EP0142900B1 - Katalytisches Wirbelschichtkrackverfahren mit doppeltem Steigrohr - Google Patents

Katalytisches Wirbelschichtkrackverfahren mit doppeltem Steigrohr Download PDF

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Publication number
EP0142900B1
EP0142900B1 EP19840201664 EP84201664A EP0142900B1 EP 0142900 B1 EP0142900 B1 EP 0142900B1 EP 19840201664 EP19840201664 EP 19840201664 EP 84201664 A EP84201664 A EP 84201664A EP 0142900 B1 EP0142900 B1 EP 0142900B1
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EP
European Patent Office
Prior art keywords
catalyst
feedstock
reactor
stripper
contacting
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.)
Expired
Application number
EP19840201664
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English (en)
French (fr)
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EP0142900A2 (de
EP0142900A3 (en
Inventor
James Fred Crocoll
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Shell Internationale Research Maatschappij BV
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Shell Internationale Research Maatschappij BV
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Publication of EP0142900A3 publication Critical patent/EP0142900A3/en
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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
    • C10G51/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more cracking processes only
    • C10G51/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more cracking processes only plural serial stages only
    • C10G51/026—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more cracking processes only plural serial stages only only catalytic cracking steps
    • 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 dual riser fluid catalytic cracking process wherein a low quality feedstock is passed through the risers in series the feedstock is in contact with freshly regenerated catalyst which is passed through the risers in parallel.
  • Catalytic cracking is the major molecular weight reduction process employed in petroleum refining for manufacturing gasoline as fuels.
  • Business incentives require the processing of heavier, low-quality feedstocks, lower output of residual products and increased energy efficiencies while meeting more stringent environmental constraints.
  • Current catalysts require high temperature and short contact time riser reactors to obtain the full benefits of the process, i.e., highest selectivity to gasoline at highest conversion yields. These catalysts require high temperature regeneration (CO combustion). This approach also allows for catalysts with greater metals tolerance, octane enhancement and SOx capture.
  • metal contaminants such as nickel, vanadium and iron are deposited on the catalyst and reduce its effectiveness in converting the feedstock to lower boiling components such as gasoline.
  • metal contaminants such as nickel, vanadium and iron are deposited on the catalyst and reduce its effectiveness in converting the feedstock to lower boiling components such as gasoline.
  • One way of at least partially overcoming these adverse effects is by treating the catalyst with agents which reduce the ability of contaminants on the catalyst to adversely affect the cracking process. For example, in U.S. 4,326,990 selected treating agents are added to the feedstock; in the reactor these agents are deposited on the catalyst.
  • Patent 3,748,251 charge stock is passed into a reaction zone together with a catalyst composition comprising two cracking components, part of which is ZSM-5, hydrocarbons are withdrawn from the reaction zone, unreacted hydrocarbon charge is separated and introduced into a second reaction zone together with said catalyst.
  • a fluid catalytic cracking process for low quality hydrocarbon feedstocks which process has a dual reactor system with a common catalyst stripper and regenerator, which comprises passing said feedstock into a first riser reactor zone and contacting said feedstock with freshly regenerated fluid cracking catalyst under reaction conditions suitable for conversion of feedstocks to lower boiling components while simultaneously reducing metal contaminants and temporary catalyst poisons contained therein; separating first riser reaction products from catalyst in a first separation zone and passing a mixture of relatively clean unconverted feedstock and reaction products from said separation zone into a second reactor zone and contacting the mixture with freshly regenerated fluid cracking catalyst under reaction conditions suitable for conversion of feedstocks to lower boiling components; separating second reactor reaction products from catalyst in a second separation zone; passing partially deactivated catalyst, containing metal contaminants, coke and unreacted hydrocarbons to a catalyst stripper and contacting said catalyst with steam under conditions to remove a substantial portion of said unreacted and/or adsorbed hydrocarbons; passing catalyst from the strip
  • This invention therefore relates to a fluid catalytic cracking process which has been improved with respect to the process of FR-A-2,378,847 in that the second reactor is a riser reactor, the partially deactivated catalyst from both separation zones is passed to the catalyst stripper and that the unreacted and/or adsorbed hydrocarbons removed in the catalyst stripper are passed to a fractionator for recovery of products.
  • the process according to the invention can be suitably applied to low quality hydrocarbon feedstocks containing metal contaminants comprising nickel and/or vanadium in amounts from about 1 to 100 parts per million by weight (ppmw). It can also be suitably applied to hydrocarbon feedstocks containing from about 300 to 8000 ppmw of basic nitrogen. Furthermore, the process can be suitably applied to hydrocarbon feedstocks containing from about 0.5 to 10 %w of coke precursors, determined as Ramsbottom Carbon Residue.
  • the process according to the invention is suitably carried out using well-known catalysts, such as commercially available cracking catalysts and, in particular X or Y type zeolites contained in a silica-alumina matrix.
  • the system includes primarily a catalyst regeneration zone 2, a catalyst striper zone 4, a first catalyst separation zone 6, and a second catalyst separation zone 8.
  • Fresh feedstock is introduced into the system via line 10, where it is contacted with freshly regenerated catalyst from regenerator 2 via line 12.
  • the feedstock and catalyst are passed under suitable reaction conditions upwardly through the first riser (line 14) wherein the feedstock is partially converted to lower boiling components.
  • the mixture of unconverted feed, conversion products and catalyst is then passed into a first separation zone, 6, wherein catalyst and gaseous hydrocarbons are separated.
  • An optional embodiment of the invention is to add prestripping steam to separation zone 6 via line 50.
  • the separated catalyst, which is partially deactivated is passed via line 16 to a riser pot 18, where it is contacted by steam introduced via line 30 and lifted via line 32 to catalyst stripper 4.
  • the gaseous hydrocarbons from separation zone 6 are passed via line 20 to the second riser (line 24) where they are contacted with freshly regenerated catalyst from regenerator 2 via line 22 and passed under suitable reaction conditions upwardly through said second riser, wherein a substantial portion of the unconverted feedstock from catalyst separation zone 6 is converted to lower boiling components.
  • the mixture of unconverted feed, conversion products and catalyst is then passed into a second separation zone 8, wherein catalyst and gaseous hydrocarbons are separated.
  • An optional embodiment of the invention is to add prestripping steam to separation zone 8 via line 51.
  • the separated catalyst, which is partially deactivated is passed via line 26 to a riser pot 18, where it is combined with catalyst from separation zone 6, and is contacted by steam introduced via line 30 and lifted via line 32 to catalyst stripper 4.
  • the gaseous hydrocarbons from catalyst separation zone 8 are passed via line 40 to a fractionator where suitable cracked products are recovered.
  • the hydrocarbons and gases stripped from the catalyst in stripper 4 are passed via line 42 to the same or another fractionator for separation of water and recovery of products.
  • the stripped catalyst from stripper 4 is passed via line 28 to a regeneration zone 2, where it is contacted with air introduced via line 38.
  • the partially deactivated catalyst is regenerated under conditions suitable to remove coke and basic nitrogen compounds. Flue gases from the regeneration zone are vented via line 44. Freshly regenerated catalyst is circulated to the first and the second riser via lines 12 and 22, respectively, and the process is continued.
  • This example illustrates the benefits to be realized by removing temporary catalyst poisons from low quality catalytic cracking feedstocks.
  • Feedstock A was a fairly high quality, clean light flashed distillate and was included for comparison.
  • Feedstock B was a low quality feed, such as those suitable for the process of the invention, which contained a significant amount of basic nitrogen compounds.
  • the deresining step consists of mixing the feedstocks with isooctane and passing the mixture over attapulgas clay.
  • suitable clays for this purpose include Fuller's Earth and Florex-S.
  • the total resins, including the basic nitrogen compounds, are adsorbed on the clay.
  • MAT micro activity test
  • the MAT used in these studies and the operating procedure were similar to those described in ASTM D 3907-80. Briefly about 5.0 grams of catalyst are contained in a small diameter reactor (ASTM specifies 15.6 mm I.D.). The feed is passed over the catalyst for about 60 seconds. Immediately after the oil addition, nitrogen is introduced to strip the catalyst. Both a liquid and a gas are recovered as products. These are conveniently analyzed by conventional chromatographic equipment.
  • Cracking Feedstock B to a low conversion in a first riser reactor will achieve essentially the same benefits as the deresining treatment.
  • the total product from this low conversion first reactor can then be easily cracked at low severity to a high conversion in a second riser reactor.

Landscapes

  • 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)

Claims (1)

  1. Ein Crackverfahren mit im fluidem Zustand vorliegenden Katalysator für Kohlenwasserstoff-Zuspeisungsmaterialien niedriger Qualität, in welchem Verfahren ein Doppelreaktor-System mit einem gemeinsamen Katalysator-Abstreifer und Regenerator verwendet wird, in welchem besagtes Zuspeisungsmaterial in eine erste Reaktorzone in Form eines Steigrohres eingeleitet und dieses Einspeisungsmaterial mit regeneriertem Crackkatalysator im fluiden Zustand unter wenig scharfen Reaktionsbedingungen kontaktiert wird, welche für einen relativ niedrigen Umwandlungsgrad von Einspeisungsmaterialien in niedriger siedende Komponenten geeignet sind, während gleichzeitig darin vorliegende metallhaltige Verunreinigungen und temporär vorhandene Katalysatorgifte verringert werden, in welchem die Reaktionsprodukte aus dem ersten Steigrohr in einer ersten Trennzone vom Katalysator abgetrennt werden und eine Mischung aus relativ reinem noch nicht umgewandeltem Zuspeisungsgut und Reaktionsprodukten aus besagter Trennzone in die zweite Reaktorzone eingespeizt wird und diese Mischung mit frisch regeneriertem Crackkatalysator im fluiden Zustand unter relativ wenig scharfen Reaktionsbedingungen kontaktiert wird, welche für einen relativ hohen Umwandlungsgrad von zugespeisten Materialien in niedriger siedende Komponenten geeignet sind, in welchem die aus dem zweiten Reaktor abgezogenen Reaktionsprodukte in einer zweiten Trennzone vom Katalysator abgetrennt werden, in welchem teilweise desaktivierter Katalysator, welcher metallhaltige Verunreinigungen, Koks und nicht umgesetzte Kohlenwasserstoff enthält, einem Katalysator-Abstreifer zugeleitet und besagter Katalysator mit Dampf unter solchen Bedingungen kontaktiert wird, daß ein wesentlicher Anteil an besagten nicht umgesetzten und/oder absorbierten Kohlenwasserstoffen daraus entfernt wird, in welchem der Katalysator von dem Abstreifer einem Regenerator zugeführt und in diesem der Katalysator mit Luft unter Reaktionsbedingungen kontaktiert wird, welche geeignet sind, um Koks und nicht umgewandelte Kohlenwasserstoffe zu verbrennen, in welchem die Verbrennungsprodukte in Form eines Abgases von dem regenerierten Katalysator abgetrennt werden, in welchem der frisch regenerierte Katalysator im Kreislauf beiden Reaktoren zur Kontaktierung mit frischer Zuspeisung und mit besagter Mischung aus nicht umgewandelter Zuspeisung und Reaktionsprodukten zugeführt wird und in welchem die aus der zweiten Trennzone abgezogenen Crackprodukte gewonnen werden, dadurch gekennzeichnet, daß auch der zweite Reaktor ein Steigrohr-Reaktor ist, daß der teil-desaktivierte Katalysator aus beiden Trennzonen dem Katalysator-Abstreifer zugeführt wird und daß die in dem Katalysator-Abstreifer entfernten nicht umgesetzten und/oder adsorbierten Kohlenwasserstoffe zur Wiedergewinnung von Produkten einem Fraktionator zugeführt werden.
EP19840201664 1983-11-22 1984-11-16 Katalytisches Wirbelschichtkrackverfahren mit doppeltem Steigrohr Expired EP0142900B1 (de)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US55446983A 1983-11-22 1983-11-22
US554469 1983-11-22

Publications (3)

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EP0142900A2 EP0142900A2 (de) 1985-05-29
EP0142900A3 EP0142900A3 (en) 1986-01-22
EP0142900B1 true EP0142900B1 (de) 1989-08-16

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EP19840201664 Expired EP0142900B1 (de) 1983-11-22 1984-11-16 Katalytisches Wirbelschichtkrackverfahren mit doppeltem Steigrohr

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EP (1) EP0142900B1 (de)
JP (1) JPS60144388A (de)
CA (1) CA1237692A (de)
DE (1) DE3479427D1 (de)
NL (1) NL8403539A (de)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US9896627B2 (en) 2015-10-14 2018-02-20 Saudi Arabian Oil Company Processes and systems for fluidized catalytic cracking

Families Citing this family (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US7029571B1 (en) 2000-02-16 2006-04-18 Indian Oil Corporation Limited Multi stage selective catalytic cracking process and a system for producing high yield of middle distillate products from heavy hydrocarbon feedstocks
US20080011644A1 (en) 2006-07-13 2008-01-17 Dean Christopher F Ancillary cracking of heavy oils in conjuction with FCC unit operations
US8124822B2 (en) 2009-03-04 2012-02-28 Uop Llc Process for preventing metal catalyzed coking
US8124020B2 (en) 2009-03-04 2012-02-28 Uop Llc Apparatus for preventing metal catalyzed coking
JP6158807B2 (ja) 2011-07-27 2017-07-05 サウジ アラビアン オイル カンパニー 下降流反応装置におけるパラフィン系ナフサの流動接触分解
EP3106504B1 (de) 2015-06-19 2020-02-05 Reliance Industries Limited Verfahren zur propylen- und lpg-rückgewinnung in fcc-brenngas
US20230407187A1 (en) * 2022-06-17 2023-12-21 Kellogg Brown & Root Llc Converting Motor Fuels Range Distillates to Light Olefins in a Multiple Riser Fluid Catalytic Cracking (FCC) Unit

Family Cites Families (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3751359A (en) * 1971-09-27 1973-08-07 Texaco Inc Conversion of hydrocarbons
US3894933A (en) * 1974-04-02 1975-07-15 Mobil Oil Corp Method for producing light fuel oil
US4090949A (en) * 1974-07-31 1978-05-23 Mobil Oil Corportion Upgrading of olefinic gasoline with hydrogen contributors
US4073717A (en) * 1976-01-26 1978-02-14 Aliev Vagab Safarovich Process for producing gasoline
FR2378847A1 (fr) * 1977-01-28 1978-08-25 Melik Akhnazarov Talyat Procede de craquage catalytique d'une charge d'hydrocarbures
US4728416A (en) * 1979-11-14 1988-03-01 Ashland Oil, Inc. Cracking blends of gas oil and residual oil

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US9896627B2 (en) 2015-10-14 2018-02-20 Saudi Arabian Oil Company Processes and systems for fluidized catalytic cracking

Also Published As

Publication number Publication date
CA1237692A (en) 1988-06-07
EP0142900A2 (de) 1985-05-29
DE3479427D1 (en) 1989-09-21
NL8403539A (nl) 1985-06-17
EP0142900A3 (en) 1986-01-22
JPS60144388A (ja) 1985-07-30

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