Abstract: The present disclosure provides systems and methods for hydrogen production as well as apparatuses useful in such systems and methods. Hydrogen is produced by steam reforming of a hydrocarbon in a gas heated reformer that is heated using one or more streams comprising combustion products of a fuel in an oxidant, preferably in the presence of a carbon dioxide circulating stream.

Abstract: A reactor (1) for preparing phosgene by gas-phase reaction of carbon monoxide and chlorine in the presence of a solid-state catalyst, which is provided in a plurality of catalyst tubes (2) which are arranged parallel to one another in the longitudinal direction of the reactor (1) and are welded at each of their two ends into a tube plate (3), with introduction of the starting materials at the upper end of the catalyst tubes (2) and discharge of the gaseous reaction mixture at the lower end of the catalyst tubes (2), in each case via a cap, and also with introduction and discharge facilities for a liquid heat transfer medium (7) in the space (4) between the catalyst tubes (2) within the shell, where the flow of the heat transfer medium (7) in the space (4) between the catalyst tubes (2) within the shell is meandering as a result of deflection plates (5), each alternative deflection plate (5) leaves two openings (6) having the shape of a segment of a circle free on opposite sides at the interior wall of the rea

Abstract: A Fischer Tropsch (“FT”) unit that includes an FT tube that is packed with a catalyst. The catalyst is designed to catalyze an FT reaction to produce a hydrocarbon. An insert that is positioned within the FT tube. The insert comprises at least one cross-piece that contacts an inner surface of the FT tube and at least one cross-fin extending from the cross-piece. There may be a corresponding second cross-fin adjacent each cross-fin. Both the cross-fins and the second cross-fins may be disposed radially outwardly such that the edge of the cross-fins are closer to the inner surface of the FT tube than is the base of the cross-fins.

Abstract: A method and an apparatus is disclosed that uses a gas lift tubing arrangement to produce synthetic hydrocarbon related products. Using the Fischer Tropsch process as an example, the tubing is packed with a suitable catalyst and then hydrogen and carbon monoxide are injected into the top of the tubing in a fashion similar to a gas lift process. As the gases travel past the catalyst, synthetic hydrocarbons are formed and heat is rejected. The synthetic hydrocarbons and water flow out of the bottom of the tubing and travel up the annulus to the surface. In some embodiments, this process is carried out in a producing well or a in producing riser. In a producing well or a producing riser, the production from the well which flows up the annulus cools the synthetic hydrocarbon derived products. In additional and alternate embodiments, this process can be used in non-flowing wells.

Abstract: A device for mixing and cooling two reactive liquids, comprising a bundle type heat exchanger with parallel tubes, a head space open to one end of all tubes, a first inlet to the head space for introducing a first liquid and a second inlet to the head space with a multitude of nozzles for introducing a second liquid, the nozzles being located within the head space and oriented to direct the introduced liquid transverse to the axis of the tubes of the tube bundle, is useful for making peroxomonosulphuric acid from 85 to 98% by weight sulphuric acid introduced into the first inlet of the device and 50 to 80% by weight aqueous hydrogen peroxide introduced into the second inlet of the device.

Abstract: A tube bundle reactor for carrying out catalytic gas phase reactions, particularly methanation reactions, has a bundle of catalyst-filled reaction tubes through which reaction gas flows and around which heat carrier flows during operation. In the region of the catalyst filling, the reaction tubes run through at least two heat carrier zones which are separated from one another, the first of which heat carrier zones extends over the starting region of the catalyst filling. The reaction tubes each have a first reaction tube portion with a first hydraulic diameter of the catalyst filling and, downstream thereof in flow direction of the reaction gas, at least a second reaction tube portion with a second hydraulic diameter of the catalyst filling that is greater than the first hydraulic diameter of the catalyst filling.

Abstract: A multi-chamber continuous tubular reactor for the transesterification of oil (e.g., waste cooking oil and the like) and methanol into glycol and fatty acid methyl (ethel) ester. The reactor includes a plurality of tubes, a plurality of fluidly coupled chambers, an inlet fluidly coupled to a first chamber of the plurality of chambers for receiving reactants, and an outlet fluidly coupled to a second chamber of the plurality of chambers for receiving products generated during a reaction within the plurality of chambers. At least one of the plurality of tubes is at least partially disposed within a lumen of another one of the plurality of tubes. The plurality of fluidly coupled chambers are defined, at least in part, by the plurality of tubes. The reactor is configured to generate a generally helical flow pattern through at least one of the plurality of chambers.

Abstract: A system for the production of conversion products from synthesis gas, the system including a mixing apparatus configured for mixing steam with at least one carbonaceous material to produce a reformer feedstock; a reformer configured to produce, from the reformer feedstock, a reformer product comprising synthesis gas comprising hydrogen and carbon monoxide from the reformer feedstock; a synthesis gas conversion apparatus configured to catalytically convert at least a portion of the synthesis gas in the reformer product into synthesis gas conversion product and to separate from the synthesis gas conversion product a tailgas comprising at least one gas selected from the group consisting of carbon monoxide, carbon dioxide, hydrogen and methane; and one or more recycle lines fluidly connecting the synthesis gas conversion apparatus with the mixing apparatus, the reformer, or both.

Abstract: Disclosed herein is a hydrogen generator for producing hydrogen by the steam-reforming reaction of hydrocarbons, in which a pressure loss induction structure for artificially reducing the pressure of exhaust gas is provided between a combustion unit and an exhaust gas discharge pipe, thus improving the uneven distribution of exhaust gas.

Abstract: The present invention describes a steam reforming furnace for the production of hydrogen, which employs a set of porous burners interposed between the tubes to be heated, improving compactness of the furnace.

Abstract: A process for continuous heterogeneously catalyzed partial dehydrogenation of at least one hydrocarbon to be dehydrogenated in a reactor which is manufactured from a composite material which consists, on its side in contact with the reaction chamber, of a steel B with specific elemental composition which, on its side facing away from the reaction chamber, either directly or via an intermediate layer of copper, or of nickel, or of copper and nickel, is plated onto a steel A with specific elemental composition, and also partial oxidations of the dehydrogenated hydrocarbon and the reactor itself.

Abstract: A shell which encloses an interior and has at least one first orifice for feeding at least one gas stream into the interior and at least one second orifice for withdrawing a gas stream fed to the interior beforehand via the at least one first orifice from the interior, the surface of the shell, on its side in contact with the interior, being manufactured at least partly, in a layer thickness of at least 1 mm, from a steel which has a specific elemental composition, and in the interior, a process for continuous heterogeneously catalyzed partial dehydrogenation of at least one hydrocarbon to be dehydrogenated is carried out in a reactor which is manufactured from the steel on its side in contact with the reaction gas.

Abstract: In a catalyst carrier for insertion in a tube of a reactor, an annular container holds the catalyst in use and has a perforated inner wall defining a tube, a perforated outer wall, a top surface closing the annular container and a bottom surface closing the annular container. A surface closes the bottom of the tube formed by the inner wall of the annular container. A skirt extends upwardly from the perforated outer wall of the annular container from a position at or near the bottom surface to a position below the location of a seal located at or near the top surface and extending from the container by a distance which extends beyond an outer surface of the skirt.

Abstract: A catalyst unit suitable for loading into a tube in a reactor includes a plurality of catalyst particles incorporated within a removable solid matrix, said unit in the form of an elongate body in which the particles are packed together such that the volume shrinkage upon removal of the removable matrix is ?20%. The catalyst particles preferably comprise one or more metals selected from the group consisting of Fe and Co in oxidic or reduced form. The units are particularly suitable for loading catalyst into tubes in a Fischer-Tropsch reactor.

Abstract: The present invention describes a vertical cylindrical exchanger-reactor for carrying out endothermic reactions, comprising a shell enclosing a plurality of tubes inside which the reactive fluid moves, said tubes being of the bayonet type, and the heat transfer fluid, in this case hot gases, being channeled inside chimneys surrounding said bayonet tubes. The bayonet tubes and the chimneys are suspended from the upper dome of the reactor. This reactor may operate with a pressure difference between the tube side and the shell of up to 100 bars. The hot gases are admitted into the reactor at temperatures of up to 1300° C.

Abstract: The present invention provides isothermal multitube reactors suitable for the production of chlorinated and/or fluorinated propene and higher alkenes from the reaction of chlorinated and/or fluorinated alkanes and chlorinated and/or fluorinated alkenes. The reactors utilize a feed mixture inlet temperature at least 20° C. different from a desired reaction temperature.

Abstract: This invention relates to a tubular cracking furnace, especially an ethylene cracking furnace, which comprises a convection section and a or dual radiant section(s), at least one heat transfer intensifying member arranged in at least one pass each radiant tube in said radiant section, said at least one heat transfer intensifying member comprises a first heat transfer intensifying member, which is arranged at a location between 10D and 25D upstream of the extreme point of said at least one pass radiant tube metal temperature, wherein D is the inner diameter of the radiant tube having heat transfer intensifying members. The present invention could achieve the best enhanced heat transfer result with given number of heat transfer intensifying member, by optimizing the locations of heat transfer intensifying members in the radiant tube.

Abstract: Tube-bundle equipment for heat exchange operations at high pressures and temperatures, under conditions of high aggressiveness of the process fluids, comprising a titanium lining (11) and a series of tubes (1) consisting of at least one layer of zirconium (2), positioned in contact with said fluids, wherein the tube plate on which said tubes are inserted comprises an outer layer (S) of zirconium or an alloy thereof and an underlying layer (5) of titanium welded to the lining of the equipment. Said equipment is particularly used as a heat exchanger, for example as a stripper, in the high-pressure cycle of urea syntheses processes.

Abstract: Disclosed is a process and apparatus for the catalytic hydrogenation of fluoro-olefins to fluorocarbons where the reaction is carried out in a multi-tube shell and tube reactor. Reactions involving hydrogenation of fluoro-olefins are typically exothermic. In commercial processes where a fluoro-olefin CnH2n?xFx to CnH2n?x2Fx is hydrogenated (e.g., hexafluoropropylene to 236ea, 1225ye to 245eb, and the like), inadequate management or control of heat removal may induce excess hydrogenation, decomposition and hot spots resulting in reduced yields and potential safety issues. In the hydrogenation of fluoro-olefins, it is therefore necessary to control the reaction temperature as precisely as practical to overcome challenges associated with heat management and safety.

Abstract: Multi-tubular reactors for fluid processing incorporate reactor tubes containing thermally conductive monolithic catalyst structures with relative dimensions and thermal expansion characteristics effective to establish both a non-interfering or slidably interfering fit between the monolith structures and the reactor tubes at selected monolith mounting temperatures, and geometries at reactor operating temperatures such that the operating gaps between tubes and monoliths under the conditions of reactor operation do not exceed about 250 ?m over tube sections where high heat flux to or from the monoliths is required.

Abstract: The invention concerns an exchanger-reactor (1) comprising: a vessel (2); means for distributing a feed through a fixed bed catalytic zone (10); means (6) for collecting effluent from the catalytic zone (10); means for heating the catalytic zone (10); in which said collection means (6) comprise conduits passing right through the catalytic zone (10), said conduits being distributed in the catalytic zone and interposed between the heating means, and in which the heating means of the catalytic zone are contained in sheaths (8) which are partially immersed in the catalytic zone (10), the sheaths (8) being open at one of their ends and closed at the other, the open end being fixed to an upper tube plate (21) defining the collection chamber (19) which is located above the catalytic zone (10), said heating means comprising at least one combustion zone (13) located close to the catalytic zone, means for supplying said combustion zone (13) with an oxidizing gas mixture (15) and with a gaseous fuel (17), and means

Abstract: A reactor is provided comprising a reactor substrate and upper and lower manifold structures. The upper manifold structure and the lower manifold structure each comprise at least one flow directing cavity that reverses a flow direction of a fluid flowing through the relatively short open-ended channels of the substrate between the upper and lower manifold structures. The flow directing cavities of the upper and lower manifold structures are configured to direct fluid from the inlet region of the upper manifold structure to the outlet region of the lower manifold structure in an additional serpentine path defined by the flow direction reversals introduced by the upper and lower manifold structures. Additional embodiments are disclosed and claimed.

Abstract: A chemical reactor is provided that includes: a plurality of tubes having a catalytic reactor substrate therein, each of the tubes having an inlet at one end for receiving a fluid flow and an outlet at an opposing end for discharging fluid flow, and a longitudinal axis parallel to the direction of fluid flow through the tube, the longitudinal axis of each tube being parallel to one another; and a plurality of heat exchange fins disposed on and extending radially from the exterior surface of each tube; the heat exchange fins on each tube independently having a profile along a cross-section perpendicular to the longitudinal axis of each tube, and the tubes being arranged with respect to one another, such that the heat exchange fin profiles together form a tessellated pattern in a plane that is perpendicular to the longitudinal axes of the tubes.

Abstract: A hydrogen generator according to the invention comprises: a combustion gas passage (5) configured to flow combustion gas coming from a combustor; a preheat-evaporator (6) which is supplied with a material gas and water and configured to evaporate the water and heat the material gas by heat transmitted from the combustion gas passage and a carbon monoxide reducer (10) through partition a wall; a reformer (7) configured to generate reformed gas from the material gas and steam fed from the preheat-evaporator by using a reforming catalyst (8) and heat transmitted from the combustion gas passage through the partition wall; the carbon monoxide reducer (10) configured to remove carbon monoxide from the reformed gas fed from the reformer by a carbon monoxide removing catalyst (9); a cylindrical body (3) closed at both ends thereof having an internal space is divided by the partition walls (1), (2), (30), (47) to form the combustion gas passage, preheat-evaporator, reformer and carbon monoxide reducer within the cyli

Abstract: A fuel processor that extracts, from a fuel source, hydrogen gas used for an electricity generation reaction. The fuel processor includes a reformer that generates hydrogen gas by reacting a fuel source with water, a burner that heats the reformer to an appropriate temperature for a hydrogen generation reaction, a CO remover that removes CO generated during the hydrogen generation reaction in the reformer, and a heat exchanger for cooling the CO remover.

Abstract: A tube bundle falling film microreactor for performing gas-liquid reactions, which has: a) at least one vertical tube with b) a device for distributing the liquid on the inside of the tube and c) a liquid collecting system, and d) a device for gas supply and removal, and use thereof.

Abstract: Embodiments are disclosed that relate to increasing radiative heat transfer in a steam reformer from an exterior shell which includes a diffusion burner to an interior reactor via angled fins coupled to the exterior shell. For example, one disclosed embodiment provides a steam reformer, comprising an exterior shell which includes a diffusion burner and angled fins, the angled fins extending away from an inner surface of the exterior shell and downward toward the diffusion burner. The steam reformer further comprises an interior reactor positioned at least partly within the exterior shell.

Abstract: A gasification system is disclosed having a combustion or reaction vessel, a scrubber housing, and a filter housing. A carbonaceous fuel is partially combusted in the reaction vessel to generate a combustible gas. An improved ash support and removal system reduces clogging and other problems in the reaction vessel. The combustible gas passes through the scrubber housing to remove matter such as tar and oil, and the scrubbed gas passes through a hybrid blower to the filter housing. Wood chips are used in the filter housing to provide a relatively clean, dry gas. Wastewater and other waste products from the scrubber housing and filter housing are captured and returned to the reaction vessel.

Abstract: The present invention is a process for converting methane to methanol, comprising: feeding methane and gaseous air or oxygen or gaseous air enriched with oxygen to a reactor under an elevated pressure; said reactor having an internal surface, made of silica or coated with silica, surrounding a zone in which said gases react; and reacting said gases in said reaction zone at an elevated temperature at conditions effective to produce methanol and for valuable oxygenates. Advantageously the internal surface is made of quartz or coated with quartz Advantageously the internal surface, made of silica (advantageously quartz) or coated with silica (advantageously quartz), is treated with HF before the conversion of methane to methanol. Advantageously the reaction is carried out in the absence in said reaction zone of any added material which measurably affects the rate of the reaction or the yield of the product. Advantageously the reactor is operated under a pressure from 1 to 7.5 MPa.

Abstract: Disclosed is a shell-and-tube heat exchanger type reactor that can be used for a process of producing unsaturated acids from olefins via fixed-bed catalytic partial oxidation, which comprises at least one reaction tube, each including at least one first-step catalyst layer, in which olefins are oxidized by a first-step catalyst to mainly produce unsaturated aldehydes, and at least two second-step catalyst layers, in which the unsaturated aldehydes are oxidized by a second-step catalyst to produce unsaturated acids, wherein a first catalyst layer of the second-step catalyst layers, disposed right adjacent to the first-step catalyst layer, has an activity corresponding to 5˜30% of the activity of the catalyst layer having a highest activity among the second-step catalyst layers. A method of producing unsaturated acids from olefins by using the reactor is also disclosed.

Abstract: A metal tube in the present invention is a metal tube for pyrolysis reaction with superior characteristics of both the heat exchange and the pyrolysis reaction, which is suitable for use in a process in which hydrocarbons are pyrolytically decomposed. The tube is a metal tube for pyrolysis reaction consisting of 3 or 4 spiral ribs 1 provided on an inner surface which are inclined at 20 to 35 degrees to an axial direction of the metal tube, and characterized in that h/Di of 0.1 to 0.2 and h/w of 0.25 to 1.0 when a height of the rib 1 is defined as “h”, a width of the rib 1 at its bottom part is defined as “w” and an inner diameter of the tube at the bottom part is defined as “Di” in cross section of the spiral rib 1.

Abstract: A catalytic reaction device for fluid-solid heterogeneous catalytic reactions including a distributor, flow controllers, parallel reactors, temperature controllers, coolers and product receivers with reactive fluids flowing into the flow controllers to control the total flow of a fluid is provided.

Abstract: A multi-tubular reactor system for catalytically reacting a fluid reactant mixture to form a fluid product comprising a shell and a plurality of reactor tubes housed therein. The reactor system is adapted to allow heat-exchange fluid to flow between the shell and the external surface of the reactor tubes. A reactor tube comprises a reaction zone, and also a heating zone and/or a cooling zone. The reaction zone is positioned downstream of the heating zone. The cooling zone is positioned downstream of the reaction zone. The reactor tube contains a bed of solid particulate catalyst in the reaction zone. The reactor tube additionally contains a heat-exchanging essentially rod-shaped insert having a length of from 1 to 20%, preferably 1 to 5%, of the total length of the reactor tube in the heating zone and/or the cooling zone.

Abstract: Embodiments of a microchannel reactor comprise a microchannel housing comprising a plurality of channels and an upper microstructure disposed above the microchannel housing. The upper microstructure comprising a gas feed circuit, a liquid feed circuit, and at least one mixing cavity. The mixing cavity is in fluid communication with at least one reactive passage of the microchannel housing. The gas feed circuit comprises at least one gas feed inlet, and the liquid feed circuit comprises at least one liquid feed inlet and at least one liquid reservoir adjacent to the mixing cavity, wherein the liquid reservoir is operable to deliver a liquid feed into the mixing cavity.

Abstract: Disclosed is a shell-and-tube reactor or heat exchanger, which alternately comprises a doughnut-type baffle plate and a first disc-type baffle plate in order to increase heat transfer efficiency. In the reactor or heat exchanger, a second disc-type baffle plate is placed in an empty space inside of the doughnut-type baffle plate, and some tubes, through the inside of which a first object for heat transfer with a heat transfer medium, are present in a region inside of the doughnut-type baffle plate and outside of the second disc-type baffle plate. Also disclosed is a method for producing an oxide, comprising: using said reactor or heat exchanger, and causing a catalytic vapor-phase oxidation reaction in the tubes, through the inside of which the first object for heat transfer with the heat transfer medium is passed.

Abstract: The disclosed invention relates to a process for converting ethylbenzene to styrene, comprising: flowing a feed composition comprising ethylbenzene in at least one process microchannel in contact with at least one catalyst to dehydrogenate the ethylbenzene and form a product comprising styrene; exchanging heat between the process microchannel and at least one heat exchange channel in thermal contact with the process microchannel; and removing product from the process microchannel. Also disclosed is an apparatus comprising a process microchannel, a heat exchange channel, and a heat transfer wall positioned between the process microchannel and heat exchange channel wherein the heat transfer wall comprises a thermal resistance layer.

Abstract: Systems and methods for producing ammonia. The system can include a first shell having two or more discrete catalyst beds disposed therein, a second shell disposed about the first shell, a first heat exchanger disposed external to the first shell and in fluid communication therewith, a second heat exchanger disposed external to the second shell and in fluid communication therewith, and a flow path disposed within the first shell. A first portion can be reacted in the presence of the catalyst to provide an ammonia effluent. The heat of reaction from the ammonia effluent can be exchanged within the first heat exchanger and the second heat exchanger. The heated second portion of the feed gas can be introduced to the first shell and can be reacted in the presence of the catalyst.