Method of simultaneously producing dimethyl succinate and 1,4-butyl glycol
A technology of dimethyl succinate and dimethyl maleate, which is applied in the field of simultaneous production of dimethyl succinate and 1, can solve problems such as increased cost, increased operating expenses, and increased operating energy consumption, and achieves a regular Effect of pore distribution, less by-products, and high selectivity
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Embodiment 1
[0047] Such as figure 2 The schematic diagram of the process flow shown (other equipment needed in industrial production, such as pumps, heat exchangers, compressors, cycle compressors, safety valves, control valves, storage tanks, etc., are not listed in the accompanying drawings, these Auxiliary equipment can be added according to chemical engineering equipment requirements, etc.). The raw material dimethyl maleate (DMM) of 115.2kg / h enters the low-pressure preheater 2 through pipeline 1, and the circulating hydrogen from the low-pressure cycle compressor merges with the fresh hydrogen from pipeline 8 through pipeline 7, and then passes through pipeline 9 Also enter the low-pressure preheater 2, dimethyl maleate is vaporized under the stripping action of hydrogen, the mol ratio of hydrogen and dimethyl maleate in the mixed steam is 80: 1, and the mixed steam flow enters through pipeline 3 Low-pressure reactor 4, catalyst is housed in the low-pressure reactor 4, under 140 ℃...
Embodiment 2
[0051] Technological process is identical with embodiment 1, and difference is dimethyl maleate feed amount, low-pressure reaction zone hydrogen-ester ratio and medium-pressure reaction temperature, and correspondingly, the output of each product is also different, and wherein, output The purity of the dimethyl succinate product is 99.75% (analyzed by gas chromatography), specifically as shown in table 1.
[0052] In the present embodiment, the catalyst packed in the low-pressure reactor 4 is Cu / ZnO / Al 2 o 3 Three-way catalyst, the preparation process and activation process of the catalyst are as shown in Example 1, except that the molar ratio of Cu, Zn, and Al is 1:0.85:0.25. The loading capacity of the catalyst is about 76kg, the bulk density of the catalyst is about 1.52kg / L, and the specific surface area is 89m 2 / g, the average pore diameter is 19.3nm.
Embodiment 3
[0054] Process flow is identical with embodiment 1, and difference is dimethyl maleate feed amount, low pressure reaction zone hydrogen ester ratio, temperature of reaction and pressure, and the hydrogen ester ratio, temperature and pressure of middle pressure reaction zone, correspondingly , The extraction amount of each product is also different, and wherein, the purity of the dimethyl succinate product of extraction is 99.5% (analyzes with gas chromatography), specifically as shown in table 1.
[0055] In the present embodiment, the catalyst packed in the low-pressure reactor 4 is Cu / ZnO / Al 2 o 3 Three-way catalyst, the preparation process and activation process of the catalyst are as shown in Example 1, except that the molar ratio of Cu, Zn, and Al is 1:0.80:0.25. The loading capacity of the catalyst is about 74kg, the bulk density of the catalyst is about 1.48kg / L, and the specific surface area is 100m 2 / g, the average pore diameter is 20nm.
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