Startup passivation method of hydrocracking catalyst
A hydrocracking and catalyst technology, applied in hydroprocessing process, petroleum industry, hydrocarbon oil treatment, etc., to achieve the effect of energy saving, rational utilization of resources, avoidance of emissions or follow-up treatment
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[0024] Such asfigure 1 As shown, an embodiment of the hydrocracking catalyst start-up passivation method of the present invention is as follows:
[0025] After the light oil 1 with relatively high nitrogen content is mixed with hydrogen 2, it enters the hydrofining reactor 3 with an inlet temperature of 150-205°C, and the product 6 obtained after the reaction effluent 4 passes through the cooling heat exchange system 5 enters the separation system 7. The gas phase 9 obtained at the top goes to the hydrogen compressor, and the liquid phase 8 obtained by the separation system 7 enters the fractionation system 10, and after fractionation, the product exits the device; When the temperature rises higher, it generally exceeds 100°C. At this time, the product 4 obtained at this time passes through the heat exchange cooling system 5 and then lowers the temperature to about 200°C to obtain the product 11, which is mixed with the circulating hydrogen 12 and then enters the hydrocracking ...
Embodiment 1
[0028] use figure 1 process shown. After the sulfidation of the catalyst is completed, the inlet temperatures of the refining reactor and the cracking reactor are respectively lowered to 200°C and 180°C.
[0029] Introduce coking naphtha into the refining reactor, increase the temperature of the refining reactor at a rate of 15°C / h, and the refined effluent directly enters the separation system; when the temperature rise of the refining reactor reaches 130°C and is stable, the refined effluent is replaced The heat enters the cracking reactor, and the inlet temperature of the cracking reactor is maintained not higher than 205°C, waiting for ammonia to penetrate.
[0030] When the ammonia concentration in the water of the separation system reaches 0.5wt%, the inlet temperature of the cracking reactor is increased at a rate of 6°C / h through heat exchange, and the ammonia concentration in the water of the separation system is kept above 0.5wt% during the temperature rise; when th...
Embodiment 2
[0034] Main process is with embodiment 1. After the sulfidation is completed, the temperatures of the refining reactor and the cracking reactor are lowered to 180°C and 150°C respectively.
[0035] When the temperature rise of the refining reactor reaches 150° C. and stabilizes, the refining effluent is passed through the cracking reactor.
[0036] Other operations can be carried out according to Example 1.
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