US20170009146A1 - Process for fluid catalytic cracking of heavy oil - Google Patents

Process for fluid catalytic cracking of heavy oil Download PDF

Info

Publication number
US20170009146A1
US20170009146A1 US15/113,460 US201515113460A US2017009146A1 US 20170009146 A1 US20170009146 A1 US 20170009146A1 US 201515113460 A US201515113460 A US 201515113460A US 2017009146 A1 US2017009146 A1 US 2017009146A1
Authority
US
United States
Prior art keywords
catalyst
catalytic cracking
fluid catalytic
heavy oil
mass
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Abandoned
Application number
US15/113,460
Other languages
English (en)
Inventor
Hideki Ono
Tai Ohuchi
Marie Iwama
Tatsushi Ishizuka
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Eneos Corp
Original Assignee
JX Nippon Oil and Energy Corp
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by JX Nippon Oil and Energy Corp filed Critical JX Nippon Oil and Energy Corp
Assigned to JX NIPPON OIL & ENERGY CORPORATION reassignment JX NIPPON OIL & ENERGY CORPORATION ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: ISHIZUKA, TATSUSHI, OHUCHI, TAI, ONO, HIDEKI, IWAMA, MARIE
Publication of US20170009146A1 publication Critical patent/US20170009146A1/en
Abandoned legal-status Critical Current

Links

Images

Classifications

    • 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
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J29/00—Catalysts comprising molecular sieves
    • B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
    • B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
    • B01J29/08—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the faujasite type, e.g. type X or Y
    • 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
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/1033—Oil well production fluids
    • 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
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/107—Atmospheric residues having a boiling point of at least about 538 °C
    • 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
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/1077—Vacuum residues
    • 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 process for fluid catalytic cracking of a heavy oil, specifically to a fluid catalytic cracking process to produce light olefins such as propylene, butene or the like from a heavy oil at a high yield.
  • a fluid catalytic cracking unit as a unit for producing light olefins (particularly propylene) for use as petrochemical raw materials not as a unit for producing gasoline.
  • propylene, butene and the like are raw materials of alkylate and methyl-t-butyl ether (MTBE) that are high-octane gasoline blending stocks.
  • MTBE methyl-t-butyl ether
  • Examples of methods for producing light olefins by fluid catalytic cracking of a heavy oil include those comprising contacting a feedstock with a catalyst for a shortened period of time (Patent Literatures 1 to 4), that comprising carrying out a cracking reaction at elevated temperatures (Patent Literature 5), and those comprising using pentasyl type zeolites (Patent Literatures 6 and 7).
  • the reaction zone is a downflow type reaction zone that suppresses back mixing of a feedstock and the content of a rare-earth metal oxide in a fluid catalytic cracking catalyst and the mix ratio of an additive containing a shape selectivity zeolite are adjusted to further enhance the light olefin yield (Patent Literature 9).
  • Patent Literature 9 when the fluid catalytic cracking catalyst is insufficient in activity, these methods lack in cracking of a heavy feedstock and thus have not achieved the maximization of the light olefin yield.
  • Patent Literature 1 U.S. Pat. No. 4,419,221
  • Patent Literature 2 U.S. Pat. No. 3,074,878
  • Patent Literature 3 U.S. Pat. No. 5,462,652
  • Patent Literature 4 Europe Patent No. 315,179A
  • Patent Literature 5 U.S. Pat. No. 4,980,053
  • Patent Literature 6 U.S. Pat. No. 5,326,465
  • Patent Literature 7 Japanese Patent Laid-Open Translation No. 7-506389
  • Patent Literature 8 Japanese Patent Application Laid-Open Publication No. 10-60453
  • Patent Literature 9 Japanese Patent No. 3948905
  • the present invention has an object to provide a process for fluid catalytic cracking of heavy oil which can produce light olefins at a high yield and decrease the amount of dry gas generated by thermal cracking with a specific combination of a reaction mode, reaction conditions, a catalyst and the like.
  • the present invention has been accomplished on the basis of the finding that the above object is achieved by fluid catalytic cracking of a heavy oil using a catalyst containing a specific fluid catalytic cracking catalyst under specific conditions.
  • the present invention relates to a process for fluid catalytic cracking of a heavy oil to produce light olefins, comprising contacting the heavy oil with a catalyst comprising as a constituent thereof a fluid catalytic cracking catalyst with a weight ratio (Wmat/Wusy) of an active matrix weight (Wmat) to an ultrastable Y type zeolite weight (Wusy) of 0 to 0.3, under conditions where the reaction zone outlet temperature is from 580 to 630° C., the catalyst/oil ratio is from 15 to 40 weight/weight and the residence time of hydrocarbon in the reaction zone is from 0.1 to 1.0 second.
  • the present invention also relates to the foregoing process for fluid-catalytic cracking of heavy oil wherein the catalyst comprises 50 to 95 percent by mass of the fluid catalytic cracking catalyst and 5 to 50 percent by mass of an additive comprising a shape selectivity zeolite.
  • the present invention also relates to the foregoing process for fluid-catalytic cracking of heavy oil wherein the content of the ultrastable Y type zeolite in the fluid catalytic cracking catalyst is from 5 to 50 percent by mass.
  • the present invention also relates to the foregoing process for fluid-catalytic cracking of heavy oil wherein the ultrastable Y type zeolite has a crystal lattice constant of 24.20 to 24.60 ⁇ .
  • the present invention also relates to the foregoing process for fluid-catalytic cracking of heavy oil wherein the content of a rare-earth metal oxide in the fluid catalytic cracking catalyst is 1.5 percent by mass or less.
  • the present invention also relates to the foregoing process for fluid-catalytic cracking of heavy oil wherein a fluid catalytic cracking reactor having a downflow type reaction zone, a gas-solid separation zone, a stripping zone and a catalyst regeneration zone is used.
  • the present invention can produce light olefins such as propylene and butene at a high yield with a less amount of dry gas generated by thermal cracking.
  • 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 present invention is a process for fluid catalytic cracking of heavy oil to produce light olefins.
  • fluid catalytic cracking is referred to as a process wherein a heavy oil is continuously brought into contact with a catalyst that is maintained in a fluidized state to be cracked to light olefins and light hydrocarbons mainly composed of gasoline.
  • the fluid catalytic cracking unit used herein may be a fluid catalytic cracking unit having a reaction zone, a gas-solid separation zone, a stripping zone and a catalyst regeneration zone.
  • the reaction zone may be, for example, a so-called riser reaction zone wherein both catalyst particles and a feedstock ascend through a pipe or a downflow type (downer) reaction zone wherein both catalyst particles and a feedstock descend through a pipe.
  • the cracked reaction mixture comprising a mixture of a cracked reaction product having been subjected to fluid catalytic cracking in the reaction zone, an unreacted product and the used catalyst is then forwarded to a gas-solid separation zone, in which most of the hydrocarbons comprising the cracked reaction product and unreacted product are removed from the catalyst particles. If necessary, the cracked reaction mixture is quenched immediately upstream or immediately downstream of the gas-solid separation zone so as to suppress unnecessary thermal cracking or excessive cracking.
  • the used catalyst from which most of the hydrocarbons have been removed is then forwarded to the stripping zone to remove the hydrocarbons that have not been removed in the gas-solid separation zone using gas for stripping.
  • the used catalyst having carbonaceous materials and a portion of heavy hydrocarbons deposited thereon is forwarded from the stripping zone to the catalyst regeneration zone to regenerate the used catalyst.
  • the used catalyst is regenerated by being subjected to oxidation to remove the carbonaceous material and heavy hydrocarbons deposited and adhered on the catalyst.
  • the catalyst having been regenerated by oxidation is again forwarded to the reaction zone and continuously recycled thereto.
  • FIG. 1 shows an example of a fluid catalytic cracking reactor having a downflow mode reaction zone, a gas-solid separation zone, a stripping zone and a catalyst regeneration zone. The present invention will be described with reference to FIG. 1 below.
  • a heavy oil that is a feedstock is supplied through a line 10 to a mixing area 7 , in which it is mixed with a regenerated catalyst recycled from a catalyst reservoir 6 .
  • the mixture flows co-currently down through a reaction zone 1 , during which the feed heavy oil and the catalyst contact each other at an elevated temperature for a short period of time so as to crack the heavy oil.
  • the cracked reaction mixture flows from the reaction zone 1 downwardly to a gas-solid separation zone 2 located below the reaction zone 1 , in which the used catalyst is separated from the cracked reaction product and unreacted materials and then led through a dipleg 9 to an upper portion of a stripping zone 3 .
  • Hydrocarbon gas from which a majority of the used catalyst have been removed is then led to a secondary separator 8 .
  • This separator a slight amount of the used catalyst remaining in the hydrocarbon gas is removed, and the hydrocarbon gas is extracted out of the system to be recovered.
  • the secondary separator 8 is preferably a tangential cyclone.
  • the stripping conditions are usually those including 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.
  • the cracked reaction products and unreacted materials deposited and remaining on the used catalyst are removed and extracted out of the stripping zone 3 through a line 12 extending from the top thereof together with the stripping gas to be led to a recovery system.
  • the used catalyst having been stripped is fed to the catalyst regeneration zone 4 through a line provided with a first flow rate regulator 13 .
  • the catalyst regeneration zone 4 is segmented to an upper conical section and a lower cylindrical vessel section, the upper conical section being communicated with an upright tube (riser type regenerator) 5 .
  • the catalyst regeneration zone 4 has an upper conical section with an apex angle of usually 30 to 90 degrees and a height of 1 ⁇ 2 to 2 times of the diameter of the lower cylindrical section.
  • regeneration gas typically air such as oxygen-containing gas
  • the regeneration conditions are usually those including a temperature of 600 to 1000° C., preferably 650 to 750° C., a catalyst residence time of 1 to 5 minutes and a gas superficial velocity of preferably 0.4 to 1.2 m/s.
  • the regenerated catalyst regenerated in the regeneration zone 4 and flying out from an upper portion of a turbulent fluid bed is transferred from the upper conical section to a riser type regenerator 5 by being accompanied with the used regeneration gas.
  • the riser type regenerator 5 communicating with the upper conical section of the catalyst regeneration zone 4 has a diameter that is preferably 1 ⁇ 6 to 1 ⁇ 3 of the diameter of the lower cylindrical portion.
  • the regenerated catalyst ascending through the riser type regenerator 5 is conveyed to a catalyst reservoir 6 disposed on the top of the riser type regenerator.
  • the catalyst reservoir 6 also functions as a gas-solid separator, in which the used regeneration gas containing carbon dioxide is separated from the regenerated catalyst and discharged through the cyclone 15 out of the system.
  • the regenerated catalyst in the catalyst reservoir 6 is supplied to a mixing area 7 through a downward flow pipe provided with a second flow rate regulator 17 .
  • the regenerated catalyst in the catalyst reservoir 6 may be partially returned to the catalyst regeneration zone 4 via a bypass conduit provided with a third flow rate regulator 16 .
  • the catalyst is circulated in the system in the order of the downflow type reaction zone 1 , the gas-solid separation zone 2 , the stripping zone 3 , the catalyst regeneration zone 4 , the riser type regenerator 5 , the catalyst reservoir 6 and the mixing area 7 and again the downflow type reaction zone 1 .
  • the heavy oil used as the feedstock has distillation characteristics of a boiling point range of preferably 170 to 800° C., more preferably 190 to 780° C.
  • reaction zone outlet temperature is an outlet temperature of the reaction zone and is a temperature immediately before separation of the cracked reaction product from the catalyst or immediately before quenching thereof in the case where they are quenched immediately upstream of the gas-solid separation zone.
  • the reaction zone outlet temperature in the present invention is in a range of 580 to 630° C., preferably 590 to 620° C. If the temperature is lower than 580° C., light olefins will not be produced at a high yield while if the temperature is higher than 630° C., thermal cracking will occur remarkably, causing an increase in the amount of generated dry gas.
  • the catalyst/oil ratio referred herein is a ratio of the catalyst circulation rate (ton/h) and the feedstock feeding rate (ton/h).
  • the catalyst/oil ratio is necessarily 15 to 40 weight/weight, preferably 20 to 30 weight/weight. If the catalyst/oil ratio is smaller than 15 weight/weight, the temperature of the regenerated catalyst to be supplied to the reaction zone will be increased due to the heat balance, causing an increase in the amount of dry gas generated by thermal cracking. If the catalyst/oil ratio is greater than 40 weight/weight, the catalyst circulation rate will increase and thus the capacity of the catalyst regeneration zone will be undesirably too large to secure a catalyst residence time needed to regenerate the catalyst in the catalyst regeneration zone.
  • the residence time of hydrocarbons referred herein is either a time from the start of contact of the catalyst and feedstock till the separation of the catalyst from the resulting cracked reaction product in the reaction zone outlet or a time from the start of contact of the catalyst and feedstock till the quenching if the cracked reaction product is quenched immediately upstream of the gas-solid separation zone.
  • the residence time is necessarily 0.1 to 1.0 second, preferably 0.2 to 0.7 second. If the residence time of hydrocarbon in the reaction zone is shorter than 0.1 second, the cracking reaction will be insufficient, resulting in a failure to produce light olefins at a high yield. If the residence time is longer than 1.0 second, thermal cracking involves too much.
  • the main component of the zeolite is an ultrastable Y type zeolite.
  • the matrix comprises an active matrix, a binder (silica or the like), a filler (clay mineral or the like), and other components (rare-earth metal oxide, metal trap component or the like).
  • the active matrix has a cracking activity and may be alumina or silica-alumina.
  • a fluid catalytic cracking catalyst When a heavy feedstock is subjected to fluid catalytic cracking, a fluid catalytic cracking catalyst generally contains an active matrix so as to crack crudely the feedstock to be in such a form that can be cracked with an ultrastable Y type zeolite, but a catalyst with a less content of an active matrix can obtain a higher cracking activity under the preferable conditions for the present invention.
  • the fluid catalytic cracking catalyst of the present invention has a ratio of (Wmat/Wusy) of an active matrix weight (Wmat) to an ultrastable Y type zeolite weight (Wusy) in the range of necessarily 0 to 0.3, preferably 0 to 0.28.
  • the content of the rare-earth metal oxide in the fluid catalytic cracking catalyst is preferably 1.5 percent by mass or less, more preferably 1.2 percent by mass or less, particularly preferably 1.0 percent by mass or less. If the content of the rare-earth metal oxide in the fluid catalytic cracking catalyst is more than 1.5 percent by mass, the resulting catalyst will be too high in hydrogen transfer activity and thus be decreased in the yield of light olefins though be high in cracking activity.
  • the ultrastable Y type zeolite has a crystal lattice constant of preferably 24.20 to 24.60 ⁇ , more preferably 24.36 to 24.45 ⁇ . Within these ranges, the smaller that crystal lattice constant is, the lesser the gasoline yield is but the more the light olefin yield is. However, if the crystal lattice constant is smaller than 24.20 ⁇ , the resulting fluid catalytic cracking catalyst is too low in cracking activity to obtain a high conversion rate and is decreased in the light olefin yield. If the lattice constant is larger than 24.60 ⁇ , the resulting catalyst will be too high in hydrogen transfer activity.
  • the crystal lattice constant of a zeolite referred herein is measured in accordance with ASTM D-3942-80.
  • the content of the ultrastable Y type zeolite in the fluid catalytic cracking catalyst is preferably 5 to 50 percent by mass, more preferably 15 to 40 percent by mass.
  • the fluid catalytic cracking catalyst preferably has a bulk density of 0.5 to 1.0 g/ml, an average particle diameter of 50 to 90 ⁇ m, a surface area of 50 to 350 m 2 /g, and a pore volume of 0.05 to 0.5 ml/g.
  • the additive that is a constituent of the catalyst used in the present invention contains a shape selectivity zeolite.
  • constituents other than the shape selectivity zeolite include binders (silica or the like), fillers (clay mineral or the like) and the like.
  • the shape selectivity zeolite is a zeolite with a pore size smaller than that of the Y type zeolite so that only hydrocarbons with limited shapes can enter the pores.
  • zeolites include ZSM-5, ⁇ , omega, SAPO-5, SAPO-11, SAPO-34, and pentasil type metallosilicate.
  • ZSM-5 is most preferably used.
  • the content of the shape selectivity zeolite in the additive is preferably from 20 to 70 percent by mass, more preferably from 30 to 60 percent by mass.
  • the additive has preferably a bulk density of 0.5 to 1.0 g/ml, an average particle diameter of 50 to 90 ⁇ m, a surface area of 10 to 200 m 2 /g, and a pore volume of 0.01 to 0.3 ml/g.
  • the ratio of the fluid catalytic cracking catalyst and additive in the catalyst used in the present invention is 50 to 95 percent by mass, preferably 55 to 90 percent by mass of the fluid catalytic cracking catalyst and 5 to 50 percent by mass, preferably 10 to 45 percent by mass of the additive containing a shape selectivity zeolite. If the ratio of the fluid catalytic cracking catalyst is less than 50 percent by mass, or the ratio of the additive is more than 50 percent by mass, the conversion rate of a feedstock that is a heavy oil will be decreased and a higher light olefin yield cannot be obtained. Whilst, the ratio of the fluid catalytic cracking catalyst is more than 95 percent by mass, or the ratio of the additive is less than 5 percent by mass, a high conversion rate can be obtained but a higher light olefin yield cannot be obtained.
  • Fluid catalytic cracking of a heavy oil was carried our using a downflow reactor (downer) type FCC pilot unit.
  • the scale of the device includes an inventory of 5 kg and a feed amount of 1 kg/h while the operation conditions include a reaction zone outlet temperature of 600° C., a reaction pressure of 196 kPa (1.0 kg/cm 2 G), a catalyst/oil ratio of 25 weight/weight, and a catalyst regeneration zone temperature of 720° C.
  • the residence time of hydrocarbon in the reactor was 0.5 second.
  • the feedstock used in this example was a desulfurized atmospheric residue (desulfurized AR) of an oil produced in the Middle East (Arabian light).
  • the catalyst used in this example was a mixture of 75 percent by mass of fluid catalytic cracking catalyst (A) and 25 percent by mass of an additive containing ZSM-5 (produced by Davison under the trade name of OlefinsMax).
  • Fluid catalytic cracking catalyst (A) contains an active matrix and an ultrastable Y type zeolite at a ratio (Wmat/Wusy) of the active matrix weight (Wmat) to the ultrastable Y type zeolite weight (Wusy) of 0 (zero), and has a crystal lattice constant of 24.40 ⁇ .
  • Prior to being fed to the unit, fluid catalytic cracking catalyst (A) and the additive were separately subjected to steaming at 810° C. for 6 hours with 100% steam. The results of the cracking reaction are set forth in Table 1.
  • Fluid catalytic cracking of a heavy oil was conducted under the same conditions as those of Example 1 using the same unit as that of Example 1.
  • the feedstock used in this example is the same as the desulfurized atmospheric residue (desulfurized AR) of an oil produced in the Middle East (Arabian light) used in Example 1.
  • Fluid catalytic cracking catalyst (B) used in this example contains an active matrix and an ultrastable Y type zeolite at a ratio (Wmat/Wusy) of the active matrix weight (Wmat) to the ultrastable Y type zeolite weight (Wusy) of 0.13.
  • the results of the cracking reaction are set forth in Table 1.
  • Fluid catalytic cracking of a heavy oil was conducted under the same conditions as those of Example 1 using the same unit as that of Example 1.
  • the feedstock used in this example is the same as the desulfurized atmospheric residue (desulfurized AR) of an oil produced in the Middle East (Arabian light) used in Example 1.
  • Fluid catalytic cracking catalyst (C) used in this example contains an active matrix and an ultrastable Y type zeolite at a ratio (Wmat/Wusy) of the active matrix weight (Wmat) to the ultrastable Y type zeolite weight (Wusy) of 0.26, and has a rare-earth metal oxide content of 1.50 percent by mass.
  • Table 1 The results of the cracking reaction are set forth in Table 1.
  • Fluid catalytic cracking of a heavy oil was conducted under the same conditions as those of Example 1 using the same unit as that of Example 1.
  • the feedstock used in this example is a desulfurized vacuum gas oil (desulfurized VGO) of the same oil produced in the Middle East (Arabian light) used in Example 1.
  • Fluid catalytic cracking catalyst (A) used in this example contains an active matrix and an ultrastable Y type zeolite at a ratio (Wmat/Wusy) of the active matrix weight (Wmat) to the ultrastable Y type zeolite weight (Wusy) of 0 (zero). The results of the cracking reaction are set forth in Table 1.
  • Fluid catalytic cracking of a heavy oil was conducted under the same conditions as those of Example 1 using the same unit as that of Example 1.
  • the feedstock used in this example is a desulfurized vacuum gas oil (desulfurized VGO) of the same oil produced in the Middle East (Arabian light) used in Example 1.
  • Fluid catalytic cracking catalyst (B) used in this example contains an active matrix and an ultrastable Y type zeolite at a ratio (Wmat/Wusy) of the active matrix weight (Wmat) to the ultrastable Y type zeolite weight (Wusy) of 0.13.
  • the results of the cracking reaction are set forth in Table 1.
  • Fluid catalytic cracking of a heavy oil was conducted under the same conditions as those of Example 1 using the same unit as that of Example 1.
  • the feedstock used in this example is a desulfurized vacuum gas oil (desulfurized VGO) of the same oil produced in the Middle East (Arabian light) used in Example 1.
  • Fluid catalytic cracking catalyst (C) used in this example contains an active matrix and an ultrastable Y type zeolite at a ratio (Wmat/Wusy) of the active matrix weight (Wmat) to the ultrastable Y type zeolite weight (Wusy) of 0.26, and has a rare-earth metal oxide content of 1.50 percent by mass.
  • Table 1 The results of the cracking reaction are set forth in Table 1.
  • Fluid catalytic cracking of a heavy oil was carried out under the same conditions as those of Example 2 except for using a catalyst that is a mixture of 53 percent by mass of fluid catalytic cracking catalyst (B) and 47 percent by mass of an additive containing ZSM-5 (produced by Davison under the trade name of OlefinsMax).
  • B fluid catalytic cracking catalyst
  • ZSM-5 produced by Davison under the trade name of OlefinsMax
  • Fluid catalytic cracking of a heavy oil was conducted under the same conditions as those of Example 1 using the same unit as that of Example 1.
  • the feedstock used in this example is the same as the desulfurized atmospheric residue (desulfurized AR) of an oil produced in the Middle East (Arabian light) used in Example 1.
  • Fluid catalytic cracking catalyst (D) used in this example contains an active matrix and an ultrastable Y type zeolite at a ratio (Wmat/Wusy) of the active matrix weight (Wmat) to the ultrastable Y type zeolite weight (Wusy) of 0.50, and has a rare-earth metal oxide content of 0 (zero).
  • Table 1 The results of the cracking reaction are set forth in Table 1.
  • Fluid catalytic cracking of a heavy oil was conducted under the same conditions as those of Example 1 using the same unit as that of Example 1.
  • the feedstock used in this example is the same as the desulfurized vacuum gas oil (desulfurized VGO) of an oil produced in the Middle East (Arabian light) used in Example 4.
  • Fluid catalytic cracking catalyst (D) used in this example contains an active matrix and an ultrastable Y type zeolite at a ratio (Wmat/Wusy) of the active matrix weight (Wmat) to the ultrastable Y type zeolite weight (Wusy) of 0.50, and has a rare-earth metal oxide content of 0 (zero).
  • Table 1 The results of the cracking reaction are set forth in Table 1.
  • Fluid catalytic cracking of a heavy oil was carried out using an upflow reactor (riser) type FCC pilot unit.
  • the scale of the device includes an inventory of 3 kg and a feed amount of 1 kg/h, and the operation conditions include a reaction zone outlet temperature of 520° C., a reaction pressure of 196 kPa (1.0 kg/cm 2 G), a catalyst/oil ratio of 5 weight/weight, and a catalyst regeneration zone temperature of 720° C.
  • the residence time of hydrocarbon in this reactor was 1.5 second.
  • the feedstock used in this example was a desulfurized atmospheric residue (desulfurized AR) of an oil produced in the Middle East (Arabian light).
  • the catalyst used this example was a mixture of 75 percent by mass of fluid catalytic cracking catalyst (A) and 25 percent by mass of an additive containing ZSM-5 (produced by Davison under the trade name of OlefinsMax).
  • Fluid catalytic cracking catalyst (A) contains an active matrix and an ultrastable Y type zeolite at a ratio (Wmat/Wusy) of the active matrix weight (Wmat) to the ultrastable Y type zeolite weight (Wusy) of 0 (zero), and has a crystal lattice constant of 24.40 ⁇ .
  • Prior to being fed to the unit, fluid catalytic cracking catalyst (A) and the additive were separately subjected to steaming at 810° C. for 6 hours with 100% steam. The results of the cracking reaction are set forth in Table 1.
  • Fluid catalytic cracking of a heavy oil was conducted under the same conditions as those of Example 3 using the same unit as that of Example 3.
  • the feedstock used in this example is a desulfurized atmospheric residue (desulfurized AR) of an oil produced in the Middle East (Arabian light) used in Example 1.
  • the catalyst used in this example is the same as fluid catalytic cracking catalyst (B) used in Example 2, which contains an active matrix and an ultrastable Y type zeolite at a ratio (Wmat/Wusy) of the active matrix weight (Wmat) to the ultrastable Y type zeolite weight (Wusy) of 0.13.
  • the results of the cracking reaction are set forth in Table 1.
  • Fluid catalytic cracking of a heavy oil was carried out under the same conditions as those of comparative Example 3 using the same unit as that of Comparative Example 3.
  • the feedstock used in this example is a desulfurized atmospheric residue (desulfurized AR) of the same oil produced in the Middle East (Arabian light) used in Example 1.
  • Fluid catalytic cracking catalyst (C) used in this example contains an active matrix and an ultrastable Y type zeolite at a ratio (Wmat/Wusy) of the active matrix weight (Wmat) to the ultrastable Y type zeolite weight (Wusy) of 0.26, and has a rare-earth metal oxide content of 1.50 percent by mass.
  • Table 1 The results of the cracking reaction are set forth in Table 1.
  • Fluid catalytic cracking of a heavy oil was carried out under the same operation conditions as those of Example 5 except for using an upflow reactor (riser) type FCC pilot unit instead of the downflow reactor (downer) type FCC pilot unit.
  • the results are set forth in Table 1.
  • Example 1 Example 2 Example 3 Example 4 Example 5 Example 6 Example 7 Fluid catalytic catalyst mass % 75 75 75 75 75 53 Additive mass % 25 25 25 25 25 25 47 Catalyst name Catalyst (A) Catalyst (B) Catalyst (C) Catalyst (A) Catalyst (B) Catalyst (C) Catalyst (B) Catalyst USY zeolite mass % 45 40 38 45 40 38 40 38 40 composition Active matrix mass % #REF! 5 10 #REF!

Landscapes

  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Crystallography & Structural Chemistry (AREA)
  • Materials Engineering (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
US15/113,460 2014-01-24 2015-01-20 Process for fluid catalytic cracking of heavy oil Abandoned US20170009146A1 (en)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
JP2014011632A JP6234829B2 (ja) 2014-01-24 2014-01-24 重質油の流動接触分解法
JP2014-011632 2014-01-24
PCT/JP2015/051347 WO2015111566A1 (ja) 2014-01-24 2015-01-20 重質油の流動接触分解法

Publications (1)

Publication Number Publication Date
US20170009146A1 true US20170009146A1 (en) 2017-01-12

Family

ID=53681369

Family Applications (1)

Application Number Title Priority Date Filing Date
US15/113,460 Abandoned US20170009146A1 (en) 2014-01-24 2015-01-20 Process for fluid catalytic cracking of heavy oil

Country Status (6)

Country Link
US (1) US20170009146A1 (ko)
EP (1) EP3098287A4 (ko)
JP (1) JP6234829B2 (ko)
KR (1) KR20160113122A (ko)
CN (1) CN105980527B (ko)
WO (1) WO2015111566A1 (ko)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20180260314A1 (en) * 2017-03-09 2018-09-13 Accenture Global Solutions Limited Smart advisory for distributed and composite testing teams based on production data and analytics

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP6971160B2 (ja) * 2018-02-01 2021-11-24 出光興産株式会社 粉体移送配管及びこれを備える装置

Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20010042701A1 (en) * 2000-04-17 2001-11-22 Stuntz Gordon F. Cycle oil conversion process
JP2002241764A (ja) * 2001-02-21 2002-08-28 Petroleum Energy Center 重質油の流動接触分解法

Family Cites Families (14)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3074878A (en) 1957-10-18 1963-01-22 Exxon Research Engineering Co Short contact time system
US4419221A (en) 1981-10-27 1983-12-06 Texaco Inc. Cracking with short contact time and high temperatures
CN1004878B (zh) 1987-08-08 1989-07-26 中国石油化工总公司 制取低碳烯烃的烃类催化转化方法
US4985136A (en) 1987-11-05 1991-01-15 Bartholic David B Ultra-short contact time fluidized catalytic cracking process
EP0639217B1 (en) 1992-05-04 1998-09-30 MOBIL OIL CORPORATION (a New York corporation) Fluidized catalytic cracking
CN1031646C (zh) 1992-10-22 1996-04-24 中国石油化工总公司 石油烃的催化转化方法
US5462652A (en) 1993-09-24 1995-10-31 Uop Short contact FCC process with catalyst blending
JP3580518B2 (ja) 1996-06-05 2004-10-27 新日本石油株式会社 重質油の流動接触分解法
JP3574555B2 (ja) * 1996-11-15 2004-10-06 新日本石油株式会社 重質油の流動接触分解方法
WO2000031215A1 (en) * 1998-11-24 2000-06-02 Mobil Oil Corporation Catalytic cracking for olefin production
JP4223690B2 (ja) * 2001-02-21 2009-02-12 財団法人 国際石油交流センター 重質油の流動接触分解方法
JP3950437B2 (ja) * 2003-07-08 2007-08-01 キング ファハド ユニバーシティ オブ ペトロリアム アンド ミネラルズ 重質油の流動接触分解法
JP5390833B2 (ja) * 2008-11-06 2014-01-15 日揮触媒化成株式会社 炭化水素油の流動接触分解触媒
FR2986799B1 (fr) * 2012-02-15 2015-02-06 IFP Energies Nouvelles Procede de conversion d'une charge lourde, mettant en oeuvre une unite de craquage catalytique et une etape d'hydrogenation selective de l'essence issue du craquage catalytique

Patent Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20010042701A1 (en) * 2000-04-17 2001-11-22 Stuntz Gordon F. Cycle oil conversion process
JP2002241764A (ja) * 2001-02-21 2002-08-28 Petroleum Energy Center 重質油の流動接触分解法

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20180260314A1 (en) * 2017-03-09 2018-09-13 Accenture Global Solutions Limited Smart advisory for distributed and composite testing teams based on production data and analytics

Also Published As

Publication number Publication date
CN105980527A (zh) 2016-09-28
JP6234829B2 (ja) 2017-11-22
CN105980527B (zh) 2018-09-21
JP2015137360A (ja) 2015-07-30
WO2015111566A1 (ja) 2015-07-30
KR20160113122A (ko) 2016-09-28
EP3098287A4 (en) 2017-09-20
EP3098287A1 (en) 2016-11-30

Similar Documents

Publication Publication Date Title
US10184088B2 (en) Fluid catalytic cracking process and apparatus for maximizing light olefins or middle distillates and light olefins
US6656346B2 (en) Fluid catalytic cracking process for heavy oil
RU2580829C2 (ru) Способ и устройство каталитического крекинга для получения пропилена
US20020195373A1 (en) Heavy oil fluid catalytic cracking process
JP2020517793A (ja) 炭化水素供給原料の蒸気接触ダウナー熱分解による軽質オレフィン収率の向上
CN107597026B (zh) 一种催化裂解的工艺和系统
CN105980531B (zh) 用于轻质烯烃生产的整合的溶剂脱沥青和流化催化裂化方法
US20110139683A1 (en) Fcc process with spent catalyst recycle
CN103732726A (zh) 用于制备中间馏分油和低级烯烃的双提升管催化裂化方法
US10266459B2 (en) Production of propylene in a fluid catalytic cracking unit
WO2011050587A1 (zh) 一种催化裂化装置和方法
JP2021531378A (ja) 炭化水素油の接触分解方法、反応器及システム
CN103703106A (zh) 用于制备中间馏分油和低级烯烃的双提升管催化裂化方法
JP3948905B2 (ja) 重質油の流動接触分解法
US20170009146A1 (en) Process for fluid catalytic cracking of heavy oil
JP4223690B2 (ja) 重質油の流動接触分解方法
US20170218281A1 (en) Process for fluid catalytic cracking of heavy oil
US20040140246A1 (en) Process for upgrading fcc product with additional reactor
CN111423905B (zh) 催化裂解的工艺和系统
US11685866B2 (en) Method for the conversion of feedstock containing naphtha to low carbon olefins and aromatics
JP2019089907A (ja) 軽質オレフィンの製造方法
RU2474606C2 (ru) Системы и способы получения средних дистиллятов и низших олефинов из углеводородного сырья
JP3724932B2 (ja) 油の流動接触分解方法
JP3724934B2 (ja) 油の流動接触分解方法
US11891356B2 (en) Production of high yields of light olefins from heavy hydrocarbons

Legal Events

Date Code Title Description
AS Assignment

Owner name: JX NIPPON OIL & ENERGY CORPORATION, JAPAN

Free format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNORS:ONO, HIDEKI;OHUCHI, TAI;IWAMA, MARIE;AND OTHERS;SIGNING DATES FROM 20160520 TO 20160524;REEL/FRAME:039217/0688

STCB Information on status: application discontinuation

Free format text: ABANDONED -- FAILURE TO RESPOND TO AN OFFICE ACTION