Method for operating gasoline hydro-upgrading catalyst comprising molecular sieves
A gasoline hydrogenation and hydrogenation upgrading technology, applied in the petroleum industry, refined hydrocarbon oil and other directions, can solve the problems of inability to use passivation, difficult to ensure the stability of catalyst activity, improve the activity stability and avoid the loss of catalyst activity , the effect of stable start-up
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Embodiment 1
[0024] Fill 500ml gasoline hydrogenation upgrading catalyst A in a 500ml adiabatic bed hydrogenation reactor, and contact with hydrogen and naphtha for 40 hours for activation treatment. The activation reaction temperature is 270℃, the reaction pressure is 2.0MPa, and the volumetric space velocity is 3.0h- 1. The volume ratio of hydrogen to oil is 400:1.
[0025] After the catalyst is activated, the inlet temperature of the reactor is reduced to 250°C, and the catalytic cracking gasoline and naphtha are introduced into the reaction system at the same time according to the amount of FCC gasoline feedstock oil of 252g / h and the amount of naphtha oil of 468g / h; Increase the inlet temperature of the reactor at a heating rate of 3°C / h until the inlet temperature of the reactor reaches 315°C;
[0026] The inlet temperature of the reactor is lowered to 300℃. According to the feedstock oil quantity of FCC gasoline 468g / h and naphtha oil quantity 252g / h, FCC gasoline and naphtha are introdu...
Embodiment 2
[0035] Load 500ml gasoline hydrogenation upgrading catalyst C in a 500ml adiabatic bed hydrogenation reactor, and contact with hydrogen and naphtha for 35 hours for activation treatment. The activation reaction temperature is 240℃, the reaction pressure is 2.4MPa, and the volumetric space velocity is 2.0h- 1. The volume ratio of hydrogen to oil is 450:1.
[0036] After the catalyst activation is completed, the inlet temperature of the reactor is reduced to 230°C, and the coking gasoline and catalytic reforming oil are introduced into the reaction system at the same time according to the coking gasoline feedstock oil quantity 230g / h and the catalytic reforming oil quantity 346g / h; Increase the inlet temperature of the reactor by 10°C / h until the inlet temperature of the reactor reaches 310°C;
[0037] The inlet temperature of the reactor is reduced to 285°C, and the amount of coking gasoline feedstock oil is 346g / h and the amount of catalytic reforming oil is 230g / h. The coking gaso...
Embodiment 3
[0046] The gasoline hydro-upgrading catalyst A is applied to the 1.2 million tons / year catalytic cracking gasoline hydrogenation unit. Contact with hydrogen and naphtha for 48 hours for activation treatment. The activation reaction temperature is 260°C, the reaction pressure is 1.9MPa, the volumetric space velocity is 1.8h-1, and the hydrogen-to-oil volume ratio is 260:1. After activation, according to the flow rate of FCC gasoline feedstock of 64t / h and the flow rate of hydrorefined oil of 78t / h, the FCC gasoline and hydrorefined oil are introduced into the reaction system at the same time, and the system delivers 142t / h of products; ℃ / h Increase the inlet temperature of the reactor until the reactor inlet temperature reaches 310°C;
[0047] The inlet temperature of the hydro-upgrading reactor is reduced to 300°C, and the FCC gasoline feedstock flow rate is 100t / h and the hydrorefined oil product flow rate is 42t / h. FCC gasoline and hydrorefined oil are simultaneously introduced...
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