US3617480A - Two stages of coking to make a high quality coke - Google Patents

Two stages of coking to make a high quality coke Download PDF

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Publication number
US3617480A
US3617480A US829082A US3617480DA US3617480A US 3617480 A US3617480 A US 3617480A US 829082 A US829082 A US 829082A US 3617480D A US3617480D A US 3617480DA US 3617480 A US3617480 A US 3617480A
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United States
Prior art keywords
coking
coke
petroleum
gas oil
high quality
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Expired - Lifetime
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US829082A
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English (en)
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Harvey E Keel
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GREAT LAKES CARBON CORP
Daewoo Engineering and Construction Co Ltd
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Daewoo Engineering and Construction Co Ltd
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Assigned to MANUFACTURERS HANOVER TRUST COMPANY A NY CORP. reassignment MANUFACTURERS HANOVER TRUST COMPANY A NY CORP. SECURITY INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: GREAT LAKES CARBON CORPORATION, A DE CORP
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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B55/00—Coking mineral oils, bitumen, tar, and the like or mixtures thereof with solid carbonaceous material
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
    • C10B57/04—Other carbonising or coking processes; Features of destructive distillation processes in general using charges of special composition
    • C10B57/045—Other carbonising or coking processes; Features of destructive distillation processes in general using charges of special composition containing mineral oils, bitumen, tar or the like or mixtures thereof

Definitions

  • This high-boiling gas oil fraction is 208/53,208/i3i segregated during the manufacture of regular or average lnt.Cl ..Cb55l00, quality petroleum coke and is subsequently coked in a ClOg 37/00 separate coking operation under delayed coking conditions of Field of Search 208/50, 53. time, temperature and pressure to produce a superior quality l3i petroleum coke.
  • This invention relates to a method of producing a high quality petroleum coke which, when used as an aggregate in the manufacture of electrothermic graphite electrodes, will 'produce electrodes Process," a low coefficient of thermal expansion (CTE), improved electrical resistivity and other properties which will enhance the performance of large diameter graphite electrodes in electric steel furnaces.
  • Petroleum coke is usually produced by coking a high-boiling petroleum residuum such as a reduced or topped crude oil or vacuum reduced crude oil, in a variety of coking methods.
  • a distillate fraction derived from the delayed coker overhead is thermally polymerized and is then combined with the residuum feed which is then sent to the delayed coking operation. While this type of operation is designed to increase the coke yield of the original feedstock, it will have little effect, if any, upon the ultimate quality of the coke produced by this process.
  • the present invention consists of a method for producing high quality petroleum coke from a petroleum residuum, such as a topped or reduced asphaltenic or naphthenic crude oil or vacuum-reduced crude oil of this type which, in and of itself, will not produce high quality or premium petroleum coke suitable for use as a carbon aggregate in the manufacture of large diameter electrothermic graphite electrodes.
  • a petroleum residuum such as a topped or reduced asphaltenic or naphthenic crude oil or vacuum-reduced crude oil of this type which, in and of itself, will not produce high quality or premium petroleum coke suitable for use as a carbon aggregate in the manufacture of large diameter electrothermic graphite electrodes.
  • TI-le petroleum residuum is first heated in a suitable heat exchanger to a coking temperature, after which it is coked under conditions of delayed time, temperature and pressure, to produce coke and distillate products.
  • These distillate products are fractionated and there is recovered therefrom a heavy gas oil fraction at least
  • This heavy gas oil fraction is then coked in a separate or blocked out" coking operation under delayed coking conditions of time, uniform temperature and pressure.
  • the feed to the coking vessel is stopped and switched to another vessel to continue the operation and the coke is removed from the first vessel by any of a variety of procedures, such as hydraulic decoking, which are well-known to those skilled in the petroleum refinery art.
  • the resulting coke is then calcined at a temperature of up to 2,600 F. to reduce its volatile content to less than 0.5 percent by weight.
  • the calcined material is then crushed and sized and is an excellent material when employed as a carbon aggregate in the manufacture of high quality electrothermic graphite electrodes which are used in electric steel furnaces.
  • Sample electrodes prepared for CTE determination by the method disclosed in U.S. Pat. No. 2,775,549 except for calcination of the coke to 2,280 F. have a CTE (measured over the temperature range 32 to 167 F.) of 6.0 XIO'7 or less and the coke will produce large electrothermie electrodes which have advantageously low CTE and electrical resistivity properties.
  • a reduced or topped asphaltenic or naphthenic petroleum oil, or vacuum reduced oil of this type is conveyed from the crude oil tower (not shown), from which it leaves at a temperature of about 600 F., through line 21 and valves 31 and 40 (valve 36 being closed) into the bottom portion of a fractionating tower 10 which is also receiving hot overhead or distillate products from the coking vessel as later described herein.
  • the hot reduced crude oil together with small amounts of high-boiling materials which are not distilled overhead from the fractionating tower are conveyed through line 22 and valve 41 to a pump I1 and thence through line 23 to a heat exchange furnace 12 of conventional design.
  • the feed conveyed to the coker from the furnace through line 24 is at a temperature within the range of 900 to 950 F.
  • the feedstock is conveyed into coke drums 13 or by line 25 or 250.
  • Two-coke drums are normally employed in refineries using the delayed coking process because while one drum is being filled with the hot residuum and producing coke and overhead products, the other drum is being cooled and the coke removed therefrom by hydraulic or other means well-known to those skilled in the art.
  • Tl-Ie hot feed entering the coke drum undergoes decomposition (cracking), polymerization and aromatization.
  • distillate products produced by these chemical reactions are conveyed out of the drum.
  • valve 34 closed and valve 32 open these distillate products are conveyed to a stripping tower 14 where a highboiling gas oil faction, at least 80 percent of which has a boiling point (atmospheric conditions) above 700 F is collected.
  • the stripping tower 14 may be equipped with a reboiler or jacketed for recirculating of heat exchange media necessary to maintain the desired bottom temperature.
  • a partial condenser can be used as a reflux for maintaining the top stripping temperature.
  • the lighter boiling products from the stripping tower are conveyed through valve 33 and line 28 to the fractionating tower 10 from which the lower boiling products including gas, gasoline and light gas oil are recovered.
  • the high-boiling gas oil faction which collects in the stripping tower 14 is conveyed through line 27 and valve 19 to a heat exchanger 44 into a storage tank 20 to be processed in a separate or blocked out" delayed coking operation.
  • this unit may be bypassed by closing valve 40 and opening valve 36 and pumping the reduced crude, through a heat exchanger (not shown) if necessary, through line 35, pump 1 l and line 23 to the heat exchange furnace 12.
  • the reduced crude oil or equivalent feed is shut off by valve 31 and the gas oil fraction is conveyed through line 29 and valve 30 to a heat exchanger 37 and thence either to the lower zone of fractionating tower through valve 38 and line 42 or, altematively, bypassing the fractionating tower by closing valve 38 and opening valve 39 and conveying it through line 43 to pump 11 and through line 23 to the heat exchange furnace 12.
  • the heavy gas oil fraction is uniformly heated in the furnace to the temperature up to 950 F., preferably 925 to 945 F., and then conveyed to one of the coke drums 13 or 13a through line 24.
  • the heavy gas oil is passed into the coke drum under uniform temperature and pressure conditions, where it undergoes decomposition (cracking), polymerization, aromatization and ultimately coke formation.
  • the lower boiling products produced from these reactions leave the top of the coke drum and are returned to the fractionating tower through open valve 34 and line 28. in this operation, the stripping tower 14 may be omitted from the circuit and valves 32. 33 and 19 will be closed.
  • the fractionating tower most of the cracked distillate products will be fractionated as overhead products and some higher boiling material will be recycled to the coke drum through line 22 and valve 41.
  • the valve between the drums is switched and the feed is admitted to the second drum while the first drum is being cooled internally by high temperature, high pressure steam after which the coke is removed from the drum preferably by hydraulic means which are well-known to those skilled in the art.
  • the coke yield based on the fresh feed from tank 20, will be within the range of to 35 percent, depending on the coking cycle.
  • the resulting electrodes will have a CTE of about 4.0 l0 (over the temperature range 32 to 167 F.) and is an excellent material to produce carbon aggregate in the manufacture of high quality large electrothermic graphite electrodes.
  • the entire cracked, distillate product from coking the reduced crude oil or equivalent can be sent to the fractionating tower 10 which is operated at a bottom temperature sufiiciently high so that at least percent of the heavy gas oil which collects at the bottom of the unit has a boiling point of about 700 F. in such case, the reduced crude or equivalent will bypass the fractionating tower l0 and, with valves 40 and 41 closed and valves 31 and 36 open, will be sent directly to the furnace 12 and thence to one of the coke drums. This material can then be sent to storage tank 20 by closing valve 41 and opening valve 45 and conveying the material through line 46.
  • step (c) coking the heavy gas oil fraction from step (c) in a subsequent and separate coking operation under delayed coking conditions at a uniform temperature between 925 to 950 F. and underpressure.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Materials Engineering (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Coke Industry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Carbon And Carbon Compounds (AREA)
US829082A 1969-05-29 1969-05-29 Two stages of coking to make a high quality coke Expired - Lifetime US3617480A (en)

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
US82908269A 1969-05-29 1969-05-29

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US3617480A true US3617480A (en) 1971-11-02

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US829082A Expired - Lifetime US3617480A (en) 1969-05-29 1969-05-29 Two stages of coking to make a high quality coke

Country Status (6)

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US (1) US3617480A (enrdf_load_stackoverflow)
JP (1) JPS4943241B1 (enrdf_load_stackoverflow)
DE (1) DE2024804B2 (enrdf_load_stackoverflow)
ES (1) ES380055A1 (enrdf_load_stackoverflow)
GB (1) GB1263196A (enrdf_load_stackoverflow)
NO (1) NO126380B (enrdf_load_stackoverflow)

Cited By (44)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3954597A (en) * 1974-03-27 1976-05-04 Morrell Jacque C Process for the production of distillate fuels from oil shales and by-products therefrom
US3959115A (en) * 1972-03-01 1976-05-25 Maruzen Petrochemical Co., Ltd. Production of petroleum cokes
US4029749A (en) * 1974-11-29 1977-06-14 Mitsui Coke Co. Ltd. Process for manufacturing needle coke
US4235700A (en) * 1979-10-12 1980-11-25 Exxon Research & Engineering Co. Two-stage coking for the production of low metals coke
US4242196A (en) * 1978-10-27 1980-12-30 Kureha Kagaku Kogyo Kabushiki Kaisha Mass production system of highly aromatic petroleum pitch
US4351702A (en) * 1981-09-08 1982-09-28 Conoco Inc. Processing of heavy high-sulfur feedstocks
US4492625A (en) * 1983-11-17 1985-01-08 Exxon Research And Engineering Co. Delayed coking process with split fresh feed
US4501654A (en) * 1983-11-17 1985-02-26 Exxon Research & Engineering Co. Delayed coking process with split fresh feed and top feeding
US4518486A (en) * 1980-12-24 1985-05-21 The Standard Oil Company Concurrent production of two grades of coke using a single fractionator
US4551232A (en) * 1983-02-09 1985-11-05 Intevep, S.A. Process and facility for making coke suitable for metallurgical purposes
US5316655A (en) * 1990-02-20 1994-05-31 The Standard Oil Company Process for making light hydrocarbonaceous liquids in a delayed coker
US5350503A (en) * 1992-07-29 1994-09-27 Atlantic Richfield Company Method of producing consistent high quality coke
US6168709B1 (en) 1998-08-20 2001-01-02 Roger G. Etter Production and use of a premium fuel grade petroleum coke
US20030089589A1 (en) * 2001-11-09 2003-05-15 Foster Wheeler Usa Corporation Coke drum discharge system
US20040045803A1 (en) * 2002-09-05 2004-03-11 Lah Ruben F. Coke drum bottom throttling valve and system
US20040154913A1 (en) * 2001-03-12 2004-08-12 Lah Ruben F. Valve system and method for unheading a coke drum
US20050284793A1 (en) * 2004-06-25 2005-12-29 Debasis Bhattacharyya Process for the production of needle coke
WO2006000276A1 (en) * 2004-05-12 2006-01-05 Sgl Carbon Ag Graphite electrode for electrothermic reduction furnaces, electrode column, and method of producing graphite electrodes
US20060032788A1 (en) * 1999-08-20 2006-02-16 Etter Roger G Production and use of a premium fuel grade petroleum coke
US20060081456A1 (en) * 2004-04-22 2006-04-20 Lah Ruben F Remotely controlled decoking tool used in coke cutting operations
US20070038393A1 (en) * 2005-08-12 2007-02-15 Frederic Borah Vibration monitoring
US20070034496A1 (en) * 2001-03-12 2007-02-15 Lah Ruben F Delayed coker isolation valve systems
US20070251576A1 (en) * 2006-03-09 2007-11-01 Lah Ruben F Valve Body and Condensate Holding Tank Flushing Systems and Methods
US20080143059A1 (en) * 2003-04-11 2008-06-19 Lah Ruben F Dynamic Flange Seal and Sealing System
US20090145810A1 (en) * 2006-11-17 2009-06-11 Etter Roger G Addition of a Reactor Process to a Coking Process
US20090152165A1 (en) * 2006-11-17 2009-06-18 Etter Roger G System and Method for Introducing an Additive into a Coking Process to Improve Quality and Yields of Coker Products
US20090183980A1 (en) * 2008-01-23 2009-07-23 Lah Ruben F Coke Drum Skirt
US20090200152A1 (en) * 2004-04-22 2009-08-13 Lah Ruben F Remotely Controlled Decoking Tool Used in Coke Cutting Operations
US20090209799A1 (en) * 2006-11-17 2009-08-20 Etter Roger G System and Method of Introducing an Additive with a Unique Catalyst to a Coking Process
US20090214394A1 (en) * 2003-02-21 2009-08-27 Lah Ruben F Center feed system
US20090236212A1 (en) * 2008-01-23 2009-09-24 Lah Ruben F Linked coke drum support
US7632381B2 (en) 2001-03-12 2009-12-15 Curtiss-Wright Flow Control Corporation Systems for providing continuous containment of delayed coker unit operations
US20100170827A1 (en) * 2006-11-17 2010-07-08 Etter Roger G Selective Cracking and Coking of Undesirable Components in Coker Recycle and Gas Oils
US20100252409A1 (en) * 2009-02-11 2010-10-07 Lah Ruben F Center Feed System
US7819009B2 (en) 2006-02-28 2010-10-26 Frederic Borah Vibration Monitoring System
US7820014B2 (en) 2004-04-22 2010-10-26 Lah Ruben F Systems and methods for remotely determining and changing cutting modes during decoking
US20110083747A1 (en) * 2009-03-23 2011-04-14 Christopher Orino Non-Rising Electric Actuated Valve Operator
US8123197B2 (en) 2001-03-12 2012-02-28 Curtiss-Wright Flow Control Corporation Ethylene production isolation valve systems
WO2012162008A1 (en) * 2011-05-23 2012-11-29 Saudi Arabian Oil Company Process for delayed coking of whole crude oil
CN103045278A (zh) * 2011-10-17 2013-04-17 中国石油化工股份有限公司 一种釜式制备针状焦的方法
US8459608B2 (en) 2009-07-31 2013-06-11 Curtiss-Wright Flow Control Corporation Seat and valve systems for use in delayed coker system
US8679299B2 (en) 2001-03-12 2014-03-25 Curtiss-Wright Flow Control Corporation Coke drum bottom de-heading system
US9011672B2 (en) 2006-11-17 2015-04-21 Roger G. Etter System and method of introducing an additive with a unique catalyst to a coking process
US11072745B1 (en) 2020-04-20 2021-07-27 Saudi Arabian Oil Company Two-stage delayed coking process to produce anode grade coke

Families Citing this family (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB1378123A (en) * 1972-06-12 1974-12-18 Continental Oil Co Electrode grade petroleum coke process
JPS5233557U (enrdf_load_stackoverflow) * 1975-08-29 1977-03-09
AU544773B2 (en) * 1979-10-01 1985-06-13 Standard Oil Company, The Co-coking shale oil and petroleum residual
RU2537859C1 (ru) * 2013-06-18 2015-01-10 Государственное унитарное предприятие "Институт нефтехимпереработки Республики Башкортостан" (ГУП "ИНХП РБ") Способ термодеструкции нефтяных остатков
US10832226B2 (en) 2014-09-30 2020-11-10 Ricoh Company, Ltd. System and service determination method
JP6536213B2 (ja) 2015-06-23 2019-07-03 株式会社リコー システム及びサービス決定方法

Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2775549A (en) * 1954-01-25 1956-12-25 Great Lakes Carbon Corp Production of coke from petroleum hydrocarbons
US2922755A (en) * 1957-10-14 1960-01-26 Jr Roy C Hackley Manufacture of graphitizable petroleum coke

Patent Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2775549A (en) * 1954-01-25 1956-12-25 Great Lakes Carbon Corp Production of coke from petroleum hydrocarbons
US2922755A (en) * 1957-10-14 1960-01-26 Jr Roy C Hackley Manufacture of graphitizable petroleum coke

Cited By (84)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3959115A (en) * 1972-03-01 1976-05-25 Maruzen Petrochemical Co., Ltd. Production of petroleum cokes
US3954597A (en) * 1974-03-27 1976-05-04 Morrell Jacque C Process for the production of distillate fuels from oil shales and by-products therefrom
US4029749A (en) * 1974-11-29 1977-06-14 Mitsui Coke Co. Ltd. Process for manufacturing needle coke
US4242196A (en) * 1978-10-27 1980-12-30 Kureha Kagaku Kogyo Kabushiki Kaisha Mass production system of highly aromatic petroleum pitch
US4235700A (en) * 1979-10-12 1980-11-25 Exxon Research & Engineering Co. Two-stage coking for the production of low metals coke
US4518486A (en) * 1980-12-24 1985-05-21 The Standard Oil Company Concurrent production of two grades of coke using a single fractionator
US4351702A (en) * 1981-09-08 1982-09-28 Conoco Inc. Processing of heavy high-sulfur feedstocks
US4551232A (en) * 1983-02-09 1985-11-05 Intevep, S.A. Process and facility for making coke suitable for metallurgical purposes
US4501654A (en) * 1983-11-17 1985-02-26 Exxon Research & Engineering Co. Delayed coking process with split fresh feed and top feeding
US4492625A (en) * 1983-11-17 1985-01-08 Exxon Research And Engineering Co. Delayed coking process with split fresh feed
US5316655A (en) * 1990-02-20 1994-05-31 The Standard Oil Company Process for making light hydrocarbonaceous liquids in a delayed coker
US5350503A (en) * 1992-07-29 1994-09-27 Atlantic Richfield Company Method of producing consistent high quality coke
US6168709B1 (en) 1998-08-20 2001-01-02 Roger G. Etter Production and use of a premium fuel grade petroleum coke
US20060032788A1 (en) * 1999-08-20 2006-02-16 Etter Roger G Production and use of a premium fuel grade petroleum coke
US9475992B2 (en) 1999-08-20 2016-10-25 Roger G. Etter Production and use of a premium fuel grade petroleum coke
US8679299B2 (en) 2001-03-12 2014-03-25 Curtiss-Wright Flow Control Corporation Coke drum bottom de-heading system
US7632381B2 (en) 2001-03-12 2009-12-15 Curtiss-Wright Flow Control Corporation Systems for providing continuous containment of delayed coker unit operations
US20070084714A1 (en) * 2001-03-12 2007-04-19 Lah Ruben F Valve system and method for unheading a coke drum
US20070034496A1 (en) * 2001-03-12 2007-02-15 Lah Ruben F Delayed coker isolation valve systems
US7578907B2 (en) 2001-03-12 2009-08-25 Curtiss-Wright Flow Control Corporation Valve system for unheading a coke drum
US8123197B2 (en) 2001-03-12 2012-02-28 Curtiss-Wright Flow Control Corporation Ethylene production isolation valve systems
US8282074B2 (en) 2001-03-12 2012-10-09 Curtiss-Wright Flow Control Corporation Delayed coker isolation valve systems
US8512525B2 (en) 2001-03-12 2013-08-20 Curtiss-Wright Flow Control Corporation Valve system and method for unheading a coke drum
US20040154913A1 (en) * 2001-03-12 2004-08-12 Lah Ruben F. Valve system and method for unheading a coke drum
US7247220B2 (en) 2001-11-09 2007-07-24 Foster Wheeler Usa Corporation Coke drum discharge system
US7438786B2 (en) 2001-11-09 2008-10-21 Foster Wheeler Usa Corporation Coke drum discharge system
US20040238408A1 (en) * 2001-11-09 2004-12-02 Foster Wheeler Usa Corporation Coke drum discharge system
US20030089589A1 (en) * 2001-11-09 2003-05-15 Foster Wheeler Usa Corporation Coke drum discharge system
US7033460B2 (en) 2002-09-05 2006-04-25 Curtiss-Wright Flow Control Corportaion Coke drum bottom throttling valve and system
US20060175188A1 (en) * 2002-09-05 2006-08-10 Lah Ruben F Coke drum bottom throttling valve and system
US20050092592A1 (en) * 2002-09-05 2005-05-05 Lah Ruben F. Systems and methods for deheading a coke drum
US20050034969A1 (en) * 2002-09-05 2005-02-17 Lah Ruben F. Coke drum bottom throttling valve and system
US6843889B2 (en) 2002-09-05 2005-01-18 Curtiss-Wright Flow Control Corporation Coke drum bottom throttling valve and system
US20040045803A1 (en) * 2002-09-05 2004-03-11 Lah Ruben F. Coke drum bottom throttling valve and system
US7459063B2 (en) 2002-09-05 2008-12-02 Curtiss-Wright Flow Control Corporation Systems and methods for deheading a coke drum
US7399384B2 (en) 2002-09-05 2008-07-15 Curtiss-Wright Flow Control Corporation Coke drum bottom throttling valve and system
US8702911B2 (en) 2003-02-21 2014-04-22 Curtiss-Wright Flow Control Corporation Center feed system
US20090214394A1 (en) * 2003-02-21 2009-08-27 Lah Ruben F Center feed system
US7530574B2 (en) 2003-04-11 2009-05-12 Curtiss-Wright Flow Control Corporation Dynamic flange seal and sealing system
US7682490B2 (en) 2003-04-11 2010-03-23 Curtiss-Wright Flow Control Corporation Dynamic flange seal and sealing system
US20080143059A1 (en) * 2003-04-11 2008-06-19 Lah Ruben F Dynamic Flange Seal and Sealing System
US20060081456A1 (en) * 2004-04-22 2006-04-20 Lah Ruben F Remotely controlled decoking tool used in coke cutting operations
US7473337B2 (en) 2004-04-22 2009-01-06 Curtiss-Wright Flow Control Corporation Remotely controlled decoking tool used in coke cutting operations
US8197644B2 (en) 2004-04-22 2012-06-12 Curtiss-Wright Flow Control Corporation Remotely controlled decoking tool used in coke cutting operations
US7820014B2 (en) 2004-04-22 2010-10-26 Lah Ruben F Systems and methods for remotely determining and changing cutting modes during decoking
US20090200152A1 (en) * 2004-04-22 2009-08-13 Lah Ruben F Remotely Controlled Decoking Tool Used in Coke Cutting Operations
US8679298B2 (en) 2004-04-22 2014-03-25 Curtiss-Wright Flow Control Corporation Remotely controlled decoking tool used in coke cutting operations
WO2006000276A1 (en) * 2004-05-12 2006-01-05 Sgl Carbon Ag Graphite electrode for electrothermic reduction furnaces, electrode column, and method of producing graphite electrodes
DE102004035934B4 (de) * 2004-06-25 2006-09-14 Indian Oil Corp. Ltd., Mumbai Verfahren zur Erzeugung von Nadelkoks
US7604731B2 (en) 2004-06-25 2009-10-20 Indian Oil Corporation Limited Process for the production of needle coke
DE102004035934A1 (de) * 2004-06-25 2006-01-19 Indian Oil Corp. Ltd., Mumbai Ein Verfahren zur Erzeugung von Nadelkoks
US20070181462A2 (en) * 2004-06-25 2007-08-09 Debasis Bhattacharyya A process for the production of needle coke
US20050284793A1 (en) * 2004-06-25 2005-12-29 Debasis Bhattacharyya Process for the production of needle coke
US20070038393A1 (en) * 2005-08-12 2007-02-15 Frederic Borah Vibration monitoring
US7819009B2 (en) 2006-02-28 2010-10-26 Frederic Borah Vibration Monitoring System
US7931044B2 (en) 2006-03-09 2011-04-26 Curtiss-Wright Flow Control Corporation Valve body and condensate holding tank flushing systems and methods
US20070251576A1 (en) * 2006-03-09 2007-11-01 Lah Ruben F Valve Body and Condensate Holding Tank Flushing Systems and Methods
US20090152165A1 (en) * 2006-11-17 2009-06-18 Etter Roger G System and Method for Introducing an Additive into a Coking Process to Improve Quality and Yields of Coker Products
US20100170827A1 (en) * 2006-11-17 2010-07-08 Etter Roger G Selective Cracking and Coking of Undesirable Components in Coker Recycle and Gas Oils
US20090145810A1 (en) * 2006-11-17 2009-06-11 Etter Roger G Addition of a Reactor Process to a Coking Process
US8206574B2 (en) 2006-11-17 2012-06-26 Etter Roger G Addition of a reactor process to a coking process
US9187701B2 (en) 2006-11-17 2015-11-17 Roger G. Etter Reactions with undesirable components in a coking process
US9150796B2 (en) 2006-11-17 2015-10-06 Roger G. Etter Addition of a modified vapor line reactor process to a coking process
US8361310B2 (en) 2006-11-17 2013-01-29 Etter Roger G System and method of introducing an additive with a unique catalyst to a coking process
US8372264B2 (en) 2006-11-17 2013-02-12 Roger G. Etter System and method for introducing an additive into a coking process to improve quality and yields of coker products
US8372265B2 (en) 2006-11-17 2013-02-12 Roger G. Etter Catalytic cracking of undesirable components in a coking process
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Also Published As

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NO126380B (enrdf_load_stackoverflow) 1973-01-29
JPS4943241B1 (enrdf_load_stackoverflow) 1974-11-20
DE2024804B2 (de) 1974-08-08
GB1263196A (en) 1972-02-09
ES380055A1 (es) 1972-08-01
DE2024804A1 (de) 1970-12-10

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