A process for processing a desulfurized residual oil in a slurry bed wax oil catalytic cracking unit

Abstract

The application relates to a method for processing desulfurized residual oil by a slurry bed wax oil catalytic cracking device, which can process the desulfurized residual oil, and the device can ensure the product yield and the qualified environmental protection indexes by adjusting the reaction heat balance, the equipment operation condition and replacing the catalyst formula, etc. The application can reduce the raw material cost of the device, improve the residual oil processing benefit, and the price of the wax oil is 4600 yuan per ton, the price of the residual oil is 2800 yuan per ton, the price of the residual oil is 1800 yuan per ton lower than that of the wax oil, and the cost of blending 100 tons of residual oil per hour under the current working condition of the device is reduced by 432 million yuan per day.

Description

Technical Field

[0001] This invention relates to the field of oil refining technology for processing residue oil, specifically to a method for processing desulfurized residue oil in a slurry-bed wax oil catalytic cracking unit. Background Technology

[0002] Environmental regulations are imposing increasingly stringent quality requirements on fuels. Currently, my country's standards for controlling hazardous substances in gasoline for vehicles limit the content of olefins, sulfur, and aromatics. Since 2017, the National V standard (GB17930-2013) for gasoline for vehicles has been implemented nationwide, requiring that the olefin content of gasoline not exceed 24%, the aromatic content not exceed 40%, the benzene content not exceed 1.0%, and the sulfur content not exceed 10μg / g.

[0003] Existing slurry-bed wax oil catalytic units and processes cannot process blended residue oil. The coking intensity of the coking tank and dense-phase bed series process is low and cannot meet the coking requirements of cracked residue oil, which easily leads to dilute phase tail combustion in the regenerator. The catalyst has poor cracking performance and is not ideal for heavy oil cracking and product distribution, which easily leads to high catalyst carbon content. The oil slurry yield is high and the properties are poor, which easily causes coking and blockage problems in the fractionation oil slurry system. The heavy oil feedstock has high sulfur, nitrogen and heavy metal content, which increases the catalyst replacement amount and the load on the flue gas denitrification and desulfurization unit is large. Summary of the Invention

[0004] To address the technical deficiencies of existing technologies, this invention provides a method for processing desulfurized residue oil in a slurry-bed wax oil catalytic cracking unit.

[0005] The technical solution adopted in this invention is: a method for processing desulfurized residue oil in a slurry bed wax oil catalytic cracking unit, comprising the following steps:

[0006] (1) After hydrogenation, the slurry bed wax oil is mixed with the residue oil from the tank area and sent to the feed oil tank of this unit. The feed oil is pumped to the feed oil-circulating oil slurry heat exchanger and heated to about 225°C. Then, it is divided into 8 streams and enters the riser reactor through the feed oil atomizing nozzle.

[0007] (2) After the feedstock oil comes into contact with the high-temperature catalyst in the riser reactor, it is heated, vaporized and reacted. The reaction temperature in the riser reactor is 523℃, the reaction pressure is controlled at 220kPa-260kPa, and the regeneration pressure is controlled at 250kPa-290kPa. The oil and gas and catalyst after the reaction are separated by the separation system at the riser outlet to quickly separate the catalyst and oil and gas, so as to terminate the secondary reaction mainly of thermal cracking reaction and reduce the dry gas yield. The catalyst to be generated enters the stripping section set at the bottom.

[0008] (3) The reaction oil and gas after rapid separation and the entrained catalyst fine powder are directly introduced into the single-stage cyclone separator of the settling tank to prevent coking of the settling tank due to oil and gas overflow. After the catalyst fine powder is further separated by the single-stage cyclone separator of the settling tank, the reaction oil and gas enter the lower part of the fractionation tower through the large oil and gas pipeline at the top of the settling tank. The catalyst to be generated after separation by the separation system and the single-stage cyclone separator of the settling tank is in countercurrent contact with the stripping steam in the stripping section to replace the oil and gas carried by the catalyst.

[0009] (4) The carbonized catalyst enters the stripping section, where it comes into countercurrent contact with steam to strip the oil and gas carried by the catalyst. The stripped catalyst flows down along the stripping inclined tube and enters the lower part of the coking tank of the regenerator through the stripping slide valve. It mixes with the high-temperature regenerated catalyst from the two-dense phase to burn coke. During the process of the catalyst flowing upward along the coking tank, most of the coke is burned off. The catalyst with lower carbon content enters the two-dense phase through the large-hole distribution plate at the top of the coking tank. Under the condition of 680~690℃, the coke and CO combustion process is finally completed. The regenerated catalyst enters the bottom of the riser reactor through the regeneration inclined tube and the regeneration slide valve. Under the rise of dry gas / steam, the catalyst acceleration and rectification process is completed. Then it comes into contact with the atomized raw material to vaporize and react.

[0010] (5) The flue gas generated from the regenerated coke is separated from the catalyst by a two-stage cyclone separator and then enters a three-stage cyclone separator to further separate the entrained catalyst. The purified flue gas enters the flue gas machine to recover pressure energy and heat energy, and then enters the waste heat boiler to recover heat energy. It then undergoes NO removal in the denitrification section set up in the waste heat boiler. X After being removed, the gas is sent to the flue gas desulfurization unit. The flue gas desulfurization scrubbing tower uses dual pumps to inject alkali to ensure that the SO2 in the exhaust gas is below 50 mg / m³. 3 After the flue gas desulfurization meets the standards, it is discharged into the atmosphere through the flue gas desulfurization chimney;

[0011] (6) The reaction oil and gas from the settling tank enters the lower part of the fractionation tower, and comes into countercurrent contact with the circulating oil slurry through the herringbone baffle. The catalyst in the reaction oil and gas is washed and superheated, so that the oil and gas are in a "saturated state" before entering the fractionation section for fractionation. The oil and gas at the top of the fractionation tower are cooled to 40°C through the fractionation tower top oil and gas-demineralized water heat exchanger, the fractionation tower top oil and gas dry air cooler, and the fractionation tower top oil and gas condenser. It then enters the fractionation tower top oil and gas separator for gas, liquid, and water three-phase separation. The separated crude gasoline is pressurized by the crude gasoline pump and then enters the absorption stabilization system to be separated into stabilized gasoline and liquefied gas, which are sent to the downstream product refining and SZorb unit. Light diesel oil is separated from the fractionation tower 15 The stripped light diesel oil is drawn from the trays and flows by gravity to the light diesel stripping tower. After stripping, the light diesel oil is pumped out by the light diesel oil pump and heated to 120°C before being sent to the downstream diesel hydrocracking unit. The oil slurry is drawn from the bottom of the fractionation tower by the circulating oil slurry pump, and the liquid phase temperature at the bottom of the fractionation tower is controlled to be ≤335°C. After passing through the feed oil-circulating oil slurry heat exchanger for heat exchange, the oil slurry steam generator generates high-pressure saturated steam, and after the temperature drops to 280°C, it is divided into three paths. One path returns to the upper part of the washing and deheating section of the fractionation tower via the oil slurry upper return tower. Another path returns to the bottom of the fractionation tower via the oil slurry lower return tower. The third path is pressurized by the product oil slurry pump, cooled to 90°C by the product oil slurry-hot water heat exchanger, and sent to the oil slurry tank in the tank area as product oil slurry, ensuring that the amount of oil slurry thrown out is not less than 4% of the unit feed rate.

[0012] The catalyst is an LC-6 cracking wax oil and heavy oil cracking catalyst, and the catalyst consumption is 0.8 kg / t-1.0 kg / t.

[0013] The separation system is an SVQS fast separation system, and the outlet of the SVQS fast separation system is directly connected to the eight sets of single-stage vortex separators in the settling tank.

[0014] The main air required for the regenerator to burn slag in step (5) is provided by the main air fan. The main air enters the main air fan from the atmosphere, and after being pressurized, it enters the regenerator through the main air duct, auxiliary combustion chamber and main air distribution pipe. The oxygen content at the outlet of the regenerator flue gas is controlled at 6%.

[0015] In step (5), CO combustion aid is added to ensure that the dilute phase temperature of the regenerator does not exceed 695°C.

[0016] In step (5), a denitrification combustion aid is added to reduce NO in the flue gas. x Less than 100mg / m 3 .

[0017] In step (1), an interlocking system is provided between the pipelines of slurry bed wax oil and residue oil to cut off the feed when the interlocking shut-off valve is activated.

[0018] In step (5), additional substances are added to the waste heat boiler to reduce SO3 and NO in the flue gas. XSNAR acid removal, denitrification, and reducing agent to ensure particulate matter meets standards.

[0019] The beneficial effects of this invention are as follows: This invention provides a method for processing desulfurized residue oil in a slurry bed wax oil catalytic cracking unit. The unit can process desulfurized residue oil, and by adjusting the reaction heat balance, equipment operating conditions, and changing the catalyst formulation, it ensures product yield and compliance with environmental protection standards. This invention reduces the raw material cost of the unit while increasing the processing revenue of residue oil. The price of wax oil is 4600 yuan per ton, while the price of residue oil is 2800 yuan per ton. The price of residue oil is 1800 yuan per ton lower than that of wax oil. Based on the current operating conditions of the unit, the cost of blending 100 tons of residue oil per hour is reduced by 4.32 million yuan per day. Attached Figure Description

[0020] Figure 1 This is a flowchart illustrating the process flow of the present invention. Detailed Implementation

[0021] The technical solutions of the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings. Obviously, the described embodiments are only a part of the embodiments of the present invention, and not all of them. Based on the embodiments of the present invention, all other embodiments obtained by those skilled in the art without creative effort are within the scope of protection of the present invention.

[0022] The process unit of this invention is designed as the MIP-CGP process, with slurry-bed hydrotreated wax oil as the feedstock. Under high temperature and low pressure operation in the reactor, the strong acid centers on the surface of the catalytic cracking catalyst cause hydrocarbon molecules to undergo a variety of complex reactions, mainly cracking, isomerization, and hydrogen transfer reactions. This transforms large hydrocarbon molecules into a mixture of various small hydrocarbon molecules, and the subsequent fractionation and stabilization system separates dry gas, liquefied petroleum gas, gasoline, diesel, and oil slurry into products. The coke formed during the reaction process is used for process consumption and provides heat.

[0023] The process flow of this invention consists of a reaction-regeneration section, a main blower unit, a fractionation section, a gas compressor section, an absorption stabilization section, a steam generation system, and a waste heat boiler section (including a flue gas denitrification section). Slurry-bed wax oil, after hydrogenation, is mixed with cold wax oil from the tank farm and sent to the feedstock tank of this unit. The feedstock oil is pumped to a feedstock oil-circulating slurry heat exchanger and heated to approximately 225°C. It is then divided into eight streams and enters the riser reactor through feedstock oil atomizing nozzles. Inside the reactor, the feedstock comes into contact with the high-temperature catalyst, undergoes heating, vaporization, and reaction. The reaction temperature is controlled at 523°C, the reaction pressure at 220-260 kPa, and the regeneration pressure at 250-290 kPa. After the reaction, the oil and gas, along with the catalyst, are rapidly separated by the SVQS rapid separation system at the riser outlet to terminate the secondary reaction, primarily thermal cracking, and reduce the dry gas yield. The resulting catalyst then enters the stripping section located below. The outlet of the SVQS fast separation system is directly connected to the settling tank's 8-stage single-stage cyclone separator (the material leg diameter is changed from 325mm to 219mm). The reactant oil and gas after fast separation, along with the entrained catalyst fines, are directly introduced into the settling tank's 8-stage single-stage cyclone separator to prevent coking in the settling tank due to oil and gas spillage. After further separation of the catalyst fines by the settling tank's single-stage cyclone separator, the reactant oil and gas enter the lower part of the fractionation tower through the large oil and gas pipeline at the top of the settling tank. The catalyst awaiting regeneration after separation by SVQS and the settling tank's single-stage cyclone separator comes into countercurrent contact with stripping steam in the stripping section to displace the oil and gas carried by the catalyst. The coked catalyst enters the stripping section, where it comes into countercurrent contact with steam to strip the oil and gas carried by the catalyst. The stripped catalyst flows down the awaiting regeneration inclined tube and enters the lower part of the regenerator's coke burner through the awaiting regeneration slide valve. There, it mixes with the high-temperature regenerated catalyst from the two-phase system for coking. As the catalyst flows upward along the coke burner, most of the coke is burned off. The catalyst with a low carbon content enters the two-density phase at the top of the coke burner through a large-pore distribution plate, and finally completes the combustion process of coke and CO at 680~690℃. The regenerated catalyst enters the bottom of the riser reactor through the regeneration inclined tube and regeneration slide valve. Under the rise of dry gas / steam, the catalyst completes the catalyst acceleration and rectification process, and then contacts the atomized feedstock for vaporization and reaction.

[0024] The main air required for coke burning in the regenerator is supplied by the main fan. The main air enters from the atmosphere into the main fan (K-0101), is pressurized, and then enters the regenerator through the main air duct, auxiliary combustion chamber (F-0101), and main air distribution pipe. The oxygen content at the regenerator flue gas outlet is controlled at 6%. The flue gas generated from regeneration coke burning passes through 12 sets of two-stage cyclone separators to separate the catalyst, and then enters a three-stage cyclone separator to further separate any entrained catalyst. The purified flue gas enters the flue gas fan to recover pressure and heat energy, then enters the waste heat boiler to recover heat energy. After NOx removal through the denitrification section within the waste heat boiler, it is sent to the flue gas desulfurization unit. The flue gas desulfurization scrubbing tower uses dual-pump alkali injection to ensure that SO2 in the exhaust gas is below 50 mg / m³. 3After the flue gas desulfurization meets the standards, it is discharged into the atmosphere through the flue gas desulfurization chimney. Before being discharged into the atmosphere, SNAR acid removal and denitrification reducing agent skids provided by Qingdao Huicheng Environmental Protection Technology Co., Ltd. are added to the desulfurized flue gas to reduce SO3 and NO in the flue gas. X To ensure that the particulate matter content in the flue gas meets the standards, the catalyst used at startup is a customized LC-6 catalyst from PetroChina Lanzhou Catalyst Plant. It is delivered to the regenerator via non-purified compressed air from either a cold catalyst tank (V-0101) or a hot catalyst tank (V-0102). Normal catalyst replenishment is achieved via a small automatic catalyst feeder, with a feed rate of 0.8-1.0 kg / t. CO combustion improver and denitrification combustion improver are delivered to the regenerator via a small feeder pipeline using non-purified compressed air from the combustion improver feed hopper (V-0114) and combustion improver feed tank (V-0113). The addition of CO combustion improver ensures that the dilute phase temperature of the regenerator does not exceed 695℃.

[0025] The reaction oil and gas from the settling tank enter the lower part of the fractionation tower, where it comes into countercurrent contact with the circulating slurry through a herringbone baffle. This washes away the catalyst and removes superheat, bringing the oil and gas to a "saturated state" before it enters the fractionation section for further fractionation. The oil and gas at the top of the fractionation tower are cooled to 40°C via a top oil and gas-demineralized water heat exchanger, a top oil and gas dry air cooler, and a top oil and gas condenser, before entering the top oil and gas separator (V-0203) for three-phase separation of gas, liquid, and water. The separated crude gasoline is pressurized by a crude gasoline pump and then enters an absorption stabilization system to be separated into stabilized gasoline and liquefied petroleum gas (LPG), which are then sent to downstream product refining and the SZorb unit. Light diesel oil is drawn from the 15th tray of the fractionation tower and flows by gravity to the light diesel stripping tower. The stripped light diesel oil is then pumped out by a light diesel oil pump, heated to approximately 120°C, and sent to the downstream diesel hydrocracking unit. The oil slurry is drawn from the bottom of the fractionation tower by a circulating oil slurry pump, with the bottom liquid phase temperature controlled to ≤335℃. After passing through a feed oil-circulating oil slurry heat exchanger, the oil slurry is then heated by a circulating oil slurry steam generator to produce high-pressure saturated steam. Once the steam temperature drops to 280℃, it is divided into three paths: one path returns to the upper part of the fractionation tower's washing and deheating section via the oil slurry return tower; another path returns to the bottom of the fractionation tower via the oil slurry return tower; and the third path, after being pressurized by a product oil slurry pump, is cooled to 90℃ by a product oil slurry-hot water heat exchanger and sent as product oil slurry to the oil slurry tank in the tank area, ensuring that the amount of oil slurry discharged is not less than 4% of the unit's feed rate.

[0026] Key aspects of the process:

[0027] 1. The feedstock preheating temperature is increased from approximately 210℃ to 225℃ (because the properties of residue oil are less fluid and more viscous than those of wax oil, increasing the feedstock preheating temperature allows for full atomization of the feedstock through the nozzle, achieving uniform contact with the catalyst surface for reaction). The reaction temperature is increased from 515℃ to 523℃ (due to the higher amount of residue oil blended, increasing the reaction temperature by 8℃ improves the heavy oil cracking effect and ensures the heavy oil conversion rate). The reaction pressure is increased by 20 kPa compared to the regenerator (the reason for increasing the reaction pressure by 20 kPa is that after the reaction temperature is increased, the heavy oil cracking effect is better, and the amount of oil and gas produced by cracking increases, thus increasing the pressure accordingly; the regeneration pressure is increased by 20 kPa because the coke produced by heavy oil cracking has a higher density than that of wax oil, and requires a higher calorific value for combustion. Increasing the regeneration pressure improves the overall coking intensity and ensures the catalyst regeneration effect).

[0028] 2. The oxygen content of the flue gas at the regenerator outlet is increased from 3% to 6%. The regenerator ensures sufficient main air volume and high regeneration pressure, and controls high-intensity coking of the regenerator (the purpose of increasing the oxygen content to 6% is to ensure that the regenerator is in an oxygen-rich state, with sufficient oxygen to burn the coke).

[0029] 3. Control the liquid phase temperature at the bottom of the fractionation tower to ≤335℃ (after the unit blends residual oil, the content of polycyclic aromatic hydrocarbons in the slurry is high. In order to prevent the polycyclic aromatic hydrocarbons in the slurry from undergoing a high-temperature condensation reaction that leads to coking in the system, controlling the liquid phase temperature to a lower level can reduce the occurrence of this reaction and ensure the long-term operation of heat exchangers, pumps, pipelines, etc. in the unit). The amount of slurry thrown out should not be less than 4% of the feed rate (after heavy oil is sprayed into the reaction feed nozzle, large oil droplets will carry the catalyst, causing the reaction catalyst to be carried to the bottom of the fractionation tower. Maintaining a high slurry displacement rate can ensure the stability of the properties and solid content of the slurry at the bottom of the tower).

[0030] 4. The project team communicated with the China Petroleum Research Institute and China University of Petroleum to adjust the material leg of the top cyclone separator of the reactor from 325mm to 219mm in diameter, so as to enhance the sealing effect of the top material leg of the top cyclone separator and prevent oil and gas backflow from damaging the wing valve and other equipment.

[0031] 5. The project team communicated with China National Petroleum Corporation's Lanzhou Catalyst Plant to adjust the formula and replace the catalyst formula with a new type of LC-6 cracking wax oil catalyst that can also crack heavy oil, which has a better cracking strength for heavy oil and long-chain carbon molecules.

[0032] 6. Increase the catalyst replacement amount. The catalyst consumption is 0.8kg-1.0kg / t. The content of heavy metals (Fe, Ni, V) in the residue oil is much higher than that in slurry bed wax oil. The designed Ni and V content is ≤1mg / kg, but the actual test values ​​are 2.73mg / kg and 1.43mg / kg, which exceed the design values. The catalyst replacement amount is increased accordingly. The high metal content can easily cause catalyst deactivation. The replacement amount is increased to ensure the activity and selectivity of the catalyst.

[0033] 7. Since the process of this unit is a two-stage regeneration technology with the coking tank and the regenerator connected in series (fast bed and turbulent bed main air series connection), the coking intensity is low and cannot meet the coking amount of cracked residue oil, which can easily cause dilute phase tail combustion in the regenerator. CO combustion aid is added to ensure that the dilute phase temperature of the regenerator does not exceed 695℃.

[0034] 8. The flue gas desulfurization unit is operating at high load. The SO2 content at the inlet of the waste heat boiler has increased from 350 mg / m³ to 1400 mg / m³. The flue gas desulfurization alkaline injection pump is running with both pumps activated to ensure that the SO2 content in the exhaust gas is below 50 mg / m³. 3 The nitrogen content in the raw materials is increased, and NOx in the flue gas is reduced to below 100 mg / m3 by adding denitrification combustion aids.

[0035] 9. The newly added mixed desulfurization residue oil pipeline has an interlocking system. When the unit cuts off the feed, the interlocking shut-off valve will be activated, and the residue oil feed will be cut off.

[0036] 10. Due to the high slag ratio and large regeneration coke load, the mismatch between the regenerator load and the reactor load causes the regenerator top agent to run off. Before the flue gas is discharged into the atmosphere, SNAR acid removal and denitrification reducing agent (skid-mounted injection) provided by Qingdao Huicheng Environmental Protection Technology Co., Ltd. is added at the waste heat boiler location to reduce SO3 and NOx in the flue gas and ensure that particulate matter meets the standards.

[0037] Experiments and Results:

[0038] The Zhejiang Petrochemical 3 million tons / year wax oil catalytic cracking unit, which directly sends atmospheric and vacuum residue to coking, can be roughly calculated as follows: (product benefits of catalytic processing - catalytic energy consumption cost) - (product benefits of coking - coking energy consumption cost) - energy consumption cost of residue hydrogenation.

[0039] Comparison of yields between Phase I coking and Phase II catalytic cracking:

[0040]

[0041] The product benefit of processing 1 ton of residual oil by catalysis is 1183 yuan higher than that by coking.

[0042] The energy consumption costs of the three sets of equipment are shown in the table below:

[0043]

[0044] The energy consumption cost of coking is 72.49 yuan / t, the energy consumption cost of residue oil hydrogenation is 36.93 yuan / t, and the energy consumption cost of No. 2 wax catalyst is 79.43 yuan / t. Therefore, the energy consumption cost of catalytic processing is 79.43 + 36.93 - 72.49 = 43.86 yuan / t.

[0045] Therefore, the profit per ton processed is 1183 - 43.86 = 1139.14 yuan.

[0046] The catalyst consumption is 0.69 kg per ton of catalytic processing, with a cost of 15,000 yuan per ton of catalyst. The total catalyst consumption increases by 0.29 kg / t compared to before blending. The total feed volume of the No. 2 wax catalyst from January to May was 1,122,816.08 tons. Therefore, the increased catalyst consumption and associated costs compared to before the modification are 0.29 kg / t. 1122816.08 15000 / 1000=4.8842 million yuan

[0047] The total amount of residual oil processed from January to May 2022 was 108,258 tons, resulting in a total benefit of approximately 108,258 tons. 1139.14 - 488.42 = 118.4 million yuan; the estimated annual profit is 284.1 million yuan.

[0048] Please note to all technical personnel: Although the present invention has been described according to the specific embodiments above, the inventive concept of the present invention is not limited to this invention. Any modifications that utilize the inventive concept will be included within the scope of protection of this patent.

[0049] The above description is merely a preferred embodiment of the present invention. The scope of protection of the present invention is not limited to the above embodiments. All technical solutions falling within the scope of the present invention's concept are within the scope of protection of the present invention. It should be noted that for those skilled in the art, any improvements and modifications made without departing from the principle of the present invention should also be considered within the scope of protection of the present invention.

Claims

1. A method for processing desulfurized residue oil in a slurry-bed wax oil catalytic cracking unit, characterized in that, Includes the following steps: (1) After hydrogenation, the slurry bed wax oil is mixed with the residue oil from the tank area and sent to the feed oil tank of this unit. The feed oil is pumped to the feed oil-circulating slurry heat exchanger and heated to 225°C. Then, it enters the riser reactor through the feed oil atomizing nozzle. (2) After the feedstock oil comes into contact with the high-temperature catalyst in the riser reactor, it is heated, vaporized and reacted. The reaction temperature in the riser reactor is 523℃, the reaction pressure is controlled at 220kPa-260kPa, and the regeneration pressure is controlled at 250kPa-290kPa. The oil and gas and catalyst after the reaction are quickly separated by the separation system at the riser outlet. The catalyst to be generated enters the stripping section set at the bottom. (3) The reaction oil and gas after rapid separation and the entrained catalyst fine powder are directly introduced into the single-stage cyclone separator of the settling tank. After further separation of the catalyst fine powder by the single-stage cyclone separator of the settling tank, the reaction oil and gas enter the lower part of the fractionation tower through the large oil and gas pipeline at the top of the settling tank. After separation by the separation system and the single-stage cyclone separator of the settling tank, the catalyst to be generated is in countercurrent contact with the stripping steam in the stripping section to replace the oil and gas carried by the catalyst. (4) The carbonized catalyst enters the stripping section, where it comes into countercurrent contact with steam to strip the oil and gas carried by the catalyst. The stripped catalyst flows down along the stripping inclined tube and enters the lower part of the coke burner of the regenerator through the stripping slide valve. It mixes with the high-temperature regenerated catalyst for coking. The catalyst with lower carbon content enters the two-dense phase through the large-hole distribution plate at the top of the coke burner. Under the conditions of 680~690℃, the coke and CO combustion process is finally completed. The regenerated catalyst enters the bottom of the riser reactor through the regeneration inclined tube and the regeneration slide valve. Under the rise of dry gas / steam, the catalyst is accelerated and rectified. Then it comes into contact with the atomized raw material, vaporizes and reacts. (5) The flue gas generated by the regeneration of the coke is separated from the catalyst by two-stage cyclone separators, then enters a three-stage cyclone for further separation of entrained catalyst, the purified flue gas enters a flue gas turbine to recover pressure energy and heat energy, then enters a waste heat boiler to recover heat energy, and the NOx in the flue gas is removed in a denitration section arranged in the waste heat boiler X After the removal of NOx, the flue gas is sent to a flue gas desulfurization unit, a double-pump alkali injection is used to ensure that the SO2 in the flue gas discharged is lower than 50mg / m 3 After the flue gas desulfurization reaches the standard, the flue gas is discharged into the atmosphere through a flue gas desulfurization chimney (6) The reaction oil and gas from the settling tank enters the lower part of the fractionation tower. The oil and gas at the top of the fractionation tower are cooled to 40°C through the oil and gas-demineralized water heat exchanger, the dry air cooler, and the condenser. Then, they enter the oil and gas separator at the top of the fractionation tower for gas-liquid-water three-phase separation. The separated crude gasoline is pressurized by the crude gasoline pump and then enters the absorption stabilization system to be separated into stabilized gasoline and liquefied petroleum gas, which are sent to the downstream product refining and SZorb unit. Light diesel oil is discharged from the fractionation tower 15. The stripped light diesel oil is drawn from the trays and flows by gravity to the light diesel stripping tower. After stripping, the light diesel oil is pumped out by the light diesel oil pump and heated to 120°C before being sent to the downstream diesel hydrocracking unit. The oil slurry is drawn out from the bottom of the fractionation tower by the circulating oil slurry pump. After passing through the feed oil-circulating oil slurry heat exchanger for heat exchange, the oil slurry steam generator generates high-pressure saturated steam. After the temperature drops to 280°C, the oil slurry is divided into three paths: one path returns to the upper part of the washing and deheating section of the fractionation tower via the oil slurry upper return tower; another path returns to the bottom of the fractionation tower via the oil slurry lower return tower; and the third path is pressurized by the product oil slurry pump, cooled to 90°C by the product oil slurry-hot water heat exchanger, and sent to the oil slurry tank in the tank farm as product oil slurry.

2. The method for processing desulfurized residue oil in a slurry bed wax oil catalytic cracking unit according to claim 1, characterized in that, The catalyst is an LC-6 cracking wax oil and heavy oil cracking catalyst, and the catalyst consumption is 0.8 kg / t-1.0 kg / t.

3. The method for processing desulfurized residue oil in a slurry bed wax oil catalytic cracking unit according to claim 1, characterized in that, The separation system is an SVQS fast separation system, and the outlet of the SVQS fast separation system is directly connected to the eight sets of single-stage vortex separators in the settling tank.

4. The method for processing desulfurized residue oil in a slurry bed wax oil catalytic cracking unit according to claim 1, characterized in that, In step (5), the main air required for the regenerator to burn off slag is provided by the main air fan. The main air enters the main air fan from the atmosphere, and after being pressurized, it enters the regenerator through the main air duct, auxiliary combustion chamber and main air distribution pipe. The oxygen content at the outlet of the regenerator flue gas is controlled at 6%.

5. The method for processing desulfurized residue oil in a slurry bed wax oil catalytic cracking unit according to claim 1, characterized in that, In step (5), CO combustion aid is added to ensure that the dilute phase temperature of the regenerator does not exceed 695℃.

6. The method for processing desulfurized residue oil in a slurry-bed wax oil catalytic cracking unit according to claim 1, characterized in that, In step (5), a denitrification combustion aid is added to reduce NO in the flue gas. x Less than 100mg / m 3 .

7. The method for processing desulfurized residue oil in a slurry bed wax oil catalytic cracking unit according to claim 1, characterized in that, In step (1), there is an interlocking system between the pipelines of slurry bed wax oil and residue oil that cuts off the feed when the interlocking shut-off valve is activated.

8. The method for processing desulfurized residue oil in a slurry bed wax oil catalytic cracking unit according to claim 1, characterized in that, In step (5), additional additives are added to the waste heat boiler to reduce SO3 and NO in the flue gas. X SNAR acid removal, denitrification, and reducing agent to ensure particulate matter meets standards.

9. A method for processing desulfurized residue oil in a slurry-bed wax oil catalytic cracking unit according to claim 1, characterized in that, In step (6), the temperature of the liquid phase at the bottom of the distillation tower is controlled to be ≤335℃.

10. A method for processing desulfurized residue oil in a slurry-bed wax oil catalytic cracking unit according to claim 1, characterized in that, In step (6), the amount of product oil slurry thrown out shall not be less than 4% of the feed rate of the device.

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