JP2002241764A - Fluidized catalytic cracking process for heavy oil - Google Patents

Abstract

PROBLEM TO BE SOLVED: To provide a fluidized catalytic cracking process for obtaining light olefins, for example, propylene, butene, and the like, by subjecting heavy oil to fluidized catalytic cracking at elevated temperature in shortened time. SOLUTION: In this process, heavy oil is catalytically cracked in a fluidized bed catalytic cracker that comprises a down-flow type reaction zone, a gas solid separation zone, a stripping zone and a catalyst regeneration zone to produce light olefins wherein the reaction zone outlet temperature is characteristically set to 580-630 deg.C, the weight ratio of the catalyst/the oil is in the range of 15-40, the residential time of a hydrocarbon in the reaction zone is 0.1-1.0 second and the catalyst comprises 60-95 wt.% of a fluidized bed type cracking catalyst of a hyper-stable Y-type zeolite having <=0.5 wt.% content of a rare earth metal oxide and 5-40 wt.% of additives including shape-selective zeolite.

Description

DETAILED DESCRIPTION OF THE INVENTION

[0001]

The present invention relates to a fluid catalytic cracking method for heavy oil, and more particularly to a fluid catalytic cracking method for obtaining light olefins such as propylene and butene from heavy oil in high yield.

[0002]

2. Description of the Related Art In conventional catalytic cracking, petroleum hydrocarbons are decomposed by contact with a catalyst to obtain gasoline as a main product, a small amount of LPG, cracked gas oil, and the like. The catalyst is circulated and reused by burning off with air. However, recently, there has been a movement to utilize a fluid catalytic cracking unit not as a gasoline production unit but as a light olefin (particularly propylene) production unit as a petrochemical raw material. On the other hand, propylene and butene are raw materials for alkylate and methyl-t-butyl ether (MTBE) which are high octane gasoline base materials. The use of such a fluid catalytic cracking unit has a particular economic advantage in a refinery where petroleum refining and petrochemical plants are highly connected. As a method for producing a light olefin by fluid catalytic cracking of heavy oil, for example, a method of shortening the contact time between a catalyst and a feed oil (US Pat. No. 4,419,221)
No., U.S. Pat.No. 3,074,878, U.S. Pat.No. 5,462,652,
European Patent No. 315,179A), a method in which the reaction is carried out at a high temperature (US Pat. No. 4,980,053), a method using a pentasil type zeolite (US Pat. No. 5,326,465, published patent publication 7).
-506389) and the like.

However, even in these methods, the selectivity of light olefins has not yet been sufficiently increased.
For example, in a method using a high-temperature reaction, unnecessary dry gas yield increases due to simultaneous thermal decomposition, and the yield of useful light olefins is sacrificed accordingly. In addition, the high temperature reaction has the disadvantage that the quality of gasoline obtained with light olefins is deteriorated due to the increased production of diene. In the method of shortening the contact time, the hydrogen transfer reaction can be suppressed, and the rate of conversion of light olefins to light paraffin can be reduced, but the conversion cannot be increased.
Light olefin yields are still inadequate. Further, a method has been proposed in which thermal decomposition is suppressed by combining these high-temperature reactions, high catalyst / oil ratio, short contact time and other techniques, and a high conversion is achieved (Japanese Patent Laid-Open No. 10-60453). However, the light olefin yield is not yet sufficient. In addition, in the method using pentasil-type zeolite, gasoline is only decomposed to increase the light olefin yield, so that the light olefin yield is not sufficiently increased and the gasoline yield is significantly reduced. . Therefore, it is difficult to obtain a light olefin from a heavy oil in a high yield by these methods.

[0004]

SUMMARY OF THE INVENTION It is an object of the present invention to provide an improved heavy metal which can produce a small amount of dry gas due to thermal decomposition and a high yield of light olefin by a combination of a reaction type, a reaction condition and a catalyst. An object of the present invention is to provide a fluid catalytic cracking method for oil.

[0005]

Means for Solving the Problems The present inventors have developed a high-yield fluid catalytic cracking method for subjecting heavy oil to fluid catalytic cracking at a high temperature for a short contact time to obtain light olefins such as propylene and butene. As a result of intensive research focused on obtaining light olefins, a specific fluidized catalytic cracking catalyst and an additive containing shape-selective zeolite were mixed in a specific ratio and heavy oil was flowed under specific conditions. The inventors have found that the object can be achieved by catalytic decomposition, and have reached the present invention. That is, the present invention is a fluid catalytic cracking method of heavy oil for producing light olefins using a fluid catalytic cracking reactor having a down-flow type reaction zone, a gas-solid separation zone, a stripping zone and a catalyst regeneration zone,
Reaction zone outlet temperature 580-630 ° C, catalyst / oil ratio 1
Ultrastable Y having a hydrocarbon retention time of 0.1 to 1.0 second in a reaction zone of 5 to 40% by weight / weight, and a catalyst having a rare earth metal oxide content of 0.5% by mass or less. A fluid catalytic cracking method for heavy oil, comprising 60 to 95% by mass of a fluid catalytic cracking catalyst containing a zeolite and 5 to 40% by mass of an additive containing a shape-selective zeolite. Further, in the present invention, the crystal lattice constant of the ultrastable Y-type zeolite is preferably 24.30 to 24.60 °.

[0006]

BEST MODE FOR CARRYING OUT THE INVENTION Hereinafter, the present invention will be described in more detail. The present invention is a fluid catalytic cracking method for heavy oil in which a light olefin is produced using a fluid catalytic cracking reactor having a downflow type reaction zone, a gas-solid separation zone, a stripping zone and a catalyst regeneration zone. In the present invention, the fluid catalytic cracking is a method in which heavy oil is continuously brought into contact with a catalyst maintained in a fluidized state to decompose heavy oil into light hydrocarbons mainly composed of light olefins and gasoline.

The usual fluid catalytic cracking method employs a so-called riser-reaction zone in which both the catalyst particles and the feed oil rise in the tube. However, when a normal riser reaction zone is used, back mixing occurs, and the residence time of the gas is locally increased to cause thermal decomposition. In particular, when the catalyst / oil ratio is extremely large as compared with the ordinary fluid catalytic cracking method as in the present invention, the degree of back mixing increases. Thermal cracking is not preferred because it increases the generation of unnecessary dry gas and decreases the yield of the target light olefin and gasoline. The present invention employs a downflow type (downer) reaction zone in which both the catalyst particles and the feed oil descend in the tube, and thus has the characteristic that back mixing is avoided.

[0008] A cracking reaction mixture comprising a mixture of cracking reaction products, unreacted products and spent catalyst which has undergone fluid catalytic cracking in the downflow type reaction zone is then sent to a gas-solid separation zone where it is decomposed from catalyst particles. Most of the hydrocarbons such as reaction products and unreacted substances are removed. In some cases, the decomposition reaction mixture is quenched immediately before or immediately after the gas-solid separation zone in order to suppress unnecessary thermal decomposition or excessive decomposition.

The spent catalyst from which most of the hydrocarbons have been removed is further sent to a stripping zone, where the stripping gas removes hydrocarbons that could not be completely removed in the gas-solid separation zone. After the spent catalyst and hydrocarbons are separated in this way, the spent catalyst to which the carbonaceous material and some heavy hydrocarbons are attached is regenerated from the stripping zone in order to regenerate the spent catalyst. Sent to the band. In the catalyst regeneration zone, the spent catalyst is subjected to an oxidation treatment to remove and regenerate carbonaceous substances and heavy hydrocarbons deposited and adhered on the catalyst. The catalyst regenerated after the oxidation treatment is sent again to the reaction zone and continuously circulated.

FIG. 1 shows an example of a fluid catalytic cracking reactor having a downflow type reaction zone, a gas-solid separation zone, a stripping zone and a catalyst regeneration zone. The heavy oil as the raw material is supplied to the mixing area 7 through the line 10 and mixed with the regenerated catalyst circulated from the catalyst storage tank 6. The mixture flows down in the reaction zone 1 in a parallel flow, during which the raw heavy oil and the catalyst are brought into contact with each other at high temperature for a short time to carry out the cracking reaction of the heavy oil. The cracked reaction mixture from reaction zone 1 flows down to gas-solid separation zone 2 located below reaction zone 1, where the spent catalyst is separated from the cracked reaction products and unreacted raw materials and dipreg 9 is removed. Through the stripping zone 3.

The hydrocarbon gas from which most of the spent catalyst has been removed is then led to a secondary separator 8. Here, a small amount of used catalyst remaining in the gas is removed, and the hydrocarbon gas is extracted out of the system and collected. As the secondary separator 8, a tangential cyclone is preferably used.

From the spent catalyst in the stripping zone 3, hydrocarbons adhering and remaining on the surface of the spent catalyst and between the catalysts are removed by the stripping gas introduced from the line 11. As the stripping gas, an inert gas such as steam generated by a boiler or nitrogen pressurized by a compressor or the like is used.

The stripping conditions include a temperature of 500 to 900 ° C., preferably 500 to 700 ° C., and a residence time of the catalyst particles of 1 to 10 minutes. In the stripping zone 3, cracking reaction products and unreacted raw materials adhering to the used catalyst and unreacted raw materials are removed, and the stripping gas and the line 12 at the top of the stripping zone 3 are removed.
, And guided to the recovery system. On the other hand, the spent catalyst which has been subjected to the stripping treatment is supplied to the first flow controller 13
Is supplied to the catalyst regeneration zone 4 through a line provided with.

The gas superficial velocity in stripping zone 3 is:
Usually, it is preferable to keep the pressure in the range of 0.05 to 0.4 m / s, so that the fluidized bed in the stripping zone can be a bubble fluidized bed. In the bubble fluidized bed, since the gas velocity is relatively low, the consumption of the stripping gas can be reduced, and since the bed density is relatively large, the pressure control width of the first flow rate controller 13 can be increased. Therefore, the transfer of the catalyst particles from the stripping zone 3 to the catalyst regeneration zone 4 becomes easy. Stripping band 3
In order to improve the contact between the used catalyst and the stripping gas and improve the stripping efficiency, a horizontal perforated plate or other inserts can be provided in multiple stages.

The catalyst regeneration zone 4 is defined by a vessel having an upper region having a conical shape and a lower region having a cylindrical shape, and the upper conical portion thereof communicates with an upright conduit (riser-type regeneration tower) 5. In the catalyst regeneration zone 4, the apex angle of the upper conical portion is usually 30 to 90.
Preferably, the height of the upper conical portion is in the range of 1/2 to 2 times the diameter of the lower cylindrical portion. The spent catalyst supplied from the stripping zone 3 to the catalyst regeneration zone 4 is regenerated by a regeneration gas (typically an oxygen-containing gas such as air) introduced from the bottom of the catalyst regeneration zone 4.
While being fluidized, substantially all of the carbonaceous materials and heavy hydrocarbons attached to the catalyst surface are burned off and regenerated. The regeneration conditions are usually at a temperature of 600 to 10
00 ° C, preferably 650-750 ° C, catalyst residence time 1
~ 5 minutes is adopted, and the gas superficial velocity is usually 0.4 ~
1.2 m / s is preferably adopted.

The regenerated catalyst that has been regenerated in the catalyst regeneration zone 4 and has jumped out from the upper part of the turbulent fluidized bed is transferred from the upper conical portion to the riser type regeneration tower 5 together with the used regeneration gas. The diameter of the riser-type regeneration tower 5 communicating with the upper conical portion of the catalyst regeneration zone 4 is one of the diameter of the lower cylindrical portion.
/ 6 to 1/3. By doing this,
The gas superficial velocity of the fluidized bed in the catalyst regeneration zone 4 can be maintained in a range of 0.4 to 1.2 m / s suitable for forming a turbulent fluidized bed. Tower speed,
The range of 4 to 12 m / s suitable for ascending transfer of the regenerated catalyst can be maintained.

The regenerated catalyst that has risen inside the riser type regeneration tower 5 is carried to a catalyst storage tank 6 installed at the top of the riser type regeneration tower. The catalyst storage tank 6 also functions as a gas-solid separator, and the used regeneration gas containing carbon dioxide gas and the like is separated from the regeneration catalyst here and discharged outside the system via the cyclone 15.

On the other hand, the regenerated catalyst in the catalyst storage tank 6 is supplied to the mixing area 7 via a downflow pipe provided with a second flow controller 17. If necessary, a part of the regenerated catalyst in the catalyst storage tank 6 is regenerated through a bypass conduit provided with a third flow controller 16 in order to facilitate control of the amount of catalyst circulated in the riser type regenerator 5. You can change it back to 4. As described above, the catalyst passes through the reaction zone 1, the gas-solid separation zone 2, the stripping zone 3, the catalyst regeneration zone 4, the riser-type regeneration tower 5, the catalyst storage tank 6, and the mixing region 7, and is again subjected to the downflow type. The system is circulated in the reaction zone 1 in this order.

The heavy oil used as a raw material in the present invention includes straight-run gas oil, vacuum gas oil, atmospheric residual oil, vacuum residual oil, pyrolysis gas oil,
And hydrorefined heavy oils.
These heavy oils may be used alone, or a mixture of these heavy oils or a mixture of these heavy oils and a partly light oil may be used. The reaction zone outlet temperature in the present invention refers to the outlet temperature of the downflow type reaction zone, the temperature immediately before the decomposition reaction product is separated from the catalyst,
Alternatively, when quenching is performed immediately before the gas-solid separation zone, the temperature is immediately before quenching. In the present invention, the reaction zone outlet temperature is 580 to 630 ° C, preferably 590 to 62 ° C.
0 ° C. If the temperature is lower than 580 ° C., a light olefin cannot be obtained in a high yield, and if the temperature is higher than 630 ° C., thermal decomposition becomes remarkable and the amount of dry gas generated is not preferable. The term "catalyst / oil ratio" as used in the present invention refers to the ratio between the amount of circulated catalyst (ton / h) and the feed rate of feed oil (ton / h). In the present invention, the catalyst / oil ratio needs to be 15 to 40 weight / weight, preferably 20 to 3 weight / weight.
0 weight / weight. If the catalyst / oil ratio is smaller than 15% by weight, the temperature of the regenerated catalyst supplied to the reaction zone increases due to heat balance, and the amount of dry gas generated by thermal decomposition increases, which is not preferable. If the catalyst / oil ratio is greater than 40% by weight, the amount of circulated catalyst increases, and the capacity of the catalyst regeneration zone becomes too large to secure the catalyst residence time required for catalyst regeneration in the catalyst regeneration zone. Therefore, it is not preferable.

In the present invention, the hydrocarbon residence time refers to the time from the contact of the catalyst with the feed oil to the separation of the catalyst and the decomposition reaction product at the outlet of the reaction zone, or before the gas-solid separation zone. In the case of rapid cooling, it indicates the time until rapid cooling. In the present invention, the residence time is 0.1 to 1.0.
Seconds, preferably 0.2-0.7
Seconds. The residence time of the hydrocarbons in the reaction zone is 0.1
If the time is shorter than seconds, the cracking reaction becomes insufficient and a light olefin cannot be obtained in a high yield. If the residence time is longer than 1.0 second, the contribution of thermal decomposition increases, which is not preferable. The operating conditions of the fluid catalytic cracking reactor in the present invention are not particularly limited except for the above, but usually the reaction pressure is 196 to 392 kPa (1 to 3 kg / cm).
It is preferably operated at ² G).

The catalyst used in the present invention comprises a fluid catalytic cracking catalyst and an additive. The fluid catalytic cracking catalyst comprises zeolite as an active component and a matrix as a supporting matrix thereof. The main component of the zeolite is an ultra-stable Y-type zeolite, and the content of the rare earth metal oxide in the zeolite is 0.5% by mass or less. In general, the activity of the equilibrium catalyst increases as the content of the rare earth oxide in the ultra-stable Y-type zeolite increases as the heat resistance increases. On the other hand, an equilibrium catalyst containing a large amount of rare earth metal oxide also has a high hydrogen transfer activity. As the hydrogen transfer activity of the fluid catalytic cracking catalyst increases, olefins in the product decrease and paraffins increase. Olefins mainly in the gasoline fraction are decomposed into light olefins by additives including a shape-selective zeolite described later.
However, the decomposition rate of paraffins in the gasoline fraction by the additive is significantly slower than the decomposition of olefins, so the higher the hydrogen transfer activity of the fluid catalytic cracking catalyst, the lower the rate of light olefin generation by the additive. Become.
The rare earth metal oxide content in the fluid catalytic cracking catalyst used in the present invention is 0.5% by mass or less, preferably 0.3% by mass or less, and more preferably 0.1% by mass or less. When the content of the rare earth metal oxide is more than 0.5% by mass, the hydrogen transfer activity becomes too high, and the decomposition activity becomes high, but the light olefin yield decreases.

The preferred crystal lattice constant of the ultrastable Y-type zeolite in the new catalyst is from 24.30 to 24.60.
、, and more preferably 24.36 to 24.45Å
It is. The crystal lattice constant of zeolite here is AST
MD-3942-80. In this range, the smaller the crystal lattice constant, the lower the gasoline yield but the higher the light olefin yield. However, when the crystal lattice constant is less than 24.30 °, the cracking activity of the fluid catalytic cracking catalyst is too low to obtain a high conversion, and the light olefin yield decreases. If the lattice constant is larger than 24.60 °, the hydrogen transfer activity becomes too high, which is not preferable. The content of the ultra-stable Y-type zeolite in the fluid catalytic cracking catalyst is preferably 5 to 50% by mass,
-40 mass% is more preferable. The fluid catalytic cracking catalyst has a bulk density of 0.5 to 1.0 g / ml and an average particle size of 50 to 50 g / ml.
～90Myuemu, surface area 50~350m ² / g, preferably a pore volume in the range of 0.05~0.5ml / g.

The additive used in the present invention contains a shape-selective zeolite. Shape-selective zeolites are zeolites whose pore size is smaller than that of Y-type zeolites, and only hydrocarbons of a limited shape can enter the pores. Such zeolites include ZSM-5, β, omega, SAPO-5, SAPO
-11, SAPO-34, pentasil-type metallosilicate and the like. Among these shape-selective zeolites, ZSM-5 is most preferred. The preferred content of the shape-selective zeolite contained in the additive is 20 to 70% by mass, more preferably 30 to 60% by mass. The bulk density of the additive used in the present invention is 0.5 to 1.0 g / ml,
Average particle size is 50 to 90 μm, surface area is 10 to ²⁰⁰ m ²
/ G and the pore volume are preferably in the range of 0.01 to 0.3 ml / g.

The proportion of the fluid catalytic cracking catalyst in the catalyst used in the present invention is 60 to 95% by mass, and the proportion of the additive is 5 to 40% by mass. When the ratio of the fluid catalytic cracking catalyst is less than 60% by mass, or when the ratio of the additive is more than 40% by mass, the conversion of heavy oil as a feed oil decreases, and a high light olefin is produced. No yield is obtained. On the other hand, when the ratio of the fluid catalytic cracking catalyst is more than 95% by mass, or when the ratio of the additive is 5% by mass.
If less, high conversions are obtained but high light olefin yields are not obtained.

[0025]

Next, embodiments of the present invention will be described, but the present invention is not limited thereto.

Example 1 Fluid catalytic cracking of heavy oil was carried out using a down flow reactor (downer) type FCC pilot apparatus.
Equipment scale is 5kg for inventory and 1kg for feed
/ H, and operating conditions are reactor outlet temperature 600
° C, reaction pressure 196 kPa (1.0 kg / cm ² G),
Catalyst / oil ratio 30 weight / weight, catalyst regeneration zone temperature 720 ° C
It is. At this time, the hydrocarbon residence time in the reactor was 0.5 seconds. The feedstock used was a Middle Eastern (Arabian light) desulfurized vacuum gas oil (VGO). The catalyst used was a mixture of 75% by mass of the fluid catalytic cracking catalyst (A) and 25% by mass of an additive (OlefinsMax, trade name, manufactured by Davison) containing ZSM-5. The fluid catalytic cracking catalyst (A) has a rare earth oxide content of 0.05% by mass, and the ultra-stable Y-type zeolite contained in the fluid catalytic cracking catalyst (A) has a crystal lattice constant of 24.40 °. The fluid catalytic cracking catalyst (A) and the additives are each separately charged 810 before being charged to the apparatus.
Steaming was performed at 100 ° C for 6 hours with 100% steam. Table 1 shows the results of the decomposition reaction.

Example 2 Using the same apparatus as in Example 1, fluid catalytic cracking of heavy oil was performed under the same operating conditions. The raw oil used is unsulfurized Daqing VG
O. The catalyst used was the same as in Example 1 and was an additive containing 75% by mass of a fluid catalytic cracking catalyst (A) and ZSM-5 (Daviso
A mixture of 25% by mass (OlefinsMax, trade name, manufactured by n Company). Table 1 shows the results of the decomposition reaction.

Example 3 Using the same apparatus as in Example 1, fluid catalytic cracking of heavy oil was performed under the same operating conditions. The feedstock used was the same Middle Eastern (Arabian light) desulfurized VGO as in Example 1. The catalyst used was 75% by mass of a fluid catalytic cracking catalyst (B) and ZSM-
Additive 5 (Davison, trade name OlefinsMax) 2
It is a mixture of 5% by mass. The fluid catalytic cracking catalyst (B) has a rare earth oxide content of 0.05% by mass, and the ultra-stable Y-type zeolite contained in the fluid catalytic cracking catalyst (B) has a crystal lattice constant of 24.55 °. Fluid catalytic cracking catalyst (B)
Each was separately steamed at 810 ° C. for 6 hours with 100% steam before loading the additives into the apparatus. Table 1 shows the results of the decomposition reaction.

Comparative Example 1 Using the same apparatus as in Example 1, fluid catalytic cracking of heavy oil was performed under the same operating conditions. The feedstock used was the same Middle Eastern (Arabian light) desulfurized VGO as in Example 1. The catalyst used was a fluid catalytic cracking catalyst (A), and no additives were used. Before the fluidized catalytic cracking catalyst (A) was charged into the apparatus, it was steamed at 810 ° C. for 6 hours with 100% steam. Table 1 shows the results of the decomposition reaction.

Comparative Example 2 Using the same apparatus as in Example 1, fluid catalytic cracking of heavy oil was performed under the same operating conditions. The feedstock used was the same Middle Eastern (Arabian light) desulfurized VGO as in Example 1. The catalyst used was 75% by mass of a fluid catalytic cracking catalyst (C) and ZSM-
Additive 5 (Davison, trade name OlefinsMax) 2
It is a mixture of 5% by mass. The fluid catalytic cracking catalyst (C) has a rare earth oxide content of 3.5% by mass, and the ultra-stable Y-type zeolite contained in the fluid catalytic cracking catalyst (C) has a crystal lattice constant of 24.55 °. The fluid catalytic cracking catalyst (C) and the additive are each separately charged to the apparatus before charging to the apparatus.
Steaming was performed at 100C for 6 hours at 100C. Table 1 shows the results of the decomposition reaction.

Comparative Example 3 Fluid catalytic cracking of heavy oil was carried out using an upflow reactor (riser) type FCC pilot apparatus.
Equipment scale is inventory-3kg, feed amount 1kg
/ H, and operating conditions are reactor outlet temperature 600
° C, reaction pressure 196 kPa (1.0 kg / cm ² G),
Catalyst / oil ratio 10 wt / wt, catalyst regeneration zone temperature 720 ° C
It is. At this time, the hydrocarbon residence time in the reactor was 1.5 seconds. The feedstock used was Middle Eastern (Arabian Light) desulfurized VGO. The catalyst used was an additive containing 75% by mass of the fluid catalytic cracking catalyst (A) and ZSM-5 (Da
Viles, trade name OlefinsMax) 25% by weight. Each of the fluidized catalytic cracking catalyst (A) and the additive was separately charged at 810 ° C. for 6 hours before being charged into the apparatus.
Steaming was performed with 0% steam. Table 1 shows the results of the decomposition reaction.

[0032]

[Table 1]

[0033]

As described above, a specific fluid catalytic cracking catalyst and an additive containing a shape-selective zeolite are mixed at a specific ratio and used, and heavy oil is catalytically cracked under specific conditions. The amount of dry gas generated by thermal decomposition is small,
Light olefins such as propylene and butene can be obtained in high yield.

[Brief description of the drawings]

FIG. 1 is an example of a down-flow type fluid catalytic cracking reactor.

[Explanation of symbols]

 DESCRIPTION OF SYMBOLS 1 Down-flow type reaction zone 2 Gas-solid separation zone 3 Stripping zone 4 Regeneration zone 5 Riser type regeneration tower 6 Catalyst storage tank 7 Mixing area 8 Secondary separator 9 Dip-reg

 ──────────────────────────────────────────────────続 き Continuing on the front page (72) Inventor Toshiaki Okuhara, Saudi Arabia, Daharan 31261, Petroleum Industry Activation Center New FC C Saudi Branch Office (72) Inventor, Takashi Ino Kingdom of Saudi Arabia, Dahran 31261, Petroleum Industry Activation Center New FC C Saudi Branch Office (72) Inventor Mohammad Abulhamael Saudi Arabia, Daharan 31261, King Fahd University of Petroleum and Minerals (72) Inventor Abdullah Aitani Saudi Arabia, Dahlan 31261, King Fahd University of Petroleum and Minerals (72) Inventor Abdulgadel Magravi Dahran 3, Kingdom of Saudi Arabia 1261, King Fahd University of Petroleum and Minerals F-term (reference) 4G069 AA02 AA15 BA07A BA07B BC38A BC38B CC07 DA08 EA01Y EB18Y EC02Y EC03Y EC06Y EC21Y FC08 GA06 ZA05A ZA05B ZC03 4H03 BC

Claims (2)

[Claims] 1. A fluidized catalytic cracking method of heavy oil for producing light olefins using a fluidized catalytic cracking reactor having a downflow type reaction zone, a gas-solid separation zone, a stripping zone and a catalyst regeneration zone, The reaction zone outlet temperature is 580 to 630 ° C, the catalyst / oil ratio is 15 to 40% by weight, and the residence time of hydrocarbons in the reaction zone is 0.1 to 1.0.
Second and the catalyst has a rare earth metal oxide content of 0.
Fluid catalytic cracking of heavy oil comprising 60 to 95% by mass of a fluid catalytic cracking catalyst containing ultra-stable Y-type zeolite of 5% by mass or less and 5 to 40% by mass of an additive containing shape-selective zeolite. Decomposition method. 2. The process for fluid catalytic cracking of heavy oil according to claim 1, wherein the crystal lattice constant of the ultra-stable Y-type zeolite is 24.30 to 24.60 °.