A process for performing a continuous gas/liquid biphasic high-pressure reaction, wherein a gas and a liquid are introduced into a backmixed zone of a reactor and in the backmixed zone the gas is dispersed in the liquid by stirring, injection of gas and/or a liquid jet, a reaction mixture consecutively traverses the backmixed zone and a zone of limited backmixing, and a liquid reaction product is withdrawn at a reaction product outlet of the zone of limited backmixing, wherein the reactor comprises: an interior formed by a cylindrical vertically oriented elongate shell, a bottom and a cap, wherein the interior is divided by means of internals into the backmixed zone, the zone of limited backmixing and a cavity, a first cylindrical internal element which in the interior extends in the longitudinal direction of the reactor and which delimits the zone of limited backmixing from the backmixed zone, backmixing-preventing second internal elements in the form of random packings, structured packings or liquid-permeable trays arranged in the zone of limited backmixing and a third internal element which in the interior extends in the longitudinal direction of the reactor and is open at the bottom, wherein the third internal element forms the cavity in which gas bubbles collect and do not escape upwards, thus preventing the volume of the cavity from being occupied by liquid and reducing the reaction volume. The reaction volume of the reactor used in the process can be reversibly reduced in simple fashion. The invention further relates to a process for adapting the reaction volume of a reactor suitable for performing a gas/liquid biphasic high-pressure reaction having an outlet for a liquid reaction product in which an internal element is arranged so as to form a cavity open at the bottom in which gas bubbles collect and do not escape upwards, thus preventing the volume of the cavity from being occupied by liquid and reducing the reaction volume.

Disclosed is a reactor for solution polymerization process using a metallocene catalyst for preparing polyolefin. The reactor includes: a reaction vessel for mixing a hydrocarbon-based solvent and an olefin monomer to produce polyolefin; a feed inlet installed at a lower portion of the reaction vessel to feed a feed including an unreacted monomer, a solvent, and a catalyst into the reaction vessel; a guide pipe having a cylinder shape being open at respective ends, installed along a central axis of the reaction vessel, and dividing an internal space of the reaction vessel into an up-flow region where a reaction mixture flows upward and a down-flow region where the reaction mixture flows downward; a swirling flow-inducing blade attached to the exterior surface of the guide pipe, causing the reaction mixture in the reaction vessel to rise along the exterior surface of the guide pipe while forming a swirling flow.

In a chemical reaction device that improves a yield of a product and that causes a reaction, progress of which in a gaseous phase is restricted by a chemical equilibrium between a source material and the product, a cumulative value is not less than 500 mm.sup.2, the cumulative value being obtained by cumulatively adding, from one end to the other end of a cooling surface in a height direction, products of (i) a distance L between (a) a surface of a catalyst layer which surface is in contact with a transmission wall and (b) an outer surface of the cooling surface and (ii) a height H of the catalyst layer corresponding to the outer surface having the distance L.

A method uses mild fluorinating agents, such as hydrofluorocarbons—HCFs, perfluorocarbons—PFCs, hydrochlorofluorocarbons HCFCs and chlorofluorocarbons—CFCs, to fine-tune the fluorination process in battery material preparation in order to obtain uniform nanometer-sized surface fluoride coated battery materials. The use of a vertical flow-type tube reactor permits a fine-tuning of the fluorination process by accurately regulating the active gas or mixture of gases flow over battery materials using mass-flow regulators, and precisely setting the temperature with vertical rube furnace. Additionally, these fluorinating agents have slightly different reactivity, decomposing and reacting with battery materials at different temperatures, and therefore, offering additional parameter of fluorination fine-tuning. The method is scalable and can be easily adapted as an industrial solution. Moreover, all these gases are non-toxic, non-corrosive and non-flammable gases at room temperatures, hence, they are more convenient to handle than highly-toxic and highly-corrosive HF and F.sub.2 gases.

A process for isolating lignin from an alkaline process stream of thickened black liquor which is introduced continuously into a lower region of at least one circulation reactor having two reactor zones in concentric arrangement, liquid level of the alkaline process stream in the interior of the reactor is at a level with an upper end of an inner tubular reactor zone, a CO.sub.2-containing gas is blown continuously from the bottom into the inner tubular reactor zone of the reactor, wherein the CO.sub.2-containing gas is absorbed by the alkaline process stream in the inner circulation reactor zone and offgas is drawn off with residual amounts of the CO.sub.2 at the top of the reactor, the process is run at 1 atm, and thickened black liquor with a reduced lignin content together with precipitated lignin present are drawn off optionally after settling at the base of the reactor.

A method, a system, and an apparatus of certain embodiments are provided to recover water and carbon dioxide from combustion emissions. The recovery includes, among other things, electrolysis and carbon dioxide capture in a suitable solvent. The recovered water and carbon dioxide are subject to reaction, such as a catalytic methanation reaction, to generate at least methane.

A method, a system, and an apparatus of certain embodiments are provided to recover water and carbon dioxide from combustion emissions. The recovery includes, among other things, electrolysis and carbon dioxide capture in a suitable solvent. The recovered water and carbon dioxide are subject to reaction, such as a catalytic methanation reaction, to generate at least methane.

The disclosure provides for a process for a non-catalytic oxidative coupling of methane reaction remarkable in that the process comprises a step of providing a counter-current shell-tube reactor comprising at least two tubes defining a tubular part and a shell part surrounding the tubular part and at least one inlet to feed a gaseous feed stream and at least one outlet to discharge a product stream; a step of providing a gaseous feed stream comprising a gas mixture of methane and oxygen in a defined molar ratio and preheated to a defined operating inlet temperature; a step of feeding the gaseous feed stream at least in the tubular part of the counter-current shell-tube reactor and a step of recovering a product stream.

The invention is directed to a furnace suited for oxidation of a gaseous starting mixture comprising one or more sulphur compounds to obtain an oxidized gas mixture and reduction of the oxidized gas mixture to obtain a gaseous mixture of reduced sulphur compounds comprising an interior furnace space, an inlet conduit for the gaseous starting mixture, an inlet for supply of an oxygen comprising gas, a ceramic comprising outlet conduit provided with an inlet opening for the mixture of reduced sulphur compounds, an inlet for hydrogen and heating means, wherein the inlet opening of the outlet conduit is comprised of more than one opening which openings fluidly connect the interior furnace space and the interior of the outlet conduit.

A support structure for a structured catalytic packing is disclosed. The support structure is in a fixed position relative to the reactor tube containing it. It supports catalyzed casings that are free to move relative to the support structure. The support structure and casings are inserted in the reactor tube such that the support structure is located proximate the longitudinal axis of the tube and the casings are located between the support structure and the reactor tube wall. The support structure comprises a central support tube or rod proximate to, and impervious or perforated discs perpendicular to, the longitudinal axis of the reactor tube, and may comprise spacers separating the discs.