A plant, such as a hydrocarbon plant, is provided, which has a syngas stage for syngas generation and a synthesis stage where the syngas is synthesized to produce syngas derived product, such as hydrocarbon product. The plant makes effective use of various streams; in particular, CO2 and H2. The plant does not comprise an external feed of hydrocarbons. A method for producing a product stream, such as a hydrocarbon product stream is also provided.
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 3/36 - 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
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 plant and process for producing a hydrogen rich gas are provided, the process including the steps of: reforming a hydrocarbon feed in a reforming step thereby obtaining a synthesis gas including CH4, CO, CO2, H2 and H2O; shifting the synthesis gas in a shift configuration including a high temperature shift step; removal of CO2 upstream hydrogen purification unit, such as a pressure swing adsorption unit (PSA), and recycling off-gas from hydrogen purification unit and mix it with natural gas upstream prereformer feed preheater, prereformer, reformer feed preheater or ATR or shift as feed for the process.
C01B 3/40 - 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 characterised by the catalyst
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
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
B01J 19/24 - Stationary reactors without moving elements inside
B01J 23/06 - Catalysts comprising metals or metal oxides or hydroxides, not provided for in group of zinc, cadmium or mercury
C01B 3/48 - 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 followed by reaction of water vapour with carbon monoxide
C01B 3/50 - Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
C01B 3/52 - Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with liquidsRegeneration of used liquids
C01B 3/56 - Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with solidsRegeneration of used solids
F25J 3/06 - Processes or apparatus for separating the constituents of gaseous mixtures involving the use of liquefaction or solidification by partial condensation
A chemical reactor including reformer tubes for reforming a first feed stream including a hydrocarbon gas and steam. The chemical reactor includes one or more reformer tubes arranged to being heated by an electrically driven heat source. The reformer tube includes a first inlet for feeding said first feed stream into a first reforming reaction zone of the reformer tube, and a feed conduit arranged to allow a second feed stream into a second reforming reaction zone of the reformer tube. The second reforming reaction zone is positioned downstream of the first reforming reaction zone. The feed conduit is configured so that the second feed stream is only in contact with catalyst material in the second reforming reaction zone. A process of producing CO rich synthesis gas at low S/C conditions.
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
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 19/12 - Processes employing the direct application of electric or wave energy, or particle radiationApparatus therefor employing electromagnetic waves
B01J 19/24 - Stationary reactors without moving elements inside
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 plant and process for producing a hydrogen rich gas are provided, said process comprising the steps of: reforming a hydrocarbon feed in a reforming step using an autothermal reformer (ATR) thereby obtaining a synthesis gas comprising CH4, CO, CO2, H2 and H2O; shifting said synthesis gas in a shift configuration including a high temperature shift step; passing the shifted syngas to a first hydrogen purification unit, e.g. a PSA unit; passing a portion of the off-gas from the first hydrogen purification unit to a second hydrogen purification unit, and using off-gas from the first and second hydrogen purification unit as e.g. fuel for a preheater unit before the ATR.
C01B 3/48 - 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 followed by reaction of water vapour with carbon monoxide
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 plant, such as a hydrocarbon plant, is provided, which has a syngas stage (A) for syngas generation and a synthesis stage (B) where said syngas is synthesized to produce syngas derived product, such as hydrocarbon product. The syngas stage (A) primarily includes electrically heated reverse water gas shift (e-RWGS) section. Additionally, an electrically-heated steam methane reforming (e-SMR) section (II) can be arranged in parallel to the e-RWGS section (I). The plant makes effective use of various streams; in particular CO2 and H2. A method for producing a product stream, such as a hydrocarbon product stream is also provided.
B01J 19/24 - Stationary reactors without moving elements inside
B01J 19/00 - Chemical, physical or physico-chemical processes in generalTheir relevant apparatus
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 3/34 - 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
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
C10L 1/04 - Liquid carbonaceous fuels essentially based on blends of hydrocarbons
C25B 1/042 - Hydrogen or oxygen by electrolysis of water by electrolysis of steam
2/g, a total pore volume of 0.50-0.80 ml/g, as measured by mercury intrusion porosimetry, and a pore size distribution (PSD) with at least 30 vol % of the total pore volume being in pores with a radius ≥400 Å, suitably pores with a radius ≥500 Å. A process for removing impurities such as phosphorous (P) from a feedstock, by contacting the feedstock with a guard bed including the above porous material. A guard bed for a hydrotreatment system including the porous material, a hydrotreatment system including a guard bed which includes the porous material and a downstream hydrotreatment section including at least one hydrotreatment catalyst.
C10G 67/06 - Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only including a sorption process as the refining step in the absence of hydrogen
B01J 20/08 - Solid sorbent compositions or filter aid compositionsSorbents for chromatographyProcesses for preparing, regenerating or reactivating thereof comprising inorganic material comprising oxides or hydroxides of metals not provided for in group comprising aluminium oxide or hydroxideSolid sorbent compositions or filter aid compositionsSorbents for chromatographyProcesses for preparing, regenerating or reactivating thereof comprising inorganic material comprising oxides or hydroxides of metals not provided for in group comprising bauxite
B01J 20/28 - Solid sorbent compositions or filter aid compositionsSorbents for chromatographyProcesses for preparing, regenerating or reactivating thereof characterised by their form or physical properties
Array including a first and a second monolith of a structured catalyst for carrying out an endothermic reaction of a feed gas, wherein: a) the first and second monolith include a macroscopic structure of a first and second electrically conductive material; b) each of said first and second monoliths has a number of flow channels formed therein for conveying feed gas through the monoliths; c) the array includes at least a first and a second conductor electrically connected to said first and second monoliths, respectively, and to an electrical power supply, d) the first and second monolith are electrically connected by a monolith bridge; e) the array is configured to direct an electrical current to run from the first conductor through the first monolith to a second end, then through the bridge, and then through the second monolith to the second conductor.
B01J 35/00 - Catalysts, in general, characterised by their form or physical properties
C01B 3/40 - 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 characterised by the catalyst
9.
ENDOTHERMIC REACTION OF A FEED GAS HEATED BY RESISTANCE HEATING
Structured catalyst arranged for catalyzing an endothermic reaction of a feed gas, said structured catalyst comprising a macroscopic structure of electrically conductive material, said macroscopic structure supporting a ceramic coating, wherein said ceramic coating supports a catalytically active material, wherein the electrically conductive material at least partly is a composite in the form of a homogenous mixture of an electrically conductive metallic material and a ceramic material, wherein the macroscopic structure at least partly is composed of two or more materials with different resistivities.
B01J 15/00 - Chemical processes in general for reacting gaseous media with non-particulate solids, e.g. sheet materialApparatus specially adapted therefor
B01J 19/24 - Stationary reactors without moving elements inside
B01J 19/00 - Chemical, physical or physico-chemical processes in generalTheir relevant apparatus
C01B 3/40 - 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 characterised by the catalyst
A heating system and a process for heating a pressurized feed gas is provided, where the heat for the reaction is provided by resistance heating by means of electrical power.
The present invention relates to a process for thermolytic fragmentation of a sugar into a composition comprising C1-C3 oxygenates. In particular, it relates to the use of heat carrying particles providing improved yields of C1-C3 oxygenates and improved fluidization characteristics making it suitable for industrial scale production of e.g. glycolaldehyde. It also regards a circulating fluidized bed system comprising the heat carrying particles.
C07C 45/51 - Preparation of compounds having C=O groups bound only to carbon or hydrogen atomsPreparation of chelates of such compounds by pyrolysis, rearrangement or decomposition
C07C 45/56 - Preparation of compounds having C=O groups bound only to carbon or hydrogen atomsPreparation of chelates of such compounds from heterocyclic compounds
2 to a first product gas comprising CO are provided, where a methanation reaction take place in parallel to the reverse water gas shift reaction, and where the heat for the endothermic reverse water gas shift reaction is provided by resistance heating.
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
13.
Process for the conversion of light alkanes to aromatic compounds with improved selectivity
In a process for the catalytic conversion of lower hydrocarbons to aromatic compounds comprising benzene, toluene and xylenes, a process stream containing lower hydrocarbons is contacted with a zeolitic catalyst having an MFI framework and containing 0.1 to 10 percent by weight of a zinc compound. The process stream further contains one or more sulfur compounds, especially hydrogen sulfide, for improving the selectivity.
C07C 2/84 - Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by condensation of hydrocarbons with partial elimination of hydrogen oxidative coupling catalytic
C07C 7/148 - Purification, separation or stabilisation of hydrocarbonsUse of additives by treatment giving rise to a chemical modification of at least one compound
C07C 7/20 - Use of additives, e.g. for stabilisation
14.
Production of glycolaldehyde by thermolytic fragmentation
A process for the production of glycolaldehyde by thermolytic fragmentation of a carbohydrate feedstock including mono- and/or di-saccharide(s) and a system suitable for performing the process. The process and the system are suitable for industrial application, and the process may be performed in a continuous process. The salt-depleted carbohydrate feedstock may include one or more impurities selected from the group of arsenic, lead, sulfate, sulfur dioxide, and 5-(hydroxymethyl)furfural.
C07C 45/60 - Preparation of compounds having C=O groups bound only to carbon or hydrogen atomsPreparation of chelates of such compounds from heterocyclic compounds with oxygen as the only hetero atom in six-membered rings
A reactor system and a process for carrying out steam cracking of a feed gas comprising hydrocarbons is provided, i where the heat for the reaction is provided by resistance heating by means of electrical power, so that a product stream comprising at least one olefin compound is obtained.
A reactor system and a process for carrying out the methanol cracking reaction of a feedstock comprising methanol to hydrogen are provided, where the heat for the endothermic methanol cracking reaction is provided by resistance heating.
An offshore installation or offshore vessel is provided which comprises a reactor system for carrying out steam reforming of a feed gas comprising hydrocarbons.
A method is provided for rapidly switching a metal-catalysed steam methane reforming reaction of a feed gas from a first steady-state reaction condition (A) to a second steady-state reaction condition (B) or vice-versa. After applying a given voltage and/or feed gas flow, the system can work towards a thermal equilibration to reach steady state without any additional operator input.
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
B01J 12/00 - Chemical processes in general for reacting gaseous media with gaseous mediaApparatus specially adapted therefor
B01J 19/24 - Stationary reactors without moving elements inside
B01J 19/00 - Chemical, physical or physico-chemical processes in generalTheir relevant apparatus
19.
SOLID OXIDE CELL STACK WITH A PRESSURE DIFFERENCE BETWEEN ANODE AND CATHODE COMPARTMENTS
A SOC stack has interconnects with a maximum distance between the contact points which are designed to compensate for pressure difference between one side of the interconnect to the other side.
C01B 3/56 - Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with solidsRegeneration of used solids
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
B01D 53/04 - 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 adsorption, e.g. preparative gas chromatography with stationary adsorbents
21.
PROCESS FOR TREATING A FEEDSTOCK COMPRISING HALIDES
A process for conversion of a hydro-carbonaceous feed including ionic halides to a hydrocarbon product stream by hydrotreatment, wherein the stream is combined with wash water, the weight ratio between wash water and hydrocarbon product stream water is between 1:10 and 10:1, wherein the combined hydrocarbon product stream and wash water are separated in a non-polar stream of hydrocarbon product and a polar stream of wash water including ionic halides, such that from 50% of the ionic halides are transferred from the hydrocarbon product stream to the polar stream of wash water including ionic halides, wherein the polar stream of wash water is directed to a means of concentrating, to provide a stream of purified water and a stream of brine having a concentration of ionic halides being more than 2 times and less than 100 times above that of the polar stream of waste water including ionic halides.
C10G 67/02 - Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
C10G 69/06 - Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only including at least one step of thermal cracking in the absence of hydrogen
A method for upgrading biogas to methanol, including the steps of: providing a reformer feed stream comprising biogas; optionally, purifying the reformer feed stream in a gas purification unit; optionally, prereforming the reformer feed stream together with a steam feedstock in a prereforming unit; carrying out steam methane reforming in a reforming reactor heated by means of an electrical power source; providing the synthesis gas to a methanol synthesis unit to provide a product including methanol and an off-gas. Also, a system for upgrading biogas to methanol.
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 12/00 - Chemical processes in general for reacting gaseous media with gaseous mediaApparatus specially adapted therefor
B01J 19/24 - Stationary reactors without moving elements inside
B01J 19/00 - Chemical, physical or physico-chemical processes in generalTheir relevant apparatus
C01B 3/40 - 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 characterised by the catalyst
C01B 3/50 - Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
C01B 3/56 - Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with solidsRegeneration of used solids
C25B 1/04 - Hydrogen or oxygen by electrolysis of water
C25B 15/08 - Supplying or removing reactants or electrolytesRegeneration of electrolytes
A method for upgrading a hydrocarbon feed gas to methanol, including the steps of: providing a hydrocarbon feed gas; optionally, purifying the hydrocarbon feed gas in a gas purification unit; optionally, prereforming the hydrocarbon feed gas together with a steam feedstock in a prereforming unit; carrying out steam methane reforming in a reforming reactor heated by means of an electrical power source; providing the synthesis gas to a methanol synthesis unit to provide a product including methanol and an off-gas. Also, a system for upgrading a hydrocarbon feed gas to methanol.
C01B 3/40 - 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 characterised by the catalyst
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
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 29/152 - 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
C25B 1/042 - Hydrogen or oxygen by electrolysis of water by electrolysis of steam
C25B 15/08 - Supplying or removing reactants or electrolytesRegeneration of electrolytes
24.
A METHOD FOR CHROMIUM UPGRADING OF FERRITIC STEEL INTERCONNECTS FOR SOLID OXIDE CELL STACK APPLICATIONS
In a method for chromium upgrading of interconnects made of ferritic steel to be used in solid oxide cell stacks, comprising the steps of shaping the interconnect, depositing a coating comprising Cr on at least one surface of the shaped interconnect and performing one or more thermal treatments at a temperature below 1000° C., the resulting Cr concentration near the surface of the interconnect is higher than the Cr concentration in the ferritic steel before shaping. Specifically, the average Cr concentration of the shaped interconnect is increased to 26 wt % Cr or higher.
A reactor system and a process for carrying out the methanol cracking and reverse water gas shift reaction of a feedstock comprising methanol to synthesis gas are provided, where the heat for the endothermic methanol cracking and reverse water gas shift reaction is provided by resistance heating.
C01B 3/26 - Production of hydrogen or of gaseous mixtures containing hydrogen by decomposition of gaseous or liquid organic compounds of hydrocarbons using catalysts
B01J 19/00 - Chemical, physical or physico-chemical processes in generalTheir relevant apparatus
B01J 19/08 - Processes employing the direct application of electric or wave energy, or particle radiationApparatus therefor
26.
HALIDES REMOVAL WASHING SYSTEM FOR A HYDROCARBON STREAM
A halides removal washing system for absorbing halides from a process gas within a process gas duct comprising a wash water injection nozzle and anti-precipitation means arranged around the nozzle, injection pipe and within the process gas duct.
C10G 31/08 - Refining of hydrocarbon oils, in the absence of hydrogen, by methods not otherwise provided for by treating with water
C10K 1/10 - Purifying combustible gases containing carbon monoxide by washing with liquidsReviving the used wash liquors with aqueous liquids
C10G 70/06 - Working-up undefined normally gaseous mixtures obtained by processes covered by groups , , , , by physical processes by gas-liquid contact
A reactor system and a process for carrying out the reaction of a feed gas comprising an alkane such as methane, and ammonia to hydrogen cyanide and/or a nitrile are provided, where the heat for the endothermic reaction is provided by resistance heating. In particular, the reaction is the BMA (Blausäure aus Methan und Ammoniak) reaction.
In a process for monitoring the operation of hydrodeoxygenation of a feedstock, comprising the steps of directing the feedstock to contact a material catalytically active in hydrotreatment, monitoring the temperature in multiple locations of said catalytically active material, and providing an indication in a means for process monitoring when the difference between the temperature in a first location of said catalytically active material and the temperature in a second location of said catalytically active material is above a specified threshold value, the difference between the temperature in said first location of the catalytically active material and the temperature in said second location of the catalytically active material is below the specified threshold value during an initial operation time.
A reactor system and a process for carrying out the ammonia cracking reaction of a feed gas comprising ammonia to hydrogen are provided, where the heat for the endothermic ammonia cracking reaction is provided by resistance heating.
B01J 19/00 - Chemical, physical or physico-chemical processes in generalTheir relevant apparatus
B01J 19/24 - Stationary reactors without moving elements inside
B01J 35/56 - Foraminous structures having flow-through passages or channels, e.g. grids or three-dimensional monoliths
C01B 3/56 - Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with solidsRegeneration of used solids
30.
METHOD FOR PRODUCTION OF ELEMENTAL SULFUR AND SULFURIC ACID
A process for production of elemental sulfur from a feedstock gas including from 15% to 100 vol % H2S and a stream of sulfuric acid, the process including: a) providing a Claus reaction furnace feed stream substoichiometric oxygen with respect to the Claus reaction, b) directing to a reaction furnace zone operating at elevated temperature such as above 900° C., c) directing to a sulfuric acid evaporation zone downstream said reaction furnace zone, d) cooling to provide a cooled Claus converter feed gas, e) directing to contact a material catalytically active in the Claus reaction, f) withdrawing a Claus tail gas and elemental sulfur, g) directing to a Claus tail gas treatment plant, with the associated benefit of a process involving injection of sulfuric acid in a sulfuric acid evaporation zone allowing high temperature combustion of said feedstock gas, including impurities, without cooling from evaporation and decomposition of sulfuric acid.
A sulfuric acid recirculation loop and a standalone sulfuric acid concentrator including: a concentrator column, an air lift pump having a liquid inlet fed with concentrated sulfuric acid from the outlet of a sulfuric acid reservoir downstream the concentrator column, a gas inlet fed with a carrier fluid having a lower density than the concentrated sulfuric acid, and an outlet, wherein the sulfuric acid reservoir is located below the concentrator column and above the carrier fluid inlet of the air lift pump, a downcomer pipe leading down from the sulfuric acid reservoir to the liquid inlet of the air lift pump, and a riser pipe leading up from the carrier fluid inlet on the air lift pump to an inlet pipe for the concentrator column, the inlet pipe being configured for allowing a liquid flow from the inlet to the outlet.
A steam reformer is provided which comprises at least one externally-heated tube. Each tube comprises a first catalyst bed comprising a first catalyst in particulate form and a second catalyst supported on a structure, wherein said first catalyst bed is located between the inlet of the tube and the second catalyst supported on said structure. A process for steam reforming of a feed gas mixture using said steam reformer is also provided.
C01B 3/40 - 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 characterised by the catalyst
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
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 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 37/02 - Impregnation, coating or precipitation
A hydrotreatment unit for an oxygenate feedstock is provided, the unit including: a hydrotreatment reactor; a first cooling unit; a high-pressure separator and a low pressure flash unit. The hydrotreatment unit is arranged to feed at least a part of the hydrogen-rich stream from the high-pressure separator to the hydrotreatment reactor; and the hydrotreatment unit is arranged to feed a part of the degassed hydrocarbon-rich stream from said low pressure flash unit as a hydrocarbon recycle stream to the hydrotreatment reactor. Also, a method for hydrotreating an oxygenate feedstock using the hydrotreatment unit.
A process plant and process for conversion of a hydrocarbonaceous feed, having a feed temperature, to a hydrocarbonaceous effluent, having an effluent temperature, by hydrotreatment, in the presence of a material catalytically active in hydrotreatment and an amount of hydrogen, wherein the conversion is exothermal and wherein an amount of the effluent will solidify at a solidification temperature above the feed temperature and below the effluent temperature, and wherein the feed is preheated by heat exchange, utilizing thermal energy from said effluent, wherein the heat exchange is mediated by a fluid heat exchange medium being physically separated from the feed and the effluent and having a temperature above the solidification temperature, with the associated benefit of such a process being highly energy effective, while avoiding solidification in the process lines, especially when hydrotreating feedstocks including halides.
C10G 45/04 - 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 characterised by the catalyst used
C10G 69/06 - Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only including at least one step of thermal cracking in the absence of hydrogen
C10G 31/08 - Refining of hydrocarbon oils, in the absence of hydrogen, by methods not otherwise provided for by treating with water
A reactor vessel for high temperature catalytic reactions is provided, in which the inlet portion has a particular design. A plant comprising this reactor vessel is also provided.
C01B 3/40 - 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 characterised by the catalyst
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
36.
Chemical plant with a reforming section and a process for producing a chemical product
The invention relates to a chemical plant comprising a reforming section arranged to receive a feed gas comprising hydrocarbons and provide a synthesis gas, wherein the reforming section comprises: an electrically heated reforming reactor housing a first catalyst, said electrically heated reforming reactor being arranged for receiving said feed gas and generating a first synthesis gas; and an autothermal reforming reactor downstream said electrically heated reforming reactor, said autothermal reforming reactor housing a second catalyst, said autothermal reforming reactor being arranged for receiving said first synthesis gas and outputting a second synthesis gas, wherein said reforming section is arranged to output said output synthesis gas comprising said second synthesis gas. The invention also relates to a process for producing a chemical product from a feed gas comprising hydrocarbons, in a chemical plant according to the invention.
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
C01B 3/48 - 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 followed by reaction of water vapour with carbon monoxide
B01J 19/24 - Stationary reactors without moving elements inside
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 1/04 - Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon from oxides of carbon from carbon monoxide with hydrogen
The present invention refers to a method for cracking ammonia, producing hydrogen and generating electrical power comprising electrolysis (2) of water in feed ammonia, evaporation (3), pre-heating (5) and cracking (6) of ammonia, using ammonia synthesis catalysts at low temperatures.
222. The plant may comprise an external feed of hydrocarbons. A method for producing a product stream, such as a hydrocarbon product stream, is also provided.
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
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
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 29/151 - 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
C10G 2/00 - Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
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
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
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 29/151 - 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
C25B 1/04 - Hydrogen or oxygen by electrolysis of water
A synthesis gas plant for producing a synthesis gas, where the synthesis gas plant includes a reforming section arranged to receive said feed gas and provide a combined synthesis gas, wherein said reforming section includes an electrically heated reforming reactor, a fired reforming reactor and an optional third reforming reactor. The reforming section is arranged to output a combined synthesis gas. An optional post processing unit downstream the reforming section is arranged to receive said combined synthesis gas stream and provide a post processed synthesis gas stream. A gas separation unit arranged to separate the combined synthesis gas stream or the post processed synthesis gas stream into a condensate, a product synthesis gas and an off-gas. At least a part of the off-gas is recycled from said gas separation unit to said one or more burners. Also, a process for producing synthesis gas from a feed gas comprising hydrocarbons.
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
C01B 3/48 - 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 followed by reaction of water vapour with carbon monoxide
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 3/16 - 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
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 3/38 - 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
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
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
A process for producing an olefin stream, said process comprising passing a feedstock stream comprising oxygenates over catalyst comprises a zeolite with a framework having a 10-ring pore structure, in which said 10-ring pore structure comprises a unidimensional (1-D) pore structure, such as *MRE, at a pressure of 1-25 bar and a temperature of 240-360°C. The olefin stream may be converted to jet fuel, particularly sustainable aviation fuel (SAF) by further oligomerization and hydrogenation.
C10G 3/00 - Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
C10G 69/12 - Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only including at least one polymerisation or alkylation step
C10G 50/00 - Production of liquid hydrocarbon mixtures from lower carbon number hydrocarbons, e.g. by oligomerisation
C07C 1/20 - 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
C07C 2/12 - Catalytic processes with crystalline alumino-silicates, e.g. molecular sieves
A process and plant for producing hydrocarbons boiling in the jet fuel range, comprising the steps: optionally passing a feedstock stream comprising oxygenates over a catalyst thereby forming an olefin stream; passing the olefin stream trough a combined oli-gomerization and hydrogenation step thereby producing a hydrocarbon stream comprising said hydrocarbons boiling in the jet fuel range.
C10G 50/00 - Production of liquid hydrocarbon mixtures from lower carbon number hydrocarbons, e.g. by oligomerisation
C10G 69/12 - Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only including at least one polymerisation or alkylation step
C07C 2/12 - Catalytic processes with crystalline alumino-silicates, e.g. molecular sieves
C10G 3/00 - Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
C07C 1/20 - 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
A process and plant for producing an olefin stream, comprising passing a feedstock stream comprising oxygenates over a catalyst thereby forming an olefin stream; using a first reactor set including a single reactor or several reactors for the partial or full conversion of the oxygenates; and in series arrangement with the first reactor set, using a second reactor set including a single reactor or several reactors, for the further conversion of the oxygenates, and a phase separation stage in between the first reactor set and the second reactor set, for thereby forming the olefin stream.
C10G 3/00 - Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
C10G 69/12 - Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only including at least one polymerisation or alkylation step
C10G 50/00 - Production of liquid hydrocarbon mixtures from lower carbon number hydrocarbons, e.g. by oligomerisation
C07C 1/20 - 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
C07C 2/12 - Catalytic processes with crystalline alumino-silicates, e.g. molecular sieves
A process for producing an olefin stream, said process comprising passing a feedstock stream comprising oxygenates over catalyst comprises a zeolite with a framework having a 10-ring pore structure, in which said 10-ring pore structure comprises a three- dimensional (3-D) pore structure, such as MFI, wherein the pressure is 2-20 bar and the temperature is 150-350°C; or the pressure is 2-30 bar and the temperature is 340- 400°C, and wherein an olefin stream comprising C2-C3 olefins is withdrawn from said olefin stream and used as additional feed stream. The olefin stream may be converted to jet fuel, particularly sustainable aviation fuel (SAF) by further oligomerization and hydrogenation.
C10G 3/00 - Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
C07C 1/20 - 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
C10G 50/00 - Production of liquid hydrocarbon mixtures from lower carbon number hydrocarbons, e.g. by oligomerisation
C10G 69/12 - Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only including at least one polymerisation or alkylation step
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
A plant, such as a hydrocarbon plant, is provided, which consists of a syngas stage for syngas generation and a synthesis stage where said syngas is synthesized to produce syngas derived product, such as hydrocarbon product. The plant makes effective use of various streams; in particular CO2 and H2. A method for producing a product stream, such as a hydrocarbon product stream is also provided.
C01B 3/48 - 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 followed by reaction of water vapour with carbon monoxide
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 chemical plant including: a reforming section arranged to receive a feed gas comprising hydrocarbons and provide a combined synthesis gas stream, wherein the reforming section includes: an electrically heated reforming reactor housing a first catalyst, an autothermal reforming reactor in parallel with the electrically heated reforming reactor, wherein the reforming section is arranged to output a combined synthesis gas stream including at least part of the first and/or second synthesis gas streams, an optional post processing unit downstream the reforming section, a gas separation unit arranged to separate a synthesis gas stream into a water condensate and an intermediate synthesis gas, and a downstream section arranged to receive the intermediate synthesis gas and to process the intermediate synthesis gas to a chemical product and an off-gas. Also, a process for producing a chemical product from a feed gas comprising hydrocarbons.
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
C01B 3/48 - 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 followed by reaction of water vapour with carbon monoxide
C01B 3/50 - Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
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
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
49.
AMBIENT AIR SEPARATION AND SOEC FRONT-END FOR AMMONIA SYNTHESIS GAS PRODUCTION
In a method for generating ammonia synthesis gas by electrolysis, comprising the steps of compressing air and feeding it to an air separation process, in which the content of nitrogen is concentrated while the content of oxygen and CO2 is diluted, feeding a mixture of steam and the compressed and refined air into the electrolysis unit or into the first of a series of electrolysis units and passing the outlet from one electrolysis unit to the inlet of the next electrolysis unit, either together with air added after each electrolysis unit or only adding air after the last electrolysis unit, the electrolysis units are run in thermoneutral or endothermal mode and the nitrogen part of the synthesis gas is provided by burning the hydrogen produced by steam electrolysis by the refined air in or between the electrolysis units.
2222O; withdrawing from said first separation step an overhead stream and separating an overhead hydrocarbon liquid stream thereof which is passed as a reflux stream to said first separation unit; withdrawing from said first separation step a bottom stream and passing at least a portion of said bottom stream to a dewaxing step comprising the use of one or more catalytic hydrotreating units under the addition of hydrogen for producing said main hydrotreated stream; and ii) passing the main hydrotreated stream to a second separation step for producing said hydrocarbon product.
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
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
C10G 3/00 - Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
C10G 65/12 - Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including cracking steps and other hydrotreatment steps
C10G 47/00 - Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, to obtain lower boiling fractions
51.
PRODUCTION OF SYNTHESIS GAS IN A PLANT COMPRISING AN ELECTRIC STEAM REFORMER DOWNSTREAM OF A HEAT EXCHANGE REFORMER
A plant is provided which comprises a reforming section (A), a gas separation section (B) and a hydrocarbon-containing feed. The reforming section (A) comprises a heat exchange reformer and an electrical steam methane reformer (e-SMR) arranged downstream of said heat exchange reformer. The gas separation section (B) is arranged to receive a synthesis gas stream from the reforming section (A) and separate it into at least a condensate and a product gas. The plant is controlled by feedback control on the e-SMR.
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
C01B 3/50 - Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
C01B 3/56 - Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with solidsRegeneration of used solids
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
C10G 2/00 - Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
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
52.
PRODUCTION OF SYNTEHSIS GAS IN A PLANT COMPRISING AN ELECTRIC STEAM REFORMER DOWNSTREAM OF FIRED REFORMER
A plant is provided which comprises a reforming section (A), a gas separation section (B) and a hydrocarbon-containing feed. The reforming section (A) comprises a fired reformer and an electrical steam methane reformer (e-SMR) arranged downstream of said fired reformer. The gas separation section (B) is arranged to receive a synthesis gas stream from the reforming section (A) and separate it into at least a condensate, a product gas and an off-gas. The plant is controlled by feedback control on the e-SMR. In one particular aspect, at least part of the off-gas from the gas separation section (B) is arranged to be provided as fuel for the burners of the fired reformer.
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
C01B 3/50 - Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
C01B 3/56 - Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with solidsRegeneration of used solids
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
C10G 2/00 - Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
22 upstream hydrogen purification unit, thereby producing a hydrogen rich stream and an off-gas stream, and where at least part of the off-gas stream is recycled to the process, thus to the ATR and optional prereforming, and/or to the shift section.
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
C01B 3/48 - 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 followed by reaction of water vapour with carbon monoxide
2222-rich gas and a high-pressure flash gas stream. The high-pressure flash gas stream is advantageously integrated into the plant and process for further improving carbon capture.
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
C01B 3/48 - 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 followed by reaction of water vapour with carbon monoxide
C01B 3/52 - Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with liquidsRegeneration of used liquids
55.
OFF-GAS UTILIZATION IN ELECTRICALLY HEATED REFORMING PLANT
A plant and a method are provided in which a first feed comprising hydrocarbons is subjected to electrical steam methane reforming (e-SMR) to generate a first syngas stream. An upgrading section receives the syngas stream and generates a first product stream and an off-gas stream from the syngas stream. A power generator receives at least a portion of the off-gas stream and/or a portion of said first product stream from the upgrading section and/or a portion of said first feed and generates a second electricity flow. At least a portion of the second electricity flow is arranged to provide at least a part of the first electricity flow to the e-SMR reactor.
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
C01B 3/48 - 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 followed by reaction of water vapour with carbon monoxide
56.
CONVERSION OF A HYDROCARBON FEED GAS TO SYNTHESIS GAS FOR PRODUCING HYDROCARBONS
Method and plant for producing a synthesis gas for use in the production of a hydrocarbon product, particularly a synthetic fuel, comprising: providing a hydrocarbon feed gas, providing a first oxygen rich stream by passing air through an air separation unit (ASU), carrying out autothermal reforming of said hydrocarbon feed gas in an autothermal reforming (ATR) unit, said autothermal reforming including using at least a portion of said first oxygen containing stream, providing at least part of said synthesis gas to a synthetic fuel synthesis unit for converting said synthesis gas into said hydrocarbon product and producing a tail gas, recycling part or the entirety of said tail gas to upstream said ATR, providing a first hydrogen rich stream and a second oxygen rich stream, and adding at least a portion of said first hydrogen rich stream to said synthesis gas prior to entering said synthetic fuel synthesis unit.
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
C10G 2/00 - Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
C25B 1/04 - Hydrogen or oxygen by electrolysis of water
57.
PROCESS AND PLANT FOR PRODUCING GASOLINE FROM A TAR-CONTAINING FEED
The present invention relates to a process and plant for producing hydrocarbon product boiling in the gasoline boiling range from a tar-containing feedstock, the process and 5plant comprising a hydroprocessing stage which includes hydrotreating and hydrocracking for producing diesel and naphtha, and subsequent aromatization of the naphtha thereby also producing a light hydrocarbon gas as liquid petroleum gas (LPG),from which a hydrogen stream is produced.
C10G 63/04 - Treatment of naphtha by at least one reforming process and at least one other conversion process plural serial stages only including at least one cracking step
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
C10G 65/04 - Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including only refining steps
C10G 69/10 - Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only including at least one step of reforming naphtha hydrocracking of higher boiling fractions into naphtha and reforming the naphtha obtained
58.
PROCESS FOR THE PRODUCTION OF UREA FORMALDEHYDE CONCENTRATE
Parallel co-production process for the production of methanol and urea product from a hydrocarbon containing feed-stock by means of autothermal reforming, intermediary methanol and ammonia formation and conversion of the ammonia to urea product and catalytic oxidation of the methanol to formaldehyde.
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
C01B 3/02 - Production of hydrogen or of gaseous mixtures containing hydrogen
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
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
59.
PROCESS AND PLANT FOR PRODUCING GASOLINE FROM A RENEWABLE FEED
The present invention relates to a process and plant for producing hydrocarbon product boiling in the gasoline boiling range from a feedstock originating from a renewable source, the process and plant comprising a hydroprocessing stage which includeshydrodoxygenation for producing renewable diesel and renewable naphtha, and subsequent aromatization of the renewable naphtha thereby also producing a lighthydrocarbon gas stream, such as liquid petroleum gas (LPG), from which a hydrogen stream is produced.
C10G 3/00 - Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
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
C10G 63/04 - Treatment of naphtha by at least one reforming process and at least one other conversion process plural serial stages only including at least one cracking step
C10G 65/04 - Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including only refining steps
C10G 69/10 - Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only including at least one step of reforming naphtha hydrocracking of higher boiling fractions into naphtha and reforming the naphtha obtained
A reactor for catalytic reforming of a hydrocarbon gas comprises an expandable structured packing arranged within an outer casing of the reactor; despite being rigid, the expandable structured packing is able to adjust to the dimensions of the outer casing, even when these are changing due to temperature and pressure changes, keeping the gas flow and pressure constant.
The invention relates to a porous material comprising alumina, said alumina comprising alpha-alumina, said porous material comprising one or more metals selected from Co, Mo, Ni, W and combinations thereof, and said porous material having a BET-surface area of 1-110 m2/g, a total pore volume of 0.50-0.80 ml/g, as measured by mercury intrusion porosimetry, and a pore size distribution (PSD) with at least 30 vol% of the total pore volume being in pores with a radius ≥ 400 Å, suitably pores with a radius ≥ 500 Å, such as pores with a radius up to 5000 Å. The invention relates also to a process for removing impurities such as phosphorous (P) from a feedstock such as a renewable feed, by contacting said feedstock with a guard bed comprising the above porous material. The invention further relates to a guard bed for a hydrotreatment system comprising the porous material, a hydrotreatment system comprising a guard bed which comprises the porous material and a downstream hydrotreatment section comprising at least one hydrotreatment catalyst, as well as to the use of the porous material as a phosphorus guard in a hydrotreatment process.
C10G 25/00 - Refining of hydrocarbon oils, in the absence of hydrogen, with solid sorbents
B01J 20/02 - Solid sorbent compositions or filter aid compositionsSorbents for chromatographyProcesses for preparing, regenerating or reactivating thereof comprising inorganic material
B01J 20/08 - Solid sorbent compositions or filter aid compositionsSorbents for chromatographyProcesses for preparing, regenerating or reactivating thereof comprising inorganic material comprising oxides or hydroxides of metals not provided for in group comprising aluminium oxide or hydroxideSolid sorbent compositions or filter aid compositionsSorbents for chromatographyProcesses for preparing, regenerating or reactivating thereof comprising inorganic material comprising oxides or hydroxides of metals not provided for in group comprising bauxite
B01J 20/28 - Solid sorbent compositions or filter aid compositionsSorbents for chromatographyProcesses for preparing, regenerating or reactivating thereof characterised by their form or physical properties
The invention relates to a method of regenerating the catalytic activity of a spent catalyst comprising nickel on a refractory oxide support, said method comprising the steps of contacting the spent catalyst with a nitric acid solution, heat-treating the spent catalyst, calcining and reducing the catalyst.
The present invention refers to an apparatus and process for distillation of methanol (Fig. 1), however may also be used in distillation of other products such as ethanol. The present invention has the purpose of reducing the consumption of energy and of cooling water and/or electricity in a distillation process of crude intermediate products, comprising a pretreatment stage, known as stabilizing stage, for the removal of the volatile components, and a concentration stage, comprising one or more columns for distillation.
The present invention refers to an apparatus and process for distillation of methanol (Fig. 1), however may also be used in distillation of other products such as ethanol. The present invention has the purpose of reducing the consumption of energy and of cooling water and/or electricity in a distillation process of crude intermediate products, comprising a pre-treatment stage, known as stabilizing stage, for the removal of the volatile components, and a concentration stage, comprising one or more columns for distillation.
A broad aspect of the present disclosure relates to a process plant and a method for producing a hydrocarbon mixture suitable for use as an aviation fuel having an end-boiling point according to ASTM D86 below 300°C from a decarboxylation feedstock being a feedstock comprising fatty acid esters and/or triglycerides and comprising C18 side-chains, to a deoxygenated hydrocarbon mixture by directing said decarboxylation feedstock to contact a material catalytically active in decarboxylation under decarboxylation conditions where the ratio between deoxygenation by formation of carbon oxides and deoxygenation by formation of water is at least 1.5:1, 2:1 or 3:1, as measured by the ratio of C17 paraffins to C18 paraffins in the deoxygenated hydrocarbon mixture, with the associated benefit of such a decarboxylation based method selectively reducing the product carbon length by a single carbon atom, compared to a hydrodeoxygenation based method, which is beneficial for processes requiring a moderate reduction of end boiling point.
C10G 3/00 - Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
C10G 45/38 - Selective hydrogenation of the diolefin or acetylene compounds characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof in combination with chromium, molybdenum or tungsten metals, or compounds thereof
C10G 47/14 - Inorganic carriers the catalyst containing platinum group metals or compounds thereof
C10G 47/18 - Crystalline alumino-silicate carriers the catalyst containing platinum group metals or compounds thereof
C10G 45/64 - 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 characterised by the catalyst used containing crystalline alumino-silicates, e.g. molecular sieves
C10G 65/04 - Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including only refining steps
C10G 65/06 - Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including only refining steps at least one step being a selective hydrogenation of the diolefins
C10G 65/12 - Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including cracking steps and other hydrotreatment steps
A process plant and a process for production of a hydrocarbon suitable for use as jet fuel from a feedstock being a renewable feedstock or an oxygenate feedstock, including combining the renewable feedstock with an amount of a hydrocracked intermediate product, directing it to contact a material catalytically active in hydrodeoxygenation under hydrodeoxygenation conditions to provide a hydrodeoxygenated intermediate product, fractionating the hydrodeoxygenated intermediate product in at least two fractions including a first fraction of which at least 90% boils below a defined boiling point and a second fraction of which at least 90% boils above the defined boiling point, directing at least an amount of the second fraction to contact a material catalytically active in hydrocracking under hydrocracking conditions to provide the hydrocracked intermediate product, the process being suited for efficiently converting the upper-boiling point of an oxygenate feedstock such as a renewable feedstocks to a lower boiling product.
C10G 65/12 - Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including cracking steps and other hydrotreatment steps
C10G 3/00 - Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
C10G 47/18 - Crystalline alumino-silicate carriers the catalyst containing platinum group metals or compounds thereof
C10G 47/20 - Crystalline alumino-silicate carriers the catalyst containing other metals or compounds thereof
C10G 45/62 - 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 characterised by the catalyst used containing platinum group metals or compounds thereof
Method for treating a carbon black tail gas wherein the carbon black tail gas is catalytically oxidized to produce an oxidized tail gas. The oxidized tail gas is then treated to remove particulate matter and sulfur oxides. If present, nitrogen oxides can be also removed.
A tubular reactor comprises a multiple burner furnace where the multiple burners are controlled by a multiple burner management system which ensures autoignition of the fuel fluid, thereby simplifying control of the burners and 5increasing safety.
F23C 7/06 - Disposition of air supply not passing through burner for heating the incoming air
F23C 13/02 - Apparatus in which combustion takes place in the presence of catalytic material characterised by arrangements for starting the operation, e.g. for heating the catalytic material to operating temperature
F23L 15/00 - Heating of air supplied for combustion
F23N 5/02 - Systems for controlling combustion using devices responsive to thermal changes or to thermal expansion of a medium
71.
METHOD FOR THE CONTROL OF PRESSURE IN A LOOP FOR THE PREPARATION OF AMMONIA OR METHANOL
Method for the control of pressure in a loop for the preparation of ammonia or methanol by means of an anti-surge control valve of a compressor and/or a compressor flow regulation valve for the recirculation of loop recirculation gas at variating flow supply of fresh synthesis gas.
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
B01J 8/00 - Chemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes
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
A process for separation of a liquid phase from a gas phase and a process for production of a hydrocarbon product employing such a separation as well as a fractionation section and a hydrocracker section for carrying out such processes. The separation process includes: directing a feed for separation to a feed inlet of a means of separation; directing a stripping medium to a stripping medium inlet of the means of separation; withdrawing a liquid product stream from a means of separation; withdrawing a gaseous fraction comprising the stripping medium from the means of separation; directing the stripping medium fraction or the gaseous fraction as a recycled stripping medium; pressurizing at least an amount of the recycled stripping medium and directing it as the stripping medium, wherein the stripping medium comprises at least 80% vol/vol % of gases from the group comprising N2, H2, He, Ar, Ne and CO2.
In a process for the start-up of a hydrodesulfurization section, comprising the steps of providing a natural gas feed, passing the natural gas feed through the waste heat section of a reformer, thereby heating the natural gas feed, and passing the heated natural gas feed through a hydrodesulfurization section, thereby heating the hydrodesulfurization section while producing a desulfurized natural gas stream, a part of the desulfurized natural gas stream is provided as fuel for the reformer, while the remainder of the desulfurized natural gas is recycled to at least one point upstream the waste heat section.
C10L 3/10 - Working-up natural gas or synthetic natural gas
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
The present disclosure relates to a production plant and a method for production of a synthetized gasoline product from a synthetic hydrocarbon mixture produced from a mixture of reactive oxygenates comprising the steps ofa. separating the synthetic hydrocarbon mixture in at least a light hydrocarbon frac-tion, and a higher boiling hydrocarbon fraction, wherein the higher boiling fraction comprises at least 70% of the molecules comprising 10 or more carbon atoms pre-sent in the hydrocarbon mixture and less than 20% of the molecules comprising ex-actly 9 carbon atoms present in the synthetic hydrocarbon mixture,b. directing at least an amount of said higher boiling hydrocarbon fraction as a hy-drocracking feedstock to contact a material catalytically active in hydrocracking un-der effective hydrocracking conditions providing a hydrocracked hydrocarbon stream,wherein at least an amount of said hydrocracked hydrocarbon stream, optionally after further hydroprocessing, is combined with at least an amount of said light hydrocarbon fraction, to provide said synthetized gasoline product having a T90 according to ASTM D86 being below T90 according to ASTM D86 of said synthetic hydrocarbon mixture, such as 10°C or 20°C below, with the associated benefit of such a process reducing the upper boiling point of the synthetized gasoline product, by hydrocracking C10 and C11 hydrocarbons, especially two-ring aromatics, while minimizing the yield loss of gasoline product.
C10G 3/00 - Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
C10G 45/64 - 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 characterised by the catalyst used containing crystalline alumino-silicates, e.g. molecular sieves
C10G 47/02 - Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, to obtain lower boiling fractions characterised by the catalyst used
C10G 65/14 - Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural parallel stages only
76.
A PROCESS FOR THE REMOVAL OF NOx AND DINITROGEN OXIDE IN PROCESS OFF-GAS
:Process for the removal of NOx (NO, NO2) and nitrous oxide (N2O) contained in a process off-gas comprising the steps of (a) adding an amount of a NOx reducing agent into the process off-gas;(b) in a first stage passing the process off-gas admixed with the reducing agent through a catalyst active in selective catalytic reduction of NOx with the reducing agent and providing an effluent gas comprising the nitrous oxide and residual amounts of reducing agent; and(c) in a second stage passing the effluent gas through a catalyst comprising a cobalt compound and being active in decomposition of nitrous oxide and oxidation of the residual amounts of the reducing agent.
B01J 23/78 - 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 alkali- or alkaline earth metals or beryllium
Process and plant for producing a synthesis gas by catalytic steam reforming of a hydrocarbon feedstock in a steam reforming unit, wherein water is removed from the synthesis gas as a process condensate, wherein boiler feed water is introduced in the process, and wherein said process or plant produces at least two separate steam streams: a pure steam which is generated from at least a portion of said boiler feed water by the cooling of synthesis gas, and a process steam which is generated by evaporating at least a portion of the process condensate by using synthesis gas, optionally together with pure steam and/or flue gas from the steam reforming unit.
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
C01B 3/48 - 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 followed by reaction of water vapour with carbon monoxide
C01B 3/50 - Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
C01B 3/56 - Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with solidsRegeneration of used solids
A method for converting a feedstock comprising solid hydrocarbons to a sweet synthesis gas, involving the steps
a. gasifying said feedstock in the presence of steam, an oxygen rich gas and an amount of sour process gas to form a raw synthesis gas optionally comprising tar,
b. optionally conditioning said raw synthesis gas to a sour shift feed gas,
c. contacting said sour shift feed gas with a sulfided material catalytically active in the water gas shift process for providing a sour hydrogen enriched synthesis gas,
d. separating H2S and CO2 from said sour hydrogen enriched synthesis gas, for providing said sour recycle gas and a sweet hydrogen enriched synthesis gas.
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
C10J 3/84 - Gas withdrawal means with means for removing dust or tar from the gas
C10K 1/04 - Purifying combustible gases containing carbon monoxide by cooling to condense non-gaseous materials
C10K 1/08 - Purifying combustible gases containing carbon monoxide by washing with liquidsReviving the used wash liquors
C10K 1/34 - Purifying combustible gases containing carbon monoxide by catalytic conversion of impurities to more readily removable materials
Process and plant for producing hydrocarbon products from a feedstock originating from a renewable source, where a hydrogen-rich stream and on off-gas stream comprising hydrocarbons is formed. A portion of the hydrogen-rich stream is used as a recycle gas stream in a hydroprocessing stage for the production of said hydrocarbon products, and another portion may be used for hydrogen production, while the off-gas stream is treated to remove its H2S content and used as a recycle gas stream in the hydrogen producing unit, from which the hydrogen produced i.e. make-up hydrogen, is used in the hydroprocessing stage. The invention enables minimizing natural gas consumption in the hydrogen producing unit as well as steam reformer size.
C01B 3/50 - Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
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
C10G 3/00 - Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
80.
COST EFFECTIVE DEOXYGENATION PROCESS WITH GAS RECYCLE
The present disclosure relate to a process plant and a method for production of a hydrocarbon mixture from a feedstock stream comprising oxygenates and a make-up hydrogen gas stream, involving directing a feed stream, comprising the feedstock stream comprising oxygenates, the make-up hydrogen gas stream and a hydrogen rich gasstream, to contact a material catalytically active in deoxygenation under active deoxygenation conditions and withdrawing a deoxygenated product stream, characterized in the hydrogen rich gas stream comprising at least 70 vol% hydrogen, at least 0.1 vol% carbon oxides and at least 50 ppmvol H2S, with the associated benefit that such a method, where carbon oxides are allowed to be present may be realized without requiring a step of purifying said recycled hydrogen rich gas stream, e.g. by use of an amine wash.
A process for producing synthesis gas, the process comprising the steps of a) reforming a hydrocarbon feed in a reforming section thereby obtaining a synthesis gas comprising CH4, CO, CO2, H2 and H2O and impurities comprising ammonia; b) shifting the synthesis gas in a shift section comprising one or more shift steps in series to a shifted synthesis gas; c) separating from the shifted synthesis gas a process condensate originating from cooling and optionally washing of the shifted synthesis gas; d) passing a part of the process condensate to a condensate steam stripper, wherein dissolved shift byproducts comprising ammonia, methanol and amines formed during shifting the synthesis gas are stripped out of the process condensate using steam resulting in a stripper steam stream, e) adding the stripper steam stream from the process condensate steam stripper to the hydrocarbon feed and/or to the synthesis gas downstream the reforming section, up-stream the last shift step, wherein the remaining part of the process condensate is purged.
C01B 3/48 - 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 followed by reaction of water vapour with carbon monoxide
B01D 3/00 - Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
A process for producing synthesis gas, the process comprising the steps of a) reforming a hydrocarbon feed in a reforming section thereby obtaining a synthesis gas comprising CH4, CO, CO2, H2 and H2O and impurities comprising ammonia;b) shifting the synthesis gas in a shift section comprising one or more shift steps in series to a shifted synthesis gas; c) separating from the shifted synthesis gas a process condensate originating from cooling and optionally washing of the shifted synthesis gas;d) passing the process condensate to a condensate steam stripper, wherein dissolved shift byproducts comprising ammonia, methanol and amines formed during shifting the synthesis gas are stripped out of the process condensate using steam resulting in a stripper steam stream, e) adding a part of the stripper steam stream from the process condensate steam strip-per to the hydrocarbon feed and/or to the synthesis gas downstream the reforming section, up-stream the last shift step, wherein the remaining part of stripper steam is purged.
C01B 3/48 - 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 followed by reaction of water vapour with carbon monoxide
B01D 3/00 - Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
A method for increasing the carbon utilisation of a synthesis gas plant is provided, as well as a synthesis gas plant arranged to perform said method. Various gas streams can be combined and recycled to allow for efficient use of a natural gas feedstock.
C01B 3/50 - Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
C01B 3/52 - Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with liquidsRegeneration of used liquids
C01B 3/56 - Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with solidsRegeneration of used solids
Sequential and once-through (single pass) process for the co-production of methanol and ammonia and conversion of at least a part of ammonia to urea by reaction of the ammonia with carbon dioxide collected from a primary reformer flue gas together with carbon dioxide separated from reformed gas in a carbon dioxide removal stage.
C01B 3/02 - Production of hydrogen or of gaseous mixtures containing hydrogen
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
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 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
Method for the preparation of synthesis gas combining electrolysis of water, tubular steam reforming and autothermal reforming of a hydrocarbon feed stock in parallel.
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
C25B 1/04 - Hydrogen or oxygen by electrolysis of water
A Solid Oxide Cell stack has an integrated interconnect and spacer, which is formed by bending a surplus part of the plate interconnect 180° to form a spacer part on top of the interconnect and connected to the interconnect at least by the bend.
H01M 8/0202 - CollectorsSeparators, e.g. bipolar separatorsInterconnectors
H01M 8/0247 - CollectorsSeparators, e.g. bipolar separatorsInterconnectors characterised by the form
H01M 8/0271 - Sealing or supporting means around electrodes, matrices or membranes
H01M 8/124 - Fuel cells with solid electrolytes operating at high temperature, e.g. with stabilised ZrO2 electrolyte characterised by the process of manufacturing or by the material of the electrolyte
H01M 8/0258 - CollectorsSeparators, e.g. bipolar separatorsInterconnectors characterised by the configuration of channels, e.g. by the flow field of the reactant or coolant
H01M 8/0273 - Sealing or supporting means around electrodes, matrices or membranes with sealing or supporting means in the form of a frame
H01M 8/0276 - Sealing means characterised by their form
H01M 8/028 - Sealing means characterised by their material
C25B 9/00 - Cells or assemblies of cellsConstructional parts of cellsAssemblies of constructional parts, e.g. electrode-diaphragm assembliesProcess-related cell features
87.
PROCESS FOR THE REMOVAL OF PARTICULATE MATTER FROM AN AQUEOUS STREAM
Process for the removal of particulate matter from an aqueous stream containing a concentrated acid, preferably concentrated sulfuric acid, said process comprising mechanical filtration by passing said aqueous stream through a filter unit, said filter unit comprising a metallic, ceramic or polymeric filter, or a filter comprising a filter aid on a septum. The aqueous stream is the exit stream of a sulfuric acid condenser, optionally the exit stream of a sulfuric acid concentrator arranged downstream the sulfuric acid condenser.
22 to the anode side of a solid oxide electrolysis cell, oxygen is generated on the anode side of the solid oxide electrolysis cell. This way, an an-ode-side product gas is formed, in which the oxygen-enriched gas comprises at least a part. The oxygen-enriched gas has a low nitrogen content, and the temperature of the oxygen-enriched gas exiting the solid oxide electrolysis cell is between 600 and 1000°C. The method has multiple advantages, first of all as regards energy saving.
Process and reaction system for the preparation of methanol. The process comprises the steps of (a) providing a fresh methanol synthesis gas containing hydrogen, carbon monoxide and carbon dioxide;(b)) introducing and reacting the fresh methanol synthesis gas stream in a first methanol reaction unit in presence of a methanol catalyst and obtaining a first effluent stream containing methanol and unconverted synthesis gas; (c) providing a recycle gas stream containing the unconverted methanol synthesis gas contained in the first effluent stream and unconverted methanol synthesis gas from a second methanol reaction unit;(d) introducing and reacting the recycle gas stream in the second methanol reaction unit in presence of a methanol catalyst; (e) withdrawing a second effluent stream containing methanol and the unconverted methanol synthesis gas from the second methanol reaction unit; (f)) combining the first and a part of the second effluent stream;(g) cooling and separating the combined effluent into a methanol-containing liquid stream and the recycle stream; and (h) withdrawing the remaining part of the second effluent stream a purge gas stream,wherein the remaining part of the second effluent stream is withdrawn as a purge gas stream prior to combining the first and second effluent stream.
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
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
Process for dehydrogenation of a hydrocarbon feed stock in at least one fixed bed reactor, the fixed bed reactor containing a platinum and gallium comprising dehydrogenation catalyst, the process being a cyclic process with alternating steps comprising a step of dehydrogenating the hydro-carbon feed stock and a step of regenerating the platinum and gallium comprising dehydrogenation catalyst in an oxygen containing gas stream, wherein the oxygen containing gas contains water in an amount of less than 3% by volume.
A novel steam reforming catalyst comprising hibonite and potassium beta-alumina with improved resilience, improved activity, reduced potassium leaching and reduced coking problems. It also regards a method for producing the novel catalyst and uses of the novel catalyst in reforming reactors, in a plant for producing hydrogen gas, or in a plant 5for producing synthesis gas.
C01B 3/40 - 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 characterised by the catalyst
B01J 37/02 - Impregnation, coating or precipitation
B01J 35/00 - Catalysts, in general, characterised by their form or physical properties
B01J 23/00 - Catalysts comprising metals or metal oxides or hydroxides, not provided for in group
B01J 23/78 - 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 alkali- or alkaline earth metals or beryllium
92.
A PROCESS FOR METHANOL PRODUCTION USING A LOW-IRON CATALYST
The deterioration of methanol synthesis catalysts that is caused by iron poisoning of the catalyst is counteracted by using a catalyst containing a maximum of 100 ppmw Fe in the synthesis process. The method is especially useful in a methanol synthesis plant comprising a make-up gas compressor and a synthesis reactor in a methanol loop with a once-through pre-converter installed between the make-up gas compressor and the methanol loop.
C07C 29/154 - 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 catalyst used containing copper, silver, gold, or compounds thereof
B01J 23/80 - 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 zinc, cadmium or mercury
B01J 19/18 - Stationary reactors having moving elements inside
In a method for generating various synthesis gases by electrolysis, comprising feeding steam and compressed air to the cathode and anode, respectively, of the electrolysis unit or of the first of a series of electrolysis units into the first of a series of electrolysis units, the electrolysis units are operated under an elevated gas pressure, and the oxygen-rich gas leaving the anode is subsequently expanded down to approximately ambient pressure using a gas expander. The electrolysis units are preferably solid oxide electrolysis cell (SOEC) stacks.
A method for activating an oxidic fresh hydroprocessing catalyst or the catalytically active material of a spent hydroprocessing catalyst comprising a refractory oxide support and one or more base metals selected from Ni, Co, Mo and W comprises optionally regenerating the catalyst, adjusting an aqueous activating solution, which contains an organic acid, to pH > 3 with an alkaline additive, impregnating the catalytically active material with the pH-adjusted aqueous activating solution, and heat-treating the catalyst at a temperature of 120-450°C.
B01J 38/08 - Gas or vapour treatingTreating by using liquids vaporisable upon contacting spent catalyst using ammonia or derivatives thereof
B01J 38/62 - Liquid treating or treating in liquid phase, e.g. dissolved or suspended using acids organic
B01J 38/66 - Liquid treating or treating in liquid phase, e.g. dissolved or suspended using alkaline materialLiquid treating or treating in liquid phase, e.g. dissolved or suspended using salts using ammonia or derivatives thereof
The invention relates to a method for producing a synthesis gas for use in the production of a hydrocarbon product, particularly a synthetic fuel, said method comprising the steps of: providing a hydrocarbon feed gas; optionally, purifying the hydrocarbon feed gas in a gas purification unit; optionally, prereforming the hydrocarbon feed gas together with a steam feedstock in a prereforming unit; carrying out steam methane reforming in a reforming reactor heated by means of an electrical power source;providing the synthesis gas to a synthetic fuel synthesis unit, preferably a Fischer-Trop-sch synthesis unit, for converting said synthesis gas into hydrocarbon product and producing a tail gas. The invention also relates to a system for producing a synthesis gas for use in the production of a hydrocarbon product, particularly a synthetic fuel.
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
C10G 2/00 - Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
96.
BIOGAS CONVERSION TO SYNTHESIS GAS FOR PRODUCING HYDROCARBONS
The invention relates to a method for producing a synthesis gas for use in the production of a hydrocarbon product, particularly a synthetic fuel, said method comprising the steps of: providing a hydrocarbon feed stream comprising biogas; optionally, purifying the hydrocarbon feed stream in a gas purification unit; optionally, prereforming the hydrocarbon feed stream together with a steam feedstock in a prereforming unit; carrying out steam methane reforming in a reforming reactor heated by means of an electrical power source; providing the synthesis gas to a synthetic fuel synthesis unit, preferably a Fischer-Tropsch synthesis unit, for converting said synthesis gas into hydrocarbon product and producing a tail gas. The invention also relates to a system for producing a synthesis gas for use in the production of a hydrocarbon product, particularly a synthetic fuel.
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
C10G 2/00 - Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
A heating system and a process for heating a pressurized feed gas is provided, where the heat for the reaction is provided by resistance heating by means of electrical power.
Structured catalyst arranged for catalyzing an endothermic reaction of a feed gas, said structured catalyst comprising a macroscopic structure of electrically conductive material, said macroscopic structure supporting a ceramic coating, wherein said ceramic coating supports a catalytically active material, wherein the electrically conductive material at least partly is a composite in the form of a homogenous mixture of an electrically conductive metallic material and a ceramic material, wherein the macroscopic structure at least partly is composed of two or more materials with different resistivities.
A method for the preparation of methanol by conversion of a mixture of fresh methanol synthesis gas and unconverted methanol synthesis separated from produced methanol in a low pressure separator and recycled and admixed to the fresh synthesis gas upstream the suction side of a make-up gas compressor.
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
222 to a first product gas comprising CO are provided, where a methanation reaction take place in parallel to the reverse water gas shift reaction, and where the heat for the endothermic reverse water gas shift reaction is provided by resistance heating. Ø
B01J 12/00 - Chemical processes in general for reacting gaseous media with gaseous mediaApparatus specially adapted therefor
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
