EP0142900B1 - Procédé de craquage catalytique fluidisé avec double colonne montante - Google Patents

Procédé de craquage catalytique fluidisé avec double colonne montante 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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German (de)
English (en)
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EP0142900A3 (en
EP0142900A2 (fr
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 EP0142900A2 publication Critical patent/EP0142900A2/fr
Publication of EP0142900A3 publication Critical patent/EP0142900A3/en
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Publication of EP0142900B1 publication Critical patent/EP0142900B1/fr
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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. Procédé de craquage catalytique fluidisé pour alimentations hydrocarbonées de basse qualité, ledit procédé comportant un système de réacteur double avec une colonne de strippage et un régénérateur courants pour le catalyseur, qui comprend le passage de ladite alimentation dans une première zone de réacteur à colonne montante et la-mise en contact de ladite alimentation avec du catalyseur de craquage fluidisé fraîchement régénéré dans des conditions réactionnelles de sévérité relativement faible, convenables pour la conversion relativement faible des alimentations en constituants de point d'ébullition plus faible, tout en réduisant simultanément la teneur en impuretés métalliques et en poisons temporaires du catalyseur qu'il contient; la séparation d'avec le catalyseur des produits de réaction de la première colonne montante dans une première zone de séparation et le passage d'un mélange d'alimentation non transformée relativement propre et de produits de réaction depuis ladite zone de séparation dans la seconde zone de réacteur et la mise en contact du mélange avec du catalyseur de craquage fluidisé fraîchement régénéré dans des conditions réactionnelles de sévérité relativement faible, convenables pour la conversion relativement élevée des alimentations en constituants de point d'ébullition plus faible; la séparation d'avec le catalyseur des produits de réaction du second réacteur dans une seconde zone de séparation; le passage du catalyseur partiellement désactivé, contenant des impuretés métalliques, du coke et des hydrocarbures n'ayant pas réagi, vers une colonne de strippage du catalyseur et la mise en contact du catalyseur avec de la vapeur d'eau dans des conditions permettant d'éliminer une partie substantielle desdits hydrocarbures n'ayant pas reagi et/ou adsorbés; le passage du catalyseur depuis la colonne de strippage vers un régénérateur et la mise en contact dudit catalyseur avec de l'air dans des conditions réactionnelles convenables pour la combustion du coke et des hydrocarbures non transformés; la séparation des produits de combustion d'avec le catalyseur régénéré sous forme de gaz de combustion; la circulation du catalyseur fraîchement régénéré vers les deux réacteurs pour mettre en contact l'alimentation fraîche et ledit mélange d'alimentation non transformée et de produits de réaction, respectivement; et la récupération de produits craqués au sortir de la seconde zone de séparation, caractérisé en ce que le second réacteur est un réacteur à colonne montante; le catalyseur partiellement désactivé provenant des deux zones de séparation est envoyé vers la colonne de strippage du catalyseur; et les hydrocarbures n'ayant pas réagi et/ou adsorbés retirés dans la colonne de strippage du catalyseur sont envoyés vers une tour de fractionnement servant à récupérer les produits.
EP19840201664 1983-11-22 1984-11-16 Procédé de craquage catalytique fluidisé avec double colonne montante Expired EP0142900B1 (fr)

Applications Claiming Priority (2)

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

Publications (3)

Publication Number Publication Date
EP0142900A2 EP0142900A2 (fr) 1985-05-29
EP0142900A3 EP0142900A3 (en) 1986-01-22
EP0142900B1 true EP0142900B1 (fr) 1989-08-16

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EP19840201664 Expired EP0142900B1 (fr) 1983-11-22 1984-11-16 Procédé de craquage catalytique fluidisé avec double colonne montante

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

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
EP1190019A1 (fr) * 2000-02-16 2002-03-27 Indian Oil Corporation Limited Procede de craquage catalytique selectif a plusieurs etages et systeme de production d'un rendement eleve de produits de distillats moyens a partir de stocks d'alimentation d'hydrocarbures lourds
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
US9458394B2 (en) 2011-07-27 2016-10-04 Saudi Arabian Oil Company Fluidized catalytic cracking of paraffinic naphtha in a downflow reactor
EP3106504B1 (fr) 2015-06-19 2020-02-05 Reliance Industries Limited Procédé pour la récupération de gpl et de propylène dans un gaz combustible fcc
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
EP0142900A3 (en) 1986-01-22
NL8403539A (nl) 1985-06-17
DE3479427D1 (en) 1989-09-21
JPS60144388A (ja) 1985-07-30
EP0142900A2 (fr) 1985-05-29
CA1237692A (fr) 1988-06-07

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