Abstract: The invention provides a pyrolysis reaction system, the system comprising: a pyrolysis chamber comprising a feed inlet, a gas inlet and a product outlet, wherein the pyrolysis chamber is configured i) to receive a pyrolysable organic feed and an inert gas via the feed inlet and gas inlet respectively, ii) to pyrolyse the organic feed at a pyrolysis temperature to produce a carbonaceous pyrolysis product and a pyrolysis gas, wherein the pyrolysis gas will combine with the inert gas to form a gas mixture having a pyrolysis chamber pressure in the pyrolysis chamber, and iii) to discharge the carbonaceous pyrolysis product via the product outlet; a gas reactor configured to react the pyrolysis gas by combustion and/or carbon deposition at a gas reaction temperature and a gas reactor pressure; and a first partition defining a boundary between the pyrolysis chamber and the gas reactor, the first partition comprising a plurality of first apertures to provide fluid communication between the pyrolysis chamber and the

Abstract: The invention provides a pyrolysis reaction system, the system comprising: a pyrolysis chamber comprising a feed inlet, a gas inlet and a product outlet, wherein the pyrolysis chamber is configured i) to receive a pyrolysable organic feed and an inert gas via the feed inlet and gas inlet respectively, ii) to pyrolyse the organic feed at a pyrolysis temperature to produce a carbonaceous pyrolysis product and a pyrolysis gas, wherein the pyrolysis gas will combine with the inert gas to form a gas mixture having a pyrolysis chamber pressure in the pyrolysis chamber, and iii) to discharge the carbonaceous pyrolysis product via the product outlet; a gas reactor configured to react the pyrolysis gas by combustion and/or carbon deposition at a gas reaction temperature and a gas reactor pressure; and a first partition defining a boundary between the pyrolysis chamber and the gas reactor, the first partition comprising a plurality of first apertures to provide fluid communication between the pyrolysis chamber and the

Abstract: A system and method for torrefying a combination of biomass and biochar colloidal dispersion is provided.

Abstract: Continuous charcoal production system in a vertical reactor with a concentric charging zone (1) and drying zone (2), a carbonization zone (3), a cooling zone (4) and a discharge zone (5), and a method for recovering energy from carbonization gases for the production of this charcoal, comprising the extraction of carbonization gas from the drying zone (2) and subdividing it into recirculating gas and heating gas, with the remaining gas exceeding the energy required to generate electricity; burning the heating gas in a hot gas generator (11); injecting the recirculating gas into a heat recovery unit (9); injecting the heating gas after combustion into the heat recovery unit (9), indirect heating of the recirculating gas; and reinjecting the heated recirculating gas into the carbonization zone (3) of the reactor (R).

Abstract: The disclosure provides several pyrolysis reactor configurations and associated methods for generating pyrolysis products (e.g., oil, gas, and/or char) from organic feedstock.

Abstract: A gasifier may include a chamber wall defining a gasification chamber configured to allow gasification of feedstock material. The gasifier may also include an ash grate disposed in the gasification chamber. The gasifier may further include a rotary crusher disposed in the gasification chamber above the ash grate. The rotary crusher may include at least one crushing element. The rotary crusher may be configured to break apart, between the at least one crushing element and an opposing surface, the feedstock material responsive to rotation of the rotary crusher.

Abstract: This invention provides processes and systems for converting biomass into high carbon biogenic reagents that are suitable for a variety of commercial applications. Some embodiments employ pyrolysis in the presence of an inert gas to generate hot pyrolyzed solids, condensable vapors, and non-condensable gases, followed by separation of vapors and gases, and cooling of the hot pyrolyzed solids in the presence of the inert gas. Additives may be introduced during processing or combined with the reagent, or both. The biogenic reagent may include at least 70 wt %, 80 wt %, 90 wt %, 95 wt %, or more total carbon on a dry basis. The biogenic reagent may have an energy content of at least 12,000 Btu/lb, 13,000 Btu/lb, 14,000 Btu/lb, or 14,500 Btu/lb on a dry basis. The biogenic reagent may be formed into fine powders, or structural objects. The structural objects may have a structure and/or strength that derive from the feedstock, heat rate, and additives.

Abstract: This invention provides processes and systems for converting biomass into high-carbon biogenic reagents that are suitable for a variety of commercial applications. Some embodiments employ pyrolysis in the presence of an inert gas to generate hot pyrolyzed solids, condensable vapors, and non-condensable gases, followed by separation of vapors and gases, and cooling of the hot pyrolyzed solids in the presence of the inert gas. Additives may be introduced during processing or combined with the reagent, or both. The biogenic reagent may include at least 70 wt %, 80 wt %, 90 wt %, 95 wt %, or more total carbon on a dry basis. The biogenic reagent may have an energy content of at least 12,000 Btu/lb, 13,000 Btu/lb, 14,000 Btu/lb, or 14,500 Btu/lb on a dry basis. The biogenic reagent may be formed into fine powders, or structural objects. The structural objects may have a structure and/or strength that derive from the feedstock, heat rate, and additives.

Abstract: The present invention concerns a reactor (1) for the gasification of organic material included in composite raw material and the separation of gasified organic material from inorganic material included in the composite raw material, the reactor comprising at least one reaction chamber (2) and at least one rotor (3), said reaction chamber (2) comprising at least one housing (6, 6a, 6b) that is sealed in relation to the surroundings and has at least one inlet opening (8a, 8b, 8c) and at least one outlet opening (9a, 9b) and said rotor (3) comprising at least one shaft (5). Said housing (6, 6a, 6b) is in heat exchanging contact with at least one channel (20) intended to convey gas for heat exchange between the gas and said housing (6, 6a, 6b).

Abstract: A coal gasification process is provided based on the grading conversion of carbon hydrogen components of coal, wherein the coal gasification process comprises a carbonization process, a carbon monoxide-producing process and a shift reaction process. By blending the coke-oven gas, carbon monoxide and hydrogen produced in the above processes in different ratios, coal gasification syngases with various carbon hydrogen ratios can be obtained. Further, the coal gasification process does not need pure oxygen to take part in the reactions, and has several advantages, such as high gasification efficiency, low equipment investment costs, less limitation on the types of coal and flexible adjustment of the gasification products.

Abstract: A thermal reactor for the continuous thermolytic recycling of granules of scrap tires, vulcanization residues and waste plastics, and of similar products features a feed portion, a central heating-zone portion and a discharge portion arranged vertically one below the other. An extraction pipe is located centrally in the central heating-zone portion of the thermal reactor, the lateral surface of the extraction pipe featuring numerous holes and/or slits for withdrawal of the vaporized short-chain hydrocarbon compounds being formed, and the extraction pipe having conical bells pushed onto it one above the other. A device withdraws the vaporized hydrocarbon compounds from the extraction pipe. Radially arranged heating plates are provided on the lateral surface of the reactor in its central heating-zone portion, the heating plates being arranged at the heating levels, which lie one above the other, such that the plates are mutually offset.

Abstract: This invention provides processes and systems for converting biomass into high-carbon biogenic reagents that are suitable for a variety of commercial applications. Some embodiments employ pyrolysis in the presence of an inert gas to generate hot pyrolyzed solids, condensable vapors, and non-condensable gases, followed by separation of vapors and gases, and cooling of the hot pyrolyzed solids in the presence of the inert gas. Additives may be introduced during processing or combined with the reagent, or both. The biogenic reagent may include at least 70 wt %, 80 wt %, 90 wt %, 95 wt %, or more total carbon on a dry basis. The biogenic reagent may have an energy content of at least 12,000 Btu/lb, 13,000 Btu/lb, 14,000 Btu/lb, or 14,500 Btu/lb on a dry basis. The biogenic reagent may be formed into fine powders, or structural objects. The structural objects may have a structure and/or strength that derive from the feedstock, heat rate, and additives.

Abstract: A process for heat treatment of a solid, with a coolant solid, in which a stage for mixing the solid with the pre-heated coolant solid is carried out, with the coolant solid being a solid hydrocarbon. The solid hydrocarbon is ground, before the mixing stage with the solid, to obtain a solid hydrocarbon powder with a grain size of between 20 ?m and 300 ?m. The solid is ground, before the mixing stage with the coolant solid, to obtain solid pellets with a thickness of between 1 mm and 30 mm, a width of between 1 mm and 40 mm, and a length of between 1 mm and 100 mm. The mixing is carried out at a temperature of between 80° C. and 700° C.

Abstract: A fast pyrolizer includes an elongated tubular housing having a feed inlet to receive material, an outlet, and a flow path. The flow path has an internal contact surface extending from the inlet to the outlet. The inlet is to be oriented to a non-vertical relative elevation with respect to the outlet. At least a portion of the internal contact surface directly contacts the material. A heater heats the internal contact surface such that the material is heated via direct thermal transfer from the internal contact surface.

Abstract: A method for torrefaction of lignocellulosic biomass comprising: continuously feeding the biomass to an upper inlet to the torrefaction reactor vessel such that the biomass material is deposited on an upper tray assembly of tray assemblies stacked vertically within the reactor; as the biomass moves over each tray assembly, heating and drying the biomass material with a non-oxidizing gas under a pressure of at least 3 bar gauge and at a temperature of at least 200° C.; cascading the biomass down through the trays by passing the biomass through an opening in each of the trays to deposit the biomass on the tray of the next lower tray assembly; discharging torrefied biomass from a lower outlet of the torrefaction reactor, and circulating gas extracted from the reactor vessel back to the reactor.

Abstract: Apparatus for the manufacture of charcoal, comprising a unit having walls defining a primary combustion chamber, and a material inlet for allowing a feed of wood chips though said material inlet into said apparatus. A trough is located at a lower height than said material inlet such that material passing through said material inlet is able to fall into the trough. An air inlet is located below the material inlet such that, when wood chips are located within the trough piled up to said material inlet, air passing from said air inlet passes through said wood-chips and into the primary combustion chamber.

Abstract: A system for producing petroleum products from oil shale includes one or plural kiln lines made up of plural series-connected, indirect-fired, inclined rotary kilns. Plural kiln lines are operated for parallel processing. Oil shale is advanced through kilns in succession and exhausted from each kiln line substantially free of hydrocarbons. Successive kilns along the advancement of oil shale are maintained at successively higher temperatures. A fuel distinct from hydrocarbons in oil shale, such as syngas from a gasifier or hydrogen gas from a separator, drives pyrolysis to extract hydrocarbons. A refining unit located proximate to the kiln lines upgrades extracted hydrocarbons into petroleum products and separates the petroleum products by criteria. A heat extraction unit recovers heat from exhausted oil shale for reuse in kilns. A method involves drying oil shale followed by heating dry oil shale in successively hotter pyrolysis environments.

Abstract: Closed apparatus and processes by which carbon feedstock is composed of a mixture of non-coking coal fines and another carbonaceous material, such as waste coke fines, are described. The coal and coke fines are mixed together and may be formed into solid pieces. The mixture alone or as solid pieces is fired through pyrolyzation into solid pieces of coke, with solid and gaseous by-products of pyrolyzation being recycled for use within the coke-producing closed system, thereby reducing or eliminating release of undesirable substances to the environment. A char-forming binder may or may not be added to the carbon mixture prior to pyrolyzation.

Abstract: A retort heating apparatus for processing a feed material includes a heating chamber bounded at least in part by a side wall. A plurality of baffles are at least partially disposed within the heating chamber. Each baffle includes an elongated body having a top surface, at least a portion of the top surface being arched. The plurality of baffles are vertically and horizontally spaced apart so that substantially all of the feed material that vertically passes through the heating chamber is horizontally displaced as the feed material passes by the baffles. Systems are also provided for heating the feed material within the heating chamber.

Abstract: Apparatus for the pyrolysis of solid waste material includes a thermal reactor including an elongate hollow housing with a reaction chamber disposed within the housing. The thermal reactor is vertically oriented in order to cause solid waste material fed thereinto to pass through said reaction chamber by the force of gravity and a plurality of vanes are disposed for both conducting heat into said reactor chamber and for tumbling said solid waste material as said solid waste material passes through said reaction chamber. Inlets and outlets are provided for passing oxygen transversely through the reaction chamber.

Abstract: The biomass, particularly lump wood, is supplied to a shaft reactor at its top and is initially preheated to temperatures of about 150.degree. to 280.degree. C. and dried by a counterflowing hot gas. This is followed by a treatment in an underlying carbonizing zone, the upper portion of which is supplied with hot purging gas at a temperature of 250.degree. to 600.degree. C. The hot purging gas flows downwardly through the carbonizing zone co-currently with the wood. A gas mixture which contains purging gas and gas produced by carbonization is withdrawn from the lower portion of the carbonizing zone and is at least in part combusted outside the shaft reactor to produce a combustion gas, which is used at least in part as hot purging gas.

Abstract: An improved process for producing a formed activated coke for simultaneous desulfurization and denitrification, which includes passing a ground coal through a tubular or cylindrical carbonization retort by using a hot gas stream, to subject the coal to preliminary carbonization to obtain a semi-coke, adding a caking agent to the semi-coke and forming the mixture, subjecting the formed material to carbonization to obtain a formed coke, and transferring the formed coke from the top to the bottom of a vertical multi-tubular retort of indirect heating and cooling (cooling is optional) type that includes a distribution section, a heating section, an activation section and a cooling section (the distribution section and the cooling section are optional) arranged in this order (the distribution section is at the top), to activate the formed coke.

Abstract: A preferred embodiment of the apparatus 10 for recycling used automobile rubber tires is described in which small pieces of rubber tires are progressively fed into a vertical reactor 14 of the counter-flow type in which the material progressively descends downward through the reactor 14 with process gases passing upward through the downwardly descending material to decompose and volatilize the rubber material. Oxygen-bearing gas is injected into the reactor to burn a portion of the rubber carbon to generate hot combustion gases that ascend upwardly to pyrolitically decompose the rubber pieces, and to volatilize such material. The amount of oxygen is controlled in an oxygen-deficient manner to maintain the temperature in the combustion zone at a temperature of less than 500.degree. F. The gases and volatilized rubber materials and oils are removed from the reactor at a temperature of approximately 350.degree. F.

Abstract: Apparatus for the production of charcoal by the comingling of a source of wood and ground sludge where the sludge is received from a paper making plant as wet sludge, grinding the wet sludge to a desired reduction, feeding the ground sludge into a furnace where it is comingled with wood, and circulating the furnace hot gas exhaust back through the grinding of the wet sludge to initiate the drying thereof.

Abstract: An improve gasification system, in which synthesis gas is produced through the operation of a fuel gas production bed comprising an upper layer (66) of organic input material, typically in the form of pellets or briquettes of substantially uniform size and configuration which in one embodiment includes toxic waste material, two intermediate layers, one intermediate layer (70) for carbonizing the input material, and the other intermediate layer (72) for partially oxidizing and substantially completely pyrolyzing the input material and a lower layer (68) of tar-free charcoal. The length of the gas production bed from the top of the upper intermediate layer to the point where gas exits from the gas production bed is approximately at least 1.5 times the diameter of the bed, but not less than 7 feet. The residence time of the input material in the intermediate layers and the lower layers is such that activated carbon may be produced and/or the toxic waste input destroyed.

Abstract: An apparatus for removing oil, gas and by-products from pyrobituminous shale impregnated with hydrocarbons utilizes a vertically disposed reactor having a top portion, a middle portion and a bottom portion. As shale is introduced into the top portion of the reactor through a rotary seal mechanism, hot gasses are introduced into the middle portion of the reactor through hollow, parallel tubes having a hexagonal configuration with gas introducing holes disposed in the side walls which are protected by overhanging portions of the top walls. Relatively cool gasses are introduced into the bottom portion of the reactor through horizontally disposed circumferentially spaced pipes having downwardly and outwardly chamfered inner ends to prevent clogging of the pipes. The hot effluent gasses from the top portion of the reactor are passed through the cyclone, a heat regenerator for reducing the temperature of the gaseous stream and an electrostatic precipitator prior to being compressed.

Abstract: Apparatus is described for the pyrolysis of coal comprising a pyrolysis tower through which crushed coal and hot gas are counter-currently passed. The tower enables a controlled temperature profile to be maintained in the tower, and contains inner appurtenances which define cascading passageways to promote heat exchange and mixing of the coal with the hot gas. The coal volatiles are carried out of the top of the tower by the gas. The pyrolysis tower may be conjoined with a gasifier so as to most directly utilize the char residuals remaining after pyrolysis of the coal while they are still hot to more efficiently produce a hot synthesis gas, to be used to perform thermal pyrolysis in the tower.

Abstract: The friability of green needle coke is reduced by heating the green needle coke to a temperature between about 875.degree. F. and about 1,200.degree. F. for a time sufficient to reduce the friability of the green needle coke.

Abstract: Lump wood is carbonized in a shaft retort, which is flown through by hot rinse gas. The wood is charged to the retort at its top. Wood charcoal is withdrawn from the lower portion of the retort. An exhaust gas which contains gases and vapors produced by carbonization is withdrawn from the top end of the shaft retort and is directly fed to a combustion chamber. In a first section of the combustion chamber, the exhaust gas is combusted with air at an understoichiometric to stoichiometric rate at temperatures from 800.degree. to 1250.degree. C. Part of the combustion gas is withdrawn from that first section of the combustion chamber and is cooled to temperatures from about 450.degree. to 900.degree. C. and is fed as a rinse gas to the shaft retort. In a second section of the combustion chamber, the exhaust gas is completely combusted with air supplied at an overstoichiometric rate.

Abstract: An improved gasification system, in which synthesis gas is produced through the operation of a fuel gas production bed comprising an upper layer (66) of organic input material, typically in the form of pellets or briquettes of substantially uniform size and configuration, two intermediate layers, one intermediate layer (70) for carbonizing the input material, and the other intermediate layer (72) for partially oxidizing and substantially completely pyrolyzing the input material and a lower layer (68) of tar-free charcoal. The length of the gas production bed from the top of the upper intermediate layer to the point where gas exits from the gas production bed is approximately at least 1.5 times the diameter of the bed, but not less than 7 feet. The removal of charcoal from the gas production bed is controlled and the operation of the bed otherwise controlled such that the charcoal produced during the process is activated carbon.

Abstract: An apparatus and process for producing coke in a vertical furnace having an upper part for preheating and devolitalizing raw ovoids of coal, an electrically heated median part for carbonizing and coking the ovoids and a lower part for partially cooling the coked ovoids by counter current flow of recycled product gases recovered from the upper part of the furnace. A cooling chamber is connected to the lower part of the furnace for further cooling the coked ovoids by countercurrent flow of a portion of the recycled product gases which are withdrawn after flowing through the partially cooled coked ovoids and introduced into the upper part of the furnace to prevent condensation of condensibles contained in the product gases. The median part of the furnace may be electrically heated by electrodes, induction coils or a combination of electrodes and induction coils.

Abstract: Active form coke is made from coal by passing the coal granulate downwardly through a preheating and pyrolysis zone, a heating zone, an aftertreatment zone and a cooling zone by moving respective grate bars of grates in each zone so that a bed of granules on one grate trickles uniformly onto the next lower grate. In the preheating, heating and aftertreatment zone CO.sub.2 or steam are passed through the beds by laterally introducing the gas at one side and withdrawing the gas on the opposite side of a respective bed.

Abstract: An internally-fired vertical shaft kiln for calcining coke wherein a downwardly moving coke bed has a co-current preheat gas stream in the upper portion of the kiln and a counter-current combustion gas stream in the lower portion of the kiln. Both gases are removed at the midportion of the kiln. Combustion air is introduced to the kiln through an inclined grate at the bottom of the kiln which retains a layer of coke thereon for internal combustion. The calcined coke moves over the combusting coke layer on the grate and then through a passage to a cooling chamber where a gas stream is passed through the calcined coke for cooling. The gas stream heated in the cooling chamber can be used as the co-current gas preheat stream in the upper section of the kiln.

Abstract: A device for and method of working up etching and pickling liquids consisting of a vertical furnace having one or more vertical reaction spaces through which balls move at a maximum packing density.The furnace has a temperature gradient from the bottom (high) to the top (low). The reaction space and the balls consist of a material which is inert with respect to the liquid to be worked up. The liquid is introduced into the upper side of the furnace so that a film is formed in the heated surface of the balls. The salt dissolved in the liquid decomposes pyrolytically. The metal oxide is deposited on the surface of the balls and is removed therefrom after leaving the reaction space. The acid residue vapours are drained at the top and recovered in a separate absorber to the original pickling or etching acid.

Abstract: A process for the destructive distillation of hydrocarbonaceous solids in a retort, wherein a viscous bridging zone comprising viscous liquids in intimate contact with solids, which tends to impede the flow of vaporized hydrocarbons and the flow of solid particles, is agitated by reciprocating mechanical means actuated by a rotatable crankshaft.

Abstract: Slugs (4) of products dehydrated by compression are thrust into the tube (11) up to the hearth (15). The hot gases from the hearth passing round the tube (11) heat it up in order to release the gases and carbonize the solids which burn in the form of coke in the bottom (16) of the hearth. Household refuse may thus be eliminated not only without expense but with recovery of energy from it.

Abstract: A cascading bed retorting process and apparatus in which cold raw crushed shale enters at the middle of a retort column into a mixer stage where it is rapidly mixed with hot recycled shale and thereby heated to pyrolysis temperature. The heated mixture then passes through a pyrolyzer stage where it resides for a sufficient time for complete pyrolysis to occur. The spent shale from the pyrolyzer is recirculated through a burner stage where the residual char is burned to heat the shale which then enters the mixer stage.

Abstract: Hydrogen sulfide issuing from an oil shale retort is captured in an absorbent bed. When the bed is regenerated as with oxygen containing gas, the sulfur dioxide liberated is reintroduced into the retort for reaction with the spent shale.

Abstract: Oil shale is well mixed and efficiently, effectively, and economically retorted in a special gravity flow retorting process and system which utilizes novel arrangements of internal baffles in a static mixer.

Abstract: A method is provided for producing needle coke comprising the steps of heating green needle coke at temperatures between about 935.degree. F. and about 1,100.degree. F. for between about 10 minutes and about 24 hours, cooling the coke to below about 250.degree. F., and calcining the coke at calcination temperatures above about 2,000.degree. F.

Abstract: An improved retort process in which oil is recovered from crushed oil shale moved by gravity through a passageway of an elongated housing with an inlet for the crushed oil shale at the top end and an outlet for the spent crushed oil shale at the bottom end of the housing, with the rate of movement of the crushed oil shale through the passageway in the housing being controlled. Heat is transferred in sequence to or from the ground oil shale as it moves from the inlet to the outlet by means of heat exchangers which are spaced to define a drying zone, a preheating zone, a cracking and distillation zone. Waste heat recovered from the waste heat recovery zone is passed to the preheating zone. Sufficient heat is delivered to the cracking and distillation zone to raise the temperature of the crushed oil shale moving through the cracking and distillation zone to the critical temperature for separating hydrocarbons in vapor form therefrom by means of an auxiliary heating assembly.

Abstract: A method is provided for producing needle coke comprising the steps of heating green needle coke at temperatures between about 875.degree. F. and about 1,200.degree. F. for between about 10 minutes and about 24 hours, and, without first allowing the temperature of the coke to cool below about 250.degree. F., calcining the green needle coke at calcination temperatures above about 2,000.degree. F.

Abstract: An improved retort apparatus for recovering oil from crushed oil shale moved by gravity through a passageway of an elongated housing includes a control assembly connected adjacent the outlet end of the housing to control the rate of movement of the crushed oil shale through the passageway. A plurality of heat exchangers are located in the housing for transferring heat in sequence to or from the crushed oil shale. The heat exchangers are spaced to define a drying zone, a preheating zone, a hydrocarbon recovery zone, and a waste heat recovery zone. A pump recirculating circuit is provided for passing waste heat recovered from the waste heat recovery zone to the preheating zone. An auxiliary heating assembly connected to the heat exchangers in the hydrocarbon recovery zone delivers sufficient heat to raise the temperature of the crushed oil shale moving through the hydrocarbon recovery zone to the critical temperature for separating hydrocarbons in vapor form therefrom.

Abstract: Hot oil depleted shale from an indirect oil shale retorting process is charged into the top of a vertical shaft furnace together with sufficient oxygen to combust the residual carbon in the shale. Recycle process gas is fed into the bottom of the furnace for direct heating by the spent shale. The heated recycle process gas and combustion gases are withdrawn from the furnace separately to minimize dilution of the high BTU process gas. A selected quantity of coarse, cooled spent shale discharged from the bottom of the furnace is recycled to the top to moderate the temperature of combustion.

Abstract: Recycle gas for the indirect retorting of oil shale, is heated after the oil has been recovered from the gas, utilizing the residual carbon in hot oil depleted shale. The hot oil depleted shale is charged into a vertical shaft furnace where it is combusted by the introduction of air into the upper portion of the furnace. The heat so generated is recovered from the lower part of the furnace for heating the recycle gas and cooling the spent shale. A portion of the coarse fraction of the cooled spent shale discharged from the bottom of the furnace is recycled to the top to regulate the temperature of combustion. The recycle gas may be heated directly by countercurrent contact with the hot, spent shale in the lower portion of the furnace or indirectly in a heat exchanger by an inert gas which is circulated through the lower portion of the furnace.

Abstract: An apparatus for distilling shale oil from oil shale, which comprises: a vertical type distilling furnace which is divided by two vertical partitions each provided with a plurality of vent apertures into an oil shale treating chamber and two gas chambers, said oil shale treating chamber being located between said two gas chambers in said vertical type distilling furnace, said vertical type distilling furnace being further divided by at least one horizontal partition into an oil shale distilling chamber in the lower part thereof and at least one oil shale preheating chamber in the upper part thereof, said oil shale distilling chamber and said oil shale preheating chamber communicating with each other through a gap provided at an end of said horizontal partition, an oil shale supplied continuously from an oil shale supply port provided in said oil shale treating chamber at the top thereof into said oil shale treating chamber continuously moving from the oil shale preheating chamber to the oil shale distilling c

Abstract: A process and system for continuously pyrolyzing organic feedstock produces a solid carbonaceous residue of controlled volatility, in a manner that is highly energy efficient. The value of the gaseous product and of the pyrolytic oil produced are also optimized.

Abstract: A process for cracking lignin-containing feed materials, such as precipitated from black liquor, to produce hydrocarbon products such as ethylene, utilizing dual fluidized beds of particulate solids in series flow arrangement. In the process, the feedstock is introduced with a diluent gas such as steam into the first or fast fluidized bed for cracking reactions at superficial gas velocity exceeding about 5 ft/sec. A particulate solids carrier material, which can comprise at least partly coke produced in the process, is circulated between the beds, and coke deposited on the carrier in the first or cracking bed at 1000.degree.-1600.degree. F. temperature is burned off in a second or combustion bed maintained at 1400.degree.-2000.degree. F. temperature by an oxygen-containing gas and diluent steam introduced therein. Superficial upward gas velocity in the fast fluidized bed zone exceeds about 5 ft/sec. and the bed density exceeds about 3 lb/cu.ft.

Abstract: The production of hydrogenated tar and distillates from coal which is passed through successive condensing, hydrogenation, desulfurization and cooling zones of a dense bed while a flue gas is discharged into the lower portion of the desulfurization zone in admixture with steam and hydrogen for countercurrent flow contact with the coal and coke solids. The gases evolved from the desulfurization zone are passed into countercurrent contact with the coal in the preceding hydrogenation zone where the high boiling coal tar fractions evolved from the coal are hydrogenated and pyrolyzed. The total effluent from the hydrogenation zone is then passed into countercurrent contact with the coal in the condensing zone, preheating the coal by direct contact and initiating the pyrolysis of the coal. The preferred method is practiced in a vertical kiln through which the coal is passed as a dense, compact gravitating bed of solids.

Abstract: Solid heat carrier material and solid hydrocarbon-containing material, such as oil shale, tar sands or coal, are deflected be conical baffles into radially moving fluid beds which alternately flow radially outwardly and inwardly over a series of trays and downwardly into a series of peripheral and axial downcomers for a sufficient residence time to liberate hydrocarbons from the solid hydrocarbon-containing material. A fluidizing gas is injected upwardly into the beds to mix and fluidize most of the solids in the beds as well as to strip and transport the liberated hydrocarbons away from the beds for further processing downstream. Upright annular baffles can be positioned in the beds to minimize radial backmixing of solids and can also extend above the surface of the beds to minimize wave propagation. Any unfluidized coarse particles can be moved downwardly at an angle of inclination by gravity flow and jet deflectors.