Abstract: A reactor and heat exchanger assembly is provided with the heat exchanger integrally affixed to the reactor exit head and adapted to immediately cool reactor gases from the reactor.

Abstract: A reactor including a bundle of catalyst tubes through which a reaction mixture is passed, and wherein a heat exchange medium is passed through a space surrounding the catalyst tubes and including ring lines at both reactor ends with jacket orifices for feeding in and removing the heat exchange medium by at least one pump. The heat exchange medium is fed to the upper ring line and is sucked in via the lower ring line by the at least one pump having at least one vertical pump shaft mounted and operated at its upper end. The at least one pump includes a diagonal rotor and a restrictor gap in the longitudinal direction of the at least one pump shaft, within the heat exchange medium, on the pressure side of the at least one pump for sealing and mounting the at least one pump shaft and reducing axial shear of the diagonal rotor.

Abstract: Disclosed is an annular distributor having: an annular slit layer that is mounted on an inner circumferential surface of the annular distributor and has at least one slit discharging or introducing a fluid; at least one opening that is formed on an outer circumferential surface of the annular distributor and is connected with any one of a fluid supply duct and a fluid discharge duct; and at least one guide vane selected from three types of guide vanes that are installed in the annular distributor, and splits a flow rate of the fluid supplied from the duct or collects a flow rate of the fluid discharged to the duct. And disclosed are a reactor or heat exchanger has the annular distributor, and a method of producing unsaturated aldehyde or unsaturated acid from olefin by catalytic gas phase oxidation in the reactor.

Abstract: A process and reaction unit for isothermal shift conversion of a carbon monoxide containing feed gas. The process comprises the steps of introducing the feed gas in a reaction unit into reactor tubes with a fixed bed of a shift conversion catalyst in a reaction zone, contacting the feed gas with the catalyst at conditions being effective in carbon monoxide shift conversion reaction with steam reactant to hydrogen and cooling the reaction by indirect heat exchange with a cooling agent by passing the cooling agent in a falling film along shell side of the reactor tubes and removing heated cooling agent from the falling film, passing hydrogen when it is formed by the shift conversion reaction through a hydrogen selective membrane to a permeate zone, and withdrawing hydrogen from the permeate zone and carbon monoxide depleted feed gas from the reaction zone.

Abstract: Disclosed is a shell-and-tube reactor or heat exchanger comprising: first tubes, through the inside of which a first object for heat transfer with a heat transfer medium is passed, some of the first tubes being provided in a zone in which a flow of the heat transfer medium (parallel flow) parallel to the axis of the tubes is present; and a second tube, through the inside of which the first object is not passed, the second tube being provided in said zone such that it is parallel to the axis of the first tubes. Also disclosed is a method for producing an oxide, comprising using said shell-and-tube reactor or heat exchanger, and causing a catalytic vapor-phase oxidation reaction in first tubes, through the inside of which the first object for heat transfer with the heat transfer medium is passed.

Abstract: A fuel conversion reactor includes a shell-and-tube heat exchanger for controlling the temperature of a hot gaseous mixture produced by catalytic or non-catalytic reaction of a fuel with a gaseous fluid, and for controlling the temperature of the gaseous fluid and/or the fuel prior to the reaction. The reactor is either a catalytic or non-catalytic burner, or a fuel reformer for converting a fuel to hydrogen. A preferred reactor includes an outer shell having first and second ends and an inner surface, a primary inner shell extending into the outer shell, the primary inner shell defining a heat exchanging chamber and having primary and secondary ends, and a secondary inner shell having a first end located adjacent the secondary end of the primary inner shell. One or more outlet apertures are formed between the two inner shells for passage of the gaseous fluid out of the heat exchanging chamber.

Abstract: A heat exchanger including a passageway having an internal passage adapted to form a first flow path, and an array of conduits having internal passages that collectively form a second flow path. The conduits extend through the internal passage of the passageway, and a first conduit of the array is provided with a lower total heat exchange surface area per unit volume therein than a second conduit of the array. A method of performing chemical processes is provided that includes providing a catalyst bed within the second flow path, and minimizing a temperature differential between a maximum temperature of a fluid in the second flow path and a minimum temperature of the fluid in the second flow path.

Abstract: Method for carrying out in continuous, under so-called pseudo-isothermal conditions and in a predetermined reaction environment, such as a catalytic bed, a selected chemical reaction, comprising the steps of providing in the reaction environment at least one tubular heat exchanger fed with a first flow of a heat exchange operating fluid at a respective predetermined inlet temperature, the fluid passing through the at least one tubular heat exchanger according to a respective inlet/outlet path, which method also provides the step of feeding into the at least one tubular heat exchanger and at one or more intermediate positions of said path, a second flow of operating fluid having a respective predetermined inlet temperature.

Abstract: A conversion reactor (10) including an outer shell (12) having first (14) and second (16) ends and an inner surface (16) a primary inner shell (30) extending into the outer shell (12), the primary inner shell (30) defining a heat exchanging chamber (100) and having primary and secondary (34) ends, and a secondary inner shell (40) having a first end (42) located adjacent the secondary end (34) of the primary inner shell (30). One or more oulet apertures (46) are formed between the two inner shells (30,40) for passage of the gaseous fluid out of the heat exchanging chamber (100). There are also a plurality of heat exchange tubes (50) extending through the heat exchanging chamber (100) between first (58) and second (64) tube sheets and connected to same. The first tube sheet (58) is mounted in the primary inner shell (30) while the second tube sheet (64) is connected to the secondary inner shell (40).

Abstract: A multitube reactor, wherein tubes having smaller tolerance between a nominal size and actual sizes are used as reaction tubes to stably perform a high yield reaction for a long period, a catalyst is filled into the reaction tubes so that the catalyst layer peak temperature portions of the reaction tubes are not overlapped with the connection sites thereof with baffles to effectively prevent hot spots from occurring and stably perform a reaction for a long period without the clogging of the reaction tubes, a heat medium and raw material gas are allowed to flow in the direction of a countercurrent and a specified type of catalyst is filled into the reaction tubes so that activity is increased from the inlet of the raw material gas to the outlet thereof to prevent the autooxidation of products so as to prevent equipment from being damaged due to the reaction, and, at the time of starting, gas with a temperature of 100 to 400° C.

Abstract: A fuel reformer for reforming hydrocarbon base fuel into hydrogen rich gas, with one embodiment comprised of material containing at least 15 to 25% by mass Cr, 8 to 35% by mass Ni, 2 to 4% by mass Si and the remainder Fe and inevitable impurities (C, Mn, P, S or others). The material provides sigma brittleness resistance and cementation resistance, and provides a reformer that is lightweight, low-cost, highly reliable and durable. A second embodiment adds to the composition 0.05 to 1% by mass Nb, providing improved oxidation resistance, cementation resistance, intergranular corrosion resistance, with further improved reliability and durability.

Abstract: This invention relates to a method for providing controlled heat to a process utilizing a flameless distributed combustion.

Abstract: A vertical, fixed-bed ammonia converter wherein a fixed-bed catalyst zone is configured into two mechanically separated catalyst volumes and two gas streams that operate in parallel. The design maintains the ratio of gas flow to catalyst volume so that there is no catalyst effectiveness penalty. The catalyst beds and gas flow paths are configured so that gas flow is downward through each catalyst volume. Each fixed-bed catalyst zone in the present invention can hold the catalyst in an annular space formed between two concentric shrouds arranged around a shell and tube heat exchanger. The two catalyst beds associated with each zone are situated above one another along the length of an interstage heat exchanger. Pipes or conduits are disposed through the beds to effect the parallel gas flow configuration, or alternatively, annular flows are created via passages through the internal shrouds that contain the catalyst beds.

Abstract: Perforated fins are provided to improve the capabilities of fin and tube type heat exchangers, and to adapt them for flow outside of the tube that is essentially parallel to the axis of the tube. The fins are made of a thermally conductive material, such as metal, with perforations in the fins. Fins can be of any shape. Typically, one or more tubes or binding posts pass through the fins. The fins are attached to the tube or post by press fitting, furnace or torch brazing, welding, or other method of mechanical bonding. The perforations allow heat exchange with the contents of a tube of a fluid flowing essentially parallel to the axis of the tube, in contrast to conventional fin-tube heat exchangers. The fins may also be bonded to a post or other securing means and inserted into the inside of a tube or other hollow body to improve efficiency of heat exchange. In addition, the fins may carry a catalyst, optionally carried on a washcoat or similar treatment to increase surface area.

Abstract: A process for the production of melamine by pyrolysis of urea in a high-pressure reactor having a vertical central pipe is provided. The melamine flows upwards into the reactor from below, mixes in the lower part of the reactor with a urea melt, and optionally NH3, introduced into the reactor from below, and emerges from the central pipe in the upper part of the central pipe. Part of the melamine formed flows downward in the annular space between the central pipe and reactor wall, and the remainder is expelled for further work-up. The off-gases are removed at the top of the reactor. A reactor for carrying out the process is also provided.

Abstract: A vapor-phase tubular reactor in a shell heat exchanger for removal of the heat of reaction at essentially isothermal conditions has porous wicking surface applied to the external surface of reactor tubes. The porous wicking surface on the reactor tubes draws liquid heat transfer fluid from a reservoir at the bottom of the wicked tube section and provides enhanced evaporative cooling. The invention is particularly useful for highly exothermic reactions or when reaction selectivity is negatively affected by high temperature excursions.

Abstract: In a shell-and-tube type reactor, the leakage between the upper and lower chambers is substantially decreased by tightly fitting the reaction tubes to the shield. The present invention provides a reactor for use in catalytic gas phase oxidation characterized by expanding reaction tubes to at least one groove formed in the reaction tube-fixing part of an intermediate tube sheet to form a shield, thereby forming plural of chambers with the intermediate tube sheet, and forming an expansion joint around the periphery of each of the chambers.

Abstract: An auxiliary reactor for use with a reformer reactor having at least one reaction zone, and including a burner for burning fuel and creating a heated auxiliary reactor gas stream, and heat exchanger for transferring heat from auxiliary reactor gas stream and heat transfer medium, preferably two-phase water, to reformer reaction zone. Auxiliary reactor may include first cylindrical wall defining a chamber for burning fuel and creating a heated auxiliary reactor gas stream, the chamber having an inlet end, an outlet end, a second cylindrical wall surrounding first wall and a second annular chamber there between. The reactor being configured so heated auxiliary reactor gas flows out the outlet end and into and through second annular chamber and conduit which is disposed in second annular chamber, the conduit adapted to carry heat transfer medium and being connectable to reformer reaction zone for additional heat exchange.

Abstract: A hydrogen producing apparatus comprising: a reforming section having a reforming catalyst which causes a reaction between a carbon-containing organic compound as a feedstock and water; a feedstock supply section for supplying the feedstock to the reforming section; a water supply section for supplying water to the reforming section; a heating section for heating the reforming catalyst; a shifting section having a shift catalyst which causes a shift reaction between carbon monoxide and water contained in a reformed gas supplied from the reforming section; and a purifying section having a purifying catalyst which causes oxidation or methanation of carbon monoxide contained in a gas supplied from the shifting section, wherein the shift catalyst comprises a platinum group metal and a metal oxide.

Abstract: An isothermal reactor for carrying out heterogeneous exothermic or endothermic reactions, includes within a catalytic bed (3) housed in an appropriate outer shell (2), at least one tube (13) for the passage of a cooling or heating fluid which advantageously extends within the bed (3) along a plane substantially perpendicular with respect to opposed perforated side walls (4, 5) of the catalytic bed.

Abstract: An isothermal reactor for carrying out heterogeneous exothermic or endothermic reactions, includes within a catalytic bed (3) housed in an appropriate outer shell (2), at least one tube (13) for the passage of a cooling or heating fluid which advantageously extends with a cone shaped helicoidal.

Abstract: A tubular reactor (2) for catalytic reactions with a heat carrier that inside a reactor jacket (10) circulates around a contact tube bundle (8), which extends between a tube plate (4; 6; 80; 82) at the reaction gas inlet side and one at the reaction gas outlet side with gas inlet and gas outlet hoods (12, 14) spanning the face sides of the two tube plates and containing reaction-inhibiting media in the zone of the tube plate on the gas inlet side, characterize themselves in that the reaction-inhibiting media consist entirely or in part of a heat insulation layer (46; 50; 64; 80) with openings for the tube cross-sections on at least one of the two sides of the respective tube plate (4; 60; 82). In this manner, either the respective tube plate (4; 60; 82) is insulated against the hot heat carrier or the reaction gas entering into the reactor is prevented from having contact with the comparatively hot tube plate in order to prevent harmful secondary reactions at the reactor inlet.

Abstract: A reactor, in particular for exothermic reactions, of the type including: a shell (2) of substantially cylindrical shape, at least one catalytic bed (3) in the shell, including a perforated cylindrical outer side wall (4), which forms a free space (8) with the shell, and an inner side wall (5) coaxial to the previous one, a heat exchanger (13) in the bed (3), the heat exchanger (13) being formed by a plurality of tubes (15) in the form of a spiral, a coil or alike in fluid communication with feed and discharge collectors (14, 16) for a cooling fluid.

Abstract: Temperature control and efficient heat transfer are important to producing high quality polymer drag reducing agents from alpha-olefin and/or other monomers. Many polymerization reactions are exothermic, and controlling or minimizing the exotherm combined with low reaction temperatures yields high molecular weight and, for poly(alpha-olefins), high quality drag reducing agent polymers. It has been found that a shell and tube heat exchanger-type reactor, with the inner tubes hosting the reaction mixture and a coolant circulating through the shell side gives good temperature control. The use of appropriate release agents helps to keep the inner reaction chambers from building up any polymer residue. These reactors can be operated in a continuous filling and harvesting mode to facilitate the continuous production of polymer drag reducing agent and related formulations.

Abstract: Installation for the production of synthesis gas from a hydrocarbon feedstock comprising at least one reactor for steam reforming, at least one reactor for converting CO2 that is equipped with at least one feed means by the effluent that is obtained from the steam reforming and at least one other feed means by a gas comprising carbon dioxide, characterized in that at least one reactor for steam reforming or for converting CO2 is heated by a hot gas.

Abstract: A device used as a chemical reactor or heat exchanger in general, with a thin tube plate, of the type in which at least one pipe is connected to a tube plate, this tube plate being closed by a chamber with a container function, wherein this chamber is produced by a section with any shape, with a base which is joined to the plate by a lateral portion; connection elements are also provided between the tube plate and the base of the chamber.

Abstract: Syngas production process and reforming exchanger. The process involves passing a first portion of hydrocarbon feed mixed with steam and oxidant through an autothermal catalytic steam reforming zone to form a first reformed gas of reduced hydrocarbon content, passing a second portion of the hydrocarbon feed mixed with steam through an endothermic catalytic steam reforming zone to form a second reformed gas of reduced hydrocarbon content, and mixing the first and second reformed gases and passing the resulting gas mixture through a heat exchange zone for cooling the gas mixture and thereby supplying heat to the endothermic catalytic steam reforming zone. The endothermic catalytic steam reforming zone and the heat exchange zone are respectively disposed tube side and shell side within a shell-and-tube reforming exchanger.

Abstract: A method for controlling the pseudo-isothermicity of a chemical reaction in a respective reaction zone. (9) in which the use of heat exchangers (6) is foreseen having an operating heat exchange fluid flowing through them and in which heat exchange critical areas (9a) are identified, the method being distinguished by the fact that it reduces and controls, in the critical areas (9a) of the reaction zone, the value of the heat exchange coefficient between the operating fluid and the zone (9), through thermal insulation of the portions (6a, 6b) of such exchangers extending in such areas (9a).

Abstract: A cracking tube includes a lining of a fouling resistant and corrosion resistant iron aluminide alloy. The iron aluminide alloy can include 14-32 wt. % Al, at least 2 vol. % transition metal oxides, 0.003 to 0.020 wt. % B, 0.2 to 2.0 wt. % Mo, 0.05 to 1.0 wt. % Zr, 0.2 to 2.0 wt. % Ti, 0.10 to 1.0 wt. % La, 0.05 to 0.2 wt. % C., balance Fe, and optionally ≦1 wt. % Cr, and the coefficient of thermal expansion of the iron aluminide alloy is substantially the same as the coefficient of thermal expansion over the temperature range of ambient to about 1200° C. of an outer metal layer. A cracking tube utilizing the iron aluminide alloy can be formed from powders of the iron aluminide alloy by consolidation methods including cold isostatic pressing (CIP), hot isostatic pressing (HIP), reaction synthesis, spraying techniques, or co-extrusion with a second material of the cracking tube.

Abstract: Temperature controllers are provided which employ a control element of variable area containing flowing heat transfer fluid. The area of the element available for temperature control is changed by opening and closing a bank of conduits in a cascade and the conduits are opened and closed according to a temperature measuring device in the medium whose temperature is to be controlled.

Abstract: A housing for a heat exchange apparatus including a fluid passageway partially defined by a baffle plate having an extended portion. The heat exchange apparatus further includes an array of fluid conduits extending through the fluid passageway. The housing includes a plurality of housing members each having a wall and at least one flange extending from the wall. The flanges of adjacent housing members are joined at a flange joint, and the flange joint is configured to fixedly receive the extended portion of the baffle plate. The apparatus also includes a plate member is provided within the fluid passageway and intumescent material fills a gap between the baffle plate and the plate member. Additionally, a second baffle plate is provided that defines a portion of a second fluid passageway, where a refractory gasket and a layer of intumescent material are provided between the first and second baffle plates.

Abstract: The temperature distribution of a heating medium in the reactor is allayed and the occurrence of hot spots is repressed. In a shell-and-tube type reactor provided with donut type and disc type baffle plates, reaction tubes are disposed even in the holes formed in the donut type baffle plates and an empty space devoid of a configuration of the reaction tubes is formed at the center of the shell. According to this invention, (meth)acrylic acid and/or (meth)acrolein can be produced at a low energy by catalytic gas phase oxidation of propylene- or isobutylene-containing gas.

Abstract: A compact fuel processing reactor. The reactor includes a housing having an inlet for receiving a process gas and an outlet for a directing a product gas out of the housing. A catalyst bed that includes discrete particles of a refractory material is located within the housing for contacting the process gas. A coiled tubing heat exchanger is at least partially disposed within the catalyst bed for cooling the catalyst bed. The coiled tubing can comprise a smooth continuous outer surface in intimate contact with the discrete particles. The circulating cooling medium comprises water in liquid, gas or a mixture of liquid and gas phases. The discrete particles in the catalyst bed are in intimate contact with at least a portion of the coiled tubing to promote heat transfer from the catalyst bed to the coiled tubing.

Abstract: This invention relates to a compact apparatus for generating hydrogen. More particularly, this invention relates to a compact hydrogen generating apparatus suitable for use in conjunction with a fuel cell. The compact hydrogen generating apparatus comprises a fuel processor reactor having an integrated pre-reforming zone embedded within a secondary reforming zone.

Abstract: An apparatus for carrying out a multi-step process of converting hydrocarbon fuel to a substantially pure hydrogen gas feed includes a plurality of reaction zones arranged in an insulated, box-shaped, compact fuel processor. The multi-step process includes preheating the hydrocarbon fuel utilizing integration with the inherent exothermic processes utilized with the fuel processor, reacting the preheated hydrocarbon fuel to form the hydrogen rich gas, and purifying the hydrogen rich gas to produce a gas that is suitable for consumption in a fuel cell.

Abstract: A cooling system (10) is provided for use with a fuel processing subsystem (12) for reducing a level of carbon monoxide in a reformate flow (14) for a proton exchange membrane fuel cell system (16). The fuel processing subsystem (12) includes first and second preferential oxidizers (18, 20) to oxidize the carbon monoxide carried in the reformate flow. The reformate cooling system (10) includes a coolant flow path (30), a reformate flow path (32), and first, second, third, and fourth heat exchanger core portions (34, 36, 38, 40). The core portions (36-40) are arranged in numbered sequence along the reformate flow path (32) with the first and second core portions (34, 36) located upstream of the first preferential oxidizer (18), and the third and fourth core portions (38, 40) located downstream of the first preferential oxidizer (18) and upstream of the second preferential oxidizer (20).

Abstract: A method of making a micromirror unit is provided. In accordance with the method, a micromirror unit is made from a material substrate having a multi-layer structure composed of silicon layers and at least one intermediate layer. The resulting micromirror unit includes a mirror forming base, a frame and a torsion bar. The method includes the following steps. First, a pre-torsion bar is formed by subjecting one of the silicon layers to etching. The obtained pre-torsion bar is rendered smaller in thickness than the mirror forming base and is held in contact with the intermediate layer. Then, the desired torsion bar is obtained by removing the intermediate layer contacting with the pre-torsion bar.

Abstract: A process and apparatus for contacting reactants with a particulate catalyst while indirectly heating the reactants with a heat exchange medium improves temperature control by using an intermediate heat exchange fluid and system to prevent overheating of reactants and maintain parallel heating characteristics through multiple reaction-heat exchange zones. The internal flow path minimizes the circulation of the reaction zone heat exchange fluid by incorporating interstage reheating of the reaction zone heat exchange fluid as it passes in series flow. A particularly useful application of the process and apparatus is in the dehydrogenation of ethylbenzene to produce styrene. The process and apparatus can also be used with simultaneous exchange of catalyst particles by an operation that restricts reactant flow while moving catalyst through reaction stacks in which the reactant flow has been restricted.

Abstract: The present invention is an apparatus arranged to maximize heat utilization for a hydrocarbon steam reforming process to produce synthesis gas. The apparatus comprises a refractory lined vessel with partition walls that divide the inside of the vessel into (1) a combustion chamber(s) containing one or more burners, and (2) convection chambers used as a means to remove combustion products from the combustion chamber through one or more openings at the opposite end of the burner end. The combustion chamber contains one or more reformer tubes in which a mixed-feed of hydrocarbon and steam flow co-current with combustion products and receive direct radiant heat from the combustion flame through the tube wall. The convection chambers contain a tube-in-tube device filled with catalyst in the annuli.

Abstract: The invention proposes a reactor (1) having a contact tube bundle (2) through whose space surrounding the contact tubes a heat-exchange medium circuit is passed, with ring lines (3, 4) at both ends of the reactor with jacket apertures (5, 6) for the supply and discharge of a heat-exchange medium by means of a pump via an external heat exchanger, where the heat-exchange medium is fed to the lower ring line (4) and is discharged to the heat exchanger via the upper ring line (3), and with baffle plates (7) which leave a passage cross section alternately in the reactor center and at the reactor edge.

Abstract: In a reactor (1) which has a bundle of catalyst tubes (2) and in which a heat transfer medium is circulated through the space surrounding the catalyst tubes, with the ring lines (3, 4) at both ends of the reactor with openings (5, 6) through the wall for introduction or removal of a heat transfer medium by means of one or more pumps, where the heat transfer medium is introduced into the lower ring line (4) and is returned via the upper ring line (3) to the pump(s) and the heat transfer medium or a substream of the heat transfer medium may, if desired, be passed over one or more external heat exchangers, and with deflecting plates (7) which alternately leave free an open cross section in the middle of the reactor and at the edge of the reactor, the lower ring line (4) is divided by means of a horizontal dividing wall (8) into two regions between which material can pass via preferably uniformly distributed openings (9) having a regulatable open cross section.

Abstract: A reactor (1) comprising a shell (2) having a first inlet (3) and outlet (4) and a second inlet (5) and outlet (6). The shell (2) is divided into first and second non-communication volumes (7, 8) by way of a first tube plate (9) which carries a number of tubular elongate pockets (10). The pockets (10) extend generally transversely from the first tube plate (9) into the first volume (7), and the first inlet and outlet (3, 4) are arranged so as to define a flow path through the first volume (7) from the first inlet (3) to the first outlet (4) by way of external surfaces of the pockets (10). A second tube plate (11) extends across the shell (2) in the second volume (8), and supports a number of tubular elongate conduits (12) corresponding to the number of pockets (10). The conduits (12) extends from the second tube plate (11), across the second volume (8) and into the pockets (10). The conduits (12) are opened-ended and extend almost, but not quite, to the ends of the pockets (10).

Abstract: Process and plant for the production of synthesis gas, hydrogen and/or reducing gas by means of a primary reformer heated on the shell side, used in conjunction with a pressure swing adsorption unit for purifying the product gas, the purpose of which is to find a solution to the problem of utilising the work potential of the fuel gas from the pressure swing adsorption unit, which is used to fire the primary gas reformer. This is achieved by supplying the waste desorption gas from the pressure swing adsorption unit to the inlet side of an ejector, which is driven by a part stream of the fuel gas for the primary reformer, the waste desorption gas being admixed to a main fuel gas stream and/or a regulating gas stream, depending on the particular mode of operation.

Abstract: A heat exchanger (E) for systems having a heat generating furnace (F) includes at least one heat exchanging arm (10) formed from an inner (12) and an outer (14) concentric tube with an inner (16) and outer (18) passageway separated by a common wall (20). The inner concentric tube (12) has a first end (22) with a fluid flow outlet (24) for discharging an exhaust fluid (26) and a second end (28) with a fluid flow inlet (30) for receiving an input (32) of the exhaust fluid. The outer concentric tube (14) has a first end (34) with a fluid flow (36) inlet for receiving an input of an intake (38) fluid flow and a second end (40) with a fluid flow outlet (42) for discharging the intake fluid (38). The exhaust fluid (26) flows through the inner concentric tube (12) in a direction substantially opposite to the intake fluid flow (38) through the heat exchanger arm (10).

Abstract: A synthetic gas manufacturing plant includes a reformer having a reaction tube, a combustion radiation unit arranged around the reaction tube to heat the reaction tube, and a convection unit communicating with the combustion radiation unit, a source gas supply passageway to supply a natural gas to the reformer, a steam supply passageway to supply steam to the source gas supply passageway, a carbon dioxide recovery apparatus to which a total amount of combustion exhaust gas flowing through the convection unit of the reformer is supplied, and which recovers carbon dioxide from the combustion exhaust gas, a compressor to compress the recovered carbon dioxide, and a return passageway to supply part or the whole of the compressed carbon dioxide from the compressor to the source gas supply passageway.

Abstract: A process for preparing saturated carboxylic acids having from 1 to 4 carbon atoms at a reaction temperature of from 100° C. to 400° C. and pressures of from 1.2×105 Pa to 51×105 Pa by gas phase oxidation of saturated and/or unsaturated C4-hydrocarbons, with an oxygen-containing gas and water vapor in the presence of at least one catalyst. The gas leaving the reactor is partly recirculated in a reaction gas circuit. This reaction gas circuit is configured such that part of the organic acids formed in the gas-phase oxidation is taken from the gas leaving the reactor so that the acid content of the recirculated part of the gas leaving the reactor is from 0.01% to 6.0% by volume.

Abstract: A method for measuring the temperature of fluid masses being treated in a tubular reactor apparatus which comprises carrying out the treatment in reactor apparatus comprises at least two same-type tubular reactors which are filled with solid particles, at least one tubular reactor containing a temperature measuring unit, the tubular reactors being designed such that both the ratio of the mass of the solid particles to the free cross-sectional area of the respective tubular reactor and the pressure drop measured by an inert gas being conducted transversely to the free cross-sectional area are each substantially identical across the respective tubular reactor. The apparatus is suitable for treating fluid masses while generating or consuming thermal energy, the temperature being measured.

Abstract: A method for producing hydrate includes supplying hydrate producing substance in a gas state into an aqueous phase in a hydrate producing vessel, thereby providing the hydrate producing vessel having a gaseous phase including the hydrate producing substance and the aqueous phase, and spraying water including methane dissolved therein into the gaseous phase containing the hydrate producing substance in the hydrate producing vessel, thereby reacting the water and the hydrate producing substance to produce hydrate.

Abstract: The invention relates to a device for reforming educts containing hydrocarbons, having a radiation burner and a reforming reactor, which contains, at least in part, metal honeycomb bodies having a catalyst coating, and which can in particular be used to produce hydrogen from fossil energy carriers. The invention should thereby be able to convert educts containing hydrocarbons into synthesis gases with high efficiency, in particular in a low-power range. For this purpose, a radiation burner is used that heats a two-part reforming reactor by radiation and convection. The radiation burner and the two parts of the reforming reactor are thereby arranged and constructed in such a way that the radiation burner surrounds the two parts of the reforming reactor, and the educt gas and smoke gas can be conducted in counter-current between the two parts of the reforming reactor.

Abstract: A steam reformer that produces hydrogen gas from water and a carbon-containing feedstock, such as an alcohol or a hydrocarbon. The steam reformer includes a hydrogen-producing region, in which a mixed gas stream containing hydrogen gas and other gases is produced from water and a carbon-containing feedstock. The steam reformer includes a separation region, in which the mixed gas stream is separated into a hydrogen-rich stream containing at least substantially pure hydrogen gas, and a byproduct stream containing at least a substantial portion of the other gases. In some embodiments, the steam reformer is a vertically oriented fuel processor. In some embodiments, the separation region includes at least one hydrogen-selective membrane. In some embodiments, the steam reformer further includes a polishing region, in which the hydrogen-rich stream produced in the separation region is further purified. In some embodiments, the reformer includes an external metal or sealed ceramic shell.