Abstract: A reactor (1) for carrying out exothermic or endothermic heterogeneous reactions comprising an outer shell (2) of substantially cylindrical shape and at least a heat exchanger (9) embedded in a catalytic layer (10) supported in said shell (2), is characterized in that the heat exchanger (9) is a plate (14) heat exchanger.

Abstract: A fluidized-bed reactor for the oxychlorination of ethylene, oxygen and HCL, comprises a heat exchanger, having tube packets in the fluidized-bed for releasing the heat evolved from exothermic reaction to a heat-transfer medium in the tube packets, in particular to water/steam. The tube packets come into contact with water via a ring pipe and the steam being removed via a ring pipe to provide an economical solution with which expensive drilled passages are avoided, the calculation for ring pipes is facilitated and a large number of wall passages is dispensed with. This is achieved by the ring pipe being mounted as a collector or chamber directly on the reactor wall.

Abstract: A fuel evaporator composed of an evaporation chamber which evaporates a raw liquid fuel by a high temperature thermal medium to provide a raw fuel gas is disclosed. The evaporation chamber comprises a plurality of evaporation chambers serially connected to each other in a ventilation manner, and at least one raw liquid fuel injector for injecting the raw liquid fuel being provided on each of said plurality of evaporation chambers.

Abstract: A cooled discharge unit of an apparatuses for processing homogeneous/heterogeneous radioactive wastes with ion-exchange resins. The cooled discharge unit has a discharge pipe, a cooling jacket having a U-shaped form in cross section, a collector for feeding a coolant into the jacket, a discharge gate having a pipe, on one end of which is a cone-shaped tip and on the other end of which is a lid with an aperture.

Abstract: A method of producing syn gas from biomass or other carbonaceous material utilizes a controlled devolatilization reaction in which the temperature of the feed material is maintained at less than 450° F. until most available oxygen is consumed. This minimizes pyrolysis of the feed material. The method and apparatus utilizes the formed synthesis gas to provide the energy for the necessary gasification. This provides for a high purity syn gas and avoids production of slag.

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: Tubes within a radiant heating section of a coking furnace are arranged differently than in a single vertical column and connected together in a simple, planar serpentine pattern. The tubes are arranged in a plurality of offset or staggered vertical columns. This arrangement permits the upper tubes to be close to the radiant heat source and allows the tube bends connecting adjacent tubes to be of greater radius, so that the pressure at which the feedstock is passed through the tube bundle can be lower allowing more vaporization of the cracked process fluids.

Abstract: Process for the preparation of urea from ammonia and carbon dioxide in which a urea synthesis solution containing urea, ammonium carbamate and unconverted ammonia is formed in a synthesis zone, a part of the urea synthesis solution being transferred from the synthesis zone to a medium-pressure treatment zone operating at a pressure of 1-4 MPa, and a gas stream from the medium-pressure treatment zone being absorbed into the low-pressure ammonium carbamate solution from the urea recovery section.

Abstract: A reactor (1) of high cylindrical construction for continuously carrying out gas-liquid, liquid-liquid or gas-liquid-solid reactions, provided with a downward-directed jet nozzle (2) via which the starting materials and the reaction mixture are fed in and which is located in the upper region of the reactor, and provided with an offtake (3), preferably in the lower region of the reactor, via which the reaction mixture is conveyed via an external circuit back to the jet nozzle (2) by means of a pump (P), wherein a guide tube (4) which extends essentially over the total length of the reactor (1) with the exception of the reactor ends and has a cross-sectional area in the range from one tenth to one half of the cross-sectional area of the reactor (1) is located concentrically in the reactor (1), and the jet nozzle (2) is located above the upper end of the guide tube (4), preferably at a distance of from one eighth of the guide tube diameter to one guide tube diameter, or projects into the guide tube (4) to a dept

Abstract: A precooler for use in a fuel cell system between a thermal reformer and a shift converter includes an atomizing water inlet in combination with a swirling inducing reformed gas inlet which act to increase the resistance time of the reformed gas in the precooler so as to effectively cool same.

Abstract: For carrying out a heterogeneously catalyzed reaction, such as the generation of hydrogen from hydrocarbons or alcohol, a reaction mixture comprising a hydrocarbon and water is supplied to a catalyst, which is produced by pressing at least one catalyst powder into a layer. Instead of a metallic housing, stacked layers are sealed by an edge seal, introduced into the layer or applied on the layer.

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: Device for connecting a heat exchange pipe (4), whereby said pipe (4) is positioned between walls (11) that are located on both sides of pipe (4), intended for heating and/or cooling a reactor, whose internal pressure is considerably higher than the atmospheric pressure and than the pressure that prevails inside said pipe (4), and said reactor, whereby said device comprises a series of cooperating means that comprise: means for connecting this pipe (4) and jacket (2a) of said reactor, whereby said means comprise a packing box (21, 22, 23), a flange (28) that is attached to jacket (2a) of the reactor by means of a joint (18), a bellows (25) that is placed between packing box (21, 22, 23) and said flange (28) to ensure a relatively flexible connection between pipe (4) and jacket (2a) of the reactor. FIG. 3 to be published.

Abstract: A continuous flow chemical reaction apparatus comprises a tubular reactor having a length and having a first fluid reactant inlet at a first end and a product outlet at a second end, said tubular reactor having a central tube/interior conduit extending lengthwise within said tubular reaction zone, said conduit having at least one injector within the length of said conduit, said injector capable of introducing a controlled amount of a second fluid reactant into said tubular reactor.

Abstract: A reaction system comprising a reactor containing a reaction process medium and a heat exchanger providing a conduit through which flows a heat transfer fluid in which measurement of the flow and temperature change of the heat transfer fluid across the reaction is used to determine the heat generated or absorbed by the reaction system and that determination is used to monitor and control the reaction wherein

Abstract: In apparatus for heat exchange to and from a body surface using a heat transfer liquid a heat exchanger comprises a plurality of elements within a casing connected axially against one another with spacer tube elements. Each element has its periphery spaced from the body surface to provide a flow gap for heat transfer fluid in heat exchange contact with the surface. The element have plenums separating each from one another forming connecting flow spaces for the heat transfer liquid between the heat transfer flow gap and inlet and outlet passages passing through the body. A preferred apparatus is a cylindrical rotor within a cylindrical stator with an annular processing space between them, the rotor containing a stack of heat exchange elements of the respective shape permitting high heat flux rates and uniform temperature distribution over the total rotor heat transfer surface.

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 fuel gas reformer assemblage for use in a fuel cell power plant is formed from a composite plate assembly which includes spaced-apart divider plates with columns of individual gas passages. The reformer assemblage is constructed from a series of repeating sub-assemblies, each of which includes a core of separate regenerator/heat exchanger gas passages. The core in each sub-assembly is sandwiched between a pair of reformer gas passage skins, which complete the assembly. Adjacent reformer gas/regenerator/reformer gas passage sub-assemblies in the composite plate assembly are separated from each other by burner gas passages. The regenerator/heat exchanger gas passages and the reformer gas passages in each sub-assembly are connected by gas flow reversing manifolds which form a part of each sub-assembly.

Abstract: A system and method for performing hydrothermal treatment includes a scraper formed as a hollow cylinder. The scraper is positioned in the reactor vessel with the scraper axis substantially co-linear with the longitudinal axis of the cylindrical reactor vessel. A mechanism is provided to rotate the scraper about the longitudinal axis of the reactor vessel. One or more elongated scraper bars are positioned inside the reactor vessel between the scraper and the longitudinal axis of the reactor vessel. Each scraper bar may be held stationary with respect to the reactor vessel, or each scraper bar may rotated relative to an axis passing through the scraper bar to remove any solids that have accumulated on the scraper or on the scraper bar. To prevent accumulation of precipitating solids on the scraper bar itself, each scraper bar may have internal cooling channels or the capability of releasing a purging fluid.

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: An arrangement for a fluid distributor-contactor-type reactor uses perforated plates to circulate two reactants in alternate channels defined by spaces between parallel stacked plates to perform controlled distribution and mixing simultaneously with optional indirect heat transfer. One reactant enters one set of channels that serve as reaction channels. A set of second channels interleaved with the reaction channels serve as distribution channels that also provide a heat exchange function. Finely dispersed openings in the perforated plates distribute the reactant at low concentration from the distribution channels into the reaction channels. Dispersal of the reactant through the perforations will enhance the turbulence that is primarily introduced by the corrugated plates to insure good mixing of the reactants in the reaction channels.

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: There is provided a reforming apparatus which shows high efficiency and excellent operation-starting performance, in spite of its compact body and simple structure.

Abstract: The present invention is directed towards a fired heater for heating a process fluid that uses U tubes provided with increased internal heat transfer surface to reduce tube metal temperatures and coking. and at the same time is not prone to plugging from coke. The fired heater comprises a radiant section enclosure with a number of U tubes in the radiant section. The U tubes are formed by connecting one or more tubular sections, and the U tubes are provided with internal generally longitudinal fins. The invention also is directed towards a process utilizing a fined heater with U tubes as disclosed for producing olefins from hydrocarbon feedstocks.

Abstract: A reforming and hydrogen purification system operating with minimal pressure drop for producing free hydrogen from different hydrogen rich fuels includes a hydrogen reforming catalyst bed in a vessel in communication with a core unit containing a hydrogen permeable selective membrane. The vessel is located within an insulated enclosure which forms an air inlet passageway and an exhaust passageway on opposite sides of the vessel. Air and raffinate pass through a burner within the air inlet passageway, providing a heated flue gas to heat the catalyst to the reaction temperature needed to generate free hydrogen from the feedstock. The burner flue gas flows laterally over and along the length of the bed between the input and output ends of the bed. Hydrogen is recovered from the core for use by a hydrogen-consuming device such as a fuel cell. The remaining unrecovered hydrogen in the reformed gases is contained in raffinate and is used to supply process heat via the burner.

Abstract: A process and apparatus for indirectly exchanging heat with narrow channel in a heat exchange type reaction zone uses manifold space to interconnect the common ends of channels and to provide controlled distribution of additional reactants. The invention simplifies the operation and construction of the heat exchanging type reaction zone by directly communicating reaction channels and/or heating channels with a manifold located at the end of the channels. The manifold can provides the extra function of mixing additional reactants. The invention promotes simplified intermediate injection of reactants over tube and shell heat transfer arrangements that have been used for similar purposes. Improved process control has particular benefits for exothermic reactions. The narrow channels are preferably defined by corrugated plates. The reaction channels will contain a catalyst for the promotion of the primary reaction.

Abstract: A system and method for the selective catalytic reduction of nitrogen oxide in a furnace exhaust includes cooling the furnace exhaust in a first heat recovery section to a temperature between 400° F. and 500° F., introducing a reducing agent into the exhaust gas and reacting the nitrogen oxide in the exhaust gas with the reducing agent in the presence of an SCR catalyst in a reactor positioned in the furnace stack. The treated gas emerging from the reactor can be further cooled in a second heat recovery section. The system and process is particularly suitable for use in conjunction with furnaces for thermally cracking hydrocarbon feedstock to produce olefin. The feedstock is preferably preheated in the heat recovery sections prior to introduction into the furnace.

Abstract: According to the present invention, a temperature profile within a preferential oxidation reactor is controlled using a two phase water/steam system to provide a temperature range within the reactor (10) which favors the selective oxidation of CO in a hydrogen rich reformate stream. The reformate is flowed in a mixture with oxygen over a preferential oxidation catalyst (17). The temperature profile is controlled by flowing a stream of water proximate to the preferential oxidation catalyst (17) so as the stream of water and the reformate stream passing over the catalyst (17) are in a heat transfer arrangement. The stream of water is maintained as a two phase stream from a point at which the water reaches its boiling temperature to a point proximate an outlet from which the stream of water exits the reactor (10).

Abstract: A process and apparatus for contacting reactants with a particulate catalyst while indirectly contacting the reactants with a heat exchange medium performs heat exchange in a first reaction zone and moves catalyst, at least intermittently, through the second reaction zone while the process is operating. The first reaction zone is preferably a fixed bed reaction zone. The use of first reaction zone as a fixed bed reaction zone simplifies the process arrangement by not requiring means for catalyst movement in a reaction zone that performs simultaneous heat exchange. Long periods of operation are possible since the first reaction zone will typically experience a slow rate of catalyst deactivation and need infrequent regeneration. The first reaction zone may also be designed for catalyst movement, but independently controlled from the first reaction zone to facilitate the movement of catalyst therethrough.

Abstract: The invention relates to a reactor for carrying out reactions having a high enthalpy change containing catalyst particles between cooled dividing walls. According to the invention, the cooled dividing walls are formed by metal plates/metallic components in which hollow or intermediate spaces in the form of channels are provided in the metal plates/components for accommodating and conveying a cooling medium so as to cool the reactor. The reactor can be used for carrying out strongly exothermic catalytic reactions, for example for the selective hydrogenation of acetylene to ethylene.

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 reformer includes an evaporation portion for evaporating a raw material, a reforming portion for producing a reformed gas whose principal element is hydrogen from the raw materials, a CO reduction portion for reducing CO involved in the reformed gas, a circulating conduit portion having a storage tank for storing the raw material, a feeding device for feeding the raw material under pressure, a cooling device for cooling the CO reduction portion and a supply device for supplying the raw material to the evaporation portion. The supply device includes a conduit branched from the circulating conduit portion connected to the evaporation portion and a flow control device provided in the conduit.

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

Abstract: A plant for transformation of polyolefine wastes into useful hydrocarbons is provided which comprises a reactor in a shape of a vertical tank provided with an inlet charging hole, connected to a polyolefine raw material and catalyst dosing device, product vapour receiving pipe, a mixer and a liquid level regulation system, and a distillation column. In addition, a reactor is provided with a heating system in a form of a combustion chamber (8) surrounding a tank from below, and the chamber (8) is heated with at least one burner (9), supplied with reaction products.

Abstract: A tubular reactor with a catalyst bed and inserts placed within the tubes redirecting the flow from the center to the wall of the tube. The redirected flow increases the amount of heat transfer through the system by moving the reactants from the low heat transfer zone at the center of the tube to the high heat transfer zone at the wall of the tube. In one embodiment, the tubular reactor comprises a tubular reactor having a series of tubes, within the tubes are a plurality of flow obstructing inserts and a catalyst bed. The inserts may comprise a plurality of inclined, conical, or spiral plates. The plates may be affixed to the wall of the tube and may depend on the catalyst bed for structural support.

Abstract: Apparatus for radial flow reactor and methods of using the reactor for catalytic hydrocarbon processing. The reactor, of annular shaped housing, contains a core region with a heat exchange means. The core region is surrounded by a catalyst bed held by inner and outer walls. The core region and radial catalyst bed are further surrounded by an annular zone containing heat exchange means.

Abstract: A hydrocarbon fueled hydrogen generator and hydrogen fueled electric power generating system and apparatus comprising hydrocarbon fuel and oxidizer delivery and mixing apparatus, ignition and combustion apparatus igniting the mixture of fuel and oxidizer, apparatus receiving and conducting the gases of combustion through a sulfur absorbing unit and removing sulfur from the gases, a steam reformer unit reforming carbon monoxide gas into hydrogen gas and carbon dioxide gas, a carbon monoxide scavenger unit reforming residual carbon monoxide gas to hydrogen gas and carbon dioxide gas; apparatus receiving the hydrogen gas and carbon dioxide gas and operating to liquefy and separate the carbon dioxide gas from the hydrogen gas; and, structure to hold and deliver the liquid carbon dioxide to useful end; and structure to hold and deliver hydrogen gas to the anode of a hydrogen fueled electric power generating fuel cell.

Abstract: A compact fuel processor for converting a hydro-carbonaceous fuel into hydrogen and carbon dioxide comprising in series a hydrocarbon converstion zone (5) for converting the hydro-carbonaceous fuel into a product gas comprising carbon monoxide and hydrogen, a water-gas shift reaction zone (6) containing a catalyst suitable for the water-gas shift conversion reaction, an auxiliary water-gas shift reaction zone (7) containing a catalyst suitable for the water-gas shift conversion reaction, and a carbon monoxide removal zone (8). The invention further relates to a fuel cell system comprising such a fuel processor and a fuel cell and to the use of such a fuel processor or such a fuel cell system.

Abstract: A polymerization reactor comprises a heat pipe jacket for the removal of large heat fluxes and capable of maintaining essentially isothermal conditions without the use of complicated and maintenance intensive circulation heat exchangers or internal coils. This isothermal reactor is useful particularly when polymerization is conducted in multiphase system and/or when the rate of reaction is high and when consistent polymer properties are desired.

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: A polymerization reactor for exothermic liquid phase reactions comprises a reaction zone which is divided into a plurality of channels by thermally conductive heat transfer fins which are conductively mounted on one or more heat pipes for the removal of heat of reaction from reactants and reaction products flowing between the heat transfer fins. The reactor of the invention is capable of maintaining essentially isothermal conditions without the use of complicated and maintenance intensive agitators. The reactor is particularly useful when viscosity of the reactants and/or reaction products is high, when the reaction conducted has a fast reaction rate and when consistent polymer properties are desired.

Abstract: The distillation plant comprises a column (1) and a heat pump (4, 5) which operates between a sump vaporizer (3) and an exhaust vapor compressor (2) of the column. The heat pump is substitutable by devices (6, 7) which can be switched to the sump vaporizer and the exhaust vapor compressor when required. These substituting devices comprise devices (6 and 7 respectively) for the production of vapor or the provision of a coolant respectively as well as connection means (63, 63′, 72, 72′). The coolants can be liquids (water) or gases (air).

Abstract: A housing containing two or more individual operating components called modules is disclosed. The modules themselves are independently contained in one or more vessels with attendant connectivity structures such as pipes, tubes, wires and the like. Each such vessel or device is configured to conduct at least one unit reaction or operation necessary or desired for generating or purifying a hydrogen enriched product gas formed from a hydrocarbon feed stock. Any vessel or zone in which such a unit operation is conducted, and is separately housed with respect at least one other vessel or zone for conducting a unit operation, is considered a module.

Abstract: The invention concerns a method for producing carbon monoxide by reverse conversion, in gas phase, of carbonic acid gas and gaseous hydrogen while minimising the production of methane. The invention is characterised in that the reaction is carried out at a temperature between 300 and 520° C. and under pressure between 10 to 40 bars in the presence of an iron-free catalyst based on zinc oxide and chromium oxide. Said method is preferably carried out continuously and comprises preferably the following steps which consist in: a) preparing a gas mixture rich in carbon dioxide and in hydrogen having a temperature between 300 and 520° C.

Abstract: An apparatus and method for producing sulfur comprises a vessel containing a plurality of spaced-apart channels each having an upstream end communicating with an upstream manifold and a downstream end communicating with a downstream manifold. Each channel comprises a single, continuous, uninterrupted conversion stage terminating at the downstream channel end. A first mixture, of SO2 and air from the sulfur burner, is introduced into the upstream manifold and flows as a stream through each of the channels where the stream is cooled and the SO2 is converted in the conversion stage to SO3 to produce, at the downstream channel end, a second mixture consisting essentially of SO3 and air. The first mixture is not cooled between the sulfur burner and the converter. The stream flowing through the conversion stage is maintained at a temperature which sustains conversion of SO2 to SO3, without diluting the stream with a cooling fluid or diverting the stream outside the channel contained in the converter vessel.