EP1299507A1 - Procede d'hydrogenation mettant en oeuvre des reacteurs a lit bouillonnant a etapes multiples - Google Patents

Procede d'hydrogenation mettant en oeuvre des reacteurs a lit bouillonnant a etapes multiples

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Publication number
EP1299507A1
EP1299507A1 EP00936894A EP00936894A EP1299507A1 EP 1299507 A1 EP1299507 A1 EP 1299507A1 EP 00936894 A EP00936894 A EP 00936894A EP 00936894 A EP00936894 A EP 00936894A EP 1299507 A1 EP1299507 A1 EP 1299507A1
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EP
European Patent Office
Prior art keywords
reactor
stage
liquid
catalyst
catalytic
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Granted
Application number
EP00936894A
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German (de)
English (en)
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EP1299507B1 (fr
Inventor
James J. Colyar
James B. Mac Arthur
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IFP Energies Nouvelles IFPEN
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IFP Energies Nouvelles IFPEN
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Classifications

    • 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 improved catalytic hydrogenation of heavy hydrocarbonaceous feedstocks utilizing catalytic multi-stage ebullated bed reactors for producing desired lower boiling hydrocarbon liquid products. It pertains particularly to such catalytic multi-stage hydrogenation processes having increased catalyst loading and liquid volume together with reduced gas hold-up in each reactor, and thereby provides improved performance efficiency for the processes.
  • This invention provides an improved catalytic multi-stage hydrogenation process for treating heavy hydrocarbonaceous feedstocks and producing desired lower boiling hydrocarbon liquid products with enhanced process performance.
  • the catalytic ebullated bed reactor construction arrangement for the first stage reactor does not include an internal gas/liquid separation device, but instead utilizes an efficient external gas/liquid separator. Utilizing such external gas/liquid separation results in an increased volume of particulate catalyst being provided in a particular size reactor and reduces the catalyst space velocity, which is defined as the volumetric rate of feedstock processed per unit weight of fresh catalyst in the reactor.
  • a vertical distance of 5-10 ft. should be maintained between the ebullated bed maximum expansion level and the reactor outlet conduit, so as to avoid any carryover of catalyst from the reactor.
  • operating conditions for each of the two-staged catalytic ebullated bed reactors are selected so that the upward superficial gas velocity is maintained within a desired critical range, and the gas hold-up volume percentage in each reactor is beneficially reduced, which consequently permits more reactor liquid to be in contact with the catalyst bed, so that the reactor performance as well as the overall process performance results are enhanced.
  • This invention is useful for processing heavy hydrocarbonaceous feedstocks and providing overall hydroconversions in the range of 50-100 vol.% to produce desired lower boiling hydrocarbon liquid products.
  • Feedstock Residua Content vol.% 975°F + 30 - 100 50 - 90
  • the fresh feedstock together with hydrogen are introduced into a first stage catalytic ebullated bed reactor, which does not contain an internal gas/liquid phase separator device.
  • the catalyst bed is expanded by
  • the first stage reactor usually hydroconverts 30-95 vol.% of the fresh heavy feedstock and any recycled residua material to a lower boiling hydrocarbon effluent material.
  • the first stage reactor effluent material is phase separated in an external gas/liquid separator, a gas fraction is removed, and ' a sufficient portion of the remaining liquid is recycled to the reactor to maintain the desired 25-75% catalyst bed expansion therein.
  • the remaining liquid fraction is passed together with additional hydrogen to a second stage catalytic ebullated bed type reactor.
  • the second stage ebullated bed reactor is operated similarly to the first stage reactor and typically is maintained at 0-50°F, lower temperature in the broad range of 700-850°F (370-455°C) and 0.20-2.0 V ( /hr/V r space velocity, so as to effectively further hydrogenate the remaining unconverted residua material therein.
  • the second stage reactor usually further hydroconverts 30-95 vol.% of the remaining residua feed material to lower boiling hydrocarbon materials.
  • the effluent material is passed to various gas/liquid separation and distillation steps, from which gases and low-boiling hydrocarbon liquid product and distillation vacuum bottoms fraction materials are removed.
  • gases and low-boiling hydrocarbon liquid product and distillation vacuum bottoms fraction materials are removed.
  • a portion of the vacuum bottoms fraction material boiling above at least 650°F (343°C) temperature and preferably boiling above about 900°F(482°C) can be recycled back to the first stage catalytic reactor inlet at a recycle volume ratio to the fresh feedstock of 0-1.0/1 , and preferably at 0.2-0.7/1 recycle ratio for further hydroconversion reactions therein.
  • Particulate catalyst materials which are useful in this hydrogenation process may contain 2-25 wt. percent total active metals selected from the metals group consisting of cadmium, chromium, cobalt, iron, molybdenum, nickel, tin, tungsten, and mixtures thereof deposited on a support material selected from the group consisting of alumina, silica and combinations thereof. Also, catalysts having the same characteristics may be used in both the first stage and second stage reactors, or each reactor may use catalysts having different characteristics. Useful particulate catalysts will be in the form of beads, extrudates or spheres and have broad and preferred characteristics as shown in Table 2 below: TABLE 2
  • Catalysts having unimodal, bimodal and trimodal pore size distributions 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 an alumina support material.
  • This improved process for catalytic multi-stage hydrogenation of heavy hydrocarbonaceous feedstocks advantageously provides enhanced performance results by utilizing increased catalyst loading and liquid volume percent together with reduced gas hold-up in each of the multiple staged reactors with external gas/liquid separation. Such enhanced performance efficiency is manifested principally by providing better utilization of the reactor volume for any particular desired hydroconversion result.
  • This process is generally useful for catalytic hydrogenation and hydroconversion of heavy petroleum crudes, topped crudes, and vacuum residua, bitumen from tar sands, for coal hydrogenation and liquefaction, and for catalytic co-processing coal/oil blends to produce lower boiling, higher value hydrocarbon liquid products.
  • Fig. 1 is a schematic flow diagram of an improved catalytic two-stage hydrogenation process for heavy hydrocarbonaceous feedstocks for producing desired lower-boiling liquid and gas products according to the invention
  • Fig. 2 is a graph generally showing the typical general relationship between catalyst space velocity for a catalytic ebullated bed reactor and feedstock hydrodesulfurization results for the reactor;
  • Fig. 3 is a graph of experimental data generally showing the relationship between superficial gas velocity in a catalytic ebullated bed reactor and gas holdup volume percentage in the reactor for various superficial liquid velocities;
  • Fig. 4 is a graph generally showing the effect of reactor gas hold-up volume percent on hydrodesulfurization results particularly in a second stage catalytic reactor.
  • a pressurized heavy hydrocarbon feedstock such as petroleum vacuum residua containing 30-100 vol.% 975°F + residua and preferably 50-90 vol.% is provided at 10 and combined with hydrogen at 12.
  • a heavy vacuum bottoms recycle liquid can be added at 13, and the combined stream at 14 is pressurized and fed through flow distributor 15 upwardly into first stage catalytic ebullated bed reactor 16 containing ebullated bed 18.
  • the total feedstock to reactor 16 consists of the fresh hydrocarbon feed material at 10 plus any recycled vacuum bottoms material at 13.
  • the recycle volume ratio of the vacuum bottoms material to the fresh oil feedstock is in the range of 0-1.0/1, and preferably is 0.2-0.7/1 recycle ratio, with the higher recycle ratios being used for achieving higher overall percentage conversion of the feedstock residua.
  • the first stage reactor 16 contains an ebullated bed 18 of particulate supported type catalyst having the form of beads, extrudates, spheres, etc., and is maintained within the range of broad and preferred operating conditions as shown in Table 1 above.
  • the physical level of catalyst at 18a in the reactor is higher than for typical ebullated-bed reactors. This is because the usual internal recycle cup device which occupies a significant portion of reactor height, is not provided for separating the reactor liquid and vapor portions within the reactor 16. Instead, an external or interstage phase separator 20 is provided between the first and second stage catalytic reactors to effectively separate the reactor liquid and vapor effluent portions.
  • Removal of the usual internal recycle cup separator results in more catalyst and a higher level for the expanded catalyst bed in the reactor and desirably provides for a lower catalyst space velocity, which contributes to the higher levels of performance for the reactors.
  • a vertical height distance "h" of 5 -10 ft. is maintained between the maximum bed expansion level and the inlet of reactor outlet conduit 19 to prevent carryover of catalyst particles from the expanded bed 18.
  • first stage reactor 16 overhead effluent stream 19 is withdrawn and passed to the external phase separator 20. From separator 20, a vapor stream 21 is removed and passed to gas purification section 42. Also, a liquid stream 22 is withdrawn, and a sufficient flow is recirculated through conduit 24 by ebullating pump 25 back to the reactor 16 to expand the catalyst bed 18 by the desired 25- 75 percent above its normal settled bed height.
  • particulate catalyst material is added at connection 17 at the desired replacement rate, and can be used catalyst withdrawn from second stage reactor 30 at connection 36, and usually treated at unit 38 as desired to remove undesired particulate fines, etc. at 37.
  • Fresh make-up catalyst can be added to catalyst bed 18 as needed at connection 17a, and an equivalent amount of spent catalyst is withdrawn from catalyst bed 18 at connection 17b.
  • Figure 2 shows the effect of lower catalyst space velocities on hydrodesulfurization performance for ebullated-bed reactors having equal total volumes, hydrocarbon feedrates, reaction temperatures and catalyst replacement rates.
  • Figure 2 clearly shows the improvement in first stage reactor desulfurization performance provided by lower catalyst space velocities, resulting mainly from use of an external gas/liquid separation device instead of the usual internal separation device and for nominal residue conversion levels between about 65 and 90 vol.%.
  • the hydrocarbon liquid feedstock and hydrogen both react in contact with the catalyst in the reactor ebullated bed to form lower boiling components which have lower contaminant levels than the feedstock.
  • the hydrogen gas provided at 12 to the first stage reactor 16 is mainly recycled unreacted hydrogen having purity in the range of 85-95 vol. percent and some essentially pure make-up hydrogen as needed.
  • the hydrogen feed rate to the first stage reactor and to the subsequent staged reactors is established at a minimum required level, which provides at each reactor outlet a required hydrogen partial pressure which is determined based on characteristics for a particular feedstock, the catalyst characteristics, the desired level of reaction severity, and the product quality objectives.
  • the required hydrogen feed rate to a catalytic reactor is expressed as a multiple of the quantity of hydrogen chemically consumed in the reactor, and such hydrogen rate is usually in the range of 2.0 to 5.0 times the chemical hydrogen consumption therein.
  • Reactor Liquid Residence lime — — — — — — — — — — — — —
  • Reactor volume occupied by Liquid Volume total - Volume occupied by Gas - Volume occupied by solid (catalyst)
  • the volume percent of hydrogen gas hold-up in the catalytic ebullated-bed reactor including hydrocarbon vapors generated therein is primarily related to the reactor superficial gas velocity, with increased upward superficial gas velocity resulting in an increased gas hold-up volume percentage in the reactor.
  • Experimental data showing this relationship between the upward superficial gas velocity and gas hold-up volume percent in catalytic ebullated-bed reactors is shown in Figure 3.
  • the measured gas hold-up volume percent in the reactor is shown as a function of the reactor superficial gas velocity at three different levels of reactor liquid upward superficial velocity.
  • the superficial gas velocity for upflowing hydrogen gas clearly has the primary effect on gas hold-up volume in the reactor, with a secondary effect being due to different superficial liquid upward velocities for the feed liquid in the reactor
  • the present invention advantageously minimizes this excessive hydrogen gas and hydrocarbon vapor hold-up volume percentage in the reactor, so as to provide the enhanced reaction kinetics and higher overall levels of process performance for the reactor system.
  • This relationship of catalytic reactor performance such as percent hydroconversion, hydrodesulfurization, etc. of the heavy hydrocarbon feedstock to the percentage of gas hold-up in an ebullated bed reactor is further illustrated in Figure 4. This comparison was made for catalytic ebullated bed reactors having equal total volumes, hydrocarbon feedrates, reaction temperatures and catalyst replacement rates. The results indicate that for reduced gas hold-up in a second stage reactor, the hydrodesulfurization results are significantly increased for various overall hydroconversion levels of 65 vol. %and 90 vol. % for the feedstock.
  • the first stage reactor effluent stream 19 is passed to the interstage separator 20, which has two main functions: (a) to provide an ebullating recycle liquid stream back to the first stage reactor with minimal gas entrainment, and (b) to provide a liquid feed stream to the second stage reactor 30 having a minimal vapor content.
  • the effect of the function (b) is reduced gas hold-up in the second stage reactor and the same reaction benefits as described for the first stage reactor.
  • the liquid feed to the second stage reactor 30 contains the unconverted residue from the original feedstock, and hydroconversion fractions which normally boil above about 600°F (316°C).
  • Recycled hydrogen, together with fresh make-up hydrogen at 45 is added as stream 32 to the second stage reactor 30, the hydrogen gas rate being selected so as to result in a minimal hydrogen partial pressure at the reactor 30 outlet as needed to meet processing and product objectives as described above.
  • the gas rate provided at 32 to the second stage reactor 30 for this invention is substantially lower. This results in lower gas hold-up volume percentages in the reactor, greater liquid residence time, and a more efficient reactor system. In this situation, the gas hold-up is reduced from about 27 to 12 vol. percent, which results in an improvement in second stage desulfurization results from 65 to 70 wt.% based on the fresh feedstock.
  • a liquid portion 26 from the liquid stream 22 provides liquid feed material upwardly through flow distributor 27 into ebullated bed 28 of the second stage catalytic ebullated bed reactor 30.
  • the catalyst bed 28 is expanded by 25-75% above its settled height by the upflowing gas and liquid therein.
  • Reactor liquid is withdrawn from an internal phase separator 33 through conduit 34 to recycle pump 35, and is reintroduced upwardly through the flow distributor 27 into the ebullated bed 28 to maintain the desired catalyst bed expansion therein.
  • the second stage catalytic reactor 30 with ebullated catalyst bed 28 is operated within the broad and preferred conditions as shown in Table 1 above, and maximizes resid hydrogenation reactions which occur therein.
  • the second stage reaction temperature is preferably 0-50°F lower than that of the first stage reactor.
  • Recycle and fresh hydrogen is provided at 32 to the second stage reactor 30, so that a minimal but adequate level of hydrogen partial pressure of 1,000-2,500 psi is maintained at the reactor 30 outlet.
  • the catalyst particles in ebullated beds 18 and 28 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 0.025 and 0.083 inch effective diameter, including beads, extrudates, or spheres, the catalyst size is preferably particles having sizes of 0.030-0.065 inch effective diameter. In the reactor, the density of the catalyst particles, and the lifting effect of the upflowing liquid and hydrogen gas are important factors in providing the desired 25-75 percent expansion and operation of the catalyst beds. If desired, used particulate catalyst may be withdrawn from the second stage reactor bed 28 at connection 36 and fresh catalyst is added at connection 36a as needed to maintain the desired catalyst volume and catalytic activity therein.
  • This used catalyst withdrawn at 36 which has relatively low metal contaminant concentration, can be passed to a treatment unit 38 where it is washed and screened to remove undesired fines at 37, and the recovered catalyst at 39 can provide 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.
  • an effluent stream is removed at 31 and passed to a phase separator 40.
  • a hydrogen-containing gas stream 41 is passed to the gas purification section 42 for removal of contaminants such as C0 2 , H 2 S, and NH 3 at vent 43.
  • Purified hydrogen at 44 is recycled back to each catalytic reactor 16 and 30 as desired as the hydrogen 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 tower unit 48.
  • a gaseous product stream is removed at 49 and a light hydrocarbon liquid product normally boiling between 400-650°F is withdrawn at 50.
  • a bottoms nominal 650°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 removed overhead at 55.
  • Vacuum bottoms stream 56 which has been hydrogenated in the second stage catalyst reactor 30, can be recycled back as stream 13 to the first stage catalytic reactor 16.
  • the recycle volume ratio for vacuum bottoms stream 56 to fresh feed at 10 can be 0-1.0/1, and preferably should be 0.2-0.7/1 for achieving hydroconversion of the feedstock exceeding about 70 vol. percent. It is pointed out that by utilizing this two stage catalytic hydroconversion process, the thermal reactions and catalytic activity in each stage reactor can be effectively matched and enhanced . The remaining unconverted vacuum bottoms material not being recycled at 13 is withdrawn at 57 as a net product.
  • the catalytic ebullated-bed two-stage reactors are operated at typical pre-invention conditions including a high feed rate of hydrogen entering the first stage reactor, the upward ebullation liquid flow being provided from an internally located recycle cup or gas/liquid separator, and with all of the first stage reactor effluent material (vapor + liquid) being passed directly to the catalytic second stage reactor.
  • the superficial gas velocities in the first and second staged reactors are about 0.11 and 0.15 ft/s respectively, and result in undesirably large gas hold-up volumes of 18-20 vol. % and 25-27 vol. % respectively in the first and second staged reactors.
  • the improved results for the present invention utilizing the same reactor total volume and liquid hourly space velocity as for the respective base Cases No. 1 and 3 are demonstrated.
  • the catalyst volume is increased and the catalyst space velocity is decreased by 15-20 percent due to elimination of the internal recycle cup or gas/liquid separator from the reactor upper portion.
  • the first stage gas hold-up volume is reduced by 8-11 percent primarily because a lower hydrogen gas circulation rate and a lower hydrogen partial pressure at the reactor outlet are utilized.
  • the gas hold-up volume is reduced by 45-55 percent.
  • This reduction in second stage gas hold-up volume percentage is due to the use of interstage gas/liquid separation, and the use of a reduced minimal hydrogen gas recirculation rate.
  • This reduction in the second stage reactor gas hold-up volume becomes available for providing increased reactor liquid volume and increases the effective liquid residence time in the second stage reactor by 20-30 percent.
  • Table 5 The comparative process performance for hydroconversion and desulfurization for the Cases No. 1 and 2, and for Cases No. 3 and 4 are shown in Table 5 below.
  • the increase in overall desulfurization from 89.5 to 91.1 wt.% in the moderate conversion cases and from 82.8 to 85.6 wt.% in the high conversion cases is a direct result of the increase in the second stage desulfurization.
  • the moderate 65 vol.% conversion cases utilized a particulate catalyst having a unimodal pore size distribution
  • the high conversion cases utilized a catalyst having a bi-modal pore size distribution which results in a somewhat lower desulfurization level.

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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)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

L'invention concerne un procédé d'hydrogénation catalytique à étapes multiples de charges d'hydrocarbures lourds, au moyen de réacteurs catalytiques à lit bouillonnant, que l'on fait fonctionner généralement aux mêmes conditions de réactions. Dans le procédé, la charge est mise en réaction avec un hydrogène dans un réacteur catalytique à lit bouillonnant de la première étape, dans des conditions de fonctionnement à température comprise entre 700 et 850 °F, à pression partielle d'hydrogène au niveau de l'orifice de sortie du réacteur comprise entre 800 et 3000 psi, à vitesse spatiale horaire du liquide comprise entre 0.2 et 2.0 V,/h/V, à vitesse spatiale du catalyseur comprise entre 0.03 et 0.33 bbl/jour par livre de catalyseur frais et à une vitesse gazeuse superficielle réduite comprise entre 0.02 et 0.3 ft/sec dans chaque réacteur, de manière à obtenir un volume de liquide en pour-cent amélioré et une retenue de gaz réduite dans chaque réacteur. La partie liquide de l'effluent du réacteur de la première étape est alimentée dans le réacteur de la deuxième étape. L'effluent du réacteur de la deuxième étape est soumis à une séparation de phases et fractionné de manière à produire des produits liquides à point d'ébullition inférieur. Une fraction de fonds sous vide étant en ébullition généralement à une température supérieure à environ 650 °F, de préférence supérieure à 900 °F, est recyclée dans le réacteur de la première étape.
EP00936894A 2000-06-19 2000-06-19 Procede d'hydrogenation mettant en oeuvre des reacteurs a lit bouillonnant a etapes multiples Expired - Lifetime EP1299507B1 (fr)

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
PCT/EP2000/005628 WO2001098436A1 (fr) 2000-06-19 2000-06-19 Procede d'hydrogenation mettant en oeuvre des reacteurs a lit bouillonnant a etapes multiples

Publications (2)

Publication Number Publication Date
EP1299507A1 true EP1299507A1 (fr) 2003-04-09
EP1299507B1 EP1299507B1 (fr) 2006-01-04

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EP00936894A Expired - Lifetime EP1299507B1 (fr) 2000-06-19 2000-06-19 Procede d'hydrogenation mettant en oeuvre des reacteurs a lit bouillonnant a etapes multiples

Country Status (6)

Country Link
EP (1) EP1299507B1 (fr)
JP (1) JP4834875B2 (fr)
CA (1) CA2412923C (fr)
DE (1) DE60025350T2 (fr)
MX (1) MXPA02012003A (fr)
WO (1) WO2001098436A1 (fr)

Families Citing this family (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP2234710A2 (fr) 2007-11-28 2010-10-06 Saudi Arabian Oil Company Processus d'hydrotraitement catalytique des pétroles bruts sulfureux
US7938953B2 (en) * 2008-05-20 2011-05-10 Institute Francais Du Petrole Selective heavy gas oil recycle for optimal integration of heavy oil conversion and vacuum gas oil treating
US7938952B2 (en) * 2008-05-20 2011-05-10 Institute Francais Du Petrole Process for multistage residue hydroconversion integrated with straight-run and conversion gasoils hydroconversion steps
US8372267B2 (en) 2008-07-14 2013-02-12 Saudi Arabian Oil Company Process for the sequential hydroconversion and hydrodesulfurization of whole crude oil
US9260671B2 (en) 2008-07-14 2016-02-16 Saudi Arabian Oil Company Process for the treatment of heavy oils using light hydrocarbon components as a diluent
EP2445997B1 (fr) 2009-06-22 2021-03-24 Saudi Arabian Oil Company Demetallisation et desulfurisation d'un petrole brut por coquage retardé
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
ITMI20130131A1 (it) * 2013-01-30 2014-07-31 Luigi Patron Processo a migliorata produttività per la conversione di olii pesanti

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Publication number Priority date Publication date Assignee Title
US3322665A (en) * 1965-05-18 1967-05-30 Hydrocarbon Research Inc High conversion hydrogenation of heavy gas oil
US4457831A (en) * 1982-08-18 1984-07-03 Hri, Inc. Two-stage catalytic hydroconversion of hydrocarbon feedstocks using resid recycle
JPS61287438A (ja) * 1985-06-14 1986-12-17 Mitsubishi Heavy Ind Ltd 三相流動反応器の分散装置
JPS627436A (ja) * 1985-07-03 1987-01-14 Mitsubishi Heavy Ind Ltd 三相流動反応器の分散機構
US4765882A (en) * 1986-04-30 1988-08-23 Exxon Research And Engineering Company Hydroconversion process
ZA961830B (en) * 1995-03-16 1997-10-31 Inst Francais Du Petrole Catalytic hydroconversion process for heavy petroleum feedstocks.

Non-Patent Citations (1)

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Title
See references of WO0198436A1 *

Also Published As

Publication number Publication date
MXPA02012003A (es) 2003-05-27
EP1299507B1 (fr) 2006-01-04
JP2004515568A (ja) 2004-05-27
WO2001098436A1 (fr) 2001-12-27
DE60025350T2 (de) 2006-07-13
JP4834875B2 (ja) 2011-12-14
CA2412923C (fr) 2008-10-07
DE60025350D1 (de) 2006-03-30
CA2412923A1 (fr) 2001-12-27

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