Method and device for fluidized catalytic conversion

Abstract

The invention provides a method for catalytic conversion of heavy oil, which comprises a fluidized catalytic conversion process that: heavy hydrocarbon raw materials contacts a catalyst in a riser reactor or fluidized bed reactor to react; the reaction temperature is 400 to 650 DEG C (preferably 480 to 560 DEG C); the reaction pressure is 0.11 to 0.4MPa; the contact time is 0.05 to 5 seconds (preferably 0.1 to 3 seconds); and the weight ratio of the catalyst to the raw materials ( catalyst to oil ratio) generally is 3 to 15, preferably 5 to 12. The reaction products flow in a settler for catalyst and oil gas separation; the separated catalyst to be regenerated is stripped by a stripping section and enters a regenerator for coke burning regeneration; and the regenerated catalyst is cooled or directly returns to the riser reactor to be recycled. The method can solve the problems encountered in the resid-blend ratio improvement and gasoline upgrade and update processes of the prior catalytic conversion.

Description

technical field

[0001] The invention belongs to the field of catalytic cracking and relates to a method and a device for catalytic conversion of heavy oil. The present invention is particularly concerned with high density (such as more than 920kg / m 3 ) method and device for catalytic conversion of naphthenic wax oil. Background technique

[0002] With the worsening and heavy trend of crude oil quality, the blending ratio of catalytic conversion residue oil continues to increase, and the quality of gasoline produced by catalytic conversion, coking, thermal cracking and other processes becomes worse. On the one hand, olefins in gasoline are effective components with high octane number; on the other hand, they produce more pollutants in the combustion process to pollute the environment. Although the olefins in gasoline can be reduced to a very low level by traditional hydrorefining, the octane number is greatly lost. In order to solve the above problems and improve the quali...

Examples

Embodiment 1

[0172] For verifying the effect of the present invention, adopt figure 1 The process flow shown, the process conditions shown in Table 2, the raw materials shown in Table 1 and the CORH catalyst produced by Changling Refinery Catalyst Factory, the test results are shown in Table 3.

[0173] In Table 2, scheme A of the prior art adopts a conventional catalytic conversion process technology: the temperature of the catalyst bed in the regenerator is 680°C, and the reaction temperature is 505°C. The raw material temperature was 200°C, and the agent / oil ratio was 6.0. Therefore, the temperature difference between the regenerant and the raw material is 480°C. The scheme A of prior art has following deficiency:

[0174] (1) The feedstock temperature of 200°C is quite low for the cracking of residue-containing feedstock.

[0175] (2) Although the temperature of the regenerator meets the regeneration requirements, the temperature is too high when in contact with the raw material, w...

Embodiment 2

[0185] For verifying the effect of the present invention, adopt figure 2 In the process flow shown, the heavy oil riser adopts the process conditions shown in Table 2, the raw materials shown in Table 1, and the CORH catalyst produced by the Changling Refinery Catalyst Factory. The test results are listed in Table 4.

[0186] The results in Table 4 show that the yield of coke and dry gas decreased by 2.1%, the volume content of olefins in gasoline decreased by 65%, and the octane number (RON) increased by 0.6 units.

[0187] Table 4

[0188]

product

current technology

Option A this invention

Option B Product yield Wt%

fuel gas 5.2 3.7 LPG 14.4 14.1 gasoline 45.6 49.5 diesel fuel 23.6 25.1 oil slurry 3 － coke 8.2 7.6 total 100.0 100.0 gasoline quality

Olefin content V% 37.2 13.6 Aromatic content V% 31.6 37.9 Octane number RON 90.1 90.7

...

technical field

[0001] The invention belongs to the field of catalytic cracking and relates to a method and a device for catalytic conversion of heavy oil. The present invention is particularly concerned with high density (such as more than 920kg / m 3 ) method and device for catalytic conversion of naphthenic wax oil. Background technique

[0002] With the worsening and heavy trend of crude oil quality, the blending ratio of catalytic conversion residue oil continues to increase, and the quality of gasoline produced by catalytic conversion, coking, thermal cracking and other processes becomes worse. On the one hand, olefins in gasoline are effective components with high octane number; on the other hand, they produce more pollutants in the combustion process to pollute the environment. Although the olefins in gasoline can be reduced to a very low level by traditional hydrorefining, the octane number is greatly lost. In order to solve the above problems and improve the quali...

Examples

Embodiment 1

[0172] For verifying the effect of the present invention, adopt figure 1 The process flow shown, the process conditions shown in Table 2, the raw materials shown in Table 1 and the CORH catalyst produced by Changling Refinery Catalyst Factory, the test results are shown in Table 3.

[0173] In Table 2, scheme A of the prior art adopts a conventional catalytic conversion process technology: the temperature of the catalyst bed in the regenerator is 680°C, and the reaction temperature is 505°C. The raw material temperature was 200°C, and the agent / oil ratio was 6.0. Therefore, the temperature difference between the regenerant and the raw material is 480°C. The scheme A of prior art has following deficiency:

[0174] (1) The feedstock temperature of 200°C is quite low for the cracking of residue-containing feedstock.

[0175] (2) Although the temperature of the regenerator meets the regeneration requirements, the temperature is too high when in contact with the raw material, w...

Embodiment 2

[0185] For verifying the effect of the present invention, adopt figure 2 In the process flow shown, the heavy oil riser adopts the process conditions shown in Table 2, the raw materials shown in Table 1, and the CORH catalyst produced by the Changling Refinery Catalyst Factory. The test results are listed in Table 4.

[0186] The results in Table 4 show that the yield of coke and dry gas decreased by 2.1%, the volume content of olefins in gasoline decreased by 65%, and the octane number (RON) increased by 0.6 units.

[0187] Table 4

[0188]

product

current technology

Option A this invention

Option B Product yield Wt%

fuel gas 5.2 3.7 LPG 14.4 14.1 gasoline 45.6 49.5 diesel fuel 23.6 25.1 oil slurry 3 － coke 8.2 7.6 total 100.0 100.0 gasoline quality

Olefin content V% 37.2 13.6 Aromatic content V% 31.6 37.9 Octane number RON 90.1 90.7

...

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