US3544448A - Supersonic jet fuel production - Google Patents

Supersonic jet fuel production Download PDF

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US3544448A
US3544448A US791230A US3544448DA US3544448A US 3544448 A US3544448 A US 3544448A US 791230 A US791230 A US 791230A US 3544448D A US3544448D A US 3544448DA US 3544448 A US3544448 A US 3544448A
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reaction zone
temperature
jet fuel
line
jet
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William L Jacobs
Charles H Watkins
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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
    • 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
    • C10G65/04—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including only refining steps
    • C10G65/08—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including only refining steps at least one step being a hydrogenation of the aromatic hydrocarbons
    • 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
    • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
    • C10G2400/08—Jet fuel

Definitions

  • the present multiple-stage process is directed toward the production of supersonic jet ful from a sulfurous, aromatic, higher-boiling charge stock. More specifically, the process encompassed by the present invention afiords the simultaneous production of sonic, or standard jet fuel and supersonic jet fuel. Significantly, the jet fuel kerosene fractions, withdrawn as product streams, seldom requre further treatment in order to conform to the current specifications imposed upon sonic jet fuels, and those contemplated for the supersonics.
  • Suitable charge stocks for utilization as the fresh feed in the present process, are those containing snbstantial quantities of hydrocarbons having norma1 boiling points above about 550 F., whch temperature is generally considered to be the maximum end boiling point of jet fuel kerosene fractions. Therefore, the most common charge stocks Will be vacuum gas oils and/or coker gas oils. It is understood, however, that gas oils resu1ting from a particular prior converson process are also wellsuited. The latter are those vacuum gas oils which are generally derived from the converson of extremely heavy hydrocarbonaceous material commonly referred to in the art as black oils.
  • Exemplary of the hydrocarbonaceous material contemplated for converson into jet fue1 kerosene fractions are a blend of coker gas oil, diesel and light gas oil having a gravity of about 27.4 API, a sulfur concentraton of about 1.36% by weight, an initial boiling point of about 401 F. and an end boiling point of about 866 F.; a Lloydminster heavy gas oil containing about 2.2% by weight of sulfur, 600 p.p.m. of ntrogen, having a gravity of about 21.5 API, an initial boiling point of 610 F.
  • a Wainwright heavy gas oil having a gravity of 23.2 API, a sulfur concentraton of 1.23% by weight, contaim'ng 600 p.p.m. of nitrogen, having an initial boiling point of about 635 F. and an end boiling point of about 862 F.
  • a Redwater heavy gas oil having an initial boiling point of about 635 F., an end boiling point of about 855 F., a gravity of 28.1 API, and containing 0.6% by weight of sulfur and 700 p.p.m. of nitrogen
  • a virgin vacuum gas oil derived from a sonr Wyoming crude oil the properties of which are hereafter set forth in greater detail.
  • gas oil fraetions of the type hereinabove described can be converted into kerosenes having acceptable jet fue1 characteristics.
  • gasolne boiling range hydrocarbons gasolne boiling range hydrocarbons
  • the crtcal properties are generally considered to be a high octane rating, a particularly specified volatlity, a low degree of olefincity, and low concentrations of contaminating influences.
  • many more criteria are employed in descrbng a fuel for jet engines, and even these are further restricted depending upon engine complexity, speed, crusing altitude, distance, etc. Since about 1960, the quality and classfication of jet fuels has generally followed the development of jet engines.
  • specifications for jet fuels of particular physical and/or chemical characteristics have resulted in jet fuels designated as JP-1, IP3, JP-4, JP-5, JP-6, JP-8, Iet-A and Jet A1, etc.
  • Table II Propos ed supersonic jetfuel. property
  • the source of the requirements stated in the foregoing Table II is D. H. Stormont, Oil & Gas Journal, pp. 39- 42 (May 15, 1967 While it appears certain that the overall eflect of the jumbo jets and supersonc jet transports will be to increase the demand for greater quantities of jet fuels, is is not possible to project the exact quantity in terms of millons of barrels per day.
  • the supersonic jet transports displace the standard jet in use today, the demand for standard jet fuel will certainly decrease, althogh the combned demand for both sonic and supersonic jet fuels will certainly increase.
  • the process encornpassed by our invention recognizes that there will be a dramatic need for both the supersonic and sonic jet fuels, and atfords the simultaneous production of both inan economical and relatively facile manner.
  • Ai1other object is to provide a semi-series flow, mul-- tiple-reactionzone process for the production of sonic and supersonic jet fuels.
  • the present invention is drected towrd a process for producng jet fuel kerosene fractions from a sulfurous, aromatic, higher boiling charge stockwhich comprises the steps of (a) reacting said charge stock With hydrogen in a first catalytic reaction zone at a maximum catalyst bed temperature of about 850 F.
  • embodirnents of our invention are directed toward preferred processing techniques, operating conditions and various catalytic composites for utilization in the multiple reaction zones.
  • one technique involves recycling at least a portion of the fifth liquid phase containng hydrocarbons boiling above about 550 F. to the second catalytic reaction zone.
  • the first reaction zone effluent is separated in the hot separator at temperature of from about 550 F. to about 750 F.
  • the preferred catalytic composite disposed within said second catalytic reaction zone comprises a Group VIII noble metal component, and preferably a platnum and/or palladium component.
  • the primary purpose of our invention is to provide a process which aifords the simultaneous production of both sonic and supersonic jet fuels. In etect, this purpose is accomplished through the utilization of a two reaction zone system, utilizing catalytic composites of varying characteristics. Briefly, in the first reaction zone, the catalytic composite and operatng con ditions are selected for complete desulfurization of the Charge stock, whle smultaneously converting heavier hydrocarbons into a 300 F./550 F. standard (sonic) jet fuel and gasoline boiling range hydrocarbons.
  • the product efliuent from the first reaction zone is separated in such a manner to recover the standard jet fuel as a product stream, the heavier portion serving as the charge, in semi-series flow, to the second reaction zone.
  • the primary function of the second reaction zone is to saturate aromaties whle simultaneously cracking the heavy gas oil components into kerosene boiling range hydrocarbons suitable for use as supersonic jet fuelS.
  • the term semi-series flow alludes to the fact that the product efluent from the first catalytic reaction zone is passed, at substantially the same pressure, into the second catalytic reaction zone. In many instances, this charge to the second reaction zone need not be heated, but can be introduced at subst'antially the same temperature it has as it emanates from the first separation zone.
  • the present invention involves the utilization of a first catalytic reaction zone having disposed therein a catalyst comprising a metallic component from Group VI-B and the Iron-Group of the Periodic Table, the primary purpose of which is to elect substantially complete desulfuriza tion of the hydrocarbonaceous feed stock at comparatively mild severities.
  • the catalytic composite utilized in the second reaction zone for the purpose of saturating aromatic hydrocarbons and hydrocrackihg gas oil boilng range material into kerosene fraction components, comprises a Group VIII noble metal component.
  • a hot separator functioning at substantially the same pressure as the first reaction zone and at a temperature in the range of trom about 500 F. to about 800 F., and preferably trom about 550 F. to about 750 F.
  • the liquid phase from the hot separator is introduced into the second catalytic reaction zone, often without substantal change in temperature.
  • the catalytic composites utilizecl in the present process comprise metallic components selected from the metals of the Group VI-B and VIII of the Periodic Table, and compounds thereof.
  • suitable metallic components are those selected from the group consisting of chromimum, molybdenum, tungsten, iron, ruthenium, osmium, cobalt, rhodium, iridium, nickel, palladium and platinum. While neither the precisc composition, nor the method of manufacturing the catalyst is considered essential to our invention, certain aspects are preferred.
  • Suitable catalytic composites for use in electing the desulfurization reactions in the first reaction zone, generally comprise trom about 4.0% to about 40.0% by weight of a Group VI-B metallic component, and from about 1.0% to about 6.0% by weight of an IronGroup metallic component.
  • these concentrations are computed on the basis of the elemental metals, regardless of the precise state in which they exist within the catalytic composite.
  • These catalytically active components are generally composited with a suitable siliceous refractory norganic oxide carrier material, the quantity of silica generally determining the degree of hydrocracking activity.
  • Suitable refractory norganic oxides include alumina, zrconia, magnesa, titania, thoria, boria, hafma, etc.
  • Another group of suitable carrier materials are those having combined therewith from about 5.0% te about 35.0% by weight of boron phosphate.
  • the silica to alumina weight ratio will be within the range of trom about /90 to about 80/20.
  • catalytic components are also combined with one or more of the foregoing refractory norganic oxides, whch, in some instances, may be crystalline aluminosilicates, or zeolitic material.
  • refractory norganic oxides whch, in some instances, may be crystalline aluminosilicates, or zeolitic material.
  • the charge stock for example, a vacuum gas oil derived from a sour Wyoming crude oil, having a sulfur concentration of about 2.42% by weight, an initial boilng point of 540 F. and an end boilng point of 1015 F., containing about 50.5% by weight of aromatic hydrocarbons, is admixed with recycle hydrogen in an amount of about 3,000 to about 20,000 standard cubic feet per barrel.
  • recycle hydrogen in an amount of about 3,000 to about 20,000 standard cubic feet per barrel.
  • the hydrocarbon/hydrogen mixture is heated to a temperature level such that the catalyst bed temperature is controlled within the range of from about 600 to a maximum of 850 F.
  • the catalyst bed inlet temperature is regulated to control the outlet temperature at a maximum level of 850" F., and preferably not higher than 800 F. Since the principal reactions are exothermic in nature, a temperature rise will be experienced as the charge stock passes through the catalyst bed.
  • a particularly preferred technique limits the temperature increase in the first catalytic reaction zone te about F. and the use of conventional quench streams, at one or more intermediate loci of the reaction zone, is contemplated for this purpose.
  • T he reaction zone contains, for example, a catalyst of 1.8% by Weight of nickel and 16.0% by weight of molybdenum combined with a carrier material of 63.0% by weight of alumina and 37.0% by weight of silica.
  • the reaction zone is maintained under an imposed pressure of from about 1000 to about 4000 p.s.i.g., and the liquid hourly space velocity (defined as volumes of liquid hydrocarbon charge per hour per volume of catalyst) is in the range of from about 0.4 to about 3.5.
  • a vaporous phase comprising hydrogen, hydrogen sulfide, ammonia, normally gaseous hydrocarbons, butanes, pentanes and heavier hydrocarbons boiling below about 550
  • the temperature of the stream entering the hot separator is controlled at a level whch insures that substantially all of the standard jet fuel components, for example, boilng trom about 300" F. to about 550 F.
  • a portion of the liquid phase wthdrawn from the hot separator is recycled to combine with the fresh gas oil charge stock to the first reaction zone.
  • This particular technique also affords a certain degree of flexibility with respect to the quantity of standard jet fuel, since the heavier components are once again subjected to an environment conducive in part to hydrocracking.
  • Suitable combined feed ratios defined as volumes of total liquid charge per volume of fresh hydrocarbon charge, are within the range of trom about 1.1 to about 3.5. That portion of the liquid phase not being recycled serves as part of the total liquid charge to the second catalytic reaction zone.
  • the liquid phase from the cold separator is subjected to a product recovery system in order to recover a standard jet fuel fraction.
  • a bottoms fraction, containing those hydrocarbons boilng above the desired end boilng point of the standard jet fuel fraction is combined with the liquid phase from the hot separator and serves as the charge to the second catalytic reaction zone.
  • the catalyst disposed in the second reaction zone is a composite of about 0.4% by weight of platinum, calculated as the element, combined with a refractory inorganic oxide of 75.0% by weight of silica and 25.0% by weight of alumina.
  • the reaction zone is maintained at a pressure above about 1000 p.s.i:g., having an upper limit of about 3000 p.s.i.g.
  • the hydrogen circulation rate is at least about 3000 standard cubic feet per barrel, with an upper limit of about 15,000 standard cubic feet per barrel.
  • the liqud hourly space velocity, previously defined is, within the range of from about 0.5 to about 4.0. It is particularly preferred to mantain the maximum catalyst bed temperature at a level not exceeding 750 F.
  • the inlet temperature of the catalyst bed within the second catalytic reaction zone will be in the range of from about 550 to about 700 F.
  • a temperature rise is experienced as the charge stock passes through thecatalyst bed.
  • the total product effluent from the second catalytic reaction zone is introduced into a second cold separator, at substantially the Same pressure and at a temperature in the range of from about 60 F. to about 140 F.
  • the principally vaporous phase, from the cold separator to which the second catalytic zone eflluent is passed, is substantially clean with respect to hydrogen sulfide.
  • the normally liqud hydrocarbon portion emanating from the second catalytic reaction zone is recovered from the cold separator and introduced into product separatiorr means distinctly separate from the product recovery system utilized with respect to the normally liqud effluent from the first reaction zone.
  • product recovery system utilized with respect to the normally liqud effluent from the first reaction zone.
  • Exemplary of the component separation etfected with respect to the normally liqud product efliuent from the second reaction zone is a normally gaseous stream comprising butanes, lighter hydrocarbons and other gaseous components; a pentane/ hexane fraction which may be utilized as a motor fuel blending component; a heptane to 375 F. motor fuel fraction which may be utilized in combinaton with other similarly constitutcd refinery streams as the charge to a catalytic reforming system; the desired supersonic jet fuel kerosene, for exarnple having a boiling range from 375 F.
  • the drawing is presented for the sole purpose of illustration, and is not intended to be limited to the particular charge stock, quantites, rates, operating conditons, etc., employed by way of explanation.
  • the charge stock for example, the vacuum gas oil derived from a sour Wyoming crude oil, the property inspections of which are presented in the followng Table 111, is introduced into the process by way of line 1.
  • Table III Vacuum gas oil charge properties Gravity, API 21.2 ASTM distillation, F.: IBP 590 90.0% 955 95.0% 985 End point 1015 Sulfur, wt. percent 2.42 Nitrogen, wt. pp. 1300 Bromine number 2.9 ASTM elution, wt. percent:
  • the charge stock continues through line 1, being adrnixed with a recycled hydrogen stream from Iine 2, in an amount of about 6,000 standard cubic feet per barrel.
  • the charge stock rate is about 9,700 barrels per day, and it is intended that this charge stock be convcrted into jet fuels in a yield of about 50.0% by volume. With respect to the indivdual quantites of sonic and supersonic jet fuels, the intended division is approximately 50.0% of each.
  • the charge stock/hydrogen mixture following heat-exchange with relatively hot efiiuent streams, continues through line 1 into heater 4.
  • Heater 4 raises the temperature of the incoming hydrogen/charge stock stream to a level of about 675 F., as measured at the inlet to the catalyst bed disposed within reactor 6.
  • the thus-heated mixture is introduced downflow by way of line 5, and is withdrawn from reactor 6 by way of line 7 at a temperature of about 775 F.
  • the catalyst disposed within reactor 6 is principally a desulfurization catalyst having some hydrocracking activity, and comprises 1.8% by weight of nickel and 16.0% by weight of molybdenum, computed as the elemental metals, combined with a carrier material of 63.0% by weight of alumina and 37.0% by weight of silica.
  • the hot reaction zone effluent in line 7 is utilized as a heat-exchange medium to reduce its temperature to a level of about 600 F. and continues through line 7 into hot separator 8.
  • a first principally vaporous phase, containing substantially al] of the material boiling below a temperature of about 55 F., and substantially free from hydrocarbonaceous material boiling above 550 R, is removed by way of line 9, cooled to a temperature of about 100 F., and introduced into cold separator 10.
  • the second principally vaporous phase is withdrawn frorn cold separator 10, by way of compressive means not illustrated in the drawing, and continues through line 2 to be admixed With the charge stock in line 1.
  • Make-up hydrogen may be introduced fiom any suitable external source, at any suitable location in the process system.
  • the vaporous phase from line 2 may be treated, when necessary, for the removal of gaseons constituents other than hydrogen in order that the hydrogen concentration be about at least 80.0 m01 percent.
  • Such treating facilities are well known in the prior art, and, therefore, are not indicated in the drawing.
  • a first principally liqud phase is withdrawn from hot separator 8 by way of line 18, and serves as a portion of the charge ultimately introduced into reactor 14.
  • the normally liqud hydrocarbon streatn from cold separator 10 is withdrawn by way of line 11 and introduced into fractionator 12.
  • Fractionator 12 functions at conditions of temperature and pressure which provides the standard jet fuel product stream, having an initial boiling point of 300 F. and an end boiling point of 550 F., to be withdrawn by way of line 17.
  • An overhead stream comprising butanes, lighter normally gaseous hydrocarbons and other gaseous material is withdrawn by way of line 15, and may be further separated to recover particularly desred components.
  • gasoline raction is removed from fractionator 12 by way of line 16, and may be utilized, at least in part, in a pool as the charge to a catalytic reformng unit.
  • Hydrocarbonaceous material boiling above the desired end point of the standard jet fuel fracton, 550 F. is withdrawn by way of line 13, and is admixed With the hot separator liqud phase in line 18.
  • the mixture of the material in line 13 and line 18 constitutes the fresh feed to reactor 14, in an amount of: about 5,140 barrels per day.
  • This fresh feed is adrnixed With a recycle stream comprising hydrocarbonaceous material boiling above a temperature of about 530 R, in line 23, the source of which is hereinafter set forth.
  • the quantity of liqud recycle is about 3,084 barrels per day, to provide a com bined liqud feed ratio to reactor 14 of about 1.6.
  • the mixture continues through line 13, is admixed With 8,000 standard cubic feet per barrel of hydrogen from line 23, and is introduced by way of line 13 into reactor 14 at a pressure of about 1,500 p.s.i.g.
  • the catalyst disposed within reactor 14 is the comp0site of about 0.4% by weight of platium, calculated as the elemental metal, combined With a carrier material of 75.0% by weight of silica and 25.0% by weight of alumina, and is employed in an amount such that the liqud hourly space velocity, based upon fresh feed exclusive of recyc1e, is 1.00.
  • the reactor product efiiuent is withdrawn by way of line 19, at a temperature of about 625 R, is cooled to a temperature of about F., and continues through line 19 to cold separtor 20.
  • a third principally vaporous phase is withdrawn from cold separator 20 by way of line 23, the recycle therethrough, by compressive means not illustrated in the drawing, to combine With the fresh feed in line 13.
  • a principally liqud phase consisting prmarily of normally liqud hydrocarbons, is withdrawn from cold separator 20 by way of line 21, and after suitable heat-exchange With hot product effluent streams, is introduced therethrough into fractionator 22.
  • Fractionator 22 is maintained under conditions of temperature and pressure which insures the recovery of the supersonic jet fuel, having an initial boiling point of 375 F. and an end boiling point of about 530 F., by way of line 27. Hydrocarbonaceous material boiling above a temp6rature of about 530 F. is withdrawn from fractionator 22 by way of line 28, and recycled therethrough to combine With the fresh feed in line 13, thereby providing a combned liqud feed ratio of about 1.6. Butanes, lghter normally gaseous hydrocarbons and other gaseous material is withdrawn from fractionator 22 by way of line 24.
  • a pentane/hexane component fraction is removed by way of line 25' and a heavy naphtha, gasoline boiling range material is withdrawn by way of line 26.
  • the latter is indicated as comprisng heptane and hydrocarbons boiling up -to the initia1 boiling point of the supersonic jet fuel, 375 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)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
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BE (1) BE744335A (es)
BR (1) BR7016057D0 (es)
CA (1) CA935111A (es)
CH (1) CH533676A (es)
ES (1) ES375412A1 (es)
FR (1) FR2028389B1 (es)
GB (1) GB1285811A (es)
IL (1) IL33693A (es)
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Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS5034563B1 (es) * 1971-02-20 1975-11-10
US4501653A (en) * 1983-07-22 1985-02-26 Exxon Research & Engineering Co. Production of jet and diesel fuels
US4645585A (en) * 1983-07-15 1987-02-24 The Broken Hill Proprietary Company Limited Production of fuels, particularly jet and diesel fuels, and constituents thereof
US4921595A (en) * 1989-04-24 1990-05-01 Uop Process for refractory compound conversion in a hydrocracker recycle liquid
US6294080B1 (en) 1999-10-21 2001-09-25 Uop Llc Hydrocracking process product recovery method
US6843906B1 (en) 2000-09-08 2005-01-18 Uop Llc Integrated hydrotreating process for the dual production of FCC treated feed and an ultra low sulfur diesel stream
US20070170095A1 (en) * 2001-09-18 2007-07-26 Barry Freel Products produced from rapid thermal processing of heavy hydrocarbon feedstocks
US9707532B1 (en) 2013-03-04 2017-07-18 Ivanhoe Htl Petroleum Ltd. HTL reactor geometry

Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3132087A (en) * 1961-08-30 1964-05-05 Union Oil Co Manufacture of gasoline and jet fuel by hydrocracking

Family Cites Families (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3147210A (en) * 1962-03-19 1964-09-01 Union Oil Co Two stage hydrogenation process
FR1403951A (fr) * 1963-06-13 1965-06-25 Shell Int Research Procédé de conversion d'une huile minérale à point d'ébullition élevé ou d'une fraction de cette huile en essence et carburant d'aviation

Patent Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3132087A (en) * 1961-08-30 1964-05-05 Union Oil Co Manufacture of gasoline and jet fuel by hydrocracking

Cited By (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS5034563B1 (es) * 1971-02-20 1975-11-10
US4645585A (en) * 1983-07-15 1987-02-24 The Broken Hill Proprietary Company Limited Production of fuels, particularly jet and diesel fuels, and constituents thereof
US4501653A (en) * 1983-07-22 1985-02-26 Exxon Research & Engineering Co. Production of jet and diesel fuels
US4921595A (en) * 1989-04-24 1990-05-01 Uop Process for refractory compound conversion in a hydrocracker recycle liquid
US6294080B1 (en) 1999-10-21 2001-09-25 Uop Llc Hydrocracking process product recovery method
US6843906B1 (en) 2000-09-08 2005-01-18 Uop Llc Integrated hydrotreating process for the dual production of FCC treated feed and an ultra low sulfur diesel stream
US9005428B2 (en) 2000-09-18 2015-04-14 Ivanhoe Htl Petroleum Ltd. Products produced from rapid thermal processing of heavy hydrocarbon feedstocks
US20070170095A1 (en) * 2001-09-18 2007-07-26 Barry Freel Products produced from rapid thermal processing of heavy hydrocarbon feedstocks
US8062503B2 (en) * 2001-09-18 2011-11-22 Ivanhoe Energy Inc. Products produced from rapid thermal processing of heavy hydrocarbon feedstocks
US9707532B1 (en) 2013-03-04 2017-07-18 Ivanhoe Htl Petroleum Ltd. HTL reactor geometry

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ES375412A1 (es) 1972-05-16
FR2028389A1 (es) 1970-10-09
NL7000603A (es) 1970-07-17
BR7016057D0 (pt) 1973-05-03
CA935111A (en) 1973-10-09
SE353733B (es) 1973-02-12
NL165211C (nl) 1981-03-16
NL165211B (nl) 1980-10-15
JPS4912323B1 (es) 1974-03-23
GB1285811A (en) 1972-08-16
IL33693A (en) 1973-02-28
FR2028389B1 (es) 1974-03-15
DE2001134A1 (de) 1970-07-23
BE744335A (fr) 1970-06-15
CH533676A (de) 1973-02-15

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