-bottom flask, stir ultrasonically at 25° C. for 30 min, then stir in a water bath at 25° C. at a speed of 800 rpm, add the cobalt precursor and rhodium precursor mixed solution prepared by the co-impregnation method in step (2) dropwise into the round-bottom flask under stirring, and age at 25° C. for 18 h under stirring (speed of 800 rpm), dry the resulting solution at 115° C. overnight for 14 h, and grind it into powder with a mortar after drying;

[0068] (4) The obtained powdered solid was placed in a vacuum calcination furnace, high-purity nitrogen was introduced, the temperature was raised to 530° C. and calcined for 2.5 h to obtain a formed catalyst, recorded as Rh-CoOx-C, with a rhodium content of 4.5 wt% and a cobalt content of 20.4 wt%.

[0069] Comparative Example 1 (Catalyst Preparation-No Cobalt Loading)

[0070] (1) Place 5 g of activated carbon in a 100 ml round-bottom flask, add deionized water at a solid-liquid mass ratio of 1:10, and stir ultrasonically at 25 °C for 30 min to obtain an activated carbon dispersion; take 0.26 g of rhodium precursor RhCl 3 ·3H 2 O solid, according to the solid-liquid mass ratio of 1:10, was added into deionized water and ultrasonically stirred at 25°C for 30 min;

[0071] (2) Put the activated carbon dispersion into a round-bottom flask, stir it ultrasonically at 25°C for 30 minutes, then stir it in a water bath at 25°C and 800 rpm, add the rhodium precursor mixed solution in (1) dropwise into the round-bottom flask under vigorous stirring, and age it at 25°C at 800 rpm for 10 hours. Dry the resulting solution at 115°C overnight for 14 hours, and grind it into powder with a mortar after drying;

[0072] (3) The obtained powdered solid was placed in a vacuum calcination furnace, high-purity nitrogen was introduced, the temperature was raised to 500°C and calcined for 2 hours to obtain a formed catalyst, which was recorded as Rh-C.

[0073] Example 4 (tar treatment + Rh-CoOx-C catalyst)

[0074] Prepare a n-hexane solution of waste tar, in which the mass of n-hexane is 3 times that of tar. After uniform mixing, introduce a mixed gas of ozone-oxygen (in which the volume fraction of ozone is 10% and the volume fraction of oxygen is 90%) into the above solution. The reaction pressure is normal pressure and the reaction temperature is 50°C. When the ozone concentration detector detects that the ozone concentration in the reaction tail gas remains unchanged, stop ventilation. Pass nitrogen into the solution until no ozone and formaldehyde are detected in the tail gas. The intermediate solution after ozone oxidation is continuously passed into a fixed bed reactor, and a mixed gas of hydrogen and nitrogen (the volume fraction of hydrogen in the mixed gas is 60%) is continuously passed. The catalyst used in the fixed bed is the Rh-CoOx-C catalyst prepared in Example 1. The reaction temperature is 30°C, the reaction pressure is 5MPa, and the mass space velocity of the reaction liquid is 0.1h -1 , the volume space velocity of hydrogen and nitrogen is 50h -1 The liquid after the reaction was distilled to remove the solvent, thereby obtaining 2-oxopropionic acid glycidyl ester and 2-hydroxypropionic acid glycidyl ester, and the selectivity of 2-hydroxypropionic acid glycidyl ester was 99.18%.

[0075] The specific results of the reaction are shown in Table 1;

[0076] Example 5 (tar treatment + Rh-CoOx-C catalyst)

[0077] Prepare a cyclohexane solution of waste tar, in which the mass of n-hexane is 8 times that of tar. After uniform mixing, introduce a mixed gas of ozone-oxygen (in which the volume fraction of ozone is 15% and the volume fraction of oxygen is 85%) into the above solution. The reaction pressure is normal pressure and the reaction temperature is 50°C. When the ozone concentration detector detects that the ozone concentration in the reaction tail gas remains unchanged, stop ventilation. Pass nitrogen into the solution until no ozone and formaldehyde are detected in the tail gas. The intermediate solution after ozone oxidation is continuously passed into a fixed bed reactor, and a mixed gas of hydrogen and nitrogen (the volume fraction of hydrogen in the mixed gas is 30%) is continuously passed. The catalyst used in the fixed bed is the Rh-CoOx-C catalyst prepared in Example 2. The reaction temperature is 60°C, the reaction pressure is 15MPa, and the mass space velocity of the reaction liquid is 1h -1 , the volume space velocity of hydrogen and nitrogen is 10h -1 The liquid after the reaction was distilled to remove the solvent, thereby obtaining 2-oxopropionic acid glycidyl ester and 2-hydroxypropionic acid glycidyl ester, and the selectivity of 2-hydroxypropionic acid glycidyl ester was 99.34%.

[0078] The specific results of the reaction are shown in Table 1;

[0079] Example 6 (tar treatment + Rh-CoOx-C catalyst)

[0080] Prepare a cyclohexane solution of waste tar, in which the mass of n-hexane is 4 times that of tar. After uniform mixing, introduce a mixed gas of ozone-oxygen (in which the volume fraction of ozone is 8% and the volume fraction of oxygen is 92%) into the above solution. The reaction pressure is normal pressure and the reaction temperature is 40°C. When the ozone concentration detector detects that the ozone concentration in the reaction tail gas remains unchanged, stop ventilation. Pass nitrogen into the solution until no ozone and formaldehyde are detected in the tail gas. The intermediate solution after ozone oxidation is continuously passed into a fixed bed reactor, and a mixed gas of hydrogen and nitrogen (the volume fraction of hydrogen in the mixed gas is 30%) is continuously passed. The catalyst used in the fixed bed is the Rh-CoOx-C catalyst prepared in Example 3. The reaction temperature is 40°C, the reaction pressure is 10MPa, and the mass space velocity of the reaction liquid is 0.5h -1 , the volume space velocity of hydrogen and nitrogen is 20h -1 The liquid after the reaction is distilled to remove the solvent, thereby obtaining 2-oxopropionic acid glycidyl ester and 2-hydroxypropionic acid glycidyl ester, and the selectivity of 2-hydroxypropionic acid glycidyl ester is 99.09%.

[0081] The specific results of the reaction are shown in Table 1;

[0082] Example 7 (tar treatment + Rh-CoOx-C catalyst)

[0083] Prepare an n-octane solution of waste tar, in which the mass of n-octane is 6 times that of tar. After uniform mixing, introduce a mixed gas of ozone-oxygen (in which the volume fraction of ozone is 10% and the volume fraction of oxygen is 90%) into the above solution. The reaction pressure is normal pressure and the reaction temperature is 50°C. When the ozone concentration detector detects that the ozone concentration in the reaction tail gas remains unchanged, stop ventilation. Pass nitrogen into the solution until no ozone and formaldehyde are detected in the tail gas. The intermediate solution after ozone oxidation is continuously passed into a fixed bed reactor, and a mixed gas of hydrogen and nitrogen (the volume fraction of hydrogen in the mixed gas is 50%) is continuously passed. The catalyst used in the fixed bed is the Rh-CoOx-C catalyst prepared in Example 1. The reaction temperature is 30°C, the reaction pressure is 8MPa, and the mass space velocity of the reaction liquid is 0.5h -1 , the volume space velocity of hydrogen and nitrogen is 10h -1 The liquid after the reaction was distilled to remove the solvent, thereby obtaining 2-oxopropionic acid glycidyl ester and 2-hydroxypropionic acid glycidyl ester, and the selectivity of 2-hydroxypropionic acid glycidyl ester was 99.21%.

[0084] The specific results of the reaction are shown in Table 1;

[0085] Comparative Example 2 (tar treatment + Rh-C catalyst)

[0086] Prepare a n-hexane solution of waste tar, in which the mass of n-hexane is 3 times that of tar. After uniform mixing, pass a mixed gas of ozone-oxygen (in which the volume fraction of ozone is 10% and the volume fraction of oxygen is 90%) into the above solution. The reaction pressure is normal pressure, the reaction temperature is 50°C, and the ozone concentration detector detects that the ozone concentration in the reaction tail gas is unchanged, then stop the ventilation. Pass nitrogen into the solution until no ozone and formaldehyde are detected in the tail gas. The intermediate solution after ozone oxidation is continuously passed into a fixed bed reactor, and a mixed gas of hydrogen and nitrogen (the volume fraction of hydrogen in the mixed gas is 60%) is continuously passed. The catalyst used in the fixed bed is the Rh-C catalyst prepared in Comparative Example 1. The reaction temperature is 30°C, the reaction pressure is 5MPa, and the mass space velocity of the reaction liquid is 0.1h -1 , the volume space velocity of hydrogen and nitrogen is 50h -1 The liquid after the reaction was distilled to remove the solvent, thereby obtaining 2-oxopropionic acid glycidyl ester and 2-hydroxypropionic acid glycidyl ester, and the selectivity of 2-hydroxypropionic acid glycidyl ester was 55.38%.

[0087] The specific results of the reaction are shown in Table 1;

[0088] Table 1 The conversion rate of tar and the selectivity of each product in each example

[0089]

Claims

1. A method for treating tar produced as a by-product of glycidyl methacrylate, characterized in that: The following steps are involved: a. introducing ozone-oxygen mixed gas into tar for reaction; b. After the reaction is completed, stop introducing the ozone-oxygen mixed gas and replace it with a reaction inert gas; c. The reaction liquid after ozone oxidation is reacted with hydrogen in the presence of a catalyst.

2. The processing method according to claim 1, characterized in that: The tar is tar containing polyglycidyl methacrylate produced by condensing sodium methacrylate and epichlorohydrin and then distilling through a distillation tower.

3. The processing method according to claim 1 or 2, characterized in that: In the step a, the tar is first dissolved in a solvent and then an ozone-oxygen mixed gas is introduced, the solvent is one or more of n-hexane, cyclohexane, n-heptane, n-octane or n-decane, and the mass ratio of the solvent to the tar is 2-10:1, preferably 3-8:1; Preferably, in step a, in the ozone-oxygen mixed gas, the volume fraction of ozone is 2-16%, and the volume fraction of oxygen is 84-98%; the reaction can be carried out under normal pressure, and the reaction temperature is 10-50°C.

4. The processing method according to any one of claims 1 to 3, characterized in that: In the step b, a reaction inert gas is continuously introduced into the solution to perform replacement until no ozone and formaldehyde are detected in the tail gas, and the replacement is completed; Preferably, the reaction inert gas is nitrogen.

5. The processing method according to any one of claims 1 to 4, characterized in that: The catalyst is a supported rhodium-carbon catalyst modified by cobalt oxide; Preferably, in the catalyst, the content of rhodium accounts for 2-8wt% of the catalyst mass, preferably 4-6wt%; Preferably, the content of cobalt is 5-40 wt%, preferably 12-30 wt%, based on the mass of the catalyst.

6. The processing method according to any one of claims 1 to 5, characterized in that: The preparation method of the catalyst comprises the following steps: (1) adding activated carbon, a rhodium precursor, and a cobalt precursor into water to obtain an activated carbon dispersion, a rhodium precursor aqueous solution, and a cobalt precursor aqueous solution, respectively; (2) mixing the rhodium precursor aqueous solution and the cobalt precursor aqueous solution obtained in step (1) for co-impregnation, wherein the mass ratio of the rhodium precursor to the cobalt precursor is 1:3-7, and co-impregnation is performed; (3) adding the mixed solution obtained in step (2) to an activated carbon dispersion for aging, drying and grinding to obtain a solid; (4) calcining the solid obtained in step (3) under a nitrogen atmosphere; (5) The calcined catalyst obtained in step (4) is reduced by introducing hydrogen under a nitrogen atmosphere to obtain a shaped cobalt oxide-modified supported rhodium-carbon catalyst.

7. The processing method according to claim 6, characterized in that: The rhodium precursor is RhCl3, and the cobalt precursor is selected from one or more of cobalt nitrate, cobalt sulfate, and cobalt hydroxide; More preferably, the cobalt precursor is a mixture of cobalt sulfate, cobalt nitrate and cobalt hydroxide, wherein the molar ratio of cobalt sulfate, cobalt nitrate and cobalt hydroxide is (1-3): (0.5-1.5): (0.5-1.5); Preferably, in step (2), the co-impregnation is performed under ultrasonic conditions; Preferably, in step (3), aging is performed at 20-50° C. for 10-20 h, preferably under stirring; Preferably, in step (3), the mixed solution is slowly added to the activated carbon dispersion, and the adding time is 20-40 minutes; Preferably, in step (4) and / or step (5), the purity of nitrogen is greater than 99.5%; Preferably, in step (4), the calcination temperature is 400-700°C, preferably 500-550°C; the calcination time is 1-5h, preferably 2-3h; Preferably, in step (5), the hydrogen reduction temperature is 400-700°C, preferably 500-550°C; and the hydrogen reduction time is 1-5h, preferably 2-3h.

8. The processing method according to any one of claims 1 to 7, characterized in that: In the step c, the reaction temperature is 20-80°C, preferably 30-60°C; In the step c, the reaction pressure is 2-20 MPaG; preferably 5-15 MPaG; In step c, the feed mass space velocity of the reaction solution is 0.1-1h -1 ; In step c, the hydrogen is added in the form of a mixture of hydrogen and nitrogen, and the volume space velocity of the mixture of hydrogen and nitrogen is 10-50h -1 , the volume fraction of hydrogen in the mixed gas is 30-60%.

9. The processing method according to any one of claims 1 to 8, characterized in that: The reaction solution obtained after the reaction in step c is subjected to distillation to remove the solvent, and further distilled to obtain 2-oxopropionic acid glycidyl ester and 2-hydroxypropionic acid glycidyl ester.

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