More particularly, the present invention relates to a catalyst suitable for the hydroprocessing of heavy hydrocarbon oils containing a large amount of impurities such as sulfur, Conradson carbon residue (CCR), metals, and asphaltene to effect hydrodesulfurization (HDS), hydrodemetallization (HDM), asphaltene reduction (HDAsp) and/or conversion into lighter products while inhibiting the formation of sediment detrimental to the operation and/or improving the storage stability of the product produced. The present invention also relates to a process for hydroprocessing heavy hydrocarbon oils using said catalyst.

Hydrocarbon oils containing 70 wt. % or more of components boiling above 450°C, in particular hydrocarbon oils containing 50 wt. % or more of components with a boiling point of 538°C or higher, are called heavy hydrocarbon oils. These include atmospheric residue (AR) and vacuum residue (VR), which are produced in petroleum refining. It is desired to remove impurities such as sulfur from these heavy hydrocarbon oils by hydroprocessing, and/or to convert them into lighter oils, which have a higher economic value. Depending on the properties of the- feed, this is advantageously done in fixed bed or in ebullating bed operation.

Various catalysts have been proposed for this purpose in the art. Generally, these catalysts are capable of removing sulfur, Conradson carbon residue (CCR), various metals, nitrogen and/or asphaltenes. However, it was found that the decomposition of asphaltenes, which are aggregates of condensed aromatic compounds, is generally accompanied by the formation of sediment and sludge.

Sediment can be determined by the Shell hot filtration solid test (SHFST) (see Van Kerknoort et al., J. Inst. Pet., 37, 596 604 (1951)). Its ordinary content is said to be about 0.19 to 1 wt. % in product with a boiling point of 340°C or higher collected from the bottom of a flash drum.

Sediment formed during ebullating bed hydroprocessing may settle and deposit in such apparatuses as heat exchangers and reactors, and because it threatens to

close off the passage, it may seriously hamper the operation of these apparatuses.

Japanese Patent Laid-Open No. 1994-88081 discloses a hydroprocessing method for heavy hydrocarbon oils using a catalyst with a specific pore size distribution. In this method a catalyst is used with 3 to 6 wt. % of a Group Vlil metal oxide, 4.5 to 24 wt. % of a Group VIB metal oxide, and 0 to 6 wt. % of phosphorus oxides loaded onto a porous alumina carrier which has a specific surface area of 165 to 230 m2/g, a total pore volume of 0.5 to 0.8 ml/g, and a pore size distribution wherein 5% or less of the total pore volume is present in pores with a diameter less than 80 A, 65-70% of the total pore volume present in pores with a diameter below 250 A is present in a range of 20 A below the MPD to 20 A above the MPD, and 22-29% of the total pore volume is present in pores with a diameter of more than 250 A.

However, although this method can achieve efficient hydrodesulfurization and Conradson carbon reduction, it does not solve the problem of sediment formation.

Japanese Patent Laid-Open No. 1994-200261 discloses a hydroprocessing method for heavy oils, and a catalyst used to implement this method. In this reference a catalyst was proposed with 2.2 to 6 wt. % of a Group VIII metal oxide and 7 to 24 wt. % of a Group VIB metal oxide on a porous alumina carrier, which- catalyst has a surface area of 150-240 m2/g, a total pore volume of 0.7 to 0.98 ml/g, and a pore size distribution wherein less than 20% of the total pore volume is present in pores with a diameter of less than 100 A, at least 34% of the total pore volume is present in pores with a diameter of 100-200 A, and 26-46% of the total pore volume is present in pores with a diameter of more than 200 A.

However, the present inventors have found that this catalyst shows a too high sediment formation.

Japanese patent publication 2-48485 describes a process for preparing an alumina catalyst carrier which has 0.6 to 0.85 ml/g of its pore volume in pores with a diameter below 500 A and 0.1 to 0.3 ml/g of pore volume in pores with a diameter of 1,000 to 10,000 A. The pore mode in the range up to 500 A is 90-210 A. The U-value, defined as D50/ (D95-D5), is at least 0.55. The macropore volume

of this carrier is very high, making it difficult to maintain stable hydrodesulfurization activity.

US patent No. 4395329 describes a hydroprocessing catalyst for heavy oils which has a specific pore size distribution. The catalysts described in this reference have 10-25% of pore volume present in pores with a diameter above 10,000 A.

Especially when these catalysts are made by extrusion, this will detrimentally affect the strength of the catalyst and it is expected that it will be difficult to use the catalyst commercially.

As indicated above, in the improvement of ebullating bed hydroprocessing catalysts there is need for a catalyst which achieves a high level of contaminant removal, in particular metals and asphaltene removal, with low sediment formation and high conversion of the fraction boiling above 538°C.

In fixed bed operation, sediment formation is not much of a problem. However, also in fixed bed operation there is need for a catalyst which shows improved asphaltene removal and hydrodemetallization activity. Additionally, it would be attractive to have a catalyst which combines asphaltene removal with limited resin hydrogenation, because this leads to an improved storage stability of the product produced.

It has now been found that these problems can be solved by the provision of a catalyst comprising a Group VI metal and a Group VIII metal on a carrier comprising alumina, which catalyst has a specific pore size distribution, including a limited pore volume in pores with a diameter above 4,000 A, and a relatively high pore volume in pores with a diameter of 100-1,200 A.

The catalyst of the present invention shows improved metals and asphaltene removal, combined with appropriate sulfur, nitrogen, and Conradson carbon removal. The catalyst shows a significant decrease in sediment formation, which is important for ebullating bed operations. In ebullating bed operation, the catalyst shows an improved conversion, leading to the production of more valuable material boiling below 538°C. Particularly when used in fixed bed operation, the catalyst produces product with an improved storage stability. The invention also pertains to a process for hydroprocessing heavy hydrocarbon feeds with the

catalyst according to the invention, particularly in fixed bed or in ebullating bed operation.

The catalyst according to the invention comprises 7-20 wt. % of Group VI metal, calculated as trioxide, and 0.5-6 wt. % of Group Vlil metal, calculated as oxide, on a carrier comprising alumina, the catalyst having the following physical properties : a surface area of 100-180 m21g, a total pore volume of 0.55 ml/g or more, a % PV (>200 A d) of at least 50%, a % PV (>1,000 A d) of at least 5%, a % PV (100- 1,200 A d) of at least 85%, a % PV (> 4,000 A d) of 0-2%, and a % PV (> 10,000 A d) of 0-1 %.

The catalyst of the present invention comprises catalytic materials on a porous carrier. The catalytic materials present on the catalyst according to the invention comprise a Group VIB metal and a Group VIII metal of the Periodic Table of Elements applied by Chemical Abstract Services (CAS system). The Group Vlil metal used in this invention is at least one selected from nickel, cobalt, and iron.

In view of performance and economy, nickel is especially preferred. As the Group VIB metals which can be used, molybdenum, tungsten, and chromium may be mentioned, but in view of performance and economy, molybdenum is preferred.

The combination of molybdenum and nickel is particularly preferred for the catalytic materials of the catalyst according to the invention.

Based on the weight (100 wt. %) of the final catalyst including the carrier, the amounts of the respective catalytic materials are as follows.

The catalyst comprises 7-20 wt. %, preferably 8-16 wt. %, of Group VIB metal, calculated as trioxide. If less than 7 wt. % is used, the activity of the catalyst is insufficient. On the other hand, if more than 16 wt. %, in particular more than 20 wt. % is used, the catalytic performance is not improved further.

The catalyst comprises 0.5-6 wt. %, preferably 1-5 wt. %, of Group Vlil metal, calculated as oxide. If the amount is less than 0.5 wt. %, the activity of the catalyst will be too low. If more than 6 wt. % is present, the catalyst performance will not be improved further.

The carrier of the catalyst according to the invention comprises alumina.

Preferably, the carrier contains less than 5 wt. % of silica, more preferably less than 2.5 wt. % of silica, still more preferably less than 1.5 wt. %, most preferably less than 0.5 wt. %. If the silica content of the carrier is too high, the performance of the catalyst will be affected.

As the alumina carrier in this invention, a carrier consisting essentially of alumina is preferred, the wording"consisting essentially of'being intended to mean that minor amounts of other components may be present, as long as they do not influence the catalytic activity of the catalyst. However, to improve catalyst strength as well as carrier acidity, the carrier can contain at least one material selected, for example, from oxides of silicon, titanium, zirconium, boron, zinc, phosphorus, alkali metals and alkaline earth metals, zeolite, and clay minerals in a small amount of less than 5 wt. %, based on the weight of the completed catalyst, preferably less than 2.5 wt. %, more preferably less than 1.5 wt. %, still more preferably less than 0.5 wt. %.

It is important for achieving the desired objects in the hydroprocessing of a heavy hydrocarbon oil that the catalyst according to the invention meets specific requirements as to its surface area and pore size distribution.

The specific surface area of the catalyst is 100 to 180 m21g, preferably 130 to 170 m2/g. If the specific surface area is less than 100 m21g, the catalyst performance is insufficient. On the other hand, if it is above 180 m21g, it will be difficult to obtain the required pore size distribution. Additionally, a specific surface area will result in an increase in hydrogenation activity, which, in turn, will lead to an increase in sediment formation. The specific surface area is determined by nitrogen (N2) adsorption using the BET method.

The total pore volume of the catalyst as determined by mercury intrusion is at least 0.55 ml/g, preferably 0.6-0.9 ml/g. If it is less than 0.55 ml/g, the performance of the catalyst is insufficient. The determination of the total pore volume and the pore size distribution via mercury penetration is effected at a contact angle of 140° with a surface tension of 480 dynes/cm, using, for example, a mercury porosimeter Autopore 11 (trade name) produced by Micrometrics.

At least 50%, preferably 60-80%, of the catalyst pore volume is present in pores with a diameter of above 200 A. If less than 50% of the pore volume is present in this range, the catalyst's performance, especially as to asphaltene cracking, declines.

At least 5% of the total pore volume is present in pores with a diameter above 1000 A, preferably between 8 and 30%, more preferably between 8 and 25%. If less than 5% of the pore volume is present in this range, the asphaltene cracking activity decreases, which leads to increased sediment formation. If the percentage of pore volume present in pores with a diameter above 1,000 A is above 25%, particularly above 30%, the sediment formation may increase.

The catalyst according to the invention has at least 85% of its pore volume in pores with a diameter between 100 and 1,200 A. If the percentage of pore volume present in this range is less than 85%, the hydrogenation of resins increases, which leads to an increase in sediment formation. Further, since the pore volume effective for bottoms conversion decreases, a % PV (100-1,200 A d) below 85% will lead to a decrease in bottom oil conversion.

The catalyst according to the invention has 0-2% of its pore volume in pores with a diameter above 4,000 A, and 0-1% of its pore volume in pores with a diameter above 10,000 A. If the percentage of pore volume in these ranges is above the stipulated value, the catalyst strength declines to a commercially unacceptable value. Additionally, the desulfurization activity would decline to an unacceptable level.

It is preferred for the catalyst according to the invention to have less than 15%, more preferably less than 10%, of pore volume present in pores with a diameter below 100 A. If the precentage of pore volume in this range is above 15%, the hydrogenation of non-asphaltenic compounds increases, leading to an increase in sediment formation.

The catalyst particles may have the shapes and dimensions common to the art.

Thus, the particles may be spherical, cylindrical, or polylobal and their diameter may range from 0.5 to 10 mm. Particles with a diameter of 0.5-3 mm, preferably 0.7-1.2 mm, for example 0.9-1 mm, and a length of 2-10 mm, for example 2.5-4.5 mm, are preferred. For use in fixed bed operation polylobal particles are

preferred, because they lead to a reduced pressure drop in hydrodemetallization operations. Cylindrical particles are preferred for use in ebullating bed operations.

The carrier to be used in the catalyst according to the invention can be prepared by processes known in the art. A typical production method for a carrier comprising alumina is coprecipitation of sodium aluminate and aluminium sulfate.

The resulting pseudoboehmite gel is dried,. extruded, and calcined, to obtain an alumina carrier. A particular method of producing the carrier is described below.

At first, a tank containing tap water or warm water is charged with an alkali solution of sodium aluminate, aluminium hydroxide or sodium hydroxide, etc., and an acidic aluminium solution of aluminium sulfate or aluminium nitrate, etc. is added for mixing. The hydrogen ion concentration (pH) of the mixed solution changes with the progression of the reaction. It is preferable that when the addition of the acidic aluminium solution is completed, the pH is 7 to 9, and that during mixing, the temperature is 60 to 75°C.

Then, the obtained alumina hydrate gel is separated from the solution and washed using an industrially widely used method, for example, using tap water or warm water, to remove the impurities in the gel. Then, the gel is shaped into particles in a manner known in the art, e. g., by way of extrusion, beading or pelletising.

Finally, the shaped particles are dried and calcined. The drying condition is room temperature to 200°C, generally in the presence of air, and the calcining condition is 300 to 950°C, preferably 600 to 900°C, generally in the presence of air, for a period of 30 minutes to six hours.

By the above production method, it is possible to obtain a carrier having properties which will give a catalyst with the surface area, pore volume, and pore size distribution characteristics specified above. The surface area, pore volume, and pore size distribution characteristics can be adjusted in a manner know to the skilled person, for example by the addition during the mixing or shaping step of an acid, such as nitric acid, acetic acid or formic acid, or other compounds as moulding auxiliary, or by regulating the water content of the alumina gel by adding or removing water.

It is preferred that the specific surface area of the alumina carrier before it is loaded with metal components is 100 to 180 m2/g, preferably 130 to 170 m2/g.

Furthermore, it is preferred that the total pore volume is 0.55 ml/g or more, more preferably 0. 6 to 0. 9 ml/g.

The Group VIB metal components and Group VIII metal components can be incorporated into the catalyst carrier in. a conventional manner, e. g., by impregnation and/or by incorporation into the support material before it is shaped into particles. At this point in time it is considered preferred to first prepare the carrier and incorporate the catalytic materials into the carrier after it has been dried and calcined. The metal components can be incorporated into the catalyst composition in the form of suitable precursors. For the Group VIB metals, ammonium heptamolybdate, ammonium dimolybdate, and ammonium tungstenate may be mentioned as suitable precursors. Other compounds, such as oxides, hydroxides, carbonates, nitrates, chlorides, and organic acid salts, may also be used. For the Group Vlil metals, suitable precursors include oxides, hydroxides, carbonates, nitrates, chlorides, and organic acid salts. Carbonates and nitrates are particularly suitable. The impregnation solution, if applied, may contain other compounds the use of which is known in the art, such as organic acids, e. g., citric acid, ammonia water, hydrogen peroxide water, gluconic acid, tartaric acid, malic acid or EDTA (ethylenediamine tetraacetic acid). It will be clear to the skilled person that there is a wide range of variations on this method. Thus, it is possible to apply a plurality of impregnating steps, the impregnating solutions to be used containing one or more of the component precursors that are to be deposited, or a portion thereof. Instead of impregnating techniques, dipping methods, spraying methods, etc. can be used. In the case of multiple impregnation, dipping, etc., drying and/or calcining may be carried out in between.

After the active metals have been incorporated into the catalyst composition, it is optionally dried, e. g., in air flow for about 0.5 to 16 hours at a temperature between room temperature and 200°C, and subsequently calcined, generally in air, for about 1 to 6 hours, preferably 1-3 hours at 200-800°C, preferably 450- 600°C. The drying is done to physically remove the deposited water. The

calcining is done to bring at least part, preferably all, of the metal component precursors to the oxide form.

It may be desirable to convert the catalyst, i. e., the Group VIB and Group VIII metal components present therein, into the sulfidic form prior to its use in the hydroprocessing of hydrocarbon feedstocks. This can be done in an otherwise conventional manner, e. g., by contacting the catalyst in the reactor at increasing temperature with hydrogen and a sulfur-containing feedstock, or with a mixture of hydrogen and hydrogen sulfide. Ex situ presulfiding is also possible.

The catalyst of the present invention is particularly suitable for the hydroprocessing of heavy hydrocarbon feeds. The catalyst is particularly suitable for ebullating bed hydrotreating of heavy feedstocks of which at least 50 wt. % boils above 538°C (1,000°F) and which comprise at least 2 wt. % of sulfur and at least 5 wt. % of Conradson carbon. The sulfur content of the feedstock may be above 3 wt. %. Its Conradson carbon content may be above 8 wt. %. The feedstock may contain contaminant metals, such as nickel and vanadium.

Typically, these metals are present in an amount of at least 20 wtppm, calculated on the total of Ni and V, more particularly in an amount of at least 30 wtppm. The catalyst is also particularly suitable for fixed bed hydrotreating of heavy hydrocarbon feeds with such a boiling range that at least 70% by volume will boil above 450°C. The initial boiling point will generally be 300°C, frequently 350°C.

The sulfur content of such feed generally is above 0.1 wt. % and will frequently be more than 1 wt. %. The nitrogen content generally is above 500 ppm and will frequently be in the range of 500 to 4,000 ppm. The feedstock contains contaminant metals such as vanadium, nickel, and iron, generally in amounts above 3 ppm, frequently in the range of 30 to 3,500 ppm, and more frequently in the range of 100-1,000 ppm, calculated as metal.

Suitable feedstocks. include atmospheric residue, vacuum residue, residues blended with gas oils, particularly vacuum gas oils, crudes, shale oils, tar sand oils, solvent deasphalted oil, coal liquefied oil, etc. Typically they are atmospheric residue (AR), vacuum residue (VR), and mixtures thereof.

The process of this invention can be carried out in a fixed bed, in a moving bed, or in an ebullated bed. As indicated earlier, the catalyst of the present invention is particularly suitable for fixed bed and ebullating bed operations. The process conditions for the process according to the invention may be as follows. The temperature generally is 350-450°C, preferably 400-440°C. The pressure generally is 5-25 MPA, preferably 14-19 MPA. The liquid hourly space velocity generally is 0.1-3 h-1, preferably 0.3-2 h-1.. The hydrogen to feed ratio generally is 300-1,500 NI/l, preferably 600-1,000 NI/l. The process is carried out in the liquid phase.

The invention will be elucidated below by way of the following examples, though it must not be deemed not limited thereto or thereby.

Example 1 (A) Carrier preparation A sodium aluminate solution and an aluminium sulfate solution were simultaneously added dropwise to a tank containing tap water, mixed at pH 8.5 at 65°C, and held for 70 minutes. The thus produced aluminate hydrate gel was separated from the solution and washed with warm water, to remove the impurities in the gel. Then, the gel was kneaded for about 20 minutes and extruded as cylindrical particles having a diameter of 0.9 to 1 mm and a length of 3.5 mm. The extruded alumina particles were calcined at 900°C for 2 hours, to obtain an alumina carrier.

(B) Catalyst preparation 100 g of the alumina carrier obtained in A were immersed in 100 mi of a citric acid solution containing 16.4 g of ammonium molybdat tetrahydrate and 9.8 g of nickel nitrate hexahydrate at 25°C for 45 minutes, to obtain a carrier loaded with metallic components.

Subsequently the loaded carrier was dried at 120°C for 30 minutes and calcined at 600°C for 1.5 hours, to complete a catalyst. The amounts of the respective components in the produced catalyst and the properties of the catalyst are shown in Table 2.

Comparative Example 1 (A) Carrier preparation Example 1 was repeated, except that water glass (sodium silicate) was mixed into the alumina hydrate gel as a silica source. The silica content in the obtained carrier was 7 wt. %.

(B) Catalyst preparation A catalyst was prepared from the silica-containing alumina carrier as described in Example 1. The amounts of the respective components in the produced catalyst and the properties of the catalyst are shown in Table 2.

Comparative Example 2 (A) Carrier preparation Aluminium sulfate and a sodium aluminate solution were simultaneously added dropwise to a tank containing tap water at pH 7.5 and mixed at 70°C, while further sodium aluminate was added until the final pH became 9.5, after which the mixture was held for 70 minutes. The obtained alumina gel was extruded and calcined as described in Example 1, to obtain alumina particles.

(B) Catalyst preparation A catalyst was prepared from the alumina carrier as described in Example 1. The amounts of the respective components in the produced catalyst and the properties of the catalyst are shown in Table 2.

Comparative Example 3 (A) Carrier preparation Aluminium sulfate was added to a tank containing tap water, and aluminium sulfate and a sodium aluminate solution were simultaneously added dropwise, mixed at 65°C for about 60 minutes to obtain an alumina gel, and held for 70 minutes. The gel was processed further as described in Example 1 to obtain alumina particles.

(B) Catalyst preparation In this comparative example, 13.4 g of ammonium molybdat tetrahydrate and 11.2 g of nickel nitrate hexahydrate were added to and dissolved in 50 ml of ammonia water, and 100 g of the alumina carrier were immersed in 100 ml of the solution at 25°C for 45 minutes, to obtain a carrier loaded with metallic

components. Then, the loaded carrier was ui-ied at 120°C for 30 minutes and calcined at 600°C for 1.5 hours in a kiln, to complete a catalyst. The amounts of the respective components in the obtained catalyst and the properties of the catalyst are shown in Table 2.

Comparative Example 4 (A) Carrier preparation A carrier with large pores was produced as follows : The carrier obtained in Comparative Example 2 (A) was ground and kneaded again with the alumina gel of Comparative Example 2 (A), and-the mixture was extruded and calcined as described for Example 1, to obtain a catalyst carrier having a desired pore size distribution.

(B) Catalyst preparation A catalyst was prepared from the alumina carrier as described in Example 1. The amounts of the respective components in the produced catalyst and the properties of the catalyst are shown in Table 2.

The catalysts of Example 1 and Comparative Examples 1 through 4 were tested in the hydroprocessing of a heavy hydrocarbon feedstock. The feedstock used in these examples was a Middle East petroleum consisting of 50 wt. % of atmospheric residue (AR) and 50 wt. % of vacuum residue (VR) obtained by fractionating a Middle East (Kuwait) oil. The composition and properties of the feed are given in Table 1.

Table 1: Feedstock composition Middle East petroleum (VR: AR = 50 : 50)

Sulfur (wt. %) 4.79 Nitrogen (wppm) 2,890 Metals-vanadium (wppm) 85 Metals-nickel (wppm) 26 Conradson Carbon residue (wt. %) 16.2 C7-insolubles' (wt. %) 6.0 Vacuum residue (wt. %) 75 Density (g/ml at 15°C) 1.0048 'Matter insoluble in n-heptane 2 Fraction boiling above 538°C in accordance with ASTM D 5307 (distillation gas chromatography) The catalyst to be tested was packed into a fixed bed reactor. The feedstock was introduced into the unit in the liquid phase at a liquid hourly space velocity of 1.5 h-1, a pressure of 16.0 MPa, an average temperature of 427°C, with the ratio of supplied hydrogen to feedstock (H2/oil) being kept at 800 NI/l.

The oil product produced by this process was collected and analysed to calculate the amounts of sulfur (S), metals (vanadium + nickel) (M), and asphaltene (Asp) removed by the process, as well as the 538°C+fraction. The relative volume activity values were obtained from the following formulae.

RVA = 100 * k (tested catalyst)/k (Comparative Catalyst 1) wherein for HDS k = (LHSV/ (0. 7)) * (1/y°v-1/x°v) and for HDM, asphaltene removal, and 538°C+ cracking rate k = LHSV * In (x/y) with x being the content of S, M, or Asp in the feedstock, and y being the content of S, M, or Asp in the product.

The composition and properties of the catalysis and the test results are given in Table2 below: Table 2 Example 1 Comp. Comp. Comp. Comp. Example 1 Example 2 Example 3 Example 4 Catalyst composition Mo03 (wt. %) 11.9 11.4 11.8 9.7 11. 3 NiO (wt. %) 2.0 2. 1 2. 1 2. 4 2.2 silica (wt. %) 0 5. 0 0 0 0 alumina balance balance balance balance balance Impregnation via citric acid citric acid citric acid ammonia citric acid surface area (m/g) 147 195 173 162 133 Total pore volume (ml/g) 0.79 0.76 0.72 0.77 0.82 % PV (>200 Å d) 74 38 36 65 30 % PV (>1000 d) 11 9 12 2 14 % PV (100-1200 Å d) 90 79 89 99 91 % PV (>4000 A d) 0.2 0. 2 3. 5 0. 5 6.8 % PV (>10. 000 A d) 0.0 0. 0 0. 5 0. 0 4.0 Test results at LHSV = 1.5 h-1 and reaction temperature of427°C RVA H DS 87 100 94 90 42 RVA HDM 124 100 92 90 106 RVAAsp 120-100 117 102 99 Cracking rate 538°C+ 39 41 40 40 36 fraction (residue) Sediment 0. 06 0. 29 0. 26 0. 25 0. 15 'Sediment determined in accordance with the IP 375 method of the Institute of Petroleum As shown in Table 2, Example 1 achieves a desired decrease in sediment formation as compared to Comparative Example 1, while maintaining high demetallization and asphaltene removal activity. On the other hand, Comparative Examples 2 and 3 do not achieve a sufficient decrease in sediment formation.

Comparative Example 4 shows a lower residue cracking rate and hydrodesulfurization performance.

The influence of the vacuum residue cracking rate on the sediment formation for the catalysts of Example 1 and comparative Examples 1-4 was studied by changing the space velocity. Figure 1 shows the relation between the vacuum residue conversion rate and the sediment formation of the various catalysts (4 samples of each catalyst). As can be seen from Figure 1, the catalyst according to the invention of Example 1 shows lower sediment formation at all conversion

levels than the comparative catalysts. Auuoionally, the increase in sediment formation with increasing conversion is also lower for the catalyst of Example 1 than for the comparative catalysts.

In summary, as can be seen from Table 2 and Figure 1, compared with the performance of the catalysts of Comparative Examples 1 through 4, the catalyst according to the invention prepared in Example 1 shows a high demetallization performance and a high asphaltene cracking performance in combination with a decrease in sediment formation even under high vacuum residue cracking rate conditions.