Abstract: A unit for use in a fuel cell stack, the unit comprising a porous metal support with a seal made by local fusion and—having a seal depth that extends from the upper surface of the porous metal support to at least the bottom surface of the porous metal support, and wherein the seal is positioned along the periphery of the porous metal support, the seal being impermeable to gas transported in the plane of the porous metal support.

Abstract: A unit for use in a fuel cell stack, the unit comprising a porous metal support with a seal made by local fusion and—having a seal depth that extends from the upper surface of the porous metal support to at least the bottom surface of the porous metal support, and wherein the seal is positioned along the periphery of the porous metal support, the seal being impermeable to gas transported in the plane of the porous metal support.

Abstract: A unit for use in a fuel cell stack, the unit comprising a porous metal support with a seal made by local fusion and-having a seal depth that extends from the upper surface of the porous metal support to at least the bottom surface of the porous metal support, and wherein the seal is positioned along the periphery of the porous metal support, the seal being impermeable to gas transported in the plane of the porous metal support.

Abstract: A unit for use in a fuel cell stack, the unit comprising a porous metal support with a seal made by local fusion and-having a seal depth that extends from the upper surface of the porous metal support to at least the bottom surface of the porous metal support, and wherein the seal is positioned along the periphery of the porous metal support, the seal being impermeable to gas transported in the plane of the porous metal support.

Abstract: An up-flow reactor for the catalytic treatment of particle containing gas comprising at least one fixed catalytic bed; at least one drain pipe located upstream of the fixed catalytic bed, the drain pipe disposed within the reactor and a dust rectifier located downstream of the drain pipe and upstream of the fixed catalytic bed.

Abstract: The invention concerns an up-flow reactor for catalytic treatment of a particle-containing gas comprising a catalytic unit and at least one drain pipe upstream the catalytic unit within a reactor wall.

Abstract: A method for the preparation of small zeotype crystals with controlled sizes comprising the steps of synthesizing inside a porous material having a majority of pores less than 1000 Å a synthesis gel consisting essentially of (a) a zeotype precursor composition comprising hydratized oxides of Si, Al and P and metal compounds (b) a zeolite template; and heating or autoclaving the porous support material containing synthesis gel, whereby zeotype crystals are formed; and rinsing and drying the porous support material containing zeotype crystals.

Abstract: A process for the production of hydrogen rich gas from a feedstock containing dimethyl ether and/or methanol by steam reforming dimethyl ether in presence of a reforming catalyst to a product gas being rich in hydrogen, wherein necessary heat for the endothermic steam reforming reactions is supplied through oxidation of part of the hydrogen contained in the steam reformed feedstock process in heat conducting relationship with the steam reforming reactions.

Abstract: Method of direct cooling synthesis gas in a catalytic reactor with one or more catalyst beds of a metal oxide catalyst being loaded on gas permeable partitions with distribution means, which method comprises admixing the synthesis gas during its passage through the reactor with a cooling gas being introduced into a mixing zone beneath each partition, wherein the mixing zones are obtained by passing a reducing gas through the catalyst bed, so that the catalyst volume shrinks during reduction of the catalyst particles, and, thereby, providing necessary cavities for the mixing zones beneath each partition.

Abstract: In a process for carrying out non-adiabatic catalytic reactions in a tubular heat exchange reactor by indirect heat exchange between a process stream and a heat conducting medium, the wall temperature at the critical outlet end of the reactor tube is decreased, by progressively supplying the heat conducting medium to the external surface of the reactor tube in increasing amounts from a region close to the outlet end to a region between the outlet end and the inlet end of the tube.

Abstract: From a synthesis gas mainly consisting of hydrogen and carbon oxides an acetic acid product consisting of acetic acid, acetic anhydride and/or methyl acetate is prepared by reactions known per se in a technically simple reaction sequence and a high conversion degree when the reactions are combined such that in a first step at a pressure of 5-200 bar and a temperature of 150.degree.-400.degree. C. the synthesis gas is converted in the gas phase in a first reactor to methanol, of which at least a substantial proportion is converted to dimethyl ether in the same reactor in the presence of one or more catalysts which together catalyze the reactionsCO+2H.sub.2 .revreaction.CH.sub.3 OH (1)2 CH.sub.3 OH.revreaction.CH.sub.3 OCH.sub.3 +H.sub.2 O (2)andCO+H.sub.2 O.revreaction.CO.sub.2 +H.sub.2 (3)and then passing the entire effluent from the first reactor to a second reactor in which methanol and dimethyl ether at a pressure of 1-800 bar and a temperature of 100.degree.-500.degree. C.

Abstract: A method of preparing methanol by reacting synthesis gas comprising hydrogen and carbon oxides in a fixed bed of methanol synthesis catalyst. The reaction of the synthesis gas is conducted under conditions where condensation of methanol occurs on the catalyst. Pressure, temperature and/or space velocity of the gas at the exit of the catalyst bed are adjusted to where conversion levels of the gas leads to formation of liquid methanol in the catalyst bed by exceeding the dew point of the reaction mixture.

Abstract: Aliphatic hydrocarbons are alkylated in the presence of a fluorinated sulphonic acid catalyst. The catalyst, which is adsorbed on a polar contact material, is pushed sequentially through first and second reactors by a feedstream and is then recycled back to the first reactor without reversing the flow direction of the process stream.

Abstract: A process for liquid phase alkylation of a hydrocarbon substrate with an olefinic alkylating agent comprising the steps of passing a process stream of the hydrocarbon substrate and alkylating agent at alkylating conditions through a fixed bed alkylation reactor of particulate polar contact material in the presence of a fluorinated sulfonic acid catalyst.

Abstract: The present invention relates to a process for preparing acetic acid, acetic acid methyl ester or acetic anhydride or mixtures thereof by converting a synthesis gas mainly containing hydrogen and carbon oxides, by first converting the synthesis gas catalytically into a gas mixture containing methanol and dimethyl ether and then carbonylating this mixture catalytically into acetic acid and/or methyl acetate and/or acetic anhydride.

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: Process for the removal of nitrogen oxides in hot flue gas by catalytic reduction with a reducing agent, which process comprises continuously introducing the flue gas into a section of a sectional divided denitration catalyst unit countercurrently with fresh air passing through an other section of the catalyst, and continuously adding the reducing agent into a third section of the catalyst between the section traversed by the flue gas and the section traversed by the air, the third section being traversed by the air before addition of the reducing agent by continuously or stepwise changing the position of the catalyst sections.

Abstract: Superconducting products on the basis of crystalline superconducting compounds having the general formula (Me.sup.1).sub.p (Me.sup.2).sub.q Cu.sub.3 O.sub.x F.sup.Y, wherein Me.sup.1 is selected from Y, Sc and the lanthanides, Me.sup.2 is Ba and/or Sr, p is 0.8-2.5, q is 0.8-3, x is 5-8.5 and y is 0-6, are prepared by reacting oxides of the metals in the molten phase, the Me.sup.2 oxides at least in part being used as Me.sup.2 peroxide and Me.sup.1 oxide and/or Cu oxide optionally being partly replaced by fluorides. The reaction is carried out under an oxygen-free atmosphere in a closed reaction vessel having deformable walls, and during the reaction the vessel is placed in an autoclave under an isostatic pressure of 800 to 3000 bar and at a temperature of 800.degree. to 1400.degree. C., after which cooling is carried out without opening of the vessel.

Abstract: Ammonia converter for radial flow through two catalyst beds has a central heat exchanger mounted centrally in one of the beds. The process stream of synthesis gas is obtained by combining inside the converter separate feed streams: a shell stream serving to cool the converter shell, an exchange stream serving to cool the central heat exchanger, and a by-pass stream for final adjustment of the temperature of the process stream. The process stream passes in succession radially through the first catalyst bed in inwards direction through the central heat exchanger for being cooled, and radially through the second catalyst bed.