WO2015182329A1 - 重質油の流動接触分解法 - Google Patents

重質油の流動接触分解法 Download PDF

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WO2015182329A1
WO2015182329A1 PCT/JP2015/062967 JP2015062967W WO2015182329A1 WO 2015182329 A1 WO2015182329 A1 WO 2015182329A1 JP 2015062967 W JP2015062967 W JP 2015062967W WO 2015182329 A1 WO2015182329 A1 WO 2015182329A1
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catalyst
catalytic cracking
fluid catalytic
heavy oil
mass
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PCT/JP2015/062967
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English (en)
French (fr)
Japanese (ja)
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太 大内
秀樹 尾野
真理絵 岩間
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Ｊｘ日鉱日石エネルギー株式会社
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Priority to US15/313,617 priority Critical patent/US20170218281A1/en
Priority to KR1020167033344A priority patent/KR20170015301A/ko
Publication of WO2015182329A1 publication Critical patent/WO2015182329A1/ja

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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G11/14—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts
    • C10G11/18—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts according to the "fluidised-bed" technique
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G11/02—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils characterised by the catalyst used
    • C10G11/04—Oxides
    • C10G11/05—Crystalline alumino-silicates, e.g. molecular sieves
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
    • C10G2400/20—C2-C4 olefins

Definitions

  • the present invention relates to a fluid catalytic cracking method of 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.
  • Such a method of using a fluid catalytic cracker has an economic advantage particularly in a refinery where oil refining and a petrochemical factory are highly coupled.
  • Examples of the method for producing light olefins by fluid catalytic cracking of heavy oil include, for example, a method of shortening the contact time between the catalyst and the feedstock (Patent Documents 1 to 4), a method of performing a reaction at a high temperature (Patent Document 5), Examples thereof include methods using pentasil-type zeolite (Patent Documents 6 to 7).
  • the selectivity for light olefins has not been sufficiently improved.
  • the pyrolysis is combined with an increase in unnecessary dry gas yield, and the yield of useful light olefin is sacrificed accordingly.
  • the quality of gasoline obtained together with the light olefin deteriorates.
  • the method of shortening the contact time can suppress the hydrogen transfer reaction and reduce the rate of conversion of light olefins to light paraffin, but the conversion rate cannot be increased, so the yield of light olefins is still insufficient. It is.
  • Patent Document 8 a method (Patent Document 8) has been proposed that combines these techniques such as high temperature reaction, high catalyst / oil ratio, and short contact time to suppress thermal decomposition and achieve high conversion (Patent Document 8).
  • the olefin yield is not sufficient.
  • the method using pentasil-type zeolite only increases the light olefin yield by overdecomposing gasoline, so the light olefin yield is not sufficiently increased, and the gasoline yield is significantly reduced. . Therefore, it is difficult to obtain light olefins from heavy oil in high yield by these methods.
  • Patent Document 9 In addition to high temperature reaction, high catalyst / oil ratio, short contact time, a down flow type reaction zone that can suppress back mixing in the reaction zone, and content and shape selectivity of rare earth metal oxide in fluid catalytic cracking catalyst. There has been proposed a method (Patent Document 9) for further improving the light olefin yield by adjusting the mixing ratio of the additive containing zeolite. However, even if these methods are used, when the activity of the fluid catalytic cracking catalyst is not sufficient, the cracking of the heavy feedstock is insufficient and the light olefin yield has not been maximized.
  • the object of the present invention is an improved heavy material that can produce light olefins in a high yield by combining the reaction mode, reaction conditions, catalyst, etc., with a small amount of dry gas generated by thermal decomposition and a small amount of paraffin generated by hydrogen transfer reaction. It is to provide a fluid catalytic cracking process of oil.
  • the present inventors diligently focused on obtaining a light olefin in a high yield in a fluid catalytic cracking process for obtaining light olefins such as propylene and butene by fluid catalytic cracking of heavy oil at a high temperature and a short contact time.
  • the inventors have found that the object can be achieved by using a catalyst containing a specific fluid catalytic cracking catalyst and subjecting heavy oil to fluid catalytic cracking under specific conditions, and have reached the present invention. .
  • the present invention relates to a process for producing light olefins by fluid catalytic cracking of heavy oil, in which the reaction zone outlet temperature is 580 to 630 ° C., the catalyst / oil ratio is 15 to 40 weight / weight, and carbonization in the reaction zone is performed.
  • a catalyst containing 12 to 24% by mass of a shape-selective zeolite is brought into contact with heavy oil under conditions where the hydrogen residence time is 0.1 to 1.0 second, and the secondary cracking activity (C2 olefin concentration /
  • This is a heavy oil fluidized catalytic cracking method characterized in that a cracked product having a value of (C4 olefin concentration) in the range of 0.30 to 0.55 is obtained.
  • the catalyst is a catalyst comprising an additive containing a fluid catalytic cracking catalyst and a shape selective zeolite, and the content of the ultrastable Y-type zeolite in the fluid catalytic cracking catalyst is 5 to 50% by mass.
  • the present invention relates to a fluid catalytic cracking process of the heavy oil.
  • the catalyst is a catalyst comprising an additive containing a fluid catalytic cracking catalyst and a shape-selective zeolite, and the content of the shape-selective zeolite in the additive is 20 to 70% by mass.
  • the present invention relates to a fluid catalytic cracking method of the heavy oil.
  • the catalyst is a catalyst comprising an additive containing a fluid catalytic cracking catalyst and a shape-selective zeolite, wherein the ratio of the additive in the catalyst is 17 to 60% by mass.
  • the present invention relates to fluid catalytic cracking of heavy oil.
  • the present invention also relates to the above-described fluid catalytic cracking method of heavy oil, characterized in that the crystal lattice constant of the ultrastable Y-type zeolite is 24.20 to 24.60 ⁇ .
  • the catalyst is a catalyst comprising an additive containing a fluid catalytic cracking catalyst and a shape selective zeolite, and the content of the rare earth metal oxide in the fluid catalytic cracking catalyst is 1.5% by mass or less.
  • the present invention relates to a fluid catalytic cracking process for heavy oil as described above. Furthermore, the present invention relates to the above-described fluid catalytic cracking method of heavy oil, characterized by 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.
  • the amount of dry gas generated by thermal decomposition and the amount of paraffin generated by hydrogen transfer reaction are small, and light olefins such as propylene and butene can be obtained in high yield.
  • the present invention is a fluid catalytic cracking process of heavy oil for producing light olefins.
  • fluid catalytic cracking is one in which heavy oil is continuously brought into contact with a catalyst held in a fluid state to decompose heavy oil into light hydrocarbons mainly composed of light olefins and gasoline.
  • a fluid catalytic cracker having a reaction zone, a gas-solid separation zone, a stripping zone and a catalyst regeneration zone is used.
  • reaction zone examples include a so-called riser reaction zone in which both catalyst particles and feedstock oil rise in the pipe, and a downflow type (downer) reaction zone in which both catalyst particles and feedstock oil fall in the pipe.
  • riser reaction zone in which both catalyst particles and feedstock oil rise in the pipe
  • downflow type (downer) reaction zone in which both catalyst particles and feedstock oil fall in the pipe.
  • thermal decomposition is undesirable because it increases the generation of unnecessary dry gas and decreases the yield of the desired light olefin and gasoline. Therefore, in the present invention, a down flow type (downer) reaction zone in which both catalyst particles and raw material oil descend in the pipe is preferably used.
  • the cracked reaction mixture comprising the mixture of cracked reaction product, unreacted material and spent catalyst that has undergone fluid catalytic cracking in the reaction zone is then sent to the gas-solid separation zone where the cracked reaction product, unreacted from the catalyst particles. Most of hydrocarbons such as waste are removed. In some cases, the decomposition reaction mixture is quenched immediately before or 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 the stripping zone, where hydrocarbons that could not be completely removed in the gas-solid separation zone are removed by the stripping gas.
  • the used catalyst with the carbonaceous material and some heavy hydrocarbons attached is regenerated from the stripping zone in order to regenerate the spent catalyst. Sent to the band.
  • the used catalyst is oxidized, and carbonaceous substances and heavy hydrocarbons deposited and deposited on the catalyst are removed and regenerated.
  • the catalyst regenerated by this oxidation treatment is sent again to the reaction zone and continuously circulated.
  • FIG. 1 shows an example of a fluid catalytic cracking reaction apparatus having a downflow type reaction zone, a gas-solid separation zone, a stripping zone, and a catalyst regeneration zone. The present invention will be described below with reference to FIG.
  • the heavy oil as the raw material is supplied to the mixing region 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, and during this time, the raw heavy oil and the catalyst are brought into contact with each other at a high temperature for a short time, and the heavy oil is decomposed.
  • the decomposition reaction mixture from reaction zone 1 flows down to gas-solid separation zone 2 located below reaction zone 1, where spent catalyst is separated from decomposition reaction products and unreacted raw materials, and dipleg 9 is Then, it is guided to the upper part of the stripping band 3.
  • the hydrocarbon gas from which most of the spent catalyst has been removed is then led to the secondary separator 8.
  • a small amount of spent catalyst remaining in the gas is removed, and the hydrocarbon gas is extracted out of the system and recovered.
  • a tangential cyclone is preferably used as the secondary separator 8.
  • the spent catalyst in the stripping zone 3 is removed by the stripping gas introduced from the line 11 to remove remaining hydrocarbons adhering to the surface of the used catalyst or between the catalysts.
  • the stripping gas an inert gas such as nitrogen generated by a steam or a compressor generated by a boiler is used.
  • a temperature of 500 to 900 ° C., preferably 500 to 700 ° C., and a catalyst particle residence time of 1 to 10 minutes are usually employed.
  • the stripping zone 3 the decomposition reaction products and unreacted raw materials adhering to the spent catalyst are removed, and the stripping gas is extracted from the line 12 at the top of the stripping zone 3 and led to the recovery system.
  • the spent catalyst that has undergone the stripping process is supplied to the catalyst regeneration zone 4 through a line including the first flow rate regulator 13.
  • the gas superficial velocity in the stripping zone 3 is usually preferably maintained 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. Since the gas velocity is relatively small in the bubbling fluidized bed, 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 regulator 13 can be increased. Therefore, the transfer of the catalyst particles from the stripping zone 3 to the catalyst regeneration zone 4 is facilitated.
  • a horizontal perforated plate and other insertions can be provided in multiple stages for the purpose of improving the contact between the used catalyst and the stripping gas and improving the stripping efficiency.
  • the catalyst regeneration zone 4 is partitioned by a container having a conical upper portion and a cylindrical lower portion, and the upper conical portion communicates with an upright conduit (riser type regeneration tower) 5.
  • the apex angle of the upper cone portion is usually in the range of 30 to 90 degrees, and the height of the upper cone portion is preferably 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 fluidized by a regeneration gas (typically an oxygen-containing gas such as air) 14 introduced from the bottom of the catalyst regeneration zone 4. It is regenerated by burning and removing substantially all of the carbonaceous material and heavy hydrocarbons adhering to the catalyst surface.
  • a temperature of 600 to 1000 ° C., preferably 650 to 750 ° C., a catalyst residence time of 1 to 5 minutes is adopted, and a gas superficial velocity is preferably 0.4 to 1.2 m / s. Adopted.
  • the regenerated catalyst regenerated in the catalyst regeneration zone 4 and jumped out from the upper part of the turbulent fluidized bed is transferred to the riser type regeneration tower 5 from the upper conical portion along 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 preferably 1/6 to 1/3 of the diameter of the lower cylindrical portion.
  • the regenerated catalyst rising in 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 or the like is separated from the regeneration catalyst here and discharged out of the system via the cyclone 15.
  • the regenerated catalyst in the catalyst storage tank 6 is supplied to the mixing region 7 via a downflow pipe equipped with a second flow rate regulator 17. Further, if necessary, a part of the regenerated catalyst in the catalyst storage tank 6 is regenerated through a bypass conduit having a third flow rate regulator 16 in order to facilitate control of the catalyst circulation amount in the riser type regenerating tower 5. It can be returned to 4. In this way, the catalyst passes through the downflow type 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 again the downflow type. It circulates in the system in the order of reaction zone 1.
  • Examples of the heavy oil used as a raw material in the present invention include vacuum gas oil, atmospheric residue, vacuum residue, pyrolysis gas oil, and heavy oil obtained by hydrorefining these. These heavy oils may be used alone, or a mixture of these heavy oils or a mixture of these heavy oils with a part of light oil may be used.
  • the distillation properties of heavy oils used as raw material oils are preferably those having a boiling range of 170 to 800 ° C, more preferably 190 to 780 ° C.
  • the reaction zone outlet temperature as used in the present invention is the outlet temperature of the reaction zone, and when the decomposition reaction product is rapidly cooled immediately before the separation from the catalyst or before the gas-solid separation zone, it is rapidly cooled.
  • the reaction zone outlet temperature is 580 to 630 ° C., preferably 590 to 620 ° C. If the temperature is lower than 580 ° C., a light olefin cannot be obtained in a high yield, and if it is higher than 630 ° C., thermal decomposition becomes remarkable and the amount of dry gas generated is not preferable.
  • the catalyst / oil ratio indicates the ratio of the catalyst circulation rate (ton / h) to the feed oil supply rate (ton / h).
  • the catalyst / oil ratio needs to be 15 to 40 weight / weight, preferably 20 to 30 weight / weight.
  • the catalyst / oil ratio is smaller than 15 weight / weight, the temperature of the regenerated catalyst supplied to the reaction zone becomes high in view of heat balance, which is not preferable because the amount of dry gas generated by thermal decomposition increases.
  • the catalyst / oil ratio is larger than 40 weight / weight, the catalyst circulation amount becomes large, and the capacity of the catalyst regeneration zone becomes too large to secure the catalyst residence time necessary for catalyst regeneration in the catalyst regeneration zone. Therefore, it is not preferable.
  • the hydrocarbon residence time as used in the present invention is the time from when the catalyst comes into contact with the raw material oil until the catalyst and the decomposition reaction product are separated at the outlet of the reaction zone, or immediately before the gas-solid separation zone. In the case, the time until quenching is shown.
  • the residence time needs to be 0.1 to 1.0 seconds, and preferably 0.4 to 0.9 seconds.
  • the residence time of hydrocarbons in the reaction zone is shorter than 0.1 seconds, the decomposition reaction becomes insufficient and light olefins cannot be obtained in high yield.
  • the residence time is longer than 1.0 seconds, the contribution of thermal decomposition becomes large, 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 operation is preferably carried out at a reaction pressure of 150 to 400 kPa.
  • the catalyst used in the present invention comprises a fluid catalytic cracking catalyst and an additive.
  • the fluid catalytic cracking catalyst comprises a zeolite which is an active component and a matrix which is a supporting matrix thereof.
  • the main component of the zeolite is ultrastable Y-type zeolite.
  • the matrix is composed of an active matrix, a binder (such as silica), a filler (such as clay mineral), and other components (such as rare earth metal oxides and metal trap components).
  • the active matrix has decomposition activity, and examples thereof include alumina and silica alumina.
  • the additive that is a constituent of the catalyst used in the present invention contains a shape-selective zeolite.
  • Constituent components other than the shape-selective zeolite include a binder (such as silica) and a filler (such as clay mineral).
  • Shape-selective zeolite is a zeolite whose pore diameter is smaller than that of Y-type zeolite, and only limited-shaped hydrocarbons can enter the pores. Examples of such zeolite include ZSM-5, ⁇ , omega, SAPO-5, SAPO-11, SAPO-34, and pentasil-type metallosilicate. Of these shape selective zeolites, ZSM-5 is most preferred.
  • C2 olefin concentration (wt%) and C4 olefin concentration (wt%) in all fractions (cracked product) distilled from a fluid catalytic cracking apparatus are used as indicators for measuring the balance between primary cracking and secondary cracking.
  • C2 olefin concentration / C4 olefin concentration (referred to as secondary cracking activity in the present invention).
  • the secondary decomposition activity needs to be in the range of 0.30 to 0.55, preferably 0.35 to 0.50.
  • the secondary cracking activity is less than 0.30, the secondary cracking ability is insufficient with respect to the primary cracking ability, and a light olefin cannot be obtained in a high yield.
  • the secondary cracking activity is larger than 0.55, the secondary cracking ability is too high with respect to the primary cracking ability, and the light olefin cannot be obtained in high yield due to the excessive cracking of the light olefin.
  • the content of the shape selective zeolite in the catalyst used in the present invention needs to be 12 to 24% by mass, preferably 14 to 24% by mass, more preferably 16 to 23% by mass, and 18 to 22% by mass. % Is particularly preferred.
  • the secondary cracking activity can be controlled in the range of 0.30 to 0.55.
  • the shape selective zeolite in the catalyst is more than 24% by mass, the hydrogen transfer reaction proceeds, the light olefin becomes light paraffin, and the light olefin decreases.
  • the shape-selective zeolite in the catalyst is less than 12% by mass, the progress of secondary cracking becomes insufficient and light olefins are reduced.
  • the content of the rare earth metal oxide in the fluid catalytic cracking catalyst is preferably 1.5% by mass or less, more preferably 1.2% by mass or less, and particularly preferably 1.0% by mass or less.
  • the content of the rare earth metal oxide in the fluid catalytic cracking catalyst is more than 1.5% by mass, the hydrogen transfer activity becomes too high, and the cracking activity increases, but the light olefin yield decreases.
  • the rare earth oxide content in the fluid catalytic cracking catalyst increases, so the steaming resistance increases, so the activity of the catalyst increases.
  • a catalyst containing a large amount of rare earth metal oxide also has high hydrogen transfer activity.
  • the hydrogen transfer activity of the fluid catalytic cracking catalyst increases, the olefin in the product decreases and the paraffin increases.
  • Olefins mainly in gasoline fractions are decomposed into light olefins by additives containing shape selective zeolite.
  • the crystal lattice constant of the ultrastable Y-type zeolite is preferably 24.20 to 24.60 ⁇ , more preferably 24.36 to 24.45 ⁇ . In this range, the gasoline yield decreases as the crystal lattice constant decreases, but the light olefin yield increases. However, when the crystal lattice constant is smaller than 24.20 ⁇ , the cracking activity of the fluid catalytic cracking catalyst is too low to obtain a high conversion rate, so that the light olefin yield decreases. On the other hand, when the lattice constant is larger than 24.60 mm, the hydrogen transfer activity becomes too high.
  • the crystal lattice constant of zeolite here is measured by ASTM D-3942-80.
  • the ultrastable Y-type zeolite content in the fluid catalytic cracking catalyst is preferably 5 to 50% by mass, more preferably 15 to 40% by mass.
  • the bulk density of the fluid catalytic cracking catalyst is 0.5 to 1.0 g / ml, the average particle size is 50 to 90 ⁇ m, the surface area is 50 to 350 m 2 / g, and the pore volume is 0.05 to 0.5 ml / g. A range is preferred.
  • the shape-selective zeolite content in the additive is preferably 20 to 70% by mass, more preferably 30 to 60% by mass.
  • the bulk density of the additive is in the range of 0.5 to 1.0 g / ml, the average particle size is 50 to 90 ⁇ m, the surface area is 10 to 200 m 2 / g, and the pore volume is in the range of 0.01 to 0.3 ml / g. Preferably there is.
  • the ratio of the fluid catalytic cracking catalyst and the additive in the catalyst used in the present invention is 40 to 83% by mass, preferably 40 to 80% by mass, more preferably 40 to 70% by mass for the fluid catalytic cracking catalyst,
  • the additive containing the selective zeolite is 17 to 60% by mass, preferably 20 to 60% by mass, more preferably 30 to 60% by mass.
  • the amount of additive in the catalyst is relatively high, the production of coke can be suppressed. Since the additive has a low acid density, the reaction that becomes an aroma by the hydrogen transfer reaction from naphthene is suppressed, so that coke is hardly generated. Since hydrogen is generated as coke is generated, when coke generation is suppressed, the reaction from olefins to paraffin is suppressed, and the yield of light olefins is improved. However, even if the amount of the additive in the catalyst is too high, overdecomposition from olefin to paraffin occurs, and the light olefin yield decreases.
  • ⁇ Coke / Kinetic Conversion Coke yield (mass%) / (decomposition rate (mass%) / (100 ⁇ decomposition ratio (mass%)) is used (hereinafter referred to as ⁇ Coke / Kinetic Conversion). Is ⁇ Coke / K).
  • Example 1 Heavy oil fluidized catalytic cracking was carried out using a downflow reactor (downer) type FCC pilot device.
  • the equipment scale is inventory-5 kg, feed amount 1 kg / h, operating conditions are reaction zone outlet temperature 600 ° C., reaction pressure 196 kPa (1.0 kg / cm 2 G), catalyst / oil ratio 25 weight / weight.
  • the catalyst regeneration zone temperature is 720 ° C.
  • the raw material oil used was a desulfurized atmospheric residue oil (desulfurized AR) of the Middle East (Arabian Light).
  • the properties of desulfurization AR are as follows.
  • the 5% distillation temperature in distillation is 362 ° C., and the 95% distillation temperature is 703 ° C.
  • the 15 ° C. density is 0.931 g / cm 3 .
  • the residual carbon content is 2.57% by mass.
  • the sulfur content is 0.38% by mass.
  • the catalyst (A) used is a mixture of 70% by mass of a fluid catalytic cracking catalyst containing 37% by mass of an ultrastable Y-type zeolite and 30% by mass of an additive containing 43% by mass of a shape-selective zeolite.
  • the crystal lattice constant of the ultrastable Y-type zeolite contained in the fluid catalytic cracking catalyst is 24.40 ⁇ .
  • Each of the fluid catalytic cracking catalyst and the additive was separately steamed at 100% steam for 6 hours at 810 ° C. before being charged to the apparatus.
  • the results of the decomposition reaction are shown in Table 1.
  • the cut temperatures of gasoline / LCO / CLO were 221 ° C. and 343 ° C., respectively.
  • 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 material oil used was desulfurized vacuum gas oil (desulfurized VGO) of Middle Eastern (Arabian Light).
  • the properties of desulfurized VGO are as follows.
  • the 5% distillation temperature in distillation is 305 ° C, and the 95% distillation temperature is 538 ° C.
  • the 15 ° C. density is 0.0.895 g / cm 3 .
  • the residual carbon content is 0.02% by mass.
  • the sulfur content is 0.23% by mass.
  • the catalyst used is the same catalyst (A) as in Example 1.
  • the results of the decomposition reaction are shown in Table 1.
  • Example 3 Using the same apparatus as in Example 1, fluid catalytic cracking of heavy oil was performed under the same operating conditions.
  • the raw material oil used was the same Middle Eastern (Arabian light) desulfurized atmospheric residue oil (desulfurized AR) as in Example 1.
  • the used catalyst (B) is a mixture of 65% by mass of a fluid catalytic cracking catalyst containing 31% by mass of ultrastable Y-type zeolite and 35% by mass of an additive containing 54% by mass of shape-selective zeolite.
  • the crystal lattice constant of the ultrastable Y-type zeolite contained in the fluid catalytic cracking catalyst is 24.40 ⁇ .
  • Each of the fluid catalytic cracking catalyst and the additive was separately steamed at 100% steam for 6 hours at 810 ° C. before being charged to the apparatus. The results of the decomposition reaction are shown in Table 1.
  • Example 4 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 (Arabyanlite) desulfurized vacuum gas oil (desulfurized VGO) as in Example 2.
  • the catalyst used is the same catalyst (B) as in Example 3.
  • the results of the decomposition reaction are shown in Table 1.
  • Example 5 Using the same apparatus as in Example 1, fluid catalytic cracking of heavy oil was performed under the same operating conditions.
  • the raw material oil used was the same Middle Eastern (Arabian light) desulfurized atmospheric residue oil (desulfurized AR) as in Example 1.
  • the catalyst (C) used is a mixture of 50% by mass of a fluid catalytic cracking catalyst containing 36% by mass of an ultrastable Y-type zeolite and 50% by mass of an additive containing 42% by mass of a shape-selective zeolite.
  • the crystal lattice constant of the ultrastable Y-type zeolite contained in the fluid catalytic cracking catalyst is 24.40 ⁇ .
  • Each of the fluid catalytic cracking catalyst and the additive was separately steamed at 100% steam for 6 hours at 810 ° C. before being charged to the apparatus. The results of the decomposition reaction are shown in Table 1.
  • Example 6 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 (Arabyanlite) desulfurized vacuum gas oil (desulfurized VGO) as in Example 2.
  • the catalyst used is the same catalyst (C) as in Example 5.
  • the results of the decomposition reaction are shown in Table 1.
  • Example 7 Using the same apparatus as in Example 1, fluid catalytic cracking of heavy oil was performed under the same operating conditions.
  • the raw material oil used was the same Middle Eastern (Arabian light) desulfurized atmospheric residue oil (desulfurized AR) as in Example 1.
  • the catalyst (D) used was a mixture of 40% by mass of a fluid catalytic cracking catalyst containing 40% by mass of ultrastable Y-type zeolite and 60% by mass of an additive containing 39% by mass of shape-selective zeolite.
  • the crystal lattice constant of the ultrastable Y-type zeolite contained in the fluid catalytic cracking catalyst is 24.40 ⁇ .
  • Each of the fluid catalytic cracking catalyst and the additive was separately steamed at 100% steam for 6 hours at 810 ° C. before being charged to the apparatus. The results of the decomposition reaction are shown in Table 1.
  • Example 8 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 (Arabyanlite) desulfurized vacuum gas oil (desulfurized VGO) as in Example 2.
  • the catalyst used is the same catalyst (D) as in Example 7.
  • the results of the decomposition reaction are shown in Table 1.
  • Example 1 (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 raw material oil used was the same Middle Eastern (Arabian light) desulfurized atmospheric residue oil (desulfurized AR) as in Example 1.
  • the catalyst (E) used is a mixture of 80% by mass of a fluid catalytic cracking catalyst containing 40% by mass of an ultrastable Y-type zeolite and 20% by mass of an additive containing 30% by mass of a shape-selective zeolite.
  • the crystal lattice constant of the ultrastable Y-type zeolite contained in the fluid catalytic cracking catalyst is 24.40 ⁇ .
  • Each of the fluid catalytic cracking catalyst and the additive was separately steamed at 100% steam for 6 hours at 810 ° C. before being charged to the apparatus. The results of the decomposition reaction are shown in Table 1.
  • Comparative Example 2 (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 (Arabyanlite) desulfurized vacuum gas oil (desulfurized VGO) as in Example 2.
  • the catalyst used is the same catalyst (E) as in Comparative Example 1.
  • Table 1 The results of the decomposition reaction are shown in Table 1.
  • Example 3 (Comparative Example 3) Using the same apparatus as in Example 1, fluid catalytic cracking of heavy oil was performed under the same operating conditions.
  • the raw material oil used was the same Middle Eastern (Arabian light) desulfurized atmospheric residue oil (desulfurized AR) as in Example 1.
  • the catalyst (F) used is a mixture of 34% by mass of a fluid catalytic cracking catalyst containing 34% by mass of an ultrastable Y-type zeolite and 66% by mass of an additive containing 42% by mass of a shape-selective zeolite.
  • the crystal lattice constant of the ultrastable Y-type zeolite contained in the fluid catalytic cracking catalyst is 24.40 ⁇ .
  • Each of the fluid catalytic cracking catalyst and the additive was separately steamed at 100% steam for 6 hours at 810 ° C. before being charged to the apparatus. The results of the decomposition reaction are shown in Table 1.
  • Examples 1 to 8 fluid catalytic cracking was performed in an appropriate range of secondary cracking activity as compared with Comparative Examples 1 to 4, and as a result, light olefins were obtained in high yields.
  • ⁇ Coke / K which is an indicator of coke selectivity, is kept low while keeping the light olefin high, which is a preferable condition for the activity of the fluid catalytic cracking catalyst.

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  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Crystallography & Structural Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
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