Catalyst for cracking heavy oil

Abstract: A catalyst composition for the cracking of heavy oil, which has high cracking activity for heavy components in the heavy oil and features reduced deposition of coke. The catalyst composition is comprised of a zeolite, a mixed metal oxide, clay and a metal oxide, and the total acidity of a portion of said catalyst, said portion being composed of said catalyst components other than said zeolite, is from 0.02 to 0.08 mmol/g.

Description: Cross Reference to Related Applications This application claims the priority of Japanese Patent Application No. HEI 09-173081 filed June 13. 1997. Field of the Invention This invention relates to an additive to a fluidized catalytic cracking catalyst for heavy oil. Background of the Invention A variety of methods are known for obtaining light oil by cracking heavy oil, such as fluidized catalytic cracking (FCC). A great deal of research has been conducted to achieve high yields of the desirable light oil products. It is known to add and mix a catalyst, which acts to promote cracking of heavy components in heavy oil, with a cracking catalyst to improve the yield of light oil. As such additive catalysts, those composed of alumina, clay and silica have been known to date. For example, US-A-5001097 discloses a catalyst consisting primarily and preferentially of large pore, preferably Y-type zeolite, clay and silica-alumina cogel having increasing light cycle oil yields and decreasing heavy cycle oil yields, US-A-4636484 discloses a catalyst for use in catalytic cracking obtained by spray drying an aqueous slurry containing a flash calcinated alumina, kaolin, a precursor of a siliceous matrix and a crystalline aluminosilicate zeolite, and EP-A-0083163 relates to a catalyst containing a zeolite dispersed in a matrix composition comprising a clay and a refractory metal oxide such as silica, alumina, silica-alumina, silica-magnesia, silica-alumina-magnesia, silica-titania, silica-zirconia, titania, zirconia and mixture and combination thereof. However, these additive catalysts are typically accompanied by problems, such as the cracking of heavy oil not being promoted or the formation of undesirable amounts of coke. An object of the present invention is to provide an additive catalyst for the cracking of heavy oil, which has relatively high cracking activity for heavy components in the heavy oil with reduced coke deposition. With a view to attaining the above-described object, the present inventors have proceeded with extensive research, leading to the completion of the present invention. Summary of the Invention In accordance with the present invention, there is thus provided an additive catalyst for the catalytic cracking of heavy oil, characterized in that the additive catalyst comprises a large pore zeolite, a mixed metal oxide, clay and a metal oxide, and the total acidity of a portion of said catalyst, said portion being composed of said catalyst components other than said zeolite, is from 0.02 to 0.08 mmol/g. Detailed Description of the Invention The mixed metal oxides employed as a catalyst additive component in the present invention are silica-alumina wherein the silica content is in a range of from 5 to 30 wt.%, preferably from 10 to 20 wt.%. A silica content higher than this range results in a catalyst having relatively poor hydrothermal stability, while a silica content lower than the above range leads to a catalyst having relatively low cracking activity for heavy components. Silica-aluminas suitable for use in the present invention have, as expressed in terms of physical properties in their calcined form, a specific surface area ranging from 250 to 450 m 2 /g, preferably from 300 to 400 m 2 /g, a pore volume from 0.5 to 1.5 cm 3 /g (cc/g) preferably from 0.7 to 1.2 (cm 3 /g) (cc/g). It is also preferred to use a silica-alumina having a structure wherein silica is bonded in the form of a layer on a surface of alumina as a core. The mixed metal oxides employed in the present invention generally have a specific surface area from 250 to 450 m 2 /g, with 300 to 400 m 2 /g being preferred, and an overall pore volume of from 0.5 to 1.5 cm 3 /g (cc/g), with 0.7 to 1.2 cm 3 /g (cc/g) being preferred. One having relatively large pores in a large proportion in its pore volume distribution is preferred. In the present invention, the pore volume Amo of pores having diameters from 60 to 200 10 -10 m (Å) may account for at least 65%, preferably 75 to 85% of the overall pore volume Tmo, and the pore volume Bmo of pores having diameters of from 100 to 200 10 -10 m (Å) may preferably account for at least 30% of the overall pore volume Tmo. The ratio Bmo/Amo of the pore volume Bmo to the pore volume Amo may preferably be at least [40%] 0.4 , notably [45% or higher] 0.45 or greater . In the mixed metal oxide employed in the present invention. its pore characteristics such a specific surface area and pore volume can be controlled according to conditions for the production of the mixed metal oxide. The catalyst according to the present invention can be obtained by conventional methods. For example, the catalyst can be obtained by evenly mixing the zeolite, the mixed metal oxide, the metal oxide, and the clay in an aqueous [solution] medium and then spray drying the resultant slurry. Usable examples of the zeolite can include a variety of conventionally known crystalline silicates, for example, crystalline aluminosilicate and aluminometallosilicates containing a metal in their skeleton structures (e.g., crystalline aluminogallosilicate and the like). Particularly preferred are synthetic Y-type zeolite ultrastable Y-type zeolite, ZSM-5 and β-mordenite, all of which are common in crystalline structure with faujasite. It is also preferable to use one containing hydrogen and/or a rare earth metal as cations. Illustrative of the metal oxide can be silica, alumina, magnesia, zirconia, and titania. Of these, use of silica is preferred. Examples of the clay can include kaolin, bentonite and kibushi clay. Of these, use of kaolin is preferred. In general, one containing as a primary component one or more of clay minerals such as kaolinite, dickite, nacrite, halloysite and hydrated halloysite is used. In the catalyst of the present invention, the content of the zeolite can be generally from 1 to 40 wt.%, preferably from about 10 to 30 wt.%; the content of the mixed metal oxide can be generally from 5 to 80 wt.%, preferably from about 10 to 60 wt.%; the content of the metal oxide can be generally from 10 to 40 wt.%, preferably from 15 to 35 wt.%; and the content of the clay can be generally from 10 to 80 wt.%, preferably from 20 to 70 wt.%. In the portion (i.e., matrix portion) of the catalyst according to the present invention, said portion being composed of said catalyst components other than said zeolite, that is, in the portion composed of a mixture of the mixed metal oxide, the metal oxide and the clay, the specific surface area can be from 35 to 65 m 2 /g, preferably from 40 to 60 m 2 /g, and the overall pore volume can be from 0.14 to 0.45 mℓ/g, preferably from 0.20 to 0.40 mℓ/g. Further, its pore distribution may preferably be biased toward relatively large pores. The pore volume Amp of pores having diameters of from 60 to 200 10 -10 m (Å) may account for at least 45%, preferably 50% or more of the overall pore volume Tmp, and the pore volume Bmp of pores having diameters of from 100 to 200 10 -10 m (Å) may account for at least 20%, preferably 25% or more of the overall pore volume Tmp. The ratio Bmp/Amp of the pore volume Bmp to the pore volume Amp may be at least [40%] 0.4 , preferably [50% or higher] 0.5 or greater . The pore characteristics of the portion of the catalyst according to the present invention, said portion being formed of the components other than the zeolite, can be controlled by the kind and content of the mixed metal oxide and can also be controlled by the mixing proportions of the mixed metal oxide, the metal oxide and the clay, production conditions for the catalyst. In the catalyst according to the present invention, the total acidity of the portion composed of the catalyst components other than the zeolite is specified to range from 0.02 to 0.08 mmol/g, with 0.025 to 0.07 mmol/g being preferred. This makes it possible to suppress the deposition of coke and also to obtain middle distillate at a high yield in catalytic cracking of heavy oil. This total acidity can be easily controlled by adjusting the kind, composition and/or the like of the matrix portion formed of the mixed metal oxide, the metal oxide and the clay as the catalyst components other than the zeolite. For the preferred production of the catalyst of this invention, a gel of the zeolite, the clay and the mixed metal∼oxide is added to a sol solution of the metal oxide such as a silica sol solution, and the resulting mixture is uniformly stirred to prepare a dispersion. In this case, the average particle size of the zeolite can be from 0.1 to 1 µm; the average particle size of the clay can be from 0.5 to 5 µm, with 2 to 3 µm being preferred; and the average particle size of the mixed metal oxide can be from 0.5 to 10 µm, with 3 to 7 µm being preferred. Further, the total solid concentration of the dispersion can be from 10 to 50 wt.%. with 20 to 30 wt.% being preferred. The dispersion prepared as described above is next spray dried. Its drying temperature is from 180 to 300°C, preferably from 200 to 270°C. By this spray drying, the catalyst of the present invention is obtained in the form of a powder. The average particle size of this powder ranges from 50 to 80 µm, with 55 to 70 µm being preferred. The dry product obtained as described above can be used after heating it to 300 to 700°C, preferably 400 to 600°C as needed. Moreover, this powdery catalyst can be formed, if needed, by extrusion or the like into a formed product of a granular, spherical, cylindrical, rod-like or similar shape. The catalyst according to the present invention can be used by dispersing it in the form of fine powder in heavy oil. As an alternative, it can be employed by mixing the same in a conventionally-known cracking catalyst for heavy oil. Preferably, the catalyst of the present invention can be used by mixing it in the form of powder in an FCC catalyst. An FCC catalyst is composed of a porous inorganic oxide and zeolite. Usable examples of the porous inorganic oxide can include silica-alumina, silica- zirconia, and silica-magnesia. The catalyst according to the present invention can preferably be applied to FCC catalysts, especially, those composed of zeolite, silica, alumina and kaolin. The content of the catalyst of this invention in each FCC catalyst may range from 2 to 30 parts by weight, preferably From 4 to 20 parts by weight per 100 parts by weight of the FCC catalyst. When catalytically cracking heavy oil by using such an FCC catalyst, the reaction temperature may range from 470 to 550°C, preferably from 480 to 520°C. The catalyst/oil ratio can be from 3 to 6 wt/wt, preferably from 4 to 5 wt/wt. Usable examples of the heavy oil can include various feed oils as well as their atmospheric distillation residues and vacuum distillation residues. In addition, solvent-deasphalted oil, solvent-deasphalted asphalt, shale oil, tar sand oil, liquefied coal oil and the like can also be used. It is also possible to use those available by blending vacuum gas oil (boiling point range: 343 to 600°C) in the above-described heavy oils. As the total acidity of the portion (matrix portion) of the catalyst components other than the zeolite is limited to the specific range, the catalyst according to the present invention has excellent cracking activity for heavy oil. By conducting a catalytic cracking reaction of heavy oil with the catalyst of this invention added therein, naphtha and middle distillate can be obtained in high yields. Moreover, the deposition of coke can be significantly reduced in the catalytic cracking of heavy oil, thereby achieving prolongation in the service life of a cracking catalyst. EXAMPLES The present invention will next be described in further detail by Examples. Incidentally, the specific surface area and total acidity of a catalyst are defined as follows: Specific surface area A sample (0.2 g) was maintained for I hour under the conditions of 200°C and 1,3 10 -1 Pa (1 x 10 -3 torr) and was then allowed to adsorb nitrogen gas at the liquid nitrogen temperature (77K). Using the quantity of nitrogen gas so adsorbed, the specific surface area was determined. The BET method was used for the calculation of the specific surface area. Total acidity A sample (0.5 g) was maintained for 4 hours under the conditions of 400°C and 1,3 10 -2 Pa (1x 10-4 torrr) and was then allowed to adsorb ammonia gas. Heat of adsorption produced during the adsorption was measured. A quantity of adsorbed ammonia corresponding to heat of adsorption in excess of 70 KJ/mol was defined as a total acidity. Incidentally, the measurement was performed using an "Adsorption Heat Measuring Instrument" manufactured by K.K.Tokyo Riko. Referential Example 1 (Production of SiO 2 -Al 2 O 3 ) An aqueous solution (2 N) of ammonium hydroxide was added to 7,000 g of a 3 wt.% aqueous solution of aluminum sulfate having an Al 2 O 3 concentration of 1.3 wt.% (pH 3), whereby an aqueous slurry containing aluminum hydroxide, the pH of which was 8.2, was obtained. On the other hand, 2 N sulfuric acid was added to 170 g of an aqueous solution of water glass (pH 12), which had an SiO 2 content of 5.8 wt.%, so that the pH was adjusted to 3.0 to obtain a silica sol solution. Next, the aqueous slurry of aluminum hydroxide, which had been obtained as described above, was added to and mixed with the silica sol solution under stirring. A 2 N aqueous solution of ammonium hydroxide was added to the resultant mixture to adjust its pH to 8.2. The thus-obtained mixture was next allowed to age at 25°C for 3 hours to gelatinize the silica sol contained in the mixture, thereby obtaining a gel with silica gel adhered and bonded on surfaces of aluminum hydroxide particles. The gel was separated from the solution, washed with water and then collected by filtration. The gel so obtained was used as an additive component. The SiO 2 /Al 2 O 3 weight ratio of the gel was 0.11, and its SiO 2 content was 10 wt.%. Further, a portion of dry particles, which had been obtained by drying the gel at 120°C, was calcined at 500°C for 3 hours. This calcined product had a surface area of 230 m 2 /g and a pore volume of 1.2 cm 3 /g (cc/g). Example 1 (Production of Catalyst A) 2 N sulfuric acid was added to 660 g of an aqueous solution of water glass (pH 12), which had an SiO 2 content of 15.2 wt.%, so that the pH was adjusted to 3 to obtain a silica sol solution. To 1,180 g of the silica sol solution, Y-type zeolite, kaolin and the SiO 2 -Al 2 O 3 gel obtained in Referential Example 1 were next added in the proportions shown in Table 1. Subsequent to uniform dispersion, the resulting dispersion was spray dried so that a catalyst A having an average particle size of 60 µm was obtained. As the composition of the catalyst A, it was composed of 20 wt.% zeolite, 20 wt.% silicaalumina, 40 wt.% kaolin and 20 wt.% silica. Further, its silicon content other than that contained in the kaolin was 21 wt.% in terms of SiO 2 . The total acidity of the matrix portion (i.e., the portion other than the zeolite) of the catalyst was 0.02 mmol/g. Example 2 (Production of Catalysts B to F) Catalysts B to F were produced in a similar manner as in Example 1 except that the SiO 2 content of the silica-alumina prepared in a similar manner as in Referential Example 1 and the amounts of the silica sol solution, the Y-type zeolite, the kaolin and the silica-alumina were changed in various ways. Their compositions and physical properties are presented in Table 1, along with the composition and physical properties of the catalyst A obtained in Example 1. Catalyst A B C D E F SiO 2 content on silica-alumina (wt.%) 5 10 10 15 0 40 Composition (wt.%) Zeolite 20 20 20 20 20 20 Silica-alumina 20 20 20 20 5 20 Kaolin 40 40 30 40 55 40 Silica 20 20 20 20 20 20 Matrix portion Specific surface area (m 2 /g) 35 60 75 80 20 108 Total acidity (mmol/g) 0.02 0.04 0.08 0.08 0.01 0.15 Silicon content other than kaolin (as SiO 2 ) (wt.%) 21 22 23 23 20 28 Example 3 (Production of Catalysts G to L) Example 3 (Production of Catalysts G to L) Catalysts G to L were produced in a similar manner as in Example 1 and Example 2 except that ZSM-5 type zeolite was used instead of the Y-type zeolite. Concerning these catalysts G to L, their compositions and physical properties are presented in Table 2. Catalyst G H I J K L SiO 2 content in silica-alumina (wt.%) 5 10 10 15 0 40 Composition (wt.%) Zeolite 10 10 10 10 10 10 Silica-alumina 20 20 30 20 5 20 Kaolin 50 50 40 50 65 50 Silica 20 20 20 20 20 20 Matrix portion Specific surface area (m2/g) 35 65 73 80 20 118 Total acidity (mmol/g) 0.02 0.05 0.07 0.08 0.01 0.17 Silicon content other than kaolin (as SiO 2 ) (wt.%) 21 22 23 23 20 28 Application Example 1 (Cracking of heavy oil) To conduct performance tests of the various additive catalysts obtained in Examples 1 and 2, the individual additive catalysts were uniformly mixed in portions of an FCC catalyst. Using a microactivity test (MAT) apparatus, predetermined amounts of a feed heavy oil were respectively subjected to a fluidized catalytic cracking reaction in the presence of the thus-prepared catalyst mixtures under the same conditions. The results are presented in Table 3. Using as references the results of a reaction conducted in the presence of the same FCC catalyst without addition of any additive catalyst, the values in the table were all obtained by subtracting reference values from the results of the respective reactions conducted in the presence of the catalyst compositions making use of the individual additive catalysts. Further, the performance values other than the conversions are values obtained at the same conversion. As the feed heavy oil, desulfurized vacuum gas oil (VGO) was used. Further, prior to the test, the additive catalysts were calcined at 650°C for 1 hour and were then treated at 760°C for 16 hours in a 100% steam atmosphere. The fluidized catalytic cracking conditions in the test were as follows: (1) Reaction temperature: 510°C (2) Reaction pressure: atmospheric pressure (3) Catalyst/oil ratio: 2.5 to 4.5 wt/wt (4) WHW (Weight Hourly Space Velocity: g/h of feed/g catalyst): 32 hr -1 The additive catalysts A to F were each added the corresponding portions of the FCC catalyst in a proportion of 10 parts by weight per 100 parts by weight of the FCC catalyst. The additive catalysts A to F were each added the corresponding portions of the FCC catalyst in a proportion of 10 parts by weight per 100 parts by weight of the FCC catalyst. Incidentally, the conversions, naphtha yields, bottom yields and coke yields presented in Table 3 and Table 4 are defined by the following formulas, respectively: (1) Conversion (wt.%) = (A-B) / A x 100 A: Weight of the feed oil. B: Weight of distillates contained in the produced oil and having boiling points of 221°C and higher. (2) Naphtha yield (wt.%) = C/A x 100 C: Weight of naphtha (boiling point range: C5 to 221°C) in the produced oil. (3) Bottom yield (wt.%) = D/A x 100 D: Weight of a bottom (boiling point range: 343°C and higher) in the produced oil. (4) Coke yield (wt.%) = E/A x 100 E: Weight of coke deposited on the catalyst composition. Catalyst No. A B C D E F Reaction results Conversion (wt.%) +1.8 +0.7 +1.0 +1.0 -0.3 -1.0 Naphtha yield (wt.%) +1.4 +0.7 +0.5 +0.4 ±0 -0.4 Bottom yield (wt.%) -0.5 -0.8 -1.0 -0.4 ±0 +0.5 Coke yield (wt.%) -0.3 -0.4 -0.2 -0.3 ±0 +0.5 Application Example 2 Experiments were conducted in a similar manner as in Application Example 1 except that, as the additive catalysts, those obtained in Example 3 were used. The results are presented in Table 4. Catalyst No. G H I J K L Reaction results Conversion (wt.%) +1.5 +0.5 +0.9 +0.9 -0.3 -1.5 Naphtha yield (wt.%) +1.0 +0.5 +0.4 +0.2 -0.5 -0.7 Bottom yield (wt.%) - 0.5 -0.7 -0.9 -0.4 +0.1 +0.7 Coke yield (wt.%) -0.3 -0.4 -0.2 -0.3 ±0 +0.6

Claims: A catalyst for the catalytic cracking of heavy oil, comprising a zeolite, a mixed metal oxide, clay and a metal oxide, wherein the total acidity of a portion of said catalyst composed of the said catalyst components other than said zeolite and measured by the quantity of ammonia adsorbed by 0.5 g of catalyst at 400 °C and 1.3 10-1 Pa corresponding to heat adsorption in excess of 70 KJ/mol is from 0.02 to 0.08 mmol/g and wherein the mixed metal oxide is silica-alumina containing 5 to 30 wt% of silica. The catalyst of claim 1 wherein the content of the zeolite is from 1 to 40 wt%, the content of the mixed metal oxide is from 10 to 60 wt%, the content of the metal oxide is from 10 to 40 wt%, and the content of the clay is from 20 to 70 wt%. The catalyst of claim 1 wherein the zeolite is a faujasite type zeolite selected from the group consisting of zeolite Y, ultrastable Y-type zeolites, ZSM-5, and β-mordenite. The catalyst of claim 1 wherein the metal oxide is selected from silica, alumina, magnesia, zirconia, and titania. The catalyst of claim 1 wherein the clay is selected from kaolin, bentonite and kibushi clay.

Inventors: OOTAKE NOBUO, SHIBASAKI MASATO, OOTAKE, NOBUO, SHIBASAKI, MASATO
Applicants: TONEN CORP, TONEN CORPORATION
Application year: 1998
Main classification: C10G11
IPC codes: C10G11, B01J29