Method and equipment thereof for synthesizing methyl isobuthl ketone with acetone two-step method
A technology of methyl isobutyl ketone and acetone, which is applied in the field of synthesis of methyl isobutyl ketone, can solve the problems of reduced operating pressure of catalytic rectification tower, increased process complexity, increased by-product generation, etc., and achieves an improved balance Improve the conversion rate, reduce energy consumption, and solve the effect of low oil-water separation efficiency
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[0055] Example 1
[0056] Use as figure 1 The process flow of the two-step synthesis of methyl isobutyl ketone with acetone is shown.
[0057] The upper part of the catalytic distillation tower is provided with four-stage heterogeneous catalyst layers, and the lower part is provided with six-stage random packing layers.
[0058] The random packing specification θ ring (Ф3), the theoretical number of packing plates is 42, and the heterogeneous catalyst is acid cation exchange resin Amberlyst 15.
[0059] The acetone feedstock F1 enters the catalytic distillation tower from the top of the tower, the DAA-containing material F2 is extracted from the side line between the third and fourth sections of the catalytic distillation tower, and the acetone-rich gas phase F5 is placed on the catalyst bed in the first and second stages of the catalytic distillation tower The liquid phase output F6 from the acetone flash evaporator is circulated back into the tower between the fourth and fifth sect...
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[0074] Example 2
[0075] The difference from Example 1 is that the DAA decomposition reaction temperature in Example 2 is 140° C. and the pressure is 5.5 bar. Others are the same as those described in Example 1.
[0076] The content of DAA in F7 extracted from the sideline product of the catalytic distillation tower: 5.6%;
[0077] The water content in F10 from the organic phase of the phase separator: 5.9%;
[0078] The MSO content in F11 of the water phase of the phase separator: 4.7%;
[0079] MIBK product F21 was collected from the side line, and the purity was 99.55% by gas chromatography.
[0080] Other results are shown in Table 1 and Table 2.
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[0081] Example 3
[0082] The difference from Example 1 is that in Example 3, the DAA decomposition reaction temperature is 160° C. and the pressure is 8.1 bar, and the others are the same as those described in Example 1.
[0083] The content of DAA in F7 extracted from the sideline product of the catalytic distillation tower: 2.2%;
[0084] The water content in F10 from the organic phase of the phase separator: 1.8%;
[0085] MSO content in F11 of the water phase of the phase separator: 1.5%;
[0086] MIBK product F21 was collected from the side line, and the purity was 99.72% by gas chromatography.
[0087] Other results are shown in Table 1 and Table 2.
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