EP0732389A2 - Procédé d'hydroconversion de charges hydrocarbonées lourdes - Google Patents

Procédé d'hydroconversion de charges hydrocarbonées lourdes Download PDF

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Publication number
EP0732389A2
EP0732389A2 EP96103874A EP96103874A EP0732389A2 EP 0732389 A2 EP0732389 A2 EP 0732389A2 EP 96103874 A EP96103874 A EP 96103874A EP 96103874 A EP96103874 A EP 96103874A EP 0732389 A2 EP0732389 A2 EP 0732389A2
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EP
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Prior art keywords
stage
reactor
catalyst
catalytic
feedstock
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EP96103874A
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German (de)
English (en)
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EP0732389B1 (fr
EP0732389A3 (fr
Inventor
James J. Colyar
James B. Macarthur
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IFP Energies Nouvelles IFPEN
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IFP Energies Nouvelles IFPEN
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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
    • C10G65/00—Treatment of hydrocarbon oils by two or more hydrotreatment processes only
    • C10G65/02—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only
    • C10G65/10—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including only cracking steps

Definitions

  • This invention pertains to a catalytic two-stage hydroconversion process for achieving essentially complete hydroconversion of heavy petroleum-based feedstocks to produce lower-boiling hydrocarbon liquid products. It pertains particularly to such a process utilizing a high temperature first stage ebullated bed catalytic reactor and lower temperature second stage ebullated bed catalytic reactor, with extinction recycle of all distilled vacuum bottoms material back to the first stage reactor to provide 90-100 vol% hydroconversion of the feedstocks.
  • U.S. No. 3,549,517 to Lehman discloses a single stage catalytic process in which a vacuum distillation side stream is recycled to the reactor.
  • U.S. Patent No. 3,184,402 to Kozlowski, et al discloses a two-stage catalytic hydrocracking process with intermediate fractionation and some recycle of a distillation bottoms fraction to either a first or second catalytic cracking zone.
  • U.S. Patent No. 3,254,017 to Arey, Jr. et al discloses a two-stage process for hydrocracking heavy oils utilizing small pore zeolite catalyst in the second stage reactor.
  • 3,775,293 to Watkins discloses a two-stage catalytic desulfurization process with recycle of some heavy oil fraction boiling above diesel fuel oil to a second stage fixed bed type reactor.
  • U.S. No. 4,457,831 to Gendler discloses a two-stage catalytic hydroconversion process in which vacuum bottoms residue material is recycled to the second stage reactor for further hydroconversion reactions.
  • U.S. No. 4,576,710 to Nongbri et al discloses a two-stage catalytic desulfurization process for petroleum residua feedstocks utilizing catalyst regeneration.
  • the present invention advantageously overcomes the concerns of potential users and provides a desirable improvement over the known prior art hydroconversion processes for heavy petroleum feedstocks.
  • This invention provides a catalytic two-stage ebullated bed hydroconversion process for heavy petroleum, residual oil and bitumen feedstocks, which process effectively hydroconverts essentially all of the high boiling residue material in the feedstock to desirable high quality lower boiling hydrocarbon liquid products.
  • the process is particularly useful for those feedstocks containing 40-100 vol% 975°F + petroleum resid and 10-50 wt% Conradson carbon residue (CCR), and containing up to 1000 wppm total metals (V+Ni).
  • Preferred feedstocks should contain 75-100 vol% 975°F + residual material with 15-40 wt% CCR, and 100-600 wppm total metals (V+Ni).
  • Such feedstocks may include but are not limited to heavy crudes, atmospheric bottoms and vacuum resid materials from Alaska, Athabasca, Ba skilletro, Cold Lake, Lloydminster, Orinoco and Saudi Arabia.
  • the fresh feedstock is introduced together with hydrogen into a first stage catalytic ebullated bed type reactor, which is essentially a high temperature hydroconversion reactor utilizing a particulate supported hydroconversion catalyst.
  • the reactor is maintained at operating conditions of 820-875°F temperature, 1500-3500 psig hydrogen partial pressure, and space velocity of 0.30-1.0 volume feed per hour per volume of reactor (V f /hr/V r ).
  • the catalyst replacement rate should be 0.15-0.90 pound catalyst/barrel of fresh oil feed.
  • the first stage reactor hydroconverts 70-95 vol.% of the fresh feed material and recycled residue material to form lower boiling hydrocarbon materials.
  • the first stage reactor effluent material is phase separated, a gas fraction is removed and the resulting liquid fraction is passed together with additional hydrogen on to a second stage catalytic ebullated bed type reactor containing a particulate high activity catalyst and which is maintained at lower temperature conditions of 700-800°F temperature and 0.10-0.80 V f /hr/V f , space velocity, so as to effectively hydrogenate the unconverted residue material therein.
  • the second stage reactor catalyst replacement rate should be 0.15-0.90 pound catalyst/barrel feed to the second stage, which hydroconverts 10-50 vol% of the second stage feed material to lower boiling hydrocarbon materials.
  • the second stage reactor effluent material is passed to gas/liquid separation and distillation steps, from which hydrocarbon liquid product and distillation vacuum bottoms fraction materials are removed.
  • the vacuum bottoms material boiling above at least 850°F temperature and preferably above 900°F is recycled back to the first stage catalytic reactor inlet at a volume ratio to the fresh feedstock of 0.2-1.5/1, and preferably at 0.5-1.0/1 recycle ratio for further hydroconversion extinction reactions therein.
  • Particulate catalyst materials which are useful in this petroleum hydroconversion process may contain 2-25 wt. percent total active metals selected from the group consisting of cadmium, chromium, cobalt, iron, molybdenum, nickel, tin, tungsten, and mixtures thereof deposited on a support material selected from the group of alumina, silica and combinations thereof. Also, catalysts having the same characteristics may be used in both the first stage and second stage reactors.
  • Catalysts having unimodal, bimodal and trimodal pore size distribution are useful in this process.
  • Preferred catalysts should contain 5-20 wt.% total active metals consisting of combinations of cobalt, molybdenum and nickel deposited on alumina support material.
  • the heavy petroleum feedstock is first catalytically hydroconverted in the first stage catalytic higher temperature reactor, and the remaining resid fraction is catalytically hydrogenated in the second stage catalytic lower temperature reactor, after which a vacuum distilled 850°F + fraction is recycled back to the first stage reactor for further hydrocracking reactions at the higher temperature maintained therein.
  • Passing the first stage reactor liquid phase effluent material to the second stage reactor operated at lower temperature and space velocity conditions concentrates unconverted residue material, minimizes any gas velocity related problems in the second stage reactor, and reduces contaminant partial pressures (H 2 S, NH 3 , H 2 O).
  • the second stage catalytic reactions increase the hydrogen/carbon ratio of the residue being processed therein, thereby decreasing aromaticity and increasing the hydrogen donor capability of the residue, so that by its recycle back to the first stage reactor the hydrogenated residue can donate hydrogen to the fresh feedstock and the hydrogenated residue can also be more readily hydroconverted to desirable lower boiling fractions.
  • This approach is more selective to producing high yields of desirable hydrocarbon liquid fuel products, i.e. reduced hydrocarbon gas contributes to high conversion operations.
  • This catalytic hydroconversion process can also be further improved by selectively feeding fresh hydrogen to the second stage reactor and recycling hydrogen gas to the first stage reactor, so as to maximize hydrogen partial pressure in the more catalytic second stage hydrogenation reactor.
  • used catalyst in the second stage ebullated bed reactor can be withdrawn, treated to remove undesired fines, etc., and introduced into the first stage ebullated bed reactor for further use therein, before the used catalyst is withdrawn from the first stage reactor and discarded.
  • utilizing used second stage catalyst material in the first stage reactor is appropriate and beneficial, because use of fresh, high activity catalyst in the higher temperature mainly thermal type reactor would not provide substantially improved catalytic activity therein.
  • any disposition problems usually related to an unconverted bottoms fraction material are eliminated.
  • This process advantageously provides for improved matching of the reaction conditions and the catalytic activity needed in each stage reactor, by providing higher reaction temperature and lower catalyst activity in the first stage reactor and lower temperature and higher catalyst activity in the second stage reactor, so as to achieve a more complete hydroconversion of the feedstock and effective use of the catalyst.
  • This combination of the two staged reaction conditions is unexpectedly beneficial and results in essentially complete hydroconversion of heavy petroleum feedstocks to produce desirable lower boiling hydrocarbon liquid products, without substantially increasing reactor volume over the single stage approach to achieving high hydroconversion of the feedstock.
  • Fig. 1 is a schematic flow diagram of a catalytic two-stage hydroconversion process for processing heavy petroleum feedstocks to produce lower-boiling liquid and gas products according to the invention.
  • a catalytic two-stage ebullated bed reaction process and system which is adapted for achieving substantially complete hydroconversion and destruction of residue material (975°F + fraction) contained in heavy petroleum oil, residual oil, or bitumen feedstocks, and for producing desirable low-boiling hydrocarbon liquid products.
  • a pressurized heavy petroleum feedstock such as Cold Lake vacuum resid is provided at 10, combined with hydrogen at 12 and mixed with recycled hydrogenated heavy vacuum bottoms material at 13, and the combined stream 14 is fed upwardly through flow distributor 15 in first stage catalytic ebullated bed upflow reactor 16 containing catalyst ebullated bed 18.
  • the total feedstock consists of the fresh hydrocarbon feed material at 10 plus the recycled vacuum bottoms material at 13.
  • the recycle rate for the vacuum bottoms material at 13 to the first stage reactor 16 is selected so as to completely destroy or extinct this residue material in two staged catalytic reactors, with the recycle volume ratio of the vacuum bottoms material to the fresh oil feedstock being in the range of 0.2-1.5/1, and preferably 0.50-1.0/1 recycle ratio.
  • the hydrocracking reactions are primarily thermal type as the reactor is maintained at a relatively high temperature of 820-875°F, at 1,500-3,500 psig hydrogen partial pressure, and liquid hourly space velocity of 0.30-1.0 volume feed/hr/volume of reactor (V f /hr/V r ).
  • the feedstock hydroconversion achieved therein is typically 70-95 vol %, with about 75-90 vol. % conversion usually being preferred.
  • Preferred first stage reaction conditions are 825-850°F temperature, 2000-3000 psig, hydrogen partial pressure, and 0.40-0.80 V f /hr/V r space velocity.
  • the catalyst bed 18 in first stage reactor 16 is expanded by the upflowing gas and reactor liquid to 30-60% above its settled height and is ebullated as described in more detail in U.S. Patent No. 3,322,665 which is incorporated herein by reference to the extent needed to describe operation of the reactor ebullated catalyst beds.
  • first stage reactor 16 From first stage reactor 16, overhead effluent stream 19 is withdrawn and passed to phase separator 20. A liquid stream is withdrawn from the separator 20 through downcomer conduit 22, and is recirculated through conduit 24 by ebullating or recycle pump 25 back to the reactor 16.
  • the particulate catalyst material added at 17 is preferably used extrudate catalyst withdrawn at 36 from second stage reactor 30, and usually treated at zone 38 as desired to remove particulate fines, etc. at 37.
  • Fresh make-up catalyst can be added as needed at 17a, and spent catalyst is withdrawn at connection 17b from catalyst bed 18.
  • gaseous material at 21 is passed to a gas purification section 42, which is described further herein below. Also from the separator 20, a liquid portion 26 from the liquid stream 22 provides the liquid feed ( ⁇ 700°F + ) material upwardly through flow distributor 27 into the second stage catalytic ebullated bed reactor 30.
  • the second stage catalytic reactor 30 which preferably has larger volume and provides lower space velocity than for the first-stage reactor 16, less hydroconversion and more catalytic hydrogenation type reactions occur.
  • the second stage reactor 30 contains ebullated catalyst bed 28 and is operated at conditions of 700-800°F temperature 1,500-3,500 psig hydrogen partial pressure, and 0.10-0.80 V f /hr/V r space velocity, and thereby maximizes resid hydrogenation reactions which occur therein.
  • Preferred second stage reaction conditions are 730-780°F temperature, and 0.20-0.60 V f /hr/V r space velocity. Additional fresh hydrogen is provided at 32 to the second stage reactor 30, so that a high level of hydrogen partial pressure is maintained in the reactor.
  • the catalyst bed 28 is expanded by 30-60% above its settled height by the upflowing gas and liquid therein.
  • Reactor liquid is withdrawn from an internal phase separator 33 through downcomer conduit 34 to recycle pump 35, and is reintroduced upwardly through the flow distributor 27 into the ebullated bed 28.
  • Used particulate catalyst is withdrawn at 36 from the second stage reactor bed 28 and fresh catalyst is added at 36 a as needed to maintain the desired catalyst volume and catalytic activity therein.
  • This used catalyst withdrawn which is relatively low in metal contaminant concentration, is passed to a treatment unit 38 where it is washed, and screened to remove undesired fines at 37, and the recovered catalyst at 39 provides the used catalyst addition at 17 to the first stage reactor bed 18, together with any fresh make-up catalyst added at connection 17a as needed.
  • the catalyst particles in ebullated beds 18 and 28 usually have a relatively narrow size range for uniform bed expansion under controlled upward liquid and gas flow conditions. While the useful catalyst size range is between 6 and 60 mesh (U.S. Sieve Series), the catalyst size is preferably particles between 8 and 40 mesh size including beads, extrudates, or spheres of approximately 0.020-0.100 inch effective diameter. In the reactor, the density of the catalyst particles, the liquid upward flow rate, and the lifting effect of the upflowing hydrogen gas are important factors in the desired expansion and operation of the catalyst bed.
  • an effluent stream is withdrawn at 31 and passed to a phase separator 40.
  • a hydrogen-containing gas stream 41 is passed to the purification section 42 for removal of contaminants such as CO 2 , H 2 S, and NH 3 at 43.
  • Purified hydrogen at 44 is recycled back to each reactor 16 and 30 as desired as the H 2 streams 12 and 32, respectively, while fresh hydrogen is added at 45 as needed.
  • a liquid fraction 46 is withdrawn, pressure-reduced at 47 to 0-100 psig, and is introduced into fractionation unit 48.
  • a gaseous product stream is withdrawn at 49 and a light hydrocarbon liquid product normally boiling between 400-850°F are withdrawn at 50.
  • a bottoms 850°F + fraction is withdrawn at 52, reheated at heater 53, and passed to vacuum distillation step at 54.
  • a vacuum gas oil liquid product is withdrawn overhead at 55.
  • Vacuum bottoms stream 56 which has been hydrogenated in the second stage catalyst reactor 30, is completely recycled back to the first stage catalytic reactor 16 for predominantly thermal hydrocracking reactions therein using the low activity catalyst provided at 17.
  • the recycle volume ratio for vacuum bottoms stream 56 to fresh feed 10 should be 0.2-1.5/1, and preferably should be 0.50-1.0/1. It is pointed out that by utilizing this two stage catalytic hydroconversion process, the thermal reactions and catalytic activity in each stage reactor are effectively matched, so that there is essentially no net 975°F + hydrocarbon material produced from the process.
  • a typical heavy vacuum resid feedstock such as Cold Lake vacuum resid is processed by using the catalytic two-stage hydroconversion process with vacuum bottoms recycle arrangement of the present invention.
  • This Cold Lake vacuum resid feedstock contains 90 vol % 975°F + material, 5.1 wt.% sulfur, 19 wt.% CCR, and 350 wppm metals (V+Ni), with the vacuum bottoms fraction normally boiling above 975°F being recycled back to the first stage catalytic reactor of the two-reactor system for further hydroconversion reactions and extinction recycle therein.
  • the reaction conditions used and overall conversion results are summarized in Table 1 below.

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  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Catalysts (AREA)
EP96103874A 1995-03-16 1996-03-12 Procédé d'hydroconversion de charges hydrocarbonées lourdes Expired - Lifetime EP0732389B1 (fr)

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US40601695A 1995-03-16 1995-03-16
US406016 1995-03-16

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EP0732389A2 true EP0732389A2 (fr) 1996-09-18
EP0732389A3 EP0732389A3 (fr) 1996-12-18
EP0732389B1 EP0732389B1 (fr) 2001-08-01

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EP (1) EP0732389B1 (fr)
JP (1) JP3864319B2 (fr)
CA (1) CA2171894C (fr)
DE (1) DE69614165T2 (fr)
ZA (1) ZA961830B (fr)

Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2001098436A1 (fr) * 2000-06-19 2001-12-27 Institut Francais Du Petrole Procede d'hydrogenation mettant en oeuvre des reacteurs a lit bouillonnant a etapes multiples
EP1466958A2 (fr) * 2003-02-26 2004-10-13 Institut Francais Du Petrole Procédé et installation de traitement d'hydrocarbures et de séparation des phases produites par ledit traitement
US7060228B2 (en) 2001-07-06 2006-06-13 Institut Francais Du Petrole Internal device for separating a mixture that comprises at least one gaseous phase and one liquid phase
WO2009141703A2 (fr) * 2008-05-20 2009-11-26 I F P Recyclage sélectif de gazole lourd pour obtenir une intégration optimale de la conversion de pétrole lourd et du traitement de gazole sous vide
ITMI20130131A1 (it) * 2013-01-30 2014-07-31 Luigi Patron Processo a migliorata produttività per la conversione di olii pesanti
CN105441126A (zh) * 2014-09-24 2016-03-30 中国石油化工股份有限公司 一种渣油加氢处理方法
CN105524653A (zh) * 2014-09-29 2016-04-27 中国石油化工股份有限公司 一种渣油加氢处理方法
US11732203B2 (en) 2017-03-02 2023-08-22 Hydrocarbon Technology & Innovation, Llc Ebullated bed reactor upgraded to produce sediment that causes less equipment fouling

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EP1299192A1 (fr) * 2000-06-19 2003-04-09 Institut Francais Du Petrole Procede de presulfuration et preconditionnement du catalyseur d'hydroconversion residuel
JP5318410B2 (ja) 2004-04-28 2013-10-16 ヘッドウォーターズ ヘビー オイル リミテッド ライアビリティ カンパニー 沸騰床水素化処理方法およびシステムならびに既存の沸騰床システムをアップグレードする方法
US10941353B2 (en) 2004-04-28 2021-03-09 Hydrocarbon Technology & Innovation, Llc Methods and mixing systems for introducing catalyst precursor into heavy oil feedstock
CA2570685A1 (fr) 2004-06-17 2006-01-26 Exxonmobil Research And Engineering Company Combinaison de catalyseurs et procede d'hydrotraitement en deux etapes d'huiles d'hydrocarbures lourds
US20070140927A1 (en) * 2005-12-16 2007-06-21 Chevron U.S.A. Inc. Reactor for use in upgrading heavy oil admixed with a highly active catalyst composition in a slurry
WO2009073436A2 (fr) 2007-11-28 2009-06-11 Saudi Arabian Oil Company Processus d'hydrotraitement catalytique des pétroles bruts sulfureux
US8372267B2 (en) 2008-07-14 2013-02-12 Saudi Arabian Oil Company Process for the sequential hydroconversion and hydrodesulfurization of whole crude oil
EP2300566B1 (fr) 2008-07-14 2016-09-07 Saudi Arabian Oil Company Processus de traitement d'huiles lourdes au moyen de composants hydrocarbures légers utilisés comme diluent
FR2940313B1 (fr) * 2008-12-18 2011-10-28 Inst Francais Du Petrole Procede d'hydrocraquage incluant des reacteurs permutables avec des charges contenant 200ppm poids-2%poids d'asphaltenes
WO2011005476A2 (fr) 2009-06-22 2011-01-13 Saudi Arabian Oil Company Procédé de rechange pour le traitement de bruts lourds dans une raffinerie de cokéfaction
CN103857771B (zh) * 2011-07-29 2016-06-01 沙特阿拉伯石油公司 用于含有溶解的氢的原料的沸腾床方法
US9790440B2 (en) 2011-09-23 2017-10-17 Headwaters Technology Innovation Group, Inc. Methods for increasing catalyst concentration in heavy oil and/or coal resid hydrocracker
US9644157B2 (en) 2012-07-30 2017-05-09 Headwaters Heavy Oil, Llc Methods and systems for upgrading heavy oil using catalytic hydrocracking and thermal coking
US11414607B2 (en) 2015-09-22 2022-08-16 Hydrocarbon Technology & Innovation, Llc Upgraded ebullated bed reactor with increased production rate of converted products
US11414608B2 (en) 2015-09-22 2022-08-16 Hydrocarbon Technology & Innovation, Llc Upgraded ebullated bed reactor used with opportunity feedstocks
US11421164B2 (en) 2016-06-08 2022-08-23 Hydrocarbon Technology & Innovation, Llc Dual catalyst system for ebullated bed upgrading to produce improved quality vacuum residue product
US11118119B2 (en) 2017-03-02 2021-09-14 Hydrocarbon Technology & Innovation, Llc Upgraded ebullated bed reactor with less fouling sediment
CA3057131C (fr) 2018-10-17 2024-04-23 Hydrocarbon Technology And Innovation, Llc Reacteur a lit bouillonnant ameliore sans accumulation liee au recyclage d'asphaltenes dans des residus de tour sous vide

Citations (4)

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GB1193213A (en) * 1967-04-25 1970-05-28 Atlantic Richfield Co Petroleum Purification
GB2066287A (en) * 1980-12-09 1981-07-08 Lummus Co Hydrogenation of high boiling hydrocarbons
US4457831A (en) * 1982-08-18 1984-07-03 Hri, Inc. Two-stage catalytic hydroconversion of hydrocarbon feedstocks using resid recycle
EP0244244A2 (fr) * 1986-04-30 1987-11-04 Exxon Research And Engineering Company Procédé d'hydroconversion d'hydrocarbures avec un catalyseur en suspension

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB1193213A (en) * 1967-04-25 1970-05-28 Atlantic Richfield Co Petroleum Purification
GB2066287A (en) * 1980-12-09 1981-07-08 Lummus Co Hydrogenation of high boiling hydrocarbons
US4457831A (en) * 1982-08-18 1984-07-03 Hri, Inc. Two-stage catalytic hydroconversion of hydrocarbon feedstocks using resid recycle
EP0244244A2 (fr) * 1986-04-30 1987-11-04 Exxon Research And Engineering Company Procédé d'hydroconversion d'hydrocarbures avec un catalyseur en suspension

Cited By (15)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2001098436A1 (fr) * 2000-06-19 2001-12-27 Institut Francais Du Petrole Procede d'hydrogenation mettant en oeuvre des reacteurs a lit bouillonnant a etapes multiples
US7060228B2 (en) 2001-07-06 2006-06-13 Institut Francais Du Petrole Internal device for separating a mixture that comprises at least one gaseous phase and one liquid phase
EP1466958A2 (fr) * 2003-02-26 2004-10-13 Institut Francais Du Petrole Procédé et installation de traitement d'hydrocarbures et de séparation des phases produites par ledit traitement
EP1466958A3 (fr) * 2003-02-26 2005-10-19 Institut Francais Du Petrole Procédé et installation de traitement d'hydrocarbures et de séparation des phases produites par ledit traitement
RU2495086C2 (ru) * 2008-05-20 2013-10-10 Ифп Энержи Нувелль Избирательный рецикл тяжелого газойля для оптимальной интеграции перегонки тяжелой нефти и переработки вакуумного газойля
WO2009141703A3 (fr) * 2008-05-20 2010-06-17 I F P Recyclage sélectif de gazole lourd pour obtenir une intégration optimale de la conversion de pétrole lourd et du traitement de gazole sous vide
WO2009141703A2 (fr) * 2008-05-20 2009-11-26 I F P Recyclage sélectif de gazole lourd pour obtenir une intégration optimale de la conversion de pétrole lourd et du traitement de gazole sous vide
ITMI20130131A1 (it) * 2013-01-30 2014-07-31 Luigi Patron Processo a migliorata produttività per la conversione di olii pesanti
WO2014118814A3 (fr) * 2013-01-30 2015-03-05 Luigi Patron Procédé à productivité améliorée pour transformation d'huiles lourdes
US9884999B2 (en) 2013-01-30 2018-02-06 Luigi Patron Process with improved productivity for the conversion of heavy oils
CN105441126A (zh) * 2014-09-24 2016-03-30 中国石油化工股份有限公司 一种渣油加氢处理方法
CN105441126B (zh) * 2014-09-24 2017-05-24 中国石油化工股份有限公司 一种渣油加氢处理方法
CN105524653A (zh) * 2014-09-29 2016-04-27 中国石油化工股份有限公司 一种渣油加氢处理方法
CN105524653B (zh) * 2014-09-29 2017-05-24 中国石油化工股份有限公司 一种渣油加氢处理方法
US11732203B2 (en) 2017-03-02 2023-08-22 Hydrocarbon Technology & Innovation, Llc Ebullated bed reactor upgraded to produce sediment that causes less equipment fouling

Also Published As

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CA2171894C (fr) 2006-06-06
ZA961830B (en) 1997-10-31
EP0732389B1 (fr) 2001-08-01
JP3864319B2 (ja) 2006-12-27
DE69614165T2 (de) 2001-11-22
JPH08325580A (ja) 1996-12-10
DE69614165D1 (de) 2001-09-06
EP0732389A3 (fr) 1996-12-18
CA2171894A1 (fr) 1996-09-17

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