A method for upgrading liquid paraffin and gasoline and diesel oil from shale oil
A technology for liquid paraffin and shale oil, which is applied in the petroleum industry, hydrocarbon oil treatment, hydrotreating process, etc., can solve the problems of shale oil dewaxing, high energy consumption, deactivation, etc. that are not considered, and achieve good economic benefits and industrial application prospects, improve economic benefits, and increase the effect of added value
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Embodiment 1
[0021] The shale oil is cut into distillate and residual oil below 420°C by vacuum distillation. The residual oil is injected into the catalytic distillation tower, and the temperature of the kettle is controlled at 450°C. The distilled oil and gas are reacted and rectified in contact with molecular sieve / alumina catalyst. The catalytic distillation oil is mixed with distillate oil lower than 420℃, and then mixed with hydrogen through the raw material pump, and then heated by the heat exchanger to enter the hydrodewaxing reactor. The feed temperature is controlled at 380℃; the hydrogen partial pressure is 8MPa, and the volume is empty. Speed 1.0h -1 The volume ratio to hydrogen oil is 800:1. The distillate oil after hydrorefining is often distilled under pressure and cut into gasoline according to the distillation temperature ( 150°C, 220°C).
[0022] The yields and properties of liquid paraffin and gasoline and diesel obtained in this example are shown in Table 1, Table 2 ...
Embodiment 2
[0030] The shale oil is cut into distillate and residual oil below 420°C by vacuum distillation. The residual oil is injected into the catalytic distillation tower, and the temperature of the kettle is controlled at 480°C. The distilled oil and gas contact with molecular sieve / alumina catalyst to react and rectify. The catalytic distillation oil is mixed with the distillate oil lower than 420℃, and then enters into the hydrogen dewaxing reactor through the feed pump and heated by the heat exchanger. The feed temperature is controlled at 380℃; the hydrogen partial pressure is 10MPa, and the volume is empty. Speed 0.5h -1 The volume ratio to hydrogen oil is 1000:1. The distillate oil after hydrorefining is often distilled under pressure and cut into gasoline according to the distillation temperature ( 150°C, 220°C).
[0031] The yields and properties of liquid paraffin and gasoline and diesel obtained in this example are shown in Table 4, Table 5 and Table 6, respectively.
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Embodiment 3
[0039] The shale oil is cut into distillate and residual oil below 420°C by vacuum distillation. The residual oil is injected into the catalytic distillation tower, and the temperature of the kettle is controlled at 450°C. The distilled oil and gas are reacted and rectified in contact with molecular sieve / alumina catalyst. The catalytic distillation oil is mixed with distillate oil lower than 420℃, and then mixed with hydrogen through the raw material pump and heated by the heat exchanger to enter the hydrodewaxing reactor. The feed temperature is controlled to 360℃; the hydrogen partial pressure is 12MPa, and the volume is empty. Speed 0.5h -1 The volume ratio to hydrogen oil is 600:1. The distillate oil after hydrorefining is often distilled under pressure and cut into gasoline according to the distillation temperature ( 150°C, 220°C).
[0040] The yields and properties of liquid paraffin and gasoline and diesel obtained in this example are shown in Table 7, Table 8, and ...
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