System and method for catalyzing hydrocarbon for recombinant production of high-quality gasoline
A high-quality, catalytic hydrocarbon technology, applied in the direction of gasoline stabilization, refined hydrocarbon oil, petroleum industry, etc., to achieve the effect of low sulfur content, low olefin content and low cost
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Embodiment 1
[0037] Such as figure 1 Shown is a schematic flow diagram of one of the embodiments of the present invention, the distillation range is 30-205 ° C, the sulfur content is 100 ppm, the mercaptan content is 5 ppm, the olefin content is 30% (v), and the diene content is 0.1%. (v), with an aromatic content of 15% (v), an octane number (RON) of 89, and a density of 728 kg / m 3 The stable gasoline (catalytic gasoline) is cut and fractionated in distillation tower 1 with a flow rate of 100,000 tons / year. The tower top temperature of distillation tower 1 is 82 ° C, the tower bottom temperature is 190 ° C, and the tower top pressure is 0.2 MPa (absolute ), the tower bottom pressure is 0.25MPa (absolute), fractionation obtains light gasoline and heavy gasoline respectively, and described light gasoline (distillation range is 30-80 ℃) is steamed by distillation tower 1 top, and its total steaming amount is 4 10,000 tons / year; the heavy gasoline (distillation range is 80-205°C) enters th...
Embodiment 2
[0056] Such as diagram 2-1 Shown is a schematic flow chart of Embodiment 2 of the present invention. The distillation range is 30-205°C, the sulfur content is 100ppm, the mercaptan content is 5ppm, the olefin content is 30% (v), the diene content is 0.1% (v), the aromatic content is 15% (v), octane The alkane number (RON) is 89 and the density is 728 kg / m 3 The stable gasoline (catalytic gasoline) is cut and fractionated in distillation tower 1 with a flow rate of 100,000 tons / year. The tower top temperature of distillation tower 1 is 86 ° C, the tower bottom temperature is 192 ° C, and the tower top pressure is 0.2 MPa (absolute ), the pressure at the bottom of the tower is 0.25MPa (absolute), and the fractional distillation obtains light gasoline and heavy gasoline respectively. Hydrotreating, the total distillation of light gasoline after hydrogenation is 40,000 tons / year; the catalyst in the hydrogenation unit 3-1 is a selective hydrogenation catalyst GHT-20; the hydro...
Embodiment 3
[0063] Such as Figure 2-2 Shown is a schematic flow chart of the third embodiment of the present invention. The distillation range is 30-205°C, the sulfur content is 2000ppm, the mercaptan content is 50ppm, the olefin content is 40% (v), the diene content is 1.0% (v), the aromatic content is 19% (v), octane The alkane number (RON) is 91 and the density is 728 kg / m 3 The stable gasoline (catalytic gasoline) is cut and fractionated in distillation tower 1 with a flow rate of 100,000 tons / year. The tower top temperature of distillation tower 1 is 86 ° C, the tower bottom temperature is 192 ° C, and the tower top pressure is 0.2 MPa (absolute ), the pressure at the bottom of the tower is 0.25MPa (absolute), and the fractional distillation obtains light gasoline and heavy gasoline respectively. Hydrotreating, the total distillation of light gasoline after hydrogenation is 43,000 tons / year; the catalyst in the hydrogenation unit 3-1 is a selective hydrogenation catalyst GHT-20; ...
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