Separation device for maleic anhydride hydrogenation product and process thereof
A technology for a hydrogenation product and a separation device, which is applied in the field of chemical rectification, can solve the problems of large floor space, low energy utilization rate, and large number of rectification towers.
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Embodiment 1
[0035] Such as figure 1 As shown, the separation device of the present invention includes a preheater 1, a vapor-liquid separation tank 2, a bulkhead tower 3 and a vacuum device 4 connected in sequence, and the vapor-liquid separation tank 2 is provided with a defoaming section 2-1, A partition 3-5 is vertically arranged in the next-door tower 3, and the inner cavity of the next-door tower 3 is divided into two regions by the partition 3-5. The left side of the partition 3-5 is the main tower, and the main tower includes the main tower fine Distillation section 3-1, main tower stripping section 3-2 and the feed section arranged between main tower rectifying section 3-1 and main tower stripping section 3-2, main tower includes at least one feed inlet; The right side of the dividing plate 3-5 is the auxiliary tower, which includes the rectifying section 3-6 of the auxiliary tower; the feed material entering the feed section of the main tower is the gas phase material distilled f...
Embodiment 2
[0056] The difference between embodiment 2 and embodiment 1 lies in that the number of trays in each part of the dividing wall column 3 is different and the selection of process parameters is different.
[0057] The maleic anhydride hydrogenation reactant A of 200kmol / h enters the preheater 1 and is heated to 180° C., and after the pressure is 15kPa, it is sent into the vapor-liquid separation tank 2, and the mass fraction of succinic acid produced at the bottom of the tank is 12%. The mass fraction of butenedioic acid is 8% and the heavy fraction is 1.1 kmol / hr. The tank top gas phase enters the main tower of the next-door tower 3, the pressure at the top of the main tower is 13kPa, the number of plates in the rectifying section 3-1 of the main tower is 25 plates, the stripping section 3-2 of the main tower is 30 plates, The reflux ratio of the main tower of the main tower is 0.5, the temperature of the first stage condenser 3-3 of the main tower of the next wall tower 3 is c...
Embodiment 3
[0062] The difference between embodiment 3 and embodiment 1 lies in that the number of trays in each part of the dividing wall column 3 is different and the selection of process parameters is different.
[0063] The maleic anhydride hydrogenation reactant A of 300kmol / h enters the preheater 1 and is heated to 155° C., and after the pressure is 9kPa, it is sent into the vapor-liquid separation tank 2, and the mass fraction of succinic acid produced at the bottom of the tank is 18%. The mass fraction of butenedioic acid is 1.5kmol / hr of the heavy fraction of 12%. The gas phase at the top of the tank enters the main tower of the next-door tower 3, and the pressure at the top of the main tower is 7kPa. The reflux ratio of the main tower of the main tower is 1.0, the temperature of the first stage condenser 3-3 of the main tower of the next wall tower 3 is controlled at 110°C, the temperature of the second stage condenser 3-4 of the main tower 3 of the next wall tower is controlled...
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