US2388055A - Petroleum conversion process - Google Patents

Petroleum conversion process Download PDF

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Publication number
US2388055A
US2388055A US446850A US44685042A US2388055A US 2388055 A US2388055 A US 2388055A US 446850 A US446850 A US 446850A US 44685042 A US44685042 A US 44685042A US 2388055 A US2388055 A US 2388055A
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Prior art keywords
coke
catalyst
line
oil
withdrawn
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US446850A
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Charles E Hemminger
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Standard Oil Development Co
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Standard Oil Development Co
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Priority to US446850A priority patent/US2388055A/en
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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
    • C10G51/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more cracking processes only
    • C10G51/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more cracking processes only plural serial stages only
    • C10G51/04—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more cracking processes only plural serial stages only including only thermal and catalytic cracking steps

Definitions

  • the present invention relates to improvements in the art of treating hydrocarbons and, more particularly, it relates to the preparation of feed stocks for cracking operations.
  • the catalyst is in the form of a horrinized mass or extremely dense suspension and is adapted to be continuously withdrawn from the reactor, regenerated and recycled to the said reactor.
  • the catalyst When using high catalyst to oil weight ratios and making use of the heat content of the catalyst recovered from the regeneration zone, it is possible to effect the desired conversion of heavy stocks into substantial quantities of gasoline of high octane number, even though the charging heavy oil is merely preheated to temperatures considerably below cracking temperatures and in some cases where the fresh feed is fed into the reaction zone at ordinary atmospheric temperatures.
  • One object of my invention therefore is to subject a heavy petroleum hydrocarbon oil, such as a reduced crude to a viscosity reducing operation in a conversion zone where the conversion is carried out continuously in the presence of a powdered material, to recover vapors containing substantial quantities of gas oil from said conversion zone, and then to crack these gas oil vapors without substantial cooling in a separate cracking zone where preferably an active cracking catalyst i is present.
  • I shall refer to the drawing.
  • I represents a charging line into which a heavy petroleum hydrocarbon oil, such as a reduced East Texas crude oil having an A. P. I. gravity of say about 18, is introduced into the system and thence pumped by.pu'mp 3 directly into a viscosity reducing reactor containing, as will hereinafter more fully appear, a fluidized mass of powdered coke, which coke is in the form of a dense suspension having an upper level substantially at L and being maintained in this condition by a gasiform material which passes through 5 at a slow enough rate to maintain the coke in the iiuidzed condition referred to.
  • a heavy petroleum hydrocarbon oil such as a reduced East Texas crude oil having an A. P. I. gravity of say about 18
  • a viscosity reducing reactor containing, as will hereinafter more fully appear, a fluidized mass of powdered coke, which coke is in the form of a dense suspension having an upper level substantially at L and being maintained in this condition by a gasi
  • the coke may be maintained in this condition when it is ground to a size of from 100-400 mesh by forcing a gasiform material upwardly through the reactor at a linear velocity of say 0.3-5 ft. /second.
  • a gasiform material upwardly through the reactor at a linear velocity of say 0.3-5 ft. /second.
  • the coke forms a dense suspension which, however, is not to be confused with the ordinary conception of a suspension which usually means that a solid is suspended in a gas moving at a velocity sufficiently high to cause substantially concurrent movement of solid and gas.
  • my reactor 5 thel velocities are much lower so that there is a slippage of solid with respect to gas, and the final result is that the mass of coke is in a turbulent, ebullient condition resembling roughly a boiling liquid.
  • the coke is preferably maintained at a sufciently high temperature so that when cold or heated oil is discharged from I into the reactor, the cil is heated up to a temperature" of 850- 1200 F.
  • This temperature may beacquired by maintaining a high weight ratio of coke to oil where the coke is at an inlet temperature of say 100G-1100 F., up to 1300 F.
  • the oil remains resident in the vessel 5, which is maintained under a pressure just suliicient to overcome pressure ,drops inthe subsequent portions of the apparatus and may be of the order of -50 lbs gauge for a suiiicient period of time to form vaporized products containinga minimum of gasoline and tar and/or coke, the latter being absorbed by the coke present in the reactor.
  • the mass below L may have a density of from say 10-40 lbs./cu. ft.
  • the vapors in line I0 under best operating conditions will have a density of the order of say 0.01 to 0.001 lbs/cu. ft.
  • the nes are separated in cyclone separator ,I2 and then returned through line I4 to the coking vessel.
  • the overhead vapors are withdrawn through line I6 and since they are at a temperature of about 850-1200 F'.
  • the catalyst which may be an acid treated clay or a synthetic catalyst such as a mixture of silica and alumina or silica and magnesia gels, or other known catalysts is preferably in the form of a powder having a particle size of from 20D-400 mesh, and the ilow of vapors upwardly through reaction vessel I8 is so regulated as to linear velocity, that it is somewhere between 0.3-5 ft.
  • the heated vapors are in contact with the catalyst for a sucient period of time to effect the desired conversion which usually is a matter of say l0-l5 or 20 seconds, and the reaction products are withdrawn overhead through line 20 and discharged into a cyclone separator 24 where the rines are separated and returned to the reactor through line 30.
  • the vapors in line 20 contain only a very small amount of catalyst if disengaging space between L and the top of reactor is of the order of l2 ft. even where the density of the mass below L' is as high as from 10-40 lbs. per cu. ft.
  • the vapors in fractionator 35 are fractionated into two fractions, namely, an overhead product which is withdrawn through line 4I, passed through a condenser 43, thence withdrawn through line 5I 'and discharged into receiving drum 53.
  • the lighter hydrocarbons are withdrawn through a .line 5B and compressed in a compressor 5l to about 200 lbs/sq. in., or, in other words, sufciently high to liquefy not only the C5 but also the C4 hydrocarbons, or at least a major portion of them.
  • the bottoms from drum 53 are withdrawn through line 55 and these are also pumped into receiving drum 6U.
  • the liquid product consisting of gasoline is withdrawn as product through line 6I.
  • the overhead from drum 60 is withdrawn through line 62, and this overhead consists essentially of C3 and lighter hydrocarbons which may be recycled to line 40 to aid in the liuidizing of the solid material in reactor 5, and also to aid in repressing the formation of C3 y and lighter gas from the charging oil during the reaction.
  • coke is continuously withdrawn through the draw-off pipe 'Ill and preferably is discharged into an injector l2 where it is admixed with air also discharged into said injector through line 15.
  • injector l2 a suspension of the powdered coke in air is formed, and this suspension is withdrawn through line 16.
  • injector 'I2 some other suitable mixing device may be employed.
  • the suspension in line I6 is then discharged into a high speed upiiow reactor 80, that is to say, it is discharged into a reactor 8U where it flows upwardly at a linear velocity of about 2-10 ft./second, producing a suspension in 80 which is substantially different from that ot 5 or I8, in that it is less dense, weighing say from 5-20 lbs/cu. ft. and in which suspension there is much less delayed settling or slippage.
  • vessel 80 which is in effect a combustion zone, the coke or tar formed in the vessel 5 is burnt, together with some of the original coke, although the amount of the latter which is burnt is preierably limited.
  • the air discharged into the system through line 'I5 need not be heated .to cause active combustion in vessel 80Uand the entering air may be at atmospheric temperatures.
  • the revlviiied coke is withdrawn from combustion zone 80 through line 85 and thence discharged into a cyclone separator 86 in which the coke is separated from the flue gases and discharged through line 90 into the coking vessel 5.
  • Flue gases are withdrawn from cyclone separator 86 through line 92, and these gases may be sent to other dust separators or the like to recover additional coke, but preferably they are discharged directly into a waste heat boiler (discussed later) to recover a portion of their sensible heat.
  • the coke in line 90 due to its passage through combustion zone 80, will normally have its temperature increased a few hundred degrees so that as it re-enters vessel 5 it will have a temperature of 1000l-1300J F. or higher.
  • the superheat of the coke will serve to supply the heat necessary in reaction vessel 5, thus tending to make the coking phase of my operation self-sustaining with respect to heat requirements, as is previously indicated.
  • the catalyst in reaction vessel I8 is continuously withdrawn through line
  • This suspension is withdrawn through line I
  • the catalyst which is at a temperature of about say 850 drawn from reaction vessel I8 may be mixed with air, and this mixture when discharged into F. or l200 F. as it is withvessel
  • the suspension will move concurrently upward with respect to air and catalyst, in vessel
  • the total catalyst is taken of! overhead which, as previously indicated, is possible when the suspension moves at a velocity of about 2-10 ft./second where the catalyst is in a particle size of from -400 mesh or thereabouts.
  • the suspension is then discharged into cyclone separator
  • This catalyst normally would be at a temperature of 1050-1300 F.. as it enters the cracker I8, and here also by using a high catalyst to oil ratio, that is to say, using 5-20 lbs.
  • the cracking reaction taking place in I8 may bei fully satisfied as to heat requirements by the sensible heat of the catalyst. Since, of course, in this case the entering oil is not cold and depending on the temperature of the oil vapors in line I6, the amount of catalyst may be reduced and of proportion to maintain in vessel I8.
  • the ue gases are withdrawn from cyclone separator
  • 20 contain combustibles in the form of CO and slight traces of Hz-i-CH4.
  • the CO to CO2 ratio may be as high as 1 to l, giving a heat content of about 15 to 25 B. t. 11./cu. ft. Due to the low concentration of the combustibles and the low temperature they do not burn in the presence of oxygen and the heat is not recoverable. However, the u addition of the hotter gases, usually 50-100 F.
  • this heat recoverysystem allows the conversion of part of the coke formed in viscosity breaking in vessel 5 into useful heat in the form of steam.
  • This withdrawn portion is the iiner part and as such is a means'of regulating the neness of the coke circulating stream.
  • the withdrawal of this coke also cheapens and simplifles the recovery system 86.
  • all of the coke formed in the viscosity breaking can be withdrawn through line 92 and burned to generate steam in boiler
  • I may use some other material such as pumice, or I may use an active cracking catalyst such as an acid treated clay, although I prefer to limit the operation taking place in reaction vessel to the production of a maximum quantity of gas oil which I subsequently employ as a feed stock to a cracking operation.
  • I may thermally crack the gas oil in cracker I8 at high temperatures in the presence of steamy and by this means secure a gasoline product of improved quality.
  • 40 may be employed to preheat the oil entering the system through line I, in which case a lesser quantity of hot coke would have to be recirculated to vessel 5 to maintain the viscosity reducing operation.
  • reactors 5 and i8 are the bottom drawoiT type, that is, where the bulk of catalyst is drawn oil from the bottom through the standpipe, it is to be understood that it is within the scope of my invention to employ reactors where the bulk of the material is withdrawn overhead as, for example, in regenerators 80 and
  • the method of producing gasoline from reduced crude petroleum oil in a two-stage operation which comprises first discharging the oil into a heated fiuidized mass of powdered coke in cooled into a iluidized mass of heated cracking said vapors to remain in contact with the heated catalyst for a.
  • suiilcient period of time to convert a substantial portion of the gas oil into gasoline withdrawing the reaction products from contact with the said catalyst recovering therefrom a gasoline of improved quality and withdrawing both the coke and the catalyst from the viscosity reducing zone and the cracking zone respectively, causing combustion in the presence of air of combustibles associated with the coke and said catalyst in said zones whereby the temperatures of both the coke and the catalyst are increased, and returning the coke and catalyst to the viscosity reducing zone and the cracking zone respectively in suillcient quantity to maintain reactions as regards heat requirements in said zones.
  • a continuous method for producing gasoline from a relatively heavy hydrocarbon oil in a multi-stage operation which comprises discharging the heavy cosity reducing zone and said cracldng zone. respectively, separatelysubjecting said petroleum coke and said fouled catalyst to the influence of an oxygen-containing gas at temperatures sumciently elevated to cause combustion of the carbonaceous contaminants, and thereatjter returning substantially uncooled the petroleum coke to the viscosity reducing zone andthe regenerated catalyst to the cracking zone.

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  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (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)
US446850A 1942-06-13 1942-06-13 Petroleum conversion process Expired - Lifetime US2388055A (en)

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Cited By (47)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2428715A (en) * 1944-09-08 1947-10-07 Pure Oil Co Catalytic cracking of hydrocarbons
US2452569A (en) * 1946-09-10 1948-11-02 Houdry Process Corp Process of treating hydrocarbons in presence of hot contact masses
US2456707A (en) * 1944-08-17 1948-12-21 Hydrocarbon Research Inc Process for stripping spent fluid catalysts
US2461958A (en) * 1944-12-14 1949-02-15 Standard Oil Dev Co Treating hydrocarbon fluids
US2507523A (en) * 1946-08-31 1950-05-16 Houdry Process Corp Conversion of hydrocarbons
US2513294A (en) * 1946-08-02 1950-07-04 Socony Vacuum Oil Co Inc Process for conducting chemical reactions
US2521757A (en) * 1945-12-15 1950-09-12 Houdry Process Corp Conversion of heavy hydrocarbon materials
US2571342A (en) * 1947-02-18 1951-10-16 Socony Vacuum Oil Co Inc Combination hydrocarbon vaporization and cracking process
US2587703A (en) * 1948-02-18 1952-03-04 Universal Oil Prod Co Cracking heavy oils in presence of oxygen
US2610944A (en) * 1951-01-23 1952-09-16 Standard Oil Dev Co Treatment of carbonaceous solids
US2636844A (en) * 1950-08-29 1953-04-28 Standard Oil Dev Co Process for the conversion of reduced crudes in the presence of an added naphtha
US2655465A (en) * 1951-07-24 1953-10-13 Standard Oil Dev Co Residuum coking and cracking
US2655464A (en) * 1951-06-09 1953-10-13 Standard Oil Dev Co Residuum coking and cracking
US2687986A (en) * 1951-05-01 1954-08-31 Standard Oil Dev Co Hydrocarbon conversion
US2690990A (en) * 1950-09-08 1954-10-05 Standard Oil Dev Co Production of motor fuels from heavy hydrocarbon oils in a two stage conversion process with inert solids
US2731394A (en) * 1951-05-25 1956-01-17 Exxon Research Engineering Co Conversion of heavy hydrocarbon oils
US2731395A (en) * 1951-06-19 1956-01-17 Exxon Research Engineering Co Conversion of hydrocarbons in two stages with inert and catalyst particles
US2731400A (en) * 1951-06-02 1956-01-17 Standard Oil Dev Co Conversion of hydrocarbons
US2734020A (en) * 1956-02-07 Catalyst
US2734021A (en) * 1956-02-07 Preparation of catalytic feed stocks
US2734850A (en) * 1951-05-19 1956-02-14 brown
US2736687A (en) * 1951-07-14 1956-02-28 Exxon Research Engineering Co Shot heated fluid conversion system
US2737474A (en) * 1952-01-23 1956-03-06 Exxon Research Engineering Co Catalytic conversion of residual oils
US2742403A (en) * 1951-04-12 1956-04-17 Exxon Research Engineering Co Cracking of reduced crude with the use of inert and catalyst particles
US2756195A (en) * 1951-04-13 1956-07-24 Exxon Research Engineering Co Cracking of heavy hydrocarbons with inert solids
US2763600A (en) * 1951-05-19 1956-09-18 Exxon Research Engineering Co Upgrading of heavy hydrocarbonaceous residues
US2766184A (en) * 1952-02-01 1956-10-09 Exxon Research Engineering Co Combination oil refining process
US2773017A (en) * 1952-08-05 1956-12-04 Exxon Research Engineering Co Integrated refining of crude oil
US2775546A (en) * 1951-06-20 1956-12-25 Exxon Research Engineering Co Conversion of hydrocarbons in the presence of inert solids
US2789084A (en) * 1954-06-30 1957-04-16 Lummus Co Hydrocarbon conversion
US2847357A (en) * 1954-06-21 1958-08-12 Exxon Research Engineering Co Fluid coking process
US2852439A (en) * 1953-09-29 1958-09-16 Exxon Research Engineering Co Integrated fractionation, fluid coking and catalytic cracking process for hydrocarbon oils
US2852441A (en) * 1954-10-22 1958-09-16 Exxon Research Engineering Co Conversion of hydrocarbons
US2859174A (en) * 1952-04-29 1958-11-04 Exxon Research Engineering Co Treating hydrocarbon oils with inert solids and gaseous halogen containing compounds
US2861943A (en) * 1952-07-16 1958-11-25 Hydrocarbon Research Inc Hydrocracking process with the use of fluidized inert particles
US2863821A (en) * 1954-02-03 1958-12-09 Exxon Research Engineering Co Prevention of coking reactor cyclone dipleg plugging
US2871185A (en) * 1956-08-10 1959-01-27 Standard Oil Co Removal of metals from reduced crudes by mild coking in the presence of a silico ortho ester
US2871184A (en) * 1955-06-28 1959-01-27 Shell Dev Process for the production of gasoline from petroleum residues
US2879221A (en) * 1954-07-15 1959-03-24 Exxon Research Engineering Co Hydrocarbon oil conversion process
US2899376A (en) * 1959-08-11 Liquid phase - boo
US2904499A (en) * 1954-02-17 1959-09-15 Exxon Research Engineering Co Process and apparatus for conversion of heavy oil with coke particles in two stages employing inert and catalytic coke solids
US2905618A (en) * 1952-04-04 1959-09-22 Gulf Research Development Co Fluid catalytic hydrocracking of high boiling hydrocarbon oils in several stages
US2905622A (en) * 1954-04-29 1959-09-22 Phillips Petroleum Co Production of fuel gas and liquid hydrocarbon fuels
US2911353A (en) * 1955-11-08 1959-11-03 Exxon Research Engineering Co Treatment of a metal-contaminated heavy gas oil with non-adsorbent carbon particles
US2920936A (en) * 1957-05-14 1960-01-12 Texaco Inc Recovery of heavy metals from hydrocarbons
US3617481A (en) * 1969-12-11 1971-11-02 Exxon Research Engineering Co Combination deasphalting-coking-hydrotreating process
US8691077B2 (en) 2012-03-13 2014-04-08 Uop Llc Process for converting a hydrocarbon stream, and optionally producing a hydrocracked distillate

Cited By (47)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2734020A (en) * 1956-02-07 Catalyst
US2899376A (en) * 1959-08-11 Liquid phase - boo
US2734021A (en) * 1956-02-07 Preparation of catalytic feed stocks
US2456707A (en) * 1944-08-17 1948-12-21 Hydrocarbon Research Inc Process for stripping spent fluid catalysts
US2428715A (en) * 1944-09-08 1947-10-07 Pure Oil Co Catalytic cracking of hydrocarbons
US2461958A (en) * 1944-12-14 1949-02-15 Standard Oil Dev Co Treating hydrocarbon fluids
US2521757A (en) * 1945-12-15 1950-09-12 Houdry Process Corp Conversion of heavy hydrocarbon materials
US2513294A (en) * 1946-08-02 1950-07-04 Socony Vacuum Oil Co Inc Process for conducting chemical reactions
US2507523A (en) * 1946-08-31 1950-05-16 Houdry Process Corp Conversion of hydrocarbons
US2452569A (en) * 1946-09-10 1948-11-02 Houdry Process Corp Process of treating hydrocarbons in presence of hot contact masses
US2571342A (en) * 1947-02-18 1951-10-16 Socony Vacuum Oil Co Inc Combination hydrocarbon vaporization and cracking process
US2587703A (en) * 1948-02-18 1952-03-04 Universal Oil Prod Co Cracking heavy oils in presence of oxygen
US2636844A (en) * 1950-08-29 1953-04-28 Standard Oil Dev Co Process for the conversion of reduced crudes in the presence of an added naphtha
US2690990A (en) * 1950-09-08 1954-10-05 Standard Oil Dev Co Production of motor fuels from heavy hydrocarbon oils in a two stage conversion process with inert solids
US2610944A (en) * 1951-01-23 1952-09-16 Standard Oil Dev Co Treatment of carbonaceous solids
US2742403A (en) * 1951-04-12 1956-04-17 Exxon Research Engineering Co Cracking of reduced crude with the use of inert and catalyst particles
US2756195A (en) * 1951-04-13 1956-07-24 Exxon Research Engineering Co Cracking of heavy hydrocarbons with inert solids
US2687986A (en) * 1951-05-01 1954-08-31 Standard Oil Dev Co Hydrocarbon conversion
US2763600A (en) * 1951-05-19 1956-09-18 Exxon Research Engineering Co Upgrading of heavy hydrocarbonaceous residues
US2734850A (en) * 1951-05-19 1956-02-14 brown
US2731394A (en) * 1951-05-25 1956-01-17 Exxon Research Engineering Co Conversion of heavy hydrocarbon oils
US2731400A (en) * 1951-06-02 1956-01-17 Standard Oil Dev Co Conversion of hydrocarbons
US2655464A (en) * 1951-06-09 1953-10-13 Standard Oil Dev Co Residuum coking and cracking
US2731395A (en) * 1951-06-19 1956-01-17 Exxon Research Engineering Co Conversion of hydrocarbons in two stages with inert and catalyst particles
US2775546A (en) * 1951-06-20 1956-12-25 Exxon Research Engineering Co Conversion of hydrocarbons in the presence of inert solids
US2736687A (en) * 1951-07-14 1956-02-28 Exxon Research Engineering Co Shot heated fluid conversion system
US2655465A (en) * 1951-07-24 1953-10-13 Standard Oil Dev Co Residuum coking and cracking
US2737474A (en) * 1952-01-23 1956-03-06 Exxon Research Engineering Co Catalytic conversion of residual oils
US2766184A (en) * 1952-02-01 1956-10-09 Exxon Research Engineering Co Combination oil refining process
US2905618A (en) * 1952-04-04 1959-09-22 Gulf Research Development Co Fluid catalytic hydrocracking of high boiling hydrocarbon oils in several stages
US2859174A (en) * 1952-04-29 1958-11-04 Exxon Research Engineering Co Treating hydrocarbon oils with inert solids and gaseous halogen containing compounds
US2861943A (en) * 1952-07-16 1958-11-25 Hydrocarbon Research Inc Hydrocracking process with the use of fluidized inert particles
US2773017A (en) * 1952-08-05 1956-12-04 Exxon Research Engineering Co Integrated refining of crude oil
US2852439A (en) * 1953-09-29 1958-09-16 Exxon Research Engineering Co Integrated fractionation, fluid coking and catalytic cracking process for hydrocarbon oils
US2863821A (en) * 1954-02-03 1958-12-09 Exxon Research Engineering Co Prevention of coking reactor cyclone dipleg plugging
US2904499A (en) * 1954-02-17 1959-09-15 Exxon Research Engineering Co Process and apparatus for conversion of heavy oil with coke particles in two stages employing inert and catalytic coke solids
US2905622A (en) * 1954-04-29 1959-09-22 Phillips Petroleum Co Production of fuel gas and liquid hydrocarbon fuels
US2847357A (en) * 1954-06-21 1958-08-12 Exxon Research Engineering Co Fluid coking process
US2789084A (en) * 1954-06-30 1957-04-16 Lummus Co Hydrocarbon conversion
US2879221A (en) * 1954-07-15 1959-03-24 Exxon Research Engineering Co Hydrocarbon oil conversion process
US2852441A (en) * 1954-10-22 1958-09-16 Exxon Research Engineering Co Conversion of hydrocarbons
US2871184A (en) * 1955-06-28 1959-01-27 Shell Dev Process for the production of gasoline from petroleum residues
US2911353A (en) * 1955-11-08 1959-11-03 Exxon Research Engineering Co Treatment of a metal-contaminated heavy gas oil with non-adsorbent carbon particles
US2871185A (en) * 1956-08-10 1959-01-27 Standard Oil Co Removal of metals from reduced crudes by mild coking in the presence of a silico ortho ester
US2920936A (en) * 1957-05-14 1960-01-12 Texaco Inc Recovery of heavy metals from hydrocarbons
US3617481A (en) * 1969-12-11 1971-11-02 Exxon Research Engineering Co Combination deasphalting-coking-hydrotreating process
US8691077B2 (en) 2012-03-13 2014-04-08 Uop Llc Process for converting a hydrocarbon stream, and optionally producing a hydrocracked distillate

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