US3364134A - Black oil conversion and desulfurization process - Google Patents

Black oil conversion and desulfurization process Download PDF

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Publication number
US3364134A
US3364134A US597935A US59793566A US3364134A US 3364134 A US3364134 A US 3364134A US 597935 A US597935 A US 597935A US 59793566 A US59793566 A US 59793566A US 3364134 A US3364134 A US 3364134A
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hydrogen
zone
conversion
temperature
fraction
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Robert J J Hamblin
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Universal Oil Products Co
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Universal Oil Products Co
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Priority to US597935A priority Critical patent/US3364134A/en
Priority to FR129722A priority patent/FR1545345A/fr
Priority to GR670137030A priority patent/GR37030B/el
Priority to AT1074967A priority patent/AT276601B/de
Priority to YU2348/67A priority patent/YU33884B/xx
Priority to GB54023/67A priority patent/GB1196017A/en
Priority to BE707236D priority patent/BE707236A/xx
Priority to OA53112A priority patent/OA02543A/xx
Priority to SE16427/67A priority patent/SE342828B/xx
Priority to ES347769A priority patent/ES347769A1/es
Priority to DE19671645826 priority patent/DE1645826B1/de
Priority to JP42076685A priority patent/JPS503323B1/ja
Priority to NL676716296A priority patent/NL153597B/xx
Priority to CH1684867A priority patent/CH519017A/de
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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
    • C10G49/00—Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups C10G45/02, C10G45/32, C10G45/44, C10G45/58 or C10G47/00
    • C10G49/22—Separation of effluents
    • 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
    • C10G47/00—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions
    • 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

Definitions

  • the present invention is directed toward a process for converting atmospheric tower bottoms products, vacuum tower bottoms products (vacuum residuum), crude oil residuum, topped crude oils, crude oils extracted from tar sands, etc., all of which are commonly referred to as black oils, and which contain a significant quantity of asphaltic material and high concentrations of sulfur.
  • Petroleum crude oils particularly heavy oils extracted from tar sands, topped or reduced crudes, and vacuum residuum, contain high molecular weight sulfurous compounds in exceedingly large quantities, nitrogenous compounds, high molecular weight organo-metallic complexes containing principally nickel and vanadium as the metal component, and heptane-insoluble asphaltic material:
  • the latter is generally found to be complexed with, or linked to, sulfur and, to a certain extent, with metallic contaminants.
  • black oils differ considerably from heavy gas oils which are not so severely contaminated, and which normally do not have as high a boiling range.
  • a black oil can be characterized as a heavy hydrocarbonaceous material of which more than 10.0% (by volume) boils above a temperature of 1050 F., having a gravity, API at 60 F., of less than 20.0. Sulfur concentrations are exceedingly high, more than 1.0% by Weight, and are often in excess of 3.0% by weight. Conradson Carbon Residue factors exceed 1.0 Weight percent, and a great proportion of black oils exhibit a Conradson Carbon Residue factor above 10.0. There exists currently an abundant supply of such hydrocarbonaceous material, most of which has a gravity less than 10.0 API a't 60 F., and which is characterized by a boiling range indicating that 30.0% or more boils above a temperature of about 1050 F.
  • the process encompassed by the present invention is particularly directed toward the catalytic conversion of black oils into distillable hydrocarbons in yields which may be as high as 80.0% by volume, and sometimes higher.
  • Specific examples of the crude oils to which the present scheme is uniquely adaptable include a vacuum tower bottoms product having a gravity of 7.1 API at 60 F., and containing 4.05% by weight of sulfur arid 23.7% by Weight of rasphalts; a topped Middle-East Kuwait cnude oil, having a gravity of 11.0 API and containing 10.1% by weight of asphalts and 5.2% by weight of sulfur; a vacuum residuum having a gravity of 8.8*API and containing 3.0% sulfur and 4300 p.p.m.
  • the present invention affords the conversion of up to 80.0% by volume of such material into distillable hydrocarbons, heretofore having been considered impossible to achieve, especially on an economically feasible basis.
  • the principal difficulty resides in the lack of sulfur stability of many catalytic composites employed in current processes, and primarily from the presence of large quantities of asphaltic material and other non-distillables.
  • This asphaltic material comprises high molecular weight coke precursors, insoluble in pentane and/ or heptane, and which are usually complexed with nitrogen, metals and especially sulfur.
  • the asphaltic material is found to be dispersed within the black oil, and when subjected to heat, as in a Vacuum distillation process, has the tendency to fiocculate and polymerize whereby the conversion thereof to more valuable oil-insoluble products becomes extremely difficult.
  • the heavy bottoms from a crude oil vacuum distillation column indicates a Conradson Carbon Residue factor of 16.0% by Weight.
  • Such a material is generally useful only as road asphalt, or as an extremely low grade fuel when cut-back with distillate hydrocarbons such as kerosene, light gas oil. etc.
  • liquid-phase hydrogenation in the catalytic processing of such hydrocarbonaceous material, two principal approaches have been advanced: liquid-phase hydrogenation and vaporphase hydrocracking.
  • liquid phase oil is passed upwardly, in admixture with hydrogen into a fixed-bed or slurry of sub-divided catalyst; although perhaps effective in removing at least a portion of the organo-metallic complexes, this type process is relatively ineffective with respect to insoluble asphalts which are dispersed within the charge, with the consequence that the probability of effecting simultaneous contact between the catalyst particle and the asphaltic material in the presence of sufficient hydrogen is remote.
  • the reaction zone is generally maintained at an elevated temperature of at least about 500 C.
  • the present invention embodies a method whereby the asphaltic material is maintained in a dispersed state in a liquid phase which is rich in hydrogen.
  • This material comes into intimate contact with a catalyst which is capable of effecting reaction between the hydrogen and asphaltic material; the liquid phase is itself dispersed in a hydrogen-rich gas phase so that the dissolved hydrogen is continually replenished.
  • This two-fold dispersion and rapid, intimate contacting with the catalytic surfaces overcomes the difficulties encountered in previous processes whereby excessive residence times and depletion of localized hydrogen supply permit agglomeration of asphaltics and other high molecular weight species.
  • Such agglomerates are even less available to hydrogen, and are not, therefore, susceptible to catalytic reaction. They eventually form coke which becomes deposited on the catalyst,
  • the principal object of the present invention is to provide an economically feasible catalytic process for the desulfurization and conversion of black oils into distillable hydrocarbons for lower molecular weight and boiling range.
  • the practice of the present process results in a distillable hydrocarbon product in an amount of about 80.0% by volume of the black oil charge stock.
  • Another object is to convert heavy hydrocarbon charge stocks, a significant amount of which exhibits a boiling range above a temperature of 1050 F.-i.e. at least about 10.0% boils above this temperature, and often more than 30.0%-into lower-boiling distillable hydrocarbons.
  • Another object of my invention is to provide a process for desulfurizing and converting black oils having a gravity, API at 60 F., less than about 20.0, and to produce distillable hydrocarbons boiling below 800 F. from charge stocks, or select portions thereof having a cAPI gravity less than about 10.0.
  • Another object is to effect the conversion and desulfurization of black oils with minimum yield loss to asphalt and/ or residuum.
  • the present invention affords a process for the conversion of a hydrocarbon charge stock, of which at least about 10.0% by volume boils above a temperature of about 1050 F., and which contains at least about 1.0% by weight of sulfur, into lower boiling distillable hydrocarbon products, which process comprises the steps of: (a) separating said charge stock, in a first separation zone, into a light fraction having'an end boiling point of from about 650 F. to about 850 F.
  • this hot separator is also employed to separate the heavy oil as a liquid phase from a vapor phase containing lighter hydrocarbons, hydrogen and water.
  • This hot separator is maintained at essentially the same pressure as the reaction Zone and at essentially the temperature of the reaction zone effluent; as set forth, in a preferred embodiment, the temperature is controlled in the range of about 700 F. to about 750 F.
  • a second hot flash zone functions at a significantly reduced pressure of from subatmospheric to about p.s.i.g., and may comprise a low-pressure ash zonei.e. about 60 p.s.i.g.-in Vcombination with a vacuum column maintained at about 50-60 mm. of Hg absolute.
  • the hot flash system serves to eliminate further the diticulties stemming from emulsification problems by providing a residuum fraction containing the unconverted asphaltics and a significant amount of those sulfurous compounds not converted in the first reaction zone. Fur-y thermore, subsequent separations aud/ or distillations are greatly simplified.
  • a pressure substantially the same as, or -a temperature substantially the same as, is intended to connote the pressure or temperature on a downstream vessel, allowing only for the normal pressure drop due to fluid ow, and the normal temperature loss due to transfer of material from one zone to another.
  • the iirst'separation zone (hot separator) will function at a pressure of about 2530 p.s.i.g.; as previously set forth, it is preferred to quench this stream to about 750 F.
  • the second separation zone will function at a significantly reduced pressure less than 100 p.s.i.g., but at a temperature of about 750 F., subject to temperature loss due to flash evapora tion at constant enthalpy.
  • a black oil is intended to connote a hydrocarbonaceous mixture of which at least about 10.0% boils above a temperature of about 1050 F., and which contains more than 1.0% by weight of sulfur; and, distillable hydrocarbons are those normally liquid hydrocarbons, including pentanes, having boiling points below about 1050 F.
  • distillable hydrocarbons are those normally liquid hydrocarbons, including pentanes, having boiling points below about 1050 F.
  • Many of the black oils which may be desulfurized and converted by the process of this invention, are considered completely non-distillable-i.e. the total liquid boils above 1050 F. Still others are those of which from 10.0% to 60.0% by volume boils above 1050 F.
  • Conversion conditions are intended to be Vthose conditions imposed upon the conversion Zone to convert a substantial portion of the black oil linto distillable hydrocarbons.
  • the rst conversion zone conditions are intended to include temperatures above about 700 F., with an upper limit of about 800 F., as measured at the inlet to the catalyst bed. Since the bulk of the reactions being effected are exothermic, the reaction zone eil'luent will be at a higher temperature. In order that catalyst stability be preserved, it is preferred to control the inlet temperature such that the effluent temperature does no exceed a maximum limit of about 900 F.
  • Hydrogen is admixed with the black oil charge stock by way of compressive recycle, in an amount generally less than about 10,000 s.c.f./bbl., at the selected operating pressure, and preferably in an amount of from about 3000 to about 6000 scf/bbl.
  • the opera-ting pressure will be greater than 1000 p.s.i.g., and generally in the range of about 1500 p.s.i.g. to about 3000 psig.
  • the crude oil passes through the catalyst at a liquid hourly space velocity (dened as volumes of liquid hydrocarbon charge per hour, measured at 60 F., per volume of catalyst disposed in the reaction zone) of from about 0.25 to about 2.0.
  • the present process readily lends itself to continuous processing in an enclosed vessel through which the mixture of hydrocarbon charge stock and hydrogen is passed.
  • the internals of the vessel may be constructed in any suitable manner capable of providing the required intimate contact between the liquid charge stock, the gaseous mixture and the catalyst.
  • hydrogen is employed in admixture with the charge stock, and preferably in an amount of from about 3000 to about 6000 s.c.f./bbl.
  • the hydrogen-containing gas stream herein sometimes designated as recycle hydrogen, since it is conveniently recycled externally of the conversion zone, ful-fills a number of various functions: it serves as a hydrogenating agent, a heat carrier, and particularly a means for stripping converted material from the catalytic composite, thereby creating still more catalytically active sites available for the incoming, unconverted hydrocarbon charge stock. Since some hydrogenation will be effected, there will be a net consumption of hydrogen; to supplement this, hydrogen is added to the system from any suitable external source.
  • the catalytic composite disposed within the yfirst reaction zone can be characterized as comprising a metallic component having hydrogenation activity, which component is composited with a refractory inorganic oxide carrier material of either synthetic or natural origin.
  • a metallic component having hydrogenation activity is not considered essential to the present invention, although a siliceous carrier, such as 88.0% alumina and 12.0% silica, or 63.0% alumina and 37.0% silica, are generally preferred.
  • Suitable metallic components having hydrogenation activity are those selected from the group consisting of the metals of Groups VI-B and VIII of the Periodic Table, as indicated in the Periodic Chart of the Elements, Fisher Scientific Company (1953).
  • the catalytic composite may comprise one or more metallic components from the group of molybdenum, tungsten, chromium, iron, cobalt, nickel, platinum, palladium, iridium, osmium, rhodium, rnthenium, and mixtures thereof.
  • concentration of the catalytically active metallic component, or components is primarily dependent upon the particular metal as well as the characteristics of the charge stock.
  • the metallic components of Group VLB are preferably present in amounts within the range of about 1.0% to about 2.0% by Weight, the iron-group metals in an amount within the range of about 0.2% to about 10.0% by weight, whereas the platinum-group metals are preferably present in an amount within the range of about 0.1% to about 5.0% by weight, all of which are calculated as if the components existed within the finished catalytic composite as the elemental metal.
  • the refractory inorganic oxide carrier material may comprise alumina, silica, zirconia, magnesia, titania, boria, strontia, hafnia, etc., and mixtures of two or more including silica-alumina, silica-zirconia, silica-magnesia, silica-titania, alumina-zirconia, silica-alumina-boron phosphate, alumina-magnesia, alumina-titania, magnesia-zirconia, titania-zirconia, magnesia-titania, silica-aluminazirconia, silica-alumina-magnesia, silica-alumina-titania, silica-magnesia-zirconia, silica-alumina-boria, etc. It is preferred to utilize a carrier material containing at least a portion of silica, and preferably a composite of alumina
  • the light fraction initially separated from the fresh change stock, by-passes the lirst conversion zone, and is admixed with the vapor phases, or liquids condensed therefrom, from the second and third separation zones for conversion as a mixture in the second reaction zone.
  • the charge to the second reaction zone will contain both light and heavy normally liquid hydrocarbons, gaseous components including light hydrocarbon gases, hydrogen, hydrogen sulde, etc.
  • the end boiling point of this material will be 1100 F. or less, the greater volume thereof being in the range of 650 F. to 11001a F., although a significant amount will be butanes-400 F.
  • the operating conditions will be dependent to a great extent upon the characteristics of the total charge thereto, and upon the desired product quality and quantity.
  • the reactor will be maintained at a temperature of about 500 F., to about 1000 F. and under an imposed pressure within the range of about 500 to about 3000 p.s.i.g.
  • the hydrocarbon charge stock contacts the catalytic composite at a liquid hourly space velocity of from about 0.5 to about 10.0.
  • the catalyst disposed in the second reaction zone serves the dual function of further converting sulfurous and nitrogenous compounds, and converting those hydrocarbons boiling above about 700 F. to 800 F. into lower boiling hydrocarbons.
  • a particularly suitable catalyst comprises relatively large quantities of a Group VI-B metali.e. from 6.0% to 45.0% by weight of molybdenum-and lesser quantities of an iron-group metal-ie. 1.0% to about 6.0% by weight of nickel.
  • 205,530 lbs/hr. of a crude oil enters the process via line 1.
  • the contaminating inuences, characteristic of this crude oil include 3.25% by weight oirsulfur, 2400 p.p.m. of nitrogen, about 170 p.p.m. of metals and slightly more than about 8.0% by weight of heptane-insoluble asphaltics.
  • the material in line 1 is at a temperature of about 72.5 F.
  • iirst separation zone conveniently termed atmospheric Hash column 2.
  • the initial separation of the fresh charge stock may be effected in any suitable manner which produces a light fraction containing the greater Yshare of distillable hydrocarbons in the feed, the use of an essentially atmospheric pressure ash zone is selected considering the ease of separation at the selected cut point as well as the economic aspects.
  • a light principally vaporous fraction is removed overhead in line 3, in the amount of 62,763 lbs./hr.,.and has an average molecular weight of about 188.
  • a heavy fraction comprising 142,768 lbs/hr., having a molecular weight of about 548, is removed via line 4.
  • This heavy fraction at a temperature of about 720 F., is admixed with 133,734 lbs./hr. of a hot separator bottoms recycle stream in line 5, the source of which is hereafter described, and a recycle hydrogen stream, inran amount of 80,771 lbs/hr., in line 3.
  • This hydrogen-rich stream isY approximately 81.5 mol percent hydrogen, of which 2,840 lbs./hr.
  • the conversion zone eliluent leaves reactor 10 via line 11 at a temperature of about 875. F., and at a pressure of about 2600 p.s.i.
  • the eitluent is passed into ⁇ hot separator 12 at a temperature of 750 F. and a slightly lower pressure, resulting from iiuid flow through the system, of about 2590 p.s.i.g.
  • the pressure in this initial Y section-.of the process is substantially the same throughout, the lower pressures Vnaturally resulting from the normal pressure drop due to uid ow.
  • VA principally vaporous phase is withdrawn from the separator 12 through line lbs/hr;
  • a liquid phase is withdrawn from separator 12 through line 13, and a portion is diverted through line to be combined with the heavy fraction in line 4.
  • the liquid phase eiiluent in line 13 (leaving separator 12.) is in a total amount of 207,734 lbs./hr. and of this, 133,- 734 lbs./ hr. is diverted via line 5.
  • the remaining portion continues through line 13, andenters hot ash zone 15 at a temperature of about 730 F.
  • hot ash zone 15 functions at a pressure of about 75 p.s.i.g.
  • the quantity of material diverted through Vline Strom the 'hot separator eiiiuent in line 13, will be dependent primarily on the degree of contamination of the charge stock. Generally, however, the amount will be such that the combined feed ratio to reactor is within the range of 1.25 to about 3.0.
  • a residuum fraction having a molecular Weight of about 880, is withdrawn from hot Hash zone via line 16 in an amount of about 15,846 lbs./hr.
  • a vaporous fraction in an amount of 58,154 lbs/hr. is removed via line 17, and is admixed in line 3 with the light fraction from separation zone 2; also admixed with the light fraction is the principally vaporous phase from separator 12.
  • the mixture continues through line 3, in a total amount of 273,238 lbs/hr., into heater 18, wherein the temperature is increased to about 825 F.
  • 2,783 lbs./ hr. of'make-up hydrogen is Vadded to this charge by way of line 25.
  • the heated charge passes through line 19 into reactor 26 maintained at a pressure of about 2600 p.s.i.g. by compressive means not shown.
  • the eti'luent from reactor 26, leaving via line 20, is at a temperature of about 875 F.; after passing through con ⁇ denser 21 and line 22, Vthe eluent enters cold separator 23 at a temperature of about 120 F.
  • a hydrogen-rich gaseous phase is removed from separator 23 through lineV 6, in the amount of 77,931 lbs/hr. and is recycled thereby to be combined with the heavy fraction in line 4.
  • the normally liquid product is removed from separator 23 through line 24.
  • the product stream in line 24 may be subjected to a variety of subsequent separations and/ or fractionations to recover any desired boiling range mixture or mixtures, or substantially pure componentV steams. ⁇
  • the normally liquid hydrocarbonsV boiling below about 700 F., in the total product stream in line 24, contain less than 0.001% by weightY ofsulfur (less than 10.0 p.p. ⁇ m.).
  • the drawing was described in relation to a commercially scaled unit.
  • the figures presented are those vwhich stem from a unit designedV to process 15,000 bbl./ day of the crude oil, to produce maximum middle-distillate hydrocarbons.
  • the heavy fraction in line 4 is in an amount of 9,900 bbl/day having a gravity of 11.5 API;
  • the light fraction in line 3 is in an amount of 5,100 bbL/day having a gravity of 36.0 API.
  • the residuum fraction in line 16 has a gravity of 1.2 API, and is produced in an amount of 17,020 bbl./ day.
  • Table VI is presented to illustrate overall the yields of various hydrocarbon components from the crude oil charge stock.
  • the object of this commerciallyscaled unit is to maximize the yield of substantially sulfurfree liquid hydrocarbons boiling below about 700 F.
  • a process for the conversion of a hydrocarbon charge stock of which at least about 10.0% by volume boils above about 1050 F., and which contains at least about 1.0% by weight of sulfur which process comprises the steps of (a) separating said charge stock, in a rst separation zone, into a light fraction having an end boiling point of from about 650 F. to about 850 F. and a heavy fraction having an initial boiling point above about 650 F.;

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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)
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US597935A 1966-11-30 1966-11-30 Black oil conversion and desulfurization process Expired - Lifetime US3364134A (en)

Priority Applications (14)

Application Number Priority Date Filing Date Title
US597935A US3364134A (en) 1966-11-30 1966-11-30 Black oil conversion and desulfurization process
FR129722A FR1545345A (fr) 1966-11-30 1967-11-27 Procédé de conversion d'huile de pétrole brute
GR670137030A GR37030B (el) 1966-11-30 1967-11-27 Μεθοδος δια την μετατροπην αργου πετρελαιου.
YU2348/67A YU33884B (en) 1966-11-30 1967-11-28 Process for the conversion of heavy hydrocarbon black oil
GB54023/67A GB1196017A (en) 1966-11-30 1967-11-28 Black Oil Conversion Process.
AT1074967A AT276601B (de) 1966-11-30 1967-11-28 Verfahren zur Umwandlung eines Kohlenwasserstoffeinsatzes
BE707236D BE707236A (ja) 1966-11-30 1967-11-29
OA53112A OA02543A (fr) 1966-11-30 1967-11-29 Procédé de conversion d'huile de pétrole brute.
SE16427/67A SE342828B (ja) 1966-11-30 1967-11-29
ES347769A ES347769A1 (es) 1966-11-30 1967-11-29 Un procedimiento para la conversion de un material de cargahidrocarbonado.
DE19671645826 DE1645826B1 (de) 1966-11-30 1967-11-30 Verfahren zur Umwandlung eines Kohlenwasserstoffeinsatzmaterials
JP42076685A JPS503323B1 (ja) 1966-11-30 1967-11-30
NL676716296A NL153597B (nl) 1966-11-30 1967-11-30 Werkwijze voor de omzetting van een koolwaterstofvoeding, die kookt boven 370 graad c.
CH1684867A CH519017A (de) 1966-11-30 1967-11-30 Verfahren zur Konversion eines Kohlenwasserstoff enthaltenden Ausgangsmaterials und nach dem Verfahren erhaltene Mischung

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US597935A US3364134A (en) 1966-11-30 1966-11-30 Black oil conversion and desulfurization process

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JP (1) JPS503323B1 (ja)
AT (1) AT276601B (ja)
BE (1) BE707236A (ja)
CH (1) CH519017A (ja)
DE (1) DE1645826B1 (ja)
ES (1) ES347769A1 (ja)
GB (1) GB1196017A (ja)
GR (1) GR37030B (ja)
NL (1) NL153597B (ja)
OA (1) OA02543A (ja)
SE (1) SE342828B (ja)
YU (1) YU33884B (ja)

Cited By (35)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3445377A (en) * 1967-09-26 1969-05-20 Universal Oil Prod Co Desulfurization and conversion of black oils to maximize gasoline production
US3480540A (en) * 1967-03-16 1969-11-25 Exxon Research Engineering Co Process for hydrofining bitumen derived from tar sands
US4159935A (en) * 1978-08-30 1979-07-03 Uop Inc. Conversion of hydrocarbonaceous black oils
US4159937A (en) * 1978-08-30 1979-07-03 Uop Inc. Mixed-phase reaction product effluent separation process
US4695369A (en) * 1986-08-11 1987-09-22 Air Products And Chemicals, Inc. Catalytic hydroconversion of heavy oil using two metal catalyst
EP0271148A1 (en) * 1986-12-10 1988-06-15 Shell Internationale Researchmaatschappij B.V. Process for the manufacture of kerosine and/or gas oils
US5536391A (en) * 1995-01-17 1996-07-16 Howley; Paul A. Production of clean distillate fuels from heavy cycle oils
WO1999047626A1 (en) * 1998-03-14 1999-09-23 Chevron U.S.A. Inc. Integrated hydroconversion process with reverse hydrogen flow
US5958218A (en) * 1996-01-22 1999-09-28 The M. W. Kellogg Company Two-stage hydroprocessing reaction scheme with series recycle gas flow
US6096190A (en) * 1998-03-14 2000-08-01 Chevron U.S.A. Inc. Hydrocracking/hydrotreating process without intermediate product removal
US6200462B1 (en) 1998-04-28 2001-03-13 Chevron U.S.A. Inc. Process for reverse gas flow in hydroprocessing reactor systems
US6224747B1 (en) 1998-03-14 2001-05-01 Chevron U.S.A. Inc. Hydrocracking and hydrotreating
EP1342774A1 (en) * 2002-03-06 2003-09-10 ExxonMobil Chemical Patents Inc. A process for the production of hydrocarbon fluids
US20030211949A1 (en) * 2002-03-06 2003-11-13 Pierre-Yves Guyomar Hydrocarbon fluids
US20100122939A1 (en) * 2008-11-15 2010-05-20 Bauer Lorenz J Solids Management in Slurry Hydroprocessing
US10435339B2 (en) * 2017-05-12 2019-10-08 Marathon Petroleum Company Lp FCC feed additive for propylene/butylene maximization
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ES347769A1 (es) 1969-02-16
GB1196017A (en) 1970-06-24
BE707236A (ja) 1968-04-01
AT276601B (de) 1969-11-25
SE342828B (ja) 1972-02-21
NL6716296A (ja) 1968-05-31
GR37030B (el) 1969-04-08
YU234867A (en) 1977-12-31
JPS503323B1 (ja) 1975-02-03
YU33884B (en) 1978-06-30
OA02543A (fr) 1970-05-05
CH519017A (de) 1972-02-15
NL153597B (nl) 1977-06-15
DE1645826B1 (de) 1972-03-16

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