A heavy oil hydrodesulfurization and de-residue carbon catalyst and a preparation method thereof

Abstract

The application discloses a heavy oil hydrodesulfurization and de-residual carbon catalyst and a preparation method thereof. The preparation method comprises the following steps: adding an extrusion aid and a pore expanding agent into a macroporous pseudo-boehmite, mixing, then adding an acidic metal impregnation solution, kneading, shaping, drying and roasting to obtain the catalyst; the pore expanding agent comprises a carbon alcohol and polystyrene. The method is simple in process and low in cost, the prepared catalyst has a good pore structure, is beneficial to adsorption and removal of colloid and asphaltene macromolecules in heavy oil, promotes conversion of residual carbon and desulfurization, and prolongs the service life of the catalyst.

Description

TECHNICAL FIELD

[0001] The present application belongs to the field of catalyst technology, and particularly relates to a heavy oil hydrodesulfurization and de-residual carbon catalyst and a preparation method thereof. BACKGROUND

[0002] With the increasing of heavy and poor crude oil, the demand for light oil increases, and the requirement for lightening of heavy oil is higher and higher. Heavy oil is the heaviest component in crude oil, and its proportion in crude oil is usually 40-60%, and its properties are significantly worse than those of gas oil and other fractions with lower boiling range. Residual oil is complex in composition, high in average molecular weight, viscosity and density, and contains a large amount of harmful elements such as metals, sulfur, nitrogen, gum and asphaltene, and non-ideal components, and is very difficult to process.

[0003] The fixed bed residual oil hydrogenation technology is the most widely used heavy oil hydrogenation treatment technology at present. In this process, in the presence of catalyst and hydrogen, residual oil is subjected to reactions such as hydrodesulfurization, hydrodenitrogenation, hydrode-residual carbon and hydrodemetallization. The hydrogenated residual oil will become a high-quality catalytic cracking feedstock, and then the heavy oil will be converted into light oil. In the fixed bed residual oil hydrogenation industrial device, the desulfurization and de-residual carbon catalyst is loaded behind the demetallization catalyst. Most of the metal and sulfur impurities in the residual oil exist in the gum and asphaltene, and the gum and asphaltene are the components with the largest molecular weight and the most complex structure in petroleum components, and have large diffusion resistance and are prone to pore plugging (causing catalyst deactivation). Therefore, a catalyst with a large pore volume is beneficial for the passage of large molecules containing impurities, the reaction inside the catalyst pores, the increase of demetallization capacity, and the maintenance of a large specific surface area is beneficial for the activity of desulfurization and de-residual carbon. In the fixed bed or ebullated bed residual oil hydrogenation industrial device, after the poor heavy oil passes through the demetallization catalyst bed, the asphaltene and gum are reduced in size after reaction. Therefore, the preparation of a residual oil hydrodesulfurization and de-residual carbon catalyst with a directional increase of 15-20 nm and 20-30 nm pore content is beneficial for the reaction of asphaltene and gum after passing through the demetallization catalyst bed, the reduction of the deactivation rate of the desulfurization and de-residual carbon catalyst, the extension of the service life of the catalyst, and the increase of the operation cycle of the device.

[0004] CN106622314A discloses a high-activity hydrofining catalyst and a preparation method thereof. The method uses water as a solvent to prepare a slurry containing silicon-phosphorus-aluminum oxide, adds a boron-containing compound, a group VIB metal compound and a group VIII metal compound into the slurry, filters to obtain a filter cake and a filtrate, mixes the filtrate with SB powder and a peptizing agent to obtain a binder, and then the binder and the filter cake are sequentially subjected to rolling, molding, drying and calcination to obtain the hydrofining catalyst. The catalyst has a small pore volume and a fast deactivation rate.

[0005] CN108102711B provides a combined process method for producing needle coke, which is that the raw oil enters a catalytic cracking device, the catalytic oil slurry obtained after reaction and separation is mixed with hydrogen and then enters a ebullated bed reactor, the heavy component of the liquid product obtained after separation of the ebullated bed reactor reaction effluent enters a coking device, and the oil gas generated by the coking reaction is separated to obtain gas, coking gasoline, coking diesel and coking wax oil, and the needle coke generated after the reaction period ends is deposited in the coking device. In the method of the present application, a hydrogen treatment catalyst is loaded in the catalytic section of the ebullated bed reactor, the specific surface area of the special catalyst in the present application is 120m 2 / g~300m 2 / g, preferably 160m 2 / g~280m 2 / g; the pore volume is 0.2mL / g~0.8mL / g, preferably 0.4mL / g~0.6mL / g; the average pore size is 8nm~13nm, preferably 9nm~11nm, and the pore size distribution is as follows: the pore volume with a diameter of 4nm~10nm accounts for 70%~80% of the total pore volume, and the pore volume with a diameter of 15nm accounts for 5%~10% of the total pore volume. The process of the present application is complex, the pore volume and pore size of the catalyst are small, which is not conducive to the diffusion of large molecules such as asphaltene, and the hydrogenation process conditions required are harsh, although the sulfur impurities in the catalytic oil slurry can be removed, but the aromatic hydrocarbons are lost.

[0006] CN1181409A discloses a residue hydrotreating catalyst and a preparation method thereof, which takes γ-Al2O3 as the carrier and loads group VIII and group VIB metal elements, characterized in that the pore volume of the catalyst is 0.30-0.60mL / g, the specific surface area is 120-200m 2 / g, the average pore size is 9.0-13.0nm, and the ratio of the pore volume with a pore size of 7.0-13.0nm to the total pore volume is greater than 80%. The catalyst prepared by the method has a large specific surface area and a small proportion of large pores, has poor resistance to metal poisoning and is deactivated quickly.

[0007] CN1417300A discloses a hydrogenation catalyst and a preparation method thereof, which includes impregnating a macroporous alumina carrier with a solution containing group VIB and group VIII metal compounds, the preparation method of the alumina carrier includes extruding a mixture of pseudoboehmite, acid, water and extrusion aid, rapidly drying the extruded product at 90-300℃ within 35 minutes, and calcining the product in an atmosphere containing water vapor at 600-800℃ for at least 0.5 hours, and the pore distribution of the obtained alumina carrier is that the pores with a diameter of 10-20nm account for 70-90% of the total pore volume.

[0008] CN1103009A discloses a preparation method of a heavy oil hydrodemetallization catalyst carrier, which is formed by mixing and kneading two aluminum hydroxide precursors with different pore size distributions, adding carbon black and a surfactant as a pore expander, and then drying and calcining to form a double-pore alumina carrier. SUMMARY

[0009] The present application aims to provide a heavy oil hydrodesulfurization and hydrodecarbon catalyst and a preparation method thereof, which is simple and low in cost, and the prepared catalyst has a good pore structure, which is beneficial to the adsorption and removal of resin and asphaltene macromolecules in heavy oil, promotes the conversion of residual carbon and desulfurization, and prolongs the service life of the catalyst.

[0010] To achieve the above-mentioned purpose, the present application provides a preparation method of a heavy oil hydrodesulfurization and hydrodecarbon catalyst, which comprises the following steps: adding a plasticizer and a pore expander to a macroporous pseudo-boehmite, mixing, then adding an acidic metal impregnation solution, kneading, shaping, drying and calcining to obtain the catalyst; the pore expander comprises a carbon alcohol and polystyrene.

[0011] The preparation method of the heavy oil hydrodesulfurization and hydrodecarbon catalyst provided by the present application, wherein the carbon alcohol is octadecanol or tetracosanol.

[0012] The preparation method of the heavy oil hydrodesulfurization and hydrodecarbon catalyst provided by the present application, wherein the addition amount of the carbon alcohol is 0.5wt%-6wt% of the content of alumina in the pseudo-boehmite, preferably 2wt%-4wt%; the addition amount of the polystyrene is 2wt%-8wt% of the content of alumina in the pseudo-boehmite, preferably 4wt%-6wt%.

[0013] The preparation method of the heavy oil hydrodesulfurization and hydrodecarbon catalyst provided by the present application, wherein the specific surface area of the macroporous pseudo-boehmite is greater than or equal to 330m 2 / g, and the pore volume is greater than or equal to 1.15ml / g.

[0014] The preparation method of the heavy oil hydrodesulfurization and hydrodecarbon catalyst provided by the present application, wherein the acidic metal impregnation solution comprises an active metal precursor, an inorganic acid and a complexing agent.

[0015] The preparation method of the heavy oil hydrodesulfurization and hydrodecarbon catalyst provided by the present application, wherein the complexing agent is an amino acid substance, and the addition amount is 1wt%-15wt% of the pseudo-boehmite, preferably 3wt%-10wt%.

[0016] The preparation method of the heavy oil hydrodesulfurization and hydrodecarbon catalyst provided by the present application, wherein the complexing agent is one or more of arginine, histidine and lysine.

[0017] The preparation method of the heavy oil hydrodesulfurization and de-carbon residue catalyst, the active metal in the acid metal impregnation solution is the group VIB and / or group VIII metal, which is the hydrogenation active metal component, preferably the active metal is at least one of Mo and W and at least one of Ni and Co. The precursor of Mo element is one or more of ammonium molybdate, sodium phosphomolybdate and ammonium phosphomolybdate; the precursor of W element is ammonium tungstate, tungsten nitrate and ammonium metatungstate; the precursor of Ni element is one or more of nickel nitrate, nickel acetate and basic nickel carbonate; the precursor of Co element is one or more of cobalt nitrate, basic nickel cobalt carbonate and cobalt naphthenate. In terms of oxide, molybdenum and / or tungsten accounts for 8wt%-20wt% of the total mass of the catalyst, and nickel and / or cobalt accounts for 2wt%-5wt% of the total mass of the catalyst.

[0018] The preparation method of the heavy oil hydrodesulfurization and de-carbon residue catalyst, the inorganic acid is one or more of phosphoric acid, nitric acid and hydrochloric acid, and the amount of the inorganic acid is not particularly limited, which is used to dissolve the active metal precursor, and the amount can be adjusted by the person skilled in the art according to the actual situation.

[0019] The preparation method of the heavy oil hydrodesulfurization and de-carbon residue catalyst, the extrusion aid is a cellulose substance, and the addition amount is 1wt%-6wt% of the content of alumina in pseudo-boehmite, preferably 2wt%-4wt%, the cellulose substance is a commonly used substance in the art, and specifically can be methyl cellulose, ethyl cellulose and hydroxymethyl cellulose, which is not particularly limited in the present application.

[0020] The preparation method of the heavy oil hydrodesulfurization and de-carbon residue catalyst, the forming process is carried out by a screw extruder, the extrusion pressure is 15-50Mpa, and the shape of the catalyst can be changed as needed, such as cylinder, trilobes, quadrilobes and spheres; the drying temperature is 100-200℃.

[0021] The preparation method of the heavy oil hydrodesulfurization and de-carbon residue catalyst, the calcination temperature is 500-900℃, preferably 680-850℃, and the calcination time is 0.5-6 hours.

[0022] To achieve the above-mentioned purpose, the present application also provides a catalyst prepared by the method, the pore volume is 0.60-0.95ml / g, the pores with a diameter of 15nm-20nm account for 40%-60% of the total pore volume, and the pores with a diameter of 20-30nm account for 25%-35% of the total pore volume.

[0023] The present application has the following beneficial effects:

[0024] The method provided by the present application firstly uses large-pore pseudo-boehmite, adds carbon alcohol and polystyrene, and the polystyrene physically expands the pores by 15-20 nm, the hydroxyl groups in the carbon alcohol combine with the hydroxyl groups of the large-pore pseudo-boehmite, and the isomerized carbon chain expands the pores by 20-30 nm. The increase of the proportion of the large pores helps the asphaltene and colloid macromolecules to be converted in the internal pores of the catalyst, and improves the desulfurization rate; the addition of the amino acid complexing agent improves the dispersion of the metal salt and promotes the conversion of the residual carbon.

[0025] The catalyst prepared according to the method provided by the present application has higher desulfurization effect and residual carbon conversion capacity. DETAILED DESCRIPTION

[0026] The present application will be described in detail below through examples. It is necessary to point out here that the following examples are only used for further illustrating the present application and cannot be understood as limiting the protection scope of the present application, and the skilled in the art can make some non-essential improvements and adjustments to the present application according to the above content of the present application.

[0027] Example 1

[0028] Pseudo-boehmite dry gel powder 500g (specific surface 330m 2 / g, pore volume 1.18ml / g, dry basis content 70wt%) is added with 3.5g of methyl cellulose (1wt%), 1.8g of octadecanol (0.5wt%) and 7g of polystyrene (2wt%), and is uniformly mixed; 500ml of Mo-Ni-P solution (containing MoO3 10wt%, NiO 5wt% in the catalyst) is added and kneaded, wherein the Mo-Ni-H3PO4 solution is configured as follows: 50g of molybdenum trioxide is added into 100ml of H3PO4 solution and stirred to completely dissolve, 32g of basic nickel carbonate is added and stirred to completely dissolve, 15g of arginine is added and stirred to completely dissolve, and water is added to 500ml; then, the mixture is extruded into clover-shaped particles with a particle size of 1.4-1.6mm on a front-extrusion single-screw extruder, the extrusion pressure is 15MPa, and the mixture is dried at 100℃ for 3 hours, and then the mixture is calcined at 700℃ for 6 hours to obtain catalyst A1. The physical properties of the catalyst are shown in Table 1.

[0029] Example 2

[0030] Pseudo-boehmite dry gel powder 500g (specific surface 330m 2(gibbsite-like pseudoboehmite, specific surface 330 m2 / g, pore volume 1.18 ml / g, dry base content 70 wt%), 20 g of methyl cellulose (6 wt%), 20 g of octadecanol (6 wt%) and 10 g of polystyrene (3 wt%) were added and mixed uniformly; 500 ml of Mo-Ni-P solution (containing MoO3 10 wt% and NiO 5 wt% in the catalyst) was added and kneaded, wherein the Mo-Ni-H3PO4 solution was prepared as follows: 50 g of molybdenum trioxide was added into 100 ml of H3PO4 solution and stirred until completely dissolved, 32 g of basic nickel carbonate was added and stirred until completely dissolved, 45 g of lysine was added and stirred until completely dissolved, and water was added to make up to 500 ml; then it was extruded into cylindrical shape with a diameter of 1.6 mm on a front extrusion single screw extruder, the extrusion pressure was 25 MPa, dried at 120°C for 3 hours, and then calcined at 500°C for 6 hours to obtain catalyst A3. The properties of the catalyst are shown in Table 1.

[0031] Example 3

[0032] 500 g of pseudoboehmite dry gel powder (specific surface 330 m 2 (gibbsite-like pseudoboehmite, specific surface 330 m2 / g, pore volume 1.18 ml / g, dry base content 70 wt%), 20 g of methyl cellulose (6 wt%), 20 g of octadecanol (6 wt%) and 10 g of polystyrene (3 wt%) were added and mixed uniformly; 500 ml of Mo-Ni-P solution (containing MoO3 10 wt% and NiO 5 wt% in the catalyst) was added and kneaded, wherein the Mo-Ni-H3PO4 solution was prepared as follows: 50 g of molybdenum trioxide was added into 100 ml of H3PO4 solution and stirred until completely dissolved, 32 g of basic nickel carbonate was added and stirred until completely dissolved, 45 g of lysine was added and stirred until completely dissolved, and water was added to make up to 500 ml; then it was extruded into cylindrical shape with a diameter of 1.6 mm on a front extrusion single screw extruder, the extrusion pressure was 25 MPa, dried at 120°C for 3 hours, and then calcined at 500°C for 6 hours to obtain catalyst A3. The properties of the catalyst are shown in Table 1.

[0033] Example 4

[0034] 500 g of pseudoboehmite dry gel powder (specific surface 330 m 2(gibbsite, specific surface 330 m2 / g, pore volume 1.18 ml / g, dry base content 70 wt%), 10 g of methyl cellulose (3 wt%), 10 g of myricyl alcohol (3 wt%) and 28 g of polystyrene (8 wt%) were added and mixed uniformly; 500 ml of Mo-Ni-P solution (containing MoO310 wt% and NiO 5 wt% in the catalyst) was added and kneaded, wherein the Mo-Ni-H3PO4 solution was prepared as follows: 50 g of molybdenum trioxide was added into 200 ml of H3PO4 solution and stirred until completely dissolved, 32 g of basic nickel carbonate was added and stirred until completely dissolved, 50 g of serine was added, and water was added to make up to 500 ml; then it was extruded into a trilobe shape with a diameter of 1.6 mm on a front-extrusion single-screw extruder, dried at 120°C for 3 hours, and then calcined at 850°C for 5 hours to obtain catalyst A4. The catalyst properties are shown in Table 1.

[0035] Example 5

[0036] 500 g of pseudo-boehmite dry gel powder (specific surface 330 m 2 (gibbsite, specific surface 330 m2 / g, pore volume 1.18 ml / g, dry base content 70 wt%), 10 g of methyl cellulose (3 wt%), 10 g of myricyl alcohol (3 wt%) and 28 g of polystyrene (8 wt%) were added and mixed uniformly; 500 ml of Mo-Ni-P solution (containing MoO310 wt% and NiO 5 wt% in the catalyst) was added and kneaded, wherein the Mo-Ni-H3PO4 solution was prepared as follows: 50 g of molybdenum trioxide was added into 200 ml of H3PO4 solution and stirred until completely dissolved, 32 g of basic nickel carbonate was added and stirred until completely dissolved, 50 g of serine was added, and water was added to make up to 500 ml; then it was extruded into a trilobe shape with a diameter of 1.6 mm on a front-extrusion single-screw extruder, dried at 120°C for 3 hours, and then calcined at 850°C for 5 hours to obtain catalyst A4. The catalyst properties are shown in Table 1.

[0037] Example 6

[0038] 500 g of pseudo-boehmite dry gel powder (specific surface 330 m 2 / g, pore volume 1.18 ml / g, dry base content 70 wt%), 10 g of methyl cellulose (3 wt%), 20 g of tetracosanol (6 wt%) and 10 g of polystyrene (3 wt%) were added and mixed uniformly; 500 ml of Mo-Ni-P solution (containing MoO3 10 wt%, NiO 5 wt%) was added and kneaded, wherein the Mo-Ni-H3PO4 solution was prepared as follows: 50 g of molybdenum trioxide was added into 200 ml of H3PO4 solution and stirred until completely dissolved, 32 g of basic nickel carbonate was added and stirred until completely dissolved, 15 g of lysine was added, and water was added to make up to 500 ml; then it was extruded into a cylindrical shape with a diameter of 1.6 mm on a front-extrusion single-screw extruder, the extrusion pressure was 25 MPa, 120°C drying for 3 hours, and then calcination at 800°C for 5 hours to obtain catalyst A6. The catalyst properties are shown in Table 1.

[0039] Comparative Example 1

[0040] According to the method described in Chinese patent CN106622314 A, 25 g of molybdenum trioxide and 16 g of basic nickel carbonate were added to a slurry containing silicon-containing phosphorus-containing alumina, and a filter cake and a filtrate were obtained by filtration. The filtrate was mixed with SB powder and a peptizing agent to obtain a binder, and the binder was extruded into a trilobal shape with a diameter of 1.6 mm on a front-extrusion single-screw extruder together with the filter cake, 120°C drying for 3 hours, and then calcination at 800°C for 5 hours to obtain catalyst B1. The catalyst properties are shown in Table 1.

[0041] Comparative Example 2

[0042] According to the method described in Chinese patent CN1181409 A, 500 g of pseudo-boehmite dry powder (specific surface area 330 m 2 / g, pore volume 1.18 ml / g, dry base content 70 wt%), 80 g of ammonia solution (containing 3% ammonia water) was added and kneaded for 30 min, 240 g of acetic acid aqueous solution was added and kneaded for 40 min, and then it was extruded into a cylindrical shape with a diameter of 1.6 mm on a front-extrusion single-screw extruder, 800°C calcination to prepare the carrier. 150 ml of Mo-Ni-P solution (containing MoO3 10 wt%, NiO 5 wt%) was added for impregnation, wherein the Mo-Ni-H3PO4 solution was prepared as follows: 25 g of molybdenum trioxide was added into 100 ml of H3PO4 solution and stirred until completely dissolved, 16 g of basic nickel carbonate was added and stirred until completely dissolved, and water was added to make up to 150 ml; after the impregnation was completed, the excess solution was filtered off, 120°C drying for 3 hours, and then calcination at 500°C for 4 hours to obtain catalyst B2.

[0043] Comparative Example 3

[0044] According to the method described in Chinese patent CN1417300 A, 300 g of pseudo-boehmite (specific surface area 330 m 2 / g, pore volume 1.18 ml / g, dry base content 70 wt%), 3.9 g of 65 wt% nitric acid, 3 g of sesbania powder and 120 g of deionized water were mixed uniformly, and then extruded into 1.6 mm clover-shaped strips on an extruder. After drying at 110°C, the dried shaped product was calcined at 750°C for 5 h in 100% water vapor to obtain a carrier. A Mo-Ni-P solution (containing 10 wt% MoO3 and 3.5 wt% NiO) was prepared by adding 25 g of molybdenum trioxide to 100 ml of H3PO4 solution, stirring until completely dissolved, then adding 16 g of basic nickel carbonate, stirring until completely dissolved, and then adding water to 150 ml. After impregnation, the excess solution was filtered off, dried at 120°C for 3 h, and then calcined at 500°C for 4 h to obtain catalyst B3.

[0045] Comparative Example 4

[0046] 500 g of pseudoboehmite dry gel powder (specific surface area 330 m 2 / g, pore volume 1.18 ml / g, dry base content 70 wt%), 3.5 g of methyl cellulose (1 wt%), 2 g of n-propanol (0.5 wt%) and 7 g of polystyrene (2 wt%) were added and mixed uniformly. A Mo-Ni-P solution (containing 10 wt% MoO3 and 5 wt% NiO) was prepared by adding 50 g of molybdenum trioxide to 100 ml of H3PO4 solution, stirring until completely dissolved, then adding 32 g of basic nickel carbonate, stirring until completely dissolved, then adding 15 g of arginine, stirring until completely dissolved, and then adding water to 500 ml. The mixture was then extruded into 1.4-1.6 mm clover-shaped strips on a front-extrusion single-screw extruder at an extrusion pressure of 15 MPa. The extrudates were dried at 100°C for 3 h and then calcined at 700°C for 6 h to obtain catalyst B4. The properties of the catalyst are shown in Table 1.

[0047] Table 1 Catalyst properties

[0048]

[0049] The results in Table 1 show that the specific surface area and pore volume of the catalyst prepared by the method described in the examples of the present application are both greater than those of the comparative examples, and the content of pores with a pore size of 15-20 nm and 20-30 nm is significantly higher than that of the comparative examples.

[0050] The catalysts in Table 1 were evaluated for activity and stability under the conditions shown in Table 2, and the results are shown in Table 3.

[0051] Table 2 Catalyst evaluation conditions

[0052] The catalysts in Table 1 were evaluated for activity and stability under the conditions shown in Table 2, and the results are shown in Table 3. Heavy oil properties Density (20°C) / g cm-3 1.078 Sulfur, wt% 3.6 Carbon residue, wt% 12.1 Process conditions Reaction temperature, °C 385 Hydrogen partial pressure, MPa 16 volume space velocity, h -1 ]] 0.4 Hydrogen / oil ratio 700

[0053] Table 3 Evaluation results

[0054] Catalyst A1 A2 A3 A4 A5 A6 B1 B2 B3 B4 Sulfur content, wt% 0.49 0.44 0.48 0.46 0.47 0.45 0.50 0.49 0.51 0.53 Carbon residue, wt% 5.5 5.1 5.2 5.4 5.4 5.0 5.8 5.9 5.6 6.0

[0055] Of course, the present application also has other various embodiments, and those skilled in the art can make various corresponding changes and modifications according to the present application without departing from the spirit and essence of the present application, but these corresponding changes and modifications should all belong to the protection scope of the claims of the present application.

Claims

1. A method for preparing a catalyst for heavy oil hydrodesulfurization and decarbonization, characterized in that, Includes the following steps: A catalyst is obtained by mixing a pore-expanding agent and a pore-expanding agent into macroporous pseudoboehmite, then adding an acidic metal impregnation solution, kneading, molding, drying, and calcining; the pore-expanding agent includes carbon alcohol and polystyrene. The catalyst has a pore volume of 0.60~0.95 ml / g, with pores of 15nm~20nm accounting for 40%~60% of the total pore volume and pores of 20~30nm accounting for 25%~35% of the total pore volume.

2. The preparation method of the heavy oil hydrodesulfurization and decarbonization catalyst according to claim 1, characterized in that, The carbon alcohol is octadecyl alcohol or tetradecyl alcohol.

3. The preparation method of the heavy oil hydrodesulfurization and decarbonization catalyst according to claim 1, characterized in that, The amount of carbon alcohol added is 0.5wt to 6wt% of the alumina content in the pseudoboehmite; the amount of polystyrene added is 2wt% to 8wt% of the alumina content in the pseudoboehmite.

4. The preparation method of the heavy oil hydrodesulfurization and decarbonization catalyst according to claim 1, characterized in that, The specific surface area of ​​the macroporous pseudoboehmite is ≥330 μm. 2 / g, pore volume ≥1.15ml / g.

5. The preparation method of the heavy oil hydrodesulfurization and decarbonization catalyst according to claim 1, characterized in that, The acidic metal impregnation solution includes an active metal precursor, an inorganic acid, and a complexing agent.

6. The preparation method of the heavy oil hydrodesulfurization and decarbonization catalyst according to claim 5, characterized in that, The complexing agent is an amino acid-based substance, and the amount added is 1wt%~15wt% of boehmite.

7. The preparation method of the heavy oil hydrodesulfurization and decarbonization catalyst according to claim 6, characterized in that, The complexing agent is one or more of arginine, histidine, and lysine.

8. The preparation method of the heavy oil hydrodesulfurization and decarbonization catalyst according to claim 5, characterized in that, The inorganic acid is one or more of phosphoric acid, nitric acid, and hydrochloric acid.

9. The method for preparing the heavy oil hydrodesulfurization and decarbonization catalyst according to claim 5, characterized in that, The active metal is at least one of Mo and W, and at least one of Ni and Co.

10. The method for preparing the heavy oil hydrodesulfurization and decarbonization catalyst according to claim 1, characterized in that, The extrusion aid is a cellulose-based substance, and the amount added is 1wt% to 6wt% of the alumina content in the pseudoboehmite.

11. The method for preparing the heavy oil hydrodesulfurization and decarbonization catalyst according to claim 1, characterized in that, The roasting temperature is 500~900℃, and the roasting time is 0.5~6 hours.

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