EP0156614A2 - Cokéfaction de résidu en présence d'un donneur d'hydrogène - Google Patents

Cokéfaction de résidu en présence d'un donneur d'hydrogène Download PDF

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Publication number
EP0156614A2
EP0156614A2 EP85301883A EP85301883A EP0156614A2 EP 0156614 A2 EP0156614 A2 EP 0156614A2 EP 85301883 A EP85301883 A EP 85301883A EP 85301883 A EP85301883 A EP 85301883A EP 0156614 A2 EP0156614 A2 EP 0156614A2
Authority
EP
European Patent Office
Prior art keywords
hydrogen
donating
feedstock
diluent
zone
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Granted
Application number
EP85301883A
Other languages
German (de)
English (en)
Other versions
EP0156614B1 (fr
EP0156614A3 (en
Inventor
Hanbury John Woods
Frank Souhrada
Kenneth Robert Dymock
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Gulf Canada Ltd
Original Assignee
Gulf Canada Resources Inc
Gulf Canada Ltd
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Gulf Canada Resources Inc, Gulf Canada Ltd filed Critical Gulf Canada Resources Inc
Publication of EP0156614A2 publication Critical patent/EP0156614A2/fr
Publication of EP0156614A3 publication Critical patent/EP0156614A3/en
Application granted granted Critical
Publication of EP0156614B1 publication Critical patent/EP0156614B1/fr
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

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Classifications

    • 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
    • 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
    • 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
    • C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G9/005—Coking (in order to produce liquid products mainly)

Definitions

  • the present invention relates to a process for obtaining increased yields of liquid hydrocarbons from coking feedstocks by introducing hydrogen-donating hydrocarbon material together with the feedstock.
  • gas oil and/or residuum is heated rapidly to coking temperature, initiating thermal breakdown, and passed into a coking drum, where the hot material continues thermal breakdown and conversion to lighter hydrocarbons and coke.
  • Coke yields in such processes can'be as large as 30% or more, and the production of large amounts of this low-valued material is uneconomic.
  • Processes known in the art include the manufacture of premium coke, that is, coke having a low coefficient of thermal expansion (CTE), which is higher-valued than conventional coke.
  • CTE coefficient of thermal expansion
  • Coal was slurried with a hydrogen donor solvent boiling in the range from 177°C to 482°C, liquefied and the bottoms, containing liquid liquefaction products, non-liquefied solid coal particles and unconsumed hydrogen-donor solvent was passed to a fluid coking zone.
  • No temperature range of operation of the fluid coking zone was disclosed, but the examples of the process were each operated at 538°C. Delayed coking was suggested as an alternative to fluid coking, but no operating conditions were disclosed.
  • the present invention provides a method for treating heavy hydrocarbonaceous oil feedstock, comprising:
  • the invention also resides in a method for reducing the amount of coke production in the coking of heavy hydrocarbonaceous oil feedstock, comprising the steps as listed above.
  • the process of the invention utilises a hydrogen-donating hydrocarbon diluent to provide sufficient hydrogen to add to at least a portion of the radicals that are created from the residuum feedstock when it is exposed to temperatures in the coking range, i.e. from 42D°C to 500°C:
  • the hydrogen-donating diluent has a boiling range from 180°C to 400°C, preferably from 200°C to 350°C, at atmospheric pressure.
  • the donor diluent can be a highly aromatic light cycle oil generated in a catalytic cracking process; the oil is partially hydrogenated by known methods to produce a hydrogen donor diluent containing, for example, tetralin and substituted tetralins.
  • hydrogen-donating compounds and hydrogen donor precursors together comprise at least 40 percent of the hydrogen donor diluent.
  • Hydrocarbons boiling in the upper portion of the aforementioned broad boiling range that is, boiling from about 350°C to 400°C, generally participate to a minor degree, if at all, as hydrogen-donating materials during donor hydrocracking.
  • Some of those hydrocarbons, called herein hydrogen donor precursors are converted during donor hydrocracking into compounds that can be partially hydrogenated to hydrogen-donating compounds boiling in the aforementioned broad boiling range.
  • the hydrogen-donating diluent can advantageously include materials boiling up to 400°C.
  • the proportion of hydrogen-donating hydrocarbon diluent in relation to the residuum feedstock can be from about 0.02:1 to 1.0:1, preferably from 0.15:1 to 0.5:1.
  • a portion of the hydrogen donor requirement can be supplied by recycled hydrogen donor material obtained by fractionating the coker liquids product and partially hydrogenating at least a portion of a 180°C to 400°C donor precursor fraction, or preferably a 200°C to 350°C fraction, to produce a recycle hydrogen donor material.
  • the ratio of recycle hydrogen donor material to fresh hydrogen donor material can be from 0.1:1 to 2:1.
  • the temperature of. the reaction mass entering the coker from a transfer tube can be in the range from 420°C to 500°C, preferably from 450°C to 500°C.
  • the relationship of time in the heating zone and temperature of that zone is governed by the nature of the heavy hydrocarbonaceous oil being treated. Oils that tend to crack easily are kept for a shorter residence time or at a lower temperature, or both, than oils that are more refractory.
  • the heavy hydrocarbonaceous oil feedstock can comprise a residuum from atmospheric or vacuum distillation of conventional crude oil, or an atmospheric or vacuum residuum of heavy oil or bitumen.
  • bitumen can be used as the feedstock oil.
  • Mixtures of the above-mentioned oils can also be fed to the process.
  • a high temperature requires a short residence time in the heating zone, as is known to those skilled in the art.
  • the temperature maintained in a coke drum is generally lower than the material in the transfer tube, and can be from 400°C to 490°C, preferably from 425°C to 480°C.
  • Operating pressure can be from atmospheric, i.e. 101 kPa, to about 600 kPa, preferably .from .200. k p a-to 400 kPa.
  • the liquid product material obtained from an overhead stream off the coke drum can be fractionated. At least a portion of a material boiling in the heavy gas oil range, i.e. above 400°C, can be recycled to be mixed with fresh residuum feedstock.
  • the bottoms recycle-to-fresh residuum feed ratio can be up to about 0.4:1. In refinery operation, a bottoms recycle-to-fresh feed ratio of 0.1:1 to 0.3:1 is generally sufficient to remove the entire heavy gas oil product.
  • both hydrogen donor material and heavy gas oil can be recycled.
  • the hold time of reaction mass in the coke drum can be from 5 minutes to 60 minutes.
  • delayed coking according to the invention is performed using two coke drums alternately. When one of the drums is filled with coke, it is disconnected from the preheating furnace and the coke product is discharged while the other drum is being filled with reaction mass from a preheating furnace via a transfer tube. The initial reaction mass entering either coke drum after startup of that drum is subjected to a longer period of exposure to coking conditions than the last reaction mass prior to shutdown of that drum. The method of the invention can be performed in such refinery conditions.
  • Figure 1 the single drawing, represents a preferred form of apparatus for carrying out the process of the invention.
  • vacuum residuum feedstock is fed by lines 11 and 13 to surge drum 2.
  • Partially hydrogenated light cycle oil is fed by line 12, and blended with residuum to be fed into drum 2 by line 13, and optionally recycled gas oil is added by line 17.
  • the resulting blend is taken through line 14 to coker preheating furnace 6 where it is heated to coking temperature, typically 420°C to 500°C, thence by line 15 to coke drum 7 or coke drum 7a.
  • the drum not being filled at the time is cut off from the system by valves 3 and 4 or 3a and 4a.
  • the drum After a suitable holding period in the coke drum, at a temperature preferably from 40013C to 480°C, and a pressure substantially lower than the pressure in the preheating furnace 6, during which period coker overheads are removed by line 16 to fractionator 8 from which products from gases to heavy gas oil are withdrawn by lines 21 to 24, the drum is taken out of service and its coke content removed via line 18 or 18a.
  • at least a portion of heavy gas oil boiling above 4000C can be recycled via line 17 for further treatment in the coker, and if desired, all of the heavy gas oil can be thus converted to lighter petroleum products or to coke. Where such stream is not recycled, it can advantageously be fed to a fluid catalytic cracking zone.
  • a portion of the hydrogen donor requirement can be satisfied by passing through line 19 at least a portion of the gas oil fraction in line 23 boiling between 180°C and 400°C, preferably between 200°C and 350°C, partially hydrogenating the gas oil in hydrogenation zone 9 and recycling the resulting recycle hydrogen donor material through line 20 to blend with fresh donor fed by line 12.
  • the blend was heated to 493°C in a commercial-scale coker furnace at 1.48 MPa (absolute) and passed through a pressure reducing valve into a coke drum where the reaction mass was held at.471°C and 240 kPa as the coke drum filled with coke.
  • Coker overheads were taken off the fractionator with yields (net of the added cycle oil) shown as Run 1 in Table 1.
  • the coke product contained 12 percent Volatile Combustible Matter (VCM).
  • VCM Volatile Combustible Matter
  • the process of the invention is thus shown to be effective in lowering the production of coke on both laboratory-scale and commercial-scale apparatus. Additional advantages are that the process produces a more saturated gasoline product than conventional processes, and reduces fouling of furnace tubes in the heating zone.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • Materials Engineering (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Coke Industry (AREA)
EP85301883A 1984-03-20 1985-03-19 Cokéfaction de résidu en présence d'un donneur d'hydrogène Expired - Lifetime EP0156614B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
CA000450003A CA1246481A (fr) 1984-03-20 1984-03-20 Cokefaction de residus en presence d'hydrogene donneur
CA450003 1984-03-20

Publications (3)

Publication Number Publication Date
EP0156614A2 true EP0156614A2 (fr) 1985-10-02
EP0156614A3 EP0156614A3 (en) 1987-08-05
EP0156614B1 EP0156614B1 (fr) 1990-12-12

Family

ID=4127451

Family Applications (1)

Application Number Title Priority Date Filing Date
EP85301883A Expired - Lifetime EP0156614B1 (fr) 1984-03-20 1985-03-19 Cokéfaction de résidu en présence d'un donneur d'hydrogène

Country Status (9)

Country Link
EP (1) EP0156614B1 (fr)
JP (1) JPS60238388A (fr)
AU (1) AU580035B2 (fr)
BR (1) BR8501214A (fr)
CA (1) CA1246481A (fr)
DE (1) DE3580859D1 (fr)
ES (1) ES8608564A1 (fr)
NO (1) NO851067L (fr)
ZA (1) ZA851903B (fr)

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0632121A2 (fr) * 1993-07-01 1995-01-04 Kurita Water Industries Ltd. Inhibiteur d'incrustation pour procédés pétrochimiques
WO2003087267A1 (fr) * 2002-04-11 2003-10-23 Conocophillips Company Procede et appareil de separation servant a eliminer des matieres particulaires de gasoil de zone de detente
CN105331390A (zh) * 2015-11-27 2016-02-17 中国海洋石油总公司 一种供氢延迟焦化的方法
EP2616174B1 (fr) * 2010-09-14 2018-08-22 Saudi Arabian Oil Company Desulfurization des charge hydrocarbures en utilisant de l'eau supercritique et des donneurs d'hydrogene.
GB2616101A (en) * 2021-11-29 2023-08-30 Petroleo Brasileiro Sa Petrobras System and method for evaluation of the deposition in tubes of the furnaces of a delayed coking unit

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN105505449A (zh) * 2015-11-27 2016-04-20 中国海洋石油总公司 一种供氢焦化方法

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3617513A (en) * 1969-01-03 1971-11-02 Exxon Research Engineering Co Coking of heavy feedstocks
EP0008493A1 (fr) * 1978-07-17 1980-03-05 Conoco Phillips Company Procédé de cokéfaction retardée d'une charge comprenant un courant de recyclage hydrogéné et produits graphitisés obtenus à partir de coke produit par un tel procédé
DE2949935A1 (de) * 1979-12-12 1981-06-19 Metallgesellschaft Ag, 6000 Frankfurt Verfahren zur umwandlung von hochsiedenden rohoelen in erdoelaehnliche produkte
US4385980A (en) * 1981-02-26 1983-05-31 Conoco Inc. Coal treating process

Family Cites Families (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS5455005A (en) * 1977-10-12 1979-05-01 Chiyoda Chem Eng & Constr Co Ltd Cracking of heavy hydrocarbons to lighter grade
US4176046A (en) * 1978-10-26 1979-11-27 Conoco, Inc. Process for utilizing petroleum residuum
CA1122914A (fr) * 1980-03-04 1982-05-04 Ian P. Fisher Methode de valorisation des hydrocarbures lourds

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3617513A (en) * 1969-01-03 1971-11-02 Exxon Research Engineering Co Coking of heavy feedstocks
EP0008493A1 (fr) * 1978-07-17 1980-03-05 Conoco Phillips Company Procédé de cokéfaction retardée d'une charge comprenant un courant de recyclage hydrogéné et produits graphitisés obtenus à partir de coke produit par un tel procédé
DE2949935A1 (de) * 1979-12-12 1981-06-19 Metallgesellschaft Ag, 6000 Frankfurt Verfahren zur umwandlung von hochsiedenden rohoelen in erdoelaehnliche produkte
US4385980A (en) * 1981-02-26 1983-05-31 Conoco Inc. Coal treating process

Cited By (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0632121A2 (fr) * 1993-07-01 1995-01-04 Kurita Water Industries Ltd. Inhibiteur d'incrustation pour procédés pétrochimiques
EP0632121A3 (fr) * 1993-07-01 1995-05-17 Kurita Water Ind Ltd Inhibiteur d'incrustation pour procédés pétrochimiques.
CN1110534C (zh) * 1993-07-01 2003-06-04 栗田工业株式会社 用于乙烯制造设备的脱丙烷器的防垢剂
WO2003087267A1 (fr) * 2002-04-11 2003-10-23 Conocophillips Company Procede et appareil de separation servant a eliminer des matieres particulaires de gasoil de zone de detente
US6919017B2 (en) 2002-04-11 2005-07-19 Conocophillips Company Separation process and apparatus for removal of particulate material from flash zone gas oil
EP1970426A1 (fr) * 2002-04-11 2008-09-17 Conocophillips Company Processus de séparation et appareil pour supprimer un matériau à particules d'un gazole de cuisson différé
US7476295B2 (en) 2002-04-11 2009-01-13 Conocophillips Company Separation apparatus for removal of particulate material from flash zone gas oil
EP2616174B1 (fr) * 2010-09-14 2018-08-22 Saudi Arabian Oil Company Desulfurization des charge hydrocarbures en utilisant de l'eau supercritique et des donneurs d'hydrogene.
CN105331390A (zh) * 2015-11-27 2016-02-17 中国海洋石油总公司 一种供氢延迟焦化的方法
GB2616101A (en) * 2021-11-29 2023-08-30 Petroleo Brasileiro Sa Petrobras System and method for evaluation of the deposition in tubes of the furnaces of a delayed coking unit

Also Published As

Publication number Publication date
AU580035B2 (en) 1988-12-22
EP0156614B1 (fr) 1990-12-12
NO851067L (no) 1985-09-23
ES541382A0 (es) 1986-07-16
CA1246481A (fr) 1988-12-13
EP0156614A3 (en) 1987-08-05
BR8501214A (pt) 1985-11-12
DE3580859D1 (de) 1991-01-24
AU4002285A (en) 1985-09-26
ES8608564A1 (es) 1986-07-16
ZA851903B (en) 1985-10-30
JPS60238388A (ja) 1985-11-27

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