US3925190A - Preheating oil shale prior to pyrolysis thereof - Google Patents

Preheating oil shale prior to pyrolysis thereof Download PDF

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Publication number
US3925190A
US3925190A US492447A US49244774A US3925190A US 3925190 A US3925190 A US 3925190A US 492447 A US492447 A US 492447A US 49244774 A US49244774 A US 49244774A US 3925190 A US3925190 A US 3925190A
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United States
Prior art keywords
oil shale
flue gas
dilute phase
phase fluidized
fluidized bed
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Expired - Lifetime
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US492447A
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English (en)
Inventor
John A Whitcombe
Zanten Kenneth D Van
George C Kane
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Oil Shale Corp
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Oil Shale Corp
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Publication date
Application filed by Oil Shale Corp filed Critical Oil Shale Corp
Priority to US492447A priority Critical patent/US3925190A/en
Priority to AU82956/75A priority patent/AU489796B2/en
Priority to DE2532778A priority patent/DE2532778C3/de
Priority to ZA00754711A priority patent/ZA754711B/xx
Priority to IL47785A priority patent/IL47785A/en
Priority to CA232,140A priority patent/CA1046442A/en
Priority to GB31239/75A priority patent/GB1491363A/en
Priority to IT50693/75A priority patent/IT1041050B/it
Priority to BR7504829*A priority patent/BR7504829A/pt
Priority to FR7523689A priority patent/FR2280701A1/fr
Priority to IN1492/CAL/75A priority patent/IN144101B/en
Priority to SU752171405A priority patent/SU862835A3/ru
Application granted granted Critical
Publication of US3925190A publication Critical patent/US3925190A/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
    • C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
    • C10G1/02—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by distillation
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S208/00—Mineral oils: processes and products
    • Y10S208/951—Solid feed treatment with a gas other than air, hydrogen or steam

Definitions

  • the process herein described is an improvement in the oil shale preheating procedure disclosed in the above-cited prior art patents which utilizes the residual sensible heat of the flue gases previously employed in the process to heat the heat-carrying bodies.
  • U.S. Pat. No. 3,265,608 the transfer of heat from the hot flue gases to the crushed shale is accomplished by entraining the shale with flue gases heated to about 1100F in a gas lift line, i.e., dilute phase fluidized bed. The shale is thereby preheated to a temperature of about 300F.
  • the raw shale and hot flue gases pass co-currently up the lift line during the heat transfer operation.
  • the partially cooled flue gas is separated from the shale and vented to the atmosphere at a temperature substantially higher than the temperature to which the raw shale is preheated prior to being pyrolyzed. While this preheat procedure conserves a portion of the waste heat contained in the ball heater flue gas, it has not been completely satisfactory when utilized to achieve higher levels of preheating, that is, above about 300F to 400F. While the method of preheating shale is not described in detail in U.S. Pat. No. 3,691,056, the process herein described may be used to advantage to obtain high levels of preheat.
  • a primary object of the present invention to provide a process for preheating crushed oil shale prior to the retorting thereof in a pyrolysis Zone without significantly effecting premature pyrolysis of a majority of the oil shale prior to the retorting operation.
  • a further object of the invention is to provide a process for recovering the heating value of oil shale fines and pyrolyzing the remaining portion of crushed oil 2 shale so as to recover substantially 100% of the hydrocarbons contained in the oil shale.
  • a still further object of the invention is to provide for combusting oil shale fines which essentially eliminates the fines as a potential source of hydrocarbon emissions.
  • Another object of the present invention is to provide a process for preheating oil shale prior to the pyrolysis thereof which will efficiently recover a substantial portion of the heating value of the hydrocarbons generated during the preheat operation as fuel within the preheat system and thereby minimize the emission of hydrocarbons to the atmosphere.
  • the preheat procedure of this invention provides for a gradual heating of the oil shale through the use of a series of dilute phase fluidized beds which are each operated at different flue gas temperatures.
  • Dilute phase fluidized beds are used to obtain rapid heat transfer from flue gas to a solid with a fairly wide range of particle size distribution. Because of this range of particle size, the finer particles are heated much more rapidly than the larger particles. For this reason, it is important to control the flue gas temperature at the inlet to the lift line to minimize premature pyrolysis and hydrocarbon generation. It has been found that the major portion of the hydrocarbons evolved during the preheat operation occurs when the shale (Green River Formation) is heated to temperatures in excess of 350F.
  • hydrocarbon concentrations in the flue gas discharged to the atmosphere have been shown to be less than ppm.
  • hydrocarbon concentrations in the flue gas are generally in the order of 500 to 1000 ppm. These higher concentrations are caused by partial pyrolysis of the kerogen in addition to vaporization of the bitumen. From an environmental standpoint, the emission of excessive amounts of hydrocarbons is undesirable.
  • Tests which are described in greater detail below, indicate that as much as 5 to 15% of heat required to preheat oil shale from ambient temperature to about 550F can be supplied by the oil shale fines and hydrocarbons evolved during the preheat operation.
  • this process provides for a gradual preheating of the whole oil shale to a temperature of about 350F without the generation of significant concentrations of hydrocarbons, the further preheating of the whole oil shale to between 400F and 650F with the attendant generation of hydrocarbons, and the recovery of the heating value of these evolved hydrocarbons as well as the heating value of oil shale fines which are entrained in the flue gas.
  • the preheat procedures of this invention utilize the final stage of dilute phase fluidized bed preheating to generate hydrocarbons and entrain these hydrocarbons, together with the oil shale fines, in the flue gas stream which is then passed to an incineration zone wherein the heating value of these materials is recovered.
  • the evolved hydrocarbons and the entrained oil shale fines can be efficiently burned at temperatures between about 1300F and 1500F. Higher temperatures could be utilized if increased levels of carbonate decomposition can be tolerated. It has also been found that virtually complete incineration can be accomplished in about 0.3 second to 1.0 second at these temperatures.
  • the hot flue gas from the incineration zone is partially cooled by conventional heat recovery techniques and is used to preheat cooler raw shale in upstream (shale side) preheat stages.
  • the temperature of the flue gas which contacts the oil shale in the upstream preheat stages must be low enough, usually less than about 800F to 900F, to avoid generating and discharging significant amounts of hydrocarbons to the atmosphere.
  • Two stages of preheat with one intermediate flue gas incineration and reheating operation adequately accomplish the objectives discussed above; however, three stages of preheat utilizing a single flue gas incineration zone located between the second and third stages are preferred.
  • Two interstage incineration zones may also be advantageously utilized wherein one incineration zone is located between the first and second preheat zones and the other incineration zone is located between the second and third preheat zones.
  • Oil shale crushed to nominal /2-inch size is fed from the crusher and introduced into a first dilute phase fluidized bed preheat zone wherein the shale is contacted with flue gas at a temperature sufficient to partially preheat the shale and remove the free moisture.
  • the flue gas discharged from this first stage is passed to the atmosphere after passing through a dust removal apparatus, such as a bag filter, electrostatic precipitator, web scrubber, or the like.
  • a dust removal apparatus such as a bag filter, electrostatic precipitator, web scrubber, or the like.
  • the oil shale is heated to increasingly higher temperatures by contacting the shale with hotter flue gases from the heat-carrying body reheating zone.
  • the preheated oil shale from the final preheat zone is passed to the pyrolysis zone.
  • the partially cooled flue gases from the preheat zones located downstream (gas side) of the final preheat zone are passed through one or more interstage incineration zones wherein the flue gases are reheated by incinerating a mixture of fuel, entrained hydrocarbons and raw shale fines.
  • Temperature control of the flue gases fed to the various preheat zones may be accomplished by blending additional cool, fresh air or flue gas with the primary hot flue gas stream or by passing the flue gases through heat exchangers.
  • the process hereinafter described in connection with the accompanying drawing utilizes a combination of three dilute phase fluidized bed preheat zones with one interstage incineration zone located between the second and third (final) preheat zones to preheat oil shale from about 50F to a temperature of about 500F to 600F prior to the pyrolysis thereof.
  • the drawing is a process flow diagram of the preferred embodiment of the invention described in combination with the pyrolysis process described in the above-cited US. Pat. No. 3,265,608.
  • the oil shale is preheated to about 200F while being transported to accumulator 17 and cyclone separator 18 wherein oil shale particles are separated from flue gas.
  • the partially preheated oil shale is then transferred by gravity feed to the second preheat zone 12 via lines 19 and 20 at a rate of about 450 tons per hour to be further preheated therein.
  • the flue gas having a temperature of about 225F from cyclone separator 18 and containing oil shale dust and water is passed through a wet scrubber (not shown) and then vented to the atmosphere at a low temperature of about F.
  • Approximately 30 gallons per minute of water are removed from the shale in this first preheat zone 10 which do not have to be carried through the downstream preheating and retorting zones and ultimately removed from the oil product.
  • the oil shale is further preheated to about 350F while being transported by hot flue gas having an entry temperature of about 800F.
  • the hot flue gas in the second preheat zone 12 is fed thereto via line 21 and consists of the flue gas from the third preheat zone 22 having an exit gas temperature of about 575F which is fed via line 23 to interstage incinerator-recuperator 24 wherein it is reheated to a temperature of about 1400F by the combustion of hydrocarbons evolved during the final preheat operation, oil shale fines, and supplementary fuel.
  • the 1400F flue gas is cooled in a heat recovery zone 24 d to about 800F before it enters the second preheat zone 12.
  • the shale is separated from the flue gas in accumulator 25 and cyclone separator 26 and fed via lines 27 and 28 to the third preheat zone 22. Some additional water vapor is removed in the second preheat zone 12.
  • the partially preheated oil shale at about 350F is introduced into the third preheat zone 22 wherein it is contacted and transported by flue gas introduced at about 1200F to about 1400F vialine 29 so as to uniformly preheat the entire raw shale stream to about 550F without effecting significant pyrolysis thereof prior to the retorting in pyrolyzer 30.
  • the flue gas to the final preheat zone 22 comprises a blend of the ball heater flue gas fed via line 15 which may be cooled if necessary for process control purposes by adding quench air at about 100F to 120F via line 31.
  • the preheated oil shale is separated from the flue gas in accumulator 32 and cyclone separator 33 and thereafter fed to the retort via lines 34 and 35 wherein the pyrolysis of the oil shale is effected by contact with hot ceramic bodies fed from the ball heater 14 via line 36.
  • the incinerator-recuperator 24 generally comprises a combustion zone 24 a in which air and fuel are burned, a mixing zone 24 b in which the flue gas from line 23 is mixed with combustion products from zone 24 a, an incineration zone 24 0 wherein the oil shale fines and hydrocarbons from the third preheat stage 22 are incinerated, and a heat recovery zone 24 d for cooling the flue gas to about 800F prior to exiting via line 21.
  • the heat recovery zone 24 d may incorporate conventional air heat exchangers and/or waste heat boilers for steam generation.
  • ceramic balls are introduced from ball elevator 37 via line 38 into the heating chamber 39 wherein the balls are contacted with hot flue gas from a combustion chamber 40.
  • Air and fuel are supplied via lines 41 and 42, respectively, to an atomizing type burner (not shown) located in the combustion chamber wherein the mixture is burned to provide hot flue gas.
  • the ceramic balls and flue gas are cocurrently drawn downward through the ball heater, the balls are heated while the flue gas is cooled.
  • the hot flue gas is withdrawn from the ball heater 14 via disengaging zone 43 and line 44 for use in the raw shale preheat zone 22.
  • the heated balls are withdrawn from ball heating zone 39 via line 36 and fed to pyrolyzer 30.
  • the hot ceramic balls from the ball heater 14 are contacted with the raw shale preheated to about 550F to effect the pyrolysis thereof.
  • the balls and oil shale pass co-currently through the pyrolyzer 30 where the heat of the balls is imparted to the oil shale with the production of an effluent hydrocarbonaceous shale oil vapor and processed shale solids.
  • the effluent vapor, processed shale solids and cooled balls exit from pyrolysis drum 30 through tunnel 45 and pass to a rotating trommel screen 46 having openings therein such that the comminuted processed shale solids pass through while the passage of the large size balls is precluded.
  • the effluent vapor is removed from vapor dome 47 and passed via line 48 to a recovery section (not shown). Substantially all the processed shale solids pass through trommel screen 46 and into processed shale solids accumulator 49 from which they are removed via line 50 and passed to a processed shale solids disposal area. Cooled balls are removed from accumulator 51 by means of line 52,
  • the temperatures of the various flue gas and solid streams are exemplary of one set of preheat conditions that have been found to be desirable when processing a specific type and grade of oil shale. These conditions have been found applicable to oil shale from the Mahogany Zone of the Piceance Basin located in northwestern Colorado. Mahogany Zone oil shale usually contains 30 to 40 gallons of recoverable liquid hydrocarbons per ton of ore processed. If either lower or higher grades of oil shale are processed, the flue gas and solids temperatures in each of the respective lift lines may have to be altered in order to optimize the system.
  • Tests have been performed at a plant capable of processing 1000 tons per day of Mahogany Zone oil shale to determine the amount of hydrocarbons generated under specified preheat conditions for each of the three stages of preheat. From these tests, it has been determined that in preheating oil shale (crushed to minus /2- inch) from 50F to 500F in a threestage system, an average of 400 to 700 ppm of hydrocarbons is generated. Of this amount, 400 to 500 ppm of hydrocarbons are generated in the final stage of preheat, and to ppm of hydrocarbons are generated in the first two stages.
  • the lift lines were operated at flue gas inlet temperatures of approximately 500F, 900F and 1000F, respectively, while the shale was heated to successively higher temperatures of approximately 200F, 350F, and 500F, respectively, in each of the three stages of preheat.
  • Table 2 presents an average particle size analysis of oil shale fines which entered the incineration zone from the third preheat stage.
  • Table 3 presents analyses of the organic carbon content of oil shale fines which were obtained from isokinetic samples taken at the inlet and outlet of the combustion chamber while operating an incineration zone at temperatures in the range of from 1330F to I425 F.
  • the process provides a procedure for retorting or pyrolyzing oil shale which utilizes the whole shale, including the fine material, to recover substantially 100% of the recoverable hydrocarbons either as a liquid and gaseous product or as fuel in the preheat system.
  • the process provides for the preheating of raw oil shale to temperatures in the order of 400F to 650F without significantly effecting pyrolysis of a major portion of the shale 8 prior to the retorting or pyrolysis operation.
  • the process provides increased heat economy by discharging low temperature, rather than high temperature, flue gas to the atmosphere.
  • the process in addition, provides for substantial elimination of hydrocarbon emissions by combusting hydrocarbon vapors that are derived primarily by vaporization of bitumen contained in the shale.
  • the use of a single preheat lift line to obtain these higher preheat temperatures is not practical because the fresh raw shale would be contacted by high temperature flue gases, i.e., l200F to 1400F which would result in severe hydrocarbon emissions.
  • the flue gas discharge temperature would necessarily be in the order of 600F, and would obviously contain substantial amounts of unburned hydrocarbons.
  • a process for preheating oil shale to a temperature in the order of 400F to 650F prior to the pyrolysis thereof in a retort which comprises heating the oil shale in a series of at least two dilute phase fluidized beds by entraining partially preheated oil shale in the final dilute phase fluidized bed with hot flue gas to provide oil shale preheated to between about 400F and 650F for introduction into the retort and partially cooled flue gas containing entrained oil shale fines and hydrocarbon vapors, passing the partially cooled flue gas through an incineration zone and incinerating in the presence of combustion products the entrained oil shale fines and hydrocarbon vapors emanating from the final dilute phase fluidized bed to provide a portion of the fuel requirement to reheat the flue gas, cooling the flue gas from the incineration zone and entraining crushed raw oil shale in a first dilute phase fluidized bed with the cooled flue gas
  • the proces as defined in claim 5 comprising the further steps of passing the partially cooled flue gas from the second dilute phase fluidized bed through a second incineration zone so as to partially reheat the flue gas and combust entrained hydrocarbon vapors and oil shale fines emanating from the dilute phase fluheated to a temperature of about 350F. idized beds downstream of the first dilute phase fluid- 8.
  • the process as defined in claim 1 wherein the resiized bed prior to cooling and introducing the partially dence time of the flue gas in the incineration zone is bereheated flue gas into the first dilute phase fluidized 5 tween about 0.5 second and 1.0 second at an incinerabed. tion zone temperature of between about 1400F and 7.
  • the process as defined in claim 1 wherein the oil about l500F. shale feed to the final dilute phase fluidized bed is prea

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Wood Science & Technology (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
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US492447A 1974-07-29 1974-07-29 Preheating oil shale prior to pyrolysis thereof Expired - Lifetime US3925190A (en)

Priority Applications (12)

Application Number Priority Date Filing Date Title
US492447A US3925190A (en) 1974-07-29 1974-07-29 Preheating oil shale prior to pyrolysis thereof
AU82956/75A AU489796B2 (en) 1974-07-29 1975-07-11 Preheating oil shale prior to pyrolysis thereof
DE2532778A DE2532778C3 (de) 1974-07-29 1975-07-22 Verfahren zum Vorwärmen von ölschiefer vor dessen Pyrolyse
ZA00754711A ZA754711B (en) 1974-07-29 1975-07-22 Preheating oil shale prior to pyrolysis thereof
CA232,140A CA1046442A (en) 1974-07-29 1975-07-24 Preheating oil shale prior to pyrolysis thereof
IL47785A IL47785A (en) 1974-07-29 1975-07-24 Process for preheating oil shale prior to pyrolysis thereof
GB31239/75A GB1491363A (en) 1974-07-29 1975-07-25 Preheating oil shale prior to pyrolysis thereof
IT50693/75A IT1041050B (it) 1974-07-29 1975-07-28 Procedimento per il preriscaldamento di scisto oleoso
BR7504829*A BR7504829A (pt) 1974-07-29 1975-07-28 Processo para preaquecer xisto oleifero antes da pirolise do mesmo
FR7523689A FR2280701A1 (fr) 1974-07-29 1975-07-29 Prechauffage du schiste bitumineux avant pyrolyse
IN1492/CAL/75A IN144101B (de) 1974-07-29 1975-07-29
SU752171405A SU862835A3 (ru) 1974-07-29 1975-09-15 Способ предварительного нагрева горючего сланца

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BR (1) BR7504829A (de)
CA (1) CA1046442A (de)
DE (1) DE2532778C3 (de)
FR (1) FR2280701A1 (de)
GB (1) GB1491363A (de)
IL (1) IL47785A (de)
IN (1) IN144101B (de)
IT (1) IT1041050B (de)
SU (1) SU862835A3 (de)
ZA (1) ZA754711B (de)

Cited By (17)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4105536A (en) * 1976-04-23 1978-08-08 Morrell Jacque C Processes including the production of non-congealing shale oil from oil shales
US4153533A (en) * 1977-09-07 1979-05-08 Kirkbride Chalmer G Shale conversion process
US4180385A (en) * 1976-11-30 1979-12-25 Chikul Olga S Fuel composition and process for producing same
US4191630A (en) * 1976-04-23 1980-03-04 Morrell Jacque C Process for the production of shale oil from oil shales
US4226699A (en) * 1978-07-17 1980-10-07 Tosco Corporation Method and apparatus for conservation of heat from sludge produced by a retort
US4374017A (en) * 1980-10-24 1983-02-15 Tosco Corporation Heat flux control technique
US4384947A (en) * 1981-08-10 1983-05-24 Tosco Corporation Preheating of oil shale prior to pyrolysis
US4404083A (en) * 1981-08-17 1983-09-13 Standard Oil Company(Indiana) Fluid bed retorting process and system
US4408656A (en) * 1981-09-03 1983-10-11 Octave Levenspiel Countercurrent heat exchanger for two streams of solids using heat pipes
US4445976A (en) * 1981-10-13 1984-05-01 Tosco Corporation Method of entrained flow drying
US4544478A (en) * 1982-09-03 1985-10-01 Chevron Research Company Process for pyrolyzing hydrocarbonaceous solids to recover volatile hydrocarbons
US4563264A (en) * 1983-02-22 1986-01-07 Metallgesellschaft Aktiengesellschaft Method of dry distillation of volatile substances from mineral matter containing same
US4659456A (en) * 1983-07-01 1987-04-21 Metallgesellschaft Ag Process of drying and heating oil-containing solids
US20040144405A1 (en) * 2001-05-02 2004-07-29 Garrick David Stephen Apparatus and method
US20140000535A1 (en) * 2011-03-17 2014-01-02 Robert Millner Metallurgical plant with efficient waste-heat utilization
EP2585556A4 (de) * 2010-06-22 2016-10-05 Univ Curtin Tech Verfahren und system zur schleifungspyrolyse eines partikelförmigen kohlenstoffhaltigen rohmaterials
CN112210396A (zh) * 2020-11-30 2021-01-12 辽宁石油化工大学 多孔介质外热过滤式油页岩干馏炉

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB2129010B (en) * 1982-10-21 1987-03-04 Shell Int Research Combustion of coke present on solid particles

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US3008894A (en) * 1958-05-20 1961-11-14 Oil Shale Corp Method and apparatus for producing oil from solids
US3020209A (en) * 1958-10-20 1962-02-06 Oil Shale Corp Plant and process for the production of oil
US3058903A (en) * 1959-06-15 1962-10-16 Oil Shale Corp Plant and process for the production of oil from oil shale and the like
US3164541A (en) * 1960-08-08 1965-01-05 Oil Shale Corp Transport of balls by oil
US3265608A (en) * 1962-02-02 1966-08-09 Technikoil Inc Method for pyrolyzing solid carbonaceous materials
US3617468A (en) * 1968-12-06 1971-11-02 Atlantic Richfield Co Process for removing the hydrocarbon content of carbonaceous materials
US3803022A (en) * 1972-12-26 1974-04-09 Atlantic Richfield Co Retorting system

Patent Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3008894A (en) * 1958-05-20 1961-11-14 Oil Shale Corp Method and apparatus for producing oil from solids
US3020209A (en) * 1958-10-20 1962-02-06 Oil Shale Corp Plant and process for the production of oil
US3058903A (en) * 1959-06-15 1962-10-16 Oil Shale Corp Plant and process for the production of oil from oil shale and the like
US3164541A (en) * 1960-08-08 1965-01-05 Oil Shale Corp Transport of balls by oil
US3265608A (en) * 1962-02-02 1966-08-09 Technikoil Inc Method for pyrolyzing solid carbonaceous materials
US3617468A (en) * 1968-12-06 1971-11-02 Atlantic Richfield Co Process for removing the hydrocarbon content of carbonaceous materials
US3803022A (en) * 1972-12-26 1974-04-09 Atlantic Richfield Co Retorting system

Cited By (20)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4105536A (en) * 1976-04-23 1978-08-08 Morrell Jacque C Processes including the production of non-congealing shale oil from oil shales
US4161441A (en) * 1976-04-23 1979-07-17 Morrell Jacque C Process for the production of distillate fuels from oil shales and by-product therefrom
US4191630A (en) * 1976-04-23 1980-03-04 Morrell Jacque C Process for the production of shale oil from oil shales
US4180385A (en) * 1976-11-30 1979-12-25 Chikul Olga S Fuel composition and process for producing same
US4153533A (en) * 1977-09-07 1979-05-08 Kirkbride Chalmer G Shale conversion process
US4226699A (en) * 1978-07-17 1980-10-07 Tosco Corporation Method and apparatus for conservation of heat from sludge produced by a retort
US4374017A (en) * 1980-10-24 1983-02-15 Tosco Corporation Heat flux control technique
US4384947A (en) * 1981-08-10 1983-05-24 Tosco Corporation Preheating of oil shale prior to pyrolysis
US4404083A (en) * 1981-08-17 1983-09-13 Standard Oil Company(Indiana) Fluid bed retorting process and system
US4408656A (en) * 1981-09-03 1983-10-11 Octave Levenspiel Countercurrent heat exchanger for two streams of solids using heat pipes
US4445976A (en) * 1981-10-13 1984-05-01 Tosco Corporation Method of entrained flow drying
US4544478A (en) * 1982-09-03 1985-10-01 Chevron Research Company Process for pyrolyzing hydrocarbonaceous solids to recover volatile hydrocarbons
US4563264A (en) * 1983-02-22 1986-01-07 Metallgesellschaft Aktiengesellschaft Method of dry distillation of volatile substances from mineral matter containing same
US4659456A (en) * 1983-07-01 1987-04-21 Metallgesellschaft Ag Process of drying and heating oil-containing solids
US20040144405A1 (en) * 2001-05-02 2004-07-29 Garrick David Stephen Apparatus and method
EP2585556A4 (de) * 2010-06-22 2016-10-05 Univ Curtin Tech Verfahren und system zur schleifungspyrolyse eines partikelförmigen kohlenstoffhaltigen rohmaterials
US9994774B2 (en) 2010-06-22 2018-06-12 Curtin University Of Technology Method of and system for grinding pyrolysis of particulate carbonaceous feedstock
US20140000535A1 (en) * 2011-03-17 2014-01-02 Robert Millner Metallurgical plant with efficient waste-heat utilization
CN112210396A (zh) * 2020-11-30 2021-01-12 辽宁石油化工大学 多孔介质外热过滤式油页岩干馏炉
CN112210396B (zh) * 2020-11-30 2022-02-15 辽宁石油化工大学 多孔介质外热过滤式油页岩干馏炉

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DE2532778A1 (de) 1976-02-19
BR7504829A (pt) 1976-07-06
AU8295675A (en) 1977-01-13
IN144101B (de) 1978-03-25
DE2532778B2 (de) 1979-04-19
FR2280701A1 (fr) 1976-02-27
CA1046442A (en) 1979-01-16
ZA754711B (en) 1976-06-30
DE2532778C3 (de) 1979-12-20
SU862835A3 (ru) 1981-09-07
IL47785A0 (en) 1975-10-15
GB1491363A (en) 1977-11-09
IT1041050B (it) 1980-01-10
FR2280701B1 (de) 1979-06-15
IL47785A (en) 1977-12-30

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