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EP1046696A2 - Verfahren zur katalytischen Umwandlung zum Herstellen von mit Isobutan und Isoparaffinen angereichertem Benzin - Google Patents

Verfahren zur katalytischen Umwandlung zum Herstellen von mit Isobutan und Isoparaffinen angereichertem Benzin Download PDF

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Publication number
EP1046696A2
EP1046696A2 EP20000108032 EP00108032A EP1046696A2 EP 1046696 A2 EP1046696 A2 EP 1046696A2 EP 20000108032 EP20000108032 EP 20000108032 EP 00108032 A EP00108032 A EP 00108032A EP 1046696 A2 EP1046696 A2 EP 1046696A2
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Prior art keywords
reaction
reaction zone
zone
catalyst
process according
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EP20000108032
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English (en)
French (fr)
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EP1046696B1 (de
EP1046696A3 (de
Inventor
Youhao Xu
Jiushun Zhang
Yinan Yang
Jun Long
Xieqing Wang
Zaiting Li
Ruichi Zhang
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Sinopec Research Institute of Petroleum Processing
China Petrochemical Corp
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Sinopec Research Institute of Petroleum Processing
China Petrochemical Corp
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Priority claimed from CN99105904A external-priority patent/CN1076751C/zh
Priority claimed from CN99109193A external-priority patent/CN1081222C/zh
Application filed by Sinopec Research Institute of Petroleum Processing, China Petrochemical Corp filed Critical Sinopec Research Institute of Petroleum Processing
Publication of EP1046696A2 publication Critical patent/EP1046696A2/de
Publication of EP1046696A3 publication Critical patent/EP1046696A3/de
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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

Definitions

  • This invention relates to a process for catalytic, conversion of hydrocarbon feedstock in the absence of added hydrogen. More particularly, the present invention relates to a catalytic conversion process for producing isobutane and isoparaffin-enriched gasoline.
  • the mixture of isoparaffins possessing high octane number, low octane sensitivity, appropriate volatility and clean burning is an ideal blending components for aviation gasoline and motor gasoline.
  • the mixture of isoparaffins can be obtained by propylene polymerization or alkylation reaction of isobutane and olefins.
  • the conventional fluidized catalytic cracking (FCC) technology is used for producing gasoline with a yield of up to 50wt%.
  • FCC fluidized catalytic cracking
  • the phase down of leaded gasoline forced the catalytic cracking technology to go forward to the production of high octane gasoline.
  • the changing market demands have resulted in a great change in technology and catalyst types.
  • the advance in technological development is to increase reaction temperature, shorten reaction time, intensify reaction severity, suppress hydrogen transfer reaction and overcracking reaction and improve the contacting efficiency between feedstock and hot catalyst at the bottom of a riser reactor.
  • catalyst development the catalysts containing USY zeolite supported on an inert or active matrix or containing different typed zeolites have been put into commercial use.
  • FCC technology has been advanced to meet octane blending requirement, whether it is by means of changing in process parameters or using novel catalysts for increasing gasoline octane number, it results in an increase in olefin content of FCC gasoline.
  • FCC liquid petroleum gas (LPG) has an olefin content of up to 70wt%, in which butylenes is several times as much as the yield of isobutane, so it is not fit to be used as feedstock for alkylation.
  • USP5,154,818 discloses a method for the fluidized catalytic cracking of plural hydrocarbon feedstocks in a riser reactor to produce more gasoline of high octane number.
  • the process generally comprises two reaction zones. A relatively light hydrocarbon feedstock contacts with spent catalyst in a first reaction zone located in the bottom of conventional riser where aromatization and oligomerization take place. All of the first reaction zone effluent, the regenerated catalyst and heavy hydrocarbon feedstock are introduced into the second reaction zone where heavy hydrocarbon feedstock is cracked to desired reaction products. The reaction products and spent catalyst then pass through disengager for removal of entrained catalyst before the hydrocarbon vapors pass into a separation system. Spent catalyst passes into stripper and is divided into two parts, one is introduced into regenerator for burning off coke, the other part is recycled to the first reaction zone.
  • USP4,090,948 discloses a catalytic cracking process for producing the desired conversion of hydrocarbon feedstock of inferior quality (having higher contents of basic nitrogen and carbon residue) to obtain higher yields of the desired products in a riser reactor.
  • the process generally comprises contacting the hydrocarbon feedstock containing the highly reactive nitrogen and carbon residue with a recycled spent catalyst in the first reaction zone where the highly reactive nitrogen and carbon residue will deposit on the spent catalyst and then contacting the resultant mixture with freshly regenerated catalyst in the second reaction zone.
  • the reaction products and spent catalyst then pass through disengager for removal of entrained catalyst before the hydrocarbon vapors pass into a separation system.
  • Spent catalyst passes into stripper and is divided into two parts, one is introduced into regenerator for burning off coke and then returned to the second reaction zone, and the other part is recycled without regeneration to the first reaction zone.
  • An object of the present invention is to provide a catalytic conversion process for producing isobutane and isoparaffin-enriched gasoline to meet the requirement for blending components of the RFG, i.e. limiting the olefin content on the premise of maintaining higher gasoline octane number.
  • the process provided by the present invention is to contact the preheated hydrocarbon feedstock with hot regenerated catalyst in the lower part of a reactor with the result that hydrocarbon cracking reaction takes place at higher reaction temperature and shorter reaction time, and then the resultant mixture is up-flowed and enters into a suitable reaction environment with the result that isomerization and hydrogen transfer reaction take place at lower reaction temperature and longer reaction time.
  • the reaction products and spent catalyst then pass through disengager for removal of entrained catalyst.
  • the reaction products flow into subsequent separation system. Spent catalyst is shipped with steam, and then flow into the regenerator for regeneration, and thereafter the hot regenerated catalyst is recycled to the lower part of the reactor.
  • the process provided by the present invention employs a reactor to carry on two different reactions under different operating conditions, said reactor is preferably selected from the group consisting of an iso-diameter riser, an iso-linear velocity riser, a multi-cascade riser, a fluidized bed or a combination reactor of an iso-diameter riser and a fluidized bed.
  • olefins produced by catalytic cracking reaction can be selectively converted into isoparaffins and aromatics or isoparaffins and coke under specific reaction conditions and with specific catalysts.
  • the invention is a process comprising: the preheated hydrocarbon feedstock is atomized with injection steam and charged into the bottom of a conventional iso-diameter riser, and then mixed with hot regenerated catalyst with the result that feedstock is vaporized and cracked.
  • the product vapors and the coke deposited catalyst are up-flowed and are mixed with cooled regenerated catalyst with the result that isomerization and hydrogen transfer reaction take place.
  • the reaction vapors and catalyst flow into disengager where entrained catalyst is separated and dropped into the catalyst stripper.
  • the reaction vapors are separated into products in subsequent separation system.
  • Spent catalyst is stripped and introduced into regenerator for regeneration. Regenerated catalyst is divided into two parts, one is recycled into the prelift zone of the riser, and the other part is cooled in catalyst cooler and then recycled into the second reaction zone.
  • this invention is a process comprising: the preheated hydrocarbon feedstock is atomized with injection steam and charged into the bottom of a conventional iso-diameter riser, and then mixed with hot regenerated catalyst with the result that the feedstock is vaporized and cracked.
  • the product vapors and the coke deposited catalyst are up-flowed and are mixed with cooled semi-regenerated catalyst with the result that isomerization and hydrogen transfer reaction take place.
  • the reaction vapors and catalyst flow into disengager where entrained catalyst is separated and dropped into the catalyst stripper.
  • the reaction vapors are separated into products in subsequent separation system.
  • Spent catalyst is stripped and introduced into the primary regenerator for regeneration.
  • Semi-regenerated catalyst is divided into two parts, one flows into the secondary regenerator for regeneration, and then is recycled into the prelift zone of the riser, and the other part is cooled in catalyst cooler and then recycled into the second reaction zone.
  • this invention is a process comprising: the preheated hydrocarbon feedstock is atomized with injection steam and charged into the bottom of the riser in a combination reactor of an iso-diameter riser and a fluidized bed, and then mixed with hot regenerated catalyst with the result that the feedstock is vaporized and cracked.
  • the product vapors and the coke deposited catalyst in the riser flow upward and are mixed with cooled regenerated catalyst with the result that isomerization and hydrogen transfer reaction take place in the fluidizied bed.
  • the reaction vapors and catalyst flow into disengager where entrained catalyst is separated and dropped into the catalyst stripper.
  • the reaction vapors are separated into products in subsequent separation system.
  • Spent catalyst is stripped and introduced into regenerator for regeneration. Regenerated catalyst is divided into two parts, one is recycled into the prelift zone of the riser, and the other part is cooled in catalyst cooler and then recycled into the fluidized bed.
  • this invention comprises that the preheated hydrocarbon feedstock is atomized with injection steam and charged into the bottom of the first reaction zone in a multi-cascade riser, and then mixed with hot regenerated large particle size distribution catalyst containing USY zeolite with the result that feedstock is vaporized and cracked, providing the lifting force to carry die product vapors and the coke deposited catalyst in the first reaction zone into the second reaction zone where the effluents are mixed with the cooled regenerated small particle size distribution catalyst containing rare-earth Y zeolite with the result that isomerization and hydrogen transfer reaction take place.
  • the reaction vapors and catalyst flow into disengager where entrained catalyst is separated and dropped into the catalyst stripper.
  • reaction vapors are separated into products in subsequent separation system.
  • Spent catalyst is stripped and introduced into regenerator for regeneration.
  • Regenerated catalyst is divided into the large particle size distribution catalyst and the small particle size distribution catalyst, the large particle size distribution catalyst is recycled into the prelift zone of the riser, and the small particle size distribution catalyst is cooled in catalyst cooler and then recycled into the second reaction zone.
  • the process of the present invention comprises the steps as follows:
  • the process provided by the present invention employs a reactor to carry on two different reactions under different operating conditions; it is preferably selected from the group consisting of an iso-diameter riser, an iso-linear velocity riser, a multi-cascade riser, a fluidized bed or a combination of an iso-diameter riser and a fluidized bed.
  • the iso-diameter riser or iso-liner velocity riser is divided into a prelift zone, a first reaction zone, a second reaction zone from bottom to top, while the fluidized bed reactor comprises only a first reaction zone and a second reaction zone.
  • the height ratio of the first reaction zone to the second reaction zone is 10 ⁇ 40:90 ⁇ 60.
  • quenching mediums is set up at the bottom of the second reaction zone, and/or a heat remover having a height of about 50% ⁇ 90% of that of the second reaction zone is located in the second reaction zone for adjusting the reaction temperature and time in the reaction zone.
  • said quenching medium is generally one or more selected from the group consisting of quenching liquids, cooled regenerated catalyst cooled semi-regenerated catalyst or fresh catalyst or the mixtures thereof, in which quenching liquid is preferably selected from the group consisting of LPG, naphtha, stabilized gasoline, light cycle oil (LCO), heavy cycle oil (HCO) or water or the mixtures thereof.
  • LPG, naphtha and gasoline having high olefin content can not only act as quenching mediums, but also participate in reaction.
  • the cooled regenerated and semi-regenerated catalysts are obtained by cooling catalyst through catalyst cooler after the primary stage and secondary stage regeneration respectively.
  • said regenerated catalyst refers to catalyst that has a residual carbon content of below 0.1 wt%, more preferably below about 0.05wt%
  • said semi-regenerated catalyst refers to catalyst that has a residual carbon content of from about 0.1 wt% to about 0.9wt%, more preferably from about 0.15wt% to about 0.7wt%.
  • the process of the present invention is carried out in a combination reactor of an iso-diameter riser and a fluidized bed, wherein the lower iso-diameter riser refers to the first reaction zone, the upper fluidized bed refers to the second reaction zone.
  • One inlet or multi-inlets of quenching mediums is set up at the bottom of the second reaction zone and/or a heat remover having a height of about 50% ⁇ 90% of that of the second reaction zone is located in the second reaction zone for adjusting the reaction temperature and time in the reaction zone.
  • said quenching medium is generally one or more selected from the group consisting of quenching liquid, cooled regenerated catalyst , cooled semi-regenerated catalyst or fresh catalyst or the mixtures thereof, in which quenching liquid is preferably selected from the group consisting of LPG, naphtha, stabilized gasoline, light cycle oil (LCO), heavy cycle oil (HCO) or water or the mixtures thereof.
  • LPG, naphtha and gasoline having high olefin content can not only act as quenching mediums, but also participate in reaction.
  • the cooled regenerated and semi-regenerated catalysts are obtained by cooling catalyst through catalyst cooler after the primary stage and secondary stage regeneration respectively.
  • said regenerated catalyst refers to catalyst that has a residual carbon content of below 0.1 wt%, more preferably below about 0.05wt%
  • said semi-regenerated catalyst refers to catalyst that has a residual carbon content of from about 0.1 wt% to about 0.9wt%, more preferably from about 0.15wt% to about 0.7wt%.
  • the riser consists of a prelift zone a, a first reaction zone b, a second reaction zone with enlarged diameter c, the outlet zone with reduced diameter d from bottom to top along the coaxial direction.
  • the end of outlet zone is connected to a horizontal tube e.
  • the conjunct section between the first reaction zone and the second reaction zone is a circular truncated cone whose vertical section isotrapezia vertex angle ⁇ is generally about 30° ⁇ 80° .
  • the conjunct section between the second reaction zone and the outlet zone is a circular truncated cone whose vertical section isotrapezia base angle ⁇ is generally about 45° ⁇ 85°.
  • the total height of the riser is generally from about 10 meters to about 60 meters.
  • the diameter of the prelift zone is the same as that of a conventional iso-diameter riser and generally from about 0.02 meter to about 5 meters.
  • the height of die prelift zone is about 5% ⁇ 10% of the total height of the riser. The function of this zone is to lift regenerated catalyst upward and to improve initial feed and catalyst contacting with the aid of a prelift medium that is selected from steam or dry gas same as that used in a conventional iso-diameter riser reactor.
  • the structure of the first reaction zone of the riser is similar to the lower section of a conventional iso-diameter riser. Its diameter is equal to or greater than that of the prelift zone. The diameter ratio of the former to the latter is generally from about 1:1 to about 2:1. The height of the first reaction zone is about 10% ⁇ 30% of the total height of the riser.
  • the preheated feedstocks are atomized with injection steam and charged into this section, and then mixed with hot regenerated catalyst with result that cracking reaction takes place at higher reaction temperature and C/O ratio and shorter reaction time.
  • the diameter of the second reaction zone is greater than that of the first reaction zone.
  • the diameter ratio of the former to the latter is generally from about 1.5:1 to about 5:1.
  • the height of the second reaction zone is about 30 ⁇ 60% of the total height of the riser.
  • the function of this zone is to reduce the velocity of vapors and catalyst and the reaction temperature in order to suppress cracking reaction and increase isomerization reaction and hydrogen transfer reaction.
  • the method of controlling the second reaction temperature is to inject quenching mediums at the conjunct section between the first reaction zone and the second reaction zone and/or to install a heat remover in the zone.
  • the height of the heat remover is generally from about 50% to about 90% of that of the second reaction zone.
  • the zone temperature is generally from about 420°C to about 550°C.
  • the contacting time of vapor and catalyst is generally from about 2 seconds to about 30 seconds.
  • said quenching medium is generally one or more selected from the group consisting of quenching liquids cooled regenerated catalyst , cooled semi-regenerated catalyst or fresh catalyst or the mixtures thereof, in which quenching liquid is preferably selected from the group consisting of LPG, naphtha, stabilized gasoline, light cycle oil (LCO), heavy cycle oil (HCO) or water or the mixtures thereof LPG, naphtha and gasoline having high olefin content can not only act as quenching mediums, but also participate in reaction.
  • the cooled regenerated and semi-regenerated catalysts are obtained by cooling catalyst through catalyst cooler after the primary stage and secondary stage regeneration respectively.
  • said regenerated catalyst refers to catalyst that has a residual carbon content of below 0.1 wt%, more preferably below about 0.05wt%
  • said semi-regenerated catalyst refers to catalyst that has a residual carbon content of from about 0.1 wt% to about 0.9wt%, more preferably from about 0.15wt% to about 0.7wt%.
  • the structure of the outlet zone is similar to that of a conventional iso-diameter riser.
  • the diameter ratio of the outlet zone to the first reaction zone is generally about 0.8:1 to about 1.5:1.
  • the height of this zone is generally about 0 ⁇ 20% of total height of the riser.
  • the function of this zone is to increase effluent velocity and to suppress overcracking reaction.
  • One end of the horizontal tube is connected to the outlet zone and the other end is connected to the disengager.
  • one end of the horizontal tube is connected to the second reaction zone and the other end is connected to the disengager.
  • the function of the horizontal tube is to link the outlet zone with the disengager.
  • Feedstocks suitable for the process of the present invention include distillate having different boiling ranges, residue and crude. More specifically, the feedstocks are selected from the group consisting of atmospheric gas oil, naphtha, catalytic gasoline, diesel, vacuum gas oil (VGO), atmospheric residue (AR) or vacuum residue (VR), coker gas oil (CGO), deasphalted oil (DAO), hydrotreated residue, hydrocracked residue, shale oil or the mixtures thereof.
  • the processes of the present invention are adaptable for use with all known catalyst types, including amorphous silica-alumina catalysts and zeolite catalysts with the active components preferably selected from the group consisting of Y, HY, USY or ZSM-5 series or any other zeolites typically employed in the cracking of hydrocarbons with or without rare earth and/or phosphor or the mixtures thereof.
  • the different reaction zones in the processes of the present invention are adaptable for use with the different type catalysts, including large and small particle size distribution catalysts or high and low apparent bulk density catalysts with the active components preferably selected from the group consisting of Y, HY, USY or ZSM-5 series or any other zeolites typically employed in the cracking of hydrocarbons with or without rare earth and/or phosphor or mixtures thereof.
  • Large and small particle size distribution catalysts or high and low apparent bulk density catalysts flow into different reaction zone respectively.
  • the large particle size distribution catalyst with USY zeolite flows into the first reaction zone for increasing cracking reaction
  • the small particle size distribution catalyst with rare earth Y zeolite flows into the second reaction zone for increasing hydrogen transfer reaction.
  • the mixed large and small particle size distribution catalysts are stripped in a stripper and are combusted in a regenerator, and then are separated into large particle size distribution catalyst and small particle size distribution catalyst.
  • the large and small particle size distribution catalyst are partitioned within the range of about 30 ⁇ 40 ⁇ m.
  • the high and low apparent bulk density catalyst are partitioned within the range of about 0.6 ⁇ 0.7g/cm 3 .
  • Fig.2 shows the schematic flow diagram used to produce isobutane and isoparaffin enriched gasoline in a multi-cascade riser.
  • the shape and size of the apparatus and pipelines are not limited in the attached diagram but depend on specific embodiments.
  • the prelift steam is introduced into prelift zone 2 via conduit 1.
  • Hot regenerated catalyst flow into prelift zone 2 via regenerated catalyst standpipe 16 and is lifted by prelift steam.
  • the preheated feedstock via conduit 4 is mixed with atomized steam via conduit 3 in proportion to form a mixture.
  • the mixture is charged into prelift zone, and then is contacted with hot regenerated catalyst, flowing into the first reaction zone 5 where cracking reaction takes place under certain reaction conditions.
  • the effluent is mixed with quenching mediums via conduit 6, flowing into the second reaction zone 7 with the result that isomerization and hydrogen transfer reaction take place under certain reaction conditions.
  • the reacted effluent flows into outlet zone 8 where the effluent is accelerated, and then passes through disengager 9, where entrained catalyst is separated mid dropped into the catalyst stripper 12. Residual catalyst is separated from the reaction vapors in a set of cyclones 10 located in the upper section of the reactor. The reaction vapors pass to subsequent separation system via conduit 11. Spent catalyst is contacted with stripping steam via conduit 13 to remove heavy hydrocarbons on the catalyst. After steam stripping, the catalyst flows to the spent catalyst standpipe 14 to the regenerator 15, where the spent catalyst is contacted with air via conduit 17 with the result that catalyst regeneration takes place to burn off coke. Flue gas is discharged from the regenerator via conduit 18. The hot regenerated catalyst is recycled into the bottom of the riser via regenerated catalyst standpipe 16.
  • the example showed that hydrocarbon feedstock was converted to produce isobutane and isoparaffin enriched gasoline in a conventional pilot plant iso-diameter riser in accordance with the present invention.
  • the preheated hydrocarbon feedstock D listed in table 1 was charged into the riser and contacted with hot regenerated catalyst D listed in table 2 in the presence of steam with the result that some reactions took place.
  • the reaction products were separated into isobutane enriched LPG, isoparaffin enriched gasoline and other products.
  • Spent catalyst flowed into regenerator via stripping. After regeneration, the regenerated catalyst was recycled for use.
  • the example showed that hydrocarbon feedstock was converted to produce isobutane and isoparaffin enriched gasoline in a combination reactor of an iso-diameter riser and a fluidized bed in accordance with the present invention
  • the preheated hydrocarbon feedstock D listed m table 1 was charged into the riser and contacted with hot regenerated catalyst D listed in table 2 in the presence of steam with the result that some reactions took place.
  • the reaction products were separated into isobutane enriched LPG, isoparaffin enriched gasoline and other products.
  • Spent catalyst flowed into regenerator via stripping. After regeneration, regenerated catalyst was recycled for use.
  • the Comparative example was conducted in a conventional pilot plant iso-diameter riser reactor.
  • the catalyst and feedstock used were the same as that in example 2.
  • Operating conditions, product slate and gasoline properties were listed in table 5.
  • Table 5 showed that 32.80wt% of LPG was propylene, 7.76wt% of LPG was isobutane, and that the gasoline had an isoparaffin content of 17.30wt%, and an olefin content of 45.30wt%.
  • the example showed that hydrocarbon feedstock was converted to produce isobutane and isoparaffin enriched gasoline in a multi-cascade riser reactor in accordance with the present invention.
  • the total height of the multi-cascade riser is 15 meters in which the height of the prelift zone with a diameter of 0.025 meter is 1.5meters, the height of the first reaction zone with a diameter of 0.025 meter is 4 meters, the height of the second reaction zone with a diameter of 0.1 meter is 6.5 meters, and the height of the outlet zone with a diameter of 0.025 meter is 3 meters.
  • the isotrapezia vertex angle ⁇ of the vertical section of the conjunct section between the first reaction zone and the second reaction zone is about 45°
  • the isotrapezia base angle ⁇ of the vertical section of the conjunct section between the second reaction zone and the outlet zone is about 60°.
  • the preheated hydrocarbon feedstock B listed in table 1 was charged into the riser and contacted with hot regenerated catalyst C listed in table 2 in the presence of steam with the result that some reactions took place.
  • the reaction products were separated into isobutane enriched LPG, isoparaffin enriched gasoline and other products.
  • Spent catalyst flowed into regenerator via stripping. After regeneration, regenerated catalyst was recycled for use.
  • the comparative example was conducted in a conventional pilot plant iso-diameter riser reactor.
  • the catalyst and feedstock used were the same as that in example 3.
  • Operating conditions and product slate were listed in table 6.
  • Gasoline properties were listed in table 7.
  • Table 6 showed that 15.74wt% of LPG was isobutane.
  • Table 7 showed that the gasoline bad an isoparaffin content of 11.83wt%, and an olefin content of 56.49wt%.
  • the example showed that hydrocarbon feedstock was converted to produce isobutane and isoparaffin enriched gasoline over different type catalysts in a pilot plant multi-cascade riser reactor in accordance with the present invention.
  • the reactor used in the example was the same as that in example 3.
  • the feedstocks used were the mixture of 80wt% of VGO A and 20wt% of CGO C, and AR D, whose properties were listed in table 1.
  • Operating conditions, catalyst types, product slate and Gasoline properties were listed in table 8.
  • Table 8 showed that about 28 ⁇ 32wt% of LPG was isobutane, and the gasoline had an isoparaffin content of about 33 ⁇ 39wt% and an olefin content of 16.0 ⁇ 27.0wt%.
  • hydrocarbon feedstock was converted to produce isobutane and isoparaffin enriched gasoline in a pilot plant multi-cascade riser reactor wherein gasoline with higher olefin content acted as quenching medium in accordance with the present invention.
  • the reactor, catalyst and feedstock were the same as those used in example 3.
  • the gasoline with higher olefin content acting as quenching medium was that obtained in comparative example 3.
  • the gasoline was injected into the bottom of the second reaction zone, other operating conditions were similar to these of example 2.
  • the example showed that hydrocarbon feedstock was converted to produce isobutane and isoparaffin enriched gasoline in a pilot plant multi-cascade riser reactor in accordance with the present invention.
  • the total height of the multi-cascade riser is 15 meters in which the height of the prelift zone with a diameter of 0.025 meter is 1.5 meters, the height of the first reaction zone with a diameter of 0.025 meter is 4.5 meters, and the height of the second reaction zone with a diameter of 0.05 meter is 9 meters.
  • the isotrapezia vertex angle ⁇ of the vertical section of the conjunct section between the first reaction zone and the second reaction zone is about 45°.
  • the example showed that hydrocarbon feedstock was converted to produce isobutane and isoparaffin enriched gasoline in a pilot plant multi-cascade riser reactor in accordance with the present invention.
  • the reactor used was the same as tat in example 3.
  • the preheated hydrocarbon feedstock E listed in table 1 was charged into the first reaction zone and contacted with hot regenerated catalyst C listed in table 2 in the presence of steam with the result that cracking reaction took place, then the resultant mixture flowing into the second reaction zone was mixed with cooled regenerated catalyst via cooler.
  • the reaction products were separated into isobutane enriched LPG, isoparaffin enriched gasoline and other products.
  • Spent catalyst flowed into regenerator via stripping. After regeneration, the regenerated catalyst was divided into two parts. one was returned into the bottom of the first reaction zone, and the other part was cooled in catalyst cooler and recycled into the bottom of the second reaction zone for use.
  • the example showed that hydrocarbon feedstock was convened to produce isobutane and isoparaffin enriched gasoline in a pilot plant multi-cascade riser reactor in accordance with the present invention.

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  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
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EP20000108032 1999-04-23 2000-04-20 Verfahren zur katalytischen Umwandlung zum Herstellen von mit Isobutan und Isoparaffinen angereichertem Benzin Expired - Lifetime EP1046696B1 (de)

Applications Claiming Priority (4)

Application Number Priority Date Filing Date Title
CN99105904A CN1076751C (zh) 1999-04-23 1999-04-23 一种制取异丁烷和富含异构烷烃汽油的催化转化方法
CN99105904 1999-04-23
CN99109193 1999-06-23
CN99109193A CN1081222C (zh) 1999-06-23 1999-06-23 一种降低液化气和汽油中烯烃含量的催化转化方法

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EP1046696A2 true EP1046696A2 (de) 2000-10-25
EP1046696A3 EP1046696A3 (de) 2001-01-03
EP1046696B1 EP1046696B1 (de) 2014-06-11

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Cited By (15)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2003059502A1 (en) * 2002-01-10 2003-07-24 Stone & Webster Process Technology, Inc. Improved deep catalytic cracking process
US6866771B2 (en) 2002-04-18 2005-03-15 Uop Llc Process and apparatus for upgrading FCC product with additional reactor with catalyst recycle
US6869521B2 (en) 2002-04-18 2005-03-22 Uop Llc Process and apparatus for upgrading FCC product with additional reactor with thorough mixing
EP1800742A1 (de) * 2005-12-20 2007-06-27 Institut Français du Pétrole Reaktor mit zwei fluidisierbaren Reaktionsstufen und einem integrierten Gas/Feststofftrennsystem
US7575725B2 (en) 1999-08-20 2009-08-18 Uop Llc Controllable space velocity reactor
CN102277193A (zh) * 2011-03-18 2011-12-14 青岛京润石化设计研究院有限公司 一种催化裂化方法及装置
CN102391889A (zh) * 2011-10-10 2012-03-28 石宝珍 一种催化转化方法
CN102399579A (zh) * 2011-10-14 2012-04-04 石宝珍 一种催化裂化方法
CN102465006A (zh) * 2010-11-11 2012-05-23 石宝珍 一种催化裂化方法及装置
CN102477311A (zh) * 2010-11-28 2012-05-30 石宝珍 一种催化裂化方法及装置
CN102485840A (zh) * 2010-12-01 2012-06-06 石宝珍 一种催化裂化方法及装置
CN102485841A (zh) * 2010-12-01 2012-06-06 石宝珍 一种催化裂化方法及装置
US8608944B2 (en) 2005-12-23 2013-12-17 Research Institute Of Petroleum Processing Sinopec Catalytic conversion method of increasing the yield of lower olefin
US9387449B2 (en) 2010-11-11 2016-07-12 Baozhen Shi Catalytic cracking method and apparatus
WO2022132758A1 (en) * 2020-12-16 2022-06-23 Dow Global Technologies Llc Systems and methods for producing olefins

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EP0208609A1 (de) * 1985-07-10 1987-01-14 Total Raffinage Distribution S.A. Verfahren und Einrichtung für das katalytische Kracken von Kohlenwasserstoffen mit Kontrolle der Reaktionstemperatur
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US7575725B2 (en) 1999-08-20 2009-08-18 Uop Llc Controllable space velocity reactor
WO2003059502A1 (en) * 2002-01-10 2003-07-24 Stone & Webster Process Technology, Inc. Improved deep catalytic cracking process
US6905591B2 (en) 2002-01-10 2005-06-14 Stone & Webster Process Technology, Inc. Deep catalytic cracking process
US7479218B2 (en) 2002-01-10 2009-01-20 Stone & Webster Process Technology, Inc. Deep catalytic cracking process
US6866771B2 (en) 2002-04-18 2005-03-15 Uop Llc Process and apparatus for upgrading FCC product with additional reactor with catalyst recycle
US6869521B2 (en) 2002-04-18 2005-03-22 Uop Llc Process and apparatus for upgrading FCC product with additional reactor with thorough mixing
US7033546B2 (en) 2002-04-18 2006-04-25 Uop Llc Process and apparatus for contacting hydrocarbons with catalyst
US7344634B2 (en) 2002-04-18 2008-03-18 Uop Llc Process and apparatus for contacting hydrocarbons with catalyst
EP1800742A1 (de) * 2005-12-20 2007-06-27 Institut Français du Pétrole Reaktor mit zwei fluidisierbaren Reaktionsstufen und einem integrierten Gas/Feststofftrennsystem
US8608944B2 (en) 2005-12-23 2013-12-17 Research Institute Of Petroleum Processing Sinopec Catalytic conversion method of increasing the yield of lower olefin
CN102465006A (zh) * 2010-11-11 2012-05-23 石宝珍 一种催化裂化方法及装置
CN102465006B (zh) * 2010-11-11 2014-01-29 石宝珍 一种催化裂化方法及装置
US9387449B2 (en) 2010-11-11 2016-07-12 Baozhen Shi Catalytic cracking method and apparatus
CN102477311A (zh) * 2010-11-28 2012-05-30 石宝珍 一种催化裂化方法及装置
CN102485840B (zh) * 2010-12-01 2014-03-05 石宝珍 一种催化裂化方法及装置
CN102485841A (zh) * 2010-12-01 2012-06-06 石宝珍 一种催化裂化方法及装置
CN102485840A (zh) * 2010-12-01 2012-06-06 石宝珍 一种催化裂化方法及装置
CN102485841B (zh) * 2010-12-01 2014-02-26 石宝珍 一种催化裂化方法及装置
CN102277193A (zh) * 2011-03-18 2011-12-14 青岛京润石化设计研究院有限公司 一种催化裂化方法及装置
CN102277193B (zh) * 2011-03-18 2014-04-02 青岛京润石化设计研究院有限公司 一种催化裂化方法及装置
CN102391889B (zh) * 2011-10-10 2013-12-18 石宝珍 一种催化转化方法
CN102391889A (zh) * 2011-10-10 2012-03-28 石宝珍 一种催化转化方法
CN102399579A (zh) * 2011-10-14 2012-04-04 石宝珍 一种催化裂化方法
CN102399579B (zh) * 2011-10-14 2014-03-05 石宝珍 一种催化裂化方法
WO2022132758A1 (en) * 2020-12-16 2022-06-23 Dow Global Technologies Llc Systems and methods for producing olefins

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EP1046696A3 (de) 2001-01-03

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