A nitric acid plant for producing nitric acid comprises a machine train comprising a drive means, in particular a steam turbine or electric motor or as case may be a gas turbine, an air compressor, a nitrous gas compressor and a gas expander, wherein the machine train is a single shaft machine, wherein the air compressor is a compressor having an axial inlet or an axial outlet which is arranged at the end side of the machine train and/or the gas expander is configured with an axial inlet or an axial outlet and/or the nitrous gas compressor is configured with an axial inlet or an axial outlet.
The present invention relates to a plant for the synthesis of ammonia, wherein the plant includes at least one reformer for converting a hydrocarbon into hydrogen, wherein the plant includes a converter for converting hydrogen and nitrogen into ammonia, wherein the converter is integrated into a recirculation loop, wherein a first carbon dioxide separator is arranged between the reformer and the recirculation loop, wherein the recirculation loop includes an ammonia separator.
C01B 3/02 - Production d'hydrogène ou de mélanges gazeux contenant de l'hydrogène
C07C 273/04 - Préparation d'urée ou de ses dérivés, c.-à-d. de composés contenant l'un des groupes les atomes d'azote ne faisant pas partie de groupes nitro ou nitroso d'urée, de ses sels, de ses complexes ou de ses composés d'addition à partir de dioxyde de carbone et d'ammoniac
3.
AMMONIA SYNTHESIS AND UREA SYNTHESIS WITH REDUCED CO2 FOOTPRINT
The present invention relates to an apparatus for synthesis of ammonia, in which the gases formed on the burner side of the primary reformer are used at least partly as reactants.
C01B 3/02 - Production d'hydrogène ou de mélanges gazeux contenant de l'hydrogène
C01B 3/36 - Production d'hydrogène ou de mélanges gazeux contenant de l'hydrogène par réaction de composés organiques gazeux ou liquides avec des agents gazéifiants, p. ex. de l'eau, du gaz carbonique, de l'air par réaction d'hydrocarbures avec des agents gazéifiants avec l'oxygène ou des mélanges contenant de l'oxygène comme agents gazéifiants
C07C 273/10 - Préparation d'urée ou de ses dérivés, c.-à-d. de composés contenant l'un des groupes les atomes d'azote ne faisant pas partie de groupes nitro ou nitroso d'urée, de ses sels, de ses complexes ou de ses composés d'addition combinée avec la synthèse d'ammoniac
The present disclosure relates to a particulate fertilizer, where the particulate fertilizer has a coating, where the coating contains polylactic acid compound. The polylactic acid compound has a proportion of 70% to 99% of L-lactic acid monomer units and a proportion of 1% to 30% of D-lactic acid monomer units. This polylactic acid compound comprises at least one first polylactic acid and at least one second polylactic acid. The first polylactic acid has a proportion of 50% to 67% of L-lactic acid monomer units and a proportion of 33% to 50% of D-lactic acid monomer units and the second polylactic acid has a proportion of 95% to 100% of L-lactic acid monomer units and a proportion of 0% to 5% of D-lactic acid monomer units.
The present invention relates to a method for producing ammonia, comprising the steps of: providing three reactant gases, specifically a hydrocarbon-containing reactant gas, an air-based reactant gas and a vapour-containing reactant gas; heating at least one of the three reactant gases using a fuelled burner device, wherein at least one heated reactant gas is obtained; feeding the at least one heated reactant gas and the remaining of the three reactant gases to an autothermal reformer; autothermally reforming the three reactant gases, wherein a reformed gas mixture is obtained; feeding the reformed gas mixture to an ammonia synthesis circuit with a synthesis circuit gas; reacting the synthesis circuit gas in a converter, wherein ammonia is created in the synthesis circuit gas; and splitting the synthesis circuit gas into a first partial stream and a second partial stream, characterised in that the first partial stream is supplied to the fuelled burner device as hydrogen-containing combustion gas. The invention further relates to a corresponding ammonia synthesis plant and to a method for retrofitting an ammonia synthesis plant.
C01B 3/02 - Production d'hydrogène ou de mélanges gazeux contenant de l'hydrogène
C01B 3/38 - Production d'hydrogène ou de mélanges gazeux contenant de l'hydrogène par réaction de composés organiques gazeux ou liquides avec des agents gazéifiants, p. ex. de l'eau, du gaz carbonique, de l'air par réaction d'hydrocarbures avec des agents gazéifiants avec des catalyseurs
The disclosure relates to a process for producing ammonia. A hydrocarbon mixture and steam are supplied to a primary reformer. The hydrocarbon mixture and the steam are at least partly converted to carbon monoxide and hydrogen in the primary reformer. The gas mixture from the primary reformer is directed into a secondary reformer. The secondary reformer is supplied with process air, at least comprising oxygen and nitrogen, such that unconverted hydrocarbon is converted to carbon monoxide and hydrogen.
The invention relates to a method for synthesizing ammonia, having the steps of: - providing hydrogen; - supplying the hydrogen to an ammonia synthesis circulator (10) comprising an ammonia converter (3) in which ammonia is catalytically synthesized; a circulator (1) which supplies a reactant gas mixture, containing the hydrogen and nitrogen, to the ammonia converter (3); and a cooling section (5) in which ammonia is condensed out of a product gas mixture of the ammonia converter (3), wherein the ammonia synthesis circuit (10) is first operated in a full-load operation, in which the ammonia synthesis circuit (10) provides a nominal flow rate of hydrogen, and the ammonia synthesis circuit (10) is converted from the full-load operation to a partial-load operation, in which the ammonia synthesis circuit (10) provides a flow rate of hydrogen which is lower than the nominal flow rate. In the partial-load operation, a first gas flow is branched off from the reactant gas flow and is conducted to the inlet of the circulator (1), and a second gas flow is branched off from the product gas mixture and is conducted to the inlet of the circulator (1).
A process for producing hydrogen by cracking of ammonia includes cracking ammonia in the presence of a catalyst to hydrogen and nitrogen, wherein the ammonia is cracked without preceding noncatalytic oxidation in the absence of an oxidant merely by supply of heat in the presence of the catalyst. In one of several alternatively possible process variants, the cracking of the ammonia is conducted in a reactor analogously to a primary reformer, wherein the catalyst is disposed in at least one tube through which ammonia flows. In the combustion chamber of the reactor, a mixture of ammonia and hydrogen is preferably combusted, where the nitrogen formed in the reaction is an inert component that serves as an additional heat carrier. A mixture of hydrogen and ammonia is advantageous since it has a moderate flame temperature, has better combustion properties than pure ammonia and, depending on the mixing ratio, emits less NOx than the two pure substances.
The present invention relates to an ammonia synthesis plant having a hydrogen device and a synthesis circuit, wherein the synthesis circuit has a conveying device, a converter and a first bypass line. The hydrogen device is designed to provide hydrogen. The conveying device is designed to cyclically convey a gas mixture, containing nitrogen, hydrogen and ammonia, in a synthesis circuit conveying direction, wherein the conveying device has a suction side and a pressure side. The converter is designed to catalytically convert nitrogen and hydrogen at least partially into ammonia, wherein the converter has an inlet and an outlet, wherein the inlet of the converter is fluidically connected to the pressure side of the conveying device and the outlet of the converter is fluidically connected to the suction side of the conveying device. The first bypass line is arranged from the suction side of the conveying device to the pressure side of the suction device parallel to the conveying device in the fluidically opposite direction and is designed for the stoppable return of a first partial stream of the gas mixture from the pressure side of the conveying device to the suction side of the conveying device, wherein the first bypass line has a cooling device which is designed to cool the first partial stream of the gas mixture. The first bypass line has a second bypass line, which is arranged parallel to the cooling device in the fluidically same direction, and which is designed for the stoppable guiding through of a second partial stream of the first partial stream in order to bypass the cooling device.
The present invention relates to the operation of an ammonia facility, which uses renewable energy sources for producing in particular green ammonia, in the absence of the renewable energy form.
The present invention relates to a device having a steam generator (10), wherein the steam generator (10) has a first side (11) and a second side (12), wherein the second side (12) is designed to generate steam, wherein the device has a first bypass line (20), wherein the first bypass line (20) is arranged to bypass the first side (11) of the steam generator (10), wherein the first bypass line (20) has a first bypass valve (22), wherein the second side (12) is connected to a steam discharge line (30), wherein the steam discharge line (30) has a steam shut-off valve (32), wherein the second side (12) has a pressure measuring device (40), wherein the device has a control device (50), wherein the control device (50) is connected to the pressure measuring device (40) and the first bypass valve (22), wherein the control device is designed to control the first bypass valve (22) depending on the pressure recorded by the pressure measuring device (40).
A method and a system for producing synthesis gas, wherein process condensate is used to produce steam. To this end, steam is used to strip volatile impurities, in particular carbon dioxide, from the process condensate and then preferably convert the impurities together with flue gas and discharge them. Then a pH of at least 7.0 is preferably set by adding additives, the process condensate being evaporated and recycled as output steam for producing synthesis gas. In this way, it is possible to suppress the corrosive effect of the process condensate such that no, or less, corrosion-resistant stainless-steel must be used in the manufacture of the system components that come into contact with the process condensate. The steam used to strip the volatile impurities is preferably generated by heat from the synthesis gas and/or flue gas.
C01B 3/38 - Production d'hydrogène ou de mélanges gazeux contenant de l'hydrogène par réaction de composés organiques gazeux ou liquides avec des agents gazéifiants, p. ex. de l'eau, du gaz carbonique, de l'air par réaction d'hydrocarbures avec des agents gazéifiants avec des catalyseurs
The invention relates to a reactor (1) at least for the pyrolysis of hydrocarbon-containing fluids at least in order to produce at least hydrocarbon-containing fluids. The reactor (1) has at least one reactor casing (2) and a reactor chamber (3) arranged within the reactor casing (2). The reactor (1) has a reactor head (4) and a reactor sump (5), wherein the reactor head (4) and the reactor sump (5) have respective feed openings (6), which can be closed at least temporarily, and discharge openings (7), through which at least fluids or solids, in particular particles, are to be introduced or discharged such that particles are at least temporarily continuously introduced into the reactor chamber (3) through the reactor head (4) in order to produce a fluidized bed (8). In a reactor in which instabilities of the electric heat input can be prevented during a methane pyrolysis for producing hydrogen and pyrolytic carbon, multiple conical components (9) are arranged in the reactor chamber (3), wherein the conical components (9) are designed to be hollow and have an inlet opening (10) and an outlet opening (11), and the inlet opening (10) has a larger diameter than the outlet opening (11).
B01J 8/08 - Procédés chimiques ou physiques en général, conduits en présence de fluides et de particules solidesAppareillage pour de tels procédés avec des particules mobiles
B01J 8/12 - Procédés chimiques ou physiques en général, conduits en présence de fluides et de particules solidesAppareillage pour de tels procédés avec des particules mobiles se déplaçant par gravité en un flux descendant
15.
METHOD AND REACTOR ASSEMBLY FOR PYROLYZING HYDROCARBON-CONTAINING FLUIDS, AND REACTOR ASSEMBLY
The invention relates to a method and a reactor assembly at least for pyrolyzing hydrocarbon-containing fluids at least in order to generate at least hydrogen-containing fluids. The hydrocarbon-containing fluids are supplied to a reactor shaft of a reactor (1) in countercurrent with a fluidized bed of the reactor (1), said fluidized bed consisting of particles, wherein at least the particles of the fluidized bed and the hydrocarbon-containing fluids are heated to a defined temperature ranging from 800-1600 °C, and particles of the fluidized bed are introduced at a reactor head (2) and are discharged at a reactor sump (3). In a method in which instabilities of the electric heat input can be prevented during a methane pyrolysis for producing hydrogen and pyrolytic carbon, the particle size of the particles of the fluidized bed are conditioned after discharging the particles from the reactor sump (3) such that the particles subjected to the conditioning process are at least partly introduced at the reactor head (2), and the particles introduced at the reactor head (2) have a uniform particle size x1, said uniform particle size having a grain size range.
B01J 8/00 - Procédés chimiques ou physiques en général, conduits en présence de fluides et de particules solidesAppareillage pour de tels procédés
B01J 8/12 - Procédés chimiques ou physiques en général, conduits en présence de fluides et de particules solidesAppareillage pour de tels procédés avec des particules mobiles se déplaçant par gravité en un flux descendant
B01J 19/00 - Procédés chimiques, physiques ou physico-chimiques en généralAppareils appropriés
16.
METHOD AND DEVICE FOR SEPARATING A HYDROCARBON-CONTAINING FEEDSTOCK STREAM BY EXTRACTIVE DISTILLATION
The disclosure relates to a process for separating a hydrocarbon-containing feedstock stream by extractive distillation, wherein the feedstock stream is contacted with a water-soluble solvent for aromatics in countercurrent. An aliphatics fraction is distillatively removed as aliphatics product stream from the mixture obtained. The aromatics are stripped from the aromatics-enriched solvent that remains and the aromatics-depleted solvent is recycled in a solvent circuit, with compounds having a lower boiling point compared to the solvent accumulating in the solvent circuit as impurities. At least a substream of the solvent circuit is purified for removal of the impurities, wherein the substream for the purifying is subjected to a thermal separation process, in which the impurities are at least partly discharged in a top product and the purified solvent that remains is recycled into the solvent circuit. An apparatus for carrying out the process is also disclosed.
The disclosure relates to a process for separating a hydrocarbon-containing feedstock stream by extractive distillation. The feedstock stream is contacted with a water-soluble solvent for aromatics in countercurrent, an aliphatics fraction is distillatively removed as aliphatics product stream from the mixture obtained. The aromatics are stripped from the aromatics-enriched solvent that remains and the aromatics-depleted solvent is recycled in a solvent circuit, with aliphatic compounds and/or compounds with aliphatic moieties accumulating in the solvent circuit as impurities. At least a substream of the solvent circuit is purified for removal of the impurities, wherein for the purifying, a liquid/liquid extraction is carried out between the substream and an extractant for aliphatics and the raffinate of the liquid/liquid extraction is recycled into the solvent circuit. An apparatus for carrying out the process is also disclosed.
C10G 53/04 - Traitement des huiles d'hydrocarbures, en l'absence d'hydrogène, par plusieurs procédés de raffinage uniquement par plusieurs étapes en série comprenant au moins une étape d'extraction
In a process for operating an ammonia plant, a gas mixture comprising nitrogen, hydrogen and ammonia is conveyed cyclically in a synthesis circuit with a conveying device which comprises at least a first compressor, nitrogen and hydrogen are converted at least partly into ammonia in a converter, the gas mixture is cooled in a cooling device in such a way that ammonia condenses out of the gas mixture, and hydrogen is provided at least partly by electrolysis. In this process, the utilization of fluctuating renewable energies can be integrated into existing plant designs, for the provision of hydrogen; for this reason, a master controller is provided and the master controller keeps at least the pressure in the synthesis circuit approximately constant via at least one control loop, on the basis of the anticipated amount of hydrogen. For this, the apparatus comprises a first bypass line for circumventing the first compressor, and a second bypass line for circumventing the cooling device.
B01D 53/00 - Séparation de gaz ou de vapeursRécupération de vapeurs de solvants volatils dans les gazÉpuration chimique ou biologique des gaz résiduaires, p. ex. gaz d'échappement des moteurs à combustion, fumées, vapeurs, gaz de combustion ou aérosols
B01J 8/00 - Procédés chimiques ou physiques en général, conduits en présence de fluides et de particules solidesAppareillage pour de tels procédés
B01J 8/06 - Procédés chimiques ou physiques en général, conduits en présence de fluides et de particules solidesAppareillage pour de tels procédés avec des particules immobiles, p. ex. dans des lits fixes dans des réacteurs tubulairesProcédés chimiques ou physiques en général, conduits en présence de fluides et de particules solidesAppareillage pour de tels procédés avec des particules immobiles, p. ex. dans des lits fixes les particules solides étant disposées dans des tubes
C25B 15/08 - Alimentation ou vidange des réactifs ou des électrolytesRégénération des électrolytes
19.
DECOMPOSITION OF AMMONIA ON NICKEL-BASED CATALYSTS
C01B 3/04 - Production d'hydrogène ou de mélanges gazeux contenant de l'hydrogène par décomposition de composés inorganiques, p. ex. de l'ammoniac
B01J 8/06 - Procédés chimiques ou physiques en général, conduits en présence de fluides et de particules solidesAppareillage pour de tels procédés avec des particules immobiles, p. ex. dans des lits fixes dans des réacteurs tubulairesProcédés chimiques ou physiques en général, conduits en présence de fluides et de particules solidesAppareillage pour de tels procédés avec des particules immobiles, p. ex. dans des lits fixes les particules solides étant disposées dans des tubes
B01J 19/24 - Réacteurs fixes sans élément interne mobile
20.
A METHOD OF CONFIGURING A PLANT FOR THE PRODUCTION OF GREEN AMMONIA
The disclosure relates to a process for producing ammonia, wherein a hydrocarbon mixture and steam are supplied to a primary reformer. The hydrocarbon mixture and the steam are at least partly converted to carbon monoxide and hydrogen in the primary reformer. The gas mixture from the primary reformer is directed into a secondary reformer. The secondary reformer is supplied with process air, at least comprising oxygen and nitrogen, such that unconverted hydrocarbon is converted to carbon monoxide and hydrogen. In examples, the firing output of the primary reformer is increased, the oxygen content of the process air is reduced before the process air is directed into the secondary reformer.
C01B 3/04 - Production d'hydrogène ou de mélanges gazeux contenant de l'hydrogène par décomposition de composés inorganiques, p. ex. de l'ammoniac
B01J 8/06 - Procédés chimiques ou physiques en général, conduits en présence de fluides et de particules solidesAppareillage pour de tels procédés avec des particules immobiles, p. ex. dans des lits fixes dans des réacteurs tubulairesProcédés chimiques ou physiques en général, conduits en présence de fluides et de particules solidesAppareillage pour de tels procédés avec des particules immobiles, p. ex. dans des lits fixes les particules solides étant disposées dans des tubes
B01J 19/24 - Réacteurs fixes sans élément interne mobile
The present disclosure relates to an ammonia plant, wherein the ammonia plant comprises a converter, a first heat exchanger, and a removal apparatus. The converter and the first heat exchanger are connected to one another via a product gas connection in such a way that the ammonia synthesis product gas is guided out of the converter via the first heat exchanger to the removal apparatus. The removal apparatus and the converter are connected to one another via a reactant gas connection in such a way that the circulation gas is guided from the removal apparatus to the converter. The ammonia plant comprises a hydrogen feed that is connected to the converter via a second heat exchanger. The ammonia plant comprises a first electric heater and a steam turbine. The first electric heater is connected to the converter or to the steam turbine.
F01D 19/00 - Démarrage des "machines" ou machines motricesDispositifs de régulation, de commande ou de sécurité en rapport avec les organes de démarrage
F01D 25/10 - Chauffage, p. ex. réchauffage avant démarrage
23.
CHEMICAL PLANT AND METHOD FOR A HYDRODESULFURIZATION OF A HYDROCARBON- AND SULFUR-CONTAINING FEEDSTOCK STREAM
The invention relates to a chemical plant (1) for a hydrodesulfurization of a hydrocarbon- and sulfur-containing feedstock stream (17), comprising a hydrofiner (18) for generating a desulfurized product stream (20) and a hydrogen sulfide-containing byproduct stream (8) from the feedstock stream (17), thereby adding a hydrogen-containing gas stream (25), a reactor (2) which is connected downstream of the hydrofiner (18) for dissociating hydrogen sulfide contained in the hydrogen sulfide-containing byproduct stream (8) into the constituents of hydrogen and sulfur, thereby generating a dissociated stream (9), and a first separating device (19) which is connected downstream of the reactor (2) for separating sulfur from the dissociated stream (9), thereby generating a sulfur-containing stream (10) and a residual stream (23), wherein the reactor (2) comprises an electrically heated reaction chamber (5) in order to thermally dissociate the hydrogen sulfide, and the chemical plant (1) has a first recirculation line (24), by means of which the residual stream (23) can be at least partly recirculated into the hydrogen-containing gas stream (25). The invention also relates to a method for a hydrodesulfurization of a hydrocarbon- and sulfur-containing feedstock stream (17).
C10G 45/02 - Raffinage des huiles d'hydrocarbures au moyen d'hydrogène ou de composés donneurs d'hydrogène pour éliminer des hétéro-atomes sans modifier le squelette de l'hydrocarbure mis en œuvre et sans craquage en hydrocarbures à point d'ébullition inférieurHydrofinissage
C01B 3/04 - Production d'hydrogène ou de mélanges gazeux contenant de l'hydrogène par décomposition de composés inorganiques, p. ex. de l'ammoniac
C01B 17/04 - Préparation du soufrePurification à partir de composés sulfurés gazeux, y compris les sulfures gazeux
C10G 49/00 - Traitement des huiles d'hydrocarbures, en présence d'hydrogène ou de composés donneurs d'hydrogène, non prévu dans un seul des groupes , , , ou
The invention relates to a method and a system for synthesizing methanol (1), wherein: a hydrogen stream (35) including external hydrogen is supplied to a synthesis gas stream (2); part of a remaining gas stream (15) discharged from a methanol reactor assembly (4), and/or of a recovery stream (6) optionally supplied to a hydrogen recovery assembly (5), and/or of a stream (71) downstream of the hydrogen recovery assembly (5) is branched off and is supplied to a synthesis gas reactor assembly (13) as return stream (40). This concept allows the efficiency of methanol production to be significantly increased. Furthermore, undesired emissions can be reduced and thus the ecobalance of the method or the system improved.
C07C 29/151 - Préparation de composés comportant des groupes hydroxyle ou O-métal liés à un atome de carbone ne faisant pas partie d'un cycle aromatique à six chaînons par réduction exclusivement des oxydes de carbone avec de l'hydrogène ou des gaz contenant de l'hydrogène
C01B 3/04 - Production d'hydrogène ou de mélanges gazeux contenant de l'hydrogène par décomposition de composés inorganiques, p. ex. de l'ammoniac
B01D 53/34 - Épuration chimique ou biologique des gaz résiduaires
B01J 3/00 - Procédés utilisant une pression supérieure ou inférieure à la pression atmosphérique pour obtenir des modifications chimiques ou physiques de la matièreAppareils à cet effet
B01J 14/00 - Procédés chimiques généraux faisant réagir des liquides avec des liquidesAppareillage spécialement adapté à cet effet
B01J 19/00 - Procédés chimiques, physiques ou physico-chimiques en généralAppareils appropriés
B01J 19/02 - Appareils caractérisés par le fait qu'ils sont construits avec des matériaux choisis pour leurs propriétés de résistance aux agents chimiques
26.
CATALYTIC DECOMPOSITION OF AMMONIA WITH WATER VAPOUR AS HEAT TRANSFER MEDIUM
23333 is heated and evaporated. Using water or water vapour as the heat transfer medium offers advantages inter alia with regard to economy and safety.
COMMISSARIAT A L'ENERGIE ATOMIQUE ET AUX ENERGIES ALTERNATIVES (France)
AXENS (France)
BIONEXT (France)
Inventeur(s)
Gonnard, Sebastien
Morin, Mathieu
Heraud, Jean-Philippe
Abrégé
The invention relates to a device for treating a feedstock, comprising a furnace (301) having an enclosure comprising an inlet (316) and an outlet (304) for the feedstock and an inlet (317) and an outlet (318) for a gas. The device comprises a system (306) for recovering the feedstock, comprising a recovery line (305) connected to the outlet (304) for the feedstock on the enclosure and comprising a sampling and/or analysis means (319). The recovery line comprises two lines in parallel downstream of the sampling and/or analysis means (319), one of the lines being a line leading to a storage tank (308) and another line being a line leading to an opening (303) for reintroducing the feedstock into the furnace (301). The invention also relates to a method for drying or roasting and to a facility for producing hydrocarbons from the drying or roasting device.
C10G 2/00 - Production de mélanges liquides d'hydrocarbures de composition non définie à partir d'oxydes de carbone
C10G 45/58 - Raffinage des huiles d'hydrocarbures au moyen d'hydrogène ou de composés donneurs d'hydrogène pour changer la structure du squelette de certains hydrocarbures sans craquer les autres hydrocarbures présents, p. ex. pour abaisser le point d'écoulementHydrocraquage sélectif des paraffines normales
C10J 3/00 - Production de gaz contenant de l'oxyde de carbone et de l'hydrogène, p. ex. du gaz de synthèse ou du gaz de ville, à partir de matières carbonées solides par des procédés d'oxydation partielle faisant intervenir de l'oxygène ou de la vapeur
C10K 1/00 - Purification des gaz combustibles contenant de l'oxyde de carbone
C10K 1/10 - Purification des gaz combustibles contenant de l'oxyde de carbone par lavage avec des liquidesRégénération des liqueurs de lavage avec des liquides aqueux
C10K 3/04 - Modification de la composition chimique des gaz combustibles contenant l'oxyde de carbone en vue de produire un carburant amélioré, p. ex. un carburant de pouvoir calorifique différent qui peut ne pas contenir d'oxyde de carbone par traitement catalytique réduisant le taux d'oxyde de carbone
COMMISSARIAT A L'ENERGIE ATOMIQUE ET AUX ENERGIES ALTERNATIVES (France)
AXENS (France)
BIONEXT (France)
Inventeur(s)
Bournay, Laurent
Gonnard, Sebastien
Heraud, Jean-Philippe
Morin, Mathieu
Volland, Eric
Abrégé
The invention relates to a multiple hearth furnace for placing a solid and a gas in contact, comprising: a chamber (30); a plurality of trays (41, 42) which are distributed along the longitudinal axis (AA) of the chamber (30); means for circulating the solid in the chamber (45, 46); and means for circulating the gas (31, 32, 33, 45, 46, 43, 50, 51, 52) in the chamber (30) which comprise a first opening (32) for discharging the gas from the chamber (30) and first gas distribution means (31, 43, 50, 51, 52) which are associated with at least one of the trays (42), the first gas distribution means (31, 43, 50, 51, 52) comprising a plurality of openings (43) which are arranged in the tray (42) in question, an air box (50) which is arranged under the tray (42), and means for supplying gas to the air box (31, 51, 52).
F27B 3/04 - Fours à sole, p. ex. fours à réverbérationFours à arc électrique du type à plusieurs solesFours à sole, p. ex. fours à réverbérationFours à arc électrique du type à plusieurs chambresCombinaisons de fours à soles
F27B 3/06 - Fours à sole, p. ex. fours à réverbérationFours à arc électrique à chambre ou sole mobile, p. ex. inclinable
F27B 3/12 - Laboratoires ou carcassesLeurs supports
F27B 3/22 - Aménagement des dispositifs d'alimentation en air ou gaz
F27B 9/18 - Fours dans lesquels la charge est déplacée mécaniquement, p. ex. du type tunnel Fours similaires dans lesquels la charge se déplace par gravité caractérisés par le trajet de la charge pendant le traitementFours dans lesquels la charge est déplacée mécaniquement, p. ex. du type tunnel Fours similaires dans lesquels la charge se déplace par gravité caractérisés par le procédé de déplacement de la charge pendant le traitement la charge se déplaçant sur un trajet circulaire ou courbe sous l'action de racleurs ou de poussoirs
F27B 9/30 - Parties constitutives, accessoires ou équipement spécialement adaptés à ces types de fours
F27D 7/02 - Alimentation en vapeur d'eau, en gaz ou en liquides
F27B 9/02 - Fours dans lesquels la charge est déplacée mécaniquement, p. ex. du type tunnel Fours similaires dans lesquels la charge se déplace par gravité à trajets multiplesFours dans lesquels la charge est déplacée mécaniquement, p. ex. du type tunnel Fours similaires dans lesquels la charge se déplace par gravité à plusieurs chambresCombinaisons de fours
The present invention concerns a converter 10 with a very high level of catalyst loading and a very high rate of conversion for a low headroom. - Fig. 1 -
B01J 8/04 - Procédés chimiques ou physiques en général, conduits en présence de fluides et de particules solidesAppareillage pour de tels procédés avec des particules immobiles, p. ex. dans des lits fixes le fluide passant successivement à travers plusieurs lits
The present invention relates to a method for producing ammonia, for further reacting the ammonia to form urea, and for subsequently granulating the urea, wherein additionally methanol is produced, wherein the methanol is reacted to form formaldehyde and the formaldehyde is reacted to form a formaldehyde-urea mixture, wherein the formaldehyde-urea mixture is added to the urea prior to granulation, characterised in that, for methanol synthesis, three gas streams are combined, wherein a first processing gas stream (24) after the processing of an amine solution of an amine-carbon dioxide scrubber (20) is selected as the first gas stream, wherein the first processing gas stream (24) has, above all, carbon dioxide, hydrogen and nitrogen, wherein a first inert gas evacuation stream (36) from the converter circuit of the ammonia synthesis is selected as the second gas stream, wherein the first inert gas evacuation stream (36) is removed after an aqueous ammonia scrubber (33), wherein the first inert gas evacuation stream (36) has, above all, hydrogen and methane, wherein a second inert gas evacuation stream is selected as the third gas stream, wherein the second inert gas evacuation stream (37) is removed after a hydrogen recovery (34), wherein the second inert gas evacuation stream (37) has, above all, methane, nitrogen and some hydrogen.
C07C 273/10 - Préparation d'urée ou de ses dérivés, c.-à-d. de composés contenant l'un des groupes les atomes d'azote ne faisant pas partie de groupes nitro ou nitroso d'urée, de ses sels, de ses complexes ou de ses composés d'addition combinée avec la synthèse d'ammoniac
C07C 273/04 - Préparation d'urée ou de ses dérivés, c.-à-d. de composés contenant l'un des groupes les atomes d'azote ne faisant pas partie de groupes nitro ou nitroso d'urée, de ses sels, de ses complexes ou de ses composés d'addition à partir de dioxyde de carbone et d'ammoniac
C07C 29/151 - Préparation de composés comportant des groupes hydroxyle ou O-métal liés à un atome de carbone ne faisant pas partie d'un cycle aromatique à six chaînons par réduction exclusivement des oxydes de carbone avec de l'hydrogène ou des gaz contenant de l'hydrogène
C07C 45/38 - Préparation de composés comportant des groupes C=O liés uniquement à des atomes de carbone ou d'hydrogènePréparation des chélates de ces composés par oxydation avec l'oxygène moléculaire de groupes fonctionnels C—O— en groupes C=O d'un groupe hydroxyle primaire
The present invention relates to a combined system (1) for producing steel, said combined system comprising: a blast furnace (2) for producing pig iron; a converter steel mill (3) for producing crude steel; a blast furnace gas line system (4) for gases generated during the pig iron production; a combined line system (5) for gases generated during the pig iron production and/or crude steel production; a hydrogen production plant (6); a chemical plant (7); a hydrogen line (8) for hydrogen-containing gases generated during the hydrogen production, the hydrogen line (8) being connected to the combined line system (5) upstream of the chemical plant (7) in the direction of flow; a mixing device (9) for hydrogen-containing gases, the mixing device (9) being arranged downstream of the hydrogen production plant (6) and upstream of the chemical plant (7) in the direction of flow, the blast furnace gas line system (4) being connected to the hydrogen production plant (6) as an input line into the hydrogen production plant (6) and the hydrogen line (8) being connected to the hydrogen production plant (6) as an output line from the hydrogen production plant (6).
The invention relates to a combined system (1) for producing steel, said combined system comprising: a blast furnace (2) for producing pig iron; a converter steel mill (3) for producing crude steel; a blast furnace gas line system (4) for gases generated during the pig iron production; a composite line system (5) for gases generated during the pig iron production and/or crude steel production; a plant (6) for producing hydrogen or hydrogen-containing synthesis gas; a hydrogen line (8) for hydrogen-containing gases generated during the production of hydrogen or hydrogen-containing synthesis gas, the blast furnace gas line system (4) being connected to the plant (6) for producing hydrogen or hydrogen-containing synthesis gas as an input line into the plant (6) for producing hydrogen or hydrogen-containing synthesis gas, and the hydrogen line (8) being connected to the plant (6) for producing hydrogen or hydrogen-containing synthesis gas as an output line from the plant (6) for producing hydrogen or hydrogen-containing synthesis gas.
The present disclosure relates to a method of operating a reformer, wherein the reformer is operated at least with a first hydrocarbon mixture and a second hydrocarbon mixture. The reformer has a primary reformer that is supplied with a first gas stream. The reformer also has a secondary reformer that is supplied with a semifinished product gas stream from the primary reformer and with an air stream. The first gas stream and the air stream are used to form the quotient of the first gas stream divided by the air stream. A threshold value is defined, wherein the reformer is shut down below the threshold value. The threshold value is compared with the product of the quotient of the first gas stream divided by the air stream multiplied by a factor H, wherein the factor is defined depending on the chemical composition of the gas stream.
C01B 3/34 - Production d'hydrogène ou de mélanges gazeux contenant de l'hydrogène par réaction de composés organiques gazeux ou liquides avec des agents gazéifiants, p. ex. de l'eau, du gaz carbonique, de l'air par réaction d'hydrocarbures avec des agents gazéifiants
34.
APPARATUS FOR PRODUCTION OF AMMONIUM NITRATE FROM NITRIC ACID AND AMMONIA
The present invention relates to an apparatus for production of ammonium nitrate from nitric acid and ammonia, where the apparatus has a recirculation circuit with a neutralization reactor (10) disposed within said recirculation circuit, where the neutralization reactor (10) has at least a first region (12) and a second region (14), where the first region (12) is upstream of the second region (14) in the recirculation circuit for flow purposes, where the first region (12) has at least one nitric acid supply apparatus (20), where the second region (14) is a shell-and-tube reactor, where the tubes (30) of the shell-and-tube reactor are designed for supply of ammonia, characterized in that the first region (12) has at least a first perforated plate (40), where the first perforated plate (40) is arranged at right angles to the flow direction, where the first perforated plate (40) is upstream of the nitric acid supply apparatus (20) in flow direction.
A method of producing ammonia includes heating, with a start-up oven, a first synthesis gas for a first ammonia synthesis in a first reactor; transferring the heated first synthesis gas to the first reactor for initiating a chemical reaction; heating, with the start-up oven, a second synthesis gas for a second ammonia synthesis in a second reactor; and transferring the heated second synthesis gas to the second reactor for initiating a chemical reaction, wherein a high-pressure synthesis of ammonia is carried out in the first reactor and a low-pressure synthesis of ammonia is carried out in the second reactor at a process pressure which is lower than the process pressure in the first reactor.
The integrated plant for making propene oxide includes a unit for producing hydrogen peroxide by an anthraquinone process, which includes a hydrogenator, an oxidizer and an extraction column, and a unit for making propene oxide from propene and hydrogen peroxide. The unit for making propene oxide has an epoxidation reactor and a work-up section, as well as an air compressor driven by a backpressure steam turbine with a conduit connecting an outlet of the air compressor with the oxidizer and a conduit connecting the steam outlet of the backpressure steam turbine with a heat exchanger of a distillation column of the work-up section.
C07D 301/12 - Synthèse du cycle de l'oxirane par oxydation de composés non saturés, ou de mélanges de composés non saturés et de composés saturés par le peroxyde d'hydrogène ou par des peroxydes ou peracides inorganiques
B01D 53/00 - Séparation de gaz ou de vapeursRécupération de vapeurs de solvants volatils dans les gazÉpuration chimique ou biologique des gaz résiduaires, p. ex. gaz d'échappement des moteurs à combustion, fumées, vapeurs, gaz de combustion ou aérosols
B01J 8/06 - Procédés chimiques ou physiques en général, conduits en présence de fluides et de particules solidesAppareillage pour de tels procédés avec des particules immobiles, p. ex. dans des lits fixes dans des réacteurs tubulairesProcédés chimiques ou physiques en général, conduits en présence de fluides et de particules solidesAppareillage pour de tels procédés avec des particules immobiles, p. ex. dans des lits fixes les particules solides étant disposées dans des tubes
B01D 53/94 - Épuration chimique ou biologique des gaz résiduaires des gaz d'échappement des moteurs à combustion par des procédés catalytiques
C01B 3/04 - Production d'hydrogène ou de mélanges gazeux contenant de l'hydrogène par décomposition de composés inorganiques, p. ex. de l'ammoniac
C01B 21/26 - Préparation par oxydation catalytique de l'ammoniac
F02C 3/20 - Ensembles fonctionnels de turbines à gaz caractérisés par l'utilisation de produits de combustion comme fluide de travail utilisant un combustible, un oxydant ou un fluide de dilution particulier pour produire les produits de combustion
F02D 19/06 - Commande des moteurs caractérisés par l'emploi de combustible non liquide, de combustibles multiples ou de substances non combustibles ajoutées au mélange carburant particulière aux moteurs fonctionnant avec des combustibles multiples, p. ex. alternativement du fuel léger et du fuel lourd, et autres que les moteurs indifférents au combustible utilisé
F02M 21/02 - Appareils pour alimenter les moteurs en combustibles non liquides, p. ex. en combustibles gazeux stockés sous forme liquide en combustibles gazeux
F01N 3/20 - Silencieux ou dispositifs d'échappement comportant des moyens pour purifier, rendre inoffensifs ou traiter les gaz d'échappement pour rendre les gaz d'échappement inoffensifs par conversion thermique ou catalytique des composants nocifs des gaz d'échappement caractérisés par les méthodes d'opérationCommande spécialement adaptés à la conversion catalytique
B01D 53/94 - Épuration chimique ou biologique des gaz résiduaires des gaz d'échappement des moteurs à combustion par des procédés catalytiques
C01B 3/04 - Production d'hydrogène ou de mélanges gazeux contenant de l'hydrogène par décomposition de composés inorganiques, p. ex. de l'ammoniac
C01B 21/26 - Préparation par oxydation catalytique de l'ammoniac
F02C 3/20 - Ensembles fonctionnels de turbines à gaz caractérisés par l'utilisation de produits de combustion comme fluide de travail utilisant un combustible, un oxydant ou un fluide de dilution particulier pour produire les produits de combustion
F02D 19/06 - Commande des moteurs caractérisés par l'emploi de combustible non liquide, de combustibles multiples ou de substances non combustibles ajoutées au mélange carburant particulière aux moteurs fonctionnant avec des combustibles multiples, p. ex. alternativement du fuel léger et du fuel lourd, et autres que les moteurs indifférents au combustible utilisé
F02M 21/02 - Appareils pour alimenter les moteurs en combustibles non liquides, p. ex. en combustibles gazeux stockés sous forme liquide en combustibles gazeux
F01N 3/20 - Silencieux ou dispositifs d'échappement comportant des moyens pour purifier, rendre inoffensifs ou traiter les gaz d'échappement pour rendre les gaz d'échappement inoffensifs par conversion thermique ou catalytique des composants nocifs des gaz d'échappement caractérisés par les méthodes d'opérationCommande spécialement adaptés à la conversion catalytique
X23322333223333 in the combustion means. The combustion means preferably comprises at least one burner and a combustion space. The firing plant is preferably configured analogously to a primary reformer.
B01D 53/94 - Épuration chimique ou biologique des gaz résiduaires des gaz d'échappement des moteurs à combustion par des procédés catalytiques
C01B 3/04 - Production d'hydrogène ou de mélanges gazeux contenant de l'hydrogène par décomposition de composés inorganiques, p. ex. de l'ammoniac
C01B 21/26 - Préparation par oxydation catalytique de l'ammoniac
F02C 3/20 - Ensembles fonctionnels de turbines à gaz caractérisés par l'utilisation de produits de combustion comme fluide de travail utilisant un combustible, un oxydant ou un fluide de dilution particulier pour produire les produits de combustion
F02D 19/06 - Commande des moteurs caractérisés par l'emploi de combustible non liquide, de combustibles multiples ou de substances non combustibles ajoutées au mélange carburant particulière aux moteurs fonctionnant avec des combustibles multiples, p. ex. alternativement du fuel léger et du fuel lourd, et autres que les moteurs indifférents au combustible utilisé
F02M 21/02 - Appareils pour alimenter les moteurs en combustibles non liquides, p. ex. en combustibles gazeux stockés sous forme liquide en combustibles gazeux
F01N 3/20 - Silencieux ou dispositifs d'échappement comportant des moyens pour purifier, rendre inoffensifs ou traiter les gaz d'échappement pour rendre les gaz d'échappement inoffensifs par conversion thermique ou catalytique des composants nocifs des gaz d'échappement caractérisés par les méthodes d'opérationCommande spécialement adaptés à la conversion catalytique
40.
REACTOR AND METHOD FOR THE PYROLYSIS OF HYDROCARBON-CONTAINING FLUIDS
A reactor and a method at least for pyrolysis of hydrocarbon-containing fluids at least for production of at least hydrogen-containing fluids are disclosed, where the reactor has a reactor shell and a reactor shaft disposed within the reactor shell, and a reactor lining at least for thermal sealing of the reactor shaft with respect to the reactor shell is disposed between the reactor shell and the reactor shaft, and wherein the reactor shaft has an at least tetragonal geometry in cross section, wherein at least one electrode for generation of thermal energy is disposed on each of two mutually opposite side walls of the reactor shaft.
C01B 3/30 - Production d'hydrogène ou de mélanges gazeux contenant de l'hydrogène par décomposition de composés organiques gazeux ou liquides d'hydrocarbures avec des particules solides mobiles utilisant la technique du lit fluidisé
The present invention relates to an apparatus for synthesising urea, the apparatus comprising an ammonia source 10 and a urea synthesis unit 20, the ammonia source 10 being connected to the urea synthesis unit 20 via a reactant line 30, characterised in that the device comprises an ammonia gas turbine 40, wherein the ammonia source 10 is connected to the ammonia gas turbine 40 via a fuel line 50, wherein the ammonia gas turbine 40 is connected to the urea synthesis unit 20 via a steam line 60.
B01J 3/02 - Dispositifs d'alimentation ou d'évacuation appropriés
B01J 4/00 - Dispositifs d'alimentationDispositifs de commande d'alimentation ou d'évacuation
B01J 8/00 - Procédés chimiques ou physiques en général, conduits en présence de fluides et de particules solidesAppareillage pour de tels procédés
C07C 273/04 - Préparation d'urée ou de ses dérivés, c.-à-d. de composés contenant l'un des groupes les atomes d'azote ne faisant pas partie de groupes nitro ou nitroso d'urée, de ses sels, de ses complexes ou de ses composés d'addition à partir de dioxyde de carbone et d'ammoniac
A process for the epoxidation of propene involves reacting propene with hydrogen peroxide, in the presence of a methanol solvent and a shaped titanium zeolite epoxidation catalyst in a fixed bed reactor. The process then involves recovering methanol from the reaction mixture, treatment of the recovered methanol by passing it through a bed of an acidic ion exchange resin, and recycling the treated methanol to the epoxidation reaction; as well as regeneration of the acidic ion exchange resin. Catalyst breakage can be reduced or avoided by washing the regenerated bed of an acidic ion exchange resin with methanol until the methanol exiting the resin bed has an apparent pH higher than 1.8, before methanol treated with the acidic ion exchange resin is recycled to the epoxidation reaction.
C07D 301/12 - Synthèse du cycle de l'oxirane par oxydation de composés non saturés, ou de mélanges de composés non saturés et de composés saturés par le peroxyde d'hydrogène ou par des peroxydes ou peracides inorganiques
43.
REACTOR FOR THERMAL CRACKING OF A GASEOUS, HYDROCARBONACEOUS FEEDSTOCK STREAM
The invention relates to a reactor (1) for thermal cracking of a gaseous, hydrocarbonaceous feedstock stream (2) in an electrically heated moving bed (3) composed of electrically conductive granules (4) with elemental carbon deposited on the granules (4), comprising an upper reactor section (5) in which a feed conduit (6) for the granules (4) and a discharge conduit (7) for a hydrogen-containing product stream (8) are disposed, a middle reactor section (9), and a lower reactor section (13) in which a feeding device (14) for the gaseous, hydrocarbonaceous feedstock stream (2) is disposed and on the bottom side of which a discharge conduit (15) for the granules (4) is provided, wherein the discharge conduit (15) comprises at least one funnel-shaped vibrating base (16) which can be made to vibrate in the vertical and/or horizontal direction by means of at least one first vibration generator (17) and is connected to the lower reactor section (13) via a vibration-decoupling suspension (18).
B01J 8/00 - Procédés chimiques ou physiques en général, conduits en présence de fluides et de particules solidesAppareillage pour de tels procédés
B01J 8/40 - Procédés chimiques ou physiques en général, conduits en présence de fluides et de particules solidesAppareillage pour de tels procédés les particules étant fluidisées selon la technique du "lit fluidisé" le lit fluidisé étant soumis à des vibrations ou à des pulsations
B01J 8/42 - Procédés chimiques ou physiques en général, conduits en présence de fluides et de particules solidesAppareillage pour de tels procédés les particules étant fluidisées selon la technique du "lit fluidisé" le lit fluidisé étant soumis à l'action d'un courant électrique ou à des radiations
B01J 19/08 - Procédés utilisant l'application directe de l'énergie ondulatoire ou électrique, ou un rayonnement particulaireAppareils à cet usage
C10G 15/08 - Craquage des huiles d'hydrocarbures par des moyens électriques, par des vibrations électromagnétiques ou mécaniques, par des radiations particulaires ou avec des gaz surchauffés dans des arcs électriques par des moyens électriques ou par des vibrations électromagnétiques ou mécaniques
C01B 3/02 - Production d'hydrogène ou de mélanges gazeux contenant de l'hydrogène
44.
PROCEDE AMELIORE DE CONVERSION D'UNE CHARGE CONTENANT UNE FRACTION BIOMASSE POUR LA PRODUCTION D'HYDROCARBURES DE SYNTHESE FISCHER-TROPSCH
B01D 53/00 - Séparation de gaz ou de vapeursRécupération de vapeurs de solvants volatils dans les gazÉpuration chimique ou biologique des gaz résiduaires, p. ex. gaz d'échappement des moteurs à combustion, fumées, vapeurs, gaz de combustion ou aérosols
C10G 2/00 - Production de mélanges liquides d'hydrocarbures de composition non définie à partir d'oxydes de carbone
C10G 45/00 - Raffinage des huiles d'hydrocarbures au moyen d'hydrogène ou de composés donneurs d'hydrogène
C10J 3/00 - Production de gaz contenant de l'oxyde de carbone et de l'hydrogène, p. ex. du gaz de synthèse ou du gaz de ville, à partir de matières carbonées solides par des procédés d'oxydation partielle faisant intervenir de l'oxygène ou de la vapeur
C10K 1/00 - Purification des gaz combustibles contenant de l'oxyde de carbone
C10K 1/10 - Purification des gaz combustibles contenant de l'oxyde de carbone par lavage avec des liquidesRégénération des liqueurs de lavage avec des liquides aqueux
C10K 1/34 - Purification des gaz combustibles contenant de l'oxyde de carbone par conversion catalytique des impuretés en des matières plus facilement éliminables
C25B 1/04 - Hydrogène ou oxygène par électrolyse de l'eau
45.
PROCESS FOR OPERATING AN AMMONIA SYNTHESIS WITH VARYING PLANT UTILIZATION
The present invention relates to a process for operating an ammonia synthesis plant, wherein the ammonia synthesis plant has a recirculation circuit (10), wherein the recirculation circuit (10) comprises a converter (20), a first heat exchanger (30), a second heat exchanger (40), an ammonia separator (50), a compressor (60) and a reactant feed (80), characterized in that the recirculation circuit (10) comprises a heating element (70), wherein in case of partial plant utilization the heating power of the heating element (70) is subjected to closed-loop control according to the reactant gas amount supplied via the reactant feed (80).
The invention relates to an ammonia converter (10), wherein the ammonia converter (10) has a casing (20), wherein the ammonia converter (10) has an starting material inlet (30) and a product outlet (40), wherein the ammonia converter (10) has at least one first catalyst bed (50) and a second catalyst bed (60), wherein the flow passes through the first catalyst bed (50) and the second catalyst bed (60) radially from the outside to the centre, wherein the ammonia converter (10) has at least one heat exchanger, wherein the heat exchanger is in the form of a tube bundle heat exchanger, wherein the tube bundle heat exchanger has a central tube (70) and a plurality of heat exchanger tubes (80), wherein the heat exchanger tubes (80) are arranged parallel to the central tube (70) and around the central tube (70), wherein the first catalyst bed (50) surrounds the tube bundle heat exchanger in a ring shape, wherein the heat exchanger is a DC heat exchanger, which is designed such that, in same, the gas flow through the heat exchanger tubes (80) is guided in the same direction as the gas flow around the heat exchanger tubes (80), wherein the starting material inlet (30) is directly connected to the heat exchanger tubes (80) for gas flow, and wherein the central tube (70) is directly connected to the space between the casing (20) and the first catalyst bed (50) for gas flow.
B01J 8/02 - Procédés chimiques ou physiques en général, conduits en présence de fluides et de particules solidesAppareillage pour de tels procédés avec des particules immobiles, p. ex. dans des lits fixes
B01J 8/04 - Procédés chimiques ou physiques en général, conduits en présence de fluides et de particules solidesAppareillage pour de tels procédés avec des particules immobiles, p. ex. dans des lits fixes le fluide passant successivement à travers plusieurs lits
B01J 19/00 - Procédés chimiques, physiques ou physico-chimiques en généralAppareils appropriés
C01B 3/02 - Production d'hydrogène ou de mélanges gazeux contenant de l'hydrogène
The invention relates to a gas-gas heat exchanger (10), in particular an ammonia synthesis gas-gas heat exchanger (10), wherein the gas-gas heat exchanger (10) has a first gas side and a second gas side, wherein the first gas side has a first gas inlet (20) and a first gas outlet (30), wherein the second gas side has a second gas inlet (40) and a second gas outlet (50), wherein the first gas side has a first gas distribution region (60) connected to the first gas inlet (20), wherein the first gas side has a first gas collection region (70) connected to the first gas outlet (30), wherein the first gas distribution region (60) and the first gas collection region (70) are connected to one another via a plurality of first heat exchange gas guides (100), wherein the first heat exchange gas guides (100) are in thermal contact with the second gas side, characterised in that at least one first electrical heating element (120) is arranged in the first gas collection region (70).
F28D 1/04 - Appareils échangeurs de chaleur comportant des ensembles de canalisations fixes pour une seule des sources de potentiel calorifique, les deux sources étant en contact chacune avec un côté de la paroi de la canalisation, dans lesquels l'autre source de potentiel calorifique est une grande masse de fluide, p. ex. radiateurs domestiques ou de moteur de voiture avec des canalisations d'échange de chaleur immergées dans la masse du fluide avec canalisations tubulaires
F28D 9/00 - Appareils échangeurs de chaleur comportant des ensembles de canalisations fixes en forme de plaques ou de laminés pour les deux sources de potentiel calorifique, ces sources étant en contact chacune avec un côté de la paroi d'une canalisation
F28D 7/16 - Appareils échangeurs de chaleur comportant des ensembles de canalisations tubulaires fixes pour les deux sources de potentiel calorifique, ces sources étant en contact chacune avec un côté de la paroi d'une canalisation les canalisations étant espacées parallèlement
F28F 9/02 - Boîtes de distributionPlaques d'extrémité
B01J 19/00 - Procédés chimiques, physiques ou physico-chimiques en généralAppareils appropriés
B01J 8/02 - Procédés chimiques ou physiques en général, conduits en présence de fluides et de particules solidesAppareillage pour de tels procédés avec des particules immobiles, p. ex. dans des lits fixes
48.
SYSTEM NETWORK AND METHOD FOR OPERATING A SYSTEM NETWORK OF THIS TYPE FOR PRODUCING HIGHER ALCOHOLS
A plant complex may include a unit that produces CO2-containing gases, a gas conducting system for CO2-containing gases, a gas/liquid separation system, a reformer that is connected to the gas conducting system and where the CO2-containing gas reacts with H2 and/or hydrocarbons to give a CO— and H2-containing synthesis gas mixture. The reformer is connected to a reactor for producing higher alcohols in which the synthesis gas mixture reacts with H2 to give a gas/liquid mixture containing higher alcohols. For separating off the alcohols of the gas/liquid mixture, the gas/liquid separation system is connected to the reactor for producing higher alcohols.
C01B 3/32 - Production d'hydrogène ou de mélanges gazeux contenant de l'hydrogène par réaction de composés organiques gazeux ou liquides avec des agents gazéifiants, p. ex. de l'eau, du gaz carbonique, de l'air
A process can be used for recovering 1-methoxy-2-propanol and 2-methoxy-1-propanol from an aqueous effluent stream by liquid-liquid-extraction, followed by extractive distillation, distillation of methoxypropanols from the extraction solvent, and distillative separation of the methoxypropanol isomers. Recovered extraction solvent is recycled to the extraction and extractive distillation. Heat transfer from recovered extraction solvent to the extract fed to the extractive distillation reduces energy demand of the process. A facility for this process contains a countercurrent extraction column, an extractive distillation column, a solvent recovery distillation column, an isomer separation distillation column, and a heat exchanger for transferring heat from recovered extraction solvent to the extract fed to the extractive distillation.
A process for making propene oxide involves reacting propene with hydrogen peroxide in the presence of methanol, a titanium zeolite epoxidation catalyst, and nitrogen containing compounds present in an amount of from 100 to 3000 mg/kg of hydrogen peroxide. Non-reacted propene is separated from the reaction mixture; the propene depleted reaction mixture is continuously distilled in a distillation column providing an overhead product stream containing propene oxide and methanol and a bottoms product stream; and propene oxide is separated from the overhead product stream. An acid is added to the propane depleted reaction mixture and/or to the distillation column at the same level or above the feed point for the propene depleted reaction mixture and/or contacted to the feed to the distillation column to provide an apparent pH in the bottoms product stream of from 3 to 4.5, which reduces the nitrogen content of the separated propene oxide.
C07D 301/12 - Synthèse du cycle de l'oxirane par oxydation de composés non saturés, ou de mélanges de composés non saturés et de composés saturés par le peroxyde d'hydrogène ou par des peroxydes ou peracides inorganiques
An absorption tower for production of nitric acid by the Ostwald process may include sieve trays that are arranged on top of one another and each spaced apart from one another, a water inlet in an upper region of the absorption tower, an inlet for gaseous nitrogen oxides in a lower region of the absorption tower, and a column bottom that is disposed in the lower region of the absorption tower beneath a lowermost sieve tray and is divided by a dividing wall into a first, radially inner region and at least a second, radially outer region. Nitric acid that trickles down from the lowermost sieve tray with a higher concentration can be collected in a middle region. The less-concentrated nitric acid that then effluxes from sieve trays higher up can then be collected separately in a region farther outward.
C01B 21/40 - Préparation par absorption d'oxydes d'azote
B01J 10/00 - Procédés chimiques généraux faisant réagir un liquide avec des milieux gazeux autrement qu'en présence de particules solidesAppareillage spécialement adapté à cet effet
B01J 19/32 - Éléments de remplissage en forme de grille ou d'éléments composés de plusieurs pièces pour constituer une unité ou un module dans l'appareil de transfert de chaleur ou de matière
B01D 53/18 - Unités d'absorptionDistributeurs de liquides
53.
METHOD AND APPARATUS FOR STARTING UP AN APPARATUS FOR STEAM REFORMING
An apparatus for steam reforming includes a reactor, a condensate separator, a condensate stripper, and a steam boiler. The reactor produces hydrogen and is connected to the condensate separator such that a gas mixture is conducted from the reactor into the condensate separator. The condensate separator and the condensate stripper are connected so that condensate separated out in the condensate separator is conducted into the condensate stripper. The condensate separator and the steam boiler are connected such that cleaned condensate can be conducted into the steam boiler. The steam boiler is connected to the reactor and to the condensate stripper in a steam-conducting manner. The boiler water feed line of the steam boiler is connectable to the condensate stripper in a liquid-conducting manner. A supply from the boiler water feed line is at a same location of the condensate stripper as a supply of the condensate from the condensate separator.
C01B 3/34 - Production d'hydrogène ou de mélanges gazeux contenant de l'hydrogène par réaction de composés organiques gazeux ou liquides avec des agents gazéifiants, p. ex. de l'eau, du gaz carbonique, de l'air par réaction d'hydrocarbures avec des agents gazéifiants
C01B 3/50 - Séparation de l'hydrogène ou des gaz contenant de l'hydrogène à partir de mélanges gazeux, p. ex. purification
An arrangement includes a steam saturator for producing saturated steam and a device for refeeding the liquid evaporated in the steam saturator. The steam saturator includes a steam inlet via which steam is delivered to the steam saturator, a steam outlet for the saturated steam produced, a condensate inlet via which condensate is delivered to the steam saturator, and a condensate return line. In a lower region of the steam saturator, a condensate liquid level that is fluidically connected to the condensate return line is maintained. The condensate return line is connected to the device, which is a condenser and comprises a cooling apparatus for condensing steam. In the steam saturator, the evaporated liquid is replaced only if the condensate level in the steam saturator drops, through condensation of saturated steam delivered from the steam saturator to the condenser and is then condensed in the condenser by the cooling apparatus.
F01K 17/06 - Récupération dans le cycle de fonctionnement de l'énergie de la vapeur, sous forme dégradée, p. ex. utilisation de la vapeur d'évacuation pour sécher le combustible solide utilisé dans l'ensemble fonctionnel
F22B 1/14 - Méthodes de production de vapeur caractérisées par le genre de chauffage par exploitation de l'énergie thermique contenue dans une source chaude la source chaude étant de la vapeur entrant en contact direct avec l'eau dans une enceinte ou avec de l'eau en gouttelettes
A process for producing nitric acid by the Ostwald process involves reacting ammonia with atmospheric oxygen as primary air to afford a NOx-containing gas stream in an ammonia oxidation reactor at a first pressure and absorbing the NOx-containing gas stream in water in an absorption apparatus at a higher, second pressure. Nitric acid is bleached with bleach air as secondary air at approximately the first pressure. The secondary air is brought to an operating pressure of the bleaching operation via a separate secondary air compressor or compressor stage. The separate secondary air compressor is independent of the compressor that brings the primary air to the first pressure. Compression to the second higher pressure at which the absorption of the NOx gases is performed in the absorption apparatus is provided only downstream of the bleaching operation.
A process for ammonia synthesis in a synthesis circuit may involve circulating a gas mixture comprising nitrogen, hydrogen, and ammonia with a conveying device (2) in the synthesis circuit, reacting nitrogen and hydrogen at least partly to ammonia in a converter, and cooling the gas mixture in a cooling device such that ammonia condenses out of the gas mixture. The disadvantages of adsorption drying and of absorption are avoided as hydrogen and nitrogen are introduced at mutually different sections into the synthesis circuit. The process may also involve introducing nitrogen in a flow direction upstream of the converter and/or directly into the converter in the synthesis circuit.
A process for producing hydrogen and pyrolytic carbon from hydrocarbons may involve converting hydrocarbons into hydrogen and carbon in a reactor at temperatures of 1000° C. or more. The reactor may include two electrodes spaced apart from one another in a flow direction of the hydrocarbons. In a region of the reactor between the electrodes an inert gas component is supplied over an entire reactor cross section. The reactor contains carbon particles in the region between the two electrodes. By introducing an inert gas component over the entire reactor cross section, deposition of carbon in this region of the reactor inner wall is prevented, thus effectively inhibiting the formation of conductivity bridges on the reactor inner wall.
C01B 3/28 - Production d'hydrogène ou de mélanges gazeux contenant de l'hydrogène par décomposition de composés organiques gazeux ou liquides d'hydrocarbures avec des particules solides mobiles
A method can be employed to regulate and stably operate a steam reforming system that is operated by steam reforming, that has a capacity utilization level that can be regulated, and that comprises a steam reformer, a hydrogenating and desulfurizing unit that is positioned upstream of the steam reformer and is configured for feedstock desulfurization, and a firing unit of the steam reformer. According to the method, a mandated capacity utilization level for the steam reforming system is established with automated regulation of the following continuously monitored parameter ratios: a hydrogen-to-feedstock ratio in the hydrogenating and desulfurizing unit, a steam-to-carbon ratio in the steam reformer, and a fuel-to-air ratio in the firing unit of the steam reformer.
C01B 3/34 - Production d'hydrogène ou de mélanges gazeux contenant de l'hydrogène par réaction de composés organiques gazeux ou liquides avec des agents gazéifiants, p. ex. de l'eau, du gaz carbonique, de l'air par réaction d'hydrocarbures avec des agents gazéifiants
B01J 19/24 - Réacteurs fixes sans élément interne mobile
B01J 19/00 - Procédés chimiques, physiques ou physico-chimiques en généralAppareils appropriés
59.
Method for operating a descending moving bed reactor with flowable granular material
A method can be used for operating a descending moving bed reactor with flowable granular material. The method involves: (i) filling an upper lock-hopper with granular material and/or emptying a lower lock-hopper, (ii) purging the lock-hoppers with purging gas, and (iii) filling the reaction chamber containing a descending moving bed from the upper lock-hopper and/or emptying the reaction chamber into the lower lock-hopper. The pressure equalization between the reaction chamber and lock-hopper is achieved with product gas. The method then involves: (iv) optionally, relieving the lock-hoppers and conveying the product gas flow into the product line, and (v) purging the lock-hoppers with purging gas.
B01J 8/12 - Procédés chimiques ou physiques en général, conduits en présence de fluides et de particules solidesAppareillage pour de tels procédés avec des particules mobiles se déplaçant par gravité en un flux descendant
B01J 8/00 - Procédés chimiques ou physiques en général, conduits en présence de fluides et de particules solidesAppareillage pour de tels procédés
C01B 3/30 - Production d'hydrogène ou de mélanges gazeux contenant de l'hydrogène par décomposition de composés organiques gazeux ou liquides d'hydrocarbures avec des particules solides mobiles utilisant la technique du lit fluidisé
A method of continuously performing one or more heat-consuming processes, where at least one heat-consuming process is electrically heated. The maximum temperature in the reaction zone of the heat-consuming process is higher than 500° C., at least 70% of products of the heat-consuming process are continuously processed further downstream and/or fed to a local energy carrier network, and the electrical energy required for the heat-consuming process is drawn from an external power grid and from at least one local power source. The local power source is fed by at least one local energy carrier network and by products from the heat-consuming process. The local energy carrier network stores natural gas, naphtha, hydrogen, synthesis gas, and/or steam as energy carrier, and has a total capacity of at least 5 GWh. The local energy carrier network is fed with at least one further product and/or by-product from at least one further chemical process.
H02J 3/28 - Dispositions pour l'équilibrage de charge dans un réseau par emmagasinage d'énergie
C01B 3/24 - Production d'hydrogène ou de mélanges gazeux contenant de l'hydrogène par décomposition de composés organiques gazeux ou liquides d'hydrocarbures
61.
PROCESS AND INTEGRATED PLANT FOR THE TREATMENT OF THE CARBON OXIDES FORMED IN THE PRODUCTION OF ALUMINUM
A process can be used for the treatment of an offgas stream, which is formed in a plant for the production of aluminum by electrolytic reduction of aluminum oxide in a melt, using at least one anode composed of a carbon-containing material. The offgas stream contains carbon oxides due to the reduction of the aluminum oxide by the carbon. At least a substream of the carbon oxides contained in the offgas stream is reacted with hydrogen or mixed with a hydrogen stream and is subsequently passed to a use. After purification and conditioning of the offgas stream in a device, an enrichment, for example with carbon monoxide, can subsequently be carried out in a reactor and the synthesis gas obtained in this way can be fed to a chemical or biotechnological plant for the synthesis of chemicals of value.
C01B 3/38 - Production d'hydrogène ou de mélanges gazeux contenant de l'hydrogène par réaction de composés organiques gazeux ou liquides avec des agents gazéifiants, p. ex. de l'eau, du gaz carbonique, de l'air par réaction d'hydrocarbures avec des agents gazéifiants avec des catalyseurs
C10K 3/02 - Modification de la composition chimique des gaz combustibles contenant l'oxyde de carbone en vue de produire un carburant amélioré, p. ex. un carburant de pouvoir calorifique différent qui peut ne pas contenir d'oxyde de carbone par traitement catalytique
C07C 1/12 - Préparation d'hydrocarbures à partir d'un ou plusieurs composés, aucun d'eux n'étant un hydrocarbure à partir d'oxydes de carbone à partir d'anhydride carbonique avec de l'hydrogène
C07C 29/50 - Préparation de composés comportant des groupes hydroxyle ou O-métal liés à un atome de carbone ne faisant pas partie d'un cycle aromatique à six chaînons par des réactions d'oxydation avec formation de groupes hydroxyle uniquement par l'oxygène moléculaire
A process can treat a gaseous material mixture obtained by catalytic conversion of synthesis gas that contains at least alkenes, possibly alcohols and possibly alkanes, and also possibly nitrogen as inert gas and unconverted components of the synthesis gas, comprising hydrogen, carbon monoxide and/or carbon dioxide. After catalytic conversion of synthesis gas, separation of the product mixture obtained in this reaction into a gas phase and a liquid phase is performed by at least partial absorption of the alkenes, possibly of the alcohols and possibly of the alkanes, in a high boiling point hydrocarbon or hydrocarbon mixture as an absorption medium, separation as the gas phase of the gases not absorbed into the absorption medium, separating an aqueous phase from the organic phase of the absorption medium, preferably by decanting, and desorption of the alkenes, possibly of the alcohols and possibly of the alkanes, from the absorption medium.
C10G 53/08 - Traitement des huiles d'hydrocarbures, en l'absence d'hydrogène, par plusieurs procédés de raffinage uniquement par plusieurs étapes en série comprenant au moins une étape d'absorption ou d'adsorption
C07C 7/11 - Purification, séparation ou stabilisation d'hydrocarburesEmploi d'additifs par absorption, c.-à-d. purification ou séparation d'hydrocarbures gazeux à l'aide de liquides
C07C 7/08 - Purification, séparation ou stabilisation d'hydrocarburesEmploi d'additifs par distillation à l'aide de composés auxiliaires extractive
C07C 7/06 - Purification, séparation ou stabilisation d'hydrocarburesEmploi d'additifs par distillation à l'aide de composés auxiliaires azéotropique
C07C 7/144 - Purification, séparation ou stabilisation d'hydrocarburesEmploi d'additifs par emploi de membranes, p. ex. par perméation sélective
C07C 7/00 - Purification, séparation ou stabilisation d'hydrocarburesEmploi d'additifs
B01D 53/14 - Séparation de gaz ou de vapeursRécupération de vapeurs de solvants volatils dans les gazÉpuration chimique ou biologique des gaz résiduaires, p. ex. gaz d'échappement des moteurs à combustion, fumées, vapeurs, gaz de combustion ou aérosols par absorption
B01D 53/22 - Séparation de gaz ou de vapeursRécupération de vapeurs de solvants volatils dans les gazÉpuration chimique ou biologique des gaz résiduaires, p. ex. gaz d'échappement des moteurs à combustion, fumées, vapeurs, gaz de combustion ou aérosols par diffusion
B01D 61/36 - PervaporationDistillation à membranesPerméation liquide
A process can be used to prepare alkenes by catalytic conversion of synthesis gas to a first mixture comprising alkenes and alcohols. The alcohols present in the first mixture are converted to the corresponding alkenes by dehydration in a subsequent step. At least one alkene having two to four carbon atoms is obtained as isolated product from a product mixture by processing thereof and/or separation steps. In the catalytic conversion, a catalyst is preferably used that comprises grains of non-graphitic carbon having cobalt nanoparticles dispersed therein. The cobalt nanoparticles have an average diameter dp of 1-20 nm. An average distance D between individual cobalt nanoparticles in the grains is 2-150 nm. A combined total mass fraction ω of metal in the grains is from 30%-70% by weight of a total mass of the grains such that 4.5 dp/ω>D≥0.25 dp/ω.
C07C 1/04 - Préparation d'hydrocarbures à partir d'un ou plusieurs composés, aucun d'eux n'étant un hydrocarbure à partir d'oxydes de carbone à partir de monoxyde de carbone avec de l'hydrogène
C07C 29/151 - Préparation de composés comportant des groupes hydroxyle ou O-métal liés à un atome de carbone ne faisant pas partie d'un cycle aromatique à six chaînons par réduction exclusivement des oxydes de carbone avec de l'hydrogène ou des gaz contenant de l'hydrogène
C07C 1/24 - Préparation d'hydrocarbures à partir d'un ou plusieurs composés, aucun d'eux n'étant un hydrocarbure à partir de composés organiques ne renfermant que des atomes d'oxygène en tant qu'hétéro-atomes par élimination d'eau
C07C 7/11 - Purification, séparation ou stabilisation d'hydrocarburesEmploi d'additifs par absorption, c.-à-d. purification ou séparation d'hydrocarbures gazeux à l'aide de liquides
C07C 29/86 - SéparationPurificationStabilisationEmploi d'additifs par traitement physique par traitement liquide-liquide
B01J 35/00 - Catalyseurs caractérisés par leur forme ou leurs propriétés physiques, en général
B01D 53/14 - Séparation de gaz ou de vapeursRécupération de vapeurs de solvants volatils dans les gazÉpuration chimique ou biologique des gaz résiduaires, p. ex. gaz d'échappement des moteurs à combustion, fumées, vapeurs, gaz de combustion ou aérosols par absorption
64.
REACTOR AND METHOD FOR THE PYROLYSIS OF HYDROCARBON-CONTAINING FLUIDS
The present invention relates to a reactor and to a method at least for pyrolysis of hydrocarbon-containing fluids at least for production of at least hydrogen-containing fluids, wherein the reactor has a reactor shell and a reactor shaft disposed within the reactor shell, and a reactor lining at least for thermal sealing of the reactor shaft with respect to the reactor shell is disposed between the reactor shell and the reactor shaft, and wherein the reactor shaft has an at least tetragonal geometry in cross section, wherein at least one electrode for generation of thermal energy is disposed on each of two mutually opposite side walls of the reactor shaft.
B01J 8/12 - Procédés chimiques ou physiques en général, conduits en présence de fluides et de particules solidesAppareillage pour de tels procédés avec des particules mobiles se déplaçant par gravité en un flux descendant
B01J 8/42 - Procédés chimiques ou physiques en général, conduits en présence de fluides et de particules solidesAppareillage pour de tels procédés les particules étant fluidisées selon la technique du "lit fluidisé" le lit fluidisé étant soumis à l'action d'un courant électrique ou à des radiations
C01B 3/30 - Production d'hydrogène ou de mélanges gazeux contenant de l'hydrogène par décomposition de composés organiques gazeux ou liquides d'hydrocarbures avec des particules solides mobiles utilisant la technique du lit fluidisé
p from 1 to 20 nm, and an average distance D between nanoparticles is from 2 to 150 nm. The combined total mass fraction of metal ω in the grains ranges from 30% to 70% by weight of the total mass of the grains of non-graphitic carbon, wherein 4.5 dp/ω>D≥0.25 dp/ω.
C07C 27/08 - Procédés impliquant la production simultanée de plusieurs classes de composés contenant de l'oxygène par réduction de composés oxygénés par hydrogénation d'oxydes de carbone avec des catalyseurs en mouvement
B01D 53/14 - Séparation de gaz ou de vapeursRécupération de vapeurs de solvants volatils dans les gazÉpuration chimique ou biologique des gaz résiduaires, p. ex. gaz d'échappement des moteurs à combustion, fumées, vapeurs, gaz de combustion ou aérosols par absorption
B01D 53/22 - Séparation de gaz ou de vapeursRécupération de vapeurs de solvants volatils dans les gazÉpuration chimique ou biologique des gaz résiduaires, p. ex. gaz d'échappement des moteurs à combustion, fumées, vapeurs, gaz de combustion ou aérosols par diffusion
B01D 61/36 - PervaporationDistillation à membranesPerméation liquide
C07C 1/04 - Préparation d'hydrocarbures à partir d'un ou plusieurs composés, aucun d'eux n'étant un hydrocarbure à partir d'oxydes de carbone à partir de monoxyde de carbone avec de l'hydrogène
C07C 7/00 - Purification, séparation ou stabilisation d'hydrocarburesEmploi d'additifs
C07C 7/06 - Purification, séparation ou stabilisation d'hydrocarburesEmploi d'additifs par distillation à l'aide de composés auxiliaires azéotropique
C07C 7/08 - Purification, séparation ou stabilisation d'hydrocarburesEmploi d'additifs par distillation à l'aide de composés auxiliaires extractive
C07C 7/11 - Purification, séparation ou stabilisation d'hydrocarburesEmploi d'additifs par absorption, c.-à-d. purification ou séparation d'hydrocarbures gazeux à l'aide de liquides
C07C 7/144 - Purification, séparation ou stabilisation d'hydrocarburesEmploi d'additifs par emploi de membranes, p. ex. par perméation sélective
C07C 29/04 - Préparation de composés comportant des groupes hydroxyle ou O-métal liés à un atome de carbone ne faisant pas partie d'un cycle aromatique à six chaînons par addition de groupes hydroxyle à des liaisons carbone-carbone non saturées, p. ex. à l'aide de H2O2 par hydratation de liaisons doubles carbone-carbone
C10G 53/08 - Traitement des huiles d'hydrocarbures, en l'absence d'hydrogène, par plusieurs procédés de raffinage uniquement par plusieurs étapes en série comprenant au moins une étape d'absorption ou d'adsorption
A process for producing alkoxylates features a high growth ratio without the need of interim storage of a pre-polymer produced in a first reactor. The process may involve reacting a monomeric educt in the presence of a catalyst and a starting material in a first reactor equipped with a first circulation loop and thereafter passing a pre-polymer that is produced of the first circulation loop to a second reactor equipped with a second circulation loop, where a desired polymer is produced. The first reactor may comprise a smaller volume than the second reactor. The growth ratio, defined as a final batch volume of the second reactor divided by a minimum initial volume of the starting material in the first reactor, is at least 80:1.
B01J 19/24 - Réacteurs fixes sans élément interne mobile
C08G 65/26 - Composés macromoléculaires obtenus par des réactions créant une liaison éther dans la chaîne principale de la macromolécule à partir d'éthers cycliques par ouverture d'un hétérocycle à partir d'éthers cycliques et d'autres composés
A method for synthesizing methanol, wherein a fuel stream containing carbon is supplied to a synthesis gas reactor arrangement to obtain a synthesis gas stream including hydrogen and carbon oxides that is supplied to a first reactor stage of a methanol reactor arrangement for partial conversion into methanol, and is obtained with a generation pressure higher than the synthesis pressure with which the synthesis gas stream is partially converted into methanol. A residue gas stream is obtained from the methanol reactor arrangement, supplied to a recycle compressor and to the methanol reactor arrangement. Before being supplied to the first reactor stage, the synthesis gas stream is supplied to a heat recovery device to recover heat. A recovery stream is supplied to a hydrogen recovery arrangement to obtain an H-recycle stream. The pressure of the unreacted hydrogen is increased before it is supplied again to the first reactor stage.
C07C 29/152 - Préparation de composés comportant des groupes hydroxyle ou O-métal liés à un atome de carbone ne faisant pas partie d'un cycle aromatique à six chaînons par réduction exclusivement des oxydes de carbone avec de l'hydrogène ou des gaz contenant de l'hydrogène caractérisée par le réacteur utilisé
B01J 19/24 - Réacteurs fixes sans élément interne mobile
C01B 3/36 - Production d'hydrogène ou de mélanges gazeux contenant de l'hydrogène par réaction de composés organiques gazeux ou liquides avec des agents gazéifiants, p. ex. de l'eau, du gaz carbonique, de l'air par réaction d'hydrocarbures avec des agents gazéifiants avec l'oxygène ou des mélanges contenant de l'oxygène comme agents gazéifiants
C07C 29/151 - Préparation de composés comportant des groupes hydroxyle ou O-métal liés à un atome de carbone ne faisant pas partie d'un cycle aromatique à six chaînons par réduction exclusivement des oxydes de carbone avec de l'hydrogène ou des gaz contenant de l'hydrogène
68.
Apparatus and method for automatable start-up of a steam reformer arrangement into a normal operating state, and use and open-loop control/closed-loop control device and computer program product
A method can be utilized to startup into a normal operating state a steam reformer arrangement for the production of hydrogen, methanol, or ammonia. A plurality of burners that are coupled to at least one reactor having reformer tubes may be controlled and regulated. In particular, startup may be performed out and regulated in an automated manner by the burners ensuring normal operation, in particular non-startup burners, being ignited indirectly as a function of temperature by means of burners provided specifically for startup, in particular pilot burners and startup burners, as a function of automatically evaluated flame monitoring at least at the pilot burners. This method provides time savings and savings of outlay in terms of personnel and also high operational reliability.
B01J 19/00 - Procédés chimiques, physiques ou physico-chimiques en généralAppareils appropriés
B01J 19/24 - Réacteurs fixes sans élément interne mobile
C01B 3/34 - Production d'hydrogène ou de mélanges gazeux contenant de l'hydrogène par réaction de composés organiques gazeux ou liquides avec des agents gazéifiants, p. ex. de l'eau, du gaz carbonique, de l'air par réaction d'hydrocarbures avec des agents gazéifiants
69.
METHOD AND SYSTEM FOR USING THE CARBON OXIDE ARISING IN THE PRODUCTION OF ALUMINIUM
A process can utilize carbon oxides formed in the production of aluminum, by electrolytic reduction of aluminum oxide in a melt using at least one anode made of a carbon-comprising material. A pyrolysis of hydrocarbons, in particular methane or natural gas, is carried out in which pyrolysis carbon and hydrogen are formed. The pyrolysis carbon is used for the production of the at least one anode. The hydrogen formed in the pyrolysis of methane is mixed with carbon dioxide and/or carbon monoxide from the electrolytic production of aluminum, to produce a gas stream which is parsed to a further use. An integrated plant contains an electrolysis apparatus for producing aluminum by melt-electrolytic reduction of aluminum oxide, and also contains at least one reactor in which pyrolysis carbon and hydrogen are produced by pyrolysis of hydrocarbons.
An integrated process contains the following steps of: (i) pyrolysis of hydrocarbons to carbon and hydrogen, (iia) removal of at least a part of the produced carbon in step (i) and at least partly further processing of said carbon into a carbon containing electrode, and (iib) removal of the hydrogen produced in step (i) and at least partly using said hydrogen for providing energy, preferably electric energy or heat, for the electrode production in step (iia). A joint plant is also useful, which contains (a) at least one reactor for a pyrolysis process, (b) at least one reactor for the production of electrodes for an aluminum process, (c) a power plant and/or at least one gas-fired burner, and optionally, (d) at least one reactor for the electrolysis for producing aluminum.
C01B 3/24 - Production d'hydrogène ou de mélanges gazeux contenant de l'hydrogène par décomposition de composés organiques gazeux ou liquides d'hydrocarbures
C01B 32/05 - Préparation ou purification du carbone non couvertes par les groupes , , ,
C25C 3/06 - Production, récupération ou affinage électrolytique de métaux par électrolyse de bains fondus de l'aluminium
A method for the synthesis of methanol, wherein a carbonaceous energy source flow is supplied to a synthesis gas reactor arrangement for obtaining a synthesis gas flow having hydrogen and carbon oxides, wherein the synthesis gas flow is supplied to a thermal recovery apparatus for recovering heat from the synthesis gas flow and then to a synthesis gas compressor for pressure increase. The synthesis gas flow is supplied at least in part to a first reactor stage of a methanol reactor arrangement for partial conversion to methanol, a residual gas flow having unreacted carbon oxides being obtained from the methanol reactor arrangement, which residual gas flow is supplied to a recycling compressor for increasing its pressure, the pressure-increased gas flow being supplied to the methanol reactor arrangement for partial conversion to methanol, a recovery flow from an unreacted residual gas being supplied to the first reactor stage of a hydrogen recovery arrangement to obtain a H-recycling flow. The
C07C 29/152 - Préparation de composés comportant des groupes hydroxyle ou O-métal liés à un atome de carbone ne faisant pas partie d'un cycle aromatique à six chaînons par réduction exclusivement des oxydes de carbone avec de l'hydrogène ou des gaz contenant de l'hydrogène caractérisée par le réacteur utilisé
B01J 19/24 - Réacteurs fixes sans élément interne mobile
01 - Produits chimiques destinés à l'industrie, aux sciences ainsi qu'à l'agriculture
04 - Huiles et graisses industrielles; lubrifiants; combustibles
07 - Machines et machines-outils
11 - Appareils de contrôle de l'environnement
37 - Services de construction; extraction minière; installation et réparation
39 - Services de transport, emballage et entreposage; organisation de voyages
40 - Traitement de matériaux; recyclage, purification de l'air et traitement de l'eau
42 - Services scientifiques, technologiques et industriels, recherche et conception
Produits et services
Chemicals used in industry and science, in particular for
the production of hydrogen, ammonia, fuels and methanol;
industrial chemicals, namely synthesis gas for use in
production processes. Fuels (including motor spirit), in particular synthesis gas
for use in turbines, burners, motors and engines. Gas generators [compressors], gasifiers, in particular for
generating synthesis gas from carbonaceous fuels and for
superheating steam. Burners, furnaces, loading apparatus for furnaces, gas heat
generators, heat regenerators and steam generating apparatus
being parts of gasification installations, in particular
being installations for the manufacture of chemical agents,
primarily synthesis gas. Installation, assembly, repair and maintenance of apparatus
and equipment, and of installations and structural parts or
components composed thereof, for the conversion of
carbonaceous materials, in particular for the production of
synthesis gases. Gas supply services [distribution]; heat supplying
[distribution]. Heat generation, in particular through the generation of
synthesis gas. Scientific and technological services, in particular
engineering and industrial design, primarily consultancy and
planning relating to the construction, expansion,
dismantling or operation of chemical installations or parts
thereof, in particular chemical installations for the
production of synthesis gas; research and development in the
field of chemistry and engineering, in particular relating
to chemical production processes and related chemical
installations of parts thereof, primarily chemical
installations for the production of synthesis gas.
A reformer for production of synthesis gas may include a reformer firing space having a reformer base, reformer walls, and a reformer roof. The reformer may include a first reformer tube and a second reformer tube, with at least sections of the first reformer tube and the second reformer tube being arranged within the reformer firing space. At least one reformer burner is disposed outside the reformer firing space. A cooling duct on or beneath the reformer base is disposed between the first reformer tube and the second reformer tube. The first reformer tube and the second reformer tube can be connected to a collecting system outside the reformer firing space, with the collecting system being disposed beneath the reformer base.
B01J 8/06 - Procédés chimiques ou physiques en général, conduits en présence de fluides et de particules solidesAppareillage pour de tels procédés avec des particules immobiles, p. ex. dans des lits fixes dans des réacteurs tubulairesProcédés chimiques ou physiques en général, conduits en présence de fluides et de particules solidesAppareillage pour de tels procédés avec des particules immobiles, p. ex. dans des lits fixes les particules solides étant disposées dans des tubes
B01J 8/02 - Procédés chimiques ou physiques en général, conduits en présence de fluides et de particules solidesAppareillage pour de tels procédés avec des particules immobiles, p. ex. dans des lits fixes
C01B 3/38 - Production d'hydrogène ou de mélanges gazeux contenant de l'hydrogène par réaction de composés organiques gazeux ou liquides avec des agents gazéifiants, p. ex. de l'eau, du gaz carbonique, de l'air par réaction d'hydrocarbures avec des agents gazéifiants avec des catalyseurs
A process for preparing methanol by a methanol synthesis reaction of carbon dioxide with hydrogen may involve a distillation step and a condensation step following the synthesis of a crude methanol. A volatile component and water may be separated off from a methanol-containing product stream, and a gas stream containing a volatile component that has been separated off may be discharged at least partially as offgas. At least part of the gas stream that has been separated off may be recirculated into the methanol synthesis reaction. A plant for preparing methanol can store or utilize electric power generated from renewable energy sources and provide facilities for discharging the offgas stream, which can be purified by catalytic after-combustion. Alternatively, the plant can be configured without discharge of an offgas substream, or the offgas streams are so small that they can be released without treatment into the environment at a suitable position.
C07C 29/151 - Préparation de composés comportant des groupes hydroxyle ou O-métal liés à un atome de carbone ne faisant pas partie d'un cycle aromatique à six chaînons par réduction exclusivement des oxydes de carbone avec de l'hydrogène ou des gaz contenant de l'hydrogène
C25B 1/04 - Hydrogène ou oxygène par électrolyse de l'eau
C25B 15/08 - Alimentation ou vidange des réactifs ou des électrolytesRégénération des électrolytes
F25J 3/02 - Procédés ou appareils pour séparer les constituants des mélanges gazeux impliquant l'emploi d'une liquéfaction ou d'une solidification par rectification, c.-à-d. par échange continuel de chaleur et de matière entre un courant de vapeur et un courant de liquide
A process for synthesizing methanol may involve supplying a CO2 stream consisting predominantly of carbon dioxide and an H stream consisting predominantly of hydrogen to a methanol reactor arrangement for conversion to methanol. A tail gas stream comprising unreacted hydrogen may be obtained from the methanol reactor arrangement. The unreacted hydrogen may be at least partly recycled to the methanol reactor arrangement. The tail gas stream is supplied to a hydrogen recovery arrangement to obtain a return stream comprising the unreacted hydrogen. The molar proportion of hydrogen in the return stream may be higher than in the tail gas stream.
C07C 29/152 - Préparation de composés comportant des groupes hydroxyle ou O-métal liés à un atome de carbone ne faisant pas partie d'un cycle aromatique à six chaînons par réduction exclusivement des oxydes de carbone avec de l'hydrogène ou des gaz contenant de l'hydrogène caractérisée par le réacteur utilisé
B01J 19/24 - Réacteurs fixes sans élément interne mobile
B01D 53/22 - Séparation de gaz ou de vapeursRécupération de vapeurs de solvants volatils dans les gazÉpuration chimique ou biologique des gaz résiduaires, p. ex. gaz d'échappement des moteurs à combustion, fumées, vapeurs, gaz de combustion ou aérosols par diffusion
76.
Method for operating a plant for synthesizing methanol
A method for operating a plant for synthesizing methanol, wherein a synthesis gas flow having hydrogen and carbon oxides is supplied to a synthesis gas compressor of the plant to increase the pressure of the synthesis gas flow. The pressure-increased synthesis gas flow is supplied to a methanol reactor arrangement of the plant for partial conversion to methanol. The plant has a hydrogen recovery arrangement which obtains an H-recycling flow including hydrogen from a recovery flow supplied from the methanol reactor arrangement, which hydrogen is converted at least in part to methanol. Upon failure of the synthesis gas compressor, the synthesis gas flow continues to be supplied to the methanol reactor arrangement for partial conversion to methanol. Following failure of the synthesis gas compressor, a line arrangement of the plant is switched such that the H-recycling flow is adjusted to compensate for a pressure loss in the methanol reactor arrangement.
C07C 29/152 - Préparation de composés comportant des groupes hydroxyle ou O-métal liés à un atome de carbone ne faisant pas partie d'un cycle aromatique à six chaînons par réduction exclusivement des oxydes de carbone avec de l'hydrogène ou des gaz contenant de l'hydrogène caractérisée par le réacteur utilisé
B01J 19/24 - Réacteurs fixes sans élément interne mobile
77.
REACTOR FOR ENDOTHERMIC HIGH-TEMPERATURE REACTIONS
A reactor for carrying out an endothermic reaction, in particular a high-temperature reaction, in which a product gas is obtained from a feed gas, wherein: the reactor surrounds a reactor interior; the reactor is configured to provide a reactor bed in a reaction zone of the reactor interior, which reactor bed comprises a large number of solid material particles; the reactor is also configured to guide the feed gas into the reaction zone; in order to heat the feed gas, the reactor is designed to heat the solid material particles in the reaction zone such that, by transferring heat from the solid material particles to the feed gas, the feed gas in the reaction zone can be heated to a reaction temperature in order to participate as a starting product in the endothermic reaction for producing the product gas.
B01J 8/08 - Procédés chimiques ou physiques en général, conduits en présence de fluides et de particules solidesAppareillage pour de tels procédés avec des particules mobiles
B01J 8/12 - Procédés chimiques ou physiques en général, conduits en présence de fluides et de particules solidesAppareillage pour de tels procédés avec des particules mobiles se déplaçant par gravité en un flux descendant
09 - Appareils et instruments scientifiques et électriques
35 - Publicité; Affaires commerciales
42 - Services scientifiques, technologiques et industriels, recherche et conception
Produits et services
Application software; communications, networking and social
networking software; data and file management and database
software; media and publishing software; office and business
application software; artificial intelligence software and
machine learning software; software for monitoring,
analyzing, controlling and executing operations in the
physical world; virtual and augmented reality software; web
applications and server software; content management
software; electronic commerce and electronic payment
software; information technology, audio-visual, multimedia
and photographic apparatus; data storage apparatus and
media; data processing apparatus and equipment and
accessories [electrical and mechanical]; computers and
computer hardware; data processing software; data processing
equipment; data processing terminals; data processing
programs; data processing software for graphic display; data
processing programs recorded on machine-readable media;
computer software for data processing; data processing
systems. Business consulting services for data processing;
administrative data processing, systematization and
management; administrative data processing; auxiliary
services in business matters; administrative services
relating to business transactions and financial records;
registration, recording, compilation and systematization of
written communications and records; compilation of
mathematical and statistical data; office work, namely, file
management by means of computers; wholesale and retail
services relating to computer software, application
software, communications, networking, and social networking
software, data and file management and database software,
media and publishing software, office and enterprise
application software, artificial intelligence software and
machine learning software, software for monitoring,
analyzing, controlling, and executing operations in the
physical world, virtual and augmented reality software, web
applications and server software, content management
software, electronic commerce software, and electronic
payments software, information technology, audio-visual,
multimedia and photographic equipment, data storage devices
and media, data processing devices and equipment and
accessories [electrical and mechanical], computers and
computer hardware data processing software, data processing
equipment, data processing terminals, data processing
programs, data processing systems, data processing devices
and equipment and accessories [electrical and mechanical],
data processing software for graphical representations, data
processing programs recorded on machine-readable media,
computer software for data processing. Engineering and scientific services; engineering and
computer-aided engineering services; computer engineering
and technological services; IT programming services; design,
development, programming and implementation of software;
computer hardware development; hosting services; software as
a service [SaaS] and rental of software; platform as a
service [PaaS]; computer software and computer systems
design; IT consultancy, information and advisory services;
information technology [IT] consultancy; information
technology architecture and infrastructure consulting and
information services; data processing program development;
data processing program development services; data
processing program development for third parties; data
processing program design, maintenance, and updating; data
processing equipment design and development; data processing
computer program development and creation; data processing
system design and development.
79.
Device and method for the utilisation of low-temperature heat by decoupling the low-temperature heat from process gas, and use
A low-temperature heat utilization assembly may be configured to decouple low-temperature heat from process gas at temperatures below 200° C. and to provide the process gas at a lowered intermediate temperature or at a still further lowered final temperature for at least one subsequent process. In the low-temperature heat utilization assembly the process gas may be fed to a first unit, by means of which the temperature may be lowered to the intermediate temperature. The process gas may in some cases be provided to a heat exchanger stage for further lowering to the final temperature. The first unit is an ORC unit for energy transformation of the heat energy into electrical energy and may be coupled to an electrical consumer unit. The ORC unit may be configured for energy feedback of electrical energy within the low-temperature heat utilization assembly or to a process upstream of the ORC unit.
F01K 23/06 - Ensembles fonctionnels caractérisés par plus d'une machine motrice fournissant de l'énergie à l'extérieur de l'ensemble, ces machines motrices étant entraînées par des fluides différents les cycles de ces machines motrices étant couplés thermiquement la chaleur de combustion provenant de l'un des cycles chauffant le fluide dans un autre cycle
F01K 3/18 - Ensembles fonctionnels caractérisés par l'emploi d'accumulateurs de vapeur ou de chaleur ou bien de réchauffeurs intermédiaires de vapeur comportant des réchauffeurs
An exhaust air scrubber for removing dust, abraded product, and water-soluble constituents from process exhaust air may include in a single housing a cleaning stage that includes a droplet separator and a packing disposed below the droplet separator. The exhaust air scrubber may also include an inlet apparatus for process exhaust air disposed in a lower portion of the housing, a withdrawal apparatus for scrubbing solution, and a withdrawal conduit for cleaned exhaust air, with the withdrawal conduit beginning inside the housing above the cleaning stage, passing downward inside the housing, and passing out of the housing to an outside in the lower portion of the housing below the cleaning stage. The scrubber may further include a feed conduit for scrubbing solution in an upper portion of the housing above the cleaning stage.
A process can be utilized to produce hydrogen and pyrolysis carbon from hydrocarbons where the hydrocarbons are converted into hydrogen and carbon in a reactor at temperatures of 1000° C. or more and the reactor has at least two electrodes that are at a distance from one another in a flow direction of the hydrocarbons. To avoid carbon deposits in a region between the electrodes, which can lead to failure of a heating system, the carbon particles may be introduced into the reactor in countercurrent to the hydrocarbons and may be heated in a heating zone between the electrodes to a temperature above a decomposition temperature of the hydrocarbons at such a mass flow that a reaction zone in which the hydrocarbons are converted into hydrogen and carbon is spatially separated in a flow direction of the carbon particles from the heating zone.
C01B 3/28 - Production d'hydrogène ou de mélanges gazeux contenant de l'hydrogène par décomposition de composés organiques gazeux ou liquides d'hydrocarbures avec des particules solides mobiles
A method of removing inert gas dissolved in liquid ammonia involves evaporating, compressing, and then condensing the liquid ammonia together with the inert gas dissolved therein. Thereby, a product stream of warm liquid ammonia that has been freed of the inert gas is obtained, which is under elevated pressure relative to standard pressure and hence suitable for immediate use in methods in which pure liquid pressurized ammonia is required. If, by contrast, the ammonia is cooled first, for example, below the boiling temperature for ammonia and expanded to standard pressure to store it in tanks as liquid ammonia at low temperatures, it is necessary first to reheat and compress it for further processing operations. Thus the disclosed methods lead to significant energy savings.
09 - Appareils et instruments scientifiques et électriques
35 - Publicité; Affaires commerciales
42 - Services scientifiques, technologiques et industriels, recherche et conception
Produits et services
Recorded software for use in hydrogen and chemical production modeling; recorded communications, networking and social networking software for use in hydrogen and chemical production modeling; recorded data and file management and database software for use in hydrogen and chemical production modeling; recorded media and publishing software for use in hydrogen and chemical production modeling; recorded office and business application software for use in hydrogen and chemical production modeling; recorded artificial intelligence software and machine learning software for use in hydrogen and chemical production modeling; recorded software for monitoring, analyzing, controlling and executing operations in the physical world for use in hydrogen and chemical production modeling; recorded virtual and augmented reality software for use in hydrogen and chemical production modeling; recorded web applications and server software for use in hydrogen and chemical production modeling; recorded content management software for use in hydrogen and chemical production modeling; recorded electronic commerce and electronic payment software for use in hydrogen and chemical production modeling; data processing apparatus and equipment; computers and computer hardware; recorded data processing software; data processing equipment; data processing computer terminals; recorded data processing computer programs; recorded data processing software for graphic display; recorded data processing programs recorded on machine-readable media; recorded computer software for data processing Business consulting services in the field of hydrogen and chemical production modeling for data processing; administrative data processing, systematization and management in the field of hydrogen and chemical production modeling; registration, recording, compilation and systematization of written communications and records in the field of hydrogen and chemical production modeling; compilation of mathematical and statistical data; office work, namely, file management by means of computers; wholesale and retail store services store featuring computer software, application software, communications, networking, and social networking software, data and file management and database software, media and publishing software, office and enterprise application software, artificial intelligence software and machine learning software, software for monitoring, analyzing, controlling, and executing operations in the physical world, virtual and augmented reality software, web applications and server software, content management software, electronic commerce software, and electronic payments software, information technology, audio-visual, multimedia and photographic equipment, data storage devices and media, data processing devices and equipment and accessories electrical and mechanical, computers and computer hardware data processing software, data processing equipment, data processing terminals, data processing programs, data processing systems, data processing devices and equipment and accessories electrical and mechanical, data processing software for graphical representations, data processing programs recorded on machine-readable media, computer software for data processing Engineering and scientific research services; engineering and computer-aided engineering services; computer engineering and technological consulting services in the field of engineering; (IT) computer programming services; design, development, programming and implementation of computer software; computer hardware development; hosting services, namely, Hosting internet sites for others; software as a service (SaaS) services featuring software for hydrogen and chemical production modeling; rental of computer software for hydrogen and chemical production modeling; platform as a service (PaaS) services featuring software for hydrogen and chemical production modeling; computer software and computer systems design; (IT) consultancy, information and advisory services; information technology (IT) consultancy; information technology architecture and infrastructure consulting and information services, namely, (IT) consulting services; data processing computer program development; data processing computer program development services; data processing computer program development for third parties; data processing computer program design, maintenance, and updating; data processing computer equipment design and development; data processing computer program development and creation; data processing system design and development
84.
PROCESS FOR ELECTROCHEMICAL PREPARATION OF AMMONIA
A process for preparing ammonia via an electrolysis cell may involve feeding nitrogen as a first reactant into the electrolysis cell and using water or water vapor as a second reactant for electrolysis. In at least one step downstream of the electrolysis, there is a separation of other components from the ammonia, such as an at-least-partial separation of nitrogen, water, argon and/or hydrogen. Recovery of the reactants is connected upstream of the ammonia electrolysis. The nitrogen used as the first reactant may be procured beforehand in an air fractionation plant. The process may further involve removing from the electrolysis cell oxygen formed as a by-product in the electrolysis at an anode.
The invention relates to a process for producing hydrogen, carbon monoxide and a carbon-containing product in at least one reaction apparatus, wherein the at least one reaction apparatus comprises a bed of carbon-containing material and is characterized in that the bed of carbon-containing material in the at least one reaction apparatus is alternately heated to a temperature of >800° C. and, no later than upon reaching a temperature of 1800° C., cooled to a maximum of 800° C., wherein hydrogen and carbon monoxide are produced during the heating phase and carbon and hydrogen are produced during the cooling phase.
B01J 8/04 - Procédés chimiques ou physiques en général, conduits en présence de fluides et de particules solidesAppareillage pour de tels procédés avec des particules immobiles, p. ex. dans des lits fixes le fluide passant successivement à travers plusieurs lits
C01B 3/24 - Production d'hydrogène ou de mélanges gazeux contenant de l'hydrogène par décomposition de composés organiques gazeux ou liquides d'hydrocarbures
01 - Produits chimiques destinés à l'industrie, aux sciences ainsi qu'à l'agriculture
04 - Huiles et graisses industrielles; lubrifiants; combustibles
07 - Machines et machines-outils
11 - Appareils de contrôle de l'environnement
37 - Services de construction; extraction minière; installation et réparation
39 - Services de transport, emballage et entreposage; organisation de voyages
40 - Traitement de matériaux; recyclage, purification de l'air et traitement de l'eau
42 - Services scientifiques, technologiques et industriels, recherche et conception
Produits et services
Chemicals used in industry and science, in particular synthesis gas for use in production processes, in particular for the production of hydrogen, ammonia, fuels and methanol. Fuels (including motor spirit), in particular synthesis gas for use in turbines, burners, motors and engines. Gas generators, gasifiers, in particular for generating synthesis gas from carbonaceous fuels and for superheating steam. Burners, furnaces, loading apparatus for furnaces, gas generators, heat regenerators and steam generating apparatus being parts of gasification installations, in particular being installations for the manufacture of chemical agents, primarily synthesis gas. Installation, assembly, repair and maintenance of apparatus and equipment, and of installations and structural parts or components composed thereof, for the conversion of carbonaceous materials, in particular for the production of synthesis gases. Supplying consumers through the delivery of gas, distribution of gas and heat, in particular in the production of synthesis gas and steam. Heat generation, in particular through the generation of synthesis gas. Scientific and technological services, in particular engineering and industrial design, primarily consultancy and planning relating to the construction, expansion, dismantling or operation of chemical installations or parts thereof, in particular chemical installations for the production of synthesis gas; research and development in the field of chemistry and engineering, in particular relating to chemical production processes and related chemical installations of parts thereof, primarily chemical installations for the production of synthesis gas.
87.
Method and device for producing ammonia or hydrogen and use of the device
An apparatus for producing ammonia or hydrogen may include a) a gas stream feed conduit having a connecting conduit to a steam reformer with a waste heat section; b) a heat exchanger downstream of the gas stream feed conduit; c) a gas stream preheater downstream of the heat exchanger; d) a recirculation conduit which is located downstream of the gas stream preheater and leads to the gas stream feed conduit or, upstream of the heat exchanger, to the connecting conduit; and e) the steam reformer with the waste heat section, where the waste heat section may be in thermal contact with the gas stream preheater and the flow of the gas stream which has been heated in the gas stream preheater through the recirculation conduit can be regulated. A process for producing ammonia or hydrogen may employ such an apparatus.
C01B 3/02 - Production d'hydrogène ou de mélanges gazeux contenant de l'hydrogène
C01B 3/34 - Production d'hydrogène ou de mélanges gazeux contenant de l'hydrogène par réaction de composés organiques gazeux ou liquides avec des agents gazéifiants, p. ex. de l'eau, du gaz carbonique, de l'air par réaction d'hydrocarbures avec des agents gazéifiants
A process may be utilized to coat urea-containing granules with organic polymers. The process may involve compressing gaseous carbon dioxide and condensing the carbon dioxide to obtain liquid carbon dioxide, increasing the pressure and/or the temperature above the critical point of carbon dioxide and obtaining supercritical carbon dioxide, dissolving an organic polymer in the supercritical carbon dioxide to obtain a polymer-containing solution, and mixing the polymer-containing solution with urea-containing granules and lowering the temperature and/or the pressure below the critical point of carbon dioxide and obtaining coated urea-containing granules and gaseous carbon dioxide. In some cases the organic polymer may include biodegradable polymers, and the polymer-containing solution may contain between 20 to 70% by weight biodegradable polymers.
B01J 2/00 - Procédés ou dispositifs pour la granulation de substances, en généralTraitement de matériaux particulaires leur permettant de s'écouler librement, en général, p. ex. en les rendant hydrophobes
B05D 1/02 - Procédés pour appliquer des liquides ou d'autres matériaux fluides aux surfaces réalisés par pulvérisation
C07C 273/10 - Préparation d'urée ou de ses dérivés, c.-à-d. de composés contenant l'un des groupes les atomes d'azote ne faisant pas partie de groupes nitro ou nitroso d'urée, de ses sels, de ses complexes ou de ses composés d'addition combinée avec la synthèse d'ammoniac
F25J 1/00 - Procédés ou appareils de liquéfaction ou de solidification des gaz ou des mélanges gazeux
89.
METHOD FOR AVOIDING VOC AND HAP EMISSIONS FROM SYNTHESIS GAS-PROCESSING SYSTEMS
Systems and methods for the synthesis of ammonia includes a reformer; a carbon monoxide converter; a carbon dioxide scrubber unit with recovery; a methanation unit; and an ammonia synthesis unit; wherein the carbon dioxide scrubber unit with recovery is connected to at least one fired auxiliary steam boiler.
B01D 53/14 - Séparation de gaz ou de vapeursRécupération de vapeurs de solvants volatils dans les gazÉpuration chimique ou biologique des gaz résiduaires, p. ex. gaz d'échappement des moteurs à combustion, fumées, vapeurs, gaz de combustion ou aérosols par absorption
C01B 3/02 - Production d'hydrogène ou de mélanges gazeux contenant de l'hydrogène
C01B 3/58 - Séparation de l'hydrogène ou des gaz contenant de l'hydrogène à partir de mélanges gazeux, p. ex. purification par contact avec des solidesRégénération des solides usés comportant une réaction catalytique
90.
METHOD FOR PROVIDING SYNTHESIS GAS BY MEANS OF AN ADDITIONAL ELECTRIC HEATER
A reformer for steam reforming a hydrocarbon-containing mixture, including a combustion chamber, a burner arranged within the combustion chamber, a first reactor tube which is arranged at least in sections within the combustion chamber, a catalyst arranged inside the first reactor tube, and an electrically heatable heating element is arranged inside the first reactor tube.
F16L 53/38 - Chauffage par résistance ohmique en utilisant des éléments de chauffage électrique allongés, p. ex. des fils ou des rubans
C01B 3/38 - Production d'hydrogène ou de mélanges gazeux contenant de l'hydrogène par réaction de composés organiques gazeux ou liquides avec des agents gazéifiants, p. ex. de l'eau, du gaz carbonique, de l'air par réaction d'hydrocarbures avec des agents gazéifiants avec des catalyseurs
Embodiments provide a process for purifying an alkylene oxide composition, which comprises (1) obtaining a crude alkylene oxide composition comprising an ionic component; (2) passing the crude alkylene oxide composition through a molecular sieve; and (3) obtaining a purified alkylene oxide composition. A purified alkylene oxide composition suitable for a subsequent process can be obtained.
A process for performing the water gas shift reaction wherein raw synthesis gas is reacted in the presence of steam and at least one water gas shift catalyst to convert carbon monoxide into carbon dioxide and to form hydrogen. The raw synthesis gas is initially passed through at least one unit for high-temperature CO conversion and subsequently, downstream thereof, passed through at least one unit for low-temperature CO conversion. After passing through the at least one unit for high-temperature CO conversion the synthesis gas stream is divided into at least two substreams. The first substream is passed through a first unit for low-temperature CO conversion and the second substream is passed through a second unit for low-temperature CO conversion, wherein both units for low-temperature CO conversion are arranged in parallel relative to one another.
C01B 3/16 - Production d'hydrogène ou de mélanges gazeux contenant de l'hydrogène par réaction de composés inorganiques comportant un hydrogène lié électropositivement, p. ex. de l'eau, des acides, des bases, de l'ammoniac, avec des agents réducteurs inorganiques par réaction de la vapeur d'eau avec l'oxyde de carbone avec des catalyseurs
A process for the combined production of methanol and ammonia, wherein a reactant stream includes carbon monoxide is supplied to a recovery assembly to obtain first and second hydrogen-containing streams, each having an increased molar proportion of hydrogen compared to the reactant stream. The recovery assembly includes a shift conversion in which the carbon monoxide of at least one carbon monoxide-containing stream is at least partially converted into hydrogen and carbon dioxide by reaction with steam to obtain a converted stream having hydrogen and carbon dioxide at least partially recycled to a hydrogen recovery from which the first and second hydrogen-containing streams are obtained. A nitrogen stream and, at least partially, the first hydrogen-containing stream are supplied to an ammonia reactor assembly for at least partial conversion into ammonia and, at least partially, the second hydrogen-containing stream is supplied to a methanol reactor assembly for at least partial conversion into the methanol.
C01B 3/02 - Production d'hydrogène ou de mélanges gazeux contenant de l'hydrogène
C01B 3/12 - Production d'hydrogène ou de mélanges gazeux contenant de l'hydrogène par réaction de composés inorganiques comportant un hydrogène lié électropositivement, p. ex. de l'eau, des acides, des bases, de l'ammoniac, avec des agents réducteurs inorganiques par réaction de la vapeur d'eau avec l'oxyde de carbone
C01B 3/50 - Séparation de l'hydrogène ou des gaz contenant de l'hydrogène à partir de mélanges gazeux, p. ex. purification
C07C 29/151 - Préparation de composés comportant des groupes hydroxyle ou O-métal liés à un atome de carbone ne faisant pas partie d'un cycle aromatique à six chaînons par réduction exclusivement des oxydes de carbone avec de l'hydrogène ou des gaz contenant de l'hydrogène
An ammonia plant having a first and second reactor and a start-up oven having at least one first heat exchanger. The first reactor operates under a higher internal pressure than the second reactor. The start-up oven is connected via a piping system for at least one synthesis gas to the first and second reactor. Ammonia is produced by heating synthesis gas in the start-up oven and transferring the heated synthesis gas to the first reactor for initiating the chemical reaction. Synthesis gas is heated with the same start-up oven and is transferred to the second reactor for initiating the chemical reaction, wherein high-pressure synthesis of ammonia occurs in the first reactor and low-pressure synthesis of ammonia occurs in the second reactor at a lower process pressure than in the first reactor.
A tray for a mass-transfer column may allow contact between liquid and gas phases. The tray may include a tray inlet via which the tray is supplied with a liquid phase, a tray outlet via which the liquid phase flows out from the tray, first guide mechanism for guiding the liquid phase where the first guide mechanism forms a first flow path along which the liquid phase flows from the tray inlet to the tray outlet, an inlet for a temperature-control fluid, an outlet for the temperature-control fluid, and second guide mechanism for guiding the temperature-control fluid for heat exchange with the liquid phase. The second guide mechanism forms a second flow path that overlaps with the first flow path and leads from the inlet to the outlet. The temperature-control fluid flows along the second flow path in a direction opposite the flow direction of the liquid phase.
B01D 3/16 - Colonnes de fractionnement dans lesquelles la vapeur barbote à travers le liquide
B01D 3/22 - Colonnes de fractionnement dans lesquelles la vapeur barbote à travers le liquide à grilles ou plateaux perforés horizontauxConstruction de ces éléments
B01D 3/32 - Autres caractéristiques de colonnes de fractionnement
B01D 53/18 - Unités d'absorptionDistributeurs de liquides
97.
Method for producing syngas, as well as syngas cooling assembly and use
A method of producing synthesis gas in a dual pressure level ammonia plant having a first synthesis section operated in once through fashion at a first relatively lower high pressure and having a second synthesis section operated in recirculating fashion at a second relatively higher high pressure. In the first synthesis section downstream of an OT reactor of the first synthesis section the synthesis gas is cooled using cooling medium at a pressure below the first high pressure, wherein the cooling medium is provided at a pressure below the first high pressure level by means of a medium pressure steam generator or wherein the cooling is effected by means of the medium pressure steam generator. The disclosure further relates to a synthesis gas cooling assembly in such a dual pressure level ammonia plant and at least one plant component for providing or for utilizing the cooling medium.
The invention relates to a method for treating an exhaust gas flow (9) arising in a system (7) for producing aluminium via the electrolytic reduction of aluminium oxide in a melt, using at least one anode made of a carbon-containing material, said exhaust gas flow containing carbon oxides due to the reduction of the aluminium oxide by means of the carbon, wherein, according to the invention, at least one sub-flow of the carbon oxide contained in the exhaust gas flow is reacted with hydrogen (23) or mixed with a hydrogen flow and then supplied for utilisation. After a purification and conditioning of the exhaust gas flow in a device (16), e.g. an enrichment with carbon monoxide can then be carried out in a reactor (20) and the syngas obtained in this way can be supplied to a chemical or biotechnological system (25) for the synthesis of valuable chemical substances.
The invention relates to a method for the synthesis of methanol (1). wherein: a CO2 stream (2). predominantly consisting of carbon dioxide, and a H stream (3), predominantly consisting of hydrogen, is supplied to a methanol reactor assembly (7) for conversion into methanol; a residual gas stream (9) containing unreacted hydrogen is recovered from the methanol reactor assembly (7); and the unreacted hydrogen is fed back, at least in part, to the methanol reactor assembly (7). The method is characterised in that the residual gas stream (9) is supplied to a hydrogen recovery assembly (8) for recovering a return stream (4) containing the unreacted hydrogen, and in that the molar hydrogen proportion in the return stream (4) is greater than in the residual gas stream (9). The invention also relates to a corresponding system for the synthesis of methanol (1).
C07C 29/151 - Préparation de composés comportant des groupes hydroxyle ou O-métal liés à un atome de carbone ne faisant pas partie d'un cycle aromatique à six chaînons par réduction exclusivement des oxydes de carbone avec de l'hydrogène ou des gaz contenant de l'hydrogène
In a process for the epoxidation of propene, comprising continuously reacting a propene feed with hydrogen peroxide in the presence of an epoxidation catalyst in a reaction step, using propene in excess to hydrogen peroxide, to provide a liquid reaction mixture comprising non-reacted propene, extra safety measures caused by the presence of oxygen during work-up of the liquid reaction mixture of the epoxidation reaction can be avoided by stripping liquid reaction mixture from step a) with an inert gas to provide an oxygen depleted stripped liquid reaction mixture and a strip gas stream, selecting the amount of inert gas to provide an oxygen concentration in the strip gas stream in the range of from 0.1 to 10% by weight, separating non-reacted propene from the strip gas stream and recycling it to the reaction step, and separating propene oxide from the stripped liquid reaction mixture.
C07D 301/12 - Synthèse du cycle de l'oxirane par oxydation de composés non saturés, ou de mélanges de composés non saturés et de composés saturés par le peroxyde d'hydrogène ou par des peroxydes ou peracides inorganiques
