The present invention provides a process for producing hydrogen iodide. The process includes providing a vapor-phase reactant stream comprising hydrogen and iodine and reacting the reactant stream in the presence of a catalyst to produce a product stream comprising hydrogen iodide. The catalyst includes at least one selected from the group of nickel, cobalt, iron, nickel oxide, cobalt oxide, and iron oxide. The catalyst is supported on a support.

An exhaust gas treatment method by which mercury contained in exhaust gas can be separated and removed efficiently and inexpensively. The method includes cooling an exhaust gas containing mercury in metal vapor phase by spraying water or other methods to condense mercury in the exhaust gas from metal vapor phase into metal liquid and thus to separate and remove mercury from the exhaust gas. When the exhaust gas is cooled by spraying water, the sprayed water is collected and separated into separated water and a solid containing mercury that has condensed to metal liquid, and mercury is recovered from the solid. The metal mercury particles that have condensed to metal liquid are dispersed in cooling water. The metal mercury particles can thus be easily separated and recovered by using a suitable separation device.

A multi-waste processing system includes a processing chamber. The processing chamber includes one or more heaters and a piston, and the processing chamber is configured to evaporate liquid waste and compact solid waste input. A condenser is operably connected to the processing chamber. The condenser is configured to condense water from the evaporated liquid waste output from the processing chamber. A gas and water separator is operably connected to the condenser. The gas and water separator is configured to separate water from the evaporated liquid waste output from the processing chamber. A recirculation pathway connects the gas and water separator to the processing chamber to recirculate gas from the gas and water separator to the processing chamber. The piston is actuated to keep the one or more heaters in close proximity to the solid waste and the liquid waste in the processing chamber.

A carbon dioxide recovery apparatus is disclosed including a flue gas cooling unit that brings flue gas cooling water into contact with a flue gas to cool the flue gas, a circulation channel through which the flue gas cooling water and condensed water are returned to the flue gas cooling unit, an absorption unit including a carbon dioxide absorbing section, and a flue gas washing section that brings the flue gas including carbon dioxide absorbed in the carbon dioxide absorbing section into contact with flue gas washing water and washes the flue gas, a regeneration unit that removes carbon dioxide from the absorbent including carbon dioxide absorbed in the absorption unit, a supply channel through which circulating water is guided, and a discharge channel through which the circulating water circulating through the flue gas cooling unit and the circulation channel is discharged to outside of a system.

A process is proposed for separating carbon dioxide from a feed stream containing carbon dioxide, in which at least part of the feed stream is subjected to temperature swing adsorption to obtain a first and a second successive stream, wherein, in each case relative to the feed stream, the first subsequent stream is depleted in carbon dioxide and the second subsequent stream is enriched in carbon dioxide, and at least part of the second subsequent stream is subjected to membrane separation to obtain a third and a fourth subsequent stream, the third subsequent stream being depleted in carbon dioxide and the fourth subsequent stream being enriched in carbon dioxide, in each case relative to the second subsequent stream. A corresponding arrangement is also an object of the invention.

A pressurized CO.sub.2 rich gas is cooled down to condense at least part of the stream in a heat exchanger. A bulk of the CO.sub.2 is separated by partial condensation and distillation in order to obtain at least one non-condensable gas from a separation vessel. The non-condensable gas is optionally heated up to a temperature lower than −20° C. (membranes performances is greatly enhanced by low temperature operation). The non-condensable gas is introduced into a membrane permeation unit, producing a residue stream and a permeate stream (the permeate stream is enriched in CO.sub.2). The permeate stream is recycled to the process, optionally after compression. The method is auto-refrigerated, i. e. no external refrigerant is used to provide cooling below 0° C.

An apparatus for producing synthesis gas (syngas) is provided. The apparatus includes a hub, including an autothermal dry reforming of methane apparatus, configured to receive CO.sub.2 and O.sub.2, and configured to produce a first stream of syngas with low a H.sub.2/CO mole ratio; an autothermal steam reforming of methane apparatus, configured to receive steam and O.sub.2, and configured to produce a second stream of syngas with a high H.sub.2/CO mole ratio; an H.sub.2 separation apparatus, configured to receive H.sub.2 and CO.sub.2, and coupled to the autothermal dry reforming of methane apparatus to deliver CO.sub.2 thereto; and a reactor for converting CO to H.sub.2 using a water-gas shift reaction, coupled to the autothermal steam reforming of methane apparatus to receive the second stream of syngas, and coupled to the H.sub.2 separation apparatus to deliver a stream of H.sub.2 and CO.sub.2 thereto. A method for producing synthesis gas is provided. The method includes configuring an autothermal dry reforming of methane apparatus to receive CO.sub.2 from industrial emission sources and an H.sub.2 separation apparatus, which receives H.sub.2 and CO.sub.2 from a water gas shift reactor fed with a portion of the second stream of syngas from an autothermal steam reforming of methane apparatus.

An atmospheric water generation system comprises water vapor consolidation systems configured to increase the relative humidity of a controlled air stream prior to condensing water from the controlled air stream. The water vapor consolidation system comprises a fluid-desiccant flow system configured to decrease the temperature of the desiccant to encourage water vapor to be absorbed by the desiccant from an atmospheric air flow. The desiccant flow is then heated to encourage water vapor evaporation from the desiccant flow into a controlled air stream that circulates within the system. The humidity of the controlled air stream is thereby increased above the relative humidity of the atmospheric air to facilitate condensation of the water vapor into usable liquid water.

The present invention relates to the extraction of gasoline from a gas G, with (a) a step of extracting gasoline from the gas to be treated comprising methanol GM obtained from step (d), (b) a step of separating said fluid GL1 partially condensed in step (a), producing a first aqueous liquid phase A1, a first liquid phase H1 of hydrocarbon(s) a gaseous phase G1 obtained from the gas G; (c) a step of contacting a portion of the gas G to be treated with said first aqueous liquid phase A1, producing a second aqueous liquid phase A2, a gaseous phase of gas to be treated comprising methanol GM′; (d) a step of mixing said gaseous phase of gas to be treated comprising methanol GM′ with the remainder of the gas G to be treated, producing a gas to be treated comprising methanol GM, (e) a step of stabilizing said first liquid phase H1 of hydrocarbon(s).

A method and apparatus for separating a separation component from a gas stream. One exemplary method includes: flowing the gas stream across a process surface of a compliant composite heat transfer wall, wherein: the gas stream has an initial concentration of the separation component, and the gas stream has a gas temperature; flowing a cooling fluid across a cooling surface of the wall, wherein: the cooling fluid has a fluid temperature, and the fluid temperature is less than the gas temperature; and producing an output gas stream, wherein: the output gas stream has an output concentration of the separation component, and the output concentration is less than the initial concentration. Another exemplary method includes separating at least a portion of the separation component from the gas stream by: accumulating the portion proximate the process surface; and delaminating the portion from the process surface with a flow of the gas stream.