Method for increasing yield of high-performance aerospace fuel base oil through kerosene co-hydrogenation and reaction system thereof

Abstract

The invention relates to a method for producing high-performance spaceflight fuel base oil with high yield through kerosene co-hydrogenation, which comprises the following steps: mixing catalytic slurry oil, a catalyst A and pulverized coal, introducing into a micro-scale hydrogen mixer, mixing with hydrogen, and carrying out rapid hydrocracking reaction to obtain a rapid hydrocracking product; mixing a catalyst B and anthracene oil, mixing the mixture with the rapid hydrocracking product, carrying out a deep hydrocracking reaction to obtain a deep hydrocracking product, and separating to obtain a light hydrocracking product and a heavy hydrocracking product; the heavy hydrocracking product firstly passes through a hot low-pressure separator, a vacuum tower and fractionation to obtain vacuum wax oil and tailings, the vacuum wax oil and the light hydrocracking product are mixed and then mixed with hydrogen, a hydro-upgrading reaction is performed, and a hydro-upgrading product is obtained; and carrying out a hydroisomerization reaction on the hydro-upgrading product to obtain a hydroisomerization product, and separating to obtain naphtha, aerospace fuel base oil, a heavy diesel oil component and a wax oil component. According to the invention, efficient and stable deep conversion of kerosene co-hydrogenation is realized.

Description

Technical Field

[0001] The invention belongs to the technical field of energy-density aerospace fuel base oil preparation, and specifically relates to a method for co-hydrogenating kerosene to produce high-performance aerospace fuel base oil and a reaction system thereof. Background Art

[0002] With the rapid development of aerospace and military fields, there is a demand for various aircraft that can achieve supersonic, ultra-long-range, and unconventional climate environment flight missions, and thus there is an urgent need for high-energy-density aerospace fuels, which have higher performance requirements than aviation kerosene, with an energy density of at least 36Mj / L and a more concentrated distillation distribution. At present, the preparation methods of aerospace fuel base oil mainly include petroleum route and coal tar route. Kerosene co-hydrogenation is a reaction in which coal powder and heavy inferior oil are mixed as raw materials and synergistically hydrogenated under the action of a hydrogenation catalyst and in a hydrogen atmosphere. my country is rich in coal resources. The efficient hydrogenation of coal and heavy inferior oil to produce high-energy-density special oil products is not only conducive to the clean and effective use of coal and the efficient conversion of heavy inferior oil, but also conducive to ensuring the security of the national energy strategy.

[0003] CN201310241346.6 discloses a method for preparing a coal-based military fuel and the military fuel prepared, including: cutting the raw oil into light distillate oil and heavy distillate oil by distillation; mixing the catalyst, the sulfiding agent and the solvent oil evenly to make a catalyst oil slurry, mixing the catalyst oil slurry, the heavy distillate oil and the circulating oil with the catalyst for hydrocracking, separating the reaction products to obtain a liquid-solid phase mixture, and separating the liquid-solid phase mixture to obtain a light distillate oil; the light distillate oil is subjected to hydrofining or selective hydrogenation to obtain the generated oil, which is cooled and separated from the gas and liquid, and then enters the fractionation tower for product fractionation to obtain military fuel. However, the patent does not disclose or involve a technical solution on how to promote the conversion of heavy distillate oil on the basis of ensuring the stable operation of the system to ensure high-yield high-performance aerospace fuel base oil, does not disclose or involve a technical solution on how to improve the freezing point, calorific value and other indicators of aerospace fuel, and the suspended bed hydrogenation and fixed bed hydrogenation in the provided technical solution are offline modes.

[0004] CN201710813372.X discloses a method and system for producing fuel oil, aviation kerosene and diesel, the method comprising: (1) subjecting low-quality oil as a reforming raw material to a reforming reaction in a reforming reactor under hydrogen conditions to obtain a reforming product; (2) subjecting the reforming product to separation treatment to obtain at least a first separated product; (3) subjecting the first separated product to extraction and separation in an extraction and separation unit to obtain reformed oil and residue; (4) returning the residue to the reforming reaction, or discarding the residue; or returning part of the residue to the reforming reaction, and discarding the remaining part of the residue; (5) subjecting the reformed oil to a first hydrogenation treatment and / or subjecting the reformed oil to a hydrocracking treatment. This patent is a petroleum-based technical route, and does not disclose or involve a technical solution for promoting the conversion of heavy distillate oil on the basis of ensuring stable operation of the system to ensure high-yield high-performance aerospace fuel base oil, nor does it disclose or involve a technical solution for improving the freezing point, calorific value and other indicators of aerospace fuel.

[0005] In summary, the prior art has technical solutions for utilizing kerosene co-hydrogenation to produce white oil and military diesel, but does not provide a technical solution for kerosene co-hydrogenation to produce more high-performance aerospace fuel base oil, and the product added value is low. Moreover, the prior art also does not provide a technical solution for promoting the deep hydrogenation and deep cracking mutual promotion, coordinated and stable operation, and efficient conversion of kerosene co-hydrogenation reactions. There are deficiencies in the solution for promoting the deep conversion of concentrated rings in coal and oil to produce more raw materials suitable for the production of aerospace fuel base oil. Summary of the invention

[0006] In order to overcome the deficiencies of the above-mentioned prior art, the object of the present invention is to provide a method for co-hydrogenating kerosene to produce high-performance aerospace fuel base oil, which uses coal and catalytic oil slurry as raw materials, and successively undergoes microscale mixed bed rapid hydrocracking and microscale mixed bed deep hydrocracking to produce a large amount of light kerosene mixed products, and then microscale hydrogenation upgrading, microscale aromatics hydroisomerization, and alkane hydroisomerization are carried out online in sequence to achieve stable operation of the device to produce a kerosene mixed-base high-energy density aerospace fuel base oil with high performance and high yield.

[0007] A method for co-hydrogenating kerosene to produce high-performance aerospace fuel base oil comprises the following steps: (1) The catalytic oil slurry, catalyst A and coal powder are mixed and introduced into a microscale hydrogen mixer to mix with hydrogen, and then a rapid hydrocracking reaction is carried out to obtain a rapid hydrocracking product; (2) mixing the catalyst B and anthracene oil, and then mixing with the rapid hydrocracking product obtained in step (1) to perform a deep hydrocracking reaction to obtain a deep hydrocracking product, and separating the light hydrocracking product and the heavy hydrocracking product; (3) The heavy hydrocracking product is first subjected to a hot low fractionation and vacuum tower for fractionation to obtain vacuum wax oil and tailings, and the vacuum wax oil is mixed with the light hydrocracking product obtained in step (2) and then mixed with hydrogen to carry out a hydrogenation reforming reaction to obtain a hydrogenation reforming product; (4) The hydrogenation reforming product is subjected to a hydrogenation isomerization reaction to obtain a hydrogenation isomerization product, which is separated to obtain naphtha, aerospace fuel base oil, heavy diesel component and wax oil component.

[0008] Preferably, in step (1), the catalyst A is α-FeOOH / γ-FeOOH supported on a porous carbon material, the Fe content is 5.5% to 8.5%, and the mass ratio of α-FeOOH to γ-FeOOH is 1:1 to 1:3; the specific surface area of ​​the porous carbon material is 550 to 650 m 2 / g; The reaction conditions of the rapid hydrocracking reaction are: reaction temperature 450-462°C, reaction pressure 9-18MPa, hydrogen-to-oil ratio 1300-1700Nm 3 / t, airspeed 1~1.5h- 1 .

[0009] Preferably, in step (2), the catalyst B is a layered hydrotalcite Ni-Fe catalyst and a micro-scale amorphous silicon-aluminum, wherein the content of active metals Fe and Ni in the layered hydrotalcite Ni-Fe catalyst is 5% to 6% and the mass ratio of Fe to Ni is 1:9 to 3:7; the mass ratio of the layered hydrotalcite Ni-Fe catalyst to the micro-scale amorphous silicon-aluminum is 4:1 to 1:1; the deep hydrocracking reaction conditions are: reaction temperature 460 to 472°C, reaction pressure 9 to 18 MPa, hydrogen-to-oil ratio 1300 to 1700 Nm 3 / t, airspeed 0.3~0.6h -1 .

[0010] Preferably, in step (3), the 95% distillation point of the vacuum wax oil is less than 525°C; the conditions for the hydrogenation reforming reaction are: reaction temperature 375-390°C, reaction pressure 9-18Mpa, hydrogen-to-oil ratio 800-1500Nm 3 / t, airspeed 0.5~1.5h -1 .

[0011] Preferably, the catalysts for the hydroisomerization reaction in step (4) are, from top to bottom, active metal Pt catalysts supported on carriers USY molecular sieve, alumina and ZSM-5 molecular sieve, and active metal Ni-W catalysts supported on carriers USY molecular sieve, SAPO-11 molecular sieve and alumina; the active metal Pt catalysts supported on carriers USY molecular sieve, alumina and ZSM-5 molecular sieve account for 25-40% of the total catalyst amount, and in terms of mass percentage, the mass ratio of USY molecular sieve to carrier is 5%-25%, the mass ratio of ZSM-5 molecular sieve to carrier is 5%-15%, the mass ratio of Pt to carrier is 0.2-2.2%, and the balance is alumina; the active metal Ni-W catalysts supported on carriers USY molecular sieve, SAPO-11 molecular sieve and alumina are, in terms of mass percentage, SAPO-11 accounts for 15-40% of the carrier by mass, USY molecular sieve accounts for 30-5% of the carrier by mass, the active metal is Ni-W, which accounts for 14-28% of the carrier by mass, and the balance is alumina, and the mass ratio of Ni to W is 2:1-4:1; the conditions for the hydroisomerization reaction are: reaction temperature 365-385°C, reaction pressure 9-18Mpa, hydrogen-to-oil ratio 800-1500Nm3 / t, space velocity 0.5-1.5h -1 The aerospace fuel base oil has an initial distillation point of >188°C and a final distillation point of <250°C.

[0012] Preferably, the catalytic slurry in step (1) is one or more combinations of DCC catalytic slurry, FCC catalytic slurry, vacuum wax oil, medium and low temperature coal tar, high temperature coal tar, and ethylene cracking tar; the coal powder is Weiqiang coal; the mass ratio of the coal powder to the catalytic slurry is 2:8 to 4:6, and the amount of catalyst A added is 0.6 to 0.8% of the total amount of coal powder and catalytic slurry; the amount of anthracene oil added is 10% of the total amount of coal powder and catalytic slurry, and the amount of catalyst B added is 0.5 to 0.8% of the total amount of coal powder and catalytic slurry.

[0013] A reaction system for co-hydrogenating kerosene to produce high-performance aerospace fuel base oil, the reaction system comprising a microscale hydrogen mixer A (11), a microscale mixed-phase bed fast hydrocracking reactor (21), a microscale mixed-phase bed deep hydrocracking reactor (22), a thermal high-fraction unit (1), a thermal low-fraction unit (2), a vacuum tower A (3), a microscale hydrogen mixer B (12), a microscale hydro-reforming reactor (23), a microscale hydro-isomerization reactor (24), and a separation system (6) connected in sequence; The light component outlet pipeline of the thermal high fraction unit (1) is mixed with the heavy component outlet pipeline of the vacuum tower A (3) and then connected to the liquid phase inlet pipeline of the microscale hydrogen mixer B (12); The liquid phase pipeline of the microscale hydrogen mixer A (11) is respectively connected to the catalyst A pipeline, the catalytic oil slurry pipeline and the coal powder pipeline; the liquid phase inlet pipeline of the microscale mixed bed deep hydrocracking reactor (22) is also connected to the catalyst B pipeline and the anthracene oil pipeline.

[0014] Preferably, the separation system (6) comprises a separation unit (4) and a vacuum tower B (5); the gas phase outlet pipeline of the separation unit (4) is connected to the hydrogen pipeline, and the liquid phase outlet pipeline is connected to the inlet pipeline of the vacuum tower (5); the heavy component wax oil outlet pipeline of the vacuum tower B (5) is connected to the inlet of the microscale mixed bed deep hydrocracking reactor (22); the heavy component heavy diesel component outlet pipeline of the vacuum tower B (5) is connected to the inlet pipeline of the microscale hydrogen mixer B (12); and the bottom outlet of the vacuum tower A (3) is connected to the tailings pipeline.

[0015] Preferably, the height-to-diameter ratio of the microscale mixed bed rapid hydrocracking reactor is 20:1-80:1; and the height-to-diameter ratio of the microscale mixed bed deep hydrocracking reactor (22) is 8:1-12:1.

[0016] Beneficial effects of the present invention (1) The present invention constructs a "two-zone reaction" by synergistically coupling a microscale mixed-phase bed rapid hydrocracking reaction and a microscale mixed-phase bed deep hydrocracking reaction, firstly performing rapid hydrogenation, moderate cracking, and adsorption of impurities, and then performing rapid hydrogenation, deep hydrogenation, and deep cracking, thereby achieving stable operation of raw materials and promoting the production of aerospace fuel base oil; (2) The present invention sequentially performs hydrogenation reforming, aromatics hydrogenation isomerization, and alkane hydrogenation isomerization under process reaction conditions suitable for a microscale reaction system. Hydrogenation reforming produces more raw materials suitable for use as aerospace fuel base oil. The successive hydrogenation isomerization reactions of aromatics hydrogenation isomerization and alkane hydrogenation isomerization effectively improve the calorific value and freezing point of the aerospace fuel base oil. (3) The present invention realizes efficient, stable and deep conversion of kerosene co-hydrogenation by system integration and coupling of different types of catalysts, reactors, process reaction conditions, process processing routes and other technical means, and realizes efficient and directional conversion of kerosene co-hydrogenation products, thereby achieving high production and performance improvement of aerospace fuel base oil; (4) Microscale hydrogen mixer - fully disperse hydrogen into the reaction raw materials, so that the solid phase (coal or catalyst), liquid phase (catalytic oil slurry) and hydrogen of the raw materials exist in microscale form and form a mixed phase material. After entering the microscale mixed phase bed fast hydrocracking reactor, a microscale mixed phase bed will be formed, which accelerates the dissolution, diffusion and transfer of hydrogen during the reaction, and then accelerates the activation and supply of activated hydrogen. The α-FeOOH / γ-FeOOH catalyst of porous carbon material has a unique external specific surface loading structure. The presence of active metal will not affect the pore structure to fully adsorb impurities generated during the reaction; the design of the high aspect ratio fast hydrocracking reactor and the design of temperature reaction conditions can provide conditions for rapid reaction. The focus of the rapid hydrocracking reaction is to carry out preliminary hydrocracking reactions on macromolecules that are prone to cracking reactions and heteroatoms containing metals or sulfur, nitrogen and oxygen. The α-FeOOH / γ-FeOOH catalyst supported on porous carbon materials, the reactor with a height-to-diameter ratio of 20:1-80:1, and the synergistic coupling scheme of reaction process conditions and microscale mixed-phase beds can fully adsorb the metals, coke or coke precursors deposited after the reaction on the basis of providing hydrogenation activity, and quickly pass through the reactor to avoid transitional cracking leading to transitional condensation and coking, thereby achieving rapid hydrogenation, moderate cracking, and adsorption of impurities. The reaction type is dominated by free radical reactions, and at the same time, it can provide a favorable basis for delaying the rapid deactivation of catalyst B. BRIEF DESCRIPTION OF THE DRAWINGS

[0017] Figure 1 The schematic diagram of the reaction system flow for producing high-performance aerospace fuel base oil by co-hydrogenation of kerosene.

[0018] 11-microscale hydrogen mixer A; 21-microscale mixed bed fast hydrocracking reactor; 22-microscale mixed bed deep hydrocracking reactor; 1-thermal high fraction unit; 2-thermal low fraction unit; 3-vacuum tower A; 12-microscale hydrogen mixer B; 23-microscale hydrogenation reforming reactor; 24-microscale hydrogenation isomerization reactor; 6-separation system; 4-separation unit; 5-vacuum tower B. DETAILED DESCRIPTION

[0019] Example 1 A reaction system for co-hydrogenating kerosene to produce high-performance aerospace fuel base oil, the reaction system comprising a microscale hydrogen mixer A 11, a microscale mixed-phase bed fast hydrocracking reactor 21, a microscale mixed-phase bed deep hydrocracking reactor 22, a thermal high-fraction unit 1, a thermal low-fraction unit 2, a vacuum tower A 3, a microscale hydrogen mixer B 12, a microscale hydro-reforming reactor 23, a microscale hydro-isomerization reactor 24, and a separation system 6 connected in sequence; The light component outlet pipeline of the thermal high fraction unit 1 is mixed with the heavy component outlet pipeline of the vacuum tower A 3 and then connected to the liquid phase inlet pipeline of the microscale hydrogen mixer B 12; The liquid phase pipeline of the microscale hydrogen mixer A 11 is respectively connected to the catalyst A pipeline, the catalytic oil slurry pipeline and the coal powder pipeline; the liquid phase inlet pipeline of the microscale mixed bed deep hydrocracking reactor 22 is also connected to the catalyst B pipeline and the anthracene oil pipeline.

[0020] At the beginning of start-up, catalyst A, catalytic oil slurry and coal powder are introduced into microscale hydrogen mixer A11 in a certain proportion, mixed with hydrogen introduced by hydrogen, and then enter microscale mixed bed fast hydrocracking reactor 21 for fast hydrocracking reaction to obtain fast hydrocracking products; the fast hydrogenation products, anthracene oil and catalyst B are introduced into microscale mixed bed deep hydrocracking reactor 22 in a certain proportion for deep hydrocracking reaction to obtain deep hydrocracking products, and the deep hydrocracking products are separated by a thermal high fractionation unit to obtain light hydrocracking products and heavy hydrocracking products, and the heavy hydrocracking products are fractionated by a thermal low fractionation unit 2 and a vacuum tower A3 to obtain vacuum wax oil, and the tailings are discharged from the bottom of the vacuum tower A3, and the vacuum wax oil is mixed with the light hydrocracking products and enters the microscale hydrogen mixer B. 12 is mixed with the hydrogen introduced into the hydrogen relationship and then enters the microscale hydrogenation reforming reactor 23 for hydrogenation reforming reaction to obtain a hydrogenation reforming product, and the hydrogenation reforming product is introduced into the microscale hydrogenation isomerization reactor 24 for hydrogenation isomerization reaction to obtain a hydrogenation isomerization product, and the hydrogenation isomerization product is fractionated by the separation system to obtain naphtha, aerospace fuel base oil, heavy diesel component and wax oil component.

[0021] Example 2 A reaction system for producing high-performance aerospace fuel base oil by co-hydrogenation of kerosene The separation system 6 includes a separation unit 4 and a vacuum tower B5; the gas phase outlet pipeline of the separation unit 4 is connected to the hydrogen pipeline, and the liquid phase outlet pipeline is connected to the inlet pipeline of the vacuum tower 5; the heavy component wax oil outlet pipeline of the vacuum tower B5 is connected to the inlet of the microscale mixed bed deep hydrocracking reactor 22; the heavy component heavy diesel component outlet pipeline of the vacuum tower B5 is connected to the inlet pipeline of the microscale hydrogen mixer B12; the bottom outlet of the vacuum tower A3 is connected to the tailings pipeline.

[0022] After stable start-up, the hydroisomerized product is separated into circulating hydrogen and hydroisomerized liquid products through separation unit 4, and the circulating hydrogen is introduced into the hydrogen pipeline as hydrogen source to participate in the reaction; the hydroisomerized liquid products are fractionated through vacuum tower B5 to obtain naphtha, aerospace fuel base oil, heavy diesel component and wax oil component; the heavy diesel component is connected to the liquid phase inlet of microscale hydrogen mixer B12 as a raw material and participates in subsequent reactions as a raw material; the wax oil component is connected to the inlet of microscale mixed bed deep hydrocracking reactor 22 and participates in subsequent reactions.

[0023] Example 3 A method for co-hydrogenating kerosene to produce high-performance aerospace fuel base oil comprises the following steps: (1) Coal powder and catalytic oil slurry were mixed in a mass ratio of 4:6, with the amount of catalyst A added being 0.8% of the total amount of coal powder and catalytic oil slurry. After being mixed with hydrogen in a microscale hydrogen mixer A 11, the mixture was introduced into a microscale mixed bed fast hydrocracking reactor 21 at a reaction temperature of 450°C, a reaction pressure of 9 MPa, a hydrogen-to-oil ratio of 1300 Nm3 / t, and a space velocity of 1.5 h -1 The reaction is carried out under the conditions of obtaining a fast hydrocracking product; (2) Anthracene oil was introduced at 10% of the total amount of coal powder and catalytic oil slurry, and the amount of catalyst B was 0.5%. Anthracene oil, catalyst B and hydrocracking products were passed through a micro-scale mixed bed deep hydrocracking reactor with a reaction temperature of 460°C, a reaction pressure of 9 MPa, a hydrogen-to-oil ratio of 1300 Nm3 / t, and a space velocity of 0.6 h -1 Performing a deep hydrocracking reaction to obtain a deep hydrocracking product, and passing the deep hydrocracking product into a thermal high separation unit 1 for separation to obtain a light hydrocracking product and a heavy hydrocracking product; (3) The heavy hydrocracking product is fractionated through the hot low fraction unit 2 and the vacuum tower A3 to obtain vacuum wax oil, the 95% distillation point of the vacuum wax oil is less than 520°C, and the tailings are discharged from the bottom of the vacuum tower A3. The vacuum wax oil is mixed with the light hydrocracking product and then enters the microscale hydrogen mixer B12 to mix with the hydrogen introduced from the hydrogen pipeline and then enters the microscale hydrogenation reforming reactor 23. The reaction temperature is controlled to be 375°C, the reaction pressure is 9Mpa, the hydrogen-to-oil ratio is 800Nm3 / t, and the space velocity is 1.5h-1 to carry out the hydrogenation reforming reaction to obtain the hydrogenation reforming product; (4) The hydrogenation reformed product is introduced into the microscale hydrogenation isomerization reactor 24 for hydrogen isomerization reaction, and the reaction temperature is controlled at 365°C, the reaction pressure is 9 MPa, the hydrogen-oil ratio is 800 Nm3 / t, and the space velocity is 1.5 h -1 , carry out a hydroisomerization reaction to obtain a hydroisomerization product, pass the hydroisomerization product through a separation unit 4 to separate circulating hydrogen and a hydroisomerization liquid phase product, and pass the circulating hydrogen into a hydrogen pipeline as a hydrogen source to participate in the reaction; the hydroisomerization liquid phase product is fractionated through a vacuum tower B5 to obtain naphtha, aerospace fuel base oil, a heavy diesel component and a wax oil component, wherein the aerospace fuel base oil has an initial boiling point of more than 188°C and a final boiling point of less than 250°C; the heavy diesel component is connected to the liquid phase inlet of a microscale hydrogen mixer B12 as a raw material, and participates in subsequent reactions as a raw material; the wax oil component is connected to the inlet of a microscale mixed-phase bed deep hydrocracking reactor 22, and participates in subsequent reactions; In step (1), the catalyst A is α-FeOOH / γ-FeOOH supported on a porous carbon material, the Fe content is 8.5% and the mass ratio of α-FeOOH to γ-FeOOH is 1:1; the specific surface area of ​​the porous carbon material is 550 m2 / g; In step (2), the catalyst B is a layered hydrotalcite Ni-Fe catalyst and micro-scale amorphous silicon-aluminum, wherein the content of active metals Fe and Ni in the layered hydrotalcite Ni-Fe catalyst is 5%, and the mass ratio of Fe to Ni is 1:9; the mass ratio of the layered hydrotalcite Ni-Fe catalyst to the micro-scale amorphous silicon-aluminum is 4:1; The catalysts for the hydroisomerization reaction in step (4) are, from top to bottom, an active metal Pt catalyst supported on carriers USY molecular sieve, alumina and ZSM-5 molecular sieve, and an active metal Ni-W catalyst supported on carriers USY molecular sieve, SAPO-11 molecular sieve and alumina; the active metal Pt catalyst supported on carriers USY molecular sieve, alumina and ZSM-5 molecular sieve accounts for 20% of the total catalyst amount, and in terms of mass percentage, the mass ratio of USY molecular sieve to the carrier is 5%, the mass ratio of ZSM-5 molecular sieve to the carrier is 15%, the mass ratio of Pt to the carrier is 0.2%, and the balance is alumina; the active metal Ni-W catalyst supported on carriers USY molecular sieve, SAPO-11 molecular sieve and alumina, in terms of mass percentage, the mass ratio of SAPO-11 to the carrier is 15%, the mass ratio of USY molecular sieve to the carrier is 30%, the mass ratio of Ni-W to the carrier is 14%, and the balance is alumina, and the mass ratio of Ni to W is 2:1; The height-to-diameter ratio of the micro-scale mixed-phase bed fast hydrocracking reactor 21 is 20:1; the height-to-diameter ratio of the micro-scale mixed-phase bed deep hydrocracking reactor 22 is 8:1; The coal powder is Weiqiang coal; the catalytic oil slurry is FCC catalytic oil slurry.

[0024] Example 4 A method for co-hydrogenating kerosene to produce high-performance aerospace fuel base oil comprises the following steps: (1) Coal powder and catalytic oil slurry were mixed in a mass ratio of 3:7, with the amount of catalyst A added being 0.6% of the total amount of coal powder and catalytic oil slurry. After being mixed with hydrogen in a microscale hydrogen mixer A 11, the mixture was introduced into a microscale mixed bed fast hydrocracking reactor 21 at a reaction temperature of 455°C, a reaction pressure of 12 MPa, a hydrogen-to-oil ratio of 1500 Nm3 / t, and a space velocity of 1.2 h -1 The reaction is carried out under the conditions of obtaining a fast hydrocracking product; (2) Anthracene oil was introduced at 10% of the total amount of coal powder and catalytic oil slurry, and the amount of catalyst B introduced was 0.8%. Anthracene oil, catalyst B and hydrocracking products were passed through a micro-scale mixed bed deep hydrocracking reactor 22, and the reaction temperature was controlled at 465°C, the reaction pressure was 12 MPa, the hydrogen-to-oil ratio was 1400 Nm3 / t, and the space velocity was 0.6 h -1Performing a deep hydrocracking reaction to obtain a deep hydrocracking product, and passing the deep hydrocracking product into a thermal high separation unit 1 for separation to obtain a light hydrocracking product and a heavy hydrocracking product; (3) The heavy hydrocracking product is fractionated through the hot low fraction unit 2 and the vacuum tower A3 to obtain vacuum wax oil, the 95% distillation point of the vacuum wax oil is less than 520°C, and the tailings are discharged from the bottom of the vacuum tower A3. The vacuum wax oil is mixed with the light hydrocracking product and then enters the microscale hydrogen mixer B12 to mix with the hydrogen introduced from the hydrogen pipeline and then enters the microscale hydrogenation reforming reactor 23. The reaction temperature is controlled to be 380°C, the reaction pressure is 12Mpa, the hydrogen-to-oil ratio is 1200Nm3 / t, and the space velocity is 1.2h-1 to carry out the hydrogenation reforming reaction to obtain the hydrogenation reforming product; (4) The hydro-modified product is introduced into the micro-scale hydroisomerization reactor 24, and the reaction temperature is controlled at 370°C, the reaction pressure is 12 MPa, the hydrogen-oil ratio is 1200 Nm3 / t, and the space velocity is 1.2 h -1 , carry out a hydroisomerization reaction to obtain a hydroisomerization product, pass the hydroisomerization product through a separation unit 4 to separate circulating hydrogen and a hydroisomerization liquid phase product, and pass the circulating hydrogen into a hydrogen pipeline as a hydrogen source to participate in the reaction; the hydroisomerization liquid phase product is fractionated through a vacuum tower B5 to obtain naphtha, aerospace fuel base oil, a heavy diesel component and a wax oil component, wherein the aerospace fuel base oil has an initial boiling point of more than 188°C and a final boiling point of less than 250°C; the heavy diesel component is connected to the liquid phase inlet of a microscale hydrogen mixer B12 as a raw material, and participates in subsequent reactions as a raw material; the wax oil component is connected to the inlet of a microscale mixed-phase bed deep hydrocracking reactor 22, and participates in subsequent reactions; In step (1), the catalyst A is α-FeOOH / γ-FeOOH supported on a porous carbon material, the Fe content is 7% and the mass ratio of α-FeOOH to γ-FeOOH is 1:2; the specific surface area of ​​the porous carbon material is 600 m2 / g; In step (2), the catalyst B is a layered hydrotalcite Ni-Fe catalyst and micro-scale amorphous silicon-aluminum, wherein the content of active metals Fe and Ni in the layered hydrotalcite Ni-Fe catalyst is 5.5%, and the mass ratio of Fe to Ni is 2:8; the mass ratio of the layered hydrotalcite Ni-Fe catalyst to the micro-scale amorphous silicon-aluminum is 3:1; The catalysts for the hydroisomerization reaction in step (4) are, from top to bottom, an active metal Pt catalyst supported on carriers USY molecular sieve, alumina and ZSM-5 molecular sieve, and an active metal Ni-W catalyst supported on carriers USY molecular sieve, SAPO-11 molecular sieve and alumina; the active metal Pt catalyst supported on carriers USY molecular sieve, alumina and ZSM-5 molecular sieve accounts for 40% of the total catalyst amount, and in terms of mass percentage, the mass ratio of USY molecular sieve to the carrier is 15%, the mass ratio of ZSM-5 molecular sieve to the carrier is 10%, the mass ratio of Pt to the carrier is 1%, and the balance is alumina; the active metal Ni-W catalyst supported on carriers USY molecular sieve, SAPO-11 molecular sieve and alumina is, in terms of mass percentage, the mass ratio of SAPO-11 to the carrier is 30%, the mass ratio of USY molecular sieve to the carrier is 10%, the mass ratio of Ni-W to the carrier is 16%, and the balance is alumina, and the mass ratio of Ni to W is 3:1; The height-to-diameter ratio of the micro-scale mixed-phase bed fast hydrocracking reactor 21 is 50:1; the height-to-diameter ratio of the micro-scale mixed-phase bed deep hydrocracking reactor 22 is 10:1; The coal powder is Weiqiang coal; the catalytic oil slurry is DCC catalytic oil slurry.

[0025] Example 5 A method for co-hydrogenating kerosene to produce high-performance aerospace fuel base oil comprises the following steps: (1) Coal powder and catalytic oil slurry were mixed in a mass ratio of 2:8, with the amount of catalyst A added being 0.8% of the total amount of coal powder and catalytic oil slurry. After being mixed with hydrogen in a microscale hydrogen mixer A 11, the mixture was introduced into a microscale mixed bed fast hydrocracking reactor 21 at a reaction temperature of 460°C, a reaction pressure of 16 MPa, a hydrogen-to-oil ratio of 1600 Nm3 / t, and a space velocity of 1 h -1 The reaction is carried out under the conditions of obtaining a fast hydrocracking product; (2) Anthracene oil was introduced at 10% of the total amount of coal powder and catalytic oil slurry, and the amount of catalyst B was 0.6%. Anthracene oil, catalyst B and hydrocracking products were passed through a micro-scale mixed bed deep hydrocracking reactor with a reaction temperature of 470°C, a reaction pressure of 16 MPa, a hydrogen-to-oil ratio of 1600 Nm3 / t, and a space velocity of 0.5 h -1 Performing a deep hydrocracking reaction to obtain a deep hydrocracking product, and passing the deep hydrocracking product into a thermal high separation unit 1 for separation to obtain a light hydrocracking product and a heavy hydrocracking product; (3) The heavy hydrocracking product is fractionated through the hot low fraction unit 2 and the vacuum tower A3 to obtain vacuum wax oil, the 95% distillation point of the vacuum wax oil is less than 520°C, and the tailings are discharged from the bottom of the vacuum tower A3. The vacuum wax oil is mixed with the light hydrocracking product and then enters the microscale hydrogen mixer B12 to mix with the hydrogen introduced from the hydrogen pipeline and then enters the microscale hydrogenation reforming reactor 23. The reaction temperature is controlled to be 390°C, the reaction pressure is 16Mpa, the hydrogen-to-oil ratio is 800Nm3 / t, and the space velocity is 0.6h -1 , carrying out a hydrogenation-upgrading reaction to obtain a hydrogenation-upgrading product; (4) The hydro-modified product is introduced into the micro-scale hydroisomerization reactor 24, and the reaction temperature is controlled at 380°C, the reaction pressure is 16 MPa, the hydrogen-oil ratio is 800 Nm3 / t, and the space velocity is 0.6 h -1 , carry out a hydroisomerization reaction to obtain a hydroisomerization product, pass the hydroisomerization product through a separation unit 4 to separate circulating hydrogen and a hydroisomerization liquid phase product, and pass the circulating hydrogen into a hydrogen pipeline as a hydrogen source to participate in the reaction; the hydroisomerization liquid phase product is fractionated through a vacuum tower B5 to obtain naphtha, aerospace fuel base oil, a heavy diesel component and a wax oil component, wherein the aerospace fuel base oil has an initial boiling point of more than 188°C and a final boiling point of less than 250°C; the heavy diesel component is connected to the liquid phase inlet of a microscale hydrogen mixer B12 as a raw material, and participates in subsequent reactions as a raw material; the wax oil component is connected to the inlet of a microscale mixed-phase bed deep hydrocracking reactor 22, and participates in subsequent reactions; In step (1), the catalyst A is α-FeOOH / γ-FeOOH supported on a porous carbon material, the Fe content is 5.5% and the mass ratio of α-FeOOH to γ-FeOOH is 1:3; the specific surface area of ​​the porous carbon material is 650 m2 / g; In step (2), the catalyst B is a layered hydrotalcite Ni-Fe catalyst and micro-scale amorphous silicon-aluminum, wherein the content of active metals Fe and Ni in the layered hydrotalcite Ni-Fe catalyst is 6%, and the mass ratio of Fe to Ni is 3:7; the mass ratio of the layered hydrotalcite Ni-Fe catalyst to the micro-scale amorphous silicon-aluminum is 1:1; The catalysts for the hydroisomerization reaction in step (4) are, from top to bottom, an active metal Pt catalyst supported on carriers USY molecular sieve, alumina and ZSM-5 molecular sieve, and an active metal Ni-W catalyst supported on carriers USY molecular sieve, SAPO-11 molecular sieve and alumina; the active metal Pt catalyst supported on carriers USY molecular sieve, alumina and ZSM-5 molecular sieve accounts for 30% of the total catalyst amount, and in terms of mass percentage, the mass ratio of USY molecular sieve to the carrier is 25%, the mass ratio of ZSM-5 molecular sieve to the carrier is 5%, the mass ratio of Pt to the carrier is 2.2%, and the balance is alumina; the active metal Ni-W catalyst supported on carriers USY molecular sieve, SAPO-11 molecular sieve and alumina is, in terms of mass percentage, the mass ratio of SAPO-11 to the carrier is 40%, the mass ratio of USY molecular sieve to the carrier is 5%, the mass ratio of Ni-W to the carrier is 18%, and the balance is alumina, and the mass ratio of Ni to W is 4:1; The height-to-diameter ratio of the micro-scale mixed-phase bed fast hydrocracking reactor 21 is 80:1; the height-to-diameter ratio of the micro-scale mixed-phase bed deep hydrocracking reactor 22 is 12:1; The coal powder is Weiqiang coal; the catalytic oil slurry is ethylene cracking tar.

[0026] Example 6 A method for co-hydrogenating kerosene to produce high-performance aerospace fuel base oil comprises the following steps: (1) Coal powder and catalytic oil slurry were mixed in a mass ratio of 2:8, with the amount of catalyst A added being 0.8% of the total amount of coal powder and catalytic oil slurry. After being mixed with hydrogen in a microscale hydrogen mixer A 11, the mixture was introduced into a microscale mixed bed fast hydrocracking reactor 21 at a reaction temperature of 462°C, a reaction pressure of 18 MPa, a hydrogen-to-oil ratio of 1700 Nm3 / t, and a space velocity of 1 h -1 The reaction is carried out under the conditions of obtaining a fast hydrocracking product; (2) Anthracene oil was introduced at 10% of the total amount of coal powder and catalytic oil slurry, and the amount of catalyst B was 0.8%. Anthracene oil, catalyst B and hydrocracking products were passed through a micro-scale mixed bed deep hydrocracking reactor with a controlled reaction temperature of 472°C, a reaction pressure of 18 MPa, a hydrogen-to-oil ratio of 1700 Nm3 / t, and a space velocity of 0.3 h -1 Performing a deep hydrocracking reaction to obtain a deep hydrocracking product, and passing the deep hydrocracking product into a thermal high separation unit 1 for separation to obtain a light hydrocracking product and a heavy hydrocracking product; (3) The heavy hydrocracking product is fractionated through the hot low fraction unit 2 and the vacuum tower A3 to obtain vacuum wax oil, the 95% distillation point of the vacuum wax oil is less than 520°C, and the tailings are discharged from the bottom of the vacuum tower A3. The vacuum wax oil is mixed with the light hydrocracking product and then enters the microscale hydrogen mixer B12 and is mixed with the hydrogen introduced from the hydrogen pipeline and then enters the microscale hydrogenation reforming reactor 23. The reaction temperature is controlled to be 390°C, the reaction pressure is 18Mpa, the hydrogen-to-oil ratio is 800Nm3 / t, and the space velocity is 0.5h -1 , carrying out a hydrogenation-upgrading reaction to obtain a hydrogenation-upgrading product; (4) The hydro-modified product is introduced into the micro-scale hydroisomerization reactor 24, and the reaction temperature is controlled at 385°C, the reaction pressure is 18 MPa, the hydrogen-oil ratio is 800 Nm3 / t, and the space velocity is 0.5 h -1 , carry out a hydroisomerization reaction to obtain a hydroisomerization product, pass the hydroisomerization product through a separation unit 4 to separate circulating hydrogen and a hydroisomerization liquid phase product, and pass the circulating hydrogen into a hydrogen pipeline as a hydrogen source to participate in the reaction; the hydroisomerization liquid phase product is fractionated through a vacuum tower B5 to obtain naphtha, aerospace fuel base oil, a heavy diesel component and a wax oil component, wherein the aerospace fuel base oil has an initial boiling point of more than 188°C and a final boiling point of less than 250°C; the heavy diesel component is connected to the liquid phase inlet of a microscale hydrogen mixer B12 as a raw material, and participates in subsequent reactions as a raw material; the wax oil component is connected to the inlet of a microscale mixed-phase bed deep hydrocracking reactor 22, and participates in subsequent reactions; In step (1), the catalyst A is α-FeOOH / γ-FeOOH supported on a porous carbon material, the Fe content is 5.5% and the mass ratio of α-FeOOH to γ-FeOOH is 1:3; the specific surface area of ​​the porous carbon material is 650 m2 / g; In step (2), the catalyst B is a layered hydrotalcite Ni-Fe catalyst and micro-scale amorphous silicon-aluminum, wherein the content of active metals Fe and Ni in the layered hydrotalcite Ni-Fe catalyst is 6%, and the mass ratio of Fe to Ni is 3:7; the mass ratio of the layered hydrotalcite Ni-Fe catalyst to the micro-scale amorphous silicon-aluminum is 1:1; The catalysts for the hydroisomerization reaction in step (4) are, from top to bottom, an active metal Pt catalyst supported on carriers USY molecular sieve, alumina and ZSM-5 molecular sieve, and an active metal Ni-W catalyst supported on carriers USY molecular sieve, SAPO-11 molecular sieve and alumina; the active metal Pt catalyst supported on carriers USY molecular sieve, alumina and ZSM-5 molecular sieve accounts for 30% of the total catalyst amount, and in terms of mass percentage, the mass ratio of USY molecular sieve to the carrier is 25%, the mass ratio of ZSM-5 molecular sieve to the carrier is 5%, the mass ratio of Pt to the carrier is 2.2%, and the balance is alumina; the active metal Ni-W catalyst supported on carriers USY molecular sieve, SAPO-11 molecular sieve and alumina is, in terms of mass percentage, the mass ratio of SAPO-11 to the carrier is 40%, the mass ratio of USY molecular sieve to the carrier is 5%, the mass ratio of Ni-W to the carrier is 28%, and the balance is alumina, and the mass ratio of Ni to W is 4:1; The height-to-diameter ratio of the micro-scale mixed-phase bed fast hydrocracking reactor 21 is 80:1; the height-to-diameter ratio of the micro-scale mixed-phase bed deep hydrocracking reactor 22 is 12:1; The coal powder is Weiqiang coal; the catalytic oil slurry is ethylene cracking tar.

[0027] Comparative Example 1 Catalyst B was not added, and the rest was the same as in Example 3.

[0028] Comparative Example 2 In step (2), the catalyst B is a layered hydrotalcite Ni-Fe catalyst, the content of active metals Fe and Ni in the layered hydrotalcite Ni-Fe catalyst is 5%, and the mass ratio of Fe to Ni is 1:9. The rest is the same as in Example 3.

[0029] Comparative Example 3 The catalyst for the hydrogen isomerization reaction in step (4) is an active metal Pt catalyst supported on carriers of USY molecular sieve, alumina and ZSM-5 molecular sieve. The active metal Pt catalyst supported on carriers of USY molecular sieve, alumina and ZSM-5 molecular sieve is calculated by mass percentage, and the mass ratio of USY molecular sieve to the carrier is 5%, the mass ratio of ZSM-5 molecular sieve to the carrier is 15%, the mass ratio of Pt to the carrier is 0.2%, and the balance is alumina. Others are the same as in Example 3.

[0030] Comparative Example 4 In step (4), the active metal Ni-W catalyst is loaded on the carriers USY molecular sieve, SAPO-11 molecular sieve and alumina. According to the mass percentage, SAPO-11 accounts for 15% of the mass ratio of the carrier, USY molecular sieve accounts for 30% of the mass ratio of the carrier, the active metal is Ni-W accounts for 14% of the mass ratio of the carrier, and the balance is alumina. The mass ratio of Ni to W is 2:1. Other aspects are the same as those in Example 3.

[0031] The raw materials used in Examples 3-6 and Comparative Examples 1-4 and the yields and properties of the products are shown in Tables 1 to 3. Table 1 Catalytic oil slurry properties . Table 2 Coal powder properties .

[0032] Table 3 Results of Examples and Comparative Examples .

Claims

1. A method for co-hydrogenating kerosene to produce high-performance aerospace fuel base oil, characterized in that: The following steps are involved: (1) The catalytic oil slurry, catalyst A and coal powder are mixed and introduced into a microscale hydrogen mixer to mix with hydrogen, and then a rapid hydrocracking reaction is carried out to obtain a rapid hydrocracking product; (2) mixing the catalyst B and anthracene oil, and then mixing with the rapid hydrocracking product obtained in step (1) to perform a deep hydrocracking reaction to obtain a deep hydrocracking product, and separating the light hydrocracking product and the heavy hydrocracking product; (3) The heavy hydrocracking product is first subjected to a hot low fractionation and vacuum tower for fractionation to obtain vacuum wax oil and tailings, and the vacuum wax oil is mixed with the light hydrocracking product obtained in step (2) and then mixed with hydrogen to carry out a hydrogenation reforming reaction to obtain a hydrogenation reforming product; (4) The hydrogenation reforming product is subjected to a hydrogenation isomerization reaction to obtain a hydrogenation isomerization product, which is separated to obtain naphtha, aerospace fuel base oil, heavy diesel component and wax oil component.

2. The method for producing high-performance aerospace fuel base oil by co-hydrogenation of kerosene according to claim 1, characterized in that: In step (1), the catalyst A is α-FeOOH / γ-FeOOH supported on a porous carbon material, the Fe content is 5.5% to 8.5%, and the mass ratio of α-FeOOH to γ-FeOOH is 1:1 to 1:3; the specific surface area of ​​the porous carbon material is 550 to 650 m 2 / g; The reaction conditions of the rapid hydrocracking reaction are: reaction temperature 450-462°C, reaction pressure 9-18MPa, hydrogen-to-oil ratio 1300-1700Nm 3 / t, airspeed 1~1.5h- 1 .

3. The method for producing high-performance aerospace fuel base oil by co-hydrogenation of kerosene according to claim 1, characterized in that: The catalyst B in step (2) is a layered hydrotalcite Ni-Fe catalyst and micro-scale amorphous silicon-aluminum, wherein the content of active metals Fe and Ni in the layered hydrotalcite Ni-Fe catalyst is 5% to 6% and the mass ratio of Fe to Ni is 1:9 to 3:7; the mass ratio of the layered hydrotalcite Ni-Fe catalyst to the micro-scale amorphous silicon-aluminum is 4:1 to 1:1; the deep hydrocracking reaction conditions are: reaction temperature 460 to 472°C, reaction pressure 9 to 18 MPa, hydrogen-to-oil ratio 1300 to 1700 Nm 3 / t, airspeed 0.3~0.6h -1 .

4. The method for producing high-performance aerospace fuel base oil by co-hydrogenation of kerosene according to claim 1, characterized in that: In the step (3), the 95% distillation point of the vacuum wax oil is less than 525°C; the conditions of the hydrogenation reforming reaction are: reaction temperature 375-390°C, reaction pressure 9-18Mpa, hydrogen-to-oil ratio 800-1500Nm 3 / t, airspeed 0.5~1.5h -1 .

5. The method for co-hydrogenating kerosene to produce high-performance aerospace fuel base oil according to claim 1, characterized in that: The catalysts for the hydroisomerization reaction in step (4) are, from top to bottom, an active metal Pt catalyst supported on carriers USY molecular sieve, alumina and ZSM-5 molecular sieve, and an active metal Ni-W catalyst supported on carriers USY molecular sieve, SAPO-11 molecular sieve and alumina; the active metal Pt catalyst supported on carriers USY molecular sieve, alumina and ZSM-5 molecular sieve accounts for 25-40% of the total catalyst amount. In terms of mass percentage, the mass ratio of USY molecular sieve to carrier is 5%-25%, the mass ratio of ZSM-5 molecular sieve to carrier is 5%-15%, the mass ratio of Pt to carrier is 0.2-2.2%, and the balance is alumina; the active metal Ni-W catalyst supported on carriers USY molecular sieve, SAPO-11 molecular sieve and alumina is calculated in terms of mass percentage, SAPO-11 accounts for 15-40% of the carrier by mass, USY molecular sieve accounts for 30-5% of the carrier by mass, the active metal is Ni-W, which accounts for 14-28% of the carrier by mass, and the balance is alumina, and the mass ratio of Ni to W is 2:1-4:1; the conditions for the hydroisomerization reaction are: reaction temperature 365-385°C, reaction pressure 9-18Mpa, hydrogen-to-oil ratio 800-1500Nm3 / t, space velocity 0.5-1.5h -1 The aerospace fuel base oil has an initial distillation point of >188°C and a final distillation point of <250°C.

6. The method for co-hydrogenating kerosene to produce high-performance aerospace fuel base oil according to claim 1, characterized in that: The catalytic slurry in step (1) is one or more combinations of DCC catalytic slurry, FCC catalytic slurry, vacuum wax oil, medium and low temperature coal tar, high temperature coal tar, and ethylene cracking tar; the coal powder is Weiqiang coal; the mass ratio of the coal powder to the catalytic slurry is 2:8 to 4:6, the amount of catalyst A added is 0.6 to 0.8% of the total amount of coal powder and catalytic slurry; the amount of anthracene oil added is 10% of the total amount of coal powder and catalytic slurry, and the amount of catalyst B added is 0.5 to 0.8% of the total amount of coal powder and catalytic slurry.

7. The reaction system for producing high-performance aerospace fuel base oil by co-hydrogenation of kerosene according to claim 1, characterized in that: The reaction system comprises a microscale hydrogen mixer A (11), a microscale mixed-phase bed fast hydrocracking reactor (21), a microscale mixed-phase bed deep hydrocracking reactor (22), a thermal high-fraction unit (1), a thermal low-fraction unit (2), a vacuum tower A (3), a microscale hydrogen mixer B (12), a microscale hydrogenation reforming reactor (23), a microscale hydrogenation isomerization reactor (24), and a separation system (6) which are connected in sequence; The light component outlet pipeline of the thermal high fraction unit (1) is mixed with the heavy component outlet pipeline of the vacuum tower A (3) and then connected to the liquid phase inlet pipeline of the microscale hydrogen mixer B (12); The liquid phase pipeline of the microscale hydrogen mixer A (11) is respectively connected to the catalyst A pipeline, the catalytic oil slurry pipeline and the coal powder pipeline; the liquid phase inlet pipeline of the microscale mixed bed deep hydrocracking reactor (22) is also connected to the catalyst B pipeline and the anthracene oil pipeline.

8. The reaction system for producing high-performance aerospace fuel base oil by co-hydrogenation of kerosene according to claim 7, characterized in that: The separation system (6) comprises a separation unit (4) and a vacuum tower B (5); the gas phase outlet pipeline of the separation unit (4) is connected to a hydrogen pipeline, and the liquid phase outlet pipeline is connected to an inlet pipeline of the vacuum tower (5); the heavy component wax oil outlet pipeline of the vacuum tower B (5) is connected to an inlet of a micro-scale mixed-phase bed deep hydrocracking reactor (22); the heavy component heavy diesel component outlet pipeline of the vacuum tower B (5) is connected to an inlet pipeline of a micro-scale hydrogen mixer B (12); and the bottom outlet of the vacuum tower A (3) is connected to a tailings pipeline.

9. The reaction system for producing high-performance aerospace fuel base oil by co-hydrogenation of kerosene according to claim 8, characterized in that: The height-to-diameter ratio of the microscale mixed-bed rapid hydrocracking reactor is 20:1-80:1; the height-to-diameter ratio of the microscale mixed-bed deep hydrocracking reactor (22) is 8:1-12:1.

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