US20030102250A1 - Delayed coking process for producing anisotropic free-flowing shot coke - Google Patents

Delayed coking process for producing anisotropic free-flowing shot coke Download PDF

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Publication number
US20030102250A1
US20030102250A1 US10/293,373 US29337302A US2003102250A1 US 20030102250 A1 US20030102250 A1 US 20030102250A1 US 29337302 A US29337302 A US 29337302A US 2003102250 A1 US2003102250 A1 US 2003102250A1
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United States
Prior art keywords
coke
residuum
flowing
coking
anisotropic
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Abandoned
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US10/293,373
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English (en)
Inventor
Michael Siskin
David Ferrughelli
Martin Gorbaty
Simon Kelemen
Leo Brown
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ExxonMobil Technology and Engineering Co
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Individual
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Priority to US10/293,373 priority Critical patent/US20030102250A1/en
Priority to ARP020104644A priority patent/AR037685A1/es
Priority to CNA028240057A priority patent/CN1599784A/zh
Priority to PCT/US2002/038699 priority patent/WO2003048271A1/en
Priority to JP2003549451A priority patent/JP2006500431A/ja
Priority to AU2002359593A priority patent/AU2002359593A1/en
Priority to EP02794141A priority patent/EP1451266A1/en
Priority to CA002468711A priority patent/CA2468711A1/en
Assigned to EXXONMOBIL RESEARCH & ENGINEERING CO. reassignment EXXONMOBIL RESEARCH & ENGINEERING CO. ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: KELEMEN, SIMON R., BROWN, LEO D., FERRUGHELLI, DAVID T., GORBATY, MARTIN L., SISKIN, MICHAEL
Publication of US20030102250A1 publication Critical patent/US20030102250A1/en
Priority to US11/256,728 priority patent/US8147676B2/en
Abandoned legal-status Critical Current

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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
    • C10G55/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process
    • C10G55/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process plural serial stages only
    • C10G55/04—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process plural serial stages only including at least one thermal cracking step
    • 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
    • C10B57/08—Non-mechanical pretreatment of the charge, e.g. desulfurization
    • 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
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/107—Atmospheric residues having a boiling point of at least about 538 °C

Definitions

  • the present invention relates to a delayed coking process wherein substantially all of the coke produced is free-flowing anisotropic shot coke.
  • a coker feedstock such as a vacuum residuum
  • an oxidizing agent such as air
  • the oxidized feedstock is then heated to coking temperatures and passed to a coker drum for an effective amount of time to allow volatiles to evolve and to produce a substantially free-flowing anisotropic shot coke.
  • Delayed coking has been practiced for many years. The process broadly involves thermal decomposition of petroleum residua (resids) to produce gas, liquid streams of various boiling ranges, and coke. Delayed coking of resids from heavy, and heavy sour (high sulfur) crude oils is carried out primarily as a means of disposing of these low value feedstocks by converting part of the resids to more valuable liquid and gas products. Although the resulting coke is generally thought of as a low value by-product, it does have some value as a fuel (fuel grade), electrodes for aluminum manufacture (anode grade), etc.
  • the feedstock is rapidly heated in a fired heater or tubular furnace. It is then passed to a coking drum that is maintained at conditions under which coking occurs, generally at temperatures above about 400° C. under super-atmospheric pressures.
  • the heated residuum feed further decomposes in the coker drum to form volatile components that are removed overhead and passed to a fractionator leaving coke behind.
  • the coker drum is full of coke the heated feed is switched to another drum and hydrocarbon vapors are purged from the coke drum with steam.
  • the drum is then quenched with water to lower the temperature to about 200-300° F. after which the water is drained.
  • the drum is opened and the coke is removed after drilling and/or cutting using high velocity water jets.
  • a high speed, high impact water jet is used to cut the coke from the drum.
  • a hole is typically bored in the coke from water jet nozzles located on a boring tool.
  • Nozzles oriented horizontally on the head of a cutting tool cut the coke from the drum.
  • the coke removal process adds considerably to the throughput time of the process. That is, since it takes approximately 1 to 6 hours, typically about 3 hours to drill-out and remove the resulting coke mass, the coker drum turn-around time and process costs are increased.
  • the coking drum may appear to be completely cooled, occasionally, a problem arises which is referred to in the art as a “hot drum.” This problem occurs when areas of the drum do not completely cool. This may be the result of a combination of morphologies of coke in the drum resulting in a non-uniform drum.
  • the drum may contain a combination of more than one type of solid coke product, i.e., needle coke, sponge coke and shot coke. BB-sized shot coke may cool faster than another coke, such as large shot coke masses or sponge coke. Avoiding “hot drums” is another reason for producing predominantly shot coke in a delayed coker.
  • Isotropic coke is coke that has thermal expansion approximately equal along the three crystalline axes. This is achieved by air blowing a petroleum resid feedstock to a certain softening point and running the coking process at relatively high recycle ratios and preferably with a diluent oil.
  • a delayed coking process wherein substantially all of the coke produced is substantially free flowing anisotropic shot coke which process comprises:
  • a delayed coking process comprising:
  • the oxidizing agent is air.
  • a caustic can be added to the oxidized resid coker feedstock before, during, or after heating in the coker furnace.
  • FIG. 1 hereof is a cross polarized light photomicrograph of coke resulting from a San Joaquin Valley vacuum residuum that was not treated with an oxidizing agent prior to coking.
  • the area of view is 170 microns by 136 microns.
  • FIG. 2 hereof is a photomicrograph of coke resulting from a San Joaquin Valley vacuum residuum that was treated with air for 3 hours at a temperature from 185° C. to 225° C. prior to coking.
  • the area of view is 170 microns by 136 microns.
  • Feedstocks suitable for the delayed coking process of the present invention are petroleum vacuum residua.
  • Such petroleum residua are frequently obtained after removal of distillates from crude feedstocks under vacuum and are characterized as being comprised of components of large molecular size and weight, generally containing: (a) asphaltenes and other high molecular weight aromatic structures that would inhibit the rate of hydrotreating/hydrocracking and cause catalyst deactivation; (b) metal contaminants occurring naturally in the crude or resulting from prior treatment of the crude, which contaminants would tend to deactivate hydrotreating/hydrocracking catalysts and interfere with catalyst regeneration; and (c) a relatively high content of sulfur and nitrogen compounds that give rise to objectionable quantities of SO 2 , SO 3 , and NO x upon combustion of the petroleum residuum.
  • Nitrogen compounds also have a tendency to deactivate catalytic cracking catalysts.
  • Typical examples of coker petroleum feedstocks which are contemplated for use in the present invention, include residues from the atmospheric and vacuum distillation of petroleum crudes or the atmospheric or vacuum distillation of heavy oils, visbroken resids, tars from deasphalting units or combinations of these materials. Atmospheric and vacuum topped heavy bitumens can also be employed.
  • these feedstocks are high-boiling hydrocarbonaceous materials having a nominal initial boiling point of about 538° C. or higher, an API gravity of about 20° or less, and a Conradson Carbon Residue content of about 0 to 40 weight percent.
  • the coking process of the present invention is delayed coking, which is well known in the art.
  • a bottoms fraction such as a petroleum residuum chargestock is pumped to a heater at a pressure of about 50 to 550 psig, where it is heated to a temperature from about 480° C. to about 520° C. It is then discharged into a vertically oriented insulated coker drum through an inlet at the base of the drum.
  • Pressure in the drum is usually relatively low, such as about 15 to 50 psig to allow volatiles to be removed overhead. Typical operating temperatures of the drum will be between about 410° C. and 475° C.
  • the hot feedstock thermally cracks over a period of time in the coker drum, liberating volatiles composed primarily of hydrocarbon products, that continuously rise through the coke mass and are collected overhead.
  • the volatile products are sent to a coker fractionator for distillation and recovery of coker gases, gasoline, light gas oil, and heavy gas oil. At least a portion of the heavy coker gas oil present in the product stream introduced into the coker fractionator is captured for recycle and combined with the fresh feed (coker feed component), thereby forming the coker heater or coker furnace charge.
  • Needle coke is the highest quality of the three varieties. Needle coke, upon further thermal treatment, has high conductivity and is used in electric arc steel production. It is relatively low in sulfur and metals and is produced from some of the higher quality coker feedstocks that include more aromatic feedstocks such as slurry and decant oils from catalytic crackers and thermal cracking tars as opposed to the asphaltenes and resins.
  • Sponge coke a lower quality coke, sometimes called “regular coke,” is most often formed in refineries.
  • Low quality refinery coker feedstocks having significant amounts of asphaltenes, heteroatoms and metals produce this lower quality coke.
  • sponge coke can be used for the manufacture of electrodes for the aluminum industry. If the sulfur and metals content is too high, then the coke can be used as fuel.
  • the name “sponge coke” comes from its porous, sponge-like appearance.
  • Conventional delayed coking processes, using the preferred vacuum resid feedstock of the present invention will typically produce sponge coke, which is produced as an agglomerated mass that needs an extensive removal process including drilling and water-jet technology. This adds considerable time and costs to the process.
  • Shot coke has been considered the lowest quality coke because it has the highest sulfur and metals content, the lowest electrical conductivity and is the most difficult to grind.
  • the term “shot coke” comes from its shape which is similar to that of BB sized (about ⁇ fraction (1/16) ⁇ inch to 3 ⁇ 8 inch) balls. Shot coke, like the other types of coke, has a tendency to agglomerate, especially in admixture with sponge coke, into larger masses, sometimes larger than a foot in diameter. This can cause refinery equipment and processing problems. Shot coke is usually made from the lowest quality high resin-asphaltene feeds and makes a good high sulfur fuel source, particularly for use in cement kilns and steel manufacture.
  • substantially free-flowing anisotropic shot coke can be produced by first treating the residuum feedstock with an oxidizing agent to substantially increase the contents of its asphaltene, and/or polars fractions, such as those containing organically bound oxygen like ketones, carboxylic acids, etc.
  • the residuum feed is subjected to the oxidizing agent, preferably air, at effective temperatures, i.e., at temperatures that will encourage the formation of asphaltenes and organically bound oxygen groups to form.
  • Such temperatures will typically be from about 150° C. to about 325° C., preferably from about 185° C. to about 280° C., more preferably from about 185° C. to about 250° C.
  • the oxidizing agent can be in any suitable form including gas, liquid or solid.
  • oxidizing agents that can be used in the practice of the present invention include air, oxygen, ozone, hydrogen peroxide, organic peroxides, hydroperoxides, inorganic peracids, inorganic oxides and peroxides and salts of oxides, sulfuric acid, and nitric acid. Preferred is air.
  • a caustic preferably a spent caustic, may optionally be added.
  • the spent caustic can also be added before, during, or after the oxidized resid is passed to the coker furnace and heated to coking temperatures.
  • the caustic will be an alkali-metal material preferably a spent caustic soda and/or potash stream that is typically used in various refinery processes.
  • Such spent caustic streams typically contain one or more of sodium and potassium, sulfur, and other wastes, including organic contaminants that vary depending on the hydrocarbon source but can be organic acids, dissolved hydrocarbons, phenols, naphthenic acids, and salts of organic acids.
  • the spent caustic stream will usually have a relatively high water content, typically about 50 wt. % to 95 wt. % water, more typically from about 65 wt. % to about 80 wt. %.
  • the desired coke morphology that will produce substantially free-flowing coke is a coke microstructure of discrete micro-domains having an average size of about 1 to 10 ⁇ m, preferably from about 1 to 5 ⁇ m, somewhat like a mosaic (FIG. 2 hereof).
  • Coke microstructure that represents coke that is not free-flowing anisotropic shot coke is the microstructure represented in FIG. 1 hereof that show a coke microstructure that is composed substantially of non-discrete, or substantially large flow domains up to about 60 ⁇ m or greater in size, typically from about 10 to 60 ⁇ m.
  • U.S. Pat. No. 3,960,704 which is incorporated herein by reference, teaches delayed coking wherein a resid feedstock is air blown to a target softening point. The air blown feed is then passed to delayed coking process that is operated at conditions that will favor the formation of isotropic coke. That is, coke particles having substantially equal thermal expansion properties along the three major crystalline axes.
  • This '704 patent requires relatively high recycle ratios and an additional amount of oil as a diluent to produce a pellet-type isotropic coke.
  • the recycle ratio of this '704 patent is from about 1 to 5. This correlates to 100% to 500% recycle based on fresh feed.
  • the resid feedstock be first treated with an oxidizing agent to substantially increase its level of asphaltenes, polars, and organically bound oxygen groups that encourages the formation of anisotropic substantially free-flowing shot coke. It is also important to the practice of the present invention that the coker drum be kept at relatively low pressures in order to allow as much of the evolving volatiles to be collected overhead. This helps prevent agglomeration of the resulting shot coke.
  • the recycle ratio that is the volumetric ratio of furnace charge (vacuum resid plus recycle oil) to fresh feed to the continuous delayed coker operation should also be kept as low as possible. The use of recycle ratio for delayed coking is taught in more detail in U.S. Pat. No. 3,116,231 which is incorporated herein by reference.
  • Microcarbon residue tests were performed on the above feeds to generate cokes to be evaluated by microscopy. The following is the procedure used for the microcarbon tests: Heating Profile Time (min) N2 Flow (cc/min) Heat from room temp to 10 66 100° C. Heat from 100° C. to 30 66/19.5 300° C. then to 500° C. Hold at 500° C. 15 19.5 Cool to room temp 40 19.5
  • FIGS. 1 and 2 are cross polarized light photomicrographs showing the microstructure of the resulting coke from a San Joaquin Valley residuum for both the untreated residuum and the residuum treated with air in accordance with the above procedure.
  • the viewing area for both is 170 microns by 136 microns.
  • the untreated residuum resulted in a coke with a microstructure that was not discrete fine domains.
  • the domains were relatively large (10-30 ⁇ m) flow domains. This indicates that a mixture of shot coke and sponge coke will be produced in the coker drum of a delayed coker.
  • the microstructure (FIG.

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  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Materials Engineering (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Coke Industry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
US10/293,373 2001-12-04 2002-11-12 Delayed coking process for producing anisotropic free-flowing shot coke Abandoned US20030102250A1 (en)

Priority Applications (9)

Application Number Priority Date Filing Date Title
US10/293,373 US20030102250A1 (en) 2001-12-04 2002-11-12 Delayed coking process for producing anisotropic free-flowing shot coke
ARP020104644A AR037685A1 (es) 2001-12-04 2002-12-02 Proceso de coquizacion retardada para la produccion de coque anisotropico suelto en forma de granalla
AU2002359593A AU2002359593A1 (en) 2001-12-04 2002-12-03 Delayed cooking process for producing anisotropic free-flowing shot coke
PCT/US2002/038699 WO2003048271A1 (en) 2001-12-04 2002-12-03 Delayed coking process for producing anisotropic free-flowing shot coke
JP2003549451A JP2006500431A (ja) 2001-12-04 2002-12-03 異方性の自由流動性ショットコークを製造するためのディレードコーキング方法
CNA028240057A CN1599784A (zh) 2001-12-04 2002-12-03 生产各向异性自由流动细粒焦炭的延迟焦化方法
EP02794141A EP1451266A1 (en) 2001-12-04 2002-12-03 Delayed coking process for producing anisotropic free-flowing shot coke
CA002468711A CA2468711A1 (en) 2001-12-04 2002-12-03 Delayed coking process for producing anisotropic free-flowing shot coke
US11/256,728 US8147676B2 (en) 2001-12-04 2005-10-21 Delayed coking process

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US33677801P 2001-12-04 2001-12-04
US10/293,373 US20030102250A1 (en) 2001-12-04 2002-11-12 Delayed coking process for producing anisotropic free-flowing shot coke

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US11/256,728 Continuation-In-Part US8147676B2 (en) 2001-12-04 2005-10-21 Delayed coking process

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EP (1) EP1451266A1 (ja)
JP (1) JP2006500431A (ja)
CN (1) CN1599784A (ja)
AR (1) AR037685A1 (ja)
AU (1) AU2002359593A1 (ja)
CA (1) CA2468711A1 (ja)
WO (1) WO2003048271A1 (ja)

Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20050269247A1 (en) * 2004-05-14 2005-12-08 Sparks Steven W Production and removal of free-flowing coke from delayed coker drum
US20070284283A1 (en) * 2006-06-08 2007-12-13 Western Oil Sands Usa, Inc. Oxidation of asphaltenes
CN102435605A (zh) * 2011-09-19 2012-05-02 中国石油天然气股份有限公司 一种优选延迟焦化加热炉出口温度的方法
US20130075303A1 (en) * 2010-04-13 2013-03-28 IFP Energies Nouvelles Process for hydroconversion of petroleum feedstocks via a slurry technology allowing the recovery of metals from the catalyst and from the feedstock using a coking step
US9273377B2 (en) 2010-03-04 2016-03-01 Intevep, S.A. Method of metals recovery from refinery residues
US10934494B2 (en) 2019-04-09 2021-03-02 Indian Oil Corporation Limited Process for production of anisotropic coke

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US8147676B2 (en) * 2001-12-04 2012-04-03 Exxonmobil Research And Engineering Company Delayed coking process
WO2004104139A1 (en) * 2003-05-16 2004-12-02 Exxonmobil Research And Engineering Company Delayed coking process for producing free-flowing shot coke
US7658838B2 (en) 2003-05-16 2010-02-09 Exxonmobil Research And Engineering Company Delayed coking process for producing free-flowing coke using polymeric additives
US7645375B2 (en) 2003-05-16 2010-01-12 Exxonmobil Research And Engineering Company Delayed coking process for producing free-flowing coke using low molecular weight aromatic additives
CN1954052A (zh) 2004-05-14 2007-04-25 埃克森美孚研究工程公司 抑制剂增强的重油热改质
JP2007537343A (ja) 2004-05-14 2007-12-20 エクソンモービル　リサーチ　アンド　エンジニアリング　カンパニー コーカードラムからの取り出しがより容易なコークスを製造するための原料残油のブレンディング
CA2566117C (en) 2004-05-14 2012-12-04 Exxonmobil Research And Engineering Company Viscoelastic upgrading of heavy oil by altering its elastic modulus
US7914668B2 (en) * 2005-11-14 2011-03-29 Exxonmobil Research & Engineering Company Continuous coking process
US7871510B2 (en) 2007-08-28 2011-01-18 Exxonmobil Research & Engineering Co. Production of an enhanced resid coker feed using ultrafiltration
US7794587B2 (en) 2008-01-22 2010-09-14 Exxonmobil Research And Engineering Company Method to alter coke morphology using metal salts of aromatic sulfonic acids and/or polysulfonic acids
JP5728475B2 (ja) * 2010-05-31 2015-06-03 Ｊｘ日鉱日石エネルギー株式会社 リチウムイオン二次電池負極材料用原料炭組成物
CN102899079B (zh) * 2011-07-27 2014-09-10 中国石油化工股份有限公司 一种延迟焦化方法
CN103805226B (zh) * 2012-11-02 2016-05-11 中国石油化工集团公司 一种延迟焦化方法
JP6198640B2 (ja) * 2014-03-04 2017-09-20 株式会社神戸製鋼所 石油コークス吹込み高炉操業方法
US10053630B2 (en) 2014-05-14 2018-08-21 Exxonmobil Research And Engineering Company Control of coke morphology in delayed coking
US10591456B2 (en) 2016-03-30 2020-03-17 Exxonmobil Research And Engineering Company In situ monitoring of coke morphology in a delayed coker using AC impedance

Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3960704A (en) * 1974-08-27 1976-06-01 Continental Oil Company Manufacture of isotropic delayed petroleum coke
US5258115A (en) * 1991-10-21 1993-11-02 Mobil Oil Corporation Delayed coking with refinery caustic

Family Cites Families (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB844698A (en) * 1956-12-13 1960-08-17 British Petroleum Co Improvements relating to the production of petroleum coke
US3702816A (en) * 1970-06-29 1972-11-14 Exxon Research Engineering Co Low sulfur coke from virgin residua

Patent Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3960704A (en) * 1974-08-27 1976-06-01 Continental Oil Company Manufacture of isotropic delayed petroleum coke
US5258115A (en) * 1991-10-21 1993-11-02 Mobil Oil Corporation Delayed coking with refinery caustic

Cited By (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20050269247A1 (en) * 2004-05-14 2005-12-08 Sparks Steven W Production and removal of free-flowing coke from delayed coker drum
US7727382B2 (en) * 2004-05-14 2010-06-01 Exxonmobil Research And Engineering Company Production and removal of free-flowing coke from delayed coker drum
US20070284283A1 (en) * 2006-06-08 2007-12-13 Western Oil Sands Usa, Inc. Oxidation of asphaltenes
US7811444B2 (en) * 2006-06-08 2010-10-12 Marathon Oil Canada Corporation Oxidation of asphaltenes
US8529687B2 (en) 2006-06-08 2013-09-10 Marathon Oil Canada Corporation Oxidation of asphaltenes
US9273377B2 (en) 2010-03-04 2016-03-01 Intevep, S.A. Method of metals recovery from refinery residues
US20130075303A1 (en) * 2010-04-13 2013-03-28 IFP Energies Nouvelles Process for hydroconversion of petroleum feedstocks via a slurry technology allowing the recovery of metals from the catalyst and from the feedstock using a coking step
CN102435605A (zh) * 2011-09-19 2012-05-02 中国石油天然气股份有限公司 一种优选延迟焦化加热炉出口温度的方法
US10934494B2 (en) 2019-04-09 2021-03-02 Indian Oil Corporation Limited Process for production of anisotropic coke

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JP2006500431A (ja) 2006-01-05
WO2003048271A1 (en) 2003-06-12
EP1451266A1 (en) 2004-09-01
CA2468711A1 (en) 2003-06-12
AR037685A1 (es) 2004-12-01
AU2002359593A1 (en) 2003-06-17
CN1599784A (zh) 2005-03-23

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