Abstract: An energy conversion process that also exports by-product CO2 at elevated pressure where a fuel gas feed stream is mixed with a reactant stream and additional CO2 is added to at least part of, the fuel gas feed stream, the reactant stream or both through desorption by contacting with a CO2-rich solvent stream in a first stage contactor to produce a mixed feed gas stream and a CO2-lean solvent stream; passing said mixed feed gas stream to a chemical conversion step, where further CO2 is produced; chilling at least part of the products of said chemical conversion step, at a pressure of at least 10 bar to condense and partially remove CO2 as a liquid and thereby produce a CO2-lean gas stream; and passing at least part of said CO2-lean gas stream said to a second stage contactor where further CO2 is removed, by absorption in a solvent stream lean in CO2 derived from said CO2-lean solvent stream, to produce a product gas stream and a solvent stream rich in CO2 from which said CO2-rich solvent stream is subsequentl

Abstract: A pipeline pig 21 for removing condensed gas from the wall of a pipeline 23 comprises a cylindrical body 22 which is a sliding fit in the pipeline 23 and has an axial passage 26 extending therethrough and a flow gas ejector inlet tube 37 extending into the passage 26. The passage 26 is formed with a venturi 27 and the tube 37 is formed with a restriction 38, the forward end of the tube 37 terminating upstream of the venturi 27. The pig 21 is propelled through the pipeline 23 by differential gas pressure acting upon it and gas flows through the passage 26 so that condensed gas is entrained into the passage 26 by way of an annular duct 32 and radial ducts 35 into a rear tapering portion 29 of the passage 26 upstream of the venturi 27. The condensed gas is drawn to the forward end of the ejector tube 37 which end is located downstream of the ducts 35 and is subjected to the turbulent flow of the flow gas which has been accelerated by the venturi restriction 38 in the ejector tube 37.

Abstract: Heavy hydrocarbon feedstocks, e.g. gas oils, are vaporized and subsequently gasified at high temperatures without pyrolytic degradation by first admixing the hydrocarbon with a hot gaseous reactant, e.g. product gas or steam, to bring the temperature of the mixture above that of the dew point of the hydrocarbon and thereafter raising the temperature of the mixture to above that at which pyrolysis of the hydrocarbon begins to be significant by admixture with further quantities of the reactant which are superheated thereby to bring the temperature of the resultant mixture to that required for effecting a catalytic gasification reaction.

Abstract: Hydrocarbon oils, particularly oils which have a high boiling temperature, are treated to remove organic sulphur compounds by subjecting a mixture of a hydrogenating gas, e.g. a gas containing at least 90% v/v hydrogen and is substantially free from carbon oxides, and partially vaporized oil to a hydrogenation reaction over a known hydrogenation catalyst and thereafter passing the resulting liquid/vapor mixture which also contains hydrogen sulphide over zinc oxide, thereby to remove the hydrogen sulphide.

Abstract: Apparatus and a process are provided whereby constituents of liquid mixtures eg non-distillate oils are vaporized under non-decomposing conditions in the presence of gases. Liquid components form a stream comprising the gas, vaporized and liquid constituents of the mixture are removed from the stream. Process may be employed to provide a vaporized feedstock for the non-catalytic thermal hydrogenation of hydrocarbon-based materials in the production of methane containing gases wherein the gas used for vaporization is the same as that used for the subsequent hydrogenation steps.

Abstract: Substitute Natural Gas is produced by passing methanol vapour, optioally admixed with a minor proportion of recycle carbon dioxide, through a bed of nickel catalyst in an isothermal reactor and removing carbon dioxide from the product gas, the methanol vapour being passed into the catalyst bed at a temperature of at least 250.degree.C, preferably about 250.degree.C, and the bed being maintained at a temperature of from 250.degree.C to 350.degree.C, preferably about 300.degree.C, by external cooling with boiling water at a steam pressure of at least 550 psig.