Device and method for multistage acetic acid or acetate catalytic hydrogenation-based ethanol preparation
A technology for catalytic hydrogenation and acetic ester, which is applied in chemical instruments and methods, preparation of hydroxyl compounds, preparation of organic compounds, etc. Technological economy, control of bed temperature, effect of reducing hydrogen-acid ratio
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Embodiment 1
[0026] Such as figure 1 Shown: a device for producing ethanol by catalytic hydrogenation of acetic acid or acetate, including a first reactor A, a second reactor B, a first gas-liquid separator C, a second gas-liquid separator D, and circulating hydrogen gas Compressor E, first heater F, first heat exchanger G, second heater H, second heat exchanger I. The heater F is connected to the reactor A through a pipeline; the first reactor A is connected to the first heat exchanger G and the first gas-liquid separator C in turn through the pipeline, and the gas phase outlet of the first gas-liquid separator C is connected to the second A heat exchanger G and a second heater H; the outlet stream of the second heater H is connected to the second reactor B through a pipe; the outlet pipe of the second reactor B is sequentially connected to the second heat exchanger I and the second gas-liquid separation The gas phase outlet of the second gas-liquid separator D is connected to the circula...
Embodiment 2
[0035] press figure 1 As shown, the process flow of the present invention is adopted. The first reactor A and the second reactor B are both continuous heat exchange tubular reactors. The reactor uses saturated process water for heat exchange and by-product steam. The reactor is filled with platinum metal carrier composite catalyst of the same quality . The feed is acetic acid and hydrogen with a purity of 99.8%, the inlet temperature of reactor A is 200°C, the reaction pressure is 1.5MPa, and the acetic acid weight space velocity is 0.1h -1 , The molar ratio of hydrogen acid is 100:1; the inlet temperature of reactor B is 200℃, the reaction pressure is 1.48MPa, and the weight space velocity of acetic acid is 0.1h -1 . The mass ratio of the two acetic acid feed materials is 1:1.
[0036] Test proof:
[0037] 1. The ratio of hydrogen to acid in the entire reaction system is 50:1;
[0038] 2. The actual ratio of hydrogen to acid between the first reactor A and the second reactor B i...
Embodiment 3
[0042] press figure 1 As shown, using the process flow of the present invention, the first reactor A is a layered fixed-bed reactor; the second reactor B is a continuous heat exchange tubular reactor, and the heat exchange medium of the second reactor B is heat transfer oil, The first reactor A and the second reactor B are both filled with the same platinum-containing metal carrier composite catalyst, and the mass ratio of the catalyst bed in the first reactor A and the second reactor B is 1:1.2. The feed is acetic acid and hydrogen with a purity of 99.8%. The inlet temperature of reactor A is 350℃, the reaction pressure is 3.0MPa, and the weight space velocity of acetic acid is 0.7h -1 , The molar ratio of hydrogen acid is 20:1; the inlet temperature of reactor B is 350℃, the reaction pressure is 2.98MPa, and the weight space velocity of acetic acid is 0.7h -1 . The mass ratio of the two acetic acid feed materials is 1:1.2
[0043] Test proof:
[0044] 1. The ratio of hydrogen ...
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