Abstract

For producing synthesis gas by autothermal reformation of gaseous, liquid and/or solid fuels, the fuel is reacted with an oxidizing agent in a reaction space at a pressure of 10 to 120 bar and a reaction space temperature of 800 to 2,000° C. to obtain synthesis gas, wherein the oxidizing agent is introduced centrally in the upper region of the reaction space and wherein a flame is formed in the reaction space. The oxidizing agent is introduced into the reaction space separate from the fuel.

IPC Classes  ?

• B01J 7/00 - Apparatus for generating gases
• 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
• B01J 4/00 - Feed devicesFeed or outlet control devices
• B01J 8/02 - Chemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes with stationary particles, e.g. in fixed beds
• C01B 3/38 - Production of hydrogen or of gaseous mixtures containing hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts
• C10J 3/50 - Fuel charging devices

Abstract

A distillation column with external circulation evaporator and a sedimentation zone in the bottom of the column, from which the evaporator circulation is fed, and use of the distillation column for the distillation of acrylic acid.

IPC Classes  ?

• B01D 3/22 - Fractionating columns in which vapour bubbles through liquid with horizontal sieve plates or gridsConstruction of sieve plates or grids
• B01D 3/32 - Other features of fractionating columns
• C07C 51/44 - SeparationPurificationStabilisationUse of additives by change of the physical state, e.g. crystallisation by distillation

Abstract

4+ olefins in the educt stream (C) here is 0.05 to 0.5 and is calculated according to the following formula: olefin-i: molar flow rate of the olefin i.

IPC Classes  ?

• 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 2/86 - Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by condensation between a hydrocarbon and a non-hydrocarbon
• C07C 4/06 - Catalytic processes

Abstract

Process for producing synthetic natural gas (SNG) which is provided in an energy-efficient way at the inlet pressure into a downstream pipeline system. For this purpose, a synthesis gas containing carbon oxides and hydrogen is converted into a product gas rich in methane by multi-stage catalytic methanation in a main reaction zone and a post-reaction zone, wherein the adjustment of the target pressure is effected by compression before the main reaction zone and/or before or in the post-reaction zone.

IPC Classes  ?

• C07C 27/00 - Processes involving the simultaneous production of more than one class of oxygen-containing compounds

Abstract

A reformer tube (101) for producing synthesis gas by steam reforming of hydrocarbon-containing feed gases, preferably natural gas, in which one or more helically coiled heat exchanger tubes (109) which are arranged within a catalyst bed (105) of a reforming catalyst and are helically coiled over part of their length located within the catalyst bed and are otherwise straight are present, where the straight proportion of the heat exchanger tubes and/or the helix pitch of the helically coiled part alters within the catalyst bed and matching to requirements in respect of the pressure drop and the heat exchange properties and also in respect of the corrosion resistance can therefore be achieved, is proposed.

IPC Classes  ?

• 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
• 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

Abstract

A reformer tube (101) for producing synthesis gas by steam reforming of hydrocarbon-containing feed gases, preferably natural gas, in which one or more helically coiled heat exchanger tubes (109) which are arranged within a catalyst bed (105) of a reforming catalyst and are helically coiled over part of their length located within the catalyst bed and are otherwise straight are present, where the straight proportion of the heat exchanger tubes and/or the helix pitch of the helically coiled part alters within the catalyst bed and matching to requirements in respect of the pressure drop and the heat exchange properties and also in respect of the corrosion resistance can therefore be achieved, is proposed.

IPC Classes  ?

• 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 8/06 - 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

Abstract

The invention relates to the production of olefins from dimethyl ether. Gaseous dimethyl ether with a purity of 70 - 100 wt.% together with recycled gas, which contains olefinic, paraffinic, and/or aromatic hydrocarbons, and water vapor is fed to a first catalyst stage of a reactor. The aim of the invention is to form the temperature profile over the catalyst stages as flatly as possible but as close as possible to the optimal operating temperature. This is achieved in that gaseous dimethyl ether with a purity of 70 - 100 wt.% together with recycled gas, which contains olefinic, paraffinic, and aromatic hydrocarbons, is fed to at least one downstream catalyst stage. Said downstream catalyst stage is additionally supplied product gas from the upstream catalyst stage. The system for this method consists of a reactor with at least two catalyst stages, each of which has a feed line. The ratio of dimethyl ether and recycled gas in said feed lines is determined by a control or regulating device that is attached in the feed or discharge line.

IPC Classes  ?

• 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 11/04 - Ethene
• C07C 11/06 - Propene
• B01J 19/24 - Stationary reactors without moving elements inside

Abstract

Method for reforming hydrocarbon-containing feed gas into synthetic gas, comprising processing of the feed gas and, subsequent thereto, a main reforming step (14'), wherein the processing of the feed gas comprises a pre-reforming step (8') for at least partially converting higher hydrocarbons into methane, and heating the feed gas by exothermic catalytic partial oxidation of hydrocarbons (18) before the introduction thereof into the main reforming zone, with the addition of a controlled quantity of an oxidizing agent (16').

IPC Classes  ?

• 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

Abstract

There is proposed a cooled reactor for the production of dimethyl ether by catalytic dehydration of methanol in the gas phase, which comprises an adiabatic catalyst bed as starting zone, a moderator zone cooled by direct or indirect heat exchange, and optionally an adiabatic catalyst bed as conditioning zone. By using the reactor according to the invention, the conversion of methanol to dimethyl ether can be increased and the formation of undesired by-products can be decreased.

IPC Classes  ?

• 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
• C07C 41/09 - Preparation of ethers by dehydration of compounds containing hydroxy groups
• C07C 43/04 - Saturated ethers

Abstract

A method for reprocessing a phase substantially consisting of steryl glycoside/fatty acid alkyl ester/water agglomerates, which was formed when fatty acid alkyl ester generated by transesterification of vegetable oils or animal fats was washed with water, wherein the water content is evaporated by heating the phase and subsequently the steryl glycosides are split into their sterol and sugar fractions in the presence of an acid catalyst.

IPC Classes  ?

• C11B 3/00 - Refining fats or fatty oils

Abstract

This invention relates to the production of synthesis gas by partial oxidation of liquid or gaseous, carbonaceous fuel in the presence of an oxygen-containing oxidant, wherein the fuel, the oxidant and a moderator are separately supplied to a burner and wherein the fuel and the moderator are mixed in a mixing chamber of the burner, before they are brought in contact with the oxidant. To reduce the load of the burner in particular during operation with transient conditions, the oxidant is centrally introduced through an outlet opening of the burner into a combustion chamber and the mixture of fuel and moderator is introduced through the outlet opening into the combustion chamber concentrically around the oxidant.

IPC Classes  ?

• 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
• F23D 14/78 - Cooling burner parts
• F23D 14/58 - Nozzles characterised by the shape or arrangement of the outlet or outlets from the nozzle, e.g. of annular configuration

Abstract

For producing synthesis gas by autothermal reformation of gaseous, liquid and/or solid fuels, the fuel is reacted with an oxidizing agent in a reaction space at a pressure of 10 to 120 bar and a reaction space temperature of 800 to 2,000 °C to obtain synthesis gas, wherein the oxidizing agent is introduced centrally in the upper region of the reaction space and wherein a flame is formed in the reaction space. The oxidizing agent is introduced into the reaction space separate from the fuel.

IPC Classes  ?

• 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
• F23D 14/22 - Non-premix gas burners, i.e. in which gaseous fuel is mixed with combustion air on arrival at the combustion zone with separate air and gas feed ducts, e.g. with ducts running parallel or crossing each other
• 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 4/00 - Feed devicesFeed or outlet control devices
• 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

Abstract

A method for gasifying solid fuel containing carbon, such as turf, brown coal and hard coal, with the addition of an oxygen-containing gas and steam, wherein the gas condensate accumulating during the washing and cooling of the crude gas is also purified in a manner known per se, subsequently evaporated in the waste heat boiler, the steam is purified by means of thermal catalytic afterburning, the content of water vapor in the flue gas formed in the process is condensed out and the condensate is treated in a boiler feed water conditioning system and evaporated by means of the heat generated in the thermal afterburning, and the steam is supplied as process steam to the gasification of the solid raw materials.

IPC Classes  ?

• C10J 3/06 - Continuous processes
• C10J 3/02 - Fixed-bed gasification of lump fuel
• C10J 3/60 - Processes
• C10J 3/62 - Processes with separate withdrawal of the distillation products
• 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 1/00 - Purifying combustible gases containing carbon monoxide
• 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

Abstract

During the production of methanol from inert-rich syngas, a catalytic pre-reactor is installed upstream of the single- or multi-stage synthesis loop, a first part of the syngas being converted to methanol in the catalytic pre-reactor. Furthermore, an inert gas separation stage, for example a pressure swing adsorption system or a membrane system, is connected downstream of the synthesis loop, whereby a hydrogen-enriched syngas stream can be returned to the synthesis loop. In the processing of methane-rich syngas, the inert gas separation stage may also comprise an autothermal reformer in which methane is converted to carbon oxides and hydrogen, which are also returned into the synthesis loop.

IPC Classes  ?

• 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
• C07C 31/04 - Methanol

Abstract

In the preparation of low molecular weight olefins, especially of ethylene and propylene, a reactant stream (O) comprising at least one oxygenate and a reactant stream (C) comprising at least one C4+ olefin are converted simultaneously in at least one identical reactor over an identical catalyst to a product mixture (P) comprising low molecular weight olefins and gasoline hydrocarbons. In this case, the ratio (V) of oxygenates in the reactant stream (O) to C4+ olefins in the reactant stream (C) is 0.05 to 0.5 and is calculated by the following formula: formula (I) where: koxygenate-j: carbon number of the oxygenate j noxygenate-j: molar flow rate of the oxygenate j kolefin-i: carbon number of the olefin i nolefin-i: molar flow rate of the olefin i.

IPC Classes  ?

• 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 4/02 - Preparation of hydrocarbons from hydrocarbons containing a larger number of carbon atoms by cracking a single hydrocarbon or a mixture of individually defined hydrocarbons or a normally gaseous hydrocarbon fraction

Abstract

A gas scrubber, equipped with heat exchanger surfaces constructed of thermoplates, suitable for cooling and cleaning a hot gas by avoiding an excessive thermal load of the washing liquid.

IPC Classes  ?

• B01D 47/00 - Separating dispersed particles from gases, air or vapours by liquid as separating agent
• B01D 53/18 - Absorbing unitsLiquid distributors therefor
• B01D 53/78 - Liquid phase processes with gas-liquid contact
• C07D 251/60 - Preparation of melamine from urea or from carbon dioxide and ammonia
• F28D 9/00 - Heat-exchange apparatus having stationary plate-like or laminated conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall
• F28F 3/14 - Elements constructed in the shape of a hollow panel, e.g. with channels by separating portions of a pair of joined sheets to form channels, e.g. by inflation
• F28F 13/06 - Arrangements for modifying heat transfer, e.g. increasing, decreasing by affecting the pattern of flow of the heat-exchange media
• B01D 53/77 - Liquid phase processes

Abstract

The invention relates to a distillation column with an externally located circulating evaporator and a sedimentation zone in the column sump from which the evaporator is supplied, and also relates to the use of the distillation column according to the invention for distilling acrylic acid.

IPC Classes  ?

• B01D 3/32 - Other features of fractionating columns
• C07C 51/00 - Preparation of carboxylic acids or their salts, halides, or anhydrides

Abstract

For reducing nitrogen oxides during the steam reformation, wherein a gaseous carbon carrier, preferably natural gas, and water are reacted in a reactor to obtain a synthesis gas containing hydrogen, carbon monoxide and carbon dioxide, hydrogen, carbon monoxide and/or carbon dioxide are separated from the synthesis gas and the flue gas obtained in the reactor is passed over at least one catalyst stage and subjected there to a selective catalytic reduction. A part of the gaseous carbon carrier, a part of a mixture of the gaseous carbon carrier and water, a part of a gaseous fuel utilized for heating, a part of the synthesis gas, a part of the depleted synthesis gas and/or a part of the separated hydrogen is/are used in the catalyst stage as reducing agent.

IPC Classes  ?

• C10K 1/34 - Purifying combustible gases containing carbon monoxide by catalytic conversion of impurities to more readily removable materials
• B01D 53/86 - Catalytic processes
• 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

Abstract

A process for the continuous production of melamine from urea by means of a fluidized-bed reactor, wherein process gas guided in the process circuit is used as fluidizing gas and wherein the temperature of the process gas at the inlet of the conveying means for the fluidizing gas is adjusted by adjusting the mixing ratio of a process gas stream guided over a scrubber and of a process gas stream guided past the scrubber.

IPC Classes  ?

• C07D 251/60 - Preparation of melamine from urea or from carbon dioxide and ammonia
• C07D 251/62 - Purification of melamine

Abstract

The invention relates to a method for recovering high-grade biodegradable fatty alcohols from waste fats and/or waste oils. To this end the waste oils or fats are first of all split by hydrolysis. After cleaning with short-chain alkenes the recovered fatty acid is converted to fatty acid alkyl esters which, after further cleaning, are split by hydrogenation into fatty alcohols and alkanols. In this way alkanols are also recovered as desired by-products in addition to the fatty alcohols.

IPC Classes  ?

• C07C 29/149 - 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 an oxygen-containing functional group of C=O containing groups, e.g. —COOH of carboxylic acids or derivatives thereof with hydrogen or hydrogen-containing gases
• C07C 51/09 - Preparation of carboxylic acids or their salts, halides, or anhydrides from carboxylic acid esters or lactones
• C07C 67/04 - Preparation of carboxylic acid esters by reacting carboxylic acids or symmetrical anhydrides onto unsaturated carbon-to-carbon bonds
• C07C 31/125 - Monohydroxylic acyclic alcohols containing five to twenty-two carbon atoms
• C07C 33/02 - Acyclic alcohols with carbon-to-carbon double bonds
• C07C 53/126 - Acids containing more than four carbon atoms
• C07C 57/03 - Monocarboxylic acids
• C07C 69/24 - Esters of acyclic saturated monocarboxylic acids having the carboxyl group bound to an acyclic carbon atom or to hydrogen having three or more carbon atoms in the acid moiety esterified with monohydroxylic compounds
• C07C 69/52 - Esters of acyclic unsaturated carboxylic acids having the esterified carboxyl group bound to an acyclic carbon atom

Abstract

The invention relates to a tubular reactor for carrying out a catalytically supported, homogeneous chemical reaction in the gas phase at an elevated temperature and a subsequent cooling, wherein the reactor is arranged upright, and therefore the tubes extend vertically and the gas flows downward through the tubes, wherein the tubes are filled with a catalyst bed in the upper part thereof extending in the reaction zone of the reactor and are filled with a structured packing in the lower part, the cooling zone of the reactor.

IPC Classes  ?

• 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

Abstract

A method for the continuous extraction of impurities, in particular saponification products, from a fatty acid alkyl ester phase produced by transesterification of vegetable or animal oils or fats with a great tendency to form saponification products, by means of an aqueous, acid glycerol phase containing a complexing agent.

IPC Classes  ?

• C07C 51/42 - SeparationPurificationStabilisationUse of additives
• C11B 3/00 - Refining fats or fatty oils
• C11B 1/00 - Production of fats or fatty oils from raw materials

Abstract

Process for the enzymatic degradation of phosphorus-containing components and glycosides, in particular steryl glycoside from crude oil or degummed oil of vegetable or animal origin, where the addition of the enzymes in both cases is carried out in one process step.

IPC Classes  ?

• C11B 3/00 - Refining fats or fatty oils

Abstract

An apparatus for discharging bulk material (1) from a container containing process gas, which is under excess pressure, consisting of a screw conveyor with a closure in the form of a closing cone ( 4 ) and a downstream purge tank in which gas discharged with the bulk material is rinsed out of the bulk material by means of a purge gas.

IPC Classes  ?

• B65G 53/08 - Gas pressure systems operating without fluidisation of the materials with mechanical injection of the materials, e.g. by screw

Abstract

6 hydrocarbons is at least partly subjected to an etherification with methanol. The ethers thus obtained are admixed to the gasoline product stream.

IPC Classes  ?

• C10L 1/18 - Organic compounds containing oxygen
• C10G 29/22 - Organic compounds not containing metal atoms containing oxygen as the only hetero atom
• C10L 1/185 - EthersAcetalsKetalsAldehydesKetones

Abstract

In the production of purified methanol and/or dimethyl ether from crude methanol, the crude methanol is processed in at least one prepurification stage, a first partial stream of the prepurified methanol is supplied to a final methanol purification and a second partial stream of the prepurified methanol is supplied to a reactor and at least partly converted to dimethyl ether. The dimethyl ether recovered is purified in at least one purification stage, wherein non-reacted methanol is withdrawn from the dimethyl ether purification stage and at least partly supplied to the final methanol purification. In this way, both purified methanol and dimethyl ether can be produced in parallel, wherein the quantities of both products obtained are flexibly adjustable.

IPC Classes  ?

• C07C 41/18 - Preparation of ethers by reactions not forming ether-oxygen bonds
• B01J 8/00 - Chemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes
• C07C 29/80 - SeparationPurificationStabilisationUse of additives by physical treatment by distillation
• C07C 41/09 - Preparation of ethers by dehydration of compounds containing hydroxy groups

Abstract

2 reclaimed by desorption of laden methanol as purge gas.

IPC Classes  ?

• C01B 17/16 - Hydrogen sulfides
• C01B 17/48 - Sulfur dioxideSulfurous acid
• C01B 17/52 - Preparation of sulfur dioxide by roasting sulfides
• F23C 99/00 - Subject matter not provided for in other groups of this subclass

Abstract

A method for volatile compound (VC) mitigation in a syngas production process is provided. This method includes providing a hydrocarbon reforming syngas production plant, this plant includes a reformer system comprising a primary fuel and oxidant stream, where part of this system is at low pressure, a steam inlet stream, and a primary combustion system for providing heat to the reformer system and producing a reformer flue gas stream, and a gaseous vent stream mainly composed of water and containing VC. This method also includes introducing at least a portion of the vent stream into one or more of the following: the primary fuel and oxidant stream; the steam inlet stream; the reformer flue gas stream.

IPC Classes  ?

• 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

Abstract

The invention relates to a burner for partially oxidizing liquid, carbon-containing fuel, said fuel having water vapor and an oxygen-containing gas, and to the method in which said burner is used, wherein the parts of the outlet opening of the burner directed toward the combustion chamber are completely or partially provided with a coating or with a diffusion layer for protecting against thermal loading and/or corrosion.

IPC Classes  ?

• 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
• F23D 11/00 - Burners using a direct spraying action of liquid droplets or vaporised liquid into the combustion space

Abstract

The invention relates to a burner for partially oxidizing liquid, carbon-containing fuel, said fuel having water vapor and an oxygen-containing gas, and to the method in which said burner is used, wherein the parts of the outlet opening of the burner directed toward the combustion chamber are completely or partially provided with a coating or with a diffusion layer for protecting against thermal loading and/or corrosion.

IPC Classes  ?

• 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
• F23D 11/00 - Burners using a direct spraying action of liquid droplets or vaporised liquid into the combustion space

Abstract

The invention relates to a method for reprocessing solid, organic waste occurring in plant oil production, for example palm oil production, said waste being mainly composed of pressing residues of the oil plants and/or oil seeds and oil-containing wastewater, by hydrothermal carbonization (HTC), wherein the oil emulsified in the wastewater is sorbed by the carbon-rich solids arising from the solid waste.

IPC Classes  ?

• C05F 5/00 - Fertilisers from distillery wastes, molasses, vinasses, sugar plant, or similar wastes or residues
• C10L 5/44 - Solid fuels essentially based on materials of non-mineral origin on vegetable substances

Abstract

The invention relates to a method for producing substitute natural gas (SNG) which is supplied into a downstream pipeline system, at the feeding pressure and in an energy efficient manner. To this end, a syngas containing carbon monoxide and hydrogen is converted into a methane-rich product gas in a main reaction zone and a post-reaction zone by means of multi-stage catalytic methanation, the target pressure being adjusted by compression before the main reaction zone and/or before or in the post-reaction zone.

IPC Classes  ?

• C10L 3/08 - Production of synthetic natural gas
• 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

Abstract

The aim of the invention is the distillation of temperature-sensitive liquids, in particular acrylic acid and the esters thereof. This is achieved in that the liquid is heated in a column and at least partially vaporized. The vapor is conducted through a condenser that is provided within the column, said vapor being at least partially condensed in the condenser. The condensed liquid is at least partially drawn off from the column. The distillation is characterized in that the vapor that is not yet condensed is conducted through the condenser concurrently with the condensed liquid.

IPC Classes  ?

• B01D 3/00 - Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
• B01D 5/00 - Condensation of vapoursRecovering volatile solvents by condensation
• B01D 3/14 - Fractional distillation

Abstract

6 hydrocarbons together with the educt mixture is supplied to the at least one first reactor.

IPC Classes  ?

• 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 4/06 - Catalytic processes

Abstract

A process for continuous production of biodiesel from vegetable oils or animal fats by transesterification with methanol or ethanol to give crude fatty acid alkyl esters, subsequent washing with water in a wash column to remove water-soluble impurities, subsequent drying by vaporization of the water content and subsequent removal of steryl glycosides by adsorption onto calcium bentonite, wherein the adsorption column(s) used is/are regenerated in a first step, for desorption of the steryl glycosides, by rinsing with a mixture consisting of fatty acid alkyl esters and methanol or ethanol, and in a subsequent second step, for removal of methanol residues, by rinsing with fatty acid alkyl esters or with gaseous nitrogen or carbon dioxide.

IPC Classes  ?

• C11C 1/08 - Refining
• C11C 3/00 - Fats, oils or fatty acids obtained by chemical modification of fats, oils or fatty acids, e.g. by ozonolysis
• C10L 1/02 - Liquid carbonaceous fuels essentially based on components consisting of carbon, hydrogen, and oxygen only

Abstract

The invention relates to a method and system for producing an olefin flow from a hydrocarbon-mixture input flow, wherein the olefin flow is depleted regarding the olefin flow's content of organic compounds containing oxygen (oxygenates) relative to the input flow. This is achieved in that the hydrocarbon-mixture input flow is introduced into a separation column that operates according to a thermal separation process, for example a distillation column, wherein a material flow enriched in oxygenates is withdrawn through a side outlet and removed from the process. The method according to the invention is suitable in particular for preparing the product flows obtained in the olefin synthesis according to an OTO process.

IPC Classes  ?

• C07C 7/04 - Purification, separation or stabilisation of hydrocarbonsUse of additives by distillation
• C07C 11/06 - Propene
• B01D 3/00 - Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping

Abstract

2 and low-boiling water-soluble organic components. To avoid an enrichment of volatile organic compounds in the acid gas absorber, a partial stream of the liquid phase is withdrawn from an acid gas absorber and processed such that gaseous ammonia with a reduced content of volatile organic components is obtained, which is recirculated into the acid gas absorber.

IPC Classes  ?

• B01D 53/40 - Acidic components
• B01D 53/58 - Ammonia
• B01D 53/78 - Liquid phase processes with gas-liquid contact

Abstract

When producing biodiesel from fats, oils or split fatty acids rich in steryl glycosides, the light phase rich in fatty acid alkyl esters, which is obtained from the transesterification or esterification, is washed with water in a washing column, wherein the suspension layer formed is treated by stirring. In this way, the steryl glycosides are transferred into the light phase of the wash. In a subsequent treatment of the light washer phase with water in an intensive mixer, compact steryl glycoside/fatty acid alkyl ester/water agglomerates are obtained, which can easily be separated by means of centrifugation. From the light phase of centrifugation, on-spec biodiesel is obtained upon further processing by drying and/or filtration. This process is suitable for processing fats, oils or split fatty acids with a high content of steryl glycosides and avoids the use of auxiliary substances foreign to the process. It is characterized by simplicity of equipment and a low demand for energy.

IPC Classes  ?

• C10L 1/18 - Organic compounds containing oxygen

Abstract

The invention relates to a method for reprocessing a phase substantially comprising steryl glycoside/fatty acid alkyl ester/water agglomerates, said phase arising when fatty acid alkyl ester produced by transesterification of plant oils or animal fats is washed with water, wherein the water fraction is evaporated off by heating the phase and then the steryl glycosides are split into the sterol and sugar parts thereof in the presence of an acidic catalyst.

IPC Classes  ?

• C11C 1/08 - Refining
• C11C 1/10 - Refining by distillation
• C11C 3/00 - Fats, oils or fatty acids obtained by chemical modification of fats, oils or fatty acids, e.g. by ozonolysis
• C11C 3/04 - Fats, oils or fatty acids obtained by chemical modification of fats, oils or fatty acids, e.g. by ozonolysis by esterification of fats or fatty oils
• C10L 1/02 - Liquid carbonaceous fuels essentially based on components consisting of carbon, hydrogen, and oxygen only

Abstract

In a process for distilling polymerization-prone compounds from liquid mixtures of matter which, apart from the readily polymerizable compound, also contain other components and also polymerization inhibitors, the evaporator is operated in forced circulation and at a pressure which makes possible superheating of the liquid with respect to its boiling point at the pressure within the distillation column. This is achieved by transporting the superheated liquid against a flow restrictor, e.g. an orifice plate. The liquid which is expanded and partially evaporated on passage through the flow restrictor is returned to the distillation column. In this manner the formation of an open vapour space in the evaporator circuit after heating downstream of the heat exchanger is avoided in that, in the design of the evaporator of the prior art, formation of polymer deposits frequently occurs.

IPC Classes  ?

• B01D 3/32 - Other features of fractionating columns
• C07C 51/44 - SeparationPurificationStabilisationUse of additives by change of the physical state, e.g. crystallisation by distillation

Abstract

A hybrid fermentation process for the production of; fermentation products is provided. This process includes combining a saccharide-rich slurry. This saccharide-rich slurry may include, but is not limited to starch, cellulose, hemi-cellulose, cellulobios, and may or may not contain, proteins, peptides, amino acids, lignin and to other biologically produced or environmental compounds. The process also includes a fermenting organism such as yeast, bacteria, archea, algae or other biocatalyst. The process also includes nutrients for the fermenting organism in a continuous fermentation step, thereby producing a partially fermented stream. The process also includes introducing the partially fermented product stream into a batch fermentation step, thereby producing a finished fermented beer stream.

IPC Classes  ?

• C12P 7/10 - Ethanol, i.e. non-beverage produced as by-product or from waste or cellulosic material substrate substrate containing cellulosic material
• C12P 19/14 - Preparation of compounds containing saccharide radicals produced by the action of a carbohydrase, e.g. by alpha-amylase

Abstract

In a process for deodorizing edible oil by means of a semicontinuous steam distillation plant, comprising a stripping column with a plurality of separating stages which can be closed off from one another, a degassing stage upstream of the stripping column, and a downstream vapor scrubber, a vacuum generation plant connected to the degassing stage, the separating stages and the vapor scrubber, one feed line for stripping steam opening into each of the degassing stage and the separating stage, indirect heat exchange surfaces each arranged in the separating stages of the upper and lower sections of the stripping column, and a vapor outlet line which is connected to the separating stages arranged in the upper and lower sections of the stripping column and opens into the vapor scrubber, a vacuum is generated in the distillation plant and fills the degassing stage with a batch of edible oil feed which passes through the degassing stage and the separating stages in succession and is treated at the same time with stripping steam, and the batch preheated in the degassing stage is heated in the separating stages of the upper section of the stripping column to 150 to 180°C, heated in the separating stages of the middle section to 230 to 260°C, and cooled in the separating stages of the lower section to 90 to 120°C, the vapors departing from the separating stages of the upper and lower sections are scrubbed with fatty acid in the vapor scrubber and condensed to give a mixed fatty acid distillate. In order to be able to obtain a fatty acid phase rich in sterols and tocopherols and a fatty acid phase low in sterols and tocopherols separately from one another, there is indirect heating at least of the batch present in the first separating stage in flow direction in the middle section of the stripping column, said batch having condensed out of the vapors departing from the separating stages of the middle section of the stripping column in indirectly cooled form and having been fractionated selectively into a fatty acid phase rich in sterols and tocopherols and a fatty acid phase low in sterols and tocopherols.

IPC Classes  ?

• B01D 3/10 - Vacuum distillation
• B01D 5/00 - Condensation of vapoursRecovering volatile solvents by condensation
• C11B 3/12 - Refining fats or fatty oils by distillation

Abstract

In the preparation of methanol by means of a catalytic process with a plurality of serial synthesis stages, in which the severity of the reaction conditions, measured on the basis of the reaction temperature and/or the concentration of carbon monoxide in the synthesis gas, decreases from the first to the last reaction stage in flow direction, the first reaction stage involving flow traversal of synthesis gas uses a first catalyst with low activity but high long-term stability, and the last reaction stage involving flow traversal by synthesis gas uses a second catalyst with high activity but low long-term stability.

IPC Classes  ?

• 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 29/154 - 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
• C07C 31/04 - Methanol
• 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

Abstract

The invention relates to a support arrangement for accessing a removable component lying in the interior of an apparatus or container, consisting of a first support which is connected to the inner component with a detachable connection and also consisting of a second support which is connected to the outer casing. The first support is led through the second support.

IPC Classes  ?

• B65D 90/48 - Arrangements of indicating or measuring devices

Abstract

This invention relates to the production of synthesis gas by partial oxidation of liquid or gaseous, carbonaceous fuel in the presence of an oxygen-containing oxidant, wherein the fuel, the oxidant and a moderator are separately supplied to a burner and wherein the fuel and the moderator are mixed in a mixing chamber of the burner, before they are brought in contact with the oxidant. To reduce the load of the burner in particular during operation with transient conditions, the oxidant is centrally introduced through an outlet opening of the burner into a combustion chamber and the mixture of fuel and moderator is introduced through the outlet opening into the combustion chamber concentrically around the oxidant.

IPC Classes  ?

• 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
• F23D 14/22 - Non-premix gas burners, i.e. in which gaseous fuel is mixed with combustion air on arrival at the combustion zone with separate air and gas feed ducts, e.g. with ducts running parallel or crossing each other
• F23D 14/32 - Burners for combustion of a gas, e.g. of a gas stored under pressure as a liquid using a mixture of gaseous fuel and pure oxygen or oxygen-enriched air

Abstract

For producing methanol from a synthesis gas containing hydrogen and carbon oxides the synthesis gas is passed through a first, preferably water-cooled reactor in which a part of the carbon oxides is catalytically converted to methanol, and the resulting mixture containing synthesis gas and methanol vapor is supplied to a second, preferably gas-cooled reactor in which a further part of the carbon oxides is converted to methanol. The mixture withdrawn from the first reactor is guided through a gas/gas heat exchanger in which the mixture is cooled to a temperature below its dew point. Subsequently, methanol is separated from the gas stream in a methanol separator and withdrawn, while the remaining gas stream is supplied to the second reactor.

IPC Classes  ?

• C07C 27/00 - Processes involving the simultaneous production of more than one class of oxygen-containing compounds

Abstract

For producing methanol from a synthesis gas containing hydrogen and carbon oxides the synthesis gas is passed through a first, water-cooled reactor in which a part of the carbon oxides is catalytically converted to methanol. The resulting mixture containing synthesis gas and methanol vapor is supplied to a second, gas-cooled reactor in which a further part of the carbon oxides is converted to methanol. Subsequently, methanol is separated from the synthesis gas, and synthesis gas is recirculated to the first reactor. The cooling gas flows through the second reactor cocurrent to the mixture withdrawn from the first reactor.

IPC Classes  ?

• C07C 27/00 - Processes involving the simultaneous production of more than one class of oxygen-containing compounds

Abstract

The invention relates to the production of synthesis gas by partially oxidizing liquid or gaseous fuel containing carbon in the presence of an oxidizing agent containing oxygen, wherein the fuel, the oxidizing agent, and a moderator are fed separately to a burner and wherein the fuel and the moderator are mixed in a mixing chamber of the burner before the fuel and the moderator are brought in contact with the oxidizing agent. In order to reduce the load of the burner, in particular during operation under transient conditions, the oxidizing agent is introduced into a combustion chamber centrally through an outlet opening of the burner, and the mixture of fuel and moderator is introduced into the combustion chamber concentrically around the oxidizing agent through the outlet opening.

IPC Classes  ?

• 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
• F23D 14/22 - Non-premix gas burners, i.e. in which gaseous fuel is mixed with combustion air on arrival at the combustion zone with separate air and gas feed ducts, e.g. with ducts running parallel or crossing each other
• F23D 14/32 - Burners for combustion of a gas, e.g. of a gas stored under pressure as a liquid using a mixture of gaseous fuel and pure oxygen or oxygen-enriched air

Abstract

A process for recovering solid reaction products during partial oxidation of hydrocarbons in a liquid solvent as a reaction medium by multi-stage evaporative crystallization includes determining a final temperature of the multi-stage evaporative crystallization based on a melting point of the solvent. The pressure and temperature of the solvent is reduced in steps via successive crystallization stages until the final temperature is reached. Each of the crystallization stages includes a compressor configured to perform the reducing of the pressure and to withdraw vapors formed. The vapors from the compressor of a lower expansion pressure crystallization stage are introduced into a vapor discharge conduit of a next successive higher expansion pressure crystallization stage upstream of the compressor of the higher expansion pressure crystallization stage.

IPC Classes  ?

• C07D 307/34 - Heterocyclic compounds containing five-membered rings having one oxygen atom as the only ring hetero atom not condensed with other rings having two or three double bonds between ring members or between ring members and non-ring members
• C07C 51/16 - Preparation of carboxylic acids or their salts, halides, or anhydrides by oxidation

Abstract

In a method for the steam reforming of a hydrocarbon-containing input material, part of the flue gas, after leaving the waste heat part of the reformer oven and before entering the flue gas disposal system, is branched off and led back to the reformer oven. By means of varying the proportion of flue gas fed back, the quantity of export steam discharged to external loads can be varied over a wide range. In this way, the quantity of export steam can be kept constant even during partial load operation of the reformer. Alternatively, during full load operation of the reformer, a reduction or further increase in the quantity of export steam is possible by means of an appropriate change in the flue gas mass flow fed back.

IPC Classes  ?

• 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

Abstract

The invention relates to a catalyst based on pentasil-type alumosilicates, in the form of spheres having an average diameter between 0.3 and 7 mm, wherein the BET surface area of the catalyst ranges from 300 to 600 m2/g, said catalyst comprising a binder. The invention further relates to a method for producing the catalyst of the invention, wherein primary crystallites having an average diameter of at least 0.01 μm and less than 0.1 μm are mixed with a binder and are shaped into spheres having an average diameter between 0.3 and 7 mm, and the catalyst is subsequently calcined. The invention further relates to the use of a catalyst of the invention for converting methanol into olefins, in particular propylene. The invention further relates to a method for producing olefins from methanol, in which the feed gas is fed across a catalyst of the invention.

IPC Classes  ?

• B01J 29/40 - Crystalline aluminosilicate zeolitesIsomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11
• 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
• B01J 35/08 - Spheres
• B01J 35/10 - Solids characterised by their surface properties or porosity
• B01J 35/02 - Solids

Abstract

In a method for producing dimethyl ether by means of the catalytic dehydration of methanol in the gaseous phase, crude methanol is used as charge material, wherein limit values are defined for the total content of carbonyl compounds in the crude methanol which ensure a stable long-term operation of the manufacturing plant. The method according to the invention is characterised by economic advantages, since at least one distillation stage for crude methanol work-up is saved, and the energy consumption of the method is reduced by avoiding the removal by distillation of large amounts of methanol in the form of low-boilers in the pure methanol column. A DME product is obtained, which despite the use of crude methanol is especially low in troublesome impurities. The invention also relates to a charge material and a plant for carrying out the method according to the invention.

IPC Classes  ?

• C07C 41/09 - Preparation of ethers by dehydration of compounds containing hydroxy groups
• C07C 43/04 - Saturated ethers

Abstract

The invention relates to a gas scrubber, equipped with heat exchanger surfaces constructed from thermal sheets, suitable for cooling and purifying a hot gas, while avoiding excessive thermal loading of the scrubbing liquid.

IPC Classes  ?

• B01D 53/18 - Absorbing unitsLiquid distributors therefor
• B01D 53/78 - Liquid phase processes with gas-liquid contact
• C07D 251/60 - Preparation of melamine from urea or from carbon dioxide and ammonia
• F28D 9/00 - Heat-exchange apparatus having stationary plate-like or laminated conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall
• F28F 3/00 - Plate-like or laminated elementsAssemblies of plate-like or laminated elements

Abstract

The invention relates to a method for continuously producing melamine from urea by means of a fluidized bed reactor, wherein process gas conducted in the process circuit is used as the fluidizing gas, and wherein the temperature of the process gas at the inlet of the conveying element for the fluidizing gas is adjusted by adjusting the mixture ratio of a process gas flow conducted through a scrubber and a process gas flow conducted past the scrubber.

IPC Classes  ?

• C07D 251/60 - Preparation of melamine from urea or from carbon dioxide and ammonia

Abstract

The invention relates to a method for processing readily saponifiable crude oil of plant or animal origin, in particular jatropha oil, which is suitable as a raw material for producing biodiesel by means of a transesterification process, wherein the crude oil is degummed by adding acid, is then partially neutralized by adding base, and the resulting sludge substances and soaps are separated by means of a mechanical separating process, and then the content of odorous substances and free fatty acids in the oil is reduced further by stripping or by applying a vacuum, wherein the degumming, the neutralization using a base, and the separation of the sludge substances are performed in a first temperature range and the stripping and/or the vacuum treatment are performed in a second temperature range, wherein the difference between the upper limit of the first temperature range and the lower limit of the second temperature range is at least 100 K, but no greater than 220 K.

IPC Classes  ?

• C11B 3/00 - Refining fats or fatty oils
• C11B 3/04 - Refining fats or fatty oils by chemical reaction with acids
• C11B 3/06 - Refining fats or fatty oils by chemical reaction with bases
• C11B 3/10 - Refining fats or fatty oils by adsorption
• C11B 3/14 - Refining fats or fatty oils by distillation with the use of indifferent gases or vapours, e.g. steam
• C11C 3/04 - Fats, oils or fatty acids obtained by chemical modification of fats, oils or fatty acids, e.g. by ozonolysis by esterification of fats or fatty oils

Abstract

The invention relates to a method for the continuous extraction of impurities, in particular saponification products, present in a fatty acid alkyl ester phase obtained by the transesterification of vegetable and animal oils or fats, having a high tendency to form saponification products by means of an aqueous, acidic glycerin phase containing a complexing agent.

IPC Classes  ?

• C11C 1/08 - Refining
• C11C 3/00 - Fats, oils or fatty acids obtained by chemical modification of fats, oils or fatty acids, e.g. by ozonolysis
• C10L 1/02 - Liquid carbonaceous fuels essentially based on components consisting of carbon, hydrogen, and oxygen only

Abstract

In the production of methanol from a synthesis gas containing hydrogen and carbon oxides, the synthesis gas is passed through a first, preferably water-cooled reactor, in which a part of the carbon oxides is catalytically converted to methanol. The obtained mixture containing synthesis gas and methanol vapor is supplied to a second, preferably gas-cooled reactor, in which a further part of the carbon oxides is converted to methanol. Subsequently, methanol is separated from the synthesis gas, and the synthesis gas is recirculated to the first reactor. To achieve a maximum methanol yield even with an aged catalyst, a partial stream of the synthesis gas is guided past the first reactor and introduced directly into the second reactor.

IPC Classes  ?

• 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
• 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

Abstract

Method for producing fatty alcohols includes splitting vegetable oils and animal fats under pressure into fatty acids and glycerol in counterflow to steam. The reaction product is physically separated into fatty acids and sweet water containing glycerol. The fatty acids are subjected to a distillation, and the separated fatty acid fraction is mixed together with fatty alcohol at 230 to 270° C. and atmospheric pressure. The wax esters obtained by esterification are hydrogenated to fatty alcohols by adding hydrogen on a fixed-bed catalyst, and the reaction product is separated into fatty alcohols and hydrogen. The wax esters are hydrogenated on a fixed bed of uniformly shaped catalyst bodies produced by extrusion, which consist of the main components copper and copper-chromium oxide and the secondary components zinc, aluminum, iron, silicon and alkaline earth elements, at 180 to 220° C. and 70 to 100 bar(a).

IPC Classes  ?

• C07C 29/88 - SeparationPurificationStabilisationUse of additives by treatment giving rise to a chemical modification of at least one compound

Abstract

The invention relates to a method for continuously producing a mixture of phthalic acid and phthalic anhydride dissolved in an aliphatic monocarboxylic acid, preferably in acetic acid, by means of oxidation of o-xylene dissolved in the monocarboxylic acid by means of atmospheric oxygen, the oxidation being performed in the presence of a catalyst, characterized by several reaction stages, the molar ratio of o-Xylene to the intermediate products composed of 2-methylbenzaldehyde, 2-methylbenzoic acid, and phthalide being less than 1:40 in the product flow (7) fed to the last reaction stage.

IPC Classes  ?

• C07C 51/265 - Preparation of carboxylic acids or their salts, halides, or anhydrides by oxidation with molecular oxygen of compounds containing six-membered aromatic rings without ring-splitting having alkyl side chains which are oxidised to carboxyl groups
• C07C 51/56 - Preparation of carboxylic acid anhydrides from organic acids, their salts, or their esters
• C07C 63/16 - 1,2-Benzenedicarboxylic acid
• C07D 307/89 - Benzo [c] furansHydrogenated benzo [c] furans with two oxygen atoms directly attached in positions 1 and 3

Abstract

In order to produce methanol from synthesis gas having a high concentration of inerts, a catalytic secondary reactor is mounted downstream of the single-stage or multistage synthesis cycle. In said secondary reactor, some more of the synthesis gas is converted into methanol such that the method can be carried out at a lower ratio between the circulating stream and the make-up gas stream than when no secondary reactor is used. Unlike prior art methods, the method of the invention is characterized by the absence of materials that are foreign to the process or have to be disposed of or regenerated, such as absorbents. Other advantages include the low complexity and reduced size of the devices, reduced pipe size, and low energy consumption, e.g. for the required compressor power.

IPC Classes  ?

• 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
• C07C 31/04 - Methanol
• 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

Abstract

In order to produce synthetic fuels, in a first phase, an educt mixture containing water vapor and an oxygenate, like methanol and/or dimethylether, is converted to olefins using a catalyst. Subsequently, the olefin mixture is then separated in a separator system into a flow that is rich in C1-C4 carbon hydrates, and a flow that is rich in C5+ carbon hydrates. The flow that is rich in C5+ carbon hydrates is separated into a flow that is rich in C5 and C6 carbon hydrates, and a flow that is rich in C7+ carbon hydrates, wherein the flow that is rich in C5 and C6 carbon hydrates is at least partially subjected to an etherification with methanol. The ethers thus produced are added to the gasoline product flow.

IPC Classes  ?

• 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
• C10L 1/02 - Liquid carbonaceous fuels essentially based on components consisting of carbon, hydrogen, and oxygen only
• C07C 41/01 - Preparation of ethers
• C10G 29/22 - Organic compounds not containing metal atoms containing oxygen as the only hetero atom

Abstract

2 guided in counterflow.

IPC Classes  ?

• 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

Abstract

In the production of purified methanol and/or dimethyl ether from raw methanol, the raw methanol is purified in at least one preliminary purification stage, a first partial flow of the preliminarily purified methanol is fed to a final methanol purification, and a second partial flow of the preliminarily purified methanol is fed to a reactor and at least partially converted into dimethyl ether. The dimethyl ether obtained is purified in at least one purification stage, wherein unconverted methanol is removed from the dimethyl ether purification stage and is fed at least partially to the final methanol purification. Both purified methanol and dimethyl ether can hereby be produced in parallel, wherein the amounts of both products produced can be flexibly adjusted.

IPC Classes  ?

• C07C 29/80 - SeparationPurificationStabilisationUse of additives by physical treatment by distillation
• C07C 41/09 - Preparation of ethers by dehydration of compounds containing hydroxy groups
• C07C 41/42 - SeparationPurificationStabilisationUse of additives by change of physical state, e.g. by crystallisation by distillation
• C07C 31/04 - Methanol
• C07C 43/04 - Saturated ethers
• B01D 3/14 - Fractional distillation

Abstract

3 to provide a dispersion which is separated by density difference. A phase containing at least one of raw FAME and raw FAEE is mixed with an aqueous acid, washed with water, with the water being expelled to provide FAME and FAEE product.

IPC Classes  ?

• C11C 3/00 - Fats, oils or fatty acids obtained by chemical modification of fats, oils or fatty acids, e.g. by ozonolysis

Abstract

In a method for gasifying baking hard coal by way of a pressurized gasifier, the hard coal is introduced into a shaft-shaped gas generator and travels downward in the same in the form of a fluidized bed in the countercurrent to a gasifying agent introduced from beneath into the fluidized bed, wherein the hard coal is successively dried, carbonized, gasified, and burnt, and the majority of the obtained product gas is conducted out of the gas generator by way of an upwardly closed annular space formed by a pipe section attached in the upper section of the gas generator and the inner side of the gas generator located opposite of said pipe section, and the residual quantity of the product gas is suctioned through the segment of the fluidized bed located in the pipe section, conducted to the outside, and recirculated into the annular space. In order to improve the gas generator output, the invention proposes that the segment of the fluidized bed located in the pipe section be heated by the residual quantity of the product gas suctioned through to a temperature of 260 to 380ºC and loosened mechanically in the process, and that the ash particles contained in the residual quantity of the product gas exiting the fluidized bed toward the top and the fine grain portion of the added hard coal entrained by the product gas be separated and added to the segment of the fluidized bed located in the pipe section.

IPC Classes  ?

• C10J 3/84 - Gas withdrawal means with means for removing dust or tar from the gas
• C10J 3/78 - High-pressure apparatus
• C10J 3/48 - ApparatusPlants
• C10J 3/76 - Water jacketsSteam boiler jackets
• C10J 3/46 - Gasification of granular or pulverulent fuels in suspension
• C10J 3/52 - Ash-removing devices

Abstract

When producing hydrocarbons from fatty acid esters contained in fats or fat oils, the fatty acid esters initially are split up by hydrolytic decomposition into a first stream containing crude alcohol and water and a second stream containing free fatty acids, and subsequently the free fatty acids of the second stream are hydrogenated with hydrogen to obtain saturated hydrocarbons.

IPC Classes  ?

• C07C 1/213 - 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 from carbonyl compounds by splitting of esters

Abstract

In a method for producing process gas containing hydrogen sulfide and sulfur dioxide for the Claus process, feed gas containing hydrogen sulfide is burned with pure oxygen using a plurality of burners leading into a combustion chamber, wherein the pure oxygen is introduced into the combustion chamber by way of a central pipe, the feed gas is introduced by way of a pipe coaxially surrounding the central pipe, and inert gas is introduced as rinsing gas by way of a ring channel coaxially surrounding the feed gas pipe. Advantageously, the CO2 obtained from the desorption of loaded methanol can be used as the inert gas.

IPC Classes  ?

• C01B 17/04 - Preparation of sulfurPurification from gaseous sulfur compounds including gaseous sulfides
• F23D 14/22 - Non-premix gas burners, i.e. in which gaseous fuel is mixed with combustion air on arrival at the combustion zone with separate air and gas feed ducts, e.g. with ducts running parallel or crossing each other
• F23D 14/38 - Torches, e.g. for brazing or heating

Abstract

The invention relates to a method for the continuous production of pure glycerin from raw glycerin containing potassium sulphate from the transesterfication of native fats or oils. Said method consists of saponifying the organic impurities, evaporating the water, separating the potassium sulphate by crystallisation and controlling the size of the crystals such that after the subsequent rectification treatment of the raw glycerin, the potassium sulphate crystals can be extracted from the base product of the rectification column by means of a solid bowl screw centrifuge as long as the base product can be eliminated as a combustion material.

IPC Classes  ?

• C07C 29/80 - SeparationPurificationStabilisationUse of additives by physical treatment by distillation
• C07C 31/22 - Trihydroxylic alcohols, e.g. glycerol
• C11D 19/00 - Recovery of glycerol from a saponification liquor
• C07C 29/76 - SeparationPurificationStabilisationUse of additives by physical treatment

Abstract

The invention relates to a method for continuously treating a solution containing salt, running into a forced flow evaporator, in which the lower boiling liquid compounds are evaporated, the salt is separated by crystallisation whilst controlling the size of the crystals and evacuated, and the treated solution is separated from the circulating suspension by means of a separator which is installed into the circulation line, the crystals are restrained and the solution is then guided for further treatment.

IPC Classes  ?

• B01D 9/00 - Crystallisation

Abstract

The invention relates to a method for producing a product containing C3H6 and C2H4, in which MeOH and EtOH are reacted simultaneously in a reactor, which is equipped with reaction stages having a shape-selective catalyst, at temperatures ranging from 300 to 600 °C and pressures from 0.1 to 20 bar[a]. In order to improve temperature control, EtOH is fed into at least one of the reaction stages.

IPC Classes  ?

• 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 11/04 - Ethene
• C07C 11/06 - Propene

Abstract

In a method for producing dimethyl ether (DME) from methanol (MeOH) by converting raw MeOH obtained through MeOH synthesis to DME in a reactor, separating water in the process, the raw MeOH and a process-internally obtained return flow formed from unused MeOH and reaction water are evaporated together and the vaporous MeOH is fed to a reactor. In order to obtain as low a consumption of operating resources as possible and to improve the installed heat transfer capacity, according to the invention the reaction mixture taken out of the reactor is separated into a bottom product comprised substantially of water and a distillate comprised substantially of DME and MeOH and uncondensable gases, and the distillate is separated into a distillate comprised substantially of DME and uncondensable gases released overhead and into a low-water MeOH formed bottom product.

IPC Classes  ?

• C07C 41/09 - Preparation of ethers by dehydration of compounds containing hydroxy groups
• C07C 43/04 - Saturated ethers
• B01D 3/14 - Fractional distillation

Abstract

The invention relates to a method and plant for obtaining ammonia from an acidic gas mixture comprising ammonia, H2S and/or CO2 and low boiling water soluble organic components. In order to avoid an enrichment of volatile organic compounds in the acidic gas absorber, a partial stream of the liquid phase from an acidic gas absorber is extracted and worked up such that gaseous ammonia with a reduced content of volatile organic compounds is obtained which is recycled to the acidic gas absorber.

IPC Classes  ?

• C01C 1/02 - Preparation or separation of ammonia
• C01C 1/10 - Separation of ammonia from ammonia liquors, e.g. gas liquors
• C01C 1/12 - Separation of ammonia from gases and vapours
• B01D 19/00 - Degasification of liquids
• C01B 17/16 - Hydrogen sulfides
• 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

Abstract

2S separated is introduced into the feed gas of the Claus process, and the waste gas of the tail gas wash, mixed with the tail gas of the Claus process, is burnt.

IPC Classes  ?

• C01B 3/02 - Production of hydrogen or of gaseous mixtures containing hydrogen
• C01B 3/24 - Production of hydrogen or of gaseous mixtures containing hydrogen by decomposition of gaseous or liquid organic compounds of hydrocarbons
• C01B 17/04 - Preparation of sulfurPurification from gaseous sulfur compounds including gaseous sulfides

Abstract

In a process for producing fatty acid methyl ester (FAME) from fats or oils by transesterification with methanol in the presence of an alkaline catalyst in at least two reaction stages traversed in succession, each consisting of a stirred-tank reactor and a downstream separator, a phase containing FAME and a phase containing glycerol are generated, which are separated in the separator, wherein the phase containing FAME is recirculated into the stirred-tank reactor of the next succeeding reaction stage and the phase containing glycerol is recirculated into the stirred-tank reactor of the first reaction stage, and the crude FAME withdrawn from the separator of the last reaction stage is transferred into a separator and the FAME withdrawn is dried. To increase the yield of FAME, the aqueous phase containing glycerol, methanol, undissociated soaps and FAME, which is obtained upon withdrawal of the FAME, is thoroughly mixed with the phases withdrawn from the separators of the first to penultimate reaction stages, which contain glycerol and FAME, and the mixture is separated in a separator into a phase containing FAME and a phase containing glycerol.

IPC Classes  ?

• C11C 3/00 - Fats, oils or fatty acids obtained by chemical modification of fats, oils or fatty acids, e.g. by ozonolysis

Abstract

When producing biodiesel from fats, oils, or split fatty acids rich in steryl glycosides, the light phase obtained from transesterification or esterification and rich in fatty acid alkyl esters is washed in a washing column, wherein the suspension layer that forms is treated by stirring. The steryl glycosides are thereby disposed of in the light phase of the wash. In a subsequent treatment of the light washer phase in an intensive mixer with water, compact steryl glycoside/fatty acid alkyl ester/water agglomerates are obtained that can be easily precipitated by means of centrifugation. After further preparation by drying and/or filtration, biodiesel complying with specifications is obtained from the light phase of centrifugation. The method is suitable for processing fats, oils, or split fatty acids having a high steryl glycoside content, and avoids the use of additives external to the process. The method is characterized by simple apparatus and low energy consumption.

IPC Classes  ?

• C11C 1/08 - Refining
• C11C 3/00 - Fats, oils or fatty acids obtained by chemical modification of fats, oils or fatty acids, e.g. by ozonolysis

Abstract

In order to produce methanol from a syngas containing hydrogen and carbon oxides, the syngas is conducted through a first, water-cooled reactor in which some of the carbon oxides are catalytically reacted to obtain methanol. The obtained mixture containing syngas and methanol vapor is fed to a second, gas-cooled reactor in which some more of the carbon oxides are reacted to obtain methanol. Methanol is then separated from the syngas, and syngas is recirculated to the first reactor. The cooling gas flows through the second reactor as a parallel flow to the mixture withdrawn from the first reactor.

IPC Classes  ?

• 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
• C07C 31/04 - Methanol
• 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

Abstract

In order to produce methanol from a syngas containing hydrogen and carbon oxides, the syngas is conducted through a first, preferably water-cooled reactor in which some of the carbon oxides are catalytically reacted to obtain methanol, and the obtained mixture containing syngas and methanol vapor is fed to a second, preferably gas-cooled reactor in which some more of the carbon oxides are reacted to obtain methanol. The mixture withdrawn from the first reactor is conducted through a gas/gas heat exchanger, in which the mixture is cooled to a temperature lying below the dew point of the mixture. Methanol is then separated from the gas stream and withdrawn in a methanol separator, while the remaining gas stream is fed to the second reactor.

IPC Classes  ?

• 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 31/04 - Methanol
• 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
• B01D 5/00 - Condensation of vapoursRecovering volatile solvents by condensation

Abstract

2 to the supercritical state.

IPC Classes  ?

• C01B 3/24 - Production of hydrogen or of gaseous mixtures containing hydrogen by decomposition of gaseous or liquid organic compounds of 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

Abstract

The invention relates to a method for obtaining solid reaction products by partially oxidizing hydrocarbons in liquid solvents, wherein pressure and temperature are lowered incrementally in sequential crystallization stages each equipped with a compressor, wherein the vapors from a compressor of a crystallization stage having lower expansion pressure are fed into the vapor extraction line of the expansion stage having the next highest expansion pressure ahead of the compressor thereof.

IPC Classes  ?

• C07C 51/43 - SeparationPurificationStabilisationUse of additives by change of the physical state, e.g. crystallisation
• C07C 63/16 - 1,2-Benzenedicarboxylic acid
• C07C 63/15 - Monocyclic dicarboxylic acids all carboxyl groups bound to carbon atoms of the six-membered aromatic ring
• C07C 63/04 - Monocyclic monocarboxylic acids
• C07C 51/265 - Preparation of carboxylic acids or their salts, halides, or anhydrides by oxidation with molecular oxygen of compounds containing six-membered aromatic rings without ring-splitting having alkyl side chains which are oxidised to carboxyl groups
• B01D 9/00 - Crystallisation

Abstract

2O and DME and/or MEOH, using a water-saturated gas phase containing mainly DME and/or MEOH, in the direction of the following reaction stage downstream.

IPC Classes  ?

• 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

Abstract

The invention relates to producing melamine from urea, by catalytically converting the urea at least partially to melamine in a fluidized bed reactor at 350 to 450°C, feeding the gas mixture arising in the reactor, optionally after filtering in a gas filter, into a crystallizer, in which the melamine crystallizes at a reduced temperature, separating and drawing off the melamine from the process gas in a separator, and then recirculating the process gas, and fed into the fluidized-bed reactor as a fluidizing gas after washing in a urea washer, precipitating droplets, and compressing. According to the invention, the process gas is pre-warmed after precipitating the fluid droplets and after entry into the compressor.

IPC Classes  ?

• C07D 251/60 - Preparation of melamine from urea or from carbon dioxide and ammonia

Abstract

The invention relates to a method for recovering working fluid, in particular from a leakage gas flow occurring when heat is being recovered from the working fluid, the flow containing low-boiling liquid and/or gaseous components of the working fluid. The invention also relates to a plant for carrying out said method. According to the invention, in order to recover the working fluid, a liquefied gas is evaporated as refrigerant and the leakage gas flow is guided first through a pre-condenser (4) in counter-flow to the refrigerant at higher temperature and then through a main condenser (3) at lower temperature in order to condense the working fluid out of the leakage gas flow.

IPC Classes  ?

• F01K 25/10 - Plants or engines characterised by use of special working fluids, not otherwise provided forPlants operating in closed cycles and not otherwise provided for using special vapours the vapours being cold, e.g. ammonia, carbon dioxide, ether

Goods & Services

(1) Chemicals used in industry and science, namely olefinic, paraffinic, aromatic hydrocarbons, namely benzene, toluene, xylene, methanol, polymeric materials, namely polyolefins, polypropylene, polyethylene, hydrocarbon gases for use in chemical syntheses, namely methane, ethane, ethylene, propane, propylene, butanes, butenes; unprocessed artificial resins; unprocessed plastics; manures; technical gas for industrial purposes, namely, gases for power generation and for the production of synthesis gas and nitrogen, oxygen, hydrogen, carbon monoxide, synthesis gas, and mixtures thereof; liquid gas; alcohols, namely short-chain alcohols from natural gas, coal, crude oil carrier gas, carbonaceous slurry and biomass; methanol from natural gas, crude oil carrier gas, carbonaceous slurry, coal and biomass; dimethylether, propylene, ethylene, butenes, saturated hydrocarbons; engine fuel, fuel for motor vehicles namely gasoline from short-chain alcohols; motor spirits; methanol (as fuel) from natural gas, crude oil carrier gas, carbonaceous slurry, coal and biomass; otto gasolines from methanol; thermoplastic resins namely polypropylene; apparatuses, devices (machines) and machine installations for the production of short-chain alcohols from natural gas, crude oil carrier gas, carbonaceous slurry, coal and biomass by means of thermal and catalytic processes, namely for the production of methanol from natural gas, crude oil carrier gas, coal, carbonaceous slurry and biomass; industrial machinery for the production of propylene from methanol, by means of thermal and catalytic processes; machines for the chemical industry for the production of short-chain alcohols from natural gas, crude oil carrier gas, carbonaceous slurry, coal and biomass, namely for the production of methanol and for the production of propylene from methanol; industrial machinery comprised of lighting, heating, steam generating, boiling, cooling, drying, ventilating and water pipe devices as additional devices of and for later installation into, respectively, machines for the chemical industry for the production of short-chain alcohols from natural gas, crude oil carrier gas, carbonaceous slurry, coal and biomass, namely for the production of methanol and for the production of propylene from methanol; parts of the above-mentioned goods.

Abstract

In a method for the production of fatty alcohols, vegetable oils and animal fats are cleaved into fatty acids and glycerin in counter flow to pressurized steam, the reaction product is physically cleaved into a phase containing fatty acids and sugar water containing glycerin, the fatty acids are subjected to distillation, the cleaved fatty acid fraction is intensively mixed together with fatty alcohol at 230 to 270°C and atmospheric pressure, the wax esters obtained by means of ester formation are hydrated into fatty alcohols in a fixed-bed catalyst while adding hydrogen, and the reaction product is cleaved into fatty alcohols and hydrogen. In order to simplify hydrating the wax esters, the invention provides to hydrate the wax esters in a fixed bed comprising uniform catalyst molded bodies produced by means of extrusion, which comprise the main components copper and copper chromium oxide, and the secondary components zinc, aluminum, iron, silicon, and earth alkali elements at 180 to 220°C and 70 to 100 bars[a].

IPC Classes  ?

• C07C 31/125 - Monohydroxylic acyclic alcohols containing five to twenty-two carbon atoms
• C07C 29/149 - 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 an oxygen-containing functional group of C=O containing groups, e.g. —COOH of carboxylic acids or derivatives thereof with hydrogen or hydrogen-containing gases

Abstract

The invention relates to a method for producing sulfur from an input gas comprising H2S, wherein a part of the H2S is burned in the presence of O2 and/or air to form SO2 and H2O, and the SO2 is reduced to sulfur and H2O using at least one catalyst and further H2S. In order to be able to control the temperatures in the combustion chamber, feedwater is sprayed into the process gas present in the combustion chamber.

IPC Classes  ?

• C01B 17/04 - Preparation of sulfurPurification from gaseous sulfur compounds including gaseous sulfides

Abstract

The invention relates to the production of hydrocarbons from fatty acid esters present in fats or fatty oils, wherein the fatty acid esters are first split by hydrolytic splitting into a first stream comprising raw alcohol and water and a second stream comprising free fatty acids. The free fatty acids of the second stream are then hydrogenated with hydrogen into saturated hydrocarbons.

IPC Classes  ?

• C11C 1/04 - Preparation of fatty acids from fats, fatty oils, or waxesRefining the fatty acids from fats or fatty oils by hydrolysis
• C10G 3/00 - Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
• C10L 1/04 - Liquid carbonaceous fuels essentially based on blends of hydrocarbons

Abstract

The invention relates to a method for treating a process gas flow containing CO2 that is produced whilst producing pure synthesis gas from the crude gas of the process gas flow or during the partial oxidation of heavy olis, petroleum cokes and waste substances or during coal gasification or during the treatment of natural gas or gas which accompanies petroleum, from which CO2 is removed by physisorption or chemisorption and the solvent charged with CO2 is released at a low pressure for the desorption of the CO2. In order to produce CO2 as pure as possible, the unpurified CO2 is compressed at least at 60 bar[a] or below the critical temperature thereof to at least 70 bar[a] and the impurities contained in the liquid CO2 are removed by stripping with gaseous CO2 guided into the counter flow.

IPC Classes  ?

• 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

Abstract

The invention relates to a method for producing fatty acid methyl esters (FAME) or ethyl esters (FAEE) and C3H5(OH)3 from vegetable oils or animal fats in which the triglycerides contained in said oils or fats are transesterified in a base catalytic fashion with CH3OH and/or C2H5OH in the mixers of a plurality of connected mixer-settler stages and the mixtures thus produced are separated in the settlers disposed downstream of the respective mixers into a fatty acid ester (FAE) and a phase containing C3H5(OH)3. The phase containing FAE removed from the settler of the first mixer-settler stage is sent to the mixer of the subsequent mixer-settler stage, where aqueous acid is added thereto and said phase is washed with water in a counterflow. The water contained in the raw FAE thus obtained is removed and the prepared FAE is sent to further processing. The phase containing C3H5(OH)3 obtained from the settler of the second mixer-settler stage is returned to the mixer of the first mixer-settler stage and the phase containing C3H5(OH)3 removed from the settler of the first mixer-settler stage is combined with the phase containing aqueous CH3OH and/or C2H5OH, C3H5(OH)3 and salts obtained upon washing the FAE and the mixture is thermally separated into a phase containing CH3OH and/or C2H5OH, C3H5(OH)3 and an aqueous phase containing C3H5(OH)3 and salts. In order to reduce the concentration of dissolved soaps in the dissolved C3H5(OH)3, a soap-free C2H5(OH)3 is dispersed into the FAE removed from the settler of the last mixer-settler stage and the dispersion is separated into a phase comprising raw FAE and a phase loaded with C3H5(OH)5CH3OH and/or C2H5OH, dissolved soaps, and catalysts.

IPC Classes  ?

• C11C 3/00 - Fats, oils or fatty acids obtained by chemical modification of fats, oils or fatty acids, e.g. by ozonolysis
• C10L 1/02 - Liquid carbonaceous fuels essentially based on components consisting of carbon, hydrogen, and oxygen only

Abstract

5+ gasoline hydrocarbons is supplied to a second separating device, in which the aromatics contained in the mixture are separated. The residual stream largely free from aromatics is at least partly recirculated to the reactor.

IPC Classes  ?

• C07C 1/00 - Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon
• B01D 3/14 - Fractional distillation
• 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

Abstract

When producing synthesis gas from a starting material containing hydrocarbons, in particular natural gas, a feed stream of the starting material is divided into a first partial stream and a second partial stream. The first partial stream is supplied to a steam reformer (4), in which together with steam it is catalytically converted to a gas stream containing carbon oxides. Then, the first partial stream is again combined with the second partial stream and the combined gas stream is supplied to an autothermal reformer (7), in which together with gas rich in oxygen it is autothermally reformed to a synthesis gas in the presence of a cracking catalyst. Processing a starting material with a high content of higher hydrocarbons is made possible in that before the steam reformer (4) and before the autothermal reformer (7) the entire starting material is supplied to a pre-reformer (2) in which the starting material largely is liberated from higher hydrocarbons.

IPC Classes  ?

• C01B 3/24 - Production of hydrogen or of gaseous mixtures containing hydrogen by decomposition of gaseous or liquid organic compounds of 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

Abstract

During the production of hydrocarbons, especially C2-C4 olefins, by means of a combined installation (1) comprising a steam cracker (2) and at least one reactor (3) for reacting a feedstock mixture containing steam and at least one oxygenate, the respective intermediate flows of the steam cracker (4) and the reactor (5) are combined at least in part. In order to increase the yield of valuable products, a shape-selective zeolite material is used as a catalyst for reacting the oxygenate in the reactor (3), and at least part of the product flows obtained after penetrating the combined installation are recirculated to the steam cracker (2) and/or the reactor (3).

IPC Classes  ?

• C10G 11/04 - Oxides
• C07C 11/02 - Alkenes

Abstract

In the production of methanol from hydrogen and from synthesis gas containing carbon dioxides, the synthesis gas is guided through a first, preferably water-cooled reactor, in which part of the carbon dioxides is catalytically converted into methanol. The resulting mixture containing synthesis gas and methanol vapor is supplied to a second, preferably gas-cooled reactor, in which a further part of the carbon dioxides is converted into methanol. Subsequently methanol is separated from the synthesis gas, and the synthesis gas is returned to the first reactor. In order to achieve maximum methanol yield, even with the aging of the catalyst, a partial flow of the synthesis gas is guided past the first reactor and guided directly into the second reactor.

IPC Classes  ?

• 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 8/04 - 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

Abstract

The invention relates to a method for producing synthetic fuels from a reactant mixture containing hydrogen and oxygenate, such as methanol and/or dimethylether, wherein in a first process step the reactant mixture is converted, using a catalyst, into a hydrocarbon product comprising olefins having preferably 2 to 8 carbon atoms, and in a second process step the resulting hydrocarbon product is oligomerized into long-chain olefins from which gasoline and diesel products are obtained. In order to increase the quality of the products, according to the invention the hydrocarbon product obtained in the first process step is separated into a liquid and a gaseous phase before being introduced to the second process step, the gaseous phase of the hydrocarbon product is fed into the second process step, the liquid phase of the hydrocarbon product is separated in a second separating device into a mixture rich in C6-hydrocarbons and a mixture comprising C7+-hydrocarbon and aromatics, and the C6-hydrocarbon-rich mixture is fed into the second process step. The mixture comprising C7+-hydrocarbons and aromatics can be added to the gasoline product to improve quality.

IPC Classes  ?

• C10G 3/00 - Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
• C10G 50/00 - Production of liquid hydrocarbon mixtures from lower carbon number hydrocarbons, e.g. by oligomerisation
• C10L 1/08 - Liquid carbonaceous fuels essentially based on blends of hydrocarbons for compression ignition
• 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

Abstract

In a gas scrubber (10), a gas stream (27) containing at least one sublimated substance is brought into contact with a liquid or melt stream which contains at least one thermally convertible substance (8) and has a lower temperature than the gas stream. For intensive and intimate mixing of the gas stream with the liquid stream or melt stream, in the upper part of the gas scrubber (10) there is provided a perforated plate (38) having a plurality of holes (39) each surrounded by a throttling rim (40) and above the perforated plate feeds are provided for the gas stream (27) and the liquid or melt stream (8).

IPC Classes  ?

• B01D 53/18 - Absorbing unitsLiquid distributors therefor
• B01J 19/00 - Chemical, physical or physico-chemical processes in generalTheir relevant apparatus
• C07D 251/60 - Preparation of melamine from urea or from carbon dioxide and ammonia
• C07D 251/62 - Purification of melamine

Abstract

A process is described for utilization of the oxidation offgases which are obtained in the oxidative preparation of terephthalic acid from p-xylene, in which these offgases are first returned completely to standard pressure, then cleaned oxidatively and washed, and a substream of these cleaned offgases, before removal through the chimney, is branched off, compressed and dried, and then used for the pneumatic delivery of terephthalic acid.

IPC Classes  ?

• C07C 51/42 - SeparationPurificationStabilisationUse of additives
• B01D 53/68 - Halogens or halogen compounds
• F23G 7/07 - Methods or apparatus, e.g. incinerators, specially adapted for combustion of specific waste or low grade fuels, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases in which combustion takes place in the presence of catalytic material
• C07C 63/26 - 1,4-Benzenedicarboxylic acid
• C07C 51/265 - Preparation of carboxylic acids or their salts, halides, or anhydrides by oxidation with molecular oxygen of compounds containing six-membered aromatic rings without ring-splitting having alkyl side chains which are oxidised to carboxyl groups

Abstract

In the production of raw terephthalic acid, paraxylene, oxygen, and acetic acid charged with a catalyst are added to a reactor (1), wherein the paraxylene reacts in the reactor (1) under pressure and at an elevated temperature into a raw terephthalic acid, which is drawn from the reactor (1) and is discharged into a rotary pressure filter (9), in which it is separated from the solvent under pressure and purified of contamination and catalyst material.

IPC Classes  ?

• C07C 51/265 - Preparation of carboxylic acids or their salts, halides, or anhydrides by oxidation with molecular oxygen of compounds containing six-membered aromatic rings without ring-splitting having alkyl side chains which are oxidised to carboxyl groups
• B01D 33/09 - Filters with filtering elements which move during the filtering operation with rotary cylindrical filtering surfaces, e.g. hollow drums arranged for inward flow filtration with surface cells independently connected to pressure distributors
• C07C 63/26 - 1,4-Benzenedicarboxylic acid

Abstract

According to the invention, synthesis gas is produced from a starting material, particularly natural gas, which contains hydrocarbons, by dividing a feed flow of the starting material into a first partial flow and a second partial flow. The first partial flow is fed to a steam reformer (4) in which said partial flow, along with steam, is catalytically converted into a gas flow containing carbon oxides. The first partial flow is then recombined with the second partial flow, and the combined gas flow is fed to an autothermal reformer (7) in which the gas flow is autothermally reformed to a synthesis gas along with oxygen-rich gas in the presence of a cracking catalyst. In order to be able to process a starting material that has a high concentration of higher hydrocarbons, the entire starting material is fed to a pre-reformer (2) upstream of the steam reformer (4) and upstream of the autothermal reformer (7), higher hydrocarbons being largely eliminated from the starting material in said pre-reformer (2).

IPC Classes  ?

• 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

Abstract

The invention relates to producing C2-C4-olefins, in particular propylene, from an educt mixture containing water vapour and methanol and/or dimethyl ether, wherein the inventive method consists in transforming the educt mixture on a catalyst in a reactor into a reaction mixture containing low-molecular olefins and gasoline hydrocarbons, in separating said mixture in a first separation device into an olefin C5-rich mixture, a C5+- gasoline hydrocarbon-rich mixture and into a gaseous phase. In order to increase a propylene yield, the C5+- gasoline hydrocarbon-rich mixture is directed to a second separation device, wherein aromatics contained in the mixture are separated, and residue flow which is substantially aromatic-free is redirected at least partially to the reactor.

IPC Classes  ?

• 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 11/06 - Propene
• B01D 3/14 - Fractional distillation

Goods & Services

(1) Articles of metals and their alloys, namely bearing metals; plant parts of base metals, namely pipes, valves, dampers, slides, taps, pistons, piston rods, stop sockets, plugs, cross-heads, thrust rods, shafts, rollers, eccentrics, couplings, bases, conduits, frames, cylinders, wheels, scoops, drums, discs; tank containers and bunkers for storing chemicals; comminuting and milling tools; pulverizing tools; vessels for dissolving chemicals; agglomeration apparatuses; presses, compressors, condensers, technical sieves; technical filters for gaseous and liquid materials; dialysis apparatuses as well as apparatuses for the separation of emulsions by electrophoresis; centrifuges; wind sifting, sink separating and degasifying apparatuses; electrolysers; crystallization, desiccation absorption and adsorption apparatuses; mixing, kneading, emulsifying and gasifying apparatuses; furnaces; whirling bunkers and reactors for chemical and physical treatments including travelling grates, and sintering bands; tools for metal casting; cooking; disintegration and vapourization vessels; machines, apparatuses and tools for gasification and carbonization, for distillation and rectification, as well as for gas liquefaction; apparatuses for obtaining chemical catalysis; coolers; waste-heat boilers; heat exchangers, blowers, pumps, compressors, vacuum apparatuses; all the foregoing articles including their parts for the chemical industry; comminuting and milling tools, pulverizing tools, heat exchangers as well as presses for the food appetizer industry; chemical apparatuses and tools for the production, preparation, treatment, decomposition and purification of fuels, propulsion materials, fatty acids, pharmaceutical products, foods and appetizers, active carbon, cellulose, metals, metal alloys, chemical products, ceramic materials, building materials, fertilizers, spray guns for metals, synthetic materials, ceramic pastes; columns, dosing tools as well as apparatuses for annealing and degasifying and purifying waters and waste waters.