An ethylene plant comprising an electrically-powered pyrolysis reactor and a process for producing a pyrolysis reactor effluent using the ethylene plant. The pyrolysis reactor comprises a feed inlet for a hydrocarbon feedstock-diluent mixture and an outlet for a pyrolysis reactor effluent comprising ethylene. The plant further comprises a heat exchanger configured to transfer heat from the pyrolysis reactor effluent to the feed for the pyrolysis reactor. The heat exchanger comprises a feed inlet and a feed outlet upstream of the pyrolysis reactor, and further a pyrolysis reactor effluent inlet and a pyrolysis reactor effluent outlet. A feed passage way is present between the feed outlet of the heat exchanger and the feed inlet of the pyrolysis reactor and further a feed passage way is present between the reactor effluent outlet of the pyrolysis reactor and the cracked gas inlet of the heat exchanger.
C10G 9/24 - Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by heating with electrical means
B01J 19/08 - Processes employing the direct application of electric or wave energy, or particle radiationApparatus therefor
C10G 9/36 - Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by direct contact with inert preheated fluids, e.g. with molten metals or salts with heated gases or vapours
The invention provides a process for the separation of a diol from a product stream. The process includes the steps of: i) separating the product stream comprising three or more C2 to C6 diols, C3 to C6 sugar alcohols, and C4 to C6 polyhydric alcohols with at least 3 hydroxyl groups in the molecule, and a catalyst, to produce a first stream comprising the three or more C2 to C6 diols; ii) separating the first stream comprising the three or more C2 to C6 diols into a) a second stream comprising a first diol and unsaturated hydrocarbons and/or one or more compounds with a carbonyl group and b) a third stream comprising two or more diols; iii) hydrogenating the second stream comprising a first diol and unsaturated hydrocarbons and/or one or more compounds with a carbonyl group to provide a purified diol stream.
C07C 29/84 - SeparationPurificationStabilisationUse of additives by physical treatment by distillation by extractive distillation
C07C 29/17 - Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by hydrogenation of carbon-to-carbon double or triple bonds
C07C 29/82 - SeparationPurificationStabilisationUse of additives by physical treatment by distillation by azeotropic distillation
09 - Scientific and electric apparatus and instruments
37 - Construction and mining; installation and repair services
40 - Treatment of materials; recycling, air and water treatment,
42 - Scientific, technological and industrial services, research and design
Goods & Services
Electrolyzers. Construction of green energy production plants featuring
electrolyzers; construction of green hydrogen production
plants; construction of electrolysis facilities; consulting
relating to the construction of plants containing
electrolyzers for producing hydrogen gas. Electrolysis services, namely, producing hydrogen from water
for third party users of hydrogen; production of green
hydrogen; provision of equipment to produce or consume green
hydrogen and its derivatives, in particular for industrial
projects in the petrochemical, fertilizer and steel
industries. Providing technological services, design, engineering,
project studies and exploitation services to produce or
consume green hydrogen and its derivatives, in particular
for industrial projects in the petrochemical, fertilizer and
steel industries.
4.
RIBBED SLAB FOUNDATION FOR CYLINDRICAL REFRIGERATED TANKS FOR LIQUIFIED GAS STORAGE
A foundation for cylindrical refrigerated tanks for liquified gas storage, at locations where the minimum ambient temperature is always greater than 0° C., characterized by a reinforced concrete ribbed slab structure at grade level, where the clear spaces in between the parallel webs of the ribbed slab are configured as air circulation channels to provide ambient air circulation suitable to prevent the ground underneath the foundation itself from reaching freezing temperatures, i.e. ≤0° C., while providing the necessary bearing and structural capacity.
E02D 27/38 - Foundations for large tanks, e.g. oil tanks
E02D 31/14 - Protective arrangements for foundations or foundation structuresGround foundation measures for protecting the soil or the subsoil water, e.g. preventing or counteracting oil pollution against soil pressure or hydraulic pressure against frost heaves in soil
09 - Scientific and electric apparatus and instruments
37 - Construction and mining; installation and repair services
40 - Treatment of materials; recycling, air and water treatment,
42 - Scientific, technological and industrial services, research and design
Goods & Services
(1) Electrolyzers. (1) Construction of green energy production plants featuring electrolyzers; construction of green hydrogen production plants; construction of electrolysis facilities; consulting relating to the construction of plants containing electrolyzers for producing hydrogen gas.
(2) Electrolysis services, namely, producing hydrogen from water for third party users of hydrogen; production of green hydrogen; provision of equipment to produce or consume green hydrogen and its derivatives, in particular for industrial projects in the petrochemical, fertilizer and steel industries.
(3) Providing technological services, design, engineering, project studies and exploitation services to produce or consume green hydrogen and its derivatives, in particular for industrial projects in the petrochemical, fertilizer and steel industries.
6.
Flameless Combustion Burner For An Endothermic Reaction Process
The present invention relates to a combustion heater (100) for providing controlled heat (H) to an endothermic reaction process. The combustion heater comprises an integrated burner (20) to yield a hot burner exhaust gas (35) flow from burning a first fuel. The burner exhaust gas mixed with oxidant flows to a flue gas outlet along a flue gas flow path (FGP). Provided to the combustion chamber at a position outside a direct reach of flames from the burner is a secondary fuel conduit (30) with a plurality of nozzles (31) from which a second fuel (32) is transferred into a flow along the said flue gas flow path (FGP). The resulting combustion of the second fuel can be used to provide controlled heat to the to endothermic reaction operated in a reaction conduit (40) that is in thermal heat exchange with the combustion chamber.
The present disclosure concerns an ethylene plant comprising an electrically- powered pyrolysis reactor and a process for producing a pyrolysis reactor effluent using the ethylene plant. The pyrolysis reactor comprises a feed inlet for a hydrocarbon feedstock-diluent mixture and an outlet for a pyrolysis reactor effluent comprising ethylene. The plant further comprises a heat exchanger (90) configured to transfer heat from the pyrolysis reactor effluent to the feed for the pyrolysis reactor. The heat exchanger (90) comprises a feed inlet and a feed outlet upstream of the pyrolysis reactor, and further a pyrolysis reactor effluent inlet and a pyrolysis reactor effluent outlet. A feed passage way is present between the feed outlet of the heat exchanger and the feed inlet of the pyrolysis reactor and further a feed passage way is present between the reactor effluent outlet of the pyrolysis reactor and the cracked gas inlet of the heat exchanger.
C10G 9/24 - Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by heating with electrical means
C10G 9/36 - Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by direct contact with inert preheated fluids, e.g. with molten metals or salts with heated gases or vapours
8.
ETHYLENE PLANT, COMPRISING AN ELECTRICALLY-POWERED PYROLYSIS REACTOR AND A FEED-EFFLUENT HEAT EXCHANGER
The present disclosure concerns an ethylene plant comprising an electrically- powered pyrolysis reactor and a process for producing a pyrolysis reactor effluent using the ethylene plant. The pyrolysis reactor comprises a feed inlet for a hydrocarbon feedstock-diluent mixture and an outlet for a pyrolysis reactor effluent comprising ethylene. The plant further comprises a heat exchanger (90) configured to transfer heat from the pyrolysis reactor effluent to the feed for the pyrolysis reactor. The heat exchanger (90) comprises a feed inlet and a feed outlet upstream of the pyrolysis reactor, and further a pyrolysis reactor effluent inlet and a pyrolysis reactor effluent outlet. A feed passage way is present between the feed outlet of the heat exchanger and the feed inlet of the pyrolysis reactor and further a feed passage way is present between the reactor effluent outlet of the pyrolysis reactor and the cracked gas inlet of the heat exchanger.
C10G 9/24 - Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by heating with electrical means
C10G 9/36 - Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by direct contact with inert preheated fluids, e.g. with molten metals or salts with heated gases or vapours
C10G 9/00 - Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
A process for the production of a high purity first diol from a product stream comprising two or more C2 to C7 diols, said process comprising the steps of: (i) providing the product stream to a first distillation column; (ii) providing an extractant selected from the group of C3 to C6 sugar alcohols and mixtures thereof to the first distillation column; (iii) operating the first distillation column to obtain a first bottoms stream comprising at least a first diol and the extractant; (iv) providing the first bottoms stream to a second distillation column operating to obtain a second top stream comprising the first diol and diols with atmospheric boiling points at least 10° C. higher than the first diol, and (v) providing the second top stream to a third distillation column to obtain a third top stream comprising the first diol; wherein the product stream comprises 0.1 to 10 wt % of diols with atmospheric boiling points at least 10° C. higher than the first diol, calculated upon the total weight of C2 to C7 diols in the product stream.
Cracking furnace system for converting a hydrocarbon feedstock into cracked gas comprising a convection section, a radiant section and a cooling section, wherein the convection section includes a plurality of convection banks, including a first high temperature coil, configured to receive and preheat hydrocarbon feedstock, wherein the radiant section includes a firebox comprising at least one radiant coil configured to heat up the feedstock to a temperature allowing a pyrolysis reaction, wherein the cooling section includes at least one transfer line exchanger.
C10G 9/36 - Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by direct contact with inert preheated fluids, e.g. with molten metals or salts with heated gases or vapours
11.
RIBBED SLAB FOUNDATION FOR CYLINDRICAL REFRIGERATED TANKS FOR LIQUIFIED GAS STORAGE
A foundation (FV) for cylindrical refrigerated tanks for liquified gas storage, at locations where the minimum ambient temperature is always greater than 0°C, characterized by a reinforced concrete ribbed slab structure at grade level, where the clear spaces in between the parallel webs (W) of said ribbed slab are configured as air circulation channels (C) to provide ambient air circulation suitable to prevent the ground (T) underneath the foundation itself from reaching freezing temperatures, i.e. ≤0°C, while providing the necessary bearing and structural capacity.
E02D 27/38 - Foundations for large tanks, e.g. oil tanks
E02D 31/14 - Protective arrangements for foundations or foundation structuresGround foundation measures for protecting the soil or the subsoil water, e.g. preventing or counteracting oil pollution against soil pressure or hydraulic pressure against frost heaves in soil
E04H 7/02 - Containers for fluids or gasesSupports therefor
A method for separating monoethylene glycol (MEG) from one or more oxygenates. The method includes providing a stream comprising MEG and one or more oxygenates to a distillation column, providing a water feed stream to a bottom of the distillation column, and removing a recovery stream comprising MEG from the distillation column. The distillation column is operated at higher temperatures than the thermal stability of MEG and the one or more oxygenates.
The invention provides a process for the separation of a first C3 to C7 diol from a first mixture of C3 to C7 diols. The first mixture is provided to a first distillation column. An extractant is fed to the first distillation column above the first mixture. A stream comprising the first diol and the extractant is removed as a bottoms stream from the first distillation column and subjected to distillation in a second distillation column. A high purity first diol stream is removed from the top section of the second distillation column, while a used extractant stream is removed from the bottom section. The extractant is a C3 to C6 sugar alcohol or mixture thereof. The first diol is a close-boiler to and/or forms an azeotrope with one or more of the other C3 to C7 diols present in the first mixture.
Implementations of the disclosed subject matter provide a process for producing ethylene glycol and propylene glycol from a sorbitol feed which may include contacting the sorbitol feed with hydrogen in a reactor in the presence of a solvent and a bi-functional catalyst system. The bi-functional catalyst system may include a first catalyst comprising a copper compound, a zinc compound, and an additional metal compound and a second catalyst comprising sodium carbonate.
C07C 29/60 - Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by elimination of hydroxy groups, e.g. by dehydration
B01J 23/83 - Catalysts comprising metals or metal oxides or hydroxides, not provided for in group of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups with rare earths or actinides
A process for the production of high purity mono-ethylene glycol (MEG) from a product stream of a saccharide hydrogenolysis process. The process having the steps of: (i) removing solvent from the product stream to provide a solvent-lean product stream; (ii) subjecting the solvent-lean product stream to distillation to provide a bottoms stream comprising high boiling by-products and a top stream comprising a mixture comprising MEG and 1,2-butanediol (1,2-BDO); (iii) providing said mixture having MEG and 1,2-BDO as a feed to a distillation column; (iv) providing a feed comprising an extractant of C3 to C6 alcohols and mixtures thereof to the distillation column above the mixture comprising MEG and 1,2-BDO; (v) removing a stream comprising MEG and the extractant as a bottoms stream from the distillation column; and (vi) subjecting the stream comprising MEG and the extractant to distillation to provide a top stream comprising high purity MEG.
The invention provides a process for the separation of MEG and 1,2-BDO from a first mixture comprising MEG and 1,2-BDO in a weight ratio of at least 10:1 (MEG:1,2-BDO), said process comprising the steps of; (i) providing the first mixture as a feed to a distillation column at a point in the range of from 20 to 80% of the column height; (ii) operating the distillation at a temperature in the range of from 120 to 190° C. and at a pressure in the range of from 5 kPa to atmospheric pressure; (iii) removing an MEG stream from the distillation column at a point below the point at which the first mixture is fed; (iv) removing an overheads stream comprising an azeotrope of MEG and 1,2-BDO.
The invention provides a process for the separation of MEG from a glycol stream comprising MEG and 1,2-BDO, said process comprising the steps of: (a) providing the glycol stream and an azeotrope-forming agent to a distillation column, (b) subjecting the glycol stream and the azeotrope-forming agent to distillation at a distillation temperature and a distillation pressure; (c) obtaining a first overhead stream comprising an azeotrope of MEG and the azeotrope-forming agent and a first bottoms stream comprising 1,2-BDO; and (d) subjecting the first overhead stream to phase separation in the presence of water to obtain an MEG-rich aqueous stream and an azeotrope-forming agent rich stream, wherein the azeotrope-forming agent is an organic solvent that forms a homogeneous azeotrope with MEG and does not form an azeotrope with 1,2-BDO at the distillation temperature and pressure.
A process for the separation of monoethylene glycol (MEG) and 1,2-butanediol (1,2-BDO) from a first mixture including MEG and 1,2-BDO, the process including providing the first mixture of MEG and 1,2-BDO as a feed to a distillation column. The process also includes providing a feed comprising glycerol to the distillation column above the first mixture. The process also includes operating the distillation column at a temperature in the range of from 50 to 250° C. and a pressure in the range of from 0.1 to 400 kPa. The process also includes removing a stream comprising MEG and glycerol as a bottoms stream from the distillation column and removing a stream comprising 1,2-BDO above the point at which the feed comprising glycerol is provided to the distillation column.
The invention provides a process for separating monoethylene glycol from a mixture comprising monoethylene glycol and 1,2-butanediol, said process comprising the steps of: a. providing a first stream comprising monoethylene glycol and 1,2-butanediol to a first distillation zone operated at a first pressure and under conditions to remove a first bottoms stream comprising 1,2-butanediol and to remove a first azeotrope of monoethylene glycol and 1,2-butanediol from the first distillation zone as a first overheads stream; b. withdrawing said first overheads stream from said first distillation zone; and c. providing said first overheads stream to a second distillation zone operated at a second pressure higher than said first pressure and under conditions to remove a second bottoms stream comprising monoethylene glycol and providing a second azeotrope of monoethylene glycol and 1,2-butanediol as a second overheads stream; d. withdrawing said second overheads stream from the second distillation zone and providing it to the first distillation zone as at least a portion of the first stream comprising monoethylene glycol and 1,2-butanediol, e. wherein the mixture comprising monoethylene glycol and 1,2-butanediol is initially provided to at least one of the first distillation zone and the second distillation zone.
The present invention relates to a process for manufacturing succinic acid as obtained by fermentation, said process exhibiting a high yield in terms of succinic acid crystals recovery and allowing to achieve a final product with a low content of saccharides.
C07C 51/43 - SeparationPurificationStabilisationUse of additives by change of the physical state, e.g. crystallisation
C07C 51/47 - SeparationPurificationStabilisationUse of additives by solid-liquid treatmentSeparationPurificationStabilisationUse of additives by chemisorption
The present invention relates to a method for a dicarboxylic acid, which method comprises fermenting fungal cells in a vessel comprising a suitable fermentation medium, wherein a least a portion of the fungal cells are reused in the presence of a vitamin and/or a trace element.
