| 摘要 |
The reactor (1) for continuous oxide hydrogenation of a feed gas flow (2) of saturated hydrocarbons, which are previously mixed with a gas flow (3) containing oxygen, on a moving catalyst bed (4) arranged between two concentric cylindrical holding devices (5, 6) in the longitudinal direction of the reactor by leaving a central inner space and an intermediate space, comprises four reactor sections, which are separated from each other and split into sub-sections by alternating disk-type deflector plates arranged in the central inner space. The reactor (1) for a continuous oxide hydrogenation of a feed gas flow (2) of saturated hydrocarbons, which are previously mixed with a gas flow (3) containing oxygen, on a moving catalyst bed (4) arranged between two concentric cylindrical holding devices (5, 6) in the longitudinal direction of the reactor by leaving a central inner space and an intermediate space between the moving catalyst bed and an inner envelope of the reactor to obtain a reaction gas mixture, comprises four reactor sections, which are separated from each other and split into sub-sections by alternating disk-type deflector plates arranged in the central inner space, and annular deflector plates arranged in the intermediate space between the moving catalyst bed and the inner envelope of the reactor. Each reactor sections comprise a mixing device, which is arranged in the direction of flow of the reaction gas mixture upstream of the moving catalyst bed. The mixing device is formed from two or three successively arranged rows of tubes having turbulence generators on the outer side of the tubes, which narrow the cross-section for the passage of the feed gas flow to 1/3-1/6 of the free cross-section. The oxygen-containing gas flow is guided through the tubes and sprayed into the feed gas flow through holes in the tubes in addition to a perforated plate mounted upstream of the tubes and a further perforated plate mounted downstream of the tubes. The tubes are ribbed tubes with the turbulence generators. The holes in rib gears are arranged between the ribs of the ribbed tubes. The ribbed tubes have 100-300 circulations of the ribs per meter length of the ribbed tubes, are formed from tubes with cylindrical outer circumference and are welded in spiral-shaped manner on the outer circumference along a strip longitudinal edge from a longitudinal strip containing ribs, which are notched under the formation of segments with exception of a rib base. An outer diameter of the tubes is 20-50 mm. A ratio of the height of the ribs to the outer diameter of the tubes is 1/10:1/2. The segments are distorted against the rib base in an angle. A thickness of the ribs is 0.3-1.5 mm and a width of the segments is 4-8 mm. The second row of the ribbed tubes is arranged in a gap to the first row of the ribbed tubes. The third row of the ribbed tubes is arranged in a gap to the second row of the ribbed tubes. The diameter of the holes in the upstream perforated plate is smaller than the half of the small distance of the ribs between two sequential circulations on each other. A ratio of the perforated plate thickness to the diameter of the holes in the perforated plate is 0.75:2.0. The diameter of the holes in the downstream perforated plate is larger or same to the diameter of the holes in the upstream perforated plate. The upstream perforated plate is arranged in a distance to flowing level of the first row of the ribbed tubes through the feed gas flow according to 7-20 times of the diameter of the holes in the upstream perforated plate. Two holes per rib gear are arranged between the ribs at diametrically opposite positions of the rib gears with small distance to the adjacent ribbed tubes in the row of the ribbed tubes. A ratio of the holes in the upstream perforated plate is defined as sum of the free surfaces of the holes in the upstream perforated plate related to the entire cross-section area vertical to the supply direction of the feed gas flow to the mixing device of = 0.3. The downstream perforated plate is spaced from the flowing level of the ribbed tubes around 0.5-2 times of the diameter of the ribbed tubes to the last row of the ribbed tubes. A distance of the downstream perforated plate for entering the reaction mixture into the catalyst bed is 5-20 times of the diameter of the holes in the downstream perforated plate. An independent claim is included for a procedure for continuous oxide hydrogenation of a feed gas flow of saturated hydrocarbons. |
