Abstract: The steam and thermal cracking of hydrocarbons is facilely carried out by in situ generating a stream of hot combustion gases including steam, advantageously in the configuration of a downstream axially extending, axially symmetrical helical flowstream, by combustion of steam-producing reactants in a combustion first reaction zone, and serially directly contacting and intimately admixing a liquid hydrocarbon feedstock with said gas of combustion in a downstream isodistribution, non-multi-tubular second reaction zone, advantageously first at a zone of reduced pressure thereof, the momentum of said gas of combustion at the point of direct contact being such as to provide all of the thermal and mechanical energy and heat transfer required to autogenously vaporize, entrain and effect cracking therein of said liquid hydrocarbon feedstock.

Abstract: The process relates to the recovering of essentially pure acetylene from the gaseous out-put stream from a coal to acetylene conversion process. A plasma arc generator or other high energy type reactor can be used for the conversion to coal. The gaseous out-put stream is initially treated in an acid gas removal stage by absorbing HCN and H.sub.2 S in an organic solvent such as N-methyl pyrrolidone and scrubbing with a caustic agent such as NaOH to remove CO.sub.2. In a second stage, the gaseous out-put stream is scrubbed with the organic solvent to provide a sweet gas treatment and remove essentially pure acetylene as a product. In a third stage, the second stage gases are first hydrogenated, then desulfurized and then methanated. The out-put from the third stage is recycled to the coal to acetylene conversion process. In a fourth stage, the organic solvent from said second stage is refined and recycled to the first stage and/or second stage.

Abstract: A method of controlling temperature during a pyrolysis reaction wherein the predominant pyrolysis reactions are endothermic. A fuel and oxidizer are combusted in a combustion zone to produce a hot gas stream at a superatmospheric pressure. The hot gas stream is then passed through a converging-diverging nozzle to accelerate the hot gas stream to a velocity of at least about mach 2. The reactant to be pyrolyzed is injected into the supersonic hot gas stream to produce a reaction mixture flowing at supersonic velocity and initiate the endothermic pyrolysis reactions. Substantially immediately thereafter the velocity of the reaction mixture is reduced over a predetermined reaction time to convert the kinetic energy of the reaction mixture to thermal energy in an amount sufficient to substantially offset the endothermic reactions taking place while maintaining supersonic flow. At the end of the predetermined reaction time the velocity of the reaction mixture is reduced to subsonic flow and the reaction quenched.

Abstract: A diffusion flame reactor for cracking hydrocarbon gas has an oxygen-deficient zone in the center of the flame or in the center of an array of flames. Propane, n-octane, iso-octane and decalin are cracked to ethylene, acetylene, propylene, butenes, and butadienes which are withdrawn from the flame.

Abstract: Methane is converted to higher, more reactive, hydrocarbon products by a diffusion flame. Methane is converted to C.sub.2 + products by pyrolysis in the interior of the flame with oxidizing gas flowing outside of the flame. More reactive products are withdrawn from the center of the flame by a probe tube and cooled by the flowing oxidizing gas to stop the reaction.

Abstract: For the manufacture of acetylene and synthesis or reduction gas from coal by means of an electric arc or plasma process, coal converted into powder form is pyrolyzed in an electric arc reactor with an energy density of 1 to 5 kWh/Nm.sup.3, a residence period of 0.5 to 10 msec and at a temperature of at least 1500.degree. C. such that the gaseous compounds derived from the coal do not exceed 1.8 times the so-called volatile content of the coal. The coke remaining after subsequent quenching is then fed to a second electric arc reactor in which the coke, by means of a gasifying medium in conjunction with heating by means of an electric arc or plasma process, is converted into synthesis or reduction gas furing a residence period of 1 to 15 sec and at a temperature of at least 800.degree. C. The gas flow from the pyrolysis zone is cleaned and acetylene is recovered therefrom by selective solvents. The gas from the cleaning stage is similarly cooled and cleaned.

Abstract: A process wherein coal is reacted with a hot gas stream to produce acetylene. The process comprises the sequential steps of reacting a fuel, oxygen and steam under controlled conditions of temperature to produce a hot gas stream principally comprising hydrogen, carbon monoxide and steam along with minor amounts of carbon dioxide, and essentially free of O, OH and O.sub.2. The hot gas stream is accelerated to a high velocity and impinged upon a stream of particulate bituminous or subbituminous coal and thereafter the mixture of hot gas and coal is decelerated to a velocity of from about 150 to 300 feet per second. The amounts of the streams of particulate coal and hot gas are controlled to produce in the reaction zone a pressure in the range of from about 10 to 100 psia and a temperature of from about 1800.degree. to 3000.degree. F.

Abstract: A process for producing hydrocarbons suitable for use as a chemical feedstock uses coal (10) and methane-rich gas (56) as raw materials. The coal and gas are heated over 6000.degree. F. (3316.degree. C.) in an electric-arc (14) forming an atomic plasma (16). The plasma is cooled and held (18) between 5000.degree. and 6000.degree. F. (2760.degree. and 3316.degree. C.) to allow formation of the desired hydrocarbons. The product stream (22) is then quenched (24) and the hydrocarbons separated (40, 42).

Abstract: A method for the production of acetylene from coal and hydrogen is provided by electric arc heating. The coal has a content of volatile components (i.waf) from about 25 to 44 percent and a content of organic oxygen (i.waf) of less than 9 percent and is ground to a diameter of less than 0.5 mm. The coal is then separated into two to four grain size fractions and one of the grain size fractions is loaded on a hydrogen containing gas. The gas carrying the coal is heated by way of an electric arc with an energy of from about 5 to 20 kJ/l (in normal state). The ratio of electric power employed to coal stream is from about 4,000 to 40,000 kJ/kg coal. The coal is heated for a time duration about inversely proportional to the third root of the specific outer surface of the coal gain fraction. The resulting product gas is quenched with cold liquid hydrocarbons, with hydrogen or water. Acetylene yields of up to about 0.41 kg acetylene per kg coal can be obtained.

Abstract: The process relates to the recovering of essentially pure acetylene from the gaseous out-put stream from a coal to acetylene conversion process. A plasma arc generator or other high energy type reactor can be used for the conversion to coal. The gaseous out-put stream is initially treated in an acid gas removal stage by absorbing HCN and H.sub.2 S in an organic solvent such as N-methyl pyrrolidone and scrubbing with a caustic agent such as NaOH to remove CO.sub.2. In a second stage, the gaseous out-put stream is scrubbed with the organic solvent to provide a sweet gas treatment and remove essentially pure acetylene as a product. In a third stage, the second stage gases are first hydrogenated, then desulferized and then methanated. The out-put from the third stage is recycled to the coal to acetylene conversion process. In a fourth stage, the organic solvent from said second stage is refined and recycled to the first stage and/or second stage.

Abstract: This invention relates to the conversion by way of decomposing a solid carbonaceous matter to acetylene. Specifically, the invention teaches selecting the operating conditions which will produce high yield at low cost. Specific values of heat and enthalpy for the carbonaceous matter and the gas are proposed in combination with specific particle sizes and reaction time. All of the foregoing contribute to producing acetylene at a commercially competitive cost.

Abstract: A process is disclosed for heat carrier generation for the advanced cracking reaction process comprising separately preheating an oxidant stream; joining a fuel stream and at least a portion of the process steam stream to form a stream having a steam-to-fuel ration between 0.1-10; preheating the joined stream; reforming said joined stream at a temperature up to 1000.degree. C. in the presence of a reforming catalyst comprising at least one metal selected from the metals of Group VIII of the Periodic Table of Elements on an inert support; separately preheating any remainder of the process steam; and mixing said preheated oxidant, joint and steam streams to burn in admixture in a combustion zone to provide a hot gaseous combustion products stream.

Abstract: A method of recovering heat energy from hydrocarbon pyrolysis effluent characterized by differentiated cooling systems, reduced coking, and high quality steam generation. Steam quality is improved by utilization of a minimum quenched effluent temperature of at least 370.degree. C.

Abstract: A continuous process for the selective production of ethylene by the diacritic cracking of heavy hydrocarbon feeds such as residual oils, heavy vacuum gas oils, atmospheric gas oils, crude oils and coal-derived liquids. The diacritic cracking takes place in a non-tubular multi-zone reactor at elevated pressures (e.g. 70-1000 p.s.i.a.) A fuel is combusted with oxygen in the first section of the multi-zone reactor. The high temperature products of combustion of the first zone pass into a second section of the reactor where the feed is atomized and cracked to yield products including ethylene, acetylene and synthesis gas. The reaction products of the second zone then pass into a third section in which they are quenched. In each stage of the reactor the present process seeks to prevent the build-up of coke deposits on the walls of the reactor. In the first two stages, a film of gas such as CO.sub.2 or N.sub.2 is injected along the inner walls to prevent build-up of coke.