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Edit Comment Close Premium member Presentation Transcript Slide1: WEFA Conference, June 2000, Berlin L.A. Gerritsen, F. Stoop Akzo Nobel Catalyst P. Low, J. Townsend BP Amoco D. Waterfield, K. Holder BP Amoco Production of Green Diesel in the BP Amoco Refineries Slide2: Summary BP Amoco Cleaner Fuels Program Akzo Nobel STARS Catalyst Series Experience at two BP Amoco Refineries to make Green Diesel What’s next?Slide3: BP Amoco Cleaner Fuels Program BP Amoco Approach: No trade-off between performance and environmental responsibility. Meet the needs of motorists and environment. Provide answers to this challenge by introduction of clean fuels in a proactive, creative way. Slide4: BP Amoco 40 Cities Program Air quality is local issue and depends on: Severity of local air quality problems Degree of industrialization and urbanization Extent of existing controls on emission Local health care priorities. Big cities have most acute air quality problems. BP Amoco makes available clean fuels for 40 big cities by end 2000. Slide5: Akzo Nobel Catalysts Akzo Nobel’s Approach: provide state of the art catalysts and technologies at acceptable costs: Akzo Nobel is a world-class supplier of highest activity HDS and HC catalysts. Akzo Nobel participates in the MAKFining Alliance, that supplies Clean Fuel Technologies.Slide6: STARS Catalysts Introduced in Europe in 1998 based on breakthrough catalyst manufacturing technology favoring the formation of so-called Super Type II Active Reaction Sites (STARS). Single stacks STARS Technology 85% dispersion, 100% Type II active sitesSlide7: Two New STARS Catalysts Ketjenfine KF-757 Ultra-high Activity CoMo catalyst for Ultra Deep Diesel HDS. Ketjenfine KF-848 Ultra-high Activity STARS NiMo catalyst for HC-pretreat service and now also for Ultra Deep Diesel HDS. Testing of STARS KF 757 at BPA: Testing of STARS KF 757 at BPA BP Amoco recognized the potential of the new STARS catalyst technology to make 50 ppm diesel for the UK soon after introduction of KF 757. Laboratory testing of KF 757on BPA standard feed and operating conditions commenced Summer 1998. Slide9: Testwork on BPA Conditions and Feed Testwork on BPA Conditions and Feed Feedstock: 1.18 wt% S, 131 ppm N, T95= 389 °C, LHSV=4Implementation of KF 757 in BP Amoco: Implementation of KF 757 in BP Amoco Based on the test results and model simulations BP Amoco decided to apply KF 757 in two mid-distillate HDS units in respectively Grangemouth, UK and in Germany, late 1998. Other distillate HDS units of BPA in Europe coming up for a catalyst change in 1999 and 2000 were also loaded with KF 757. 1) KF 757 in Grangemouth Refinery: 1) KF 757 in Grangemouth Refinery Grassroots unit designed for 500 ppm S in 1995, 35,000 BPSD, 2-bed reactor, no quench, 45 bars ppH2, LHSV 1.5, now making 10-20 ppm Sulfur at 45,000 BPSD. KF 757 was loaded in March 1999, replacing Competitive Catalyst, Dense loading, DMDS presulfiding. Forties LGO with 0-15% LVGO and occasionally 0-5% LCO and 0-10% LGO/HGO from tankage.Grangemouth Operating Philosophy: Grangemouth Operating Philosophy Feed composition mainly LGO plus a small percentage LVGO (top draw of VDU). Feeds targeted for back-end distillation limits. Unit operated to sulfur spec dependent on blending requirements (for ULSD). Stripper section operated to flash specifications. Cycle length 3-5 years.North-Sea Feed has low sulfur: North-Sea Feed has low sulfur Grangemouth Relatively “heavy” Feed with T95 of 340-370 C.: Relatively “heavy” Feed with T95 of 340-370 C. Untreated Kero is blended to diesel pool to obtain T95 and density in specification Grangemouth About 65 bars and 1.5 LHSV: About 65 bars and 1.5 LHSV Grangemouth 10-20 ppm Sulfur in Product: 10-20 ppm Sulfur in Product Grangemouth 2-3 wt% PNA in Product.: 2-3 wt% PNA in Product. Grangemouth Product Cetane Index 54-59. : Product Cetane Index 54-59. Grangemouth Unit performs as expected. (one exception: period 250-325 days on stream): Unit performs as expected. (one exception: period 250-325 days on stream) Grangemouth Catalyst Deactivation only 7 0C after one Year: Catalyst Deactivation only 7 0C after one Year Grangemouth LCO intake and Tailing of LVGO responsible for higher Temperature? : LCO intake and Tailing of LVGO responsible for higher Temperature? Grangemouth Conclusions Grangemouth: Conclusions Grangemouth Successfully producing 10-20 ppm sulfur from N-Sea crude for more than 1 year now: Stable operation Deactivation only 7 °C in 1 year. Required Operating Temperature influenced by LCO intake and LVGO Tailing. Unit makes 2-3 wt% PNA and 54-59 Cetane Index.Slide26: 2) Experience with KF 757 in Coryton Unit revamped for 500 ppm S in 1991, 50,000 BPSD, 2-bed reactor with quench. KF 757 was loaded in September 1999, replacing KF 752, Dense loading, DMDS presulfiding. 28 bars ppH2, LHSV 2.25 , H2/Oil 150 Nm3/m3. Low-medium Sulfur SRGO.Slide27: Feed Properties Coryton Feed Distillation (D-86): Feed Distillation (D-86) Coryton Severe operating Conditions (high LHSV, low Pressure): Severe operating Conditions (high LHSV, low Pressure) Coryton Slide30: About 40-50 ppm Sulfur in Product. Coryton Unit performs as expected: Unit performs as expected Coryton KF 757 operates at 20 °C lower Reactor Temperature: KF 757 operates at 20 °C lower Reactor Temperature Coryton Testrun suggests a “Temperature Wall Effect”.: Testrun suggests a “Temperature Wall Effect”. Coryton 4,6-Dimethyl Dibenzothiophene Reaction Mechanism: 4,6-Dimethyl Dibenzothiophene Reaction Mechanism Direct Route Hydrogenation Route Dibenzothiophene molecule is in a single plane Sulfur orbitals extend above and below the plane for angular approach to an active site Alkyl groups adjacent to sulfur restrict angle of approach Direct route of HDS much slower Hydrogenation route allows one ring to flex for easier approach to active site Removal of 4,6 DMDBT: Removal of 4,6 DMDBT Removal of 4,6,-DMDBT is favored by pre-hydrogenation of the aromatic ring. Pre-hydrogenation of the aromatic ring is favored: by high ppH2 and H2/Oil. by a high-activity hydrogenation catalyst. Catalyst activity must be high enough to operate at a temperature below thermodynamic limitation for aromatics saturation Slide37: New STARS Catalyst Ketjenfine KF-848 Even more active than KF 757 under ultra-deep HDS at medium-high pressure conditions. Additional advantage: better HDA, Density and Cetane improvement. First commercial introduction in Distillate HDS operations Summer 2000. Diesel HDS Summary: Diesel HDS Summary KF-757 is commercially proven to provide 10-20 ppm sulfur with an activity up to 20 oC higher than other catalysts, like KF-752. With good unit operation, straight run feeds and high-activity catalyst, it is possible to reach 50 ppm S and below in existing units without unit revamp. The HDS of substituted dibenzothiophenes controls the ability to produce ultra low sulfur diesel A next step in UD-HDS is made by application of STARS KF 848, especially at medium-high pressure and low product sulfur.Slide43: Thank You Leen GerritsenSlide44: Production of Green Diesel in the BP Amoco Refineries WEFA Conference, June 2000, Berlin L.A. Gerritsen, F. Stoop Akzo Nobel Catalyst P. Low, J. Townsend BP Amoco D. Waterfield, K. Holder BP Amoco You do not have the permission to view this presentation. In order to view it, please contact the author of the presentation.
sr AkzoNobel4 Pumbaa Download Post to : URL : Related Presentations : Share Add to Flag Embed Email Send to Blogs and Networks Add to Channel Uploaded from authorPOINTLite Insert YouTube videos in PowerPont slides with aS Desktop Copy embed code: (To copy code, click on the text box) Embed: URL: Thumbnail: WordPress Embed Customize Embed The presentation is successfully added In Your Favorites. Views: 347 Category: Entertainment License: All Rights Reserved Like it (0) Dislike it (0) Added: October 12, 2007 This Presentation is Public Favorites: 0 Presentation Description No description available. Comments Posting comment... By: mary_chemist (20 month(s) ago) hi please let me to download akzo nobel file now! Saving..... Post Reply Close Saving..... Edit Comment Close By: hzw83 (26 month(s) ago) I want to download it ! Saving..... Post Reply Close Saving..... Edit Comment Close Premium member Presentation Transcript Slide1: WEFA Conference, June 2000, Berlin L.A. Gerritsen, F. Stoop Akzo Nobel Catalyst P. Low, J. Townsend BP Amoco D. Waterfield, K. Holder BP Amoco Production of Green Diesel in the BP Amoco Refineries Slide2: Summary BP Amoco Cleaner Fuels Program Akzo Nobel STARS Catalyst Series Experience at two BP Amoco Refineries to make Green Diesel What’s next?Slide3: BP Amoco Cleaner Fuels Program BP Amoco Approach: No trade-off between performance and environmental responsibility. Meet the needs of motorists and environment. Provide answers to this challenge by introduction of clean fuels in a proactive, creative way. Slide4: BP Amoco 40 Cities Program Air quality is local issue and depends on: Severity of local air quality problems Degree of industrialization and urbanization Extent of existing controls on emission Local health care priorities. Big cities have most acute air quality problems. BP Amoco makes available clean fuels for 40 big cities by end 2000. Slide5: Akzo Nobel Catalysts Akzo Nobel’s Approach: provide state of the art catalysts and technologies at acceptable costs: Akzo Nobel is a world-class supplier of highest activity HDS and HC catalysts. Akzo Nobel participates in the MAKFining Alliance, that supplies Clean Fuel Technologies.Slide6: STARS Catalysts Introduced in Europe in 1998 based on breakthrough catalyst manufacturing technology favoring the formation of so-called Super Type II Active Reaction Sites (STARS). Single stacks STARS Technology 85% dispersion, 100% Type II active sitesSlide7: Two New STARS Catalysts Ketjenfine KF-757 Ultra-high Activity CoMo catalyst for Ultra Deep Diesel HDS. Ketjenfine KF-848 Ultra-high Activity STARS NiMo catalyst for HC-pretreat service and now also for Ultra Deep Diesel HDS. Testing of STARS KF 757 at BPA: Testing of STARS KF 757 at BPA BP Amoco recognized the potential of the new STARS catalyst technology to make 50 ppm diesel for the UK soon after introduction of KF 757. Laboratory testing of KF 757on BPA standard feed and operating conditions commenced Summer 1998. Slide9: Testwork on BPA Conditions and Feed Testwork on BPA Conditions and Feed Feedstock: 1.18 wt% S, 131 ppm N, T95= 389 °C, LHSV=4Implementation of KF 757 in BP Amoco: Implementation of KF 757 in BP Amoco Based on the test results and model simulations BP Amoco decided to apply KF 757 in two mid-distillate HDS units in respectively Grangemouth, UK and in Germany, late 1998. Other distillate HDS units of BPA in Europe coming up for a catalyst change in 1999 and 2000 were also loaded with KF 757. 1) KF 757 in Grangemouth Refinery: 1) KF 757 in Grangemouth Refinery Grassroots unit designed for 500 ppm S in 1995, 35,000 BPSD, 2-bed reactor, no quench, 45 bars ppH2, LHSV 1.5, now making 10-20 ppm Sulfur at 45,000 BPSD. KF 757 was loaded in March 1999, replacing Competitive Catalyst, Dense loading, DMDS presulfiding. Forties LGO with 0-15% LVGO and occasionally 0-5% LCO and 0-10% LGO/HGO from tankage.Grangemouth Operating Philosophy: Grangemouth Operating Philosophy Feed composition mainly LGO plus a small percentage LVGO (top draw of VDU). Feeds targeted for back-end distillation limits. Unit operated to sulfur spec dependent on blending requirements (for ULSD). Stripper section operated to flash specifications. Cycle length 3-5 years.North-Sea Feed has low sulfur: North-Sea Feed has low sulfur Grangemouth Relatively “heavy” Feed with T95 of 340-370 C.: Relatively “heavy” Feed with T95 of 340-370 C. Untreated Kero is blended to diesel pool to obtain T95 and density in specification Grangemouth About 65 bars and 1.5 LHSV: About 65 bars and 1.5 LHSV Grangemouth 10-20 ppm Sulfur in Product: 10-20 ppm Sulfur in Product Grangemouth 2-3 wt% PNA in Product.: 2-3 wt% PNA in Product. Grangemouth Product Cetane Index 54-59. : Product Cetane Index 54-59. Grangemouth Unit performs as expected. (one exception: period 250-325 days on stream): Unit performs as expected. (one exception: period 250-325 days on stream) Grangemouth Catalyst Deactivation only 7 0C after one Year: Catalyst Deactivation only 7 0C after one Year Grangemouth LCO intake and Tailing of LVGO responsible for higher Temperature? : LCO intake and Tailing of LVGO responsible for higher Temperature? Grangemouth Conclusions Grangemouth: Conclusions Grangemouth Successfully producing 10-20 ppm sulfur from N-Sea crude for more than 1 year now: Stable operation Deactivation only 7 °C in 1 year. Required Operating Temperature influenced by LCO intake and LVGO Tailing. Unit makes 2-3 wt% PNA and 54-59 Cetane Index.Slide26: 2) Experience with KF 757 in Coryton Unit revamped for 500 ppm S in 1991, 50,000 BPSD, 2-bed reactor with quench. KF 757 was loaded in September 1999, replacing KF 752, Dense loading, DMDS presulfiding. 28 bars ppH2, LHSV 2.25 , H2/Oil 150 Nm3/m3. Low-medium Sulfur SRGO.Slide27: Feed Properties Coryton Feed Distillation (D-86): Feed Distillation (D-86) Coryton Severe operating Conditions (high LHSV, low Pressure): Severe operating Conditions (high LHSV, low Pressure) Coryton Slide30: About 40-50 ppm Sulfur in Product. Coryton Unit performs as expected: Unit performs as expected Coryton KF 757 operates at 20 °C lower Reactor Temperature: KF 757 operates at 20 °C lower Reactor Temperature Coryton Testrun suggests a “Temperature Wall Effect”.: Testrun suggests a “Temperature Wall Effect”. Coryton 4,6-Dimethyl Dibenzothiophene Reaction Mechanism: 4,6-Dimethyl Dibenzothiophene Reaction Mechanism Direct Route Hydrogenation Route Dibenzothiophene molecule is in a single plane Sulfur orbitals extend above and below the plane for angular approach to an active site Alkyl groups adjacent to sulfur restrict angle of approach Direct route of HDS much slower Hydrogenation route allows one ring to flex for easier approach to active site Removal of 4,6 DMDBT: Removal of 4,6 DMDBT Removal of 4,6,-DMDBT is favored by pre-hydrogenation of the aromatic ring. Pre-hydrogenation of the aromatic ring is favored: by high ppH2 and H2/Oil. by a high-activity hydrogenation catalyst. Catalyst activity must be high enough to operate at a temperature below thermodynamic limitation for aromatics saturation Slide37: New STARS Catalyst Ketjenfine KF-848 Even more active than KF 757 under ultra-deep HDS at medium-high pressure conditions. Additional advantage: better HDA, Density and Cetane improvement. First commercial introduction in Distillate HDS operations Summer 2000. Diesel HDS Summary: Diesel HDS Summary KF-757 is commercially proven to provide 10-20 ppm sulfur with an activity up to 20 oC higher than other catalysts, like KF-752. With good unit operation, straight run feeds and high-activity catalyst, it is possible to reach 50 ppm S and below in existing units without unit revamp. The HDS of substituted dibenzothiophenes controls the ability to produce ultra low sulfur diesel A next step in UD-HDS is made by application of STARS KF 848, especially at medium-high pressure and low product sulfur.Slide43: Thank You Leen GerritsenSlide44: Production of Green Diesel in the BP Amoco Refineries WEFA Conference, June 2000, Berlin L.A. Gerritsen, F. Stoop Akzo Nobel Catalyst P. Low, J. Townsend BP Amoco D. Waterfield, K. Holder BP Amoco