Synthesis device of methyl acetate and technological method thereof
A kind of technology of methyl acetate and process method, applied in the field of reactive rectification synthesis device, can solve problems such as reducing rectifying tower products and the like
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example 1
[0023] Example 1: if figure 1 process shown. The number of theoretical plates in each area is shown in Table 1, and the feed flow rate and composition are shown in Table 2. The molar ratio of methanol feed to acetic acid feed is 1.2:1, and the mass ratio of concentrated sulfuric acid to acetic acid feed is 0.5:100. , the feeding positions of concentrated sulfuric acid and methanol (counting from top to bottom) are the 7th theoretical plate, the 15th theoretical plate of the rectification section (1) and the 10th theoretical plate of the stripping section (2). Both are at 30°C, and the heat transfer coefficient of the heat exchanger is 1000W / m 2 .℃. The top reflux ratio of the rectification section (1) of the internal thermally coupled reaction distillation column is 0.76, and the top reflux ratio of the methanol recovery tower (8) is 2.5. The flow rates and compositions of each stream are shown in Table 2. The top temperature of the rectification section (1) is 68.3°C, the di...
example 2
[0029] Example 2: if figure 1 process shown. Feed composition, feed heat state, feed position and the number of theoretical plates in each area and the heat transfer coefficient of the heat exchanger are the same as in Example 1, except that the molar ratio of methanol feed and acetic acid feed becomes 1.3:1. The top reflux ratio of the rectification section (1) of the internal thermally coupled reaction distillation column is 0.76, and the top reflux ratio of the methanol recovery tower (8) is 2.5. The flow rates and compositions of the various streams are shown in Table 3. is 68.6°C, the distillation section (2) still temperature is 75.3°C, the top temperature of the methanol recovery tower (8) is 64.2°C, and the kettle temperature is 99.2°C, the stripping section (2) and the methanol recovery tower operate under normal pressure, rectifying Section (1) pressure is 0.15MPa. The obtained acetic acid conversion rate is 99.45%, and the total heat transfer area required to comp...
example 3
[0032] Example 3: if figure 1 process shown. Except that the methanol feed is a mixture containing a small amount of impurity water with a methanol mass fraction of 98%, the composition of the feed, the thermal state of the feed, the position of the feed, the number of theoretical plates in each area, and the heat transfer coefficient of the heat exchanger are the same as in Example 1. The top reflux ratio of the rectification section (1) of the internal thermally coupled reaction distillation column is 0.73, and the top reflux ratio of the methanol recovery tower (8) is 2.5. The flow rates and compositions of the various streams are shown in Table 4. is 68.3°C, the still temperature of the stripping section (2) is 79.2°C, the top temperature of the methanol recovery tower (8) is 64.3°C, and the kettle temperature is 99.5°C, the stripping section (2) and the methanol recovery tower operate under normal pressure, rectifying Section (1) pressure is 0.15MPa. The obtained acetic...
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