US3775292A - Combination process for the conversion of hydrocarbonaceous black oil - Google Patents

Combination process for the conversion of hydrocarbonaceous black oil Download PDF

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US3775292A
US3775292A US00277025A US3775292DA US3775292A US 3775292 A US3775292 A US 3775292A US 00277025 A US00277025 A US 00277025A US 3775292D A US3775292D A US 3775292DA US 3775292 A US3775292 A US 3775292A
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solvent
extraction
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C Watkins
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Honeywell UOP LLC
Universal Oil Products Co
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Universal Oil Products Co
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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
    • C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
    • C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
    • C10G67/04—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only including solvent extraction as the refining step in the absence of hydrogen
    • C10G67/0454—Solvent desasphalting
    • C10G67/049—The hydrotreatment being a hydrocracking

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  • ABSTRACT Maximum conversion of black oil charge stocks to distillable hydrocarbon products is achieved through a combination process involving solvent deasphalting, solvent deresining and multiple-stage hydrocracking.
  • Petroleum crude oils particularly the heavy oils extracted from tar sands, topped or reduced crudes, vacuum residuum, etc., contain high molecular weight sulfurous compounds in exceedingly large quantities.
  • black oils contain excessive quantities of nitrogenous compounds, high molecular weight organometallic complexes, principally containing nickel and vanadium, and varying quantities of asphaltenic material.
  • An abundant supply of these hydrocarbonaceous charge stocks exists, most of which have a gravity less than about 20.0 API.
  • Black oils are generally further characterized by a boiling range indicating that 10.0 percent by volume, or more, boils above a temperature of about 1,050F.
  • the combination process of the present invention is particularly directed toward the catalytic conversion of black oils to produce desulfurized, distillable hydrocarbons, and to effect such conversion in a manner which results in a volumetric yield approaching and/or exceeding 100.0 percent.
  • black oils illustrative of those to which the present process is applicable, include a vacuum tower bottoms having a gravity of 7.1 API, and containing 4.05 percent by weight of sulfur and 23.7 percent by weight of asphaltics; a topped crude oil, having a gravity of 11.0 API, and containing 10.1 percent by weight of asphaltics and 5.20 percent by weight of sulfur; and, a vacuum residuum having a gravity of about 8.8 API, containing 3.0 percent by weight of sulfur and 4,300 ppm. by weight of nitrogen, and having a 20.0 volumetric distillation temperature of about 1,055F.
  • An object of the present invention is to provide an economically feasible fixed-bed catalytic process for converting hydrocarbonaceous black oils into distillable hydrocarbons of lower molecular weight and boiling range.
  • a corollary objective is to maximize the production of desulfurized hydrocarbons from a given quantity of an asphaltene-containing black oil.
  • Another object is to provide a process which affords an extension of the effective, acceptable life of the catalytic composite employed in the conversion reaction zones.
  • the present invention encompasses a process for the conversion of an asphaltene-containing hydrocarbonaceous charge stock, to produce lowerboiling hydrocarbon products, which process comprises the steps of: (a) deasphalting said charge stock with a selective solvent, in a first solvent extraction zone, at extraction conditions selected to provide (i) a solvent-lean asphaltic pitch and (ii) a solvent-rich, deasphalted first liquid phase; (b) deresining at least a portion of said first liquid phase with a selective solvent, in a second solvent extraction zone, at extraction conditions selected to provide (i) a solvent-lean resin concentrate and (ii) a deresined second liquid phase; (0) reacting at least a portion of said resin concentrate with hydrogen, in a first catalytic reaction zone, at hydrocracking conditions selected to convert resins into lower-boiling hydrocarbons; (d) reacting at least a portion of said deresined second liquid phase and at least a portion of the resulting first reaction zone eff
  • the extraction conditions in said second extraction zone include a higher temperature (10F. to 200F. higher) than that in said first extraction zone.
  • at least a portion of the resulting first reaction zone effluent is introduced into the second solvent extraction zone.
  • the asphaltic material is dispersed within the black oil, and, when subjected to the operating conditions required to effect desulfurization, has the tendency to agglomerate and polymerize, as a result of which the active surfaces of the catalytic composite are effectively shielded from the material being processed.
  • the combination process encompassed by the pres- 'ent inventive concept, utilizes a solvent deasphalting, or solvent extraction zone to precipitate and remove a metal-containing asphaltic concentrate. It must necessarily be acknowledged that the prior art is replete with a wide spectrum of techniques for effecting solvent deasphalting of asphaltene-containing hydrocarbonaceous charge stocks. No attempt is herein made to claim solvent deasphalting other than as an integral element of the present combination process. Any suitable solvent deasphalting technique known in the prior art may be employed, several examples of which are hereinafter described. In the interest of brevity, no attempt will be made to delineate exhaustively the solvent deasphalting art.
  • Suitable solvents include light petroleum hydrocarbons such as naphtha, casing-head gasoline, light petroleum fractions comprising propane, n-butane and isobutane, certain alcohols, ether and mixtures thereof, etc.
  • US. Pat. No. 2,002,004 (Class 208-l4) involves a 2-stage deasphalting process wherein the second stage completes the precipitation of asphalts which was only partially effected in the first stage.
  • the described solvents include naphtha, casing head gasoline, and liquefied normally gaseous hydrocarbons such as ethane, propane, butanes, and mixtures thereof, etc.
  • U.S. Pat. No. 2,914,457 (Class 208-79) describes a multiple combination process involving fractionation, vacuum distillation, solvent deasphalting,. hydrogenation and catalytic reforming.
  • the suitable liquid deasphalting solvents include liquefied normally gaseous hydrocarbons such as propane, n-butane, isobutane, as well as ethane, ethylene, propylene, nbutylene, isobutylene, pentane, isopentane, and mixtures thereof.
  • the deasphalting zone functions to reject an asphaltic pitch and to produce a deasphalted oil containing convertible resins.
  • prior art techniques do not distinguish between the asphaltenic material and resins; that is, prior art processes reject resins along with the asphaltic pitch. This is contrary to the present combination process wherein the resin-containing deasphalted oil is subjected to a solvent deresining technique.
  • the solvent-lean resin concentrate is subsequently reacted with hydrogen, in a first catalytic reaction zone at hydrocracking conditions selected to convert resins into lower-boiling hydrocarbons.
  • the deasphalted and deresined oil preferably in admixture with the lowerboiling hydrocarbons from the conversion of the resin concentrate, is reacted in a second catalytic reaction zone at hydrocracking conditions selected to produce additional lower-boiling hydrocarbons.
  • deasphalting and deresining designate the separate rejection of an asphaltic pitch and a resin concentrate from the black oil charge stock.
  • the precise nature of these two fractions is widely dependent upon the origin of the crude oil and on the extraction conditions employed.
  • deasphalting generally refers to a one-stage precipitation as applied to an asphalt-containing residuum
  • deresining refers to a similar treatment conducted on an essentially asphalt-free residuum. Accordingly, deasphalting and deresining apply to the rejection of two contiguous bottoms fractions regardless of their exact nature.
  • Deasphalting and deresining are carried out under the same general range of operating conditions.
  • a preferred technique involves operating the deresining zone at a higher temperature than the deasphalting zone, about 10F. to about 200F. higher, in order to recover the resin concentrate with the deasphalted oil, while rejecting an asphaltic pitch.
  • the solvent extraction zones will function at temperatures in the range of about 50F. to about 600F., and preferably from about F. to about 400F.; the pressure will be maintained within the range of about 100 to about 1,000 psig., and preferably from about 200 to about 600 psig.
  • the solvent/oil volumetric ratio will generally be in the range of about 2.0:1.0 to about 30011.0.
  • the deresining operation will employ a higher temperature and a greater solvent/oil volumetric ratio.
  • deasphalting will be effected at a solvent/oil ratio of 6.0210 and a temperature of 100F. to F.; the deresining zone will utilize a propane/oil ratio of l0.0:1.0 and a temperature of 140F. to about 180F.
  • the rejected asphaltic pitch has an average molecular weight in the range of 3,000 to 6,000, and will contain 75.8 percent to 90.0 percent by weight of the metallic contaminants originally present in the fresh feed charge stock.
  • the sulfur content will be approximately twice that of the charge stock.
  • the resin concentrate will exhibit a significantly lower average molecular weight, about 1,000 to about 4,000, and will contain a minor proportion of metals; the sulfur content will be about one and one-half times that of the charge stock.
  • the precise operating conditions in the solvent extraction zones will generally depend upon the physical characteristics of the feed stock as well as the selected solvent.
  • Suitable solvents include those hereinbefore described with respect to prior art deasphalting techniques.
  • the, solvent will be selected from the group of light hydrocarbons including ethane, methane, propane, butane, isobutane, pentane, isopentane, neopentane, hexane, isohexane, heptane, the mono-olefinic counterparts thereof, etc.
  • the solvent may be a normally liquid naphtha fraction containing hydrocarbons having from about five to about 14 carbon atoms per molecule, and preferably a naphtha distillate having an end boiling point below about 200F.
  • the solvent-rich, normally liquid phase is introduced into a suitable solvent recovery system, the design and operation of which are thoroughly described in the prior art.
  • the convertible resin concentrate is processed in a separate reaction zone at conditions selected to convert the sameinto lower-boiling hydrocarbons.
  • the scheme additionally permits the processing of the deasphalted and deresined oil in the absence of both asphalts and resins and under conditions reflecting greater yields of normally liquid hydrocarbon products.
  • a preferred operating techique involves introducing at least a portion of the converted resin concentrate effluent into the deresining zone for the recovery therein of the lower-boiling products along with the normally liquid deasphalted oil. The mixture is then separately processed in a second hydrocracking and/or hydrotreating reaction zone.
  • the catalytic composites disposed within the first and second reaction zones, may be of different physical and chemical characteristics in many instances, suchis not an essential feature of my invention, and the catalytic composites may, therefore, be identical.
  • the catalytic composites utilized in the present combination process comprise metallic components selected from the metals of Groups Vl-B and VIII of the Periodic Table, as well as compounds thereof.
  • suitable metallic components are those selected from the group consisting of chromium, molybdenum, tungsten, iron, ruthenium, osmium, cobalt, rhodium, iridium, nickel, palladium, and platinum.
  • catalytic composites especially for utilization in the conversion of exceedingly high sulfur content feed stocks, are improved through the incorporation of a zinc, tin and/or bismuth component.
  • the latter three metallic components are more advantageously utilized, in the present invention, as part of the catalytic composite selected to process the resin concentrate.
  • the utilization of the term component when referring to the catalytically active metal, or metals, is intended to encompass the existence of the metal as a compound, such as oxide, sulfide, etc., or in the elemental state. Regardless, the concentrations of metallic components are calculated as if the metal existed within the composite in theelemental state. While neither the precise composition, nor the method of manufacturing the various catalytic composites, is considered essential to my invention, certain aspects are preferred.
  • the charge stock to the present process is generally of a high-boiling nature, it is preferred that the catalytically active metallic components possess the propensity for effecting hydrocracking reactions while simultaneously promoting the conversion of sulfurous compounds into hydrogen sulfide and hydrocarbons.
  • concentration of the active metallic component, or components is primarily depended upon the particular metal as well as the physical and/or chemical characteristics of the charge stocks.
  • the metallic components of Group Vl-B are generally present in an amount within the range of about 4.0 percent to about 30.0 percent by weight, the iron-group metals in an amount within the range of about 0.2 percent to about 10.0 percent by weight, whereas the noble metals of Group VIII are preferably present in an amount within the range of about 0.1 percent to about 5.0 percent by weight.
  • a zinc, tin and/or bismuth component is employed, the same will generally be present in an amount within the range of about 0.01 percent to about 2.0 percent by weight. All concentrations are computed as if the metallic components existed within the catalytic composite in the elemental state.
  • the porous carrier material comprises a refractory inorganic oxide of the character thoroughly described in the literature.
  • alumina or alumina in combination with about 10.0 percent to about 10.0 percent to about 90.0 percent by weight of silica is preferred.
  • a carrier material comprising a crystalline aluminosilicate, or zeolitic molecular sieve.
  • a carrier material will;b e utilized in processing the deasphalted oil admixture with the resin concentrate effluent.
  • Suitable zeolitic material includes mordenite, faujasite, Type A or Type U molecular sieves, etc., and these may be employed in a substantially pure state; however, it is understood that the zeolitic material may be included within an amorphous matrix such as silica, alumina, and mixtures of alumina and silica.
  • the catalytic composites may have incorporated therein a halogen component, such component being selected from the group consisting of fluorine, chlorine, iodine, bromine, and mixtures thereof.
  • the halogen, component will be composited with the carrier materialin such a manner as-results in a final catalytic composite containing from about 0.1 percent to about 2.0 percent by weight, again calculated as the element.
  • a particularly preferred catalytic composite, for utilization in the first reaction zone processing the resin concentrate, is that described in U. S. Pat. No. 3,640,817 (Class 208 -59). Briefly, this catalytic composite is described as having more than 50.0 percent of the macropore volume characterized by pores having pore diameters greater than about 1,000 Angstroms. This catalytic composite will contain, in addition to alumina and silica, boron phosphate in theamount of about 5.0 percent to about 30.0 percent by weight.
  • the metallic components may be incorporated within the catalytic composite in any suitable manner including co-precipitation or cogellation with the carrier material, ion-exchange or impregnation of the carrier material, or during a co-extrusion procedure.
  • the catalytic composite is dried and subjected to a high temperature calcination or oxidation technique at a temperature of about 750F. to about 1,300F.
  • the upper limit for the calcination technique is preferably about 1,000F.
  • the second reaction zone will generally function at operating conditions providing a greater severity of operation, although such technique is not necessarily essential.
  • the variance in operating severity between the two reaction zones may be obtained by the adjustment of the pressure, maximum catalyst bed temperature and liquid hourly space velocities.
  • the higher severity operation within the second reaction zone will normally be effected at an increased pressure, an increased maximum catalyst bed temperature and at a somewhat decreased liquid hourly space velocity, or some combination thereof.
  • the pressure will generally be within the range of about 200 to about 3,000 psig.
  • the hydrogen concentration will be about 500 to about 30,000 scf./Bbl.
  • the maximum catalyst bed temperature will range from about 600F. to about 900F.
  • the liquid hourly space velocity will vary from about 0.25 to about 2.50.
  • Preferred operating techniques dictate that the increased temperature gradient be limited to a maximum of about 100F., and, in order to control the temperature gradient, it is within the scope of the present invention to employ quench streams, either normally liquid, or normally gaseous, introduced at one or more intermediate loci of the catalyst bed.
  • the vacuum bottoms charge stock in an amount of about 100,000 Bbl./day, is introduced, via line 1, into deasphalter 2, wherein it countercurrently contacts a pentane solvent being introduced via line 3.
  • the solvent to charge stock volumetric ratio is 3.0 and a liquid-phase operation is maintained in deasphalter 2 at a temperature of 295F. and a pressure of 400 psig.
  • An asphaltic pitch in an amount of about 14.92 percent by weight is withdrawn as a solvent-lean phase in line 4, while a deasphalted oil, containing a resin concentrate, is removed via line 5.
  • the deasphalted oil having a gravity of about 13.3 API, and containing 50.0 ppm.
  • deresinator 7 by weight of metals, is introduced into deresinator 7 in admixture with a resin concentrate effluent from line 6, the source of which is hereinafter described. Additional pentane solvent, added to give a volumetric ratio to the deasphalted oil of 6.0, is introduced via line 8, and the deresinator is maintained at a temperature of 320F. and a pressure of about 400 psig.
  • a solvent-lean resin concentrate in an amount of about 27,000 BbL/day, is withdrawn by way of line 9, and introduced thereby into fixed-bed reactor 10.
  • the resin concentrate is admixed with hydrogen in an amount of about 7,500 scf./Bbl., and the mixture enters reactor 10 at a temperature of 700F. (the increasing temperature gradient is maintained at 50F.) and a pressure of about 3,000 psig.; the liquid hourly space velocity, based only a fresh feed exclusive of liquid recycle, is 0.5.
  • Reactor 10 contains a catalytic composite similar to that described in the previously mentioned U.S. Pat. No. 3,640,817 (Class 208-59).
  • the catalyst is a composite of 66.90 percent by weight alumina, 7.90 percent silica, 7.20 percent boron phosphate, 2.0 percent nickel and 16.0 percent by weight of molybdenum.
  • Product yields and component distribution of the resin concentrate product effluent are presented in the following Table I:
  • metal-containing resins are removed, via line 11, in an amount of about 7.46 percentby weight of the fresh vacuum bottoms feed.
  • the deasphalted oil, inclusive of the 21,338 BbL/day of the 650F.-PLUS resin concentrate effluent is removed by way of line 12, and introduced thereby, in the total amount of 81,338 BbL/day into reactor 13.
  • Reactor 13 contains a catalytic composite of 1.9 percent by weight of nickel and 14.0 percent by weight of molybdenum combined with an amorphous carrier material of 33.0 percent by weight of silica and 67.0 percent by weight of alumina.
  • the charge to reactor 13 has a gravity of 16.9 API, a sulfur content of 2.01 percent by weight, a nitrogen content of 2,900 ppm. and contains only 3.0 ppm. of metal contaminants.
  • the feed is admixed with about 13,000 scf./Bbl. of hydrogen and contacts the catalyst at a liquid hourly space velocity of 0.35.
  • the maximum catalyst bed temperature is controlled at 775F., and the pressure is maintained at a level of 3,000 psig.
  • That portion of the normally liquid product effluent boiling above 700F. is recycled to reactor 13 to provide a combined liquid feed ratio of 1:11.
  • the remainder is sent via line 14 to suitable separation facilities for recovery of various product streams. Yields and component distribution of the effluent from reactor 13 are presented in the following Table 11:
  • TOTALS 102.30 102,289 Based upon 100,000 BbL/day fresh feed It will be immediately noted that the present combination process produces a 102.3 percent volumetric yield of normally liquid hydrocarbons, based upon the quality of fresh feed charge stock, notwithstanding the by-product production of 14.92 percent of weight of the asphaltic pitch and 7.46 percent by weight of the heavy metallic resins both of which may be used in road asphalt. Analyses indicate that all treams are substantially sulfur-free and that the heptane-350F. stream, having a gravity of about 55.0 API, contains 7.0 percent aromatics, 60.0 percent naphthenes and 33.0 percent paraffins. As will be recognized, this constitutes an excellent feed stock for a catalytic reforming unit.
  • a process for the conversion of an asphaltenecontaining hydrocarbonaceous charge stock, to produce lower-boiling hydrocarbon products comprises the steps of:
  • the hydrocracking conditions, in said first and second reaction zones include a pressure from about 500 to about 5,000 psig., a hydrogen concentration in the range of about 1,000 to about 30,000 scf./Bbl., a liquid hourly space velocity of from about 0.25 to about 2.50 and a maximum catalyst bed temperature in the range of 600F. to about 900F.

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  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
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US00277025A 1972-08-01 1972-08-01 Combination process for the conversion of hydrocarbonaceous black oil Expired - Lifetime US3775292A (en)

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Cited By (22)

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US4062758A (en) * 1975-09-05 1977-12-13 Shell Oil Company Process for the conversion of hydrocarbons in atmospheric crude residue
US4125459A (en) * 1977-03-28 1978-11-14 Kerr-Mcgee Refining Corporation Hydrocarbon solvent treatment of bituminous materials
US4126538A (en) * 1976-09-22 1978-11-21 Shell Oil Company Process for the conversion of hydrocarbons
US4155833A (en) * 1978-01-30 1979-05-22 Energy Modification, Inc. Separation of true asphaltenes from microcrystalline waxes
US4239616A (en) * 1979-07-23 1980-12-16 Kerr-Mcgee Refining Corporation Solvent deasphalting
US4305814A (en) * 1980-06-30 1981-12-15 Kerr-Mcgee Refining Corporation Energy efficient process for separating hydrocarbonaceous materials into various fractions
US4391700A (en) * 1980-04-21 1983-07-05 Institut Francais Du Petrole Process for converting heavy hydrocarbon oils, containing asphaltenes, to lighter fractions
US4405441A (en) * 1982-09-30 1983-09-20 Shell Oil Company Process for the preparation of hydrocarbon oil distillates
US4440633A (en) * 1981-04-30 1984-04-03 Institut Francais Du Petrole Process for solvent deasphalting heavy hydrocarbon fractions
US4454023A (en) * 1983-03-23 1984-06-12 Alberta Oil Sands Technology & Research Authority Process for upgrading a heavy viscous hydrocarbon
US4686028A (en) * 1985-04-05 1987-08-11 Driesen Roger P Van Upgrading of high boiling hydrocarbons
US4747936A (en) * 1986-12-29 1988-05-31 Uop Inc. Deasphalting and demetallizing heavy oils
US6533925B1 (en) 2000-08-22 2003-03-18 Texaco Development Corporation Asphalt and resin production to integration of solvent deasphalting and gasification
US20040084351A1 (en) * 2001-02-20 2004-05-06 Yoshinori Mashiko Method of refining heavy oil and refining apparatus
US20090057195A1 (en) * 2005-12-16 2009-03-05 Christopher Alan Powers Systems and Methods for Producing a Crude Product
US20090301931A1 (en) * 2006-10-20 2009-12-10 Omer Refa Koseoglu Asphalt production from solvent deasphalting bottoms
US20100122934A1 (en) * 2008-11-15 2010-05-20 Haizmann Robert S Integrated Solvent Deasphalting and Slurry Hydrocracking Process
US20100243518A1 (en) * 2009-03-25 2010-09-30 Zimmerman Paul R Deasphalting of Gas Oil from Slurry Hydrocracking
KR101186726B1 (ko) 2003-12-23 2012-09-28 아이에프피 에너지스 누벨 수지 제거를 포함하는 탄화수소 공급원료의 처리 방법
WO2013019687A1 (en) * 2011-07-29 2013-02-07 Foster Wheeler Usa Corporation Integration of solvent deasphalting with resin hydroprocessing
WO2013142313A1 (en) * 2012-03-19 2013-09-26 Foster Wheeler Usa Corporation Integration of solvent deasphalting with resin hydroprocessing and with delayed coking
US9493710B2 (en) 2011-07-29 2016-11-15 Saudi Arabian Oil Company Process for stabilization of heavy hydrocarbons

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NL8105660A (nl) * 1981-12-16 1983-07-18 Shell Int Research Werkwijze voor de bereiding van koolwaterstofoliedestillaten.
NL8201119A (nl) * 1982-03-18 1983-10-17 Shell Int Research Werkwijze voor de bereiding van koolwaterstofoliedestillaten.
JPH0676585B2 (ja) * 1982-12-28 1994-09-28 三菱化成株式会社 溶剤精製炭の水素化方法
NL8301352A (nl) * 1983-04-18 1984-11-16 Shell Int Research Werkwijze voor de bereiding van asfaltenenarme koolwaterstofmengsels.
MX164713B (es) * 1983-12-07 1992-09-18 Mexicano Inst Petrol Un metodo para procesamiento de crudos pesados

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US2914457A (en) * 1957-06-28 1959-11-24 Texaco Inc Petroleum refining process
US2973313A (en) * 1957-05-13 1961-02-28 Texaco Inc Treatment of deasphalted oil and asphalt to make reformed gasoline
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US2002004A (en) * 1933-08-07 1935-05-21 Union Oil Co Process for treating oil
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US2973313A (en) * 1957-05-13 1961-02-28 Texaco Inc Treatment of deasphalted oil and asphalt to make reformed gasoline
US2914457A (en) * 1957-06-28 1959-11-24 Texaco Inc Petroleum refining process
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Cited By (31)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4062758A (en) * 1975-09-05 1977-12-13 Shell Oil Company Process for the conversion of hydrocarbons in atmospheric crude residue
US4126538A (en) * 1976-09-22 1978-11-21 Shell Oil Company Process for the conversion of hydrocarbons
US4125459A (en) * 1977-03-28 1978-11-14 Kerr-Mcgee Refining Corporation Hydrocarbon solvent treatment of bituminous materials
US4155833A (en) * 1978-01-30 1979-05-22 Energy Modification, Inc. Separation of true asphaltenes from microcrystalline waxes
US4239616A (en) * 1979-07-23 1980-12-16 Kerr-Mcgee Refining Corporation Solvent deasphalting
US4391700A (en) * 1980-04-21 1983-07-05 Institut Francais Du Petrole Process for converting heavy hydrocarbon oils, containing asphaltenes, to lighter fractions
US4305814A (en) * 1980-06-30 1981-12-15 Kerr-Mcgee Refining Corporation Energy efficient process for separating hydrocarbonaceous materials into various fractions
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JPS5213524B2 (enrdf_load_stackoverflow) 1977-04-15
FR2194766B1 (enrdf_load_stackoverflow) 1976-05-07
GB1440363A (en) 1976-06-23
JPS49132101A (enrdf_load_stackoverflow) 1974-12-18
FR2194766A1 (enrdf_load_stackoverflow) 1974-03-01
DE2338385B2 (de) 1976-02-12
CA997700A (en) 1976-09-28
IT990112B (it) 1975-06-20
ES417444A1 (es) 1976-03-01

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