JP2003105345A - Method for fluid catalytic cracking of heavy hydrocarbon oil - Google Patents

Abstract

PROBLEM TO BE SOLVED: To provide a method for fluid catalytic cracking of heavy hydrocarbon oil, which has slight reduction of cracking reaction activity of catalyst and has high yield of gasoline and kerosene fractions even if large amounts of nickel and vanadium are deposited on a catalyst in fluid catalytic cracking of a heavy hydrocarbon oil such as normal-pressure residual oil, a reduced- pressure residual oil, etc. SOLUTION: This method for fluid catalytic cracking of heavy hydrocarbon oil comprises subjecting heavy hydrocarbon oil containing nickel and vanadium in the weight ratio of nickel to vanadium of >=1.0 to fluid catalytic cracking in the presence of a catalytic composition for fluid catalytic cracking consisting of faujasite type zeolite having the weight ratio of nickel to vanadium deposited on the catalyst of >=1.0 and a unit lattice constant in the range of 24.25-24.40 Åand an inorganic oxide matrix.

Description

Detailed Description of the Invention

[0001]

BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a fluid catalytic cracking method for heavy hydrocarbon oils, and more specifically, it contains nickel (Ni) and vanadium (V) and contains nickel (Ni) and vanadium (V). ) And the weight ratio (Ni /
By fluid catalytically cracking a feedstock oil having V) of 1.0 or more in the presence of a specific catalyst composition for fluid catalytic cracking, a decrease in activity of the catalyst is small, and consumption of the catalyst is small. TECHNICAL FIELD The present invention relates to a fluid catalytic cracking method for a small amount of heavy hydrocarbon oil.

[0002]

BACKGROUND OF THE INVENTION Generally, fluid catalytic cracking (flui) of hydrocarbon oils is used.
d catalytic cracking: sometimes abbreviated as FCC hereinafter. ) The process follows the flow of the catalyst to bring the raw hydrocarbon oil into contact with the catalyst in the riser to carry out a cracking reaction,
The decomposition product and the catalyst are separated in the reaction tower, the separated catalyst (spent catalyst) is stripped by steam, and then transferred to the regeneration tower, where the coke on the catalyst is burned to regenerate the catalyst. Then, the regenerated catalyst (equilibrium catalyst) is transferred to the riser. Then, in order to maintain the decomposition reaction activity of the catalyst at a constant level, a certain amount of new catalyst (fresh catalyst) is charged into the regeneration tower and a certain amount of equilibrium catalyst is extracted.

The fluid catalytic cracking of hydrocarbon oils is originally intended for the production of gasoline, and the catalyst used therein must have high cracking activity and high gasoline selectivity. Further, it is required that the yield of kerosene oil fraction is high. In recent years, the catalytic cracking of hydrocarbon oils has reduced the demand for heavy oils and the demand for gasoline and kerosene has increased. cracking: Below, R
It may be abbreviated as FCC. ) Is increasing. The RFC
The feedstock oil used for C contains a large amount of heavy metals such as nickel and vanadium, Conradson carbon, and polymer compounds mainly composed of polycyclic aromatic compounds called resin and asphaltene. In the catalytic cracking of oil, it is known that heavy metals are deposited on the catalyst and adversely affect the cracking activity of the catalyst and the selectivity of gasoline.

In particular, vanadium deposited on the catalyst is known to destroy the crystal structure of zeolite, which is the active component of the catalyst, and significantly reduce the decomposition activity (eg,
Masuda et al., Journal of Japan Petroleum Institute, 26 , 19 (1983)). The crystal structure destruction of zeolite by vanadium mainly occurs in the regeneration tower, but the mechanism of crystal structure destruction is as follows.
Various theories have been proposed. For example, the theory that a low melting point eutectic is formed by the interaction between vanadium pentoxide and zeolite, or vanadium pentoxide reacts with water vapor in the regeneration tower to become vanadic acid and destroys the crystal structure of zeolite. There is such a theory. It is also said that vanadium having a valence of 5 or less does not cause destruction of the zeolite crystal structure.

Further, nickel deposited on the catalyst has a small effect on the reduction of the cracking activity of the catalyst for fluid catalytic cracking, but the dehydrogenation reaction by nickel causes a marked increase in the production rate of coke and hydrogen, thereby improving the gasoline selectivity. There is a problem of lowering. In order to solve the above problems, various compounds that inactivate heavy metals such as nickel and vanadium deposited on the catalyst are contained in the catalyst as a metal scavenger, and various catalysts having improved metal resistance are available. It has been proposed (for example, JP-A-3-293037). Catalysts containing these metal scavengers have a tentative effect in catalytic cracking of vacuum gas oil (VGO) having a low nickel or vanadium content. However, in RFCC for catalytically cracking heavy residual oil containing a large amount of nickel or vanadium, there is a problem that the amount of nickel or vanadium deposited on the catalyst is large and the effect is lost and the catalyst is deactivated.

Further, in the above-mentioned RFCC process, in order to maintain the decomposition reaction activity of the catalyst and the like at a constant level, the fresh catalyst is charged and the equilibrium catalyst is withdrawn, but nickel and vanadium are allowed in the equilibrium catalyst. Since the deposited amount is small, it is necessary to increase the amount of the fresh catalyst to be charged, which increases the consumption of the catalyst and raises the cost.

[0007]

DISCLOSURE OF THE INVENTION The present invention is directed to fluid catalytic cracking of heavy hydrocarbon oils such as atmospheric residue oil and vacuum residue oil, even if a large amount of nickel and vanadium are deposited on the catalyst. It is an object of the present invention to provide a fluid catalytic cracking method for heavy hydrocarbon oils, in which the cracking reaction activity is less likely to decrease and the yield of gasoline or kerosene gas oil fraction is high.

Another object of the present invention is to provide a method for fluidized catalytic cracking of heavy hydrocarbon oil, which consumes less fresh catalyst in the above RFCC process.

[0009]

In order to solve the above problems, the present inventors have examined the effect of nickel and vanadium deposited on the catalyst on the decomposition reaction activity of the catalyst, and as a result, nickel ( Ni) and vanadium (V), and a specific fluid catalytic cracking of a heavy hydrocarbon oil containing nickel (Ni) and vanadium (V) in a weight ratio (Ni / V) of 1.0 or more. When fluid catalytic cracking is carried out in the presence of a catalyst composition for use in the catalyst, the decomposition reaction activity of the catalyst is not significantly reduced even if the amount of nickel and vanadium deposited on the catalyst is large, and furthermore, the production of hydrogen and coke is suppressed. The present invention has been completed by finding out that.

That is, according to the first aspect of the present invention,
Nickel deposited with heavy hydrocarbon oil containing nickel (Ni) and vanadium (V) and having a weight ratio (Ni / V) of nickel (Ni) and vanadium (V) of 1.0 or more The weight ratio (Ni / V) of (Ni) to vanadium (V) is 1.0 or more, and the unit cell constant is 2
Fluidization of heavy hydrocarbon oil that undergoes fluid catalytic cracking in the presence of a fluid catalytic cracking catalyst composition containing a faujasite-type zeolite and an inorganic oxide matrix in the range of 4.25 to 24.40Å A catalytic cracking method is provided.

According to the second aspect of the present invention, the first aspect
In the invention, the weight ratio of nickel (Ni) and vanadium (V) contained in the heavy hydrocarbon oil (Ni /
A method for fluidized catalytic cracking of heavy hydrocarbon oil having V) in the range of 1.1 to 40 is provided. According to a third invention of the present invention, in the first or second invention, heavy carbonization in which vanadium (V) contained in the heavy hydrocarbon oil is in the range of 1 to 50 ppm by weight. A method for fluid catalytic cracking of hydrogen oil is provided.

Further, according to a fourth aspect of the present invention, in any one of the first to third aspects, the fluid catalytic cracking catalyst composition contains vanadium (V) in an amount of 100 wtpp.
A method for fluid catalytic cracking of a heavy hydrocarbon oil containing m or more is provided. According to a fifth aspect of the present invention, in any one of the first to fourth aspects, the fluid catalytic cracking catalyst composition has an average particle size of 50 to 100 μm and a specific surface area (SA). Is 70 m ² / g or more, the pore volume (PV) is 0.10 ml / g or more, and the pore volume (pv) occupied by pores with a pore diameter (PD) in the range of 500 to 2000Å is pores. 40% or more of the volume (PV),
And the abrasion resistance (Attr. Res.) Is 0.3% by weight.
A method for fluid catalytic cracking of a heavy hydrocarbon oil having a pressure of less than / hr is provided.

According to a sixth aspect of the present invention, the first aspect
To the fifth invention, the fluid catalytic cracking catalyst composition is faujasite-type zeolite 5 to 5
A fluid catalytic cracking process for heavy hydrocarbon oils is provided that comprises 0 wt%, 1 to 30 wt% metal scavenger, and 20 to 94 wt% inorganic oxide matrix.

[0014]

BEST MODE FOR CARRYING OUT THE INVENTION Preferred embodiments of the present invention will be described in detail below. The fluid catalytic cracking method for heavy hydrocarbon oil of the present invention contains nickel (Ni) and vanadium (V), and has a weight ratio (Ni / V) of nickel (Ni) and vanadium (V) of 1 Heavy hydrocarbon oils of 0.0 or more are used as feedstock oils. In catalytic cracking of hydrocarbon oil in FCC equipment, almost all heavy metals such as nickel and vanadium contained in heavy hydrocarbon oil are deposited on the catalyst used by circulating between the reaction tower and the regeneration tower. However, when the weight ratio (Ni / V) of nickel and vanadium contained in the heavy hydrocarbon oil is less than 1.0, the weight of nickel and vanadium deposited on the catalyst. Since the ratio (Ni / V) is also smaller than 1.0, the desired effect cannot be obtained. By using a heavy hydrocarbon oil having a weight ratio (Ni / V) of nickel (Ni) and vanadium (V) of 1.0 or more as the feedstock oil, the catalytic activity of vanadium deposited on the catalyst can be reduced. The adverse effect is suppressed, and the reduction rate of the decomposition reaction activity of the catalyst is reduced.

The weight ratio (Ni / V) of nickel and vanadium contained in the heavy hydrocarbon oil is preferably 1.
It is desirable that it is 1 or more, more preferably 1.3 or more, and further preferably in the range of 1.5 to 40. The amount of vanadium contained in the above heavy hydrocarbon oil is 1 to 5
It is preferably in the range of 0 ppm by weight. The method of the present invention is effective even when the vanadium content is less than 1 weight ppm, but when the content is less than 1 weight ppm, the amount of vanadium deposited on the catalyst is also small, and thus the catalyst is decomposed. The effect is small because the degree of influence on the reaction activity is small. If the vanadium content exceeds 50 ppm by weight, the amount of nickel and vanadium deposited on the catalyst will increase in a short period of time, and the amount of fresh catalyst used will increase to maintain the decomposition reaction activity of the catalyst at a certain level. May be. The vanadium content contained in the heavy hydrocarbon oil is preferably 2 to 30 weight pp.
The range is m.

As the heavy hydrocarbon oil used in the present invention, there are usually used heavy gas oil, vacuum gas oil, deasphalted oil, pyrolysis oil, heavy residue oil and the like which are used as a feedstock for the FCC process. It is possible. In particular, heavy residue oil such as atmospheric residual oil containing vanadium and nickel and impurities, desulfurized atmospheric residual oil, reduced pressure residual oil, desulfurized reduced pressure residual oil or mixed oil of these residual oils and reduced pressure gas oil. Is preferably used.

The catalytic composition for catalytic cracking used in the present invention is a catalyst that is used by circulating it between a reaction column and a regeneration column in catalytic cracking of hydrocarbon oil in an FCC unit, that is, an equilibrium catalyst composition. is there. The catalyst composition is constituted by containing a faujasite-type zeolite having a unit cell constant of 24.25 to 24.40Å and an inorganic oxide matrix. When the unit lattice constant is smaller than 24.25Å, the number of aluminum atoms in the zeolite skeleton becomes very small, and the solid acid amount of the zeolite becomes small, so that the decomposition reaction activity of the catalyst may decrease. If the lattice constant is larger than 24.40Å, the hydrothermal stability of the zeolite may be lowered, and the zeolite crystals may be collapsed to lower the decomposition reaction activity. The unit cell constant is preferably 24.27 to 24.35Å
It is desirable to be in the range of.

Further, the catalyst composition contains nickel (Ni) and vanadium (V) deposited on the catalyst in a Ni / V weight ratio of 1.0 or more. When the Ni / V weight ratio in the catalyst is 1.0 or more, the adverse effect of vanadium on the catalytic activity is suppressed, and the reduction rate of the decomposition reaction activity of the catalyst becomes small. The Ni / V weight ratio is preferably 1.1 or more, more preferably 1.3 or more, and further preferably 1.
It is preferably in the range of 5-40. The amount of vanadium contained in the catalyst is preferably 100 ppm by weight or more. Even if the amount of vanadium contained in the catalyst is less than 100 ppm by weight, the effect of the present invention is obtained, but the effect of the present invention becomes remarkable when the amount of vanadium is 100 ppm by weight or more. The content of vanadium contained in the catalyst is preferably 500 to 150.
It is in the range of 00 ppm by weight, and the content of nickel is 5
It is preferably in the range of 0 to 20000 ppm by weight.

The average particle size of the above catalyst composition may be the same as that commonly used in fluid catalytic cracking, and is 50 to 50.
It is preferably in the range of 100 μm. The specific surface area (SA) is in the range of 70 to 250 m ² / g, and the pore volume (PV) is 0.10 ml / g or more, more preferably 0.15 to 0.35 ml / g. It is desirable that the pore volume (pv) occupied by the pores having a pore diameter (PD) in the range of 500 to 2000Å is 40% or more, preferably 50% or more of the pore volume (PV).

When the specific surface area (SA) of the catalyst is less than 70 m ² / g and the pore volume (PV) is less than 0.10 ml / g, the desired decomposition reaction activity may not be obtained. Further, in the catalytic cracking of hydrocarbon oil, especially heavy residual oil, the pores of the catalyst have a pore diameter of 50 from the reaction surface.
It is preferable that the particle diameter is larger than 0 Å because the diffusivity of the reactant is improved, but the pore diameter larger than 2000 Å may deteriorate the wear resistance of the catalyst, and therefore it is preferably smaller. The pore volume (PV) is a value measured by the mercury porosimetry method. Furthermore, the wear resistance of the catalyst (Att
r. Res. ) Is preferably 0.3% by weight / hr or less (according to the UOP method).

Further, the catalyst composition of the present invention comprises 5 to 50% by weight of the faujasite type zeolite, 1 to 30% by weight of the metal scavenger, and 20 to 20% of the inorganic oxide matrix.
It is preferably constituted by containing 94% by weight. The inorganic oxide matrix of the present invention includes silica, silica-alumina, alumina, silica-magnesia, alumina-magnesia, silica-magnesia-alumina, and other conventional catalytic cracking catalysts that act as binders. A matrix component is used. Such matrix components also include clay minerals such as kaolin and halloysite. As the metal scavenger, a metal scavenger generally used for catalytic cracking catalysts can be used, and specifically, alumina particles, phosphorus-alumina particles, crystalline calcium aluminate, sepiolite, barium titanate, Examples include calcium stannate, strontium titanate, rare earth oxides, manganese oxide, magnesia, magnesia-alumina and the like.

The reaction conditions and the like in the catalytic cracking method of the present invention may be the reaction conditions and regeneration conditions adopted in the ordinary FCC process, and the combined use of a nickel passivating agent and the like is preferable. The preferable range of the reaction temperature for catalytically cracking the hydrocarbon oil is 450 to 600 ° C, more preferably 470 to 550 ° C. When the reaction temperature is lower than 450 ° C, the heavy residual oil may not be sufficiently decomposed because the reaction temperature is too low, and when the reaction temperature is higher than 600 ° C, overcracking may occur and the amount of gas and coke produced. It is not preferable because it may increase and the yield of gasoline may be significantly reduced.

The reaction pressure for catalytically cracking hydrocarbon oil is generally in the range of atmospheric pressure to 5 kg / cm ² , more preferably about 1 to 3 kg / cm ² , A preferred range of oil weight ratio is about 2-20, more preferably about 3-15, and a preferred range of contact time is
It is about 0.1 to 10 seconds, more preferably about 0.3 to 6 seconds.

The catalyst used for the catalytic cracking reaction of hydrocarbon oil is separated from the cracked products by a conventional method, and the separated spent catalyst is stripped with steam or the like and then regenerated by burning coke. . Catalyst regeneration is generally
Firing is performed in the presence of steam at a temperature range of about 600 to 850 ° C, more preferably about 650 to 800 ° C. In the catalytic cracking method of the present invention, since the heavy hydrocarbon oil containing nickel and vanadium and having the Ni / V atomic ratio of 1.0 or more is used as the feedstock oil, nickel contained in the catalyst is used. And vanadium have a weight ratio (Ni / V) of 1.
When the amount is 0 or more, even if a large amount of vanadium or nickel is deposited on the catalyst, the decomposition reaction activity of the catalyst is not significantly decreased, and the production of hydrogen and coke is suppressed. The reason for this is not clear, but when the weight ratio (Ni / V) of nickel and vanadium deposited on the catalyst is 1.0 or more, nickel and vanadium interact with each other under regeneration conditions of the catalyst. It is estimated that vanadium does not destroy the zeolite crystal structure and the dehydrogenation reaction by nickel is suppressed.

[0025]

The present invention will be described below with reference to examples.
The present invention is not limited to this.

[0026]

[Reference Example 1] A commercially available FCC catalyst (trade name: DCT, manufactured by Catalyst Kasei Kogyo Co., Ltd.) having the properties shown in Table 1 was calcined at 600 ° C. for 2 hours, and then nickel (Ni) 4000 wt.
pm and 4000 ppm by weight of vanadium (V) were measured by the Mitchell method (Ind. Eng. Ch.
em. , Prod. Res. Dev. , 19 , 209
(1980)). That is, the catalyst was impregnated with a toluene solution of nickel naphthenate and vanadium naphthenate, and then toluene was evaporated to obtain 50
Steam for 0.5 hours at 0 ° C, then 600 in air
It was baked at 1 ° C for 1 hour. Further, in order to make the catalyst performance equal to that of the equilibrium catalyst, the catalyst was steamed at 780 ° C. for 13 hours and calcined again at 600 ° C. for 1 hour to obtain a pseudo equilibrium catalyst A. Table 1 shows the properties of the pseudo-equilibrium catalyst A.

In the same manner as in the above method, 2000 wt ppm of nickel (Ni) and vanadium (V) 4 were added to the above catalyst.
A quasi-equilibrium catalyst B supporting 000 ppm by weight was prepared.
Table 1 shows the properties of the pseudo-equilibrium catalyst B.

[0028]

Example 1 and Comparative Example 1 Using the pseudo-equilibrium catalysts A and B prepared in Reference Example 1, the following raw material oils were used, and an ASTM MAT activity evaluation test was conducted under the following reaction conditions. Feedstock: Desulfurization atmospheric pressure residual oil 60% by volume + Desulfurization vacuum gas oil 40% by volume Specific gravity: 0.917 15/4 ° C. Sulfur: 0.37 wt% Ni: 4.7 wtppm V: 3.9 wtppm Ni / V: 1.2 Weight ratio Reaction conditions Reaction temperature: 515 ° C. Space velocity: 40 hr ⁻¹ Catalyst / oil ratio: 3 (weight ratio) The evaluation results are also shown in Table 1.

As can be seen from Table 1, Example 1 using the pseudo-equilibrium catalyst A corresponding to the method of the present invention is compared with Comparative Example 1 using the pseudo-equilibrium catalyst B not corresponding to the present invention.
Despite the large amount of deposited metal, it has high cracking activity and high gasoline and LCO yields.

[0030]

[Table 1]

[0031]

[Reference Example 2] A method for supporting a metal in which the deposition of nickel and vanadium on the catalyst in a reaction tower and a regeneration tower in a fluid catalytic cracking actual apparatus is assumed, that is, a cyclic metal deposition method. Nickel and vanadium were loaded according to That is, Reference Example 1
Using the commercially available catalyst used in 1., while keeping the catalyst fluidized in a fluidized bed, the temperature was kept at 500 ° C., and a toluene solution containing a predetermined amount of nickel naphthenate and vanadium naphthenate was mixed with vacuum gas oil to obtain a stock oil. It was supplied for 10 minutes and reacted. Then, raise the temperature to 820 ° C. and increase to 50%.
The catalyst was regenerated by keeping the same temperature for 15 minutes in a steam atmosphere. Then, the temperature was lowered to 500 ° C., and a raw material oil was supplied to cause a reaction. Repeat this reaction / reproduction operation 6
The operation was repeated 3 times to allow a predetermined amount of Ni and V to be supported, and finally, calcination was performed in air at 600 ° C. for 1 hour to obtain a pseudo equilibrium catalyst C.

Pseudo-equilibrium catalysts D and E having different Ni and V contents were prepared by the same method as described above. Table 2 shows the properties of these pseudo-equilibrium catalysts.

[0033]

Example 2 and Comparative Example 2 Using the pseudo equilibrium catalysts C, D and E prepared in Reference Example 2, the catalytic activity was evaluated in the same manner as in Example 1. The evaluation results are also shown in Table 2. The metal loading method of Reference Example 2 is the method for best reproducing the equilibrium catalyst in the actual apparatus in the laboratory. Example 2 using pseudo-equilibrium catalysts C and D corresponding to the method of the present invention,
As can be seen from Table 2, as compared with Comparative Example 2 which uses the pseudo-equilibrium catalyst E that does not correspond to the present invention, the decomposition activity is high and the gasoline and LC
O yield is high.

[0034]

[Table 2]

[0035]

Effects of the Invention According to the fluid catalytic cracking method for hydrocarbon oils of the present invention, there is little activity deterioration of the catalyst in the fluid catalytic cracking of heavy residual oil containing metal contaminants such as nickel and vanadium, and Since the production of hydrogen and coke is small, the yield of gasoline and kerosene fraction is high. Further, even if the catalyst composition contains a large amount of nickel or vanadium, the activity of the catalyst does not decrease so much, so that the consumption of the fresh catalyst in the FCC process becomes small.

   ─────────────────────────────────────────────────── ─── Continued front page    (72) Inventor Yoshiaki Kato             No. 13-2 Kitaminato-cho, Wakamatsu-ku, Kitakyushu City, Fukuoka Prefecture             Medium Chemical Industry Co., Ltd. Wakamatsu Factory (72) Inventor Hiroyuki Kiyofuji             No. 13-2 Kitaminato-cho, Wakamatsu-ku, Kitakyushu City, Fukuoka Prefecture             Medium Chemical Industry Co., Ltd. Wakamatsu Factory (72) Inventor Hidehiro Higashi             No. 13-2 Kitaminato-cho, Wakamatsu-ku, Kitakyushu City, Fukuoka Prefecture             Medium Chemical Industry Co., Ltd. Wakamatsu Factory (72) Inventor Hitoshi Konaka             Catalyst, 580 Horikawa-cho, Saiwai-ku, Kawasaki-shi, Kanagawa             Kasei Industry Co., Ltd. F-term (reference) 4G069 AA03 BA07A BA07B BC54A                       BC54B BC68A BC68B CC07                       EA01X EA01Y EB18X EB18Y                       EC02X EC02Y EC03X EC03Y                       EC04X EC05X EC06X EC06Y                       EC07X EC08X EC18X EC18Y                       ED03 ED07 FC08 ZA03A                       ZA04B ZC03 ZF02A ZF02B                       ZF05A ZF05B                 4H029 CA00 DA00

Claims (6)

[Claims] 1. A heavy hydrocarbon oil containing nickel (Ni) and vanadium (V) and having a weight ratio (Ni / V) of nickel (Ni) and vanadium (V) of 1.0 or more. Is a faujasite-type zeolite having a weight ratio (Ni / V) of deposited nickel (Ni) and vanadium (V) of 1.0 or more and a unit cell constant of 24.25 to 24.40Å. And a method for fluid catalytic cracking of a heavy hydrocarbon oil, which comprises fluid catalytic cracking in the presence of a fluid catalytic cracking catalyst composition containing an inorganic oxide matrix. 2. A weight ratio of nickel (Ni) and vanadium (V) contained in the heavy hydrocarbon oil (Ni /
V) exists in the range of 1.1-40, The fluid catalytic cracking method of the heavy hydrocarbon oil of Claim 1 characterized by the above-mentioned. 3. The flow of the heavy hydrocarbon oil according to claim 1, wherein vanadium (V) contained in the heavy hydrocarbon oil is in the range of 1 to 50 ppm by weight. Catalytic decomposition method. 4. The flow of a heavy hydrocarbon oil according to claim 1, wherein the fluid catalytic cracking catalyst composition contains 100 weight ppm or more of vanadium (V). Catalytic decomposition method. 5. The fluid catalytic cracking catalyst composition has an average particle size of 50 to 100 μm and a specific surface area (SA).
Is 70 m ² / g or more, and the pore volume (PV) is 0.1
0 ml / g or more, pore diameter (PD) 500 to 20
The pore volume (pv) occupied by pores in the range of 00Å is 40% or more of the pore volume (PV), and the abrasion resistance (At
tr. Res. ) Is 0.3 wt% / hr or less, the fluid catalytic cracking method for heavy hydrocarbon oil according to any one of claims 1 to 4, wherein 6. The fluid catalytic cracking catalyst composition comprises 5 to 50% by weight of faujasite type zeolite, and a metal scavenger 1.
~ 30 wt% and inorganic oxide matrix 20-9
The fluid catalytic cracking method for heavy hydrocarbon oil according to any one of claims 1 to 5, wherein the fluid catalytic cracking method comprises 4% by weight.