Abstract: The present invention relates to a method of catalytic production of ammonia, where a gas mixture consisting mainly of unconverted synthesis gas, some ammonia, inert gases and possibly also water is recirculated to the synthesis reactor being first freed from the main part of the ammonia and possibly also water by absorption. The gas mixture is brought in contact with a hygroscopic abosrption agent having two or more OH-groups for absorption of ammonia and possibly also water. The absorption is carried out at a pressure being substantially the same as the ammonia synthesis pressure, and ammonia being desorbed from the absorption agent at a lower pressure and higher temperature than at the absorption. At least part of the possibly present water is removed from the absorption agent before it is supplied to the absorption column. Preferably it si applied ethylene glycol, diethylene glycol or triethylene glycol alone or in mixture as absorption agent.

Abstract: A diffusion process from steam reforming of a hydrocarbon to produce H.sub.2, Co and CO.sub.2, that includes: providing a generally tubular, porous, ceramic membrane, and providing a heated reaction zone in a container into which the membrane is received; the membrane carrying a catalytically active metallic substance; passing a hydrocarbon and steam containing first fluid stream into the zone and into contact with one side of the membrane, to produce CO, CO.sub.2 and H.sub.2 ; and passing a second fluid stream adjacent the opposite side of the membrane in such manner as to promote hydrogen diffusion through the membrane from said one side to said opposite side thereof; and removing hydrogen from the opposite side of the membrane. Such a process may be combined with operation of a heat engine or gas turbine, producing heat transferred to the referenced reaction zone.

Abstract: A method is described which enables ammonia plant process condensate contaminated with ammonia, carbon dioxide and methanol and urea plant condensate contaminated with urea, ammonia, carbon dioxide and other combined forms of ammonia and carbon dioxide to be simultaneously converted, in a single treatment vessel, substantially and continuously to a vaporous stream rich in ammonia, carbon dioxide and methanol and an liquid stream poor in ammonia, carbon dioxide, methanol and urea. The vaporous stream thus produced is recycled and employed as a feedstock in the reforming section in the ammonia plant.

Abstract: To make and use nitrogeneous fertilizer on a farm, nitrogen oxides are prepared in a continuous process from air or from ammonia in a reactor, with the ammonia either being transported to the farm or local site in a farming area or being prepared on the site in a continuous process from water and air. The nitrogen oxides are mixed with a continuous flow of water to form a solution of nitric acid, which may be applied to the field through the irrigation system as top dressing or mixed within the system with ammonium or other cations to form ammonium nitrate or other desired nitrogen solutions for application to the fields in a continuous process or concentrated without requiring storage of large amounts of gas or creating heat exchange problems in the manufacturing process.

Abstract: The present invention is directed to a method for producing carbon dioxide and nitrogen from combustion exhaust gas containing less than about 10% oxygen by weight which comprises the steps of (a) treating the exhaust gas to remove particulate matter, (b) compressing the exhaust gas to a pressure in the range from about 25 psia to about 200 psia, (c) purifying the exhaust gas to remove trace contaminants, (d) separating the exhaust gas to produce a carbon dioxide rich fraction and a nitrogen rich fraction, (e) liquifying the carbon dioxide rich fraction and distilling off volatile contaminants to produce pure carbon dioxide, (f) purifying the nitrogen rich fraction to remove contaminants, and (g) cryogenically fractionally distilling the nitrogen rich fraction to produce pure nitrogen. In another embodiment, the invention is directed to a method for producing carbon dioxide, nitrogen, and argon from a combustion exhaust gas.

Abstract: An integrated process for making methanol and ammonia from a hydrocarbon feed stock and air is disclosed. An air separation unit is used to produce substantially pure oxygen and nitrogen gas streams. The oxygen gas is used in the secondary reformer to increase the operating pressure of the reformers so that compression to methanol synthesis pressure may be done by a single stage compressor. The nitrogen gas is used to remove carbon oxides impurities from a ammonia synthesis feed stream in a nitrogen wash unit in addition to supplying the nitrogen reactant in the ammonia synthesis gas. Use of nitrogen wash obviates the need for steam shift and methanation reactions used in prior art processes.

Abstract: When producing ammonia in a conventional ammonia plant there is obtained a substantially improved process economy by incorporating a fuel cell into the ammonia plant. A gas stream rich in carbon dioxide, obtained during the production of ammonia, is passed to the cathode gas loop of the fuel cell; and/or a purged gas stream emanating from the process plant and containing one or more components usable as fuel for the fuel cell is fed to the anode chamber of the fuel cell. Finally, exhaust gas usable as fuel is passed from the anode chamber of the fuel cell to the front end of the process plant. An improved production of electricity is obtained in the fuel cell; and the stream rich in carbon dioxide formed in the ammonia plant is utilized, whereas normally it is a waste product.

Abstract: A process and apparatus for steam reforming of hydrocarbons. Heat from a product stream of reformed gas is utilized to supply heat required for endothermic reforming of a process gas of hydrocarbons and steam by indirect heat exchange between the product stream and process gas. The temperature of metallic materials of gas heated reactors used in the reforming is controlled so as to avoid metal dusting on tube walls of the gas heated reactors.

Abstract: A continuous process for recovering ammonia from a purge gas of an ammonia synthesis system wherein the purge gas is scrubbed by an aqueous liquid solution in counter-current flow with continuous cooling which is controlled to maintain temperature levels safely above the freezing point and to produce an aqueous solution of high ammonia concentration which is mixed with an anhydrous ammonia product of the ammonia synthesis system to form a blended ammonia product with a minimum water concentration high enough to provide corrosion protection to carbon steel storage equipment and a maximum water concentration low enough to meet a maximum design specification for the concentration of water in the blended ammonia product.

Abstract: Modifications are made to the standard process for the manufacture of ammonia and related compounds, resulting in lower operating costs through reduced total energy consumption. In one aspect of the invention, this is achieved by directing ammonia gas through one feed line, and carbon dioxide gas and steam through another feed line, into a closed reaction chamber to form ammonium carbonate. The formation of this solid compound results in a reduced pressure in the chamber. This reduced pressure can be used to drive heat engines in the reactant feed lines. In another aspect of the invention, the cost of running the potassium carbonate loop while the rest of the system is down is reduced by constructing an alternate pathway along part of the loop. The carbon dioxide gas and water vapor formed by the heating of the potassium bicarbonate flow through a heat engine and are cooled. The cooled water vapor and carbon dioxide gas are then recycled.

Abstract: Disclosed herein is a process for the separate control of the methane and rare gas contents of an ammonia-hydrogen recovery-rare gas plant complex. By the controlled withdrawal of a purge gas from the synthesis gas circulation, splitting of the purge gas into two partial streams and recycling of a partial stream to the synthesis gas generation section, the increase in inert gas to be taken out of the synthesis gas circulation as a result of the modernization of the ammonia plant can be prevented negative effect on the downstream hydrogen recovery/rare; thus energetic disadvantages or costly expansions or modifications of the ammonia-hydrogen recovery-rare gas plant complex are voided.

Abstract: A method is disclosed for producing ammonia synthesis gas by splitting a methane stream, combusting a portion of the methane with steam and oxygen-enriched air, converting a second portion of the methane with steam in a reformation heated by the combustion products of the first portion and combining the two portions for the water gas shift reaction followed by adsorptive separation of contained carbon dioxide.

Abstract: The process of the present invention which produces the flexible integration for the production of ammonia and urea uses adiabatic reforming of the carbonaceous feedstock such as natural gas. With adiabatic reforming of natural gas, a surplus of carbon dioxide is produced. With adiabatic reforming, substantially pure oxygen and nitrogen may be used which does not involve inert gases such as argon in the system. More importantly, adibatic reforming allows operation at much higher pressure than standard primary reforming, namely, between 700 and 3000 psig. When these pressures are used, the process includes a recycle of the methane and hydrogen from the ammonia synthesis loop to the adiabatic reformer.The process of the present invention uniquely removes the carbon dioxide which is produced by the reforming of the carbonaceous feedstock and treatment by the watergas shift reaction in two independent stages.

Abstract: Nitrogen is economically recovered from the flue gas evolved in a hydrocarbon steam reforming furnace by hydrogenation of free oxygen therein and removal of carbon dioxide and other minor impurities from the flue gas by pressure swing adsorption with recovery of high purity nitrogen as unsorbed effluent. The process is utilized to highest advantage in the production of ammonia syngas wherein natural gas or other hydrocarbon feed is subjected to steam reforming in a fuel-fired furnace. The nitrogen obtained by purification of the flue gas is combined with the purified hydrogen separated from the reformate providing the syngas for conversion to ammonia. In a preferred embodiment, the steam reforming is carried out in two stages, the first stage being performed in a conventional fuel-fired steam reforming furnace to which a major portion of the fresh hydrocarbon feed is charged.

Abstract: Ammonia synthesis gas is prepared by primary and secondary reforming followed by shift and carbon oxides removal. So that the process can use naphtha and methane, e.g. natural gas, as alternative feedstocks, at least the initial part of the primary reforming catalyst is alkalized. When using a methane feedstock, the primary reformer heating and outlet temperature are reduced compared to when using naphtha, and the amount of air fed to the secondary reformer is increased, so that, after shift, the hydrogen to nitrogen molar ratio of the gas stream is lower and is such that the gas contains an excess of nitrogen. This excess of nitrogen is subsequently removed, e.g. from the ammonia synthesis loop by a cryogenic hydrogen-recovery unit treating a loop purge stream and recovering hydrogen for recycle to the loop.

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: Ammonia synthesis gas is made from a raw gas comprising hydrogen, carbon dioxide and medium boiling point gases including nitrogen in excess of the proportion required an ammonia synthesis gas, by a pressure swing adsorption process characterized by feeding to the absorbent a raw gas in which hydrogen and total medium boiling point gases are present in a volume ratio in the range 1.25 to 2.5, and the medium boiling point gases comprise nitrogen to the extent of at least 90% v/v on the total of such gases. Preferred ways of making the raw gas, of ensuring purity of the product gas and of recovering useful heat are described.

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: An integrated process for producing higher alcohols, methanol and ammonia is set forth wherein two parallel reformations of methane are utilized to produce synthesis gas for the feed to the alcohol production and hydrogen for the ammonia production.

Abstract: An integrated ammonia urea process where the reaction of carbon dioxide and ammonia is in a urea reactor having a condensing section, a reaction section having more than one stage and a stripping section. The raw ammonia synthesis gas containing carbon dioxide is introduced into the stripping section of the urea reactor at a pressure selected within the range of 2000 and 3500 psig. The stripping effluent removed from the stripping section comprises the raw ammonia synthesis gas, carbon dioxide and ammonia which is introduced into a state of the reaction section.

Abstract: This invention pertains to the field of producing ammonia. More specifically, the present invention relates to reducing the costs of producing a unit amount of ammonia, particularly the energy costs, by the utilization of an enhanced boiling surface in the refrigeration zone of the process.

Abstract: A process for the production of ammonia from a hydrocarbonaceous feed, comprising preheating an inlet stream comprising a hydrocarbonaceous feed, H.sub.2 O, air and oxygen to a preheat temperature sufficiently high to initiate catalytic oxidation of the feed, introducing the preheated inlet stream into a first catalyst zone comprising a monolithic body having a plurality of gas flow passages extending therethrough and having a catalytically effective amount of palladium and platinum catalytic components dispersed therein, passing the first zone effluent to a second catalyst zone containing a platinum group metal steam reforming catalyst to form a hydrogen-containing synthesis gas, and passing the synthesis gas into an ammonia synthesis loop.

Abstract: Part of the synthesis gas produced by coal gasification in an allothermically heated fluidized bed reactor is burned after removal of dust and sulfur and serves as a source of energy to heat the reactor by indirect heat exchange and to produce the steam required for the gasification process. The flue gas exiting from the heat exchanger of the reactor can be used to perform work in expansion turbines. The rest of the synthesis gas is available for use in downstream processes, such as iron ore reduction, or can be burned and used to perform work in turbines to produce electric current. The result is a process that is environmentally safer and operates with a better yield than direct coal burning or autothermal coal gasification, but requires no outside source of energy, such as nuclear power, as prior art allothermal coal gasification processes do.

Abstract: Crude ammonia synthesis gas is obtained by primary steam reforming of a hydrocarbon gas mixture rich in methane, such as natural gas, followed by secondary reforming of the primary reformate with added air and shift conversion of the contained CO to CO.sub.2. The shift conversion product is first freed of contained CO.sub.2 by selective absorption in a novel PSA unit having an integrated B section for removal of remaining impurities such as carbon monoxide and methane, thereby providing as product a gas stream comprised of hydrogen and nitrogen in approximate 3:1 molar ratio accompanied by a small amount or argon derived from the air stream used in the secondary reforming step. Alternative embodiments are disclosed for removal of CO from the gas stream, before its entry into the NH.sub.3 conversion operation; any residual CO that might have slipped thorugh the absorbent bed of the B section is converted to CH.sub.4.

Abstract: A process for producing ammonia by reaction of a hydrogen and nitrogen-containing synthesis gas in the presence of a solid particulate catalyst for the reaction, includes conducting the reaction at pressures significantly lower than that of conventional ammonia synthesis, e.g., at about 30 to 70 atmospheres, in a fluidized bed of the catalyst. The synthesis gas is used to fluidize the catalyst and the resultant fluidized bed is preferably maintained under substantially isothermal conditions, e.g., by flowing a coolant liquid in indirect heat exchange relationship with the fluidized bed. Suitable catalysts for the process include activated iron catalysts which may be of very fine particle size.

Abstract: Integrated primary-secondary reforming operations are carried out with the partly reformed product effluent from the reformer tubes of the primary reforming zone passing to a catalyst-free reaction space at the feed end of a catalyst bed in the secondary reforming zone. The exothermic heat of reaction generated in said reaction space supplies the necessary heat for the endothermic reforming reaction that occurs in the catalyst bed of the secondary reforming zone, and the still hot secondary product effluent leaving the secondary reforming zone is passed in the shell side of the primary reformer zone to supply the endothermic heat of reaction required in said primary reforming zone. Essentially autothermal operating conditions are thereby achieved so as to essentially eliminate the necessity for employing an external fuel-fired primary reformer and/or for consuming a portion of the hyrocarbon feed material for fuel purposes.

Abstract: Gas or vapor phase chemical reactions are conducted inside an open loop Stirling cycle apparatus which may operate as a heat engine or as a heat pump. Adsorbent surfaces are associated with the thermal regenerators of the Stirling cycle apparatus, so that pressure swing adsorption separation of reactant and product gas species may be achieved in response to cyclic variations of flow and pressure within the apparatus. Flow control means are provided to introduce the feed gas into the working space of the apparatus and to remove separated product fractions. The feed gas is chemically reactive in a reaction zone of the working space, with reactant and product species separated by the apparatus to remove desired product(s) from the reaction zone while retaining reactant(s) in the reaction zone, so that conversion and selectivity objectives can be achieved.

Abstract: Multi-column pressure swing adsorption process for simultaneous production of ammonia synthesis gas and carbon dioxide from a reformer off gas having hydrogen, nitrogen and carbon dioxide as major components accompanied by minor quantities of methane, carbon monoxide and argon as impurities. The PSA system features two groups of adsorbent columns in which CO.sub.2 is adsorbed in adsorbers of the first group, the essentially CO.sub.2 -freed effluent being charged to an adsorber of the second group for removal of minor impurities while discharging an effluent gas having an H.sub.2 /N.sub.2 content stoichiometric for NH.sub.3 synthesis. The CO.sub.2 recovered from the first group of adsorbers is available at a high purity for reaction with the ammonia product for production of urea.

Abstract: A process for the simultaneous production of methanol synthesis gas and ammonia synthesis gas proceeds from the crude gas of a coal gasification, which initially is subjected to a H.sub.2 S-washing at low temperatures. Then follows a splitting of the desulfurized gas into two partial streams, of which one partial stream is led directly into the CO.sub.2 -washing which serves for production of the methanol-synthesis gas. Another partial stream is in contrast initially subjected to a conversion. From the converted gas then a partial stream is branched off which is provided for the production of ammonia-synthesis gas, whereas the remainder of the converted gas is led into the CO.sub.2 -washing serving for the production of the methanol-synthesis gas. The partial straem serving for the production of the ammonia-synthesis gas is treated to a separate CO.sub.2 -washing, in which simultaneously the so-called purge gas from the ammonia-synthesis is led in. The H.sub.2 S-washing and the CO.sub.

Abstract: An ammonia synthesis gas mixture comprised of substantially pure hydrogen and nitrogen in approximately 3/1 molar ratio is obtained form two stage reforming of a methane-rich hydrocarbon charge such as natural gas. About 40% of the fresh natural gas is charged to primary steam reforming and the obtained primary reformate product, containing about 17 volume percent of unreacted methane, is mixed with the other 60% of the fresh natural gas and the mixture is subjected to oxidative reforming with enriched air containing 30 to 35 of O.sub.2, said enriched air being supplied in an amount to produce a secondary reformate containing principally hydrogen and nitrogen, accompanied by a minor amount of oxides of carbon (CO and CO.sub.2). The secondary reformate subjected to shift reaction with steam results in conversion of contained CO to CO.sub.2, thereby releasing hydrogen in an amount which together with the hydrogen previously present in said reformate obtains a H.sub.2 /N.sub.2 molar ratio of about 3/1.

Abstract: An ammonia production process in which excess nitrogen and traces of carbon oxides are removed from raw ammonia synthesis gas firstly by application of partial condensation and secondly by application of washing action provided by carbon-oxides-free liquified gas, rich in nitrogen, which is derived from a cryogenic process used preferentially for separation of hydrogen from the ammonia synthesis loop purge gas as produced in processes which use excess of nitrogen above stoichiometric requirements in the circulating gas in the synthesis loop.

Abstract: An apparatus for the production of ammonia synthesis gas comprises a hydrocarbon convertor for converting a hydrocarbon feed to an effluent containing hydrogen and carbon monoxide by reaction with air which hydrocarbon convertor includes means to provide air in excess of the stoichiometric amount of nitrogen required for ammonia synthesis. The effluent from the hydrocarbon convertor is in communication with a water gas shift convertor for converting the carbon monoxide in the effluent to carbon dioxide. The water gas shift convertor is in communication with a pressure-swing adsorption system capable of selectively adsorbing carbon dioxide, carbon monoxide, methane and other impurities from hydrogen and a portion of the nitrogen fed in the gas mixture to the pressure swing adsorption system. The pressure swing adsorption system is provided with a conduit for discharging a partially purified ammonia synthesis gas mixture of hydrogen and nitrogen and a conduit for discharging purge gas.

Abstract: Low energy start-up procedure for ammonia plants which employs ammonia as the start-up media, thereby avoiding the BTU loss associated with venting unconverted hydrocarbons and the threat to catalyst beds associated with rapid buildup of temperatures therein.

Abstract: Production of ammonia synthesis gas by partial oxidation of a hydrocarbon feedstock, using air, oxygen enriched air, or oxygen depleted air, in admixture with steam, followed by shift and the removal of the excess of nitrogen, and also impurities such as carbon oxides and methane, by pressure swing adsorption (PSA). The PSA waste gas is combusted and used to heat the air and/or steam prior to the use thereof in the partial oxidation.

Abstract: A carbonaceous feedstock, e.g. coal or heavy oil, having a low hydrogen to carbon atomic ratio is partially oxidized using air, or oxygen enriched or depleted air, to form a crude gas which is subjected to catalytic shift and excess steam removal. Carbon dioxide and nitrogen are then removed from the resultant raw gas, which has a hydrogen to nitrogen, plus carbon monoxide, volume ratio in the range 0.5 to 1.5 and a nitrogen content at least 10 times the carbon monoxide content, in a pressure swing adsorption process thereby producing a product gas stream containing at least 50% hydrogen and 0.5 to 40% nitrogen, by volume. The waste gas from the pressure swing adsorption may be catalytically combusted to power a turbine driving the compressor for the air or the crude gas.

Abstract: The invention relates to the compression of a gaseous stream 1. The stream 1 is cooled by a liquid 15 that evaporates at least partially in the gaseous stream. The injected liquid has a composition different from that of the gas to be compressed, and is a component employed in the process in which compression is required and conducted. Alternatively, the liquid is selected from the starting materials to be employed in the process.

Abstract: Pressure swing adsorption gas separations are conducted inside an open loop Stirling cycle apparatus which may operate as an engine, refrigerator or heat pump. Adsorbent surfaces are associated with the thermal regenerators of the Stirling cycle apparatus, so that a preferentially adsorbed gas fraction is concentrated by parametric pumping into a colder end of an engine or into a warmer end of a refrigerator or heat pump, while a less readily adsorbed gas fraction is concentrated into warmer end of an engine or into colder end of a refrigerator or heat pump. Flow control means are provided to introduce the feed gas into the working space of the apparatus and to remove separated product fractions. Feed gases may be chemically reactive within a portion of the working space, with reactant and product species of the reaction separated by the apparatus to drive the reaction off equilibrium.

Abstract: In a process for preparing ammonia from hydrogen and nitrogen the synthesis gas mixture is produced by partial oxidation, in the presence of a suitable catalyst, at a pressure of from 35 to 150 bar and temperatures of from 850.degree.-1200.degree. C. at the exit of the partial oxidation zone, followed by removal of the carbon oxides and water from the gaseous effluent of the partial oxidation zone. The air used for the catalytic partial oxidation is supplied in such a quantity that the molar ratio of hydrogen to nitrogen in the synthesis gas is between 2.5 and 3 to 1 and is enriched with such a quantity of oxygen that the total quantity of oxygen is sufficient to effect the required degree of hydrocarbon conversion.

Abstract: Ammonia synthesis gas is made from a raw gas comprising hydrogen, carbon dioxide and medium boiling point gases including nitrogen in excess of the proportion required in ammonia synthesis gas, by a pressure swing adsorption process characterized by feeding to the adsorbent a raw gas in which hydrogen and total medium boiling point gases are present in a volume ratio in the range 1.25 to 2.5, and the medium boiling point gases comprise nitrogen to the extent of at least 90% v/v on the total such gases. Preferred ways of making the raw gas, of ensuring purity of the product gas and of recovering useful heat are described.

Abstract: The combined production of ammonia and urea by the reaction of gases containing hydrocarbons with steam is conducted by using a steam reformer, downstream secondary reformer, and shift converter. The ammonia synthesis gas (hydrogen, nitrogen and carbon dioxide) is subjected to a high pressure scrubbing step with a physical solvent, to remove the acid impurities, especially CO.sub.2. The pressure on the loaded solvent is reduced to a first intermediate pressure for degasing of the coabsorbed inerts and then to a second intermediate pressure for removal of the bulk of the absorbed CO.sub.2, which is then used for urea synthesis. To remove residual CO.sub.2, the solvent is stripped with air and the resultant air stream containing the stripped residual CO.sub.2 is fed to the secondary reformer.

Abstract: In an ammonia synthesis process a nitrogen-hydrogen gas is reacted partially over a catalyst at a pressure in the range 30-120 bar abs, 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 8.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: Production of ammonia by the sequence of steam hydrocarbon primary reforming, secondary reforming with air, carbon monoxide shift conversion, carbon oxides removal and catalytic ammonia synthesis is improved by using oxygen-enriched air at secondary reforming and/or by operating the reforming steps so that 5-15% by carbon atoms of the starting hydrocarbon is not reformed but is purged from the synthesis. The oxygen enriched air can be the by-product of a simple air separation plant producing nitrogen, and the nitrogen can be used to aid start-up or shut-down of the process or to keep the process plant in a hot stand-by condition.

Abstract: Carbon dioxide is removed from a raw gas containing hydrogen, carbon dioxide, and intermediate boiling gas, e.g. nitrogen, to give a gas suitable for use as a synthesis gas by a wet carbon dioxide removal process, and the resultant carbon dioxide depleted gas is subjected to pressure swing adsorption (PSA) to remove some, or all, of the intermediate boiling gas and the bulk of any residual carbon dioxide. The PSA waste gas is used to strip the absorbent liquid in the regeneration of the latter in the wet carbon dioxide removal process.The process is of particular utility in the manufacture of ammonia synthesis gas from a raw gas containing an excess of nitrogen, particularly as prepared by primary/secondary reforming/shift of a carbonaceous feedstock with partial bypass of the primary reforming stage.

Abstract: A method of using solar energy in a chemical synthesis process comprising steam reforming hydrocarbons or gasifying carbonaceous fuel, converting the product of the steam reforming of hydrocarbons or the gasifying of carbonaceous fuels to an ammonia synthesis gas, converting the ammonia synthesis gas to ammonia, supplying the heat required for the steam reforming of hydrocarbons or the gasifying of carbonaceous fuels by a heat transfer fluid, heating the heat transfer fluid in a solar receiver when solar energy is available, heating the heat transfer fluid by combusting a portion of the ammonia when sufficient solar energy is not available to supply the necessary heat to the heat transfer fluid.

Abstract: The synthesis gas for an ammonia synthesis process is refined by treating same in an adsorption-desorption unit to remove nitrogen either during the carbon oxide removal step or in the ammonia synthesis loop.

Abstract: A process for the production of ammonia wherein excess nitrogen is fed to the secondary reformer and a cryogenic unit is employed to obtain a nitrogen-rich stream which is recycled at least in part to the cryogenic unit.

Abstract: An improved process for making synthetic ammonia wherein a make-up synthesis gas is added to recycled unreacted gas from a catalytic conversion loop including the steps of introducing a volatile anti-icing compound into the hot make-up gas to vaporize the compound, cooling the gas and vaporized anti-icing compound to condense part of the anti-icing compound, separating the condensed anti-icing compound and dissolved impurities from the make-up gas, further cooling the make-up gas to a temperature at which the remaining anti-icing compound condenses essentially completely, separating the condensed remaining anti-icing compound from the make-up gas, mixing the resulting make-up gas at the low temperature with liquid ammonia to saturate the make-up gas with ammonia, separating unvaporized liquid ammonia from the saturated make-up gas, mixing the saturated make-up gas with recycle and passing the mixed gases directly to the catalytic ammonia synthesis converter.

Abstract: An apparatus for carrying out a catalytic chemical reaction in the presence of a granular catalyst under conditions such that both the reactants and the reaction product are gaseous at the temperature and pressure of the reaction. According to the present invention, a vertically extending, annular, intercylinder space, defined between a cylindrical outer catalyst retainer and a cylinder inner catalyst retainer, is divided by radially extending vertical partition walls into a plurality of chambers. Heat-exchanging tubes are disposed vertically in at least one of the chambers. A granular catalyst is packed in at least two of said chambers to form at least two reaction chambers. A feed gas is caused to flow successively and in radial directions through these reaction chambers. Since the invention reactor achieves an improved linear gas flow velocity and a greater overall heat-transfer coefficient, the reactor of the invention requires fewer heat-exchanging tubes and can thus be made smaller.

Abstract: In a process for producing ammonia which comprises: (a) primary catalytically reforming at super atmospheric pressure in a direct-fired primary reforming zone, a hydrocarbon feedstock with steam to produce a gas containing carbon oxides, hydrogen and methane; (b) secondary catalytically reforming the gas from step (a) by introducing air and bringing the mixture towards equilibrium thereby producing a secondary reformer effluent gas containing nitrogen, carbon oxides, hydrogen and a decreased quantity of methane; (c) converting carbon monoxide catalytically with steam to carbon dioxide and hydrogen; (d) removing carbon oxides to give an ammonia synthesis gas comprising nitrogen and hydrogen and compressing the gas to ammonia synthesis pressure; (e) reacting the synthesis gas in an ammonia synthesis zone to produce ammonia and recovering ammonia from the reacted gas to produce an ammonia-depleted gas stream; (f) recycling at least a portion of the ammonia-depleted gas stream to the ammonia synthesis zone; and (

Abstract: A process for producing ammonia synthesis gas in which a pressure swing adsorption unit is utilized to replace former CO.sub.2 removal, methanation, drying and purification steps. To increase the efficiency of the process, a hydrogen fuel cell is utilized to generate electricity and a high purity nitrogen purge stream for a pressure swing absorption unit. Accordingly, after reforming and high temperature catalytic shift conversion, the feed stream is divided into a first stream to feed the fuel cell and a second stream which is directly introduced to the pressure swing adsorption unit. After the first stream is reacted in the fuel cell, a nitrogen rich stream is passed to a de-oxygenation unit and then utilized as the pressure swing adsorption purge stream.