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 of hydrogen or of gaseous mixtures containing hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts
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 - Chemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes with moving particles
B01J 8/12 - Chemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes with moving particles moved by gravity in a downward flow
7.
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 - Chemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes
B01J 8/12 - Chemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes with moving particles moved by gravity in a downward flow
B01J 19/00 - Chemical, physical or physico-chemical processes in generalTheir relevant apparatus
8.
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 - Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural serial stages only including at least one extraction step
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 - Separation of gases or vapoursRecovering vapours of volatile solvents from gasesChemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases or aerosols
B01J 8/00 - Chemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes
B01J 8/06 - Chemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes with stationary particles, e.g. in fixed beds in tube reactorsChemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes with stationary particles, e.g. in fixed beds the solid particles being arranged in tubes
C25B 15/08 - Supplying or removing reactants or electrolytesRegeneration of electrolytes
11.
DECOMPOSITION OF AMMONIA ON NICKEL-BASED CATALYSTS
C01B 3/04 - Production of hydrogen or of gaseous mixtures containing hydrogen by decomposition of inorganic compounds, e.g. ammonia
B01J 8/06 - Chemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes with stationary particles, e.g. in fixed beds in tube reactorsChemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes with stationary particles, e.g. in fixed beds the solid particles being arranged in tubes
B01J 19/24 - Stationary reactors without moving elements inside
12.
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 of hydrogen or of gaseous mixtures containing hydrogen by decomposition of inorganic compounds, e.g. ammonia
B01J 8/06 - Chemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes with stationary particles, e.g. in fixed beds in tube reactorsChemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes with stationary particles, e.g. in fixed beds the solid particles being arranged in tubes
B01J 19/24 - Stationary reactors without moving elements inside
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.
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 - Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbonsHydrofinishing
C01B 3/04 - Production of hydrogen or of gaseous mixtures containing hydrogen by decomposition of inorganic compounds, e.g. ammonia
C01B 17/04 - Preparation of sulfurPurification from gaseous sulfur compounds including gaseous sulfides
C10G 49/00 - Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups , , , , or
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 - Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases
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)
Inventor
Gonnard, Sebastien
Morin, Mathieu
Heraud, Jean-Philippe
Abstract
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 of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
C10G 45/58 - Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour pointSelective hydrocracking of normal paraffins
C10J 3/00 - Production of gases containing carbon monoxide and hydrogen, e.g. synthesis gas or town gas, from solid carbonaceous materials by partial oxidation processes involving oxygen or steam
C10K 1/10 - Purifying combustible gases containing carbon monoxide by washing with liquidsReviving the used wash liquors with aqueous liquids
C10K 3/04 - Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide by catalytic treatment reducing the carbon monoxide content
COMMISSARIAT A L'ENERGIE ATOMIQUE ET AUX ENERGIES ALTERNATIVES (France)
AXENS (France)
BIONEXT (France)
Inventor
Bournay, Laurent
Gonnard, Sebastien
Heraud, Jean-Philippe
Morin, Mathieu
Volland, Eric
Abstract
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 - Hearth-type furnaces, e.g. of reverberatory typeElectric arc furnaces of multiple-hearth typeHearth-type furnaces, e.g. of reverberatory typeElectric arc furnaces of multiple-chamber typeCombinations of hearth-type furnaces
F27B 3/06 - Hearth-type furnaces, e.g. of reverberatory typeElectric arc furnaces with movable working chambers or hearths, e.g. tiltable
F27B 3/12 - Working chambers or casingsSupports therefor
F27B 3/22 - Arrangements of air or gas supply devices
F27B 9/18 - Furnaces through which the charge is moved mechanically, e.g. of tunnel type Similar furnaces in which the charge moves by gravity characterised by the path of the charge during treatmentFurnaces through which the charge is moved mechanically, e.g. of tunnel type Similar furnaces in which the charge moves by gravity characterised by the means by which the charge is moved during treatment the charge moving in a circular or arcuate path under the action of scrapers or pushers
F27B 9/30 - Details, accessories or equipment specially adapted for furnaces of these types
F27D 7/02 - Supplying steam, vapour, gases or liquids
F27B 9/02 - Furnaces through which the charge is moved mechanically, e.g. of tunnel type Similar furnaces in which the charge moves by gravity of multiple-track typeFurnaces through which the charge is moved mechanically, e.g. of tunnel type Similar furnaces in which the charge moves by gravity of multiple-chamber typeCombinations of furnaces
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 - Chemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
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 - Preparation of urea or its derivatives, i.e. compounds containing any of the groups the nitrogen atoms not being part of nitro or nitroso groups of urea, its salts, complexes or addition compounds combined with the synthesis of ammonia
C07C 273/04 - Preparation of urea or its derivatives, i.e. compounds containing any of the groups the nitrogen atoms not being part of nitro or nitroso groups of urea, its salts, complexes or addition compounds from carbon dioxide and ammonia
C07C 273/14 - SeparationPurificationStabilisationUse of additives
C07C 29/151 - Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases
C07C 45/38 - Preparation of compounds having C=O groups bound only to carbon or hydrogen atomsPreparation of chelates of such compounds by oxidation with molecular oxygen of C—O— functional groups to C=O groups being a primary hydroxy group
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 of hydrogen or of gaseous mixtures containing hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
26.
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 - Synthesis of the oxirane ring by oxidation of unsaturated compounds, or of mixtures of unsaturated and saturated compounds with hydrogen peroxide or inorganic peroxides or peracids
B01D 53/00 - Separation of gases or vapoursRecovering vapours of volatile solvents from gasesChemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases or aerosols
B01J 8/06 - Chemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes with stationary particles, e.g. in fixed beds in tube reactorsChemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes with stationary particles, e.g. in fixed beds the solid particles being arranged in tubes
B01D 53/94 - Chemical or biological purification of waste gases of engine exhaust gases by catalytic processes
C01B 3/04 - Production of hydrogen or of gaseous mixtures containing hydrogen by decomposition of inorganic compounds, e.g. ammonia
C01B 21/26 - Preparation by catalytic oxidation of ammonia
F02C 3/20 - Gas-turbine plants characterised by the use of combustion products as the working fluid using a special fuel, oxidant, or dilution fluid to generate the combustion products
F02D 19/06 - Controlling engines characterised by their use of non-liquid fuels, pluralities of fuels, or non-fuel substances added to the combustible mixtures peculiar to engines working with pluralities of fuels, e.g. alternatively with light and heavy fuel oil, other than engines indifferent to the fuel consumed
F02M 21/02 - Apparatus for supplying engines with non-liquid fuels, e.g. gaseous fuels stored in liquid form for gaseous fuels
F01N 3/20 - Exhaust or silencing apparatus having means for purifying, rendering innocuous, or otherwise treating exhaust for rendering innocuous by thermal or catalytic conversion of noxious components of exhaust characterised by methods of operationControl specially adapted for catalytic conversion
B01D 53/94 - Chemical or biological purification of waste gases of engine exhaust gases by catalytic processes
C01B 3/04 - Production of hydrogen or of gaseous mixtures containing hydrogen by decomposition of inorganic compounds, e.g. ammonia
C01B 21/26 - Preparation by catalytic oxidation of ammonia
F02C 3/20 - Gas-turbine plants characterised by the use of combustion products as the working fluid using a special fuel, oxidant, or dilution fluid to generate the combustion products
F02D 19/06 - Controlling engines characterised by their use of non-liquid fuels, pluralities of fuels, or non-fuel substances added to the combustible mixtures peculiar to engines working with pluralities of fuels, e.g. alternatively with light and heavy fuel oil, other than engines indifferent to the fuel consumed
F02M 21/02 - Apparatus for supplying engines with non-liquid fuels, e.g. gaseous fuels stored in liquid form for gaseous fuels
F01N 3/20 - Exhaust or silencing apparatus having means for purifying, rendering innocuous, or otherwise treating exhaust for rendering innocuous by thermal or catalytic conversion of noxious components of exhaust characterised by methods of operationControl specially adapted for catalytic conversion
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 - Chemical or biological purification of waste gases of engine exhaust gases by catalytic processes
C01B 3/04 - Production of hydrogen or of gaseous mixtures containing hydrogen by decomposition of inorganic compounds, e.g. ammonia
C01B 21/26 - Preparation by catalytic oxidation of ammonia
F02C 3/20 - Gas-turbine plants characterised by the use of combustion products as the working fluid using a special fuel, oxidant, or dilution fluid to generate the combustion products
F02D 19/06 - Controlling engines characterised by their use of non-liquid fuels, pluralities of fuels, or non-fuel substances added to the combustible mixtures peculiar to engines working with pluralities of fuels, e.g. alternatively with light and heavy fuel oil, other than engines indifferent to the fuel consumed
F02M 21/02 - Apparatus for supplying engines with non-liquid fuels, e.g. gaseous fuels stored in liquid form for gaseous fuels
F01N 3/20 - Exhaust or silencing apparatus having means for purifying, rendering innocuous, or otherwise treating exhaust for rendering innocuous by thermal or catalytic conversion of noxious components of exhaust characterised by methods of operationControl specially adapted for catalytic conversion
32.
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 of hydrogen or of gaseous mixtures containing hydrogen by decomposition of gaseous or liquid organic compounds of hydrocarbons using moving solid particles using the fluidised bed technique
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 4/00 - Feed devicesFeed or outlet control devices
B01J 8/00 - Chemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes
C07C 273/04 - Preparation of urea or its derivatives, i.e. compounds containing any of the groups the nitrogen atoms not being part of nitro or nitroso groups of urea, its salts, complexes or addition compounds from carbon dioxide and ammonia
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 - Synthesis of the oxirane ring by oxidation of unsaturated compounds, or of mixtures of unsaturated and saturated compounds with hydrogen peroxide or inorganic peroxides or peracids
35.
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 - Chemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes
B01J 8/40 - Chemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes with fluidised particles according to "fluidised-bed" technique with fluidised bed subjected to vibrations or pulsations
B01J 8/42 - Chemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes with fluidised particles according to "fluidised-bed" technique with fluidised bed subjected to electric current or to radiations
B01J 19/08 - Processes employing the direct application of electric or wave energy, or particle radiationApparatus therefor
C10G 15/08 - Cracking of hydrocarbon oils by electric means, electromagnetic or mechanical vibrations, by particle radiation or with gases superheated in electric arcs by electric means or by electromagnetic or mechanical vibrations
C01B 3/02 - Production of hydrogen or of gaseous mixtures containing hydrogen
36.
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 - Chemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes with stationary particles, e.g. in fixed beds
B01J 8/04 - Chemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
B01J 19/00 - Chemical, physical or physico-chemical processes in generalTheir relevant apparatus
C01B 3/02 - Production of hydrogen or of gaseous mixtures containing hydrogen
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 - Heat-exchange apparatus having stationary conduit assemblies for one heat-exchange medium only, the media being in contact with different sides of the conduit wall, in which the other heat-exchange medium is a large body of fluid, e.g. domestic or motor car radiators with the heat-exchange conduits immersed in the body of fluid with tubular conduits
F28D 9/00 - Heat-exchange apparatus having stationary plate-like or laminated conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall
F28D 7/16 - Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits being arranged in parallel spaced relation
B01J 19/00 - Chemical, physical or physico-chemical processes in generalTheir relevant apparatus
B01J 8/02 - Chemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes with stationary particles, e.g. in fixed beds
39.
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 of hydrogen or of gaseous mixtures containing hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, 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 - Synthesis of the oxirane ring by oxidation of unsaturated compounds, or of mixtures of unsaturated and saturated compounds with hydrogen peroxide or inorganic peroxides or peracids
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 - Preparation by absorption of oxides of nitrogen
B01J 10/00 - Chemical processes in general for reacting liquid with gaseous media other than in the presence of solid particlesApparatus specially adapted therefor
B01J 19/32 - Packing elements in the form of grids or built-up elements for forming a unit or module inside the apparatus for mass or heat transfer
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.
F22B 1/14 - Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers the heat carrier being steam coming in direct contact with water in bulk or in sprays
45.
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 of hydrogen or of gaseous mixtures containing hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
C01B 3/50 - Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
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 of hydrogen or of gaseous mixtures containing hydrogen by decomposition of gaseous or liquid organic compounds of hydrocarbons using moving solid particles
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 of hydrogen or of gaseous mixtures containing hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
B01J 19/24 - Stationary reactors without moving elements inside
B01J 19/00 - Chemical, physical or physico-chemical processes in generalTheir relevant apparatus
50.
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 - Chemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes with moving particles moved by gravity in a downward flow
B01J 8/00 - Chemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes
C01B 3/30 - Production of hydrogen or of gaseous mixtures containing hydrogen by decomposition of gaseous or liquid organic compounds of hydrocarbons using moving solid particles using the fluidised bed technique
51.
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 of hydrogen or of gaseous mixtures containing hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts
C10K 3/02 - Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide by catalytic treatment
C07C 1/12 - Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon from oxides of carbon from carbon dioxide with hydrogen
C07C 29/50 - Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by oxidation reactions with formation of hydroxy groups with molecular oxygen only
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 - Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural serial stages only including at least one sorption step
C07C 7/11 - Purification, separation or stabilisation of hydrocarbonsUse of additives by absorption, i.e. purification or separation of gaseous hydrocarbons with the aid of liquids
C07C 7/08 - Purification, separation or stabilisation of hydrocarbonsUse of additives by distillation with the aid of auxiliary compounds by extractive distillation
C07C 7/06 - Purification, separation or stabilisation of hydrocarbonsUse of additives by distillation with the aid of auxiliary compounds by azeotropic distillation
C07C 7/144 - Purification, separation or stabilisation of hydrocarbonsUse of additives using membranes, e.g. selective permeation
C07C 7/00 - Purification, separation or stabilisation of hydrocarbonsUse of additives
B01D 53/14 - Separation of gases or vapoursRecovering vapours of volatile solvents from gasesChemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases or aerosols by absorption
B01D 53/22 - Separation of gases or vapoursRecovering vapours of volatile solvents from gasesChemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases or aerosols by diffusion
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 - Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon from oxides of carbon from carbon monoxide with hydrogen
C07C 29/151 - Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases
C07C 1/24 - Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon starting from organic compounds containing only oxygen atoms as hetero atoms by elimination of water
C07C 7/11 - Purification, separation or stabilisation of hydrocarbonsUse of additives by absorption, i.e. purification or separation of gaseous hydrocarbons with the aid of liquids
C07C 29/86 - SeparationPurificationStabilisationUse of additives by physical treatment by liquid-liquid treatment
B01J 35/00 - Catalysts, in general, characterised by their form or physical properties
B01D 53/14 - Separation of gases or vapoursRecovering vapours of volatile solvents from gasesChemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases or aerosols by absorption
54.
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 - Chemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes with moving particles moved by gravity in a downward flow
B01J 8/42 - Chemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes with fluidised particles according to "fluidised-bed" technique with fluidised bed subjected to electric current or to radiations
C01B 3/30 - Production of hydrogen or of gaseous mixtures containing hydrogen by decomposition of gaseous or liquid organic compounds of hydrocarbons using moving solid particles using the fluidised bed technique
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 - Processes involving the simultaneous production of more than one class of oxygen-containing compounds by reduction of oxygen-containing compounds by hydrogenation of oxides of carbon with moving catalysts
B01D 53/14 - Separation of gases or vapoursRecovering vapours of volatile solvents from gasesChemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases or aerosols by absorption
B01D 53/22 - Separation of gases or vapoursRecovering vapours of volatile solvents from gasesChemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases or aerosols by diffusion
C07C 1/04 - Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon from oxides of carbon from carbon monoxide with hydrogen
C07C 7/00 - Purification, separation or stabilisation of hydrocarbonsUse of additives
C07C 7/06 - Purification, separation or stabilisation of hydrocarbonsUse of additives by distillation with the aid of auxiliary compounds by azeotropic distillation
C07C 7/08 - Purification, separation or stabilisation of hydrocarbonsUse of additives by distillation with the aid of auxiliary compounds by extractive distillation
C07C 7/11 - Purification, separation or stabilisation of hydrocarbonsUse of additives by absorption, i.e. purification or separation of gaseous hydrocarbons with the aid of liquids
C07C 7/144 - Purification, separation or stabilisation of hydrocarbonsUse of additives using membranes, e.g. selective permeation
C07C 29/04 - Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by addition of hydroxy groups to unsaturated carbon-to-carbon bonds, e.g. with the aid of H2O2 by hydration of carbon-to-carbon double bonds
C10G 53/08 - Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural serial stages only including at least one sorption step
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 - Stationary reactors without moving elements inside
C08G 65/26 - Macromolecular compounds obtained by reactions forming an ether link in the main chain of the macromolecule from cyclic ethers by opening of the heterocyclic ring from cyclic ethers and other compounds
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 - Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases characterised by the reactor used
B01J 19/24 - Stationary reactors without moving elements inside
C01B 3/36 - Production of hydrogen or of gaseous mixtures containing hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using oxygen or mixtures containing oxygen as gasifying agents
C07C 29/151 - Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases
58.
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 - Chemical, physical or physico-chemical processes in generalTheir relevant apparatus
B01J 19/24 - Stationary reactors without moving elements inside
C01B 3/34 - Production of hydrogen or of gaseous mixtures containing hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
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 - Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases characterised by the reactor used
B01J 19/24 - Stationary reactors without moving elements inside
01 - Chemical and biological materials for industrial, scientific and agricultural use
04 - Industrial oils and greases; lubricants; fuels
07 - Machines and machine tools
11 - Environmental control apparatus
37 - Construction and mining; installation and repair services
39 - Transport, packaging, storage and travel services
40 - Treatment of materials; recycling, air and water treatment,
42 - Scientific, technological and industrial services, research and design
Goods & 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 - Chemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes with stationary particles, e.g. in fixed beds in tube reactorsChemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes with stationary particles, e.g. in fixed beds the solid particles being arranged in tubes
B01J 8/02 - Chemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes with stationary particles, e.g. in fixed beds
C01B 3/38 - Production of hydrogen or of gaseous mixtures containing hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts
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 - Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases
C07C 29/74 - SeparationPurificationStabilisationUse of additives
C07C 29/78 - SeparationPurificationStabilisationUse of additives by physical treatment by condensation or crystallisation
C07C 29/80 - SeparationPurificationStabilisationUse of additives by physical treatment by distillation
C25B 1/04 - Hydrogen or oxygen by electrolysis of water
C25B 15/08 - Supplying or removing reactants or electrolytesRegeneration of electrolytes
F25J 3/02 - Processes or apparatus for separating the constituents of gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
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 - Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases characterised by the reactor used
B01J 19/24 - Stationary reactors without moving elements inside
B01D 53/22 - Separation of gases or vapoursRecovering vapours of volatile solvents from gasesChemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases or aerosols by diffusion
64.
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 - Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases characterised by the reactor used
B01J 19/24 - Stationary reactors without moving elements inside
09 - Scientific and electric apparatus and instruments
35 - Advertising and business services
42 - Scientific, technological and industrial services, research and design
Goods & 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.
66.
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 - Plants characterised by more than one engine delivering power external to the plant, the engines being driven by different fluids the engine cycles being thermally coupled combustion heat from one cycle heating the fluid in another cycle
F01K 3/18 - Plants characterised by the use of steam or heat accumulators, or intermediate steam heaters, therein having heaters
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 of hydrogen or of gaseous mixtures containing hydrogen by decomposition of gaseous or liquid organic compounds of hydrocarbons using moving solid particles
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 - Scientific and electric apparatus and instruments
35 - Advertising and business services
42 - Scientific, technological and industrial services, research and design
Goods & 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
71.
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 - Chemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
C01B 3/24 - Production of hydrogen or of gaseous mixtures containing hydrogen by decomposition of gaseous or liquid organic compounds of hydrocarbons
01 - Chemical and biological materials for industrial, scientific and agricultural use
04 - Industrial oils and greases; lubricants; fuels
07 - Machines and machine tools
11 - Environmental control apparatus
37 - Construction and mining; installation and repair services
39 - Transport, packaging, storage and travel services
40 - Treatment of materials; recycling, air and water treatment,
42 - Scientific, technological and industrial services, research and design
Goods & 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.
74.
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 of hydrogen or of gaseous mixtures containing hydrogen
C01B 3/34 - Production of hydrogen or of gaseous mixtures containing hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
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 - Processes or devices for granulating materials, in generalRendering particulate materials free flowing in general, e.g. making them hydrophobic
B05D 1/02 - Processes for applying liquids or other fluent materials performed by spraying
C07C 273/10 - Preparation of urea or its derivatives, i.e. compounds containing any of the groups the nitrogen atoms not being part of nitro or nitroso groups of urea, its salts, complexes or addition compounds combined with the synthesis of ammonia
F25J 1/00 - Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
76.
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 - Separation of gases or vapoursRecovering vapours of volatile solvents from gasesChemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases or aerosols by absorption
C01B 3/02 - Production of hydrogen or of gaseous mixtures containing hydrogen
C01B 3/58 - Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with solidsRegeneration of used solids including a catalytic reaction
77.
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 - Ohmic-resistance heating using elongate electric heating elements, e.g. wires or ribbons
C01B 3/38 - Production of hydrogen or of gaseous mixtures containing hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts
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 of hydrogen or of gaseous mixtures containing hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents by reaction of water vapour with carbon monoxide using catalysts
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 of hydrogen or of gaseous mixtures containing hydrogen
C01B 3/12 - Production of hydrogen or of gaseous mixtures containing hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents by reaction of water vapour with carbon monoxide
C01B 3/50 - Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
C07C 29/151 - Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases
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.
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 - Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases
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 - Synthesis of the oxirane ring by oxidation of unsaturated compounds, or of mixtures of unsaturated and saturated compounds with hydrogen peroxide or inorganic peroxides or peracids
A device for waste gas scrubbing in a urea plant may be configured such that a waste gas passes along a transportation direction in the duct. The duct may include a first region for removing urea dust particles from the waste gas and a second region for removing chemical compounds from the waste gas, which can be integrated by an acid-base reaction into an aqueous liquid phase. A cross-sectional area of the duct extending perpendicular to the transportation direction in the second region may be greater than a cross-sectional area extending perpendicular to the transportation direction in the first region. Further, the device may be configured such that the duct extends horizontally at least in sections and/or the transportation direction of the waste gas through the duct extends horizontally in an installed state.
The present invention relates to an apparatus for the production of ammonia or hydrogen, comprising a) a gas stream feed conduit having a connecting conduit to a steam reformer with a waste heat section, b) a heat exchanger located downstream of the gas stream feed conduit; c) a gas stream preheater located 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 is 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. The invention further relates to a process for the production of ammonia or hydrogen using the apparatus of the invention and also to the use of this apparatus.
C01B 3/02 - Production of hydrogen or of gaseous mixtures containing hydrogen
C01B 3/34 - Production of hydrogen or of gaseous mixtures containing hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
2 content of <20% by volume with a chosen amount of ammonia. The oxygen-containing gas stream is produced by a device for: diluting an air stream with a gas stream comprising less than 20% by volume oxygen; or depleting oxygen from an oxygen-containing gas mixture, preferably from air; or by a combination thereof.
B01J 23/83 - Catalysts comprising metals or metal oxides or hydroxides, not provided for in group of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups with rare earths or actinides
B01J 23/00 - Catalysts comprising metals or metal oxides or hydroxides, not provided for in group
The integrated process comprises a step a) of dehydrogenating propane providing a stream S1 comprising propane and propene; a step b) of separating stream S1 in at least one rectification column, providing an overhead product stream S2 comprising more than 99% by weight propene, a side stream S3 comprising from 90 to 98% by weight propene and a bottoms product stream S4 enriched in propane; a step c) of reacting propene with hydrogen peroxide in the presence of an epoxidation catalyst using propene in molar excess; and a step d) of separating non-reacted propene and propene oxide from the reaction mixture of step c) providing a propene oxide product and a stream S5 comprising propene and propane; wherein stream S3 is passed to step c), stream S5 is recycled to step b) and stream S4 is recycled to step a).
C07D 301/12 - Synthesis of the oxirane ring by oxidation of unsaturated compounds, or of mixtures of unsaturated and saturated compounds with hydrogen peroxide or inorganic peroxides or peracids
C07C 5/32 - Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with formation of free hydrogen
During start-up of a continuous epoxidation of propene with hydrogen peroxide in a methanol solvent with a shaped titanium silicalite catalyst in a tube bundle reactor with a cooling jacket, cooling medium is fed at the rate for full load of the reactor with a constant entry temperature of from 20° C. to 50° C., methanol solvent is fed at a rate of from 50 to 100% for full load of the reactor, hydrogen peroxide is fed at a rate that starts with no more than 10% of the rate for full load and is increased continuously or stepwise to maintain a maximum temperature in the fixed bed of no more than 60° C. and a difference between the maximum temperature in the fixed bed and the cooling medium entry temperature of no more than 20° C., and propene is fed at a rate of from 20 to 100% of the rate for full load, increasing the feeding rate when the molar ratio of propene to hydrogen peroxide reaches the molar ratio for full load.
B01J 8/02 - Chemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes with stationary particles, e.g. in fixed beds
B01J 8/06 - Chemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes with stationary particles, e.g. in fixed beds in tube reactorsChemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes with stationary particles, e.g. in fixed beds the solid particles being arranged in tubes
C07D 301/12 - Synthesis of the oxirane ring by oxidation of unsaturated compounds, or of mixtures of unsaturated and saturated compounds with hydrogen peroxide or inorganic peroxides or peracids
In a process for the epoxidation of an olefin with hydrogen peroxide in the presence of a solvent, where a mixture comprising olefin, an aqueous hydrogen peroxide solution and a solvent is continuously passed through a fixed bed of an epoxidation catalyst comprising a titanium zeolite, addition of a chelating agent to the aqueous hydrogen peroxide solution before mixing it with solvent reduces or prevents formation of deposits on the catalyst and blocking of orifices of a liquid distributor.
C07D 301/12 - Synthesis of the oxirane ring by oxidation of unsaturated compounds, or of mixtures of unsaturated and saturated compounds with hydrogen peroxide or inorganic peroxides or peracids
B01J 29/89 - Silicates, aluminosilicates or borosilicates of titanium, zirconium or hafnium
C07B 41/04 - Formation or introduction of functional groups containing oxygen of ether, acetal or ketal groups
C07D 303/04 - Compounds containing oxirane rings containing only hydrogen and carbon atoms in addition to the ring oxygen atoms
B01J 19/24 - Stationary reactors without moving elements inside
91.
Process and reactor for the epoxidation of propene
Propene is continuously reacted with hydrogen peroxide in a tube bundle reactor comprising a multitude of parallel reaction tubes in the presence of a titanium silicalite catalyst arranged as a fixed bed in the reaction tubes. A cooling jacket encloses the reaction tubes, which has a feed point for cooling medium near the entry of the reaction tubes, a withdrawal point for cooling medium near the end of the reaction tubes and at least one additional withdrawal point upstream of the withdrawal point near the end of the reaction tubes. Cooling medium is fed to the feed point for cooling medium, a part of the cooling medium is withdrawn at the at least one additional withdrawal point and the remainder exits at the withdrawal point near the end of the reaction tubes.
C07D 301/12 - Synthesis of the oxirane ring by oxidation of unsaturated compounds, or of mixtures of unsaturated and saturated compounds with hydrogen peroxide or inorganic peroxides or peracids
C07D 303/04 - Compounds containing oxirane rings containing only hydrogen and carbon atoms in addition to the ring oxygen atoms
B01J 19/24 - Stationary reactors without moving elements inside
In a process for the epoxidation of an olefin by continuously reacting the olefin with hydrogen peroxide in a methanol solvent on a fixed bed epoxidation catalyst comprising a titanium zeolite, the hydrogen peroxide is used as an aqueous hydrogen peroxide solution made by an anthraquinone process, the aqueous hydrogen peroxide solution is mixed with methanol to give a feed mixture and this feed mixture is filtered before being contacted with the fixed bed epoxidation catalyst.
C07D 301/12 - Synthesis of the oxirane ring by oxidation of unsaturated compounds, or of mixtures of unsaturated and saturated compounds with hydrogen peroxide or inorganic peroxides or peracids
B01J 8/04 - Chemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
B01J 19/24 - Stationary reactors without moving elements inside
B01J 29/89 - Silicates, aluminosilicates or borosilicates of titanium, zirconium or hafnium
C07D 303/04 - Compounds containing oxirane rings containing only hydrogen and carbon atoms in addition to the ring oxygen atoms
01 - Chemical and biological materials for industrial, scientific and agricultural use
09 - Scientific and electric apparatus and instruments
Goods & Services
Solvents for aromatic extractive distillation for industrial and commercial use Chemical and physical apparatus for the production of pure organochemical combinations for scientific industrial purposes, namely distillation and extractive distillation with counter-flow apparatus being columns equipped with packings and trays, heat exchangers, control and regulation instruments, namely, control valves for pressure, temperature, level and flow of gases and liquids
In a process for the epoxidation of propene, comprising the steps of reacting propene with hydrogen peroxide, separating propene oxide and a recovered propene stream from the reaction mixture, separating propane from all or a part of the recovered propene stream in a C3 splitter column, and passing the overhead product stream of the C3 splitter column to the epoxidation step, a propane starting material with a propane fraction of from 0.002 to 0.10 is used, the epoxidation is operated to provide a propane fraction in the reaction mixture of from 0.05 to 0.20 and the C3 splitter column is operated to provide an overhead product stream which comprises a propane fraction of at least 0.04 in order to reduce the size and the energy consumption of the C3 splitter column.
C07D 301/12 - Synthesis of the oxirane ring by oxidation of unsaturated compounds, or of mixtures of unsaturated and saturated compounds with hydrogen peroxide or inorganic peroxides or peracids
C07D 301/19 - Synthesis of the oxirane ring by oxidation of unsaturated compounds, or of mixtures of unsaturated and saturated compounds with organic hydroperoxides
B01J 29/70 - Crystalline aluminosilicate zeolitesIsomorphous compounds thereof of types characterised by their specific structure not provided for in groups
B01D 53/14 - Separation of gases or vapoursRecovering vapours of volatile solvents from gasesChemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases or aerosols by absorption
C07C 273/10 - Preparation of urea or its derivatives, i.e. compounds containing any of the groups the nitrogen atoms not being part of nitro or nitroso groups of urea, its salts, complexes or addition compounds combined with the synthesis of ammonia
In a process for the epoxidation of propene, comprising the steps: reacting propene with hydrogen peroxide in the presence of a titanium silicalite catalyst and a methanol solvent; separating non-reacted propene and propene oxide from the resulting reaction mixture to provide a solvent mixture comprising methanol and water in a combined amount of at least 90% by weight; and feeding this solvent mixture as a feed stream to a continuously operated methanol distillation column at a feed point in the middle section of said column to provide an overhead product comprising at least 90% by weight methanol and a bottoms product comprising at least 90% by weight water; the addition of a liquid defoamer, having a solubility in the feed stream of less than 10 mg/kg at 25° C. and a surface tension at the liquid air interface of less than 22 mN/m at 20° C., at or above the feed point in an amount exceeding the solubility of the liquid defoamer in the feed stream suppresses foam formation in the methanol distillation column.
C07D 301/12 - Synthesis of the oxirane ring by oxidation of unsaturated compounds, or of mixtures of unsaturated and saturated compounds with hydrogen peroxide or inorganic peroxides or peracids
C07D 303/04 - Compounds containing oxirane rings containing only hydrogen and carbon atoms in addition to the ring oxygen atoms
B01D 3/34 - Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping with one or more auxiliary substances
A process for preparing nitric acid may involve vaporizing ammonia in at least one first ammonia vaporizer to produce an ammonia gas, oxidizing this ammonia gas to nitrogen dioxide in a plant section of a nitric acid plant, and absorbing the nitrogen dioxide in water to produce nitric acid. A residual gas containing nitrous gases may be taken off from the plant section of the nitric acid plant and conveyed to a residual-gas cleaning apparatus. The residual gas containing nitrous gases may be reduced by means of ammonia in the residual-gas cleaning apparatus, wherein ammonia-containing wastewater obtained in the at least one first ammonia vaporizer may be conveyed to the residual-gas cleaning apparatus. Such a process may eliminate or at least substantially reduce ammonia-containing wastewater. Furthermore, a plant can be used in this process for preparing nitric acid.
C02F 1/04 - Treatment of water, waste water, or sewage by heating by distillation or evaporation
C01C 1/12 - Separation of ammonia from gases and vapours
B01D 53/00 - Separation of gases or vapoursRecovering vapours of volatile solvents from gasesChemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases or aerosols
09 - Scientific and electric apparatus and instruments
11 - Environmental control apparatus
42 - Scientific, technological and industrial services, research and design
Goods & Services
Offshore power generation plants, mobile work platforms and floating platforms for transforming renewable energy, offshore wind energy or offshore water energy into chemicals or chemical energy; mobile work platforms and floating platforms for chemical plants, in particular ocean-going offshore mobile work platforms and floating platforms for chemical plants; plants for synthesizing ammonia, in particular ocean-going offshore plants; plants for the electrolysis of water, in particular ocean-going offshore plants for the electrolysis of sea water. Devices and instruments for storing energy; devices and instruments for chemically storing energy; electric control devices for energy management; computer hardware and computer software for information retrieval, analytics, and machine learning; computer software platforms for performing cluster computations; computer software for use in data management, collaborative data analysis, and statistics and machine learning, for general use; computer databases, database management software, computer software for database integration, computer software for accessing databases, computer software for creating searchable databases of information and data; computer and communications networks, data networks and data transmission networks; computer software for accessing and connecting computer networks; virtual assistant software; computer software for machine learning; artificial intelligence apparatus; computer software for information sharing via hosted services and communications devices, namely personal computers, mobile computers, mobile phones, mobile apps, mobile communication and telecommunication apparatus; computer software for real-time condition monitoring; computer software for use as an application programming interface (API); graphical user interface, computer software for user interface. Sea water desalination plants, sea water cleaning plants, sea water clarifying plants, sea water filtration plants, sea water purification plants, sea water osmosis or reverse osmosis plants, sea water desalination plants, all foregoing plants in particular ocean-going offshore plants. Development of energy and power management systems; programming of energy management software; advisory services relating to energy efficiency; computer programming for the energy industry; research in the field of energy; consultancy in the field of energy-saving; design and development of energy management software; design and development of energy distribution networks; engineering services in the field of energy technology; engineering services relating to energy supply systems; advisory services relating to the use of energy; design and development of regenerative energy generation systems; maintenance of computer software; design of computer database, installation of database software, hosting of databases; maintaining computer databases; providing temporary use of on-line non-downloadable operating software for accessing and using a cloud computing network; providing temporary use of web-based applications for innovation and knowledge management.
99.
Integrated process for making propene oxide and an alkyl tert-butyl ether
An integrated process for making propene oxide and an alkyl tert-butyl ether comprises dehydrogenating a feed stream comprising iso-butane to provide a stream comprising iso-butene and hydrogen and separating this stream into a stream consisting essentially of hydrogen and a stream comprising iso-butene; reacting a part or all of the stream comprising iso-butene with an alkanol in the presence of a solid acid catalyst to provide an alkyl tert-butyl ether; reacting a part or all of the stream consisting essentially of hydrogen with oxygen, providing a stream comprising hydrogen peroxide; and reacting a part or all of the stream comprising hydrogen peroxide with propene in the presence of an epoxidation catalyst to provide propene oxide.
C07D 301/12 - Synthesis of the oxirane ring by oxidation of unsaturated compounds, or of mixtures of unsaturated and saturated compounds with hydrogen peroxide or inorganic peroxides or peracids
C07C 41/09 - Preparation of ethers by dehydration of compounds containing hydroxy groups
C07C 41/34 - SeparationPurificationStabilisationUse of additives
An integrated process for making propene oxide and an alkyl tert-butyl ether comprises dehydrogenating a feed stream comprising propane and iso-butane to provide a stream comprising propene, iso-butene and hydrogen; separating this stream into a stream consisting essentially of hydrogen and a stream comprising propene and iso-butene; separating the stream comprising propene and iso-butene into a stream comprising propene and a stream comprising iso-butene; reacting a part or all of the stream comprising iso-butene with an alkanol in the presence of a solid acid catalyst to provide an alkyl tert-butyl ether; and reacting a part or all of the stream comprising propene with hydrogen peroxide in the presence of an epoxidation catalyst to provide propene oxide.
C07D 301/19 - Synthesis of the oxirane ring by oxidation of unsaturated compounds, or of mixtures of unsaturated and saturated compounds with organic hydroperoxides
C07C 41/06 - Preparation of ethers by addition of compounds to unsaturated compounds by addition of organic compounds only
C07C 5/32 - Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with formation of free hydrogen
C01B 15/023 - Preparation from organic compounds by the alkyl-anthraquinone process
B01J 21/06 - Silicon, titanium, zirconium or hafniumOxides or hydroxides thereof
