EP0142900A2 - Dual riser fluid catalytic cracking process - Google Patents
Dual riser fluid catalytic cracking process Download PDFInfo
- 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.)
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Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- 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.
Abstract
Description
- 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.
- In the catalytic cracking of low quality hydrocarbon feedstocks, 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.
- In catalytic cracking many different reactor configurations have been proposed, all claiming to have certain advantages. For example, in U.S. Patent 4,090,949 a dual riser reactor catalytic cracking system is disclosed, having a common catalyst regenerator supplying freshly regenerated catalyst to each riser, whilst fresh gas oil feed is contacted with freshly regenerated catalyst in the first riser and light C2-C5 olefins are contacted with freshly regenerated catalyst in the second riser. In another dual riser catalytic cracking system, as disclosed in U.S. 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.
- It is an object of this invention to remove from the feedstock essentially all of the temporary catalyst poisons, such as basic nitrogen constituents and coke precursors, and metal contaminants at relatively low conversions, e.g., 15 to 25% in the first reactor, thereby requiring low severity, i.e., lower catalyst/oil ratios.
- It is another object of the invention to catalytically crack the total product from the first reactor to a high conversion at low severity over freshly regenerated catalyst.
- It is a further object of the invention that the total severi'ty required for these two separate subsequent steps of cracking will be significantly lower than that required if the same total conversion were achieved in a single step.
- It is a still further object of the invention to use a common catalyst inventory to remove metal contaminants comprising nickel and/or vanadium and temporary catalyst poisons and to achieve a high conversion of low quality feedstocks.
- 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 and/or adsorbed hydrocarbons; passing catalyst from the stripper to a regenerator and contacting said catalyst with air under reaction conditions suitable to combust coke and unconverted hydrocarbons; separating conbustion products from regenerated catalyst as flue gas; circulating freshly regenerated catalyst to both risers for contacting fresh feedstock and said mixture of unconverted feedstock and reaction products respectively; and recovering cracked products from the second separation zone.
- 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 process according to the present invention, which is carried out in a two reactor-one regenerator system with the feed in series flow and the catalyst in parallel flow, is illustrated in Fig. 1.
- In the dual riser catalytic cracking process shown in Fig. 1, the system includes primarily a
catalyst regeneration zone 2, acatalyst 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 fromregenerator 2 vialine 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 vialine 50. The separated catalyst, which is partially deactivated, is passed vialine 16 to ariser pot 18, where it is contacted by steam introduced vialine 30 and lifted vialine 32 tocatalyst 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 fromregenerator 2 vialine 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 vialine 51. The separated catalyst, which is partially deactivated, is passed vialine 26 to ariser pot 18, where it is combined with catalyst from separation zone 6, and is contacted by steam introduced vialine 30 and lifted vialine 32 tocatalyst 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 vialine 42 to the same or another fractionator for separation of water and recovery of products. - The stripped catalyst from
stripper 4 is passed vialine 28 to aregeneration zone 2, where it is contacted with air introduced vialine 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 vialine 44. Freshly regenerated catalyst is circulated to the first and the second riser vialines - This example illustrates the benefits to be realized by removing temporary catalyst poisons from low quality catalytic cracking feedstocks.
- Two feedstocks, A (light flashed distillate) and B (commercial FCCU feed) , were deresined in the laboratory. Properties of the total and deresined feedstocks are shown in Table 1. 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. other 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.
- Feedstocks A and B, both before and after deresining, were then tested in a micro activity test (MAT) unit.
- 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.
- The results of the micro activity tests are plotted in Figs. 2A-2C (feedstock A) and 3A-3C (feedstock B). In all graphs, the straight lines relate to experiments carried out with total feed and the dotted lines relate to experiments carried out with deresined feedstock.
- In Figures 2A and 3A the conversions of total feed and deresined feedstock, respectively into 232 "C material, expressed as 100-%w of 232 °C material are plotted (on the horizontal axis) against the coke production in %w. In Figures 2B and 3B the conversions (as expressed for Figures 2A and 3 A) are plotted against the yield of the C5-232 °C fraction. Finally, in Figures 2C and 3C, respectively, the weight hourly space velocities are plotted (on the horizontal axis) against the conversions of total feed and deresined feedstock, respectively, as expressed hereinbefore. It will be clear from the Figures 3A-3C in comparison with Figures 2A-2C that the improvement in cracking characterstics (less refractory, more gasoline and less coke) following deresining is significantly greater for Feedstock B than for Feedstock A.
-
Claims (7)
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 (en) | 1985-05-29 |
EP0142900A3 EP0142900A3 (en) | 1986-01-22 |
EP0142900B1 EP0142900B1 (en) | 1989-08-16 |
Family
ID=24213454
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP19840201664 Expired EP0142900B1 (en) | 1983-11-22 | 1984-11-16 | Dual riser fluid catalytic cracking process |
Country Status (5)
Country | Link |
---|---|
EP (1) | EP0142900B1 (en) |
JP (1) | JPS60144388A (en) |
CA (1) | CA1237692A (en) |
DE (1) | DE3479427D1 (en) |
NL (1) | NL8403539A (en) |
Cited By (7)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2001060951A1 (en) * | 2000-02-16 | 2001-08-23 | Indian Oil Corporation Limited | A multi stage selective catalytic cracking process and a system for producing high yield of middle distillate products from heavy hydrocarbon feedstocks |
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 (en) | 2015-06-19 | 2016-12-21 | Reliance Industries Limited | Process for propylene and lpg recovery in fcc fuel gas |
WO2023245200A1 (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 |
Families Citing this family (1)
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)
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 (en) * | 1977-01-28 | 1978-08-25 | Melik Akhnazarov Talyat | Two=stage catalytic hydrocarbon cracking - with co-current and counter current reaction stages |
EP0076889A1 (en) * | 1981-04-28 | 1983-04-20 | Ashland Oil, Inc. | Cracking blends of gas oil & residual oil |
-
1984
- 1984-11-06 CA CA000467099A patent/CA1237692A/en not_active Expired
- 1984-11-16 EP EP19840201664 patent/EP0142900B1/en not_active Expired
- 1984-11-16 DE DE8484201664T patent/DE3479427D1/en not_active Expired
- 1984-11-20 JP JP24356084A patent/JPS60144388A/en active Pending
- 1984-11-21 NL NL8403539A patent/NL8403539A/en not_active Application Discontinuation
Patent Citations (6)
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 (en) * | 1977-01-28 | 1978-08-25 | Melik Akhnazarov Talyat | Two=stage catalytic hydrocarbon cracking - with co-current and counter current reaction stages |
EP0076889A1 (en) * | 1981-04-28 | 1983-04-20 | Ashland Oil, Inc. | Cracking blends of gas oil & residual oil |
Cited By (10)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2001060951A1 (en) * | 2000-02-16 | 2001-08-23 | Indian Oil Corporation Limited | A multi stage selective catalytic cracking process and a system for producing high yield of middle distillate products from heavy hydrocarbon feedstocks |
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 (en) * | 2000-02-16 | 2009-01-07 | 印度石油股份有限公司 | Multi-stage selective catalytic cracking process and system for producing high yield of middle distillate products from heavy hydrocarbon feedstocks |
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 (en) | 2015-06-19 | 2016-12-21 | Reliance Industries Limited | Process for propylene and lpg recovery in fcc fuel gas |
US10329223B2 (en) | 2015-06-19 | 2019-06-25 | Reliance Industries Limited | Process for propylene and LPG recovery in FCC fuel gas |
WO2023245200A1 (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 |
Also Published As
Publication number | Publication date |
---|---|
JPS60144388A (en) | 1985-07-30 |
CA1237692A (en) | 1988-06-07 |
NL8403539A (en) | 1985-06-17 |
EP0142900A3 (en) | 1986-01-22 |
DE3479427D1 (en) | 1989-09-21 |
EP0142900B1 (en) | 1989-08-16 |
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