Abstract: The ammonia synthesis system of the present invention includes an ammonia synthesis reaction unit that synthesizes ammonia from nitrogen and hydrogen; an ammonia cooler that cools an ammonia-containing gas discharged from the ammonia synthesis reaction unit; a gas-liquid separator that separates ammonia liquefied by the ammonia cooler from a circulated gas; and an ammonia synthesizing gas supplying unit that supplies nitrogen gas and hydrogen gas, the circulated gas being supplied to the ammonia synthesis reaction unit, the circulated gas supplied to the ammonia synthesis unit having an ammonia gas concentration of 3% by volume or more. The method for producing ammonia of the present invention includes reacting nitrogen and hydrogen using a circulated gas having an ammonia gas concentration of 3% by volume or more and using an ammonia synthesis catalyst under a condition of a reaction pressure of 10 MPa or less to produce ammonia.

Abstract: An ammonia synthesis converter for small production units which provides full access for routine maintenance and catalyst replacement while providing adequate catalyst pressure drop to ensure kinetic performance and reduce heat leak from the catalyst beds. A shell has a removable top head and an annular basket is removably mounted in the shell. First and second catalyst beds are disposed in the annular zone of the basket for axial down-flow in series. A quench gas is introduced into effluent from the first catalyst bed and the resulting mixture into a top of the second catalyst bed. A feed-effluent interchanger in the inner basket zone is adapted to receive effluent from the second catalyst bed and indirectly heat a feed to the first catalyst bed. Also, methods of operating and servicing the converter.

Abstract: A system for production of hydrogen includes a steam methane reformer (SMR) including an outer tube, wherein a first end of the outer tube is closed; and an inner tube disposed in the outer tube, wherein a first end of the inner tube is open. An SMR flow channel is defined within the inner tube and an annular space is defined between the outer tube and the inner tube. The flow channel is in fluid communication with the annular space. The SMR includes a foam disposed in the annular space. The system includes a water gas shift reactor comprising a reaction tube, wherein a reaction channel is defined within the reaction tube, and wherein the reaction channel is in fluid communication with the SMR flow channel; a heat transfer material disposed in the reaction channel; and a catalyst disposed in the reaction channel.

Abstract: A system for production of hydrogen includes a steam methane reformer (SMR) including an outer tube, wherein a first end of the outer tube is closed; and an inner tube disposed in the outer tube, wherein a first end of the inner tube is open. An SMR flow channel is defined within the inner tube and an annular space is defined between the outer tube and the inner tube. The flow channel is in fluid communication with the annular space. The SMR includes a foam disposed in the annular space. The system includes a water gas shift reactor comprising a reaction tube, wherein a reaction channel is defined within the reaction tube, and wherein the reaction channel is in fluid communication with the SMR flow channel; a heat transfer material disposed in the reaction channel; and a catalyst disposed in the reaction channel.

Abstract: A heat exchanger for a steam generator according to one embodiment of the present invention comprises a plate and channels formed on the plate by an photo-chemical etching method, wherein the channels comprise: a primary heat transmission section formed in a manner of having a bent or curved flow path so as to be extended longer than the length at which one side and the other side are connected in a straight line; and a flow path resistance section, formed having a smaller width than the width of the channels formed on the primary heat transmission section and being connected to the one side of the primary transmission section in a manner of having a bent or curved flow path so as to be extended longer than the length at which an inlet and an outlet are connected in a straight line.

Abstract: A system and method for supplying an energy grid with energy from an intermittent renewable energy source having a production unit for producing Hydrogen and Nitrogen, a mixing unit configured to receive and mix the Hydrogen and the Nitrogen produced by the production unit, an Ammonia source for receiving and processing the Hydrogen-Nitrogen-mixture, an Ammonia power generator for generating energy for the energy grid, a heat distribution system with one or more heat exchangers, and an Ammonia cracker, which is fluidly connected to the Ammonia storage vessel and to the Ammonia power generator, and which is configured and arranged to receive Ammonia from the Ammonia storage vessel, to effect a partial cracking of the received Ammonia to form an Ammonia-Hydrogen-mixture and to direct the Ammonia-Hydrogen-mixture to the Ammonia power generator for combustion.

Abstract: The present invention provides a process of coproducing methanol and ammonia by using natural gas, LPG, butane, or naphtha as a raw material, having a methanol production process (A) composed of specific steps and an ammonia production process (B) also composed of specific steps.

Abstract: Described herein is an apparatus for the synthesis of ammonia from a synthesis gas containing N2 and H2, comprising at least one first reactor. The apparatus comprises a first non-cooled catalyst bed unit, at least one heat exchanger apparatus, and at least two cooled catalyst bed units. Each cooled catalyst bed unit is equipped with a plurality of cooling pipes. The apparatus further comprises a circuit line having at least one feed apparatus and at least one outlet apparatus, wherein the circuit line, starting from the feed apparatus, comprises in consecutive downstream arrangement the plurality of cooling pipes, the first non-cooled catalyst bed unit, the at least one heat exchanger apparatus, and the at least two cooled catalyst bed units up to the outlet apparatus.

Abstract: Systems and methods for producing syngas and ammonia are provided. The method can include reforming a hydrocarbon in a first reaction zone in the presence of one or more first catalysts and steam at conditions sufficient to produce an effluent comprising a portion of the hydrocarbon, carbon monoxide, carbon dioxide, and hydrogen. The effluent can be reformed in a second reaction zone in the presence of one or more second catalysts and nitrogen at conditions sufficient to produce a syngas comprising methane, hydrogen, nitrogen, carbon monoxide, and carbon dioxide, or any combination thereof. At least a portion of the nitrogen and hydrogen in the syngas can be converted to ammonia to produce an ammonia effluent. The ammonia effluent can be separated to produce an ammonia product and a purge gas comprising nitrogen. At least a portion of the purge gas can be recycled to the hydrocarbon, the effluent, or a combination thereof.

Abstract: Process for the production of ammonia from a hydrocarbon feedstock all steam produced in the waste heat boilers of the reforming and ammonia section of the plant is superheated in one or more steam superheaters located downstream the ammonia converter in the ammonia section of the plant. There is no need for steam superheater (s) in the reforming section of the plant to cool the synthesis gas. A steam superheater for use in the process is also provided. The superheater comprises two compartments in which the first and second compartments are connected in series with respect to the steam flow and in parallel with respect to the process gas flow.

Abstract: Systems and processes for producing one or more products from syngas are provided. A feedstock can be gasified in the presence of an oxidant to provide a syngas comprising carbon dioxide, carbon monoxide, and hydrogen. At least a portion of the syngas can be combusted to provide an exhaust gas. At least a portion of the exhaust gas can be introduced to a channel having one or more reaction zones at least partially disposed therein, wherein the one or more reaction zones are in indirect heat exchange with the exhaust gas, wherein the one or more reaction zones comprises one or more catalyst-containing tubes. A reactant can be reacted in at least one of the one or more reaction zones to provide one or more reactor products.

Abstract: Systems and methods for producing ammonia. Nitrogen and hydrogen can be supplied to a reaction zone disposed inside an inner shell. The inner shell can be disposed inside an outer shell such that a space is formed therebetween. The reaction zone can include at least one catalyst bed in indirect heat exchange with the space. The nitrogen and hydrogen can be reacted in the reaction zone in the presence of at least one catalyst to form an effluent comprising ammonia. The effluent can be recovered from the inner shell and cooled to provide a cooled effluent stream. A cooling fluid can be provided to the outer shell such that the cooling fluid flows through at least a portion of the space and is in fluid communication with the exterior of the inner shell. At least a portion of the cooled effluent can provide at least a portion of the cooling fluid. The cooling fluid can then be recovered from the outer shell as an ammonia product.

Abstract: The invention relates to a method for extracting hydrogen from a gas containing methane, especially natural gas. Hydrocarbons contained in the gas are catalytically broken down in a reformer (4) by steam in order to form hydrogen, carbon monoxide and carbon dioxide. Catalytic conversion of the obtained carbon monoxide with steam occurs in a downstream conversion step in order to form carbon monoxide and water. Carbon dioxide is removed from the converted gas flow (8) by gas washing (7), and the washed hydrogen-rich gas flow (10) is subsequently divided in a pressure-swing adsorption system (11) into a product gas flow (12) made of hydrogen and a waste gas flow (13). The waste gas flow (13) is introduced with hydrogen (14), which is separated from the gas flow (10) after gas washing, into a reformer (4) which is essentially a carbon-free combustible gas, and is combusted there. The invention also relates to a system for carrying out the method.

Abstract: Ammonia is produced in a reactor 22, 24, 246, 248, 250 or 252, in which pseudoisothermal conditions can be approached by convective cooling of a reaction zone of the reactor by positioning at least a portion of the reaction zone in indirect contact with a flow of hot gas such as exhaust gas 18 or preheated air. The hot gas 18 may be supplied from a fired heater, a boiler 10, a reformer 202, a process air preheat furnace, a gas turbine, or the like. The reactor converts a feed stream of a purge gas 12 or syngas to ammonia. The method may be implemented in a primary synthesis loop (as at 246, 248, 250, 252) or in a purge gas loop 12 of a new ammonia plant, or by retrofitting an existing ammonia plant. Cooperatively installed with a primary ammonia synthesis loop, the reactor increases total ammonia production.

Abstract: A horizontal chemical reactor comprises at least one catalytic bed (5a-5d) arranged horizontally in the reactor and comprising a lower gas-permeable wall (6) for gas outlet, and a holding element (2) of the at least one catalytic bed.

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: Ammonia is produced from a synthesis gas containing nitrogen and hydrogen on a granular catalyst in at least one reactor at pressures in the range from 50 to 300 bar and temperatures in the range from 100 to 600° C. A product mixture containing NH3 vapor is withdrawn from the reactor, is cooled, and ammonia is condensed and separated. There is obtained a recycle gas to which fresh synthesis gas is admixed, the recycle gas being recirculated to the reactor as synthesis gas. Unreacted synthesis gas is passed through a first catalyst bed free of cooling tubes and subsequently as partly reacted synthesis gas with an NH3 content of 5 to 20 vol-% as heating fluid through a heat exchanger. Partly reacted synthesis gas is passed through at least one further catalyst bed, through which extend cooling tubes. Unreacted synthesis gas is passed as cooling gas through the cooling tubes of the further catalyst bed, and cooling gas heated to 300 to 500° C. is introduced into the first catalyst bed.

Abstract: Transition metal doped II–V nitride material films exhibit ferromagnetic properties at or above room temperature. A III–V nitride material film may be doped with a transition metal film in-situ during metal-organic chemical vapor deposition and/or by solid-state diffusion processes. Doping of the III–V nitride material films may proceed in the absence of hydrogen and/or in the presence of nitrogen. In some embodiments, transition metal-doped III–V nitride material films comprise carbon concentrations of at least 1017 atoms per cubic centimeter.

Abstract: Process for the preparation of ammonia comprising steps of contacting an ammonia synthesis gas with an ammonia synthesis catalyst arranged as reaction zone in one or more catalyst tubes; cooling the reaction zone by heat conducting relationship with a cooling agent; and withdrawing an ammonia rich effluent stream from the reaction zone.

Abstract: An improved method for synthesizing a double metal cyanide (DMC) catalyst combines and sonicates aqueous and non-aqueous solutions of a first metal salt, such as Zn(OAc)2, of a second metal salt, such as CoCl2, and of an alkali metal cyanide, such as NaCN, to synthesize the DMC catalyst, Zn3[Co(CN)6]2. An improved method of producing a polyether polyol uses the DMC catalyst to produce the polyol.

Abstract: The invention relates to a process for the production of ammonia from synthesis gas, the synthesis of ammonia from synthesis gas taking place in several lined-up synthesis systems, whereby ammonia is produced from a portion of the synthesis gas in each system with a part-stream being withdrawn and the respective downstream synthesis system being operated at a higher pressure than the respective upstream synthesis system.

Abstract: A method for producing ammonia from natural gas, fed to an autothermic reformer with an O2 rich gas. Crude synthesis gas is produced at temperatures of 900 to 1200° C., pressures of 40 to 100 bar and in the presence of a cracking catalyst. The crude synthesis gas is led through a catalytic conversion system to convert CO to H2, thereby obtaining a conversion synthesis gas with a H2 content of at least 55 vol.-% and a CO content of not more than 8 vol.-%. The conversion synthesis gas is subjected to a gas purification to remove CO2, CO and CH4, thereby producing an N2-H2 mixture that is subjected to a catalytic ammonia synthesis. The ammonia produced can at least be partially converted to urea by reacting it with CO2.

Abstract: Process and reactor for the preparation of ammonia at elevated pressure and temperature in an ammonia reactor, wherein a process stream of ammonia synthesis gas is successively passed through at least three catalyst beds with intermediate cooling of partially reacted synthesis gas leaving the catalyst beds by heat exchange in heat exchangers arranged between each catalyst bed. The process stream is obtained by combining prior to introduction into a first catalyst bed, a first feed stream of synthesis gas having been preheated through indirect heat exchange during the intermediate cooling of the partially converted synthesis gas and a second feed stream of synthesis gas for adjustment of temperature of the process stream. The first feed stream is passed successively through the interbed heat exchangers for cooling the partially converted synthesis gas and space velocity of the synthesis gas is adjusted to be substantially in the same range in all catalyst beds.

Abstract: Process for the preparation of ammonia, wherein three separate streams of fresh ammonia synthesis gas are used. The ammonia converter contains at least two catalyst beds connected in series. The second and third synthesis gas streams are passed through heat exchanger steps, where they are heated by effluent streams from the first catalyst bed. The preheated streams are mixed with the first synthesis gas stream and are fed to the first catalyst bed. The partly converted synthesis gas is used to heat the second and third stream and is fed to at least the second catalyst bed.

Abstract: A Method for in-situ modernization of a heterogeneous exothermic synthesis reactor, comprising the steps of providing at least a first and at least a second catalytic bed (12, 13) in an upper (2a) respectively lower (2b) portion of the reactor, providing additionally a lowermost catalytic bed (14) in the lower portion (2b) of the reactor having a reaction volume smaller than the reaction volume of the second catalytic bed (13), and loading the lowermost catalytic bed (14) with a catalyst having an activity higher that the activity of the catalyst loaded in the other beds (12, 13). Thanks to the above steps, the present method allows to obtain a reactor with high conversion yield.

Abstract: A process and apparatus cools a heat exchange type reaction zone by passing the incoming reactants through heat exchange channels in heat exchange relationship with the reaction zone. The invention simplifies the operation and construction of the heat exchanging type reaction zone by directly communicating reaction channels that contain the reaction with the heating channels that heat reactant across an open manifold located at the end of the channels. Additional reactants, cooling fluids, or other diluents may enter the process directly through the manifold space to permit further temperature control of the reaction zone. The invention promotes better heat transfer efficiency than tube and shell heat transfer arrangements that have been used for similar purposes. The narrow channels are preferably defined by corrugated plates. The reaction channels will contain a catalyst for the promotion of the primary reaction.

Abstract: Disclosed is a reactor and process for exothermic vapour phase reaction, wherein the reactor (1; 101) comprises a pressure vessel (2; 102) having an inlet (3;103) for reactant(s) and an outlet (4; 104) for products; a plurality of beds (5; 105) with heterogeneous catalyst, each bed supported by a catalyst support grating (6; 106); a vapour collection chamber (9; 109) and a vapour redistribution chamber (10; 110) between successive pair(s) of beds for redistribution of vapourous reaction mixture over the inlet of the next bed; a diaphragm (11; 111) separating the vapour collection chamber (9; 109) from the vapour redistribution chamber; at least one pair of nested trough members extending at least partially across the diaphragm, each comprising an inner trough member (14; 114) having one or more apertures (18; 118), an outer trough (20; 120) having one or more apertures (21; 121) and a quench gas conduit (15; 115) provided with apertures (17; 117); the apertures (18; 118; 21; 121; 17; 117) arranged to provide

Abstract: Process for the preparation of ammonia at elevated pressure and temperature in an ammonia reactor, comprising passing a process stream of ammonia synthesis gas successively through at least three catalyst beds and reacting the synthesis gas in the beds;intermediately cooling of partially reacted synthesis gas leaving the catalyst beds by heat exchange in heat exchangers arranged between each catalyst bed and withdrawing a product effluent being rich in ammonia, wherein the process stream is obtained by combining prior to introduction into a first catalyst bed, a first feed stream of synthesis gas having been preheated through indirect heat exchange during the intermediate cooling of the partially converted synthesis gas, a second feed stream of synthesis gas having been preheated by indirect heat exchange with the product effluent, and a third feed stream of synthesis gas for adjustment of temperature of the process stream and wherein the first feed stream is passed successively through the interbed heat exch

Abstract: A process for the preparation of ammonia from a hydrogen- and nitrogen-containing synthesis gas having a combined compression step in the recirculation of synthesis gas from at least two ammonia synthesis loops. The process includes admixing to the synthesis gas a recycle gas from a first and a second ammonia separation step. The admixed gases are pressurized, and the gas is divided into a first make-up gas stream and a second make-up gas stream. The first make-up gas stream is introduced to a first ammonia reactor, and a first process stream rich in ammonia is withdrawn. The second ammonia make-up gas stream is introduced into a second ammonia reactor, and a second process stream rich in ammonia is withdrawn. Ammonia from the first and second process streams is separated. The remainders of the first and second process streams are recycled for admixing with the synthesis gas. The separated ammonia is combined and withdrawn as an ammonia product stream.

Abstract: In a method of modernizing a heterogeneous exothermic synthesis reactor (1) of the type comprising an external shell (2), in which at least one catalytic bed (15, 16, 17) is supported, the catalytic bed (15, 16, 17) is connected to an external boiler (21), for generating high pressure steam, by means of a reacted gas outlet nozzle (4) and a conduit (29) extending in said nozzle (4) thereby forming an annular airspace (30). Advantageously, the airspace (30) defines an outlet flowpath of the gases cooled in the boiler (21) which avoids overheating of the nozzle (4).

Abstract: The present invention discloses application of axial-radial reactors to the Braun synloop using an external heat sink between the feed/effluent exchanger and the inlet to the second reactor. The advantages of the axial-radial reactors in the Braun synloop have been heretofor unavailable for failure of the prior art to combine the advantages of the high conversion disclosed in U.S. Pat. No. 4,867,959 with axial-radial reactors.

Abstract: A process and apparatus are disclosed to achieve high per-pass synthesis conversion of ammonia. A nitrogen/hydrogen synthesis gas mixture is passed sequentially through a plurality of catalyst beds. The effluent from a subsequent catalyst bed is cooled by direct quench with a partially reacted gas which has passed through at least a first catalyst bed.

Abstract: Reactors for the catalytic conversion of carbon monoxide into carbon dioxide are advantageously modified in situ from axial flow reactors into substantially radial flow reactors, and more particularly into axial-radial flow reactors. To this end at least an external cylindrical wall perforated for its whole length and an internal wall preferably perforated for most of its length are inserted inside the conventional reactor shell and cartridge.

Abstract: In a process for exothermic and heterogeneous synthesis, for example of ammonia, in which the synthesis gas is reacted in several catalytic beds with axial-radial or only radial flow, the reaction gas is collected at the outlet from the last catalytic bed but one and is transferred to a system for heat recovery external to the reactor, and is re-introduced into the last catalytic bed.

Abstract: A system for modernizing exothermic heterogeneous reactors used in the synthesis of ammonia, methanol and the like, which include a pressure shell, a wall for forming an airspace, a wall or cartridge for containing a catalyst bed, and catalyst-containing basket. An airspace-forming wall is formed of a single piece substantially the whole axial length of the reactor. A bed forming wall is distinct from, and unconnected to, the airspace forming wall, and it constitutes independent modules, each module containing at least one catalyst bed and each module resting either on an underlying module or on an extension of an inside gas distribution collector. The bed forming walls contain the catalyst and distribute gas therethrough. A portion of the catalyst contacts the airspace-forming wall.

Abstract: In an ammonia synthesis process a nitrogen-hydrogen gas is reacted partially over a catalyst at a pressure in the range 30.degree.-120.degree. C., ammonia is separated as liquid after cooling the reacted synthesis gas and unreacted synthesis gas is recycled. The liquid ammonia is evaporated in heat exchange with reacted synthesis gas to provide the required cooling effect. Such heat exchange is effected using a heat exchange surface (as in a plate-fin heat exchanger) of at least 1.5 m.sup.2 per kg mol per hour of ammonia to be condensed, with cold-end temperature approach of less than 80.degree. C. and a hot-end temperature approach of less than 5.degree. C. whereby exploit the heat effect of, inter alia, the non-ideality of ammonia to provide product gaseous ammonia at a convenient pressure with minimal mechanical refrigeration.

Abstract: In reactors for heterogeneous synthesis, comprising a boiler and a heat exchanger inserted at least partially into the end catalytic beds, and at least an intermediate catalytic bed, two airspaces are now provided in each catalytic bed by introducing couples of annular walls, one of said airspaces being produced between the cartridge's internal wall and the perforated wall inserted close to it.

Abstract: Improved process for heterogeneous synthesis and related reactors according to which the synthesis catalyst is distributed in three catalytic beds either axial-radial or radial, control of the temperature between beds being effected by means of fresh quench gas between the first and the second bed and by means of indirect cooling with an exchanger between the second and the third bed of the gas leaving the second bed, using fresh gas which is heated inside the tubes of said exchanger.

Abstract: The energy consumption of conventional reactors for heterogeneous synthesis, e.g., ammonia synthesis and methanol synthesis, wherein the synthesis gas flows substantially axially through catalyst beds, is substantially reduced by inserting in at least one catalyst bed: two concentric cylindrical substantially perforated walls to laterally delimit the bed; a bottom closure between these walls; and optionally a diaphragm on top of the bed. Optionally also, a catalyst granulometry gradient may be employed in the upper part of the bed. An upper minor portion of at least one of the cylindrical walls may be unperforated. The synthesis gas now traverses the bed substantially radially.

Abstract: The system to reduce the energy consumption of heterogeneous synthesis reactors, particularly of ammonia reactors, f.i. the "Chemico"-type reactor, foresees the insertion of two cylindrical walls at least partially perforated in order to annularly delimit the catalytic beds; the first outer wall (Fe) having a diameter (Di) slightly smaller than diameter (Dc) of the cartridge (C), has a height (Hi) higher than (H'i) of the internal cylindrical wall (Fi) which has a diameter inferior to the above mentioned (Di), but superior to the external diameter (Dt) of the central feed pipe (T) of the quench gas (QG). The top (SO) of the internal cylindrical wall (Fi) is closed by a cover (CO) that has a distance from the bottom (FO) of the basket equal to the mentioned height (H'i) of the internal cylindrical wall. The catalytic bed is therefore annular in diameter (Di-D'i) on all of the said height (H'i), but is substantially cylindrical (of diameter Di) on the height (Hi-H'i).

Abstract: A reactor for heterogeneous synthesis with reduced energy consumption. The reactor includes two cylindrical walls that are at least partly perforated and which annularly deliminate the catalytic beds. An outer wall (Fe) has height (Hi) and a diameter (Di) that is slightly smaller than diameter (Dc) of cartridge (C). An internal, cylindrical wall (Fi) has a height (H'i) and a diameter (D'i) much smaller than diameter (Di). The diameter (D'i) is about equal to diameter (Dt) of a central tube (T) which is an outlet for reacted gas (RG). The top of the cylindrical wall (Fi) is closed by a cover (CO) and is located at a distance (D) from the upper edge of the external wall of the basket (Fe). The basket is closed at its bottom by a tapered wall (PR).

Abstract: The energy consumption of conventional reactors for heterogeneous synthesis, e.g., ammonia synthesis and methanol synthesis, wherein the synthesis gas flows substantially axially through catalyst beds, is substantially reduced by inserting in at least one catalyst bed: two concentric cylindrical substantially perforated walls to laterally delimit the bed; a bottom closure between these walls; and optionally a diaphragm on top of the bed. Optionally also, a catalyst granulometry gradient may be employed in the upper part of the bed. An upper minor portion of at least one of the cylindrical walls may be unperforated. The synthesis gas now traverses the bed substantially radially.

Abstract: An oxygen injector assembly for directing substantially pure oxygen into the path of an effluent or exhaust stream from a primary reformer process for mixing of the oxygen with the effluent, the assembly comprising an oxygen delivery tube for discharging the oxygen into the path of the effluent, and a cooling jacket disposed around the outer periphery of the delivery tube for moderation of the ambient temperature conditions surrounding the oxygen injector assembly and thus compensating for the increased temperature conditions created by the mixing of the oxygen with the effluent in lieu of mixing air therewith.

Abstract: The invention relates to a reactor for industrial plants, e.g. for an ammonia synthesis plant, comprising several catalyst beds in series charged by a radial gas flow. The object is to provide for a uniform gas flow through the catalyst bed along its entire height, otherwise different space velocities are experienced within the catalyst bed involving irregularities in the reaction. The problem is solved when the cross-section of the annular space for the effluent reaction gas flowing in axial direction is equal to or larger than the cross-section of the annular space for the influent fresh gas flowing in axial direction.

Abstract: Means are disclosed for lowering the temperature of the gaseous effluent from the first catalyst bed in a continuous ammonia synthesis process in which a syngas mixture containing nitrogen and hydrogen is passed sequentially over two or more catalyst beds containing ammonia synthesis catalyst. This cooling, effected to promote the exothermic ammonia-forming reaction, is accomplished by subjecting the gaseous effluent from the first catalyst bed to heat exchange in a high temperature heat sink, preferably after having undergone heat exchange with the synthesis gas feed to the first catalyst bed, to control the temperature of the effluent entering the second catalyst bed to a desired level.

Abstract: Process for obtaining an optimal synthesis gas distribution in catalytic beds for heterogeneous reactions in reactors comprising a cylindrical pressure vessel with an internal cartridge containing a catalyst.

Abstract: A converter for heterogeneous synthesis. The converter contains a variable number of internal cartridges, each having a non-perforated external wall which forms an interspace with a internal shell wall. The converter also has a corresponding variable number of catalytic beds, each having granular catalyst. The catalyst beds are contained in a vessel having a closed bottom, an open top, and two cylindrical concentric perforated walls. The perforated walls allow for adduction and extraction of reaction gases which flow axially and radially through the catalyst beds. Heat exchangers are orientated on the same axis with the annular catalyst beds and consist of tube-bundles within a shell. Reaction gas feed tubes extend through some of the heat exchanger tube bundles.

Abstract: The energy consumption of conventional reactors for heterogeneous synthesis, e.g., ammonia synthesis and methanol synthesis, wherein the synthesis gas flows substantially axially through catalyst beds, is substantially reduced by inserting in at least one catalyst bed: two concentric cylindrical substantially perforated walls to laterally delimit the bed; a bottom closure between these walls; and optionally a diaphragm on top of the bed. Optionally also, a catalyst granulometry gradient may be employed in the upper part of the bed. An upper minor portion of at least one of the cylindrical walls may be unperforated. The synthesis gas now traverses the bed substantially radially.

Abstract: Means are disclosed for lowering the temperature of the gaseous effluent from the first catalyst bed in a continuous ammonia synthesis process in which a syngas mixture containing nitrogen and hydrogen is passed sequentially over two or more catalyst beds containing ammonia synthesis catalyst. This cooling, effected to promote the exothermic ammonia-forming reaction, is accomplished by subjecting the gaseous effluent from the first catalyst bed to heat exchange in a steam superheater, preferably after having undergone heat exchange with the synthesis gas feed to the first catalyst bed, to control the temperature of the effluent entering the second catalyst bed to a desired level.

Abstract: A horizontal, cold wall, multi-bed ammonia converter having two, shell and tube interchangers for cooling reaction gas streams leaving respectively the first and second catalyst beds with incoming reactant gases wherein each of the interchangers is vertically oriented and physically located between catalyst beds. The catalyst beds are adiabatic, slab-shape beds defined in part by side portions of the inner wall of the converter and are arranged for downward, transverse flow of reacting gases. Longitudinal conduits and baffling in cooperation with the arrangement of catalyst beds and interchangers provide serial flow of gas through the cold side of each of the interchangers, a first catalyst bed, the hot side of one of the interchangers, a second catalyst bed, the hot side of the other interchanger, a third catalyst bed, and, optionally, a fourth catalyst bed.