Abstract: Described herein are integrated thermochemical processes for the deliberate decomposition, extraction and conversion of coal into high-value products and goods via solvent extraction, chemical reaction and/or separation. The described systems and methods are versatile and may be used to generate a variety of intermediate, derivative and finished high value products including chemicals (aromatics, asphaltenes, naphthalenes, phenols and precursors for the production of polyamides, polyurethanes, polyesters, graphitic materials), polymer composite products (resins, paints, coatings, adhesives), agricultural materials, building materials, carbon fiber, graphene products and other materials that are substantially more valuable that the energy generated via combustion.

Abstract: A method of producing hydrocarbons from a subterranean reservoir comprises pre-heating by exposure to electromagnetic radiation from a electromagnetic radiation source, injecting through at least one injection well a solvent into the reservoir to dilute the hydrocarbons contained in the pre-conditioned portion, and producing through at least one production well a mixture of hydrocarbons and solvent. An apparatus for producing hydrocarbons from a subterranean reservoir comprises at least one radio frequency antenna configured to transmit radio frequency energy into a subterranean reservoir, a power source to provide power to the at least one radio frequency antenna, at least one injection well configured to inject a solvent from a solvent supply source into the subterranean reservoir to lower the viscosity of the hydrocarbons, and at least one production well configured to produce a mixture comprising hydrocarbons and solvent from the subterranean reservoir.

Abstract: A coal processing method includes adding coal powder, water and catalyst into a series of tandem reactors and processing therein, wherein the coal powder, water and catalyst are added into the first reactor of the series of tandem reactors; and the temperature and pressure of the series reactors is alternatively arranged in sub-critical state and supercritical state of water from the first reactor, the total product from the previous reactor is used as the feed of the next reactor without any further separation.

Abstract: Use of chemical pretreatment agents on the subsequent enzymatic conversion of coal is described. As an example, fungal manganese peroxidase (MnP) produced by the agaric white-rot fungus Bjerkandera adusta, where the enzyme MnP has little effect on the untreated coal controls, was investigated. The nature of pretreatment agents and their applied concentrations were found to have significant impact on subsequent enzymatic conversion of coal. Four agents were investigated: HNO3, catalyzed H2O2, KMnO4, and NaOH. Hydrogen peroxide was found to generate the greatest quantity of total organic carbon from the coal samples employed. Combined chemical and enzymatic treatment of coal is appropriate for enhanced depolymerisation of coal and coal-derived constituents and results in chemically heterogeneous and complex liquefaction products like humic and fulvic acids, which will have important ramifications in the generation of liquid and gaseous fuels from coals as nonpetroleum-derived fuel alternatives.

Abstract: Methods for extracting bitumen from bituminous material through the use of a polar solvent. The method may include a primary leaching or extraction process that separates most of the bitumen from a material comprising bitumen and produces first solvent-wet tailings. A polar solvent is added to the first solvent-wet tailings in order to remove the first solvent (plus any entrained bitumen) from the tailings. A mixture of polar solvent and first solvent produced by the addition of the polar solvent to the first solvent-wet tailings may be phase separated by maintaining the polar solvent-first solvent mixture for a period of time. Alternatively, the polar solvent and first solvent may leave the tailings in a phase separated state. Phase separation may occur due to the presence of water in the polar solvent-first solvent mixture. Water may also be added to the mixture of solvents to serve as an antisolvent and initiate phase separation. The separated solvents may then be recovered and reused in the method.

Abstract: A method for treating an organic waste, in which the organic waste is pressurized and continuously supplied to a high temperature and pressure treatment apparatus to produce a slurried material by blowing steam into the organic waste to cause a reaction while heating, pressurizing and agitating. The slurried material is dehydrated to produce a separated liquid product and a separated solid product. The separated solid product includes sufficient combustible content to produce a fuel product. The separated liquid product is purified.

Abstract: A method and system for extracting hydrocarbon products from waste tailings of a froth flotation unit and a paraffinic froth treatment process are provided. Bitumen and asphaltenes from the waste tailings are extracted using a serial addition of an aromatic solvent, followed by a polar-non-polar solvent. The method and system divert valuable hydrocarbons from tailings ponds. The hydrocarbon product can be used as a coating material or an emulsion fuel, for example.

Abstract: A method and apparatus for removing and recovering oil from wellbore cuttings is provided. Oil-contaminated solids are transported through two or more solvent baths on vibrating conveyors and contacted with solvent flowing countercurrent to the direction of transport of the oil-contaminated solids through the baths such that oil contaminant is separated from the solids.

Abstract: In treatment equipment of organic waste provided with a high temperature and pressure treatment apparatus to produce a slurried material by conducting the high temperature and high pressure treatment of the organic waste, a dehydration treatment apparatus to recover the dehydrated solid matter by conducting the dehydration treatment of the slurried material and a water treatment apparatus to conduct the purification treatment of a separated liquid separated by the dehydration treatment apparatus, the treatment equipment of organic waste is characterized by having a crusher to crush said organic waste before conducting the high pressure and temperature treatment and providing to said high temperature and pressure treatment apparatus a steam blowing means to blow steam into the organic waste in said high temperature and pressure treatment apparatus, wherein said high temperature and pressure treatment apparatus is formed as a continuous reaction tank to which the organic waste is continuously supplied and to wh

Abstract: A method for producing synthetical oils and storable products of calorific energy, by co-processing waste rubber materials, especially waste tires, and coal optionally in the presence of a material containing Fe as a catalyst, comprising the steps of mixing triturated waste rubber material having a particle size of preferredly 1-5 mm, and coal having particle sizes of 0.2-1 mm, and, when used, the catalyst having a referred particle size of 0.05-0.015 mm, until obtaining a mixture, heating the mixture in a reactor to a temperature between 300.degree. C. and 500.degree. C., during 3-180 minutes, at a pressure between atmospheric pressure and 10 MPa, to enable a processing step basically consisting of a pyrolysis/hydropyrolysis. During the processing step, there is a generation of gases containing approximately 50% CO and CO.sub.2, and approximately another 50% by volume of C.sub.1 -C.sub.4 hydrocarbons, and having a calorific energy between 6000 and 8000 kcal/Nm.sup.

Abstract: An improved process for extracting hydrocarbons from a diatomite ore which comprises the combination of the steps of:a) Reducing the particle size of the ore to form a processed ore;b) Grinding the processed ore in an enclosed pin mixer to form pelletized ore;c) Feeding the pellets into each section of a ROTOCEL.RTM. extractor unit containing 5-8 sections or baskets to form columns of pelletized ore;d) Distributing a solvent from the top of each column of the ROTOCEL.RTM. extractor and allowing the solvent to permeate the pelletized ore column to form a hydrocarbon-rich solvent stream while leaving behind spent ore mixture;e) Separating extracting solvent from the hydrocarbon solvent stream to form a hydrocarbon product stream and an extracting solvent stream;f) Removing the spent ore mixture from the extracting zone;g) Recycling the extracting solvent; andh) Recovering the hydrocarbon product.

Abstract: In a process for producing distillates from coal by a first stage thermal liquefaction followed by a catalytic hydrogenation, liquefaction solvent is added at points spaced over the length of the thermal liquefaction heater.Coal may be co-processed with petroleum oil by adding pre-hydrogenated oil to the first stage or unhydrogenated oil to the second stage.

Abstract: In a process for reducing the sulfur and ash contents of coal, coal is sequentially contacted with fused alkali metal caustic, water, carbonic acid, and a strong acid. Caustic removed from the coal by the water and the carbonic acid is recovered as anhydrous caustic for again contacting coal.

Abstract: I disclose a method for upgrading low-grade uintaite to high-grade uintaite having a desired meltpoint. It comprises dissolving the uintaite in a medium polarity solvent, mixing the dissolved uintaite with a nonpolar saturated hydrocarbon solvent at a volume-to-volume ratio that determines the meltpoint of the upgraded uintaite product, separating residual asphaltenes from the mixture, and recovering the medium polarity solvent and nonpolar saturated hydrocarbon to produce an upgraded uintaite having the desired meltpoint.

Abstract: In a coal liquefaction process an aqueous slurry of coal is prepared containing a dissolved liquefaction catalyst. A small quantity of oil is added to the slurry and then coal-oil agglomerates are prepared by agitation of the slurry at atmospheric pressure. The resulting mixture is drained of excess water and dried at atmospheric pressure leaving catalyst deposited on the agglomerates. The agglomerates then are fed to an extrusion device where they are formed into a continuous ribbon of extrudate and fed into a hydrogenation reactor at elevated pressure and temperature. The catalytic hydrogenation converts the extrudate primarily to liquid hydrocarbons in the reactor. The liquid drained in recovering the agglomerates is recycled.

Abstract: An improved method of recovering oil from diatomite is described. A solvent is injected into the diatomite followed by an aqueous surface active solution. The aqueous surface active solution contains a diatomite/oil water wettability improving agent and an oil/water surface tension lowering agent. The method may be supplemented by injection of water and/or steam into the diatomite.

Abstract: Hydrocarbon liquids are recovered from oil shale and other solids containing organic material by heating the solids to a temperature below about 900.degree. F., preferably between about 550.degree. F. and about 900.degree. F., in the absence of an added liquid organic solvent and then contacting the heated solids with a liquid organic solvent in such a manner that the solids and solvent do not form a slurry and under conditions such that hydrocarbons are extracted from the heated solids into the organic solvent. The extracted hydrocarbons are then recovered from the solvent by fractionation. Normally, the solids will be heated by contacting them with a hot, monoxidizing gas, preferably an oxygen-free flue gas generated within the process.

Abstract: An improved tar sands derived bitumen and coal liquification process is disclosed wherein substantial percentages of subdivided coal particles and tar sands derived bitumen liquids are mixed and then corefined with hydrogen under hydrocracking conditions, but in the absence of a separate catalyst, at a temperature range of 800.degree. to 900.degree. F. and a pressure of about 2400 psig. The resutling fluid after removal of residual solids is a suitable liquid feedstock for conventional refinery equipment to produce petroleum fractions useful as transportation and heating fuels. Preferably, a portion of the corefined bitumen-coal liquid product may be recycled for mixture with the bitumen liquid and coal. Raw or native tar sands may also be mixed with the liquid butumen and coal in the process.

Abstract: The present invention relates to a novel method for improving the recovery of hydrocarbon fluids from oil shale. The method comprises treating a mixture of oil shale and hydrocarbon fluid at a temperature below the retorting temperature of the shale and for a period of time sufficient to recover product hydrocarbon fluids in amount equivalent to at least 100 percent Fischer Assay.

Abstract: Hydrocarbon liquids are recovered from oil shale and other solids containing organic material by heating the solids to a temperature below about 900.degree. F., preferably between about 550.degree. F. and about 900.degree. F., in the absence of an added liquid organic solvent and then contacting the heated solids with a liquid organic solvent in such a manner that the solids and solvent do not form a slurry and under conditions such that hydrocarbons are extracted from the heated solids into the organic solvent. The extracted hydrocarbons are then recovered from the solvent by fractionation. Normally, the solids will be heated by contacting them with a hot, nonoxidizing gas, preferably an oxygen-free flue gas generated within the process.

Abstract: A multi-stage coal liquefaction method in which coal is slurried with a primary light solvent, such as toluene, hexane and/or cyclohexane, and a process-derived primary heavy solvent. The coal-primary solvent slurry is treated under coal-liquefying conditions to form a first feed solution containing coal liquefaction products. The first feed solution is treated by a multi-stage supercritical solvent extraction procedure. The final heavy phase produced by this procedure is mixed with a secondary solvent, such as pentane, to produce a second feed mixture, which is treated in a second multi-stage supercritical solvent extraction procedure. Heavy phases recovered from the separate stages of both solvent extraction procedures are blended to provide a recycled primary heavy solvent.

Abstract: A process for the production of reformer feed and heating or diesel oil from coal which comprises introducing a pulverized coal-oil slurry together with a hydrogenation gas into a liquid-phase hydrogenation stage; remoping solids-containing residue from the discharge from the liquid phase hydrogenation stage, cooling the resulting residue-free volatile coal-oil fraction from the discharge and, if necessary, removing a slurry oil fraction therefrom before feeding the volatile coal-oil fraction to a gas-phase hydrogenation stage; introducing fresh hydrogen which is substantially free of contaminants into the gas-phase hydrogenation stage together with the volatile coal-oil fraction, the fresh hydrogen introduced into the gas-phase hydrogenation stage constituting the entire amount of hydrogen required for the process; and utilizing the waste-gas from the gas-phase hydrogenation as the hydrogenation gas for the liquid-phase hydrogenation.

Abstract: Disclosed is a process for removing mineral matter from Rundle oil-shale by contacting the oil-shale with (a) an ammonium salt solution and (b) an organic solvent, at a temperature from about 0.degree. C. to about 300.degree. C. for a time which is sufficient to substantially separate at least about 80 wt. % of the carbonate mineral matter from the oil-shale.

Abstract: Disclosed is a process for beneficiating oil-shale wherein the oil-shale is treated in a first stage with an aqueous ammonium salt solution and in a second stage and optionally a third stage in the presence of a solution containing ammonium ions/ammonia, or both. The pH of the first stage is from about 5 to 9, and the pH of the second and third stages are from about 0.5 to 5 or about 9 to 12 with the proviso that the pH of the second and third stage is not in the same range.