A process for producing syngas that uses the syngas product from an oxygen-fired reformer to provide all necessary heating duties, which eliminates the need for a fired heater. Without the flue gas stream leaving a fired heater, all of the carbon dioxide produced by the reforming process is concentrated in the high-pressure syngas stream, allowing essentially complete carbon dioxide capture.

Devices and methods for reducing the specific energy required to reform or pyrolyze reactants in plasmas operating at high flow rates and high pressures are presented. These systems and methods include 1) introducing electrons and/or easily ionized materials to a plasma reactor, 2) increasing turbulence and swirl velocity of the flows of feed gases to have improved mixing in a plasma reactor, and 3) reducing slippage from a plasma reactor system. Such plasma systems may allow plasma reactors to operate at lower temperatures, higher pressure, with improved plasma ignition, increased throughput and improved energy efficiency. In preferred embodiments, the plasma reactors are used to produce hydrogen and carbon monoxide, hydrogen and carbon, or carbon monoxide through reforming and pyrolysis reactions. Preferred feedstocks include methane, carbon dioxide, and other hydrocarbons.

A process for producing synthesis gas, the process comprising the steps of a) reforming a hydrocarbon feed in a reforming section thereby obtaining a synthesis gas comprising CH4, CO, CO2, H2 and H2O and impurities comprising ammonia;b) shifting the synthesis gas in a shift section comprising one or more shift steps in series to a shifted synthesis gas; c) separating from the shifted synthesis gas a process condensate originating from cooling and optionally washing of the shifted synthesis gas;d) passing the process condensate to a condensate steam stripper, wherein dissolved shift byproducts comprising ammonia, methanol and amines formed during shifting the synthesis gas are stripped out of the process condensate using steam resulting in a stripper steam stream, e) adding a part of the stripper steam stream from the process condensate steam strip-per to the hydrocarbon feed and/or to the synthesis gas downstream the reforming section, up-stream the last shift step, wherein the remaining part of stripper steam is purged.

An integrated process for the production of a useful liquid hydrocarbon product comprises: feeding a gasification zone with an oxygen-containing feed and a first carbonaceous feedstock comprising waste materials and/or biomass, gasifying the first carbonaceous feedstock in the gasification zone to produce first synthesis gas, partially oxidising the first synthesis gas in a partial oxidation zone to generate partially oxidised synthesis gas, combining at least a portion of the first synthesis gas and/or the partially oxidised synthesis gas and at least a portion of electrolysis hydrogen obtained from an electrolyser in an amount to achieve the desired hydrogen to carbon monoxide molar ratio of from about 1.5:1 to about 2.5:1, and to generate a blended synthesis gas, wherein the electrolyser operates using green electricity; and subjecting at least a portion of the blended synthesis gas to a conversion process effective to produce the liquid hydrocarbon product.

A hydrogen reforming system includes: a reformer that generates first mixed gas through a reforming reaction between fuel gas and water; a transformer that is fed with the first mixed gas and generates second mixed gas from which carbon monoxide is removed by a water gas shift reaction; a pressure swing adsorption that purifies and separate hydrogen from the second mixed gas generated in the transformer; a heat exchanger that is provided between the reformer and the transformer and between the transformer and the PSA unit to control temperatures of the first mixed gas and the second mixed gas through heat exchange with water; a water feeder that communicates with the heat exchanger and supplies water to the heat exchanger; and a control value that is provided on a line through which water is discharged from the water feeder and adjusts a flow rate of water.

A process for producing synthesis gas, the process comprising the steps of a) reforming a hydrocarbon feed in a reforming section thereby obtaining a synthesis gas comprising CH4, CO, CO2, H2 and H2O and impurities comprising ammonia; b) shifting the synthesis gas in a shift section comprising one or more shift steps in series to a shifted synthesis gas; c) separating from the shifted synthesis gas a process condensate originating from cooling and optionally washing of the shifted synthesis gas; d) passing a part of the process condensate to a condensate steam stripper, wherein dissolved shift byproducts comprising ammonia, methanol and amines formed during shifting the synthesis gas are stripped out of the process condensate using steam resulting in a stripper steam stream, e) adding the stripper steam stream from the process condensate steam stripper to the hydrocarbon feed and/or to the synthesis gas downstream the reforming section, up-stream the last shift step, wherein the remaining part of the process condensate is purged.

A plant and a method for the production of hydrogen and bicarbonate. The plant includes a gasifier, a reformer, a direct contact exchanger and an apparatus for the production of bicarbonate. The plant is suitable for receiving fuel, oxygen, water, carbonate, brine at the inlet and for producing hydrogen, bicarbonate and calcium chloride at the outlet. The plant uses a self-cleaning direct contact heat exchanger to cool the syngas downstream of the reformer and to produce the superheated steam that feeds the gasifier: this heat exchanger allows the production of hydrogen at low costs and in modular plants.

A method for decreasing the SFFC of a steam reforming plant, including establishing a base operating mode. Then modifying the base operating mode by introducing the shift gas stream into a solvent based, non-cryogenic separator prior to introduction into the pressure swing adsorption and introducing the compressed hydrogen depleted off-gas stream in a membrane separation unit, wherein the membrane is configured to produce the hydrogen enriched permeate stream at a suitable pressure to allow the hydrogen enriched permeate stream to be combined with carbon dioxide lean shift gas stream, prior to introduction into the pressure swing adsorption unit without requiring additional compression. Thereby establishing a modified operating mode. Wherein said pressure swing adsorption unit has a modified overall hydrogen recovery. Wherein said modified operating mode has a modified hydrogen production, a modified hydrogen production unit firing duty, a modified SCO2e, and a modified SFFC.

The disclosure is directed to a process and an apparatus for providing a feedstock. A gaseous feed stream comprising at least one hydrocarbon is passed to a reforming unit followed by a water gas shift reaction zone to provide a first gaseous stream comprising H.sub.2, CO, and CO.sub.2. The first gaseous stream is fed a hydrogen separation zone to separate it into a hydrogen enriched stream and a second gaseous stream comprising CO, CO.sub.2 and H.sub.2. The second gaseous stream is fed to a CO.sub.2 to CO conversion system to produce a third gaseous stream comprising H.sub.2 and CO having a H.sub.2:CO molar ratio of less than 5:1. The third gaseous stream is fed as the feedstock for a gas fermentation unit to have increased stability and product selectivity.

A method is provided for inputting thermal energy into fluidic medium in a process or processes related to oil refining and/or petrochemical industries by at least one rotary apparatus comprising a casing with at least one inlet and at least one exit, a rotor comprising at least one row of rotor blades arranged over a circumference of a rotor hub mounted onto a rotor shaft, and a stator configured as an assembly of stationary vanes arranged at least upstream of the at least one row of rotor blades. In the method, an amount of thermal energy is imparted to a stream of fluidic medium directed along a flow path formed inside the casing between the inlet and the exit by virtue of a series of energy transformations occurring when said stream of fluidic medium passes through stationary and rotating components of said rotary apparatus, respectively. The method further comprises: integration of said at least one rotary apparatus into a heat-consuming process facility configured as a refining and/or petrochemical facility and further configured to carry out heat-consuming process or processes related to refining of oil and/or producing petrochemicals at temperatures essentially equal to or exceeding 500 degrees Celsius (° C.), and conducting an amount of input energy into the at least one rotary apparatus integrated into the heat-consuming process facility, the input energy comprises electrical energy. A rotary apparatus and related uses are further provided.