EP0142900A2 - 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
EP0142900A2
EP0142900A2 EP84201664A EP84201664A EP0142900A2 EP 0142900 A2 EP0142900 A2 EP 0142900A2 EP 84201664 A EP84201664 A EP 84201664A EP 84201664 A EP84201664 A EP 84201664A EP 0142900 A2 EP0142900 A2 EP 0142900A2
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EP
European Patent Office
Prior art keywords
catalyst
feedstock
riser
contacting
process according
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.)
Granted
Application number
EP84201664A
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German (de)
English (en)
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EP0142900B1 (fr
EP0142900A3 (en
Inventor
James Fred Crocoll
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.)
Shell Internationale Research Maatschappij BV
Original Assignee
Shell Internationale Research Maatschappij BV
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Application filed by Shell Internationale Research Maatschappij BV filed Critical Shell Internationale Research Maatschappij BV
Publication of EP0142900A2 publication Critical patent/EP0142900A2/fr
Publication of EP0142900A3 publication Critical patent/EP0142900A3/en
Application granted granted Critical
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 tenperature regeneration (CO combustion). This approach also allows for catalysts with greater metals tolerance, octane enhancement and SO 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.
  • the effectiveness of a cracking catalyst is also reduced by temporary catalyst poisons such as basic nitrogen components and high boiling coke precursors, which reduce the ability of the catalyst to achieve high conversion of the feed without excessive cracking to undesirable light hydrocarbons.
  • 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 fran the reaction zone, unreacted hydrocarbon charge is separated and introduced into a seoond reaction zone together with said catalyst.
  • This invention relates to an improved fluid catalytic cracking process for low quality hydrocarbon feedstocks, said process having a dual riser 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 relatively low severity reaction conditions suitable for relatively low 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 riser reactor zone, and contacting the mixture with freshly regenerated fluid cracking catalyst under relatively low severity reaction conditions suitable for relatively high conversion of feedstocks to lower boiling components; separating second riser reaction products from catalyst in a second separation zone; passing partially deactivated catalyst, containing metal contaminants, coke and unreacted hydrocarbons, from both separation zones to a catalyst stripper and contacting said catalyst with steam under conditions to remove a substantial portion of said unreacted
  • 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 (ppnw). 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, detennined as Ramsbottan 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 stripper 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 fran 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 etnbodiment 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 gaseaus 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 deactived 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 cmpounds.
  • 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 mn I.D.). The feed is passed over the catalyst for about 60 seoonds. 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.

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

Family

ID=24213454

Family Applications (1)

Application Number Title Priority Date Filing Date
EP19840201664 Expired EP0142900B1 (fr) 1983-11-22 1984-11-16 Procédé de craquage catalytique fluidisé avec double colonne montante

Country Status (5)

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

Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2001060951A1 (fr) * 2000-02-16 2001-08-23 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
US8124020B2 (en) 2009-03-04 2012-02-28 Uop Llc Apparatus for preventing metal catalyzed coking
US8124822B2 (en) 2009-03-04 2012-02-28 Uop Llc Process for preventing metal catalyzed coking
US8877042B2 (en) 2006-07-13 2014-11-04 Saudi Arabian Oil Company Ancillary cracking of heavy oils in conjunction with FCC unit operations
US9458394B2 (en) 2011-07-27 2016-10-04 Saudi Arabian Oil Company Fluidized catalytic cracking of paraffinic naphtha in a downflow reactor
EP3106504A1 (fr) 2015-06-19 2016-12-21 Reliance Industries Limited Procédé pour la récupération de gpl et de propylène dans un gaz combustible fcc
WO2023245200A1 (fr) * 2022-06-17 2023-12-21 Kellogg Brown & Root Llc Conversion de distillats de gammes de carburants moteurs en oléfines légères dans une unité de craquage catalytique fluide (fcc) à colonnes montantes multiples

Families Citing this family (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

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3894933A (en) * 1974-04-02 1975-07-15 Mobil Oil Corp Method for producing light fuel oil
GB1438795A (en) * 1971-09-27 1976-06-09 Texaco Development Corp Conversion of hydrocarbons
US4073717A (en) * 1976-01-26 1978-02-14 Aliev Vagab Safarovich Process for producing gasoline
US4090949A (en) * 1974-07-31 1978-05-23 Mobil Oil Corportion Upgrading of olefinic gasoline with hydrogen contributors
FR2378847A1 (fr) * 1977-01-28 1978-08-25 Melik Akhnazarov Talyat Procede de craquage catalytique d'une charge d'hydrocarbures
EP0076889A1 (fr) * 1981-04-28 1983-04-20 Ashland Oil, Inc. Craquage de mélanges de gas-oil et d'huile résiduelle

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB1438795A (en) * 1971-09-27 1976-06-09 Texaco Development Corp 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
EP0076889A1 (fr) * 1981-04-28 1983-04-20 Ashland Oil, Inc. Craquage de mélanges de gas-oil et d'huile résiduelle

Cited By (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2001060951A1 (fr) * 2000-02-16 2001-08-23 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
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
CN100448953C (zh) * 2000-02-16 2009-01-07 印度石油股份有限公司 由重烃原料以高产率生产中间馏分产品的多级选择性催化裂化方法和系统
US8877042B2 (en) 2006-07-13 2014-11-04 Saudi Arabian Oil Company Ancillary cracking of heavy oils in conjunction with FCC unit operations
US8124020B2 (en) 2009-03-04 2012-02-28 Uop Llc Apparatus for preventing metal catalyzed coking
US8124822B2 (en) 2009-03-04 2012-02-28 Uop Llc Process 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
EP3106504A1 (fr) 2015-06-19 2016-12-21 Reliance Industries Limited Procédé pour la récupération de gpl et de propylène dans un gaz combustible fcc
US10329223B2 (en) 2015-06-19 2019-06-25 Reliance Industries Limited Process for propylene and LPG recovery in FCC fuel gas
WO2023245200A1 (fr) * 2022-06-17 2023-12-21 Kellogg Brown & Root Llc Conversion de distillats de gammes de carburants moteurs en oléfines légères dans une unité de craquage catalytique fluide (fcc) à colonnes montantes multiples

Also Published As

Publication number Publication date
CA1237692A (fr) 1988-06-07
DE3479427D1 (en) 1989-09-21
EP0142900B1 (fr) 1989-08-16
EP0142900A3 (en) 1986-01-22
JPS60144388A (ja) 1985-07-30
NL8403539A (nl) 1985-06-17

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