A method for refining mixed alcohols by rectification-pervaporation coupled process
A technology of pervaporation and alcohol mixing, applied in the field of separation, can solve the problems of using a large number of rectifying towers, high energy consumption, not in line with energy conservation and environmental protection, etc., so as to save reprocessing costs, achieve high purity, and achieve cleanliness. production effect
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Embodiment 1
[0028] The rectification-pervaporation coupling process refines the method for mixed alcohol, and its specific steps are as follows:
[0029] 1) A mixed alcohol solution with a water content of 93.8wt% and a feed flow rate of 15 L / h, the reflux ratio of the dehydration tower is 1, the feed is fed in the middle, and the dehydration tower T1 rectifies and dehydrates, and the distilled material in the tower still is water. Top distillate composition is as shown in table 1;
[0030] 2) The top product enters the crude separation tower T2, the reflux ratio of the crude separation tower is 3, and the middle part feeds; the content of the tower top product is shown in Table 2, and the content of the tower bottom product is shown in Table 3; the obtained tower bottom product enters the separation Phase device V1, the temperature of the phase separator is 50°C, the oil phase product enters the pervaporation device M2 for further dehydration; the top product of the crude separation towe...
Embodiment 2
[0032] Fischer-Tropsch synthetic wastewater mixed alcohol refining process coupled with rectification-pervaporation process, the specific steps are as follows:
[0033] 1) A mixed alcohol solution with a water content of 93.8wt% and a feed flow rate of 15L / h. The reflux ratio of the dehydration tower is 1, and the feed is fed in the middle. It is dehydrated by rectification and dehydration in the dehydration tower T1. Composition is as shown in table 1;
[0034] 2) The top product enters the crude separation tower T2, the reflux ratio of the crude separation tower is 3, and the middle part feeds; the content of the tower top product is shown in Table 2, and the content of the tower bottom product is shown in Table 3; the obtained tower bottom product enters the separation The phase separator V1, the temperature of the phase separator is 50°C, the oil phase product enters the pervaporation device M2 for further dehydration; the top product directly enters the pervaporation devi...
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