Dimethyl oxalate production method with byproduct (dimethyl carbonate)
A technology of dimethyl oxalate and dimethyl carbonate, applied in the purification/separation of carbonate/haloformate, preparation of carbonate/haloformate, separation/purification of carboxylate, etc., capable of Solve the problems of complicated separation process of methanol and dimethyl carbonate, large amount of methanol consumption, complicated process, etc., and achieve the effects of saving equipment investment and floor area, reducing steam consumption, and simplifying equipment
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Embodiment 1
[0051] The gas phase raw material containing CO and methyl nitrite enters the coupling reactor 21 through the pipeline 25, and the output of the coupling reactor enters between the extraction section 22b and the stripping section 22c of the ester separation tower 22 through the pipeline 26, and is connected with the pipeline 33 The dimethyl oxalate absorbing liquid that enters the ester separation tower extraction section 22b top and flows down is countercurrently contacted, and the absorption liquid obtained at the bottom of the extraction section 22b of the ester separation tower flows to the ester separation tower stripping section 22c, and passes through the stripping section 22c After the stripping, the mixture of dimethyl oxalate and dimethyl carbonate obtained by separating from the bottom of the stripping section 22c of the ester separation tower enters the refining tower 23 through a pipeline 29 . The gas phase stream obtained at the top of the extraction section 22b a...
Embodiment 2
[0062] It is the same as [Example 1], except that the equipment parameters and operating conditions of the tower are different.
[0063]The reaction temperature of the coupling reactor is 120°C, and the reaction pressure is 0.3Mpa.
[0064] The ratio of the absorption section to the extraction section of the ester separation tower is 1:1.5, and the number of theoretical plates in the stripping section is 25; the operating pressure is 0.16Mpa; the operating temperature at the top of the tower is 38°C, and the operating temperature at the bottom of the tower is 180°C; The volume ratio of the dimethyl ester) stream to the absorbent (methanol) stream was 2.2:1.
[0065] Dimethyl oxalate refining tower has 40 theoretical plates, reflux ratio 8.5; operating pressure 0.12Mpa; tower top operating temperature 96°C, tower bottom operating temperature 176°C; dimethyl oxalate extractant and dimethyl oxalate product The ratio is 2.3:1; the dimethyl oxalate extractant is cooled to 100°C by...
Embodiment 3
[0071] The implementation is the same as [Example 1], except that the feed composition, reaction conditions, and tower equipment parameters and operating conditions are different.
[0072] The reaction temperature of the coupling reactor is 130°C, and the reaction pressure is 0.4Mpa.
[0073] The ratio of the absorption section to the extraction section of the ester separation tower is 1:2, and the number of theoretical plates in the stripping section is 15; the operating pressure is 0.2Mpa; the operating temperature at the top of the tower is 42°C, and the operating temperature at the bottom of the tower is 186°C; the extractant (oxalic acid The volume ratio of the dimethyl ester) stream to the absorbent (methanol) stream was 1.8:1.
[0074] Dimethyl oxalate refining tower has 30 theoretical plates, reflux ratio 8.8; operating pressure 0.20Mpa; tower top operating temperature 113°C, tower bottom operating temperature 193°C; dimethyl oxalate extractant and dimethyl oxalate pro...
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