Reaction device for lightening treatment of residual oil and lightening treatment method of residual oil

Abstract

The invention provides a reaction device for conversion of residual oil to light weight and a method for conversion of residual oil to light weight, and relates to the technical field of heavy oil processing and utilization, the reaction device comprises a first reaction zone, a gas-solid separation zone, a first steam stripping section, a second reaction zone, a settlement zone and a second steam stripping section; an outlet of the first reaction zone is connected with the gas-solid separation zone through a gas-solid separation device, the first steam stripping section is located at the bottom of the gas-solid separation zone, an oil-gas outlet of the gas-solid separation zone is connected with the second reaction zone, an outlet of the second reaction zone is connected with the settling zone, the settling zone is provided with a separation device, and the second steam stripping section is located at the bottom of the settling zone. According to the method, the purpose that the raw materials are in contact reaction with the two catalysts respectively can be achieved, meanwhile, the two catalysts can be separated and regenerated, and the technical effects that the applicable raw materials are wide, inferior raw materials such as atmospheric pressure residual oil, vacuum residual oil, oil sand asphalt and hydrogenation tail oil can be effectively treated, and the target product yield is high are achieved.

Description

Technical Field

[0001] The present invention relates to the technical field of heavy oil processing and utilization, and in particular to a reaction device and a residual oil lightening treatment method for residual oil. Background Art

[0002] At present, the main method of treating residual oil light weight is delayed coking process, but the delayed coking process has high petroleum coke yield and low liquid yield, and the economic efficiency of the device is poor. The residual oil hydrogenation process and the traditional heavy oil catalytic cracking process have certain requirements for the residual carbon and metal content of heavy oil, and it is difficult to treat residual oil with high residual carbon, high heavy metal content, high colloid and asphaltene content.

[0003] Prior art CN113926390A discloses a catalytic conversion reactor, which consists of a first reaction zone, a second reaction zone, a gas-solid separation zone, and a stripping zone located below the second reaction zone and connected to the second reaction zone from bottom to top; the crude oil enters the first reaction zone for a low-severity reaction, and undergoes high-severity catalytic cracking in the second reaction zone to generate propylene, and the oil and gas after the reaction are separated into gas and solid.

[0004] Prior art CN109833834A discloses a petroleum hydrocarbon catalytic cracking reaction method and reactor, wherein the catalytic cracking of the crude oil is completed in a multi-stage reactor with upper and lower partitions; the reactor is provided with a first reaction section, a catalyst diverter, a catalyst replenishing and heat extraction section, a second reaction section and a settler from bottom to top; the second reaction section is provided with a second reaction zone; a first catalyst stripping section is provided around the first reaction zone of the first reaction section; the catalyst diverter is provided at the outlet of the first reaction zone and is located at the top of the catalyst stripping section of the first catalyst stripping section; a partition is provided between the first catalyst stripping zone and the catalyst heat extraction section of the catalyst replenishing and heat extraction section, and a first reaction zone logistics conveying pipe is provided on the partition; the outlet of the first reaction zone logistics conveying pipe is located at the inlet of the second reaction zone at the top of the catalyst heat extraction section or below the inlet; a catalyst heat extraction pipe is vertically provided in the catalyst heat extraction section around the first reaction zone logistics conveying pipe; a first reaction section catalyst inlet is provided in the first reaction section, and a second reaction zone catalyst inlet is provided in the catalyst replenishing and heat extraction section.

[0005] At present, the lightweight treatment of residual oil urgently needs to improve the adaptability of raw materials and increase the yield of target products.

[0006] In view of this, the present invention is proposed. Summary of the invention

[0007] One of the purposes of the present invention is to provide a reaction device for residual oil light treatment, so that the raw materials can be contacted and reacted with two catalysts respectively, and the two catalysts can be separated and regenerated, achieving the technical effect of not only wide applicability of raw materials but also high yield of target products.

[0008] The second object of the present invention is to provide a method for light-weighting residual oil, which is beneficial to improving the adaptability of raw materials and at the same time is beneficial to improving the yield of the target product.

[0009] In order to achieve the above-mentioned purpose of the present invention, the following technical solutions are particularly adopted:

[0010] In a first aspect, a reaction device for treating residual oil lightness comprises a first reaction zone, a gas-solid separation zone, a first stripping section, a second reaction zone, a settling zone and a second stripping section;

[0011] The outlet of the first reaction zone is connected to the gas-solid separation zone through a gas-solid separation device, so that the oil gas and the first catalyst coming out of the first reaction zone enter the gas-solid separation zone after separation;

[0012] The first stripping section is located at the bottom of the gas-solid separation zone and is used to strip the oil and gas in the first catalyst;

[0013] The oil and gas outlet of the gas-solid separation zone is connected to the second reaction zone, so that the oil and gas coming out of the gas-solid separation zone enter the second reaction zone to react with the second catalyst;

[0014] The outlet of the second reaction zone is connected to the settling zone, so that the oil gas from the second reaction zone and the second catalyst enter the settling zone for separation;

[0015] The settling zone is provided with a separation device for separating the oil gas from the second catalyst;

[0016] The second stripping section is located at the bottom of the settling zone and is used for stripping oil and gas in the second catalyst.

[0017] Furthermore, the height-to-diameter ratio of the first reaction zone is 5 to 20:1, preferably 5 to 10:1;

[0018] Preferably, the first reaction zone is located below the gas-solid separation zone;

[0019] Preferably, the outlet of the first reaction zone is located in the lower middle part of the gas-solid separation zone.

[0020] Furthermore, the gas-solid separation zone includes, from bottom to top, a first straight tube section, an expanded diameter section, a second straight tube section, and a reduced diameter section;

[0021] Preferably, the height-to-diameter ratio of the first straight tube section is 0.5 to 5:1, preferably 1 to 3:1;

[0022] Preferably, the expansion angle of the diameter expansion section is 1° to 30°, preferably 5° to 20°;

[0023] Preferably, the height of the expanded diameter section is 1m to 10m, preferably 2m to 5m;

[0024] Preferably, the height-to-diameter ratio of the second straight tube section is 0.5 to 2:1, preferably 0.5 to 1:1;

[0025] Preferably, the reduction angle of the reduced diameter section is 30° to 60°, preferably 30° to 45°.

[0026] Furthermore, the height-to-diameter ratio of the second reaction zone is 5 to 20:1, preferably 8 to 10:1;

[0027] Preferably, the bottom of the second reaction zone is connected to the oil and gas outlet at the top of the gas-solid separation zone.

[0028] Furthermore, the first stripping section is located in the annular space surrounded by the shell of the gas-solid separation zone and the outer wall of the first reaction zone.

[0029] Furthermore, the second stripping section is located in the annular space surrounded by the shell of the settling zone and the outer wall of the gas-solid separation zone and the second reaction zone.

[0030] Furthermore, the first stripping section and the second stripping section are each independently provided with a stripping component;

[0031] Preferably, the bottoms of the first stripping section and the second stripping section are independently provided with fluidizing gas distributors.

[0032] Furthermore, the second reaction zone is placed inside the sedimentation zone or placed in parallel outside the sedimentation zone.

[0033] In a second aspect, a method for treating residual oil lightness using the reaction device described in any one of the above items comprises the following steps:

[0034] The residual oil reacts with the first catalyst in the first reaction zone, the oil gas and the first catalyst from the first reaction zone are separated by the gas-solid separation device and then enter the gas-solid separation zone, and the separated first catalyst enters the first stripping section to strip the oil gas;

[0035] The oil and gas coming out of the gas-solid separation zone enter the second reaction zone to react with the second catalyst, the oil and gas coming out of the second reaction zone and the second catalyst enter the sedimentation zone for separation, the separated oil and gas are fractionated, and the separated second catalyst enters the second stripping section to strip the oil and gas.

[0036] Furthermore, the processing method further comprises the following steps:

[0037] Passing the first catalyst through the first stripping section into the first regenerator for regeneration;

[0038] Passing the second catalyst through the second stripping section into the second regenerator for regeneration;

[0039] Preferably, the first catalyst comprises a high hydrothermal stability base active center catalytic material;

[0040] Preferably, the second catalyst comprises a catalytic cracking acidic catalyst.

[0041] Compared with the prior art, the present invention has at least the following beneficial effects:

[0042] The reaction device for residual oil light-weight treatment provided by the present invention is capable of reacting raw materials in contact with two catalysts respectively, and the two catalysts can be separated and regenerated at the same time; on the one hand, the raw materials have strong adaptability and can realize light-weight treatment of heavy raw materials such as atmospheric residual oil, vacuum residual oil, oil sand asphalt and hydrogenation tail oil; on the other hand, the residual oil raw materials can react in contact with the two catalysts successively, and compared with the traditional catalytic cracking process, the coke yield of the product is lower and the light olefin yield is higher.

[0043] The method for lightening the residual oil provided by the present invention is beneficial to improving the adaptability of raw materials and at the same time is beneficial to improving the yield of the target product. BRIEF DESCRIPTION OF THE DRAWINGS

[0044] In order to more clearly illustrate the specific implementation methods of the present invention or the technical solutions in the prior art, the drawings required for use in the specific implementation methods or the description of the prior art will be briefly introduced below. Obviously, the drawings described below are some implementation methods of the present invention. For ordinary technicians in this field, other drawings can be obtained based on these drawings without paying creative work.

[0045] Figure 1 A schematic diagram of the structure of a reaction device provided in Example 1 of the present invention;

[0046] Figure 2 This is a schematic diagram of the structure of the reaction device provided in Example 2 of the present invention.

[0047] Icons: 1-first stage lifting steam inlet; 2-first catalyst inlet; 3-first reaction zone pre-lifting section; 4-raw material feed inlet; 5-first reaction zone; 6-first stripping steam inlet; 7-first stripping section; 8-water vapor inlet; 9-gas-solid separation zone; 10-second stripping steam inlet; 11-second stage lifting steam distributor; 12-second catalyst inlet; 13-recycled oil inlet; 14-second reaction zone; 15-sedimentation zone; 16-first stage cyclone separation; 17-second stage cyclone separation; 18-oil and gas outlet; 19-second stripping section; 20-second catalyst outlet; 21-first catalyst outlet. DETAILED DESCRIPTION

[0048] The technical solution of the present invention will be clearly and completely described below in conjunction with the embodiments. Obviously, the described embodiments are part of the embodiments of the present invention, rather than all of the embodiments. Based on the embodiments of the present invention, all other embodiments obtained by ordinary technicians in this field without creative work are within the scope of protection of the present invention.

[0049] According to a first aspect of the present invention, there is provided a reaction device for treating residual oil lightness, comprising a first reaction zone, a gas-solid separation zone, a first stripping section, a second reaction zone, a settling zone and a second stripping section;

[0050] The outlet of the first reaction zone is connected to the gas-solid separation zone through a gas-solid separation device, so that the oil gas and the first catalyst coming out of the first reaction zone enter the gas-solid separation zone after separation;

[0051] The first stripping section is located at the bottom of the gas-solid separation zone and is used to strip the oil and gas in the first catalyst;

[0052] The oil and gas outlet of the gas-solid separation zone is connected to the second reaction zone, so that the oil and gas coming out of the gas-solid separation zone enter the second reaction zone to react with the second catalyst;

[0053] The outlet of the second reaction zone is connected to the settling zone, so that the oil and gas from the second reaction zone and the second catalyst enter the settling zone for separation;

[0054] The settling zone is provided with a separation device for separating the oil gas from the second catalyst;

[0055] The second stripping section is located at the bottom of the settling zone and is used to strip the oil and gas in the second catalyst.

[0056] The reaction device for residual oil light-weight treatment provided by the present invention is capable of reacting raw materials in contact with two catalysts respectively, and the two catalysts can be separated and regenerated at the same time; on the one hand, the raw materials have strong adaptability and can realize light-weight treatment of heavy raw materials such as atmospheric residual oil, vacuum residual oil, oil sand asphalt and hydrogenation tail oil; on the other hand, the residual oil raw materials can react in contact with the two catalysts successively, and compared with the traditional catalytic cracking process, the coke yield of the product is lower and the low-carbon olefin yield is higher.

[0057] In a preferred embodiment, the aspect ratio of the first reaction zone can be 5 to 20:1, and typical but non-limiting aspect ratios are, for example, 5:1, 6:1, 7:1, 8:1, 9:1, 10:1, 12:1, 14:1, 16:1, 18:1, and 20:1, and may further preferably be 5 to 10:1.

[0058] The first reaction zone may be provided with a lifting gas inlet, a catalyst inlet and at least one raw material inlet, wherein the raw material inlet may be located above the catalyst inlet, and a pre-lifting section is provided between the raw material inlet and the catalyst inlet; at the same time, a gas-solid rapid separation device is provided at the outlet of the first reaction zone, and the gas-solid rapid separation device may be at least one of an umbrella cap type, a T-elbow and a distribution plate; and is used to quickly separate the oil and gas from the first catalyst.

[0059] In the present invention, the first reaction zone may be located below the gas-solid separation zone; and the outlet of the first reaction zone may be located in the lower middle portion of the gas-solid separation zone.

[0060] In the present invention, a two-stage lifting steam inlet may be provided at the top of the gas-solid separation zone for lifting the second catalyst.

[0061] In a preferred embodiment, the gas-solid separation zone includes, from bottom to top, but is not limited to, a first straight cylinder section, an expanded diameter section, a second straight cylinder section, and a reduced diameter section.

[0062] In a preferred embodiment, the height-to-diameter ratio of the first straight tube section may be 0.5-5:1, and typical but non-limiting height-to-diameter ratios are, for example, 0.5:1, 1:1, 2:1, 3:1, 4:1, 5:1, and may further preferably be 1-3:1.

[0063] In a preferred embodiment, the expansion angle of the expansion section can be 1° to 30°, and its typical but non-limiting expansion angles are, for example, 1°, 5°, 10°, 15°, 20°, 25°, and 30°, and it can be further preferably 5° to 20°; the height of the expansion section can be 1m to 10m, and its typical but non-limiting heights are, for example, 1m, 2m, 3m, 4m, 5m, 6m, 7m, 8m, 9m, and 10m, and it can be further preferably 2m to 5m.

[0064] In the present invention, the outlet of the first reaction zone may be located at the lower part of the expanded diameter section of the gas-solid separation zone.

[0065] In a preferred embodiment, the height-to-diameter ratio of the second straight tube section can be 0.5-2:1, and its typical but non-limiting height-to-diameter ratio is, for example, 0.5:1, 1:1, 1.5:1, and 2:1, and it can be further preferably 0.5-1:1; the reduction angle of the reduced diameter section can be 30°-60°, and its typical but non-limiting reduction angle is, for example, 30°, 35°, 40°, 45°, 50°, 55°, and 60°, and it can be further preferably 30°-45°.

[0066] In the present invention, the bottom of the second reaction zone is connected to the oil and gas outlet at the top of the gas-solid separation zone, the top of the reduced diameter section can be the inlet of the second reaction zone, and the inner diameter of the reduced diameter section can be the inner diameter of the second reaction zone; at the same time, a two-stage lifting steam inlet can be provided at the top of the reduced diameter section, a second catalyst inlet can be provided at the bottom of the second reaction zone, and a recycled oil inlet can be provided above the second catalyst inlet.

[0067] In a preferred embodiment, the height-to-diameter ratio of the second reaction zone can be 5-20:1, and typical but non-limiting height-to-diameter ratios are, for example, 5:1, 6:1, 7:1, 8:1, 9:1, 10:1, 12:1, 14:1, 16:1, 18:1, and 20:1, and may be further preferably 8-10:1.

[0068] It should be noted that the first reaction zone, the gas-solid separation zone and the second reaction zone can be coaxially arranged.

[0069] In a preferred embodiment, the first stripping section may be located in the annular space surrounded by the shell of the gas-solid separation zone and the outer wall of the first reaction zone.

[0070] In a preferred embodiment, the second stripping section may be located in the annular space surrounded by the shell of the settling zone and the outer wall of the gas-solid separation zone and the second reaction zone.

[0071] In the present invention, the first stripping section may be provided with a stripping steam inlet and a first catalyst outlet, and the second stripping section may be provided with a stripping steam inlet and a second catalyst outlet; at the same time, the interiors of the first stripping section and the second stripping section (in the stripping area) are independently provided with stripping components; the bottoms of the first stripping section and the second stripping section are independently provided with fluidizing gas distributors.

[0072] In the present invention, the sedimentation zone is provided with an oil gas and catalyst separation device for separating the oil gas from the second catalyst, and an oil gas outlet can be provided at the top of the sedimentation zone; in addition, the positional relationship between the sedimentation zone and the second reaction zone: the second reaction zone can be placed inside the sedimentation zone, and the second reaction zone can also be placed side by side outside the sedimentation zone.

[0073] According to a second aspect of the present invention, there is provided a method for treating residual oil lightness using any one of the above-mentioned reaction devices, comprising the following steps:

[0074] The residual oil reacts with the first catalyst in the first reaction zone, the oil gas and the first catalyst from the first reaction zone are separated by the gas-solid separation device and then enter the gas-solid separation zone, and the separated first catalyst enters the first stripping section to strip the oil gas;

[0075] The oil and gas coming out of the gas-solid separation zone enter the second reaction zone to react with the second catalyst, the oil and gas coming out of the second reaction zone and the second catalyst enter the sedimentation zone for separation, the separated oil and gas are fractionated, and the separated second catalyst enters the second stripping section to strip the oil and gas.

[0076] The method for lightening the residual oil provided by the present invention is beneficial to improving the adaptability of raw materials and at the same time is beneficial to improving the yield of the target product.

[0077] In a preferred embodiment, the method for treating residual oil to be light-weight further comprises the following steps:

[0078] Passing the first catalyst through the first stripping section into the first regenerator for regeneration;

[0079] The second catalyst passes through the second stripping section and enters the second regenerator for regeneration.

[0080] In the present invention, the first catalyst may be a catalytic material having a high hydrothermal stability and a base active center, but is not limited thereto; the second catalyst may be a catalytic cracking acidic catalyst, but is not limited thereto.

[0081] The present invention is further described below by way of examples. Unless otherwise specified, the materials in the examples are prepared according to existing methods or directly purchased from the market.

[0082] Example 1

[0083] A reaction device for treating residual oil light weight, see Figure 1 , including a first reaction zone 5, a gas-solid separation zone 9, a first stripping section 7, a second reaction zone 14, a settling zone 15 and a second stripping section 19;

[0084] The first reaction zone 5 is located below the gas-solid separation zone 9, and the outlet of the first reaction zone 5 is located at the lower part of the expanded diameter section of the gas-solid separation zone; at the same time, a gas-solid rapid separation device is provided at the outlet of the first reaction zone 5 to quickly separate the oil and gas from the first catalyst, so that the oil and gas and the first catalyst coming out of the first reaction zone 5 enter the gas-solid separation zone 9 after separation;

[0085] The first reaction zone 5 is provided with a lifting steam inlet 1, a first catalyst inlet 2 and a raw material feed inlet 4, the raw material feed inlet 4 is located above the first catalyst inlet 2, and the raw material feed inlet 4 and the first catalyst inlet 2 are between the pre-lifting section; wherein, the pipe diameter of the first reaction zone 5 is 1m, the height is 8m, and 4 raw material feed nozzles are symmetrically arranged around the circumference;

[0086] In this embodiment, the gas-solid separation zone 9 is composed of a first straight tube section, an expansion section, a second straight tube section and a reduction section from bottom to top; wherein the diameter of the first straight tube section is 3m and the height is 4m; the expansion angle of the expansion section is 15° and the height is 4m; the height of the second straight tube section is 6m; the reduction angle of the reduction section is 45°, the top of the reduction section is the entrance of the second reaction zone 14, and the inner diameter of the reduction section is the inner diameter of the second reaction zone 14; the diameter of the second reaction zone 14 is 1m and the height is 8m;

[0087] The top of the gas-solid separation zone 9 is provided with an oil and gas outlet and a two-stage lifting steam distributor 11, and the top of the reduced diameter section is provided with a two-stage lifting steam inlet, so as to lift the second catalyst; the bottom of the gas-solid separation zone 9 is provided with a first catalyst collecting zone, and the first stripping section 7 is located at the bottom of the gas-solid separation zone 9, and is used to strip the oil and gas in the first catalyst;

[0088] The first stripping section 7 is located in the annular space surrounded by the shell of the gas-solid separation zone 9 and the outer wall of the first reaction zone 5; the first stripping section 7 is provided with a first stripping steam inlet 6 and a first catalyst outlet 21, a stripping component is provided in the stripping zone of the first stripping section 7, a traditional disc ring baffle internal component is provided in the stripping zone, and a fluidizing gas distributor is provided at the bottom;

[0089] The oil and gas outlet at the top of the gas-solid separation zone 9 is connected to the second reaction zone 14, so that the oil and gas coming out of the gas-solid separation zone 9 enter the second reaction zone 14 and react with the second catalyst;

[0090] The first reaction zone 5, the gas-solid separation zone 9 and the second reaction zone 14 are coaxially arranged;

[0091] The second reaction zone 14 is provided with a second catalyst inlet 12 and a recycled oil inlet 13 at the bottom, and the recycled oil inlet 13 is provided above the second catalyst inlet 12; the outlet of the second reaction zone 14 is connected to the settling zone 15, so that the oil gas and the second catalyst coming out of the second reaction zone 14 enter the settling zone 15 for separation; the second reaction zone 14 is placed inside the settling zone 15, and an oil gas and second catalyst separation device is provided in the settling zone 15, and an oil gas outlet is provided at the top of the settling zone 15; the bottom of the settling zone 15 is provided with a second stripping section 19 for stripping the oil gas in the second catalyst;

[0092] The second stripping section 19 is located in the annular space surrounded by the shell of the sedimentation zone 15, the gas-solid separation zone 9 and the outer wall of the second reaction zone 14; the second stripping section 19 is provided with a second stripping steam inlet 10 and a second catalyst outlet 20, a stripping component is provided in the stripping zone of the second stripping section 19, a traditional disc ring baffle internal component is provided in the stripping zone, and a fluidizing gas distributor is provided at the bottom.

[0093] Example 2

[0094] This embodiment provides a reaction device for treating residual oil lightness. Figure 2 , which is different from Example 1 in that the second reaction zone 14 is placed outside the settling zone 15 in parallel;

[0095] The rest of the settings are the same as those in Example 1.

[0096] Comparative Example 1

[0097] This comparative example provides a conventional heavy oil catalytic cracking unit (a coaxial regeneration system), which is composed of a riser, a settler and a regenerator;

[0098] The raw materials enter the riser through the bottom of the pre-lifting section for reaction. After the reaction, the oil, gas and catalyst enter the sedimentation area for separation. The oil and gas enter the distillation tower through the large oil and gas pipeline. The catalyst is stripped by oil and gas in the stripping section and then enters the regenerator for regeneration. The length of the riser is 33m and the inner diameter of the riser is 0.8m.

[0099] Comparative Example 2

[0100] This comparative example provides a reaction device for treating residual oil lightness, which is different from Example 1 in that the first stripping section 7 is not provided at the bottom of the gas-solid separation zone 9;

[0101] The rest of the settings are the same as those in Example 1.

[0102] Compared with Example 1, the defect of this comparative example is that after the reaction, part of the oil and gas is carried out with the catalyst and enters the regenerator, which on the one hand will lead to a decrease in the product yield of the device; on the other hand, since the oil and gas enter the regenerator and come into contact with air, they are easily flammable, resulting in the risk of explosion of the device.

[0103] Comparative Example 3

[0104] This comparative example provides a reaction device for residual oil lightening treatment, which is different from Example 1 in that the second stripping section 19 is not provided at the bottom of the settling zone 15;

[0105] The rest of the settings are the same as those in Example 1.

[0106] Compared with Example 1, the defects of this comparative example are that, on the one hand, it will lead to a decrease in the product yield of the device, and on the other hand, since the oil and gas enter the regenerator and come into contact with the air, they are easily burned, resulting in the risk of explosion of the device.

[0107] Comparative Example 4

[0108] This comparative example provides a reaction device for residual oil lightening treatment, which is different from Example 1 in that no settling zone 15 is provided at the outlet of the second reaction zone 14;

[0109] The rest of the settings are the same as those in Example 1.

[0110] Compared with Example 1, the defect of this comparative example is that the oil and gas and the catalyst cannot be effectively separated after the reaction, and the catalyst may enter the distillation tower together with the oil and gas through the large oil and gas pipeline. The large oil and gas pipeline and the inside of the distillation tower are prone to coking, resulting in an increase in the solid content in the product.

[0111] Comparative Example 5

[0112] This comparative example provides a reaction device for residual oil lightening treatment, which is different from Example 1 in that no oil-gas and second catalyst separation device is provided in the settling zone 15;

[0113] The rest of the settings are the same as those in Example 1.

[0114] Compared with Example 1, the defect of this comparative example is that the catalyst may enter the distillation tower together with the oil and gas through the large oil and gas pipeline, and the large oil and gas pipeline and the inside of the distillation tower are prone to coking, resulting in an increase in the solid content in the product.

[0115] Test Example 1

[0116] The reaction device provided in Example 1 is used to carry out light-weight treatment of residual oil, and the method is as follows:

[0117] Residue oil of a certain refinery is used as a raw material (raw material properties are shown in Table 1) and reacts with catalyst a (first catalyst) in the first reaction zone 5. Oil gas and catalyst a at the outlet of the first reaction zone 5 enter the gas-solid separation zone 9 through a gas-solid rapid separation device. Catalyst a enters the first regenerator through the first stripping section 7 at the bottom of the gas-solid separation zone 9 for regeneration.

[0118] The oil and gas coming out from the top of the gas-solid separation zone 9 react with the catalyst b (second catalyst) in the second reaction zone 14, and then enter the settling zone 15 to separate the oil and gas from the catalyst b. The oil and gas are fractionated from the top of the settling zone 15 to the fractionation device, and the catalyst b enters the second regenerator through the second stripping section 19 at the bottom of the settling zone 15 for regeneration;

[0119] Wherein, catalyst a is a catalytic material with a high hydrothermal stability and an alkaline active center, and catalyst b is a conventional catalytic cracking acidic catalyst;

[0120] The reaction temperature of the first reaction zone 5 is 480°C, and the temperature of the gas-solid separation zone 9 is the same as that of the first reaction zone; the reaction temperature of the second reaction zone 14 is 520°C, and the temperature of the settling zone 15 is the same as that of the second reaction zone; the operating temperatures of the first regenerator and the second regenerator are both 700°C; the mass ratio of catalyst a to raw material feed in the first reaction zone 5 is 10:1; the mass ratio of catalyst b to raw material feed in the second reaction zone 14 is 7:1; the raw material inlet temperature is 240°C;

[0121] The test results are shown in Table 2.

[0122] Test Example 2

[0123] The reaction device provided in Example 2 was used to carry out the light-weight treatment of the residual oil, and the experimental raw materials and method conditions were referred to those in Experimental Example 1;

[0124] The test results are shown in Table 2.

[0125] Comparative test example 1

[0126] The reaction device provided in Comparative Example 1 was used to carry out the light-weight treatment of the residual oil, and the test raw materials were the same as those in Test Example 1;

[0127] The catalyst used is catalyst B, with a catalyst-oil ratio of 7:1; the riser reaction temperature is 520°C; the regeneration temperature is 700°C; the raw material inlet temperature is 240°C;

[0128] The test results are shown in Table 2.

[0129] Table 1 Properties of experimental raw materials

[0130]

[0131] Table 2 Distribution of test products

[0132] Product distribution, % Test Example 1 Test Example 2 Comparative test example 1 Dry gas 7.17 7.05 7.24 Liquefied gas 22.03 22.14 20.82 Gasoline (<180℃) 35.25 35.29 34.29 Diesel (180℃-350℃) 19.28 18.96 22.63 Oil slurry (>350℃) 9.62 9.58 6.43 Coke 6.65 6.98 8.59 Ethylene yield 1.68 1.65 1.52 Propylene yield 10.10 10.17 9.75 Butene yield 8.48 8.56 7.31

[0133] From the comparison of the test results of Test Example 1 and Test Example 2, it can be seen that the distribution of each fraction of the product is relatively close, indicating that the two structural reaction devices have similar effects on the reaction; compared with the comparative test example 1, the dry gas yield of Test Example 1 and Test Example 2 is slightly reduced, the coke yield is significantly reduced, the liquefied gas, gasoline and oil slurry yields are increased, and the diesel yield is reduced. It can be seen that the reaction device provided by the present invention can well realize the fluidization and separation of the two catalysts in the reactor. The inferior residual oil is first refined by catalyst a to produce more intermediate fractions, and then reacts with catalyst b for deep cracking, thereby improving the residual oil conversion rate; at the same time, the present invention is applicable to a wide range of raw materials, and can process inferior raw materials such as atmospheric residual oil, vacuum residual oil, oil sand asphalt and hydrogenation tail oil.

[0134] In summary, the present invention can well realize the fluidization and separation of two catalysts in the reaction device through two-stage lifting and two-stage stripping. It not only has strong adaptability to raw materials and can realize the lightweight treatment of heavy raw oils such as atmospheric residue oil, vacuum residue oil, oil sand asphalt and hydrogenation tail oil, but also the residue oil can be contacted and reacted with the two catalysts in succession. Compared with the traditional catalytic cracking process, the coke yield of the product is lower and the light olefin yield is higher.

[0135] Finally, it should be noted that the above embodiments are only used to illustrate the technical solutions of the present invention, rather than to limit it. Although the present invention has been described in detail with reference to the aforementioned embodiments, those skilled in the art should understand that they can still modify the technical solutions described in the aforementioned embodiments, or replace some or all of the technical features therein with equivalents. However, these modifications or replacements do not cause the essence of the corresponding technical solutions to deviate from the scope of the technical solutions of the embodiments of the present invention.

Claims

1. A reaction device for treating residual oil lightness, characterized in that: It includes a first reaction zone, a gas-solid separation zone, a first stripping section, a second reaction zone, a settling zone and a second stripping section; The outlet of the first reaction zone is connected to the gas-solid separation zone through a gas-solid separation device, so that the oil gas and the first catalyst coming out of the first reaction zone enter the gas-solid separation zone after separation; The first stripping section is located at the bottom of the gas-solid separation zone and is used to strip the oil and gas in the first catalyst; The oil and gas outlet of the gas-solid separation zone is connected to the second reaction zone, so that the oil and gas coming out of the gas-solid separation zone enter the second reaction zone to react with the second catalyst; The outlet of the second reaction zone is connected to the settling zone, so that the oil gas from the second reaction zone and the second catalyst enter the settling zone for separation; The settling zone is provided with a separation device for separating the oil gas from the second catalyst; The second stripping section is located at the bottom of the settling zone and is used for stripping oil and gas in the second catalyst.

2. The reaction device according to claim 1, characterized in that: The height-to-diameter ratio of the first reaction zone is 5 to 20:1, preferably 5 to 10:1; Preferably, the first reaction zone is located below the gas-solid separation zone; Preferably, the outlet of the first reaction zone is located in the lower middle part of the gas-solid separation zone.

3. The reaction device according to claim 2, characterized in that: The gas-solid separation zone includes, from bottom to top, a first straight tube section, an expanded diameter section, a second straight tube section, and a reduced diameter section; Preferably, the height-to-diameter ratio of the first straight tube section is 0.5 to 5:1, preferably 1 to 3:1; Preferably, the expansion angle of the diameter expansion section is 1° to 30°, preferably 5° to 20°; Preferably, the height of the expanded diameter section is 1m to 10m, preferably 2m to 5m; Preferably, the height-to-diameter ratio of the second straight tube section is 0.5 to 2:1, preferably 0.5 to 1:1; Preferably, the reduction angle of the reduced diameter section is 30° to 60°, preferably 30° to 45°.

4. The reaction device according to claim 1, characterized in that: The height-to-diameter ratio of the second reaction zone is 5 to 20:1, preferably 8 to 10:1; Preferably, the bottom of the second reaction zone is connected to the oil and gas outlet at the top of the gas-solid separation zone.

5. The reaction device according to claim 1, characterized in that: The first stripping section is located in the annular space surrounded by the shell of the gas-solid separation zone and the outer wall of the first reaction zone.

6. The reaction device according to claim 1, characterized in that: The second stripping section is located in the annular space surrounded by the shell of the settling zone, the gas-solid separation zone and the outer wall of the second reaction zone.

7. The reaction device according to claim 5 or 6, characterized in that: The first stripping section and the second stripping section are each independently provided with a stripping component; Preferably, the bottoms of the first stripping section and the second stripping section are independently provided with fluidizing gas distributors.

8. The reaction device according to claim 1, characterized in that: The second reaction zone is placed inside the settling zone or placed in parallel outside the settling zone.

9. A method for treating residual oil lightness using the reaction device according to any one of claims 1 to 8, characterized in that: The following steps are involved: The residual oil reacts with the first catalyst in the first reaction zone, the oil gas and the first catalyst from the first reaction zone are separated by the gas-solid separation device and then enter the gas-solid separation zone, and the separated first catalyst enters the first stripping section to strip the oil gas; The oil and gas coming out of the gas-solid separation zone enter the second reaction zone to react with the second catalyst, the oil and gas coming out of the second reaction zone and the second catalyst enter the sedimentation zone for separation, the separated oil and gas are fractionated, and the separated second catalyst enters the second stripping section to strip the oil and gas.

10. The method for treating residual oil to be light-weight according to claim 9, characterized in that: The processing method further comprises the following steps: Passing the first catalyst through the first stripping section into the first regenerator for regeneration; Passing the second catalyst through the second stripping section into the second regenerator for regeneration; Preferably, the first catalyst comprises a high hydrothermal stability base active center catalytic material; Preferably, the second catalyst comprises a catalytic cracking acidic catalyst.

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