Residual oil lightening treatment device and process

Abstract

The invention provides a residual oil lightening treatment device and process, and relates to the technical field of heavy oil processing, the residual oil lightening treatment device comprises a reactor, a first regenerator and a second regenerator; the reactor comprises a first reaction zone, a second reaction zone, a first separation zone and a second separation zone; the first outlet extends into the first separation area and is provided with a gas-solid separator; the bottom end of the second reaction zone is communicated with the top end of the first separation zone, the second outlet extends into the second separation zone and is provided with a separation assembly, and an outlet of the separation assembly is connected with the oil-gas outlet. The residual oil can react with the catalyst a firstly, so that the purpose of moderately cracking heavy oil to produce more middle fractions is achieved; and deep cracking is carried out through a catalyst b, so that the purpose of increasing the yield of light fractions and low-carbon olefins is achieved. The residual oil lightening treatment device is high in liquid product and low-carbon olefin yield, low in coke yield and high in raw material adaptability, and can realize lightening treatment of heavy raw oil such as vacuum residual oil, normal pressure residual oil, hydrogenated heavy oil and heavy deasphalted oil.

Description

Technical Field

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

[0002] Residue oil is the part of crude oil with the highest boiling point, largest relative molecular mass, highest viscosity, lowest hydrogen-to-carbon ratio, most heteroatom content and most complex chemical structure.

[0003] At present, the main method of treating residual oil light weight is to use delayed coking process, but the delayed coking process has high petroleum coke yield, low liquid yield and poor unit economics. In addition, the residual oil hydrogenation process and the traditional heavy oil catalytic cracking process have certain requirements on 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. Summary of the invention

[0004] The object of the present invention is to provide a residual oil light-weight processing device to solve the technical problem of high petroleum coke yield and low liquid yield in the residual oil light-weight processing process in the prior art.

[0005] The residual oil lightening treatment device provided by the present invention comprises a reactor;

[0006] The reactor comprises a first reaction zone, a second reaction zone, a first separation zone, and a second separation zone;

[0007] The first reaction zone is provided with a first catalyst inlet, a raw material inlet and a first outlet; the first outlet extends into the first separation zone, and the first outlet is provided with a gas-solid separator;

[0008] The bottom end of the second reaction zone is connected to the top end of the first separation zone, and the second reaction zone is provided with a second catalyst inlet and a second outlet; the second outlet extends into the second separation zone, and the second outlet is provided with a separation assembly;

[0009] An oil and gas outlet is provided on the top of the second separation zone, and the outlet of the separation component is connected to the oil and gas outlet.

[0010] Further, the separation assembly includes a primary cyclone separator and a secondary cyclone separator;

[0011] The second outlet, the first-stage cyclone separator, the second-stage cyclone separator and the oil and gas outlet are connected in sequence.

[0012] Furthermore, the residual oil lightening treatment device further comprises a first regenerator;

[0013] The bottom of the first separation zone is provided with a first stripping section, the first stripping section is provided with a first stripping steam inlet and a first catalyst outlet, and a first stripping component is provided in the first stripping section;

[0014] The first catalyst outlet is connected to the inlet of the first regenerator, and the outlet of the first regenerator is connected to the first catalyst inlet.

[0015] Furthermore, the residual oil lightening treatment device further comprises a second regenerator;

[0016] The bottom of the second separation zone is provided with a second stripping section, the second stripping section is provided with a second stripping steam inlet and a second catalyst outlet, and the second stripping section is provided with a second stripping component;

[0017] The second catalyst outlet is connected to the interior of the second regenerator, and the outlet of the second regenerator is connected to the second catalyst inlet.

[0018] Further, the second separation zone is arranged above the first separation zone, and the second reaction zone is arranged in the second separation zone.

[0019] Furthermore, the second separation zone is arranged in the second regenerator; and the second stripping steam inlet extends to the outside of the second regenerator.

[0020] Furthermore, the first reaction zone is also provided with a first lifting steam inlet, which is arranged below the first catalyst inlet, and the first catalyst inlet is arranged below the raw material inlet; a second lifting steam inlet is arranged at the top of the first separation zone, and the second reaction zone is also provided with a recycled oil inlet.

[0021] The present invention also aims to provide a residual oil light-weight treatment process, using the residual oil light-weight treatment device provided by the present invention to perform light-weight treatment on the residual oil;

[0022] The method comprises the following steps: residual oil reacts with catalyst a in a first reaction zone, oil gas and catalyst a at a first outlet are separated by a gas-solid separator, and the oil gas separated by the gas-solid separator enters a second reaction zone;

[0023] The oil and gas react with the catalyst b in the second reaction zone, and the oil and gas and the catalyst b at the second outlet are separated by the separation component, and the oil and gas separated by the separation component are discharged through the oil and gas outlet.

[0024] Further, the catalyst a separated from the gas-solid separator is passed through the first stripping section and enters the first regenerator for regeneration;

[0025] The catalyst b separated from the separation assembly enters the second regenerator through the second stripping section for regeneration.

[0026] Furthermore, catalyst a is a catalytic material with a high hydrothermal stability and a base active center, and catalyst b is a catalytic cracking acidic catalyst.

[0027] The residual oil light-weight processing device provided by the present invention comprises a reactor; the reactor comprises a first reaction zone, a second reaction zone, a first separation zone and a second separation zone; the first reaction zone is provided with a first catalyst inlet, a raw material inlet and a first outlet; the first outlet extends into the first separation zone, and the first outlet is provided with a gas-solid separator; the bottom end of the second reaction zone is connected with the top end of the first separation zone, and the second reaction zone is provided with a second catalyst inlet and a second outlet; the second outlet extends into the second separation zone, and the second outlet is provided with a separation assembly; the top of the second separation zone is provided with an oil and gas outlet, and the outlet of the separation assembly is connected with the oil and gas outlet. The residual oil can first react with catalyst a to achieve the purpose of mild cracking of heavy oil to produce more middle distillates; and then deep cracking with catalyst b to achieve the purpose of producing more light distillates and light olefins. The residual oil light-weight processing device has high yields of liquid products and light olefins, low coke yield, strong raw material adaptability, and can achieve light-weight processing of heavy raw material oils such as vacuum residual oil, atmospheric residual oil, hydrogenated heavy oil, and heavy deasphalted oil. BRIEF DESCRIPTION OF THE DRAWINGS

[0028] 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.

[0029] Figure 1 : is a structural schematic diagram of a residual oil lightening treatment device provided in an embodiment of the present invention (the second separation zone is arranged above the first separation zone);

[0030] Figure 2 It is a structural schematic diagram of a residual oil lightening treatment device provided in an embodiment of the present invention (the second separation zone is arranged in the second regenerator).

[0031] Icons: 1-first lifting steam inlet; 2-first catalyst inlet; 3-pre-lifting section; 4-feedstock inlet; 5-first reaction zone; 6-first stripping steam inlet; 7-first stripping section; 8-water vapor inlet; 9-first separation zone; 10-second stripping steam inlet; 11-second lifting steam inlet; 12-second catalyst inlet; 13-recycled oil inlet; 14-second reaction zone; 15-second separation zone; 16-first cyclone separator; 17-second cyclone separator; 18-oil and gas outlet; 19-second stripping section; 20-second catalyst outlet; 21-first catalyst outlet; 22-first regenerator inlet; 23-first regenerator outlet; 24-second regenerator inlet; 25-second regenerator outlet; 26-first regenerator; 27-second regenerator. DETAILED DESCRIPTION

[0032] The technical solution of the present invention will be described clearly and completely below in conjunction with the accompanying drawings. Obviously, the described embodiment is a differentiated embodiment of the present invention, rather than a full embodiment. 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.

[0033] The present invention provides a residual oil light-weight processing device and process. A plurality of embodiments are given below to describe in detail the residual oil light-weight processing device and process provided by the present invention.

[0034] The residual oil lightening treatment device provided in this embodiment is as follows: Figure 1 to Figure 2 As shown, it includes a reactor; the reactor includes a first reaction zone 5, a second reaction zone 14, a first separation zone 9 and a second separation zone 15; the first reaction zone 5 is provided with a first catalyst inlet 2, a raw material inlet 4 and a first outlet; the first outlet extends into the first separation zone 9, and the first outlet is provided with a gas-solid separator; the bottom end of the second reaction zone 14 is connected with the top end of the first separation zone 9, and the second reaction zone 14 is provided with a second catalyst inlet 12 and a second outlet; the second outlet extends into the second separation zone 15, and the second outlet is provided with a separation component; the top of the second separation zone 15 is provided with an oil and gas outlet 18, and the outlet of the separation component is connected to the oil and gas outlet 18.

[0035] Catalyst a enters the first reaction zone 5 from the first catalyst inlet 2, and the residual oil enters the first reaction zone 5 from the raw material inlet 4. The residual oil reacts with the catalyst a in the first reaction zone 5. The oil and gas and catalyst a after the reaction in the first reaction zone 5 flow to the gas-solid separator through the first outlet. The oil and gas and catalyst a at the first outlet are separated by the gas-solid separator. The gas-solid separator can separate the oil and gas and catalyst a. The catalyst a falls to the bottom of the first separation zone 9. The oil and gas separated by the gas-solid separator enter the second reaction zone 14. Catalyst b enters the second reaction zone 14 from the second catalyst inlet 12. The oil and gas react with the catalyst b in the second reaction zone 14. The oil and gas and catalyst b after the reaction in the second reaction zone 14 flow to the separation component through the second outlet. The oil and gas and catalyst b at the second outlet are separated by the separation component. The separation component can separate the oil and gas and catalyst b. The catalyst b falls to the bottom of the second separation zone 15. The oil and gas separated by the separation component is discharged from the second separation zone 15 through the oil and gas outlet 18 and flows to the fractionation device for fractionation.

[0036] The residual oil light-weight processing device provided in this embodiment can make the residual oil react with catalyst a first to achieve the purpose of mild cracking of heavy oil to produce more middle distillates; and then deep cracking with catalyst b to achieve the purpose of producing more light distillates and light olefins. The residual oil light-weight processing device has high yields of liquid products and light olefins, low coke yield, strong raw material adaptability, and can achieve light-weight processing of heavy raw material oils such as vacuum residual oil, atmospheric residual oil, hydrogenated heavy oil, and heavy deasphalted oil.

[0037] The gas-solid separator can separate the oil gas and the catalyst a, and the separation component can separate the oil gas and the catalyst b, thereby achieving effective separation of the catalyst a and the catalyst b.

[0038] Furthermore, the separation assembly includes a primary cyclone separator 16 and a secondary cyclone separator 17; the second outlet, the primary cyclone separator 16, the secondary cyclone separator 17 and the oil and gas outlet 18 are connected in sequence.

[0039] The oil and gas and catalyst b at the second outlet are separated by the first-level cyclone separator 16, which can separate the oil and gas and the catalyst b. The catalyst b separated by the first-level cyclone separator 16 falls into the bottom of the second separation zone 15. The oil and gas separated by the first-level cyclone separator 16 enter the second-level cyclone separator 17 for separation. The second-level cyclone separator 17 can separate the oil and gas and the catalyst b. The catalyst b separated by the second-level cyclone separator 17 falls into the bottom of the second separation zone 15. The oil and gas separated by the second-level cyclone separator 17 is discharged from the second separation zone 15 through the oil and gas outlet 18 and flows to the fractionation device for fractionation.

[0040] The oil gas and the catalyst b are separated by the primary cyclone separator 16 and the secondary cyclone separator 17, and the separation effect is good.

[0041] In other optional embodiments, the separation assembly may include one cyclone separator, or three cyclone separators, or any other suitable form.

[0042] Furthermore, the residual oil light-weight processing device also includes a first regenerator 26; the bottom of the first separation zone 9 is provided with a first stripping section 7, the first stripping section 7 is provided with a first stripping steam inlet 6 and a first catalyst outlet 21, and a first stripping component is provided in the first stripping section 7; the first catalyst outlet 21 is connected to the inlet 22 of the first regenerator, and the outlet 23 of the first regenerator is connected to the first catalyst inlet 2.

[0043] The catalyst a separated by the gas-solid separator falls into the first stripping section 7 at the bottom of the first separation zone 9. The catalyst a passes through the first stripping section 7 via the first catalyst outlet 21 and the first regenerator inlet 22 to enter the first regenerator 26 for regeneration.

[0044] The catalyst a regenerated by the first regenerator 26 can enter the first reaction zone 5 through the outlet 23 of the first regenerator and the first catalyst inlet 2 for reaction in the first reaction zone 5 .

[0045] Catalyst a first reacts with the residual oil and then can be cyclically regenerated through the first regenerator 26 .

[0046] Furthermore, the residual oil light-weight processing device also includes a second regenerator 27; the bottom of the second separation zone 15 is provided with a second stripping section 19, the second stripping section 19 is provided with a second stripping steam inlet 10 and a second catalyst outlet 20, and a second stripping component is provided in the second stripping section 19; the second catalyst outlet 20 is connected to the inside of the second regenerator 27, and the outlet 25 of the second regenerator is connected to the second catalyst inlet 12.

[0047] The catalyst b separated by the separation assembly falls into the second stripping section 19 at the bottom of the second separation zone 15. The catalyst b passes through the second stripping section 19 and enters the first regenerator 26 via the second catalyst outlet 20 for regeneration.

[0048] The catalyst b regenerated by the first regenerator 26 can enter the second reaction zone 14 through the outlet 25 of the second regenerator and the second catalyst inlet 12 for reaction in the second reaction zone 14 .

[0049] The catalyst b first reacts with the oil and gas, and then can be cyclically regenerated through the second regenerator 27.

[0050] In an alternative embodiment, Figure 1 As shown, the second separation zone 15 is arranged above the first separation zone 9 , and the second reaction zone 14 is arranged in the second separation zone 15 .

[0051] Specifically, the second separation zone 15 is fixedly arranged above the first separation zone 9, the second reaction zone 14 is arranged inside the second separation zone 15, the second catalyst outlet 20 is connected to the inlet 24 of the second regenerator, and the catalyst b enters the first regenerator 26 through the second stripping section 19 via the second catalyst outlet 20 and the inlet 24 of the second regenerator for regeneration. The second separation zone 15 is arranged above the first separation zone 9, so that the reactor, the first regenerator 26 and the second regenerator 27 are easily arranged.

[0052] In another alternative embodiment, Figure 2 As shown, the second separation zone 15 is disposed in the second regenerator 27 ; the second stripping steam inlet 10 extends to the outside of the second regenerator 27 .

[0053] Specifically, the second separation zone 15 is arranged in the second regenerator 27, the second stripping steam inlet 10 extends to the outside of the second regenerator 27, the second catalyst outlet 20 is arranged in the second regenerator 27, the catalyst b passes through the second stripping section 19 and the second catalyst outlet 20 and directly falls into the second regenerator 27 for regeneration, and an oil and gas outlet 18 is provided at the top of the second separation zone 15. The oil and gas outlet 18 is not blocked by the second regenerator 27, and the oil and gas outlet 18 is connected to the outside of the second regenerator 27.

[0054] The second separation zone 15 is disposed in the second regenerator 27, which can save space.

[0055] Furthermore, the first reaction zone 5 is also provided with a first lifting steam inlet 1, which is arranged below the first catalyst inlet 2, and the first catalyst inlet 2 is arranged below the raw material inlet 4; a second lifting steam inlet 11 is provided at the top of the first separation zone 9, and the second reaction zone 14 is also provided with a recycled oil inlet 13.

[0056] Specifically, the raw material inlet 4 is arranged above the first catalyst inlet 2, and the pre-lifting section 3 is between the raw material inlet 4 and the first catalyst inlet 2. The lifting steam enters the first reaction zone 5 from the first lifting steam inlet 1, the catalyst a enters the first reaction zone 5 from the first catalyst inlet 2, and the residual oil enters the first reaction zone 5 from the raw material inlet 4. The first outlet is arranged at the top of the first reaction zone 5, and the raw material inlet 4, the first catalyst inlet 2 and the first lifting steam inlet 1 are all arranged at the bottom of the first reaction zone 5.

[0057] A water vapor inlet 8 is also provided in the middle of the first separation zone 9 .

[0058] A second lifting steam inlet 11 is provided at the top of the first separation zone 9, and the lifting steam enters the second reaction zone 14 through the second lifting steam inlet 11 to lift the catalyst b. The recycle oil inlet 13 is arranged above the second catalyst inlet 12. The recycle oil inlet 13 and the second catalyst inlet 12 are both arranged at the bottom of the second reaction zone 14, and the second outlet is arranged at the top of the first reaction zone 5.

[0059] The residual oil light-weight treatment process provided in this embodiment uses the residual oil light-weight treatment device provided in this embodiment to perform light-weight treatment on the residual oil;

[0060] The method comprises the following steps: the residual oil reacts with the catalyst a in the first reaction zone 5, the oil gas and the catalyst a at the first outlet are separated by a gas-solid separator, and the oil gas separated by the gas-solid separator enters the second reaction zone 14;

[0061] The oil and gas react with the catalyst b in the second reaction zone 14 , and the oil and gas and the catalyst b at the second outlet are separated by a separation component, and the oil and gas separated by the separation component are discharged through the oil and gas outlet 18 .

[0062] Specifically, catalyst a enters the first reaction zone 5 from the first catalyst inlet 2, and residual oil enters the first reaction zone 5 from the raw material inlet 4. The residual oil reacts with catalyst a in the first reaction zone 5. The oil and gas and catalyst a after the reaction in the first reaction zone 5 flow to the gas-solid separator through the first outlet. The oil and gas and catalyst a at the first outlet are separated by the gas-solid separator. The gas-solid separator can separate the oil and gas and catalyst a. Catalyst a falls to the bottom of the first separation zone 9. The oil and gas separated by the gas-solid separator enter the second reaction zone 14. Catalyst b enters the second reaction zone 14 from the second catalyst inlet 12. The oil and gas react with catalyst b in the second reaction zone 14. The oil and gas and catalyst b after the reaction in the second reaction zone 14 flow to the separation component through the second outlet. The oil and gas and catalyst b at the second outlet are separated by the separation component. The separation component can separate the oil and gas and catalyst b. Catalyst b falls to the bottom of the second separation zone 15. The oil and gas separated by the separation component is discharged from the second separation zone 15 through the oil and gas outlet 18 and flows to the fractionation device for fractionation.

[0063] The residual oil light-weight processing process provided in this embodiment can make the residual oil react with catalyst a first to achieve the purpose of mild cracking of heavy oil to produce more middle distillates; and then deep cracking with catalyst b to achieve the purpose of producing more light distillates and light olefins. The residual oil light-weight processing process has high yields of liquid products and light olefins, low coke yield, strong raw material adaptability, and can achieve light-weight processing of heavy raw material oils such as vacuum residual oil, atmospheric residual oil, hydrogenated heavy oil, and heavy deasphalted oil.

[0064] Further, the catalyst a separated by the gas-solid separator enters the first regenerator 26 through the first stripping section 7 for regeneration;

[0065] The catalyst b separated from the separation assembly enters the second regenerator 27 through the second stripping section 19 for regeneration.

[0066] The catalyst a separated by the gas-solid separator falls into the first stripping section 7 at the bottom of the first separation zone 9. The catalyst a passes through the first stripping section 7 via the first catalyst outlet 21 and the first regenerator inlet 22 to enter the first regenerator 26 for regeneration.

[0067] The catalyst a regenerated by the first regenerator 26 can enter the first reaction zone 5 through the outlet 23 of the first regenerator and the first catalyst inlet 2 for reaction in the first reaction zone 5. The catalyst a first reacts with the residual oil and then can be cyclically regenerated by the first regenerator 26.

[0068] The catalyst b separated by the separation assembly falls into the second stripping section 19 at the bottom of the second separation zone 15. The catalyst b passes through the second stripping section 19 and enters the first regenerator 26 via the second catalyst outlet 20 for regeneration.

[0069] The catalyst b regenerated by the first regenerator 26 can enter the second reaction zone 14 through the outlet 25 of the second regenerator and the second catalyst inlet 12 for reaction in the second reaction zone 14. The catalyst b first reacts with the oil and gas, and then can be cyclically regenerated by the second regenerator 27.

[0070] Furthermore, 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.

[0071] Example 1

[0072] Example 1 uses Figure 1 In the residue lightening treatment device shown, the second separation zone 15 is arranged above the first separation zone 9 , and the second reaction zone 14 is arranged in the second separation zone 15 .

[0073] Among them, the first reaction zone 5 is in a circular tubular shape, the inner diameter of the first reaction zone 5 is 1m, and the height is 8m. The first reaction zone 5 is provided with 4 raw material inlets 4, and the 4 raw material inlets 4 are all provided with feed nozzles. The 4 raw material inlets 4 are symmetrically arranged along the circumference of the first reaction zone 5.

[0074] The first separation zone 9 is composed of the first straight cylinder section, the diameter expansion section, the second straight cylinder section and the diameter reduction section from bottom to top. The first straight cylinder section is cylindrical, the inner diameter of the first straight cylinder section is 3m, and the height of the first straight cylinder section is 4m; the expansion angle of the diameter expansion section is 15°, and the height of the diameter expansion section is 4m; the second straight cylinder section is cylindrical, and the height of the second straight cylinder section is 6m; the diameter reduction angle of the diameter reduction section is 45°.

[0075] The second reaction zone 14 is in the shape of a circular tube, with an inner diameter of 1 m and a height of 8 m. The gas-solid separator can be an umbrella-shaped device, and a conventional disk ring baffle internal component (first stripping component) is provided in the first stripping section 7 .

[0076] The raw material is vacuum residue oil from a certain refinery, and the properties of the vacuum residue oil are shown in Table 1. The reaction temperature of the first reaction zone 5 is 480°C, and the temperature of the first separation zone 9 is the same as the reaction temperature of the first reaction zone 5; the reaction temperature of the second reaction zone 14 is 520°C, and the temperature of the second separation zone 15 is the same as the reaction temperature of the second reaction zone 14; the operating temperatures of the first regenerator 26 and the second regenerator are both 700°C; the mass ratio of the catalyst a to the feed of the first reaction zone 5 (vacuum residue oil) is 10:1; the mass ratio of the catalyst b to the feed of the second reaction zone 14 (oil and gas separated by the gas-solid separator) is 7:1, and the temperature of the feed (oil and gas separated by the gas-solid separator) entering the second reaction zone 14 is 240°C.

[0077] Example 2

[0078] Example 2 uses the same residual oil lightening treatment device as Example 1.

[0079] The raw material is vacuum residue oil from a certain refinery, and the properties of the vacuum residue oil are shown in Table 1. The reaction temperature of the first reaction zone 5 is 500°C, and the temperature of the first separation zone 9 is the same as the reaction temperature of the first reaction zone 5; the reaction temperature of the second reaction zone 14 is 550°C, and the temperature of the second separation zone 15 is the same as the reaction temperature of the second reaction zone 14; the operating temperatures of the first regenerator 26 and the second regenerator are both 700°C; the mass ratio of the catalyst a to the feed of the first reaction zone 5 and the feed of the raw material (vacuum residue oil) is 10:1; the mass ratio of the catalyst b to the feed of the second reaction zone 14 and the feed of the raw material (oil and gas separated by the gas-solid separator) is 7:1, and the temperature of the feed (oil and gas separated by the gas-solid separator) entering the second reaction zone 14 is 240°C.

[0080] Example 3

[0081] Example 3 uses the same residual oil lightening treatment device as Example 1.

[0082] The raw material is vacuum residue oil from a certain refinery, and the properties of the vacuum residue oil are shown in Table 1. The reaction temperature of the first reaction zone 5 is 500°C, and the temperature of the first separation zone 9 is the same as the reaction temperature of the first reaction zone 5; the reaction temperature of the second reaction zone 14 is 550°C, and the temperature of the second separation zone 15 is the same as the reaction temperature of the second reaction zone 14; the operating temperatures of the first regenerator 26 and the second regenerator are both 700°C; the mass ratio of the catalyst a to the feed of the first reaction zone 5 (vacuum residue oil) is 15:1; the mass ratio of the catalyst b to the feed of the second reaction zone 14 (oil and gas separated by the gas-solid separator) is 7:1, and the temperature of the feed (oil and gas separated by the gas-solid separator) entering the second reaction zone 14 is 240°C.

[0083] Example 4

[0084] Example 4 uses the same residual oil lightening treatment device as Example 1.

[0085] The raw material is vacuum residue oil from a certain refinery, and the properties of the vacuum residue oil are shown in Table 1. The reaction temperature of the first reaction zone 5 is 500°C, and the temperature of the first separation zone 9 is the same as the reaction temperature of the first reaction zone 5; the reaction temperature of the second reaction zone 14 is 550°C, and the temperature of the second separation zone 15 is the same as the reaction temperature of the second reaction zone 14; the operating temperatures of the first regenerator 26 and the second regenerator are both 700°C; the mass ratio of the catalyst a to the feed of the first reaction zone 5 and the feed of the raw material (vacuum residue oil) is 10:1; the mass ratio of the catalyst b to the feed of the second reaction zone 14 and the feed of the raw material (oil and gas separated by the gas-solid separator) is 12:1, and the temperature of the feed (oil and gas separated by the gas-solid separator) entering the second reaction zone 14 is 240°C.

[0086] Example 5

[0087] Example 1 uses Figure 2 In the residue lightening treatment device shown, the second separation zone 15 is arranged in the second regenerator 27 ; the second stripping steam inlet 10 extends to the outside of the second regenerator 27 .

[0088] Among them, the first reaction zone 5 is in a circular tubular shape, the inner diameter of the first reaction zone 5 is 1m, and the height is 8m. The first reaction zone 5 is provided with 4 raw material inlets 4, and the 4 raw material inlets 4 are all provided with feed nozzles. The 4 raw material inlets 4 are symmetrically arranged along the circumference of the first reaction zone 5.

[0089] The first separation zone 9 is composed of the first straight cylinder section, the diameter expansion section, the second straight cylinder section and the diameter reduction section from bottom to top. The first straight cylinder section is cylindrical, the inner diameter of the first straight cylinder section is 3m, and the height of the first straight cylinder section is 4m; the expansion angle of the diameter expansion section is 15°, and the height of the diameter expansion section is 4m; the second straight cylinder section is cylindrical, and the height of the second straight cylinder section is 6m; the diameter reduction angle of the diameter reduction section is 45°.

[0090] The second reaction zone 14 is in the shape of a circular tube, with an inner diameter of 1 m and a height of 8 m. The gas-solid separator can be an umbrella-shaped device, and a conventional disk ring baffle internal component (first stripping component) is provided in the first stripping section 7 .

[0091] The raw material is vacuum residue oil from a certain refinery, and the properties of the vacuum residue oil are shown in Table 1. The reaction temperature of the first reaction zone 5 is 480°C, and the temperature of the first separation zone 9 is the same as the reaction temperature of the first reaction zone 5; the reaction temperature of the second reaction zone 14 is 520°C, and the temperature of the second separation zone 15 is the same as the reaction temperature of the second reaction zone 14; the operating temperatures of the first regenerator 26 and the second regenerator are both 700°C; the mass ratio of the catalyst a to the feed of the first reaction zone 5 (vacuum residue oil) is 10:1; the mass ratio of the catalyst b to the feed of the second reaction zone 14 (oil and gas separated by the gas-solid separator) is 7:1, and the temperature of the feed (oil and gas separated by the gas-solid separator) entering the second reaction zone 14 is 240°C.

[0092] Example 6

[0093] Example 6 adopts the same residual oil lightening treatment device as Example 1.

[0094] The raw material is atmospheric residue oil from a refinery, and the properties of vacuum residue oil are shown in Table 1. The reaction temperature of the first reaction zone 5 is 480°C, and the temperature of the first separation zone 9 is the same as the reaction temperature of the first reaction zone 5; the reaction temperature of the second reaction zone 14 is 520°C, and the temperature of the second separation zone 15 is the same as the reaction temperature of the second reaction zone 14; the operating temperatures of the first regenerator 26 and the second regenerator are both 700°C; the mass ratio of the catalyst a to the feed of the first reaction zone 5 (vacuum residue oil) is 10:1; the mass ratio of the catalyst b to the feed of the second reaction zone 14 (oil and gas separated by the gas-solid separator) is 7:1, and the temperature of the feed (oil and gas separated by the gas-solid separator) entering the second reaction zone 14 is 240°C.

[0095] Comparative Example

[0096] The experimental device adopts a conventional heavy oil catalytic cracking device, which is a coaxial reverse regeneration system. The experimental raw materials are the same as those in Example 6. The catalyst adopts the catalyst b in Example 1-5, the catalyst-oil ratio is 7:1, the riser reaction temperature is 520°C, the regeneration temperature is 700°C, and the raw material inlet temperature is 240°C.

[0097] In Example 2, compared with Example 1, the temperatures of the first reaction zone 5 and the second reaction zone 14 are increased, the yields of dry gas and coke are increased, the yields of liquefied gas, gasoline and diesel are increased, and the yield of oil slurry is reduced; in Example 3, compared with Example 2, the agent-oil ratio of the first reaction zone 5 is increased, the yields of dry gas and coke are reduced, the yields of liquefied gas, gasoline and diesel are increased, and the yield of oil slurry is reduced; in Example 4, compared with Example 2, the agent-oil ratio of the second reaction zone 14 is increased, the yields of dry gas and coke are slightly reduced, the yields of liquefied gas, gasoline and diesel are increased, and the yield of oil slurry is significantly reduced; in Example 5, compared with Example 1, from the reaction results, the two forms of residual oil lightening treatment devices have little effect on the product distribution; in Example 6, compared with the comparative example, catalyst a is used to react with the residual oil first, the yield of dry gas is slightly reduced, the yield of coke is significantly reduced, the yields of liquefied gas, gasoline and oil slurry are increased, and the yield of diesel is reduced.

[0098] Table 1 shows the properties of experimental raw materials.

[0099] Table 1

[0100]

[0101] Table 2 shows the product distribution of Examples 1-6 and the comparative example.

[0102] Table 2

[0103] Product distribution, % Example 1 Example 2 Example 3 Example 4 Example 5 Example 6 Comparative Example Dry gas 11.43 12.59 11.92 12.24 11.37 7.17 7.24 Liquefied gas 17.71 18.81 19.05 19.29 17.76 22.03 20.82 Gasoline (<180℃) 23.16 24.59 25.87 26.03 23.54 35.25 34.29 Diesel (180℃-350℃) 18.94 20.1 22.13 21.71 18.69 19.28 22.63 Oil slurry (>350℃) 16.7 10.44 8.18 7.56 16.43 9.62 6.43 Coke 12.06 13.47 12.85 13.17 12.21 6.65 8.59 Ethylene yield 2.86 3.15 2.98 3.01 2.83 1.68 1.52 Propylene yield 8.12 8.62 8.73 8.84 8.14 10.10 9.75 Butene yield 6.82 7.24 7.34 7.43 6.83 8.48 7.31

[0104] 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 make equivalent replacements for the distinguishing or overall technical features therein. However, these modifications or replacements do not make the essence of the corresponding technical solutions deviate from the scope of the technical solutions of the embodiments of the present invention.

Claims

1. A residual oil lightening treatment device, characterized in that: including a reactor; The reactor comprises a first reaction zone (5), a second reaction zone (14), a first separation zone (9) and a second separation zone (15); The first reaction zone (5) is provided with a first catalyst inlet (2), a raw material inlet (4) and a first outlet; the first outlet extends into the first separation zone (9), and the first outlet is provided with a gas-solid separator; The bottom end of the second reaction zone (14) is connected to the top end of the first separation zone (9), and the second reaction zone (14) is provided with a second catalyst inlet (12) and a second outlet; the second outlet extends into the second separation zone (15), and the second outlet is provided with a separation assembly; An oil and gas outlet (18) is provided at the top of the second separation zone (15), and the outlet of the separation component is connected to the oil and gas outlet (18).

2. The residual oil lightening treatment device according to claim 1, characterized in that: The separation assembly comprises a primary cyclone separator (16) and a secondary cyclone separator (17); The second outlet, the first-stage cyclone separator (16), the second-stage cyclone separator (17) and the oil and gas outlet (18) are connected in sequence.

3. The residual oil lightening treatment device according to claim 1, characterized in that: The residual oil lightening treatment device further comprises a first regenerator (26); The bottom of the first separation zone (9) is provided with a first stripping section (7), the first stripping section (7) is provided with a first stripping steam inlet (6) and a first catalyst outlet (21), and a first stripping component is provided in the first stripping section (7); The first catalyst outlet (21) is connected to the first regenerator inlet (22), and the first regenerator outlet (23) is connected to the first catalyst inlet (2).

4. The residual oil lightening treatment device according to any one of claims 1 to 3, characterized in that: The residual oil lightening treatment device further comprises a second regenerator (27); The bottom of the second separation zone (15) is provided with a second stripping section (19), the second stripping section (19) is provided with a second stripping steam inlet (10) and a second catalyst outlet (20), and a second stripping component is provided in the second stripping section (19); The second catalyst outlet (20) is connected to the interior of the second regenerator (27), and the outlet (25) of the second regenerator is connected to the second catalyst inlet (12).

5. The residual oil lightening treatment device according to claim 1, characterized in that: The second separation zone (15) is arranged above the first separation zone (9), and the second reaction zone (14) is arranged within the second separation zone (15).

6. The residual oil lightening treatment device according to claim 4, characterized in that: The second separation zone (15) is arranged in the second regenerator (27); and the second stripping steam inlet (10) extends to the outside of the second regenerator (27).

7. The residual oil lightening treatment device according to claim 1, characterized in that: The first reaction zone (5) is also provided with a first lifting steam inlet (1), and the first lifting steam inlet (1) is arranged below the first catalyst inlet (2), and the first catalyst inlet (2) is arranged below the raw material inlet (4); the top of the first separation zone (9) is provided with a second lifting steam inlet (11), and the second reaction zone (14) is also provided with a recycled oil inlet (13).

8. A process for treating residual oil to lighten the quality, characterized in that: Using the residual oil lightening treatment device according to any one of claims 1 to 7 to perform lightening treatment on residual oil; The method comprises the following steps: residual oil reacts with catalyst a in a first reaction zone (5), oil gas and catalyst a at a first outlet are separated by a gas-solid separator, and the oil gas separated by the gas-solid separator enters a second reaction zone (14); The oil and gas react with the catalyst b in the second reaction zone (14), and the oil and gas and the catalyst b at the second outlet are separated by a separation component, and the oil and gas separated by the separation component are discharged through the oil and gas outlet (18).

9. The process for lightening the residual oil according to claim 8, characterized in that: The catalyst a separated from the gas-solid separator passes through the first stripping section (7) and enters the first regenerator (26) for regeneration; The catalyst b separated by the separation assembly enters the second regenerator (27) through the second stripping section (19) for regeneration.

10. The process for lightening the residual oil according to claim 8, characterized in that: Catalyst a is a catalytic material with a high hydrothermal stability and an alkaline active center, and catalyst b is a catalytic cracking acidic catalyst.

Images