Split Flow Contactor

Systems and methods for contacting a liquid, gas, and/or a multi-phase mixture with particulate solids. The system can include a body having a first head and a second head disposed thereon. Two or more discrete fixed beds can be disposed across a cross-section of the body. One or more unobstructed fluid flow paths can bypass each fixed bed, and one or more baffles can be disposed between the fixed beds.

Vessel For Containing Catalyst In A Tubular Reactor

A catalyst carrier for insertion in a radial tube reactor, said catalyst carrier comprising: an annular container for holding catalyst in use, said container having a perforated inner wall defining a tube, a perforated outer wall, a top surface closing the annular container and a bottom surface closing the annular container; a surface closing the bottom of said tube formed by the inner wall of the annular container; a skirt extending upwardly from the perforated outer wall of the annular container from a position at or near the bottom surface of said container to a position below the location of a seal; and a seal located at or near the top surface and extending from the container by a distance which extends beyond an outer surface of the skirt.

Process for Selective Removal of a Product from a Gaseous System

A process for selective removal of a gaseous product (P) from a gaseous system comprising said product and other components (R 1 , R 2 ), wherein the gaseous system is admitted to a first environment, which is separated from a second environment by a boundary wall, and a permeation membrane ( 3, 300 ) forms at least part of said boundary wall; a spatially non-uniform electric field ( 4 ) is generated between a first electrode or first plurality of electrodes ( 1, 301 ) located in the first environment and a second electrode or second plurality of electrodes ( 2, 302 ) located in the second environment, so that field lines of said non-uniform electric field cross said membrane, and a dielectrophoretic force generated on particles of said gaseous component (P) is at least part of a driving force of the permeation through said membrane, an amount of said product (P) being selectively removed from the first environment and collected in the second environment.

Hydrogen/syngas generator

The present invention relates to a compact, concentric auto thermal hydrogen/syngas generator for production of hydrogen/syngas without any external heating. Further, the auto thermal hydrogen/syngas generator of the present invention involves combination of reactions such as partial oxidation, steam reforming, dry reforming, auto thermal reforming, dry autothermal reforming, water gas shift, preferential oxidation or methanation that takes place without external heating, for converting air, steam and fuel into a reformate mainly containing CO, CO 2 , N 2 , CH 4 and H 2 O which is subsequently converted to hydrogen/syngas as a feed for fuel cell or syngas applications.

Heat exchanger reformer

A catalytic reformer assembly includes a heated medium flow path for a first medium and a reforming flow path for a second medium. A catalyst substrate is located within the reforming flow path and supports a catalyst. A heat exchanger is disposed within the heated medium flow path for transferring heat from the heated medium flow path to the catalyst substrate.

Sulfur recovery unit and sulfur recovery method

A sulfur recovery unit comprising: a reaction furnace configured to carry out a high-temperature Claus reaction between hydrogen-sulfide-containing gas and oxygen-containing gas introduced to the reaction furnace; a sulfur condenser configured to cool reaction gas discharged from the reaction furnace and condense sulfur contained in the reaction gas; and a pipe that connects the reaction furnace to the sulfur condenser, wherein the reaction furnace is fixed to the ground; and the sulfur condenser and the pipe are arranged so as to be able to move relative to the reaction furnace.

Bi-Modal Radial Flow Reactor

A bi-modal radial flow reactor comprising a cylindrical outer housing surrounding at least five cylindrical, concentric zones, including at least three annulus vapor zones and at least two catalyst zones. The at least two catalyst zones comprise an outer catalyst zone and an inner catalyst zone. The at least three annulus vapor zones comprise an outer annulus vapor zone, a middle annulus vapor zone, and a central annulus vapor zone, wherein the central annulus vapor zone extends along a centerline of the bi-modal radial flow reactor. The outer catalyst zone is intercalated with the outer annulus vapor zone and the middle annulus vapor zone, and the inner catalyst zone is intercalated with the middle annulus vapor zone and the central annulus vapor zone. A removable head cover can be fixably coupled to a top of the cylindrical outer housing to seal a top of the bi-modal radial flow reactor.

BAYONET CATALYTIC REACTOR

A bayonet reactor including a catalytic reactor in the form of an annular structured packing is provided with increased surface area for the transfer of heat between annulus gas and return gas, an increased coefficient of heat transfer between the annulus and return gases, and a reduced overall pressure drop relative to conventional reactors. The reactors of the present technology can enable intensified catalytic processing. 1. A bayonet catalytic reactor comprising:an outer tube having an open first end and a closed second end;an inner tube disposed at least partially within the outer tube, the inner tube having an open first end and an open second end; anda catalytic reactor comprising a structured packing disposed within an annulus defined by an inner diameter of the outer tube and an outer diameter of the inner tube,wherein the outer diameter of the inner tube is at least 0.45 times the inner diameter of the outer tube.2. The bayonet catalytic reactor of claim 1 , wherein the outer diameter of the inner tube is at least 0.63 times the inner diameter of the outer tube.3. The bayonet catalytic reactor of claim 1 , wherein the outer diameter of the inner tube is at least 0.77 times the inner diameter of the outer tube.4. The bayonet catalytic reactor of claim 1 , further comprising a second catalytic reactor disposed within the inner tube proximate the second end of the inner tube.5. The bayonet catalytic reactor of claim 4 , wherein the second catalytic reactor is a structured reactor comprising a honeycomb catalytic reactor.6. The bayonet catalytic reactor of claim 4 , wherein the second catalytic reactor extends from the second end of the inner tube toward the first end of the inner tube to a distance less than 50% of the distance from the second end of the inner tube to the first end of the inner tube.7. The bayonet catalytic reactor of claim 1 , wherein the bayonet catalytic reactor is a steam reforming reactor.8. The bayonet catalytic reactor of claim 1 , ...

GUARD BED SYSTEM AND PROCESS

The invention provides a reaction system for the production of ethylene carbonate and/or ethylene glycol. The system having a guard bed system upstream of a catalytic EO reactor. The guard bed system having a feed line supplying a gaseous feed to be treated and an effluent line configured to remove the treated gaseous feed. The guard bed system has two or more guard bed vessels arranged in series in sequential order, each having an inlet, a bed of guard bed material and an outlet. The inlet of each guard bed vessel is attached by means of valves to both the feed line and the outlet of the guard bed vessel preceding it in sequential order. The outlet of each guard bed vessel is attached by means of valves to both the effluent line and to the inlet of the guard bed vessel following it in sequential order. 2. A process as claimed in claim 1 , wherein the guard bed material is a silver on alumina-based material or a palladium/gold based material claim 1 , preferably supported on silica.3. A process as claimed in claim 2 , whereinthe guard bed material is a silver on alumina-based material and the guard bed vessels are operated at a temperature of at least 100° C. and at most 145° C.; orthe guard bed material is a palladium/gold based material, preferably supported on silica, and the guard bed vessels are operated at a temperature of at least 65° C. and at most 95° C.4. A process as claimed in claim 1 , wherein the iodide-containing impurities formed in the EO absorber include vinyl iodide and alkyl iodides such as ethyl and methyl iodide.5. A process as claimed in claim 1 , wherein each bed of guard bed material is a radial fixed bed.6. A process as claimed in claim 1 , wherein the reaction system further comprises a carbon dioxide absorber and the guard bed system is also upstream of the carbon dioxide absorber claim 1 , which is upstream of the catalytic EO reactor.7. A process as claimed in claim 1 , wherein two or more guard bed systems operated by this process are ...

SYSTEMS AND METHODS FOR CARBON MONOXIDE PRODUCTION BY REDUCTION OF CARBON DIOXIDE WITH ELEMENTAL SULFUR

Thermoneutral systems and methods for producing carbon monoxide (CO) and sulfur dioxide (SO) are disclosed. The systems can include a first reaction zone and a second reaction zone, where heat generated in the first reaction zone is sufficient to drive a carbon dioxide gas (CO(g)) and elemental sulfur gas (S(g)) reaction to produce a product stream that includes CO(g) and SO(g). 1. A system for producing carbon monoxide (CO) and sulfur dioxide (SO) , the system comprising:(a) a first reaction zone configured to produce heat from an exothermic reaction of a first reaction mixture and a first product stream;{'sub': 2', '2, '(b) a second reaction zone comprising a gaseous reaction mixture of carbon dioxide (CO(g)) and elemental sulfur and configured to receive the produced heat from the first reaction zone in an amount sufficient to heat the gaseous reaction mixture and produce a second product stream comprising CO and SO;'}(c) a first outlet in fluid communication with the first reaction zone and configured to remove the first product stream from the first reaction zone; and{'sub': '2', '(d) a second outlet in fluid communication with the second reaction zone and configured to remove the second product stream comprising CO and SOfrom the second reaction zone.'}2. The system of claim 1 , wherein exothermic first reaction mixture comprises carbonyl sulfide (COS) and oxygen source oxygen (O) and the first product stream comprises COand SO.3. The system of claim 1 , wherein the second reaction zone encompasses the first reaction zone.4. The system of claim 3 , wherein the first reaction zone and the second reaction zone form a concentric reactor claim 3 , and wherein the first reaction zone is the annulus of the concentric reactor.5. The system of claim 1 , wherein the first product stream absorbs heat from the exothermic reaction claim 1 , and the system further comprises a heat exchanging unit in fluid communication with the first outlet and the second reaction zone and ...

MULTI-BED CATALYTIC CONVERTER WITH INTER-BED COOLING

A multi-bed catalytic converter comprising at least a first catalytic bed, a second catalytic bed and a heat exchanger arranged between said first bed and said second bed, wherein said heat exchanger is arranged to transfer heat from the hot effluent of the first bed to a cooling medium; said heat exchanger comprises a plurality of stacked round plates, wherein adjacent plates define gaps therebetween, and the effluent of the first catalytic bed and the cooling medium are respectively fed into alternate gaps. 124-. (canceled)25. A multi-bed cylindrical catalytic converter , comprising:a first catalytic bed;a second catalytic bed;a heat exchanger arranged between said first catalytic bed and said second catalytic bed, said heat exchanger being arranged to transfer heat from a first medium to a second medium;an input and an output for the first medium; andan input and an output for the second medium;wherein the first medium is the hot effluent of the first catalytic bed before admission into the second catalytic bed, and the second medium is a cooling medium;wherein said heat exchanger comprises a plurality of stacked round plates, said plurality of stacked round plates being full circular plates or annular plates, and adjacent plates of the plurality of stacked round rates define gaps therebetween;wherein the hot effluent of the first catalytic bed and the cooling medium pass respectively through alternating ones of the gaps between the plurality of stacked round plates;wherein said first catalytic bed is a hollow cylinder comprising a cavity and said heat exchanger is arranged coaxially to the first catalytic bed inside said cavity.26. The multi-bed cylindrical catalytic converter according to claim 25 , wherein said plurality of stacked round plates are stamped plates obtained mechanically by metal sheet pressing.27. The multi-bed cylindrical catalytic converter according to claim 25 , wherein at least one of the input or the output of at least one of the first ...

Inherently safe odh operation

In the operation of an oxidative dehydrogenation (ODH) process, it is desirable to remove oxygen in the product stream for a number of reasons, including to reduce oxidation of the product. This may be achieved by having several pre-reactors upstream of the main reactor having a catalyst system containing labile oxygen. The feed passes through one or more reactors saturated with labile oxygen. When the labile oxygen is consumed through a valve system, the pre-reactor accepts product from the main reactor and complexes reactive oxygen in the product stream until the catalyst system is saturated with labile oxygen. Then the reactor becomes a pre-reactor and another pre-reactor becomes a scavenger.

SYSTEMS AND METHODS FOR THE OXIDATIVE COUPLING OF METHANE

The present disclosure provides systems and methods for producing olefins via an oxidative coupling of methane (OCM) process. The systems and methods may comprise the use of a staged process comprising at least one non-adiabatic section that is in thermal communication with a heat transfer medium and at least one substantially adiabatic section. The systems and methods may also comprise the use of a diluent stream which may improve methane conversion in an OCM reactor and an ethylene/ethane ratio in a post-bed cracking unit. The methods and systems may further comprise injecting oxygen (O) and a paraffin into a gas stream containing a radical transfer agent to provide a reaction mixture. The reaction mixture may be held in a vessel for a time period greater than an auto-ignition delay time (AIDT), such that the reaction mixture may ignite to liberate heat and convert to a product mixture comprising olefins. 1. A method for producing an olefin , the method comprising:{'sub': 4', '2, '(a) producing a gas stream comprising methane (CH), oxygen (O), and a diluent; and'}{'sub': 4', '2+, '(b) passing the gas stream over an oxidative coupling of methane (OCM) catalyst at a pressure of at least 2 bar(g) to convert at least some of the CHinto hydrocarbon compounds having two or more carbon atoms (C compounds),'}wherein a ratio of diluent molecules to carbon atoms in the gas stream is at least 0.1:1.2. The method of claim 1 , wherein the diluent comprises water (HO).3. The method of claim 1 , wherein the diluent comprises carbon dioxide (CO).4. The method of claim 1 , wherein the diluent comprises HO and CO.5. The method of claim 1 , wherein the ratio of diluent molecules to carbon atoms in the gas stream is at least 0.5:1.6. The method of claim 1 , wherein the ratio of diluent molecules to carbon atoms in the gas stream is at most 20:1.7. The method of claim 1 , wherein the ratio of diluent molecules to carbon atoms in the gas stream is from 0.1:1 to 5:1.8. The method of ...

Methods for alkane dehydrogenation

Disclosed herein are methods for dehydrogenation of alkanes to olefins by co-injecting the alkane feed with hydrogen. The present methods provide the improved feed conversion, desired product selectivity, total olefins in product stream, and lower catalyst deactivation rate.

METHOD FOR PRODUCING A HORIZONTAL FLOW ADSORBER AND DIVIDING WALL MODULE FOR USE IN SAID METHOD

The method serves for producing a horizontal through flow adsorber with two adsorbents which contains two immediately adjacent packings in a horizontal or vertical container. Between the two packings there is a vertical interface. In a step (a) a vertical dividing wall is positioned on the bottom of the adsorption bed and then on each side of the dividing wall one of the two adsorbents is charged up to a first height that does not exceed the upper edge of the separating ring. In the following step (b) the vertical dividing wall is displaced upwardly until the lower edge thereof is still placed in the existing packing. Then, on each side of the dividing wall one of the two adsorbents is charged up to a second height that does not exceed the upper edge of the displaced dividing wall. Finally, step (b) is repeated until a predetermined filling height is achieved. According to the invention, the vertical dividing wall is composed of at least three dividing wall modules () that extend only over a part of the length or of the periphery of the vertical dividing wall and are movable in a vertical direction independently of one another. 1. The method for producing a horizontal through flow adsorber with two adsorbents which contains two immediately adjacent packings in a horizontal or vertical container , wherein there is a vertical interface between the two packings , and wherein a first packing contains a first adsorbent and a second packing contains a second adsorbent that differs from the first adsorbent in the chemical composition and/or particle size thereof , wherein , in the method(a) a vertical dividing wall is positioned on the bottom of the adsorption bed and then on each side of the dividing wall one of the two adsorbents is charged up to a first height that does not exceed the upper edge of the dividing wall,(b) the vertical dividing wall is displaced upwardly until the lower edge thereof is still placed in the existing packing, and on each side of the dividing ...

Axial/radial flow converter

In a cooled axial/radial flow converter, in which process gas passes from an outer annulus via a catalyst bed to an inner centre tube, the catalyst bed is divided into identical modules stacked on top of each other. The process gas reaches the catalyst through openings facing the outer annulus, passes axially down the catalyst bed of each module, leaves the module through collectors in the bottom thereof, and flows to the centre tube. The catalyst bed is cooled by cooling panels, in which the process gas is pre-heated to the reaction temperature, while at the same time the heat of reaction is partly removed from the catalyst bed. The converter is especially suitable as ammonia converter.

REACTOR WITH A CATALYTIC BED

A catalytic bed for a chemical reactor, said catalytic bed having an annular-cylindrical geometry and comprising at least one collector made with a gas-permeable cylindrical wall, containing at least a first catalyst and a second catalyst, wherein the second catalyst has a finer particle size than the first catalyst, and wherein the first catalyst forms a layer of catalyst adjacent to and in contact with said collector. 122-. (canceled)23. A catalytic reactor , comprising:a catalytic bed suitable for a chemical reaction of conversion of a gaseous charge into a gaseous product, said catalytic bed having an annular-cylindrical geometry, said catalytic bed including at least one collector made with a gas-permeable cylindrical wall;wherein said at least one collector includes at least one annular layer of a first granular material that includes a catalyst adapted to catalyse said reaction of conversion, and at least one annular layer of a second granular material;wherein the second granular material is coarser than the first granular material, the second granular material having a larger particle size than the first granular material;wherein said at least one collector includes an outlet collector and said layer of second granular material is adjacent to and in contact with said outlet collector, so that said layer of first granular material is separated from the collector by the layer of second granular material.24. The catalytic reactor according to claim 23 , wherein said outlet collector is an inner collector.25. The catalytic reactor according to claim 23 , further comprising:an outer collector and an inner collector;wherein said outer and inner collectors are cylindrical, coaxial, and gas-permeable;wherein said outer and inner collectors including two annular layers of said second granular material;wherein a first layer of said second granular material is in contact with the outer collector and a second layer of said second granular material is in contact with the ...

METHOD FOR CARBON MONOXIDE SHIFT CONVERSION

A shift conversion catalyst layer is divided into at least two front and back stages. A first catalyst and a second catalyst are provided on the upstream side and the downstream side, respectively. The first catalyst has a property that a carbon monoxide conversion rate decreases with an increase in carbon dioxide concentration in a supplied reaction gas at a constant carbon monoxide concentration in the supplied reaction gas and a constant reaction temperature. The first catalyst is combined with the second catalyst such that the degree of decrease in carbon monoxide conversion rate with respect to an increase in carbon dioxide concentration in the supplied reaction gas in the second catalyst is lower than that in the first catalyst. Whereby, the conversion rate of a carbon monoxide concentration of a carbon monoxide shift conversion apparatus can be improved without increasing the used amount of a shift conversion catalyst. 1. A method of carbon monoxide shift conversion for reacting carbon monoxide and water vapor contained in a reaction gas and converting them into carbon dioxide and hydrogen , comprising:a shift reaction step divided into at least two continuous shift reaction steps, where a first catalyst stage is used upstream in a first shift conversion step, whereas a second catalyst stage is used downstream in a second shift reaction step, each of the first and second catalyst stages having an upstream end and a downstream end, wherein the first catalyst stage has a property that a carbon monoxide conversion rate decreases with an increase in carbon dioxide concentration in a supplied reaction gas from 1 vol % to 14 vol % at the upstream end of the first catalyst stage due to carbon dioxide poisoning in the case of a constant carbon monoxide concentration in the supplied reaction gas at the upstream end of the first catalyst stage and a constant reaction temperature, andthe second catalyst stage has a property that the degree of decrease in carbon monoxide ...

METHOD FOR REVAMPING AN AMMONIA CONVERTER

Method for revamping a multi-bed ammonia converter, wherein said converter comprises a plurality of adiabatic catalytic beds including a first catalytic bed and one or more further catalytic bed(s), said catalytic beds being arranged in series so that the effluent of a bed is further reacted in the subsequent bed; at least a first inter-bed heat exchanger arranged between said first catalytic bed and a second catalytic bed to cool the effluent of said first bed before admission into said second bed, and optionally further inter-bed heat exchanger(s) arranged between consecutive beds; said method involves the conversion of said first catalytic bed into an isothermal catalytic bed. 1. A method for revamping a multi-bed ammonia converter , wherein said converter comprises:a plurality of adiabatic catalytic beds including a first catalytic bed and one or more further catalytic bed(s), said catalytic beds being arranged in series so that the effluent of a bed is further reacted in the subsequent bed;at least a first inter-bed heat exchanger arranged between said first catalytic bed and a second catalytic bed to cool the effluent of said first bed before admission into said second bed, and optionally further inter-bed heat exchanger(s) arranged between consecutive beds;wherein said first catalytic bed is converted into an isothermal catalytic bed.2. The method according to claim 1 , wherein said first catalytic bed is converted to isothermal by adding a heat exchanger immersed in the catalyst of said first catalytic bed.3. The method according to claim 1 , wherein said first catalytic bed is replaced with a new catalytic bed containing a heat exchanger immersed in the catalyst.4. The method according to claim 1 , further comprising:replacing said first inter-bed heat exchanger with a new heat exchanger smaller than the previous one, wherein the smaller size of the new heat exchanger clears a volume inside the converter, andat least part of said volume is used to ...

Annular Catalyst Carrier Container For Use In A Tubular Reactor

A catalyst carrier for insertion in a reactor tube of a tubular reactor, said catalyst carrier comprising: a container for holding catalyst in use, said container having a bottom surface closing the container, and a top surface; a carrier outer wall extending from the bottom surface to the top surface; a seal extending from the container by a distance which extends beyond the carrier outer wall; said carrier outer wall having apertures located below the seal. 1. A catalyst carrier for insertion in a reactor tube of a tubular reactor , said catalyst carrier comprising:a container for holding catalyst in use, said container having a bottom surface closing the container, and a top surface;a carrier outer wall extending from the bottom surface to the top surface;a seal extending from the container by a distance which extends beyond the carrier outer wall;said carrier outer wall having apertures located below the seal.2. The catalyst carrier according to comprising:an annular container for holding catalyst in use, said container having a perforated inner container wall defining an inner channel, a perforated outer container wall, a top surface closing the annular container and a bottom surface closing the annular container;a surface closing the bottom of said inner channel formed by the inner container wall of the annular container.3. The catalyst carrier according to comprising a cap closing the inner channel formed by the perforated inner container wall claim 2 , said cap including one or more apertures.4. The catalyst carrier according to wherein the carrier outer wall is smooth or shaped.5. The catalyst carrier according to wherein the apertures in the carrier outer wall are slots.6. The catalyst carrier according to wherein the wall material is left partially attached to the carrier wall when the apertures are formed.7. The catalyst carrier according to wherein the attached material is configured to induce direction for the fluid flow.8. The catalyst carrier ...

REACTOR FOR CONDUCTING EXOTHERMIC EQUILIBRIUM REACTIONS

A reactor for conducting exothermic equilibrium reactions, especially for the performance of methanol synthesis by heterogeneously catalysed conversion of synthesis gas, is proposed, which enables readjustment and hence optimization of the reaction conditions along the longitudinal coordinate of the reactor. For this purpose, in accordance with the invention, the reactor is divided into a multitude of series-connected reaction cells, each of which comprises a preheating zone, a cooled reaction zone, one or more cooling zones and a deposition zone for condensable reaction products. In this way, the reaction conditions are adjustable to the respective, local composition of the reaction mixture and variable over the reactor length. 116- (canceled)17. A reactor for conducting exothermic equilibrium reactions , in which a gaseous feed mixture is at least partly converted over a solid catalyst to a product mixture comprising at least one liquid reaction product condensable at a reactor pressure and at temperatures below a reactor temperature , the reactor comprising at least two series-connected reaction cells that are in fluid connection with one another and are arranged in a common reactor shell , wherein each reaction cell comprises the following series-connected assemblies that are in fluid connection with one another:(a) a preheating zone suitable for heating the feed mixture or the gaseous product stream from the upstream reaction cell, wherein the preheating zone can optionally be dispensed with in the first reaction cell in flow direction of the gaseous feed mixture;(b) at least one reaction zone comprising a catalyst active in respect of the exothermic equilibrium reaction to be conducted and a cooling apparatus in a heat-exchanging relationship with the catalyst;(c) at least one cooling zone comprising a cooling apparatus suitable for cooling the partly converted, gaseous product stream that has been laden with condensable reaction product and exits from the ...

Hydroprocessing Reactor to Lower Pressure Drop and Extend Catalyst Life

A reactor for accommodating high contaminant feedstocks includes a reactor vessel having an inlet for introducing a feedstock containing contaminants into an interior of the reactor vessel. A basket is located within the reactor vessel interior and contains a particulate material for removing contaminants from the feedstock to form a purified feedstock that is discharged to a purified feedstock outlet. A catalyst is located within the reactor vessel and in fluid communication with the purified feedstock outlet of the basket for contacting the purified feedstock to form a desired product. 1. A reactor for accommodating high contaminant feedstocks comprising:a reactor vessel having an inlet for introducing a feedstock containing contaminants into an interior of the reactor vessel, the interior being defined by an interior wall of the reactor vessel;a distributor assembly located below and in fluid communication with the inlet for discharging the feedstock radially outward towards the interior walls of the reactor vessel;a basket located within the reactor vessel interior and below the distributor assembly, the basket having a fluid permeable outer wall and a first fluid permeable inner wall that is spaced radially inward from the outer wall to define a first annular interior space of the basket, the first annular interior space of the basket containing a particulate material for removing contaminants from the feedstock, the outer wall of the basket being spaced radially inward from the interior wall of the reactor vessel to define an annular flow space between the outer wall of the basket and the interior wall of the reactor vessel, and wherein feedstocks introduced into the reactor vessel from the distributor assembly flow through the annular flow space and radially inward through the first annular interior space of the basket and through the particulate material to facilitate removal of contaminants from the feedstock to form a purified feedstock, the first fluid ...

Selective Poisoning of Aromatization Catalysts to Increase Catalyst Activity and Selectivity

Spent aromatization catalysts containing a transition metal and a catalyst support are selectively poisoned in the disclosed reforming methods, resulting in improvements in overall aromatics yield and selectivity.

PROCESS FOR METHANOL PRODUCTION

A process for the synthesis of methanol from an input stream of synthesis gas, comprising the following steps: subjecting a portion of said input stream as feed stream to an adiabatic reactive step, providing an effluent containing methanol and unreacted synthesis gas; quenching of said effluent with a further portion of said input stream, providing a quenched stream; subjecting said quenched stream to an isothermal reactive step, providing a methanol-containing product stream. 1. A process for the synthesis of methanol from an input stream of synthesis gas , comprising the following steps:subjecting a portion of said input stream as feed stream to an adiabatic reactive step, providing an effluent containing methanol and unreacted synthesis gas;quenching of said effluent with a further portion of said input stream, providing a quenched stream;subjecting said quenched stream to an isothermal reactive step, providing a methanol-containing product stream.2. The process according to claim 1 , wherein the feed stream to said adiabatic reactive step comprises a fraction of said input stream which has been pre-heated by acting as a cooling medium of said isothermal reactive step claim 1 , thus forming a pre-heated stream.3. The process according to claim 2 , wherein said pre-heated stream mixes with a further fraction of said input stream to form the feed stream to said adiabatic reactive step claim 2 , said further fraction being directly sent to said adiabatic reactive step.4. The process according to claim 2 , wherein said isothermal reactive step is carried out in a catalytic bed comprising heat exchange bodies and said fraction acting as a cooling medium traverses said heat exchange bodies.5. The process according to claim 1 , wherein said input stream is obtained by pre-heating at least a portion of a stream of synthesis gas by indirect heat exchange with said methanol-containing product stream.6. The process according to claim 1 , which is suitable to be performed ...

Annular Catalyst Carrier Container For Use In A Tubular Reactor

A catalyst carrier for insertion in a reactor tube of a tubular reactor, said catalyst carrier comprising: a container for holding catalyst in use, said container having a bottom surface closing the container, and a top surface; a carrier outer wall extending from the bottom surface to the top surface; a seal extending from the container by a distance which extends beyond the carrier outer wall; said carrier outer wall having apertures located below the seal. 1. A catalyst carrier for insertion in a reactor tube of a tubular reactor , said catalyst carrier comprising:a container for holding a monolith catalyst in use, said container having a bottom surface closing the container, and a top surface;a carrier outer wall extending from the bottom surface to the top surface;a seal extending from the container by a distance which extends beyond the carrier outer wall;said carrier outer wall having apertures located below the seal.2. The catalyst carrier according to comprising feet on the bottom surface such that claim 1 , in use claim 1 , the monolith catalyst is supported on the feet and there is a gap between the bottom of the monolith catalyst and the bottom surface of the container.3. The catalyst carrier according to wherein the top surface is an annulus which extends over at least a portion of the monolith catalyst and to the carrier outer wall.4. The catalyst carrier according to wherein the monolith catalyst has a channel extending longitudinally therethrough.5. The catalyst carrier according to claim 4 , wherein the channel is located on a central axis of the monolith catalyst such that the monolith catalyst is of annular cross-section.6. The catalyst carrier according to claim 4 , wherein the top surface extends over the monolith but leaves the channel uncovered.7. The catalyst carrier according to wherein the carrier outer wall is smooth or shaped.8. The catalyst carrier according to wherein the apertures in the carrier outer wall are slots.9. The catalyst ...

Aromatization Reactors with Hydrogen Removal and Related Reactor Systems

The present invention discloses aromatization reactor vessels with hydrogen membrane tubes, and associated aromatization reactor vessel systems. Also disclosed are processes for conducting aromatization reactions utilizing these reactor vessels and systems. 120-. (canceled)21. An aromatization process comprising:{'sub': '2', 'claim-text': (a) a reactor wall;', '(b) a catalyst bed positioned within the reactor vessel;', '(c) an outer annulus positioned between the reactor wall and an outer particle barrier, the outer particle barrier and the outer annulus surrounding the catalyst bed;', '(d) a reactor inlet for the feed stream;', 'wherein a flow path for the feed stream begins at the reactor inlet, continues to the outer annulus, through the outer particle barrier and the catalyst bed, into the center pipe, and to the reactor outlet; and', '(e) a reactor outlet connected to a center pipe, the center pipe positioned in the reactor vessel and surrounded by the catalyst bed;'}, {'sub': '2', '(f) a membrane tube configured to remove H, the membrane tube positioned in the center pipe or the outer annulus, the membrane tube having an inner permeate side and an outer process side;'}], '(i) introducing a feed stream comprising Hand a non-aromatic hydrocarbon into an aromatization reactor vessel, the aromatization reactor vessel comprising(ii) contacting the feed stream with the catalyst bed comprising an aromatization catalyst;{'sub': '2', '(iii) catalytically converting at least a portion of the non-aromatic hydrocarbon within the aromatization reactor vessel to produce an aromatic hydrocarbon and H;'}{'sub': 2', '2, '(iv) removing a portion of the Hfrom the center pipe or the outer annulus via the membrane tube to reduce a partial pressure of Hin the process; and'}(v) discharging a reactor effluent comprising the aromatic hydrocarbon from the aromatization reactor vessel via the reactor outlet.22. The process of claim 21 , wherein:the aromatic hydrocarbon comprises benzene ...

BI-MODAL RADIAL FLOW REACTOR

A bi-modal radial flow reactor comprising: a cylindrical outer housing surrounding at least five cylindrical, concentric zones, including at least three annulus vapor zones including an outer annulus vapor zone, a middle annulus vapor zone, and a central annulus vapor zone, and at least two catalyst zones, including an outer catalyst zone and an inner catalyst zone, wherein the outer catalyst zone is intercalated with the outer annulus vapor zone and the middle annulus vapor zone, and wherein the inner catalyst zone is intercalated with the middle annulus vapor zone and the central annulus vapor zone; and a manifold configured to introduce a feed vertically into a bottom end of each of one or two of the at least three annulus vapor zones, and remove a product from a bottom end of each of the one or two remaining of the at least three annulus vapor zones. 1. A bi-modal radial flow reactor comprising:a cylindrical outer housing surrounding at least five cylindrical, concentric zones, including at least three annulus vapor zones and at least two catalyst zones, wherein the at least two catalyst zones comprise an outer catalyst zone and an inner catalyst zone, and wherein the at least three annulus vapor zones comprise an outer annulus vapor zone, a middle annulus vapor zone, and a central annulus vapor zone, wherein the central annulus vapor zone extends along a centerline of the bi-modal radial flow reactor, and wherein the outer catalyst zone is intercalated with the outer annulus vapor zone and the middle annulus vapor zone, and wherein the inner catalyst zone is intercalated with the middle annulus vapor zone and the central annulus vapor zone,wherein each of the at least five cylindrical, concentric zones has a top end and a bottom end; and(a) wherein each of the at least three annulus vapor zones has an opening at the bottom end thereof, operable as an inlet or an outlet of the bi-modal radial flow reactor; or (b) wherein (i) the middle annulus vapor zone has an ...

Radial-parallel catalytic reactor

The present invention comprises an axial radial catalytic reactor with a shell (as gas tight seal to maintain process gas flows within it) and a feed tube (passing from a source of process gas flow through the shell and into it do deliver feed gas to one or more levels of two annularly sequential catalyst beds), where one end of the feed tube is used as an inlet for feeding reaction mass. In one embodiment of the invention, an interior end of the feed tube is sealed.

GUARD BED SYSTEM AND PROCESS

The invention provides a reaction system for the production of ethylene carbonate and/or ethylene glycol. The reaction system having a guard bed system upstream of a catalytic EO reactor. The guard bed system having a feed line supplying a gaseous feed and an effluent line configured to remove the treated gaseous feed. The guard bed system has two or more guard bed vessels arranged in series in sequential order, each having an inlet, a bed of guard bed material and an outlet. The inlet of each guard bed vessel is attached by means of valves to both the feed line and the outlet of the guard bed vessel preceding it in sequential order. The outlet of each guard bed vessel is attached by means of valves to both the effluent line and to the inlet of the guard bed vessel following it in sequential order. 1. A reaction system for the production of ethylene carbonate and/or ethylene glycol , said reaction comprising a guard bed system positioned upstream of a catalytic EO reactor , said guard bed system comprising a feed line supplying a gaseous feed to be treated and an effluent line configured to remove the treated gaseous feed and two or more guard bed vessels arranged in series in sequential order , each guard bed vessel comprising an inlet , a bed of guard bed material and an outlet , wherein the inlet of each guard bed vessel is attached by means of valves to both the feed line and the outlet of the guard bed vessel preceding it in sequential order and wherein the outlet of each guard bed vessel is attached by means of valves to both the effluent line and to the inlet of the guard bed vessel following it in sequential order and wherein the guard bed vessel following the last guard bed vessel in sequential order is the first guard bed vessel in sequential order.2. The system according to claim 1 , wherein each bed of guard bed material is a radial fixed bed.3. The system according to claim 1 , wherein the guard bed system is also upstream of a carbon dioxide absorber ...

Hydroprocessing Reactor to Lower Pressure Drop and Extend Catalyst Life

A reactor for accommodating high contaminant feedstocks includes a reactor vessel having an inlet for introducing a feedstock containing contaminants into an interior of the reactor vessel. A basket is located within the reactor vessel interior and contains a particulate material for removing contaminants from the feedstock to form a purified feedstock that is discharged to a purified feedstock outlet. A catalyst is located within the reactor vessel and in fluid communication with the purified feedstock outlet of the basket for contacting the purified feedstock to form a desired product. 1. A reactor for accommodating high contaminant feedstocks comprising:a reactor vessel having an inlet for introducing a feedstock containing contaminants into an interior of the reactor vessel, the interior being defined by an interior wall of the reactor vessel;a distributor assembly located below and in fluid communication with the inlet for discharging the feedstock radially outward towards the interior walls of the reactor vessel;a basket located within the reactor vessel interior and below the distributor assembly, the basket having a fluid permeable outer wall and a first fluid permeable inner wall that is spaced radially inward from the outer wall to define a first annular interior space of the basket, the first annular interior space of the basket containing a particulate material for removing contaminants from the feedstock, the outer wall of the basket being spaced radially inward from the interior wall of the reactor vessel to define an annular flow space between the outer wall of the basket and the interior wall of the reactor vessel, and wherein feedstocks introduced into the reactor vessel from the distributor assembly flow through the annular flow space and radially inward through the first annular interior space of the basket and through the particulate material to facilitate removal of contaminants from the feedstock to form a purified feedstock, the first fluid ...

Installation for treatment of fluids comprising multiple beds of particles supported by a separation grid

The installation is an improved version of the classical form and is used in pressure swing adsorption techniques, in particular vacuum pressure swing adsorption(VPSA), for the separation of gases. The installation comprises a treatment vessel (R) containing a primary bed (L1) with particles(P1) of size g1, and a secondary bed (L2) with particles (P2) of size g2. The beds are adjacent and separated by a perforated structure with orifices (OG) for passage of the fluid and of dimension(d) such that g1 is greater than d which is greater than g2. An Independent claim is also included for the treatment process.

Systems and methods for the oxidative coupling of methane

The present disclosure provides systems and methods for producing olefins via an oxidative coupling of methane (OCM) process. The systems and methods may comprise the use of a staged process comprising at least one non-adiabatic section that is in thermal communication with a heat transfer medium and at least one substantially adiabatic section. The systems and methods may also comprise the use of a diluent stream which may improve methane conversion in an OCM reactor and an ethylene/ethane ratio in a post-bed cracking unit. The methods and systems may further comprise injecting oxygen (O2) and a paraffin into a gas stream containing a radical transfer agent to provide a reaction mixture. The reaction mixture may be held in a vessel for a time period greater than an auto-ignition delay time (AIDT), such that the reaction mixture may ignite to liberate heat and convert to a product mixture comprising olefins.

Method and apparatus for reducing the content of NOx and N2O in gases

Das Verfahren umfasst das Leiten des N¶2¶O und NO¶x¶ enthaltenden Gases über eine Folge zweier Katalysatorbetten, enthaltend einen oder mehrere mit Eisen beladene Zeolithe, die Zugabe eines Reduktionsmittels für NO¶x¶ zwischen den Katalysatorbetten, das Einstellen einer Temperatur von weniger als 500 DEG C im ersten und zweiten Katalysatorbett, das Einstellen eines Gasdruckes von mindestens 2 bar in den beiden Katalysatorbetten, und die Auswahl einer solchen Raumgeschwindigkeit im ersten und zweiten Katalysatorbett, so dass im ersten Katalysatorbett ein Abbau des N¶2¶O-Gehalts des Gases um höchstens bis zu 90%, bezogen auf den N¶2¶O-Gehalt am Eingang des ersten Katalysatorbettes, erfolgt, und dass im zweiten Katalysatorbett ein weiterer Abbau des N¶2¶O-Gehalts des Gases um mindestens 30%, bezogen auf den N¶2¶O-Gehalt am Eingang des zweiten Katalysatorbettes, erfolgt. DOLLAR A Die erste Reaktionszone dient zum Abbau von N¶2¶O und in der zweiten Reaktionszone wird das NO¶x¶ reduziert und zumindest ein Teil des verbliebenen N¶2¶O wird zersetzt. DOLLAR A Die beschriebene Vorrichtung umfasst mindestens ein radial durchströmtes Katalysatorbett. The process comprises passing the gas containing N 2 O 2 and NO 3 x 10 over a series of two catalyst beds containing one or more iron-loaded zeolites, adding a reducing agent for NO 2+ between the catalyst beds, adjusting a temperature of less than 500 ° C in the first and second catalyst beds, setting a gas pressure of at least 2 bar in the two catalyst beds, and selecting such a space velocity in the first and second catalyst beds such that in the first catalyst bed there is a reduction in N 2 O 2 Content of the gas at most up to 90%, based on the N¶2¶O content at the entrance of the first catalyst bed, takes place, and that in the second catalyst bed, a further reduction of the N¶2¶O content of the gas by at least 30 %, based on the N¶2¶O content at the entrance of the second catalyst bed, takes place. DOLLAR A The first ...

Multiple catalyst bed radial flow reactor

Catalytic reactor

Metodo para a producao de formol

메탄의 산화적 커플링를 위한 시스템 및 방법

본 개시는 메탄의 산화적 커플링(OCM) 공정을 통해 올레핀을 제조하는 시스템 및 방법을 제공한다. 상기 시스템 및 방법은 열 전달 매질과 열적으로 연통하는 적어도 하나의 비-단열 구획 및 적어도 하나의 실질적 단열 구획을 포함하는 단계식 공정의 이용을 포함할 수 있다. 상기 시스템 및 방법은 OCM 반응기에서 메탄 전환을 개선할 수 있고 포스트-층 분해 유닛에서 에틸렌/에탄 비를 개선할 수 있는 희석제 스트림의 사용도 포함할 수 있다. 상기 방법 및 시스템은 산소(O 2 ) 및 파라핀을, 라디칼 전달제를 함유하는 가스 스트림에 주입하여 반응 혼합물을 제공하는 단계를 추가로 포함할 수 있다. 상기 반응 혼합물은 자가점화 지연 시간(AIDT)보다 더 긴 시간 동안 용기에 보유될 수 있으므로, 상기 반응 혼합물은 점화하여 열을 방출할 수 있고 올레핀을 포함하는 생성물 혼합물로 전환될 수 있다.

Systems and methods for the oxidative coupling of methane

The present disclosure provides systems and methods for producing olefins via an oxidative coupling of methane (OCM) process. The systems and methods may comprise the use of a staged process comprising at least one non-adiabatic section that is in thermal communication with a heat transfer medium and at least one substantially adiabatic section. The systems and methods may also comprise the use of a diluent stream which may improve methane conversion in an OCM reactor and an ethylene/ethane ratio in a post-bed cracking unit. The methods and systems may further comprise injecting oxygen (O 2 ) and a paraffin into a gas stream containing a radical transfer agent to provide a reaction mixture. The reaction mixture may be held in a vessel for a time period greater than an auto-ignition delay time (AIDT), such that the reaction mixture may ignite to liberate heat and convert to a product mixture comprising olefins.

Method and reactor for formaldehyde heterogeneous exothermic synthesis

A process for the heterogeneous exothermic synthesis of formaldehyde, in particular in reactors (1) of the type comprising a plurality of adiabaric catalytic beds (5a-5c) connected in series, provides the step of flowing the gaseous reagents across at least one of the catalytic beds (5a-5c) with substantially radial flow.

Reactor for exothermic catalytic reaction

Process for the synthesis of methanol

FLUID TREATMENT PLANT COMPRISING SEVERAL PARTICLE BEDS HOLDED BY A SEPARATION GRID

Verfahren zur Nachrüstung eines heterogenen exothermischen Synthesereaktors

CATALYTIC REACTOR

Reactor

In an ammonia synthesis column, the combination of a tube bundle heat exchanger and a boiler with two superposedly arranged catalyst beds permits to recover considerable amounts of reaction heat, the flow of the gases being reacted running in a radial direction.

Reactor for conducting exothermic equilibrium reactions

FIELD: engineering. SUBSTANCE: proposed is a reactor for conducting exothermic equilibrium reactions, wherein a gaseous feed mixture is at least partially converted by means of a solid catalyst into a finished mixture containing at least one liquid reaction product condensed at a pressure in the reactor and temperatures below the temperature in the reactor, containing at least two reaction chambers connected consequently, fluidly communicating with each other and located in a common reactor shell, wherein each reaction chamber comprises the following consequently connected units in fluid communication with each other: (a) a preheating area suitable for heating a feed mixture or a gaseous product stream from an upstream reaction chamber, wherein use of the preheating area is optional in the first reaction chamber in the direction of the gaseous feed mixture stream, (b) at least one reaction area containing a catalyst, active with respect to the conducted exothermic equilibrium reaction, and a cooling apparatus in heat exchange communication with the catalyst, (c) at least one cooling area containing a cooling apparatus suitable for cooling a partially converted gaseous product stream filled with a condensable reaction product and outflowing from the reaction area to a temperature below the dew point of the gas, (d) a precipitation area containing a gas-liquid phase separation apparatus intended to separate the product stream outflowing from the cooling area into a stream of gaseous product freed from condensate and a condensate stream containing a liquid reaction product, (e) a pipeline tool for discharge of the condensate stream containing a liquid reaction product from the reactor and optionally a tool for supplying a condensate stream to an apparatus for processing a reaction product, (f) a tool for diverting the gaseous product stream freed from the condensate, and a tool for supplying the gaseous product stream to a downstream reaction chamber and/or a tool for ...

System and method with a protective layer

FIELD: chemical industry. SUBSTANCE: invention relates to a method for operating a system with a protective layer in a reaction system for the production of ethylene carbonate and/or ethylene glycol. The reaction system contains a reactor for the catalytic production of ethylene oxide, a system with a protective layer and an ethylene oxide absorber. The gaseous composition from the reactor is fed to an ethylene oxide absorber, in which it contacts the lean absorbent in the presence of catalysts promoting carboxylation and hydrolysis, and the gases not absorbed in the ethylene oxide absorber are taken from the upper part of the ethylene oxide absorber and returned to the reactor. The method includes supply of a gaseous raw material, which is a recirculating gas from an ethylene oxide absorber, supply of the raw material through two or more containers with a protective layer arranged in series and containing a layer of material capable of removing impurities from the raw material, bringing the raw material into contact with the material of the protective layer of the containers, with the removal of impurities from the raw material, withdrawal of the purified raw material, excluding the first container from the raw material flow after a certain time and allowing the raw material flow to continue through the second and subsequent containers, renewing the cover material in the first container and restoring the raw material flow through the first container so that it is the last container in the sequence. EFFECT: invention provides a high level of removal of impurities, as well as reliability, efficiency and economy. 10 cl, 3 dwg РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2 746 130 C2 (51) МПК B01J 8/04 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (52) СПК B01J 8/04 (2021.01) (21)(22) Заявка: 2018125893, 13.12.2016 (24) Дата начала отсчета срока действия патента: Дата регистрации: 07.04.2021 15.12.2015 EP 15200254.9 (43) ...

Реактор дл экзотермического гетерогенного каталитического синтеза

Реактор содержит кожух, образующий наполнительный патрон, практически независим от коррозии с катализатором, при этом по крайней мере перва  концева  корзина опираетс  на промежуточную корзину, котора  в свою очередь опираетс  на упаковочное кольцо, выполненное заодно с указанным кожухом наполнительного патрона, при этом днище обеих указанных корзин, соединенных вместе изогнуто противоположно по отношению к кривой изгиба на днище реактора. В указанном первом концевом слое помещен коллектор между наружной стенкой корзины и внутренней поверхностью кожуха наполнительного патрона . В промежуточный слой помещен коллектор внутри внутренней цилиндрической стенки, образующей корзину. Теплообменник газ/газ помещен в центральном положении внутри цилиндрической стенки, по крайней мере корзины с катализатором, котора  находитс  ближе всего к выходу реактора дл  горючего прореагировавшего типа газа. 2 з.п. ф-лы, 2 ил. сл

Method and the device for reduction of the contents of nitrogen oxides in the gases

FIELD: chemical industry; other industries; methods and the devices for reduction of the nitrogen oxides content in the technological and effluent gases. SUBSTANCE: the invention is pertaining to the method of reduction of the nitrogen oxides content in the gases, in particular, to the technological and effluent gases and also to the device used for realization of this purpose. The method provides for gating of N 2 O - and NO x -containing gas through the row of two catalyst layers containing one type or some types of zeolites loaded with iron, addition of the reducing agent foe NO x between these layers of the catalyst, maintenance of the temperature less, than 500°C in first layer of the catalyst and in the second layer of the catalyst, maintenance of the gas pressure, at least of 2 bar in both layers of the catalysts, selection of a such volumetric speed flow in the first and second catalyst layers, that in first layer of the catalyst the decomposition of N 2 O till its content of no more then 90 % with the respect to the contents of N 2 O at the inlet of the first layer of the catalyst and set the content of N 2 O more, than 200 parts per million, and that in the second layer of the catalyst the further decomposing of N 2 O contained in the gas, at least, by 30 % with the respect to the contents of N 2 O at the inlet of the second catalyst layer. The device used for reduction of the contents of NO X and N 2 O in the gases, in particular, in the technological gases and the effluent gases includes: two catalyst layers disposed one after another and containing one type or some types of the iron loaded zeolites, through which the gas containing NO X and N 2 O passes. At that the device is disposed between catalyst layers for injection of the gaseous reducing agent in the stream containing NO X and N 2 O of the gas includes the mixer, through which the gas is gated after passing the first layer of the catalyst and including the pipe duct for the reducing agent, which ...

Fixed-bed catalytic reactor

FIELD: chemistry. SUBSTANCE: invention relates to chemical industry and can be used particularly for synthesising ammonia, methanol, formaldehyde or styrene. Catalyst layers are put on the axis of a cylindrical body of a radial reactor. The layers have inlet sides, through which gaseous reagents enter, and outlet sides through which a reaction mixture comes out, and several heat exchangers distributed on the circular part of the layers. In the first catalyst layer heat exchangers are only placed on the part of this layer near its outlet side. In the second layer heat exchangers are only placed on the part of this second catalyst layer near its inlet side. In the method of catalytic synthesis, gaseous reagents are passed through the first adiabatic zone in the first catalyst layer, and then through the first pseudoisothermal zone in the first catalyst layer, through the second pseudoisothermal zone in the second catalyst layer and, finally, through the second adiabatic zone in the second catalyst layer. EFFECT: increased conversion output of reactors with simultaneous reduction of energy consumption, capital expenditure and expenses on servicing and repair. 7 cl, 8 dwg РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) 2 361 657 (13) C2 (51) МПК B01J 8/04 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ, ПАТЕНТАМ И ТОВАРНЫМ ЗНАКАМ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (30) Конвенционный приоритет: 29.07.2004 EP 04017905.3 (73) Патентообладатель(и): МЕТАНОЛ КАСАЛЕ С.А. (CH) (43) Дата публикации заявки: 10.09.2008 (45) Опубликовано: 20.07.2009 Бюл. № 20 (85) Дата перевода заявки PCT на национальную фазу: 28.02.2007 2 3 6 1 6 5 7 R U (87) Публикация PCT: WO 2006/010565 (02.02.2006) Адрес для переписки: 101000, Москва, М.Златоустинский пер., 10, кв.15, "ЕВРОМАРКПАТ", пат.пов. И.А.Веселицкой, рег. № 11 (54) РЕАКТОР С НЕПОДВИЖНЫМ СЛОЕМ КАТАЛИЗАТОРА расположены только в части этого второго (57) Реферат: слоя катализатора ближе к его входной Изобретение относится к химической ...

Method for preparing polybutene

C4 혼합물 중 이소부텐의 활용을 극대화함으로써, 기존의 C4 혼합물로 폴리부텐을 생산하던 것보다 증량 생산이 가능한 폴리부텐의 제조방법이 개시된다. 상기 폴리부텐의 제조방법은, C4 혼합물이 이성화 반응기에 공급되어, 이성화 영역에서는 이성화 촉매를 이용한 수소이성화 반응에 의해 1-부텐이 2-부텐으로 이성화되고, 분별 증류 영역에서는 이소부텐 및 2-부텐이 분별 증류되어 분리되는 단계; 상기 이성화 반응기에서 분리된 2-부텐이 포함된 C4 혼합물이 골격 이성화 반응기로 공급되어, 골격 이성화 촉매를 이용한 골격 이성화 반응에 의해, 노르말부텐 중 일부가 이소부텐으로 골격 이성화되고, 이로부터 얻어진 골격 이성화 혼합물은, 상기 이성화 반응기로 공급되어 재순환되는 단계; 및 상기 이성화 반응기에서 분리된 고농도의 이소부텐이 포함된 반응 원료 및 중합 촉매가 폴리부텐 중합 반응기에 공급되어, 중합 반응에 의해 폴리부텐이 생성되는 단계를 포함하며, 상기 중합 반응 후, 미반응 C4의 전체 또는 일부를, 상기 이성화 반응기 및/또는 폴리부텐 중합 반응기로 되돌려 보내 재순환시킨다. A method for producing polybutene capable of increasing the production of polybutene by using the C4 mixture as compared with the production of polybutene by maximizing the utilization of isobutene in the C4 mixture is disclosed. In the above polybutene production method, a C4 mixture is supplied to an isomerization reactor, 1-butene is isomerized into 2-butene by a hydrogen isomerization reaction using an isomerization catalyst in the isomerization region, isobutene and 2-butene Separating and separating; A C4 mixture containing 2-butene separated from the isomerization reactor is fed to the skeleton isomerization reactor, and a part of the normal butene is isomerized into isobutene by the skeleton isomerization reaction using the skeleton isomerization catalyst, and the skeletal isomerization The mixture being fed to the isomerization reactor and recycled; And a step of supplying a reaction raw material containing a high concentration of isobutene separated from the isomerization reactor and a polymerization catalyst to a polybutene polymerization reactor to produce polybutene by a polymerization reaction, Are returned to the isomerization reactor and / or the polybutene polymerization reactor and recycled.

Method of modernization of a reactor of a heterogeneous exothermic synthesis

FIELD: chemical industry; a method of modernization of a completely detectable reactor. SUBSTANCE: the invention is pertaining to the method of modernization of a completely detectable reactor. The method provides for modernization of an in-situ reactor of a heterogeneous exothermic synthesis having an external body with several located in it one over another and at some space from each other layers of a catalyst, at realization of which on the initial stage in the upper part of the body form at least the first layer of the catalyst filled in with the first catalyst having the activity picked beforehand; also form several layers of the catalyst located in the lower part of the body in parallel to each other. The layers located in the lower part of the body are filled in with the second catalyst, activity of which exceeds the activity of the first catalyst with which at least the first layer is filled in. The method of an exothermic heterogeneous synthesis with high yield is realized by feeding of the gaseous reagents in the reactor of a synthesis, which has a body with several catalyst layers resting on it, which are placed one over another at some space from each other and in which a reaction of interaction between the gaseous reagents runs. A reaction mixture also is fed at least from the first layer of the catalyst located in the upper part of the body into several layers of the catalyst located in parallel to each other in the lower part of the body. Let the reaction mixture run through the catalyst layers located in the lower part of the body and filled in with the catalyst the reaction activity of which exceeds activity of the catalyst, with which at least the first layer of the catalyst is filled in and the products of the reaction of the synthesis are taken out from the reactor catalyst layers located in the lower part of the body. The technical result is an increased conversion yield and productivity of the reactor at low operational costs and a low power ...

Fixed bed catalytic reactor

Patent RU2019139840A3

РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2019 139 840 A (51) МПК B01J 8/04 (2006.01) B01J 8/06 (2006.01) C07C 29/152 (2006.01) C07C 31/04 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ЗАЯВКА НА ИЗОБРЕТЕНИЕ (21)(22) Заявка: 2019139840, 26.04.2018 (71) Заявитель(и): Л'ЭР ЛИКИД, СОСЬЕТЕ АНОНИМ ПУР Л'ЭТЮД Э Л'ЭКСПЛУАТАСЬОН ДЕ ПРОСЕДЕ ЖОРЖ КЛОД (FR) Приоритет(ы): (30) Конвенционный приоритет: 12.05.2017 EP 17400024.0 (85) Дата начала рассмотрения заявки PCT на национальной фазе: 06.12.2019 (86) Заявка PCT: (87) Публикация заявки PCT: WO 2018/206153 (15.11.2018) R U (54) РЕАКТОР ДЛЯ ПРОВЕДЕНИЯ ЭКЗОТЕРМИЧЕСКИХ РАВНОВЕСНЫХ РЕАКЦИЙ (57) Формула изобретения 1. Реактор для проведения экзотермических равновесных реакций, в котором газообразная сырьевая смесь по меньшей мере частично конвертируется посредством твердого катализатора в готовую смесь, содержащую по меньшей мере один жидкий продукт реакции, конденсируемый при давлении в реакторе и температурах ниже температуры в реакторе, содержащий по меньшей мере две последовательно соединенные реакционные камеры, которые находятся в соединении по текучей среде друг с другом и расположены в общей оболочке реактора, причем каждая реакционная камера содержит следующие последовательно соединенные узлы, которые находятся в соединении по текучей среде друг с другом: (a) зону предварительного нагрева, подходящую для нагрева сырьевой смеси или потока газообразного продукта из реакционной камеры, расположенной выше по потоку, причем в первой реакционной камере в направлении потока газообразной сырьевой смеси необязательно можно обойтись без зоны предварительного нагрева, (b) по меньшей мере одну реакционную зону, содержащую катализатор, активный в отношении экзотермической равновесной реакции, подлежащей проведению, и охлаждающее устройство, находящееся в теплообменной взаимосвязи с катализатором, (c) по меньшей мере одну зону охлаждения, содержащую охлаждающее устройство, подходящее для охлаждения потока частично ...

Псевдоизотермический радиальный реактор

Устройство предназначено для проведения каталитических реакций. Псевдоизотермический радиальный химический реактор имеет цилиндрический корпус, закрытый с противоположных концов плоскими днищами, и зону реакции. В зоне реакции находится слой катализатора и множество расположенных в нем теплообменников. Дополнительно реактор имеет, по меньшей мере, одну вторую зону реакции, в которой находится слой катализатора и множество расположенных в нем теплообменников. При этом вторая зона сообщается с первой зоной реакции. Данная конструкция устройства обеспечивает возможность эффективного контроля протекающей реакции. 2 н. и 5 з.п. ф-лы, 3 ил. ÐÎÑÑÈÉÑÊÀß ÔÅÄÅÐÀÖÈß RU (19) (11) 2 340 391 (13) C2 (51) ÌÏÊ B01J 8/04 (2006.01) ÔÅÄÅÐÀËÜÍÀß ÑËÓÆÁÀ ÏÎ ÈÍÒÅËËÅÊÒÓÀËÜÍÎÉ ÑÎÁÑÒÂÅÍÍÎÑÒÈ, ÏÀÒÅÍÒÀÌ È ÒÎÂÀÐÍÛÌ ÇÍÀÊÀÌ (12) ÎÏÈÑÀÍÈÅ ÈÇÎÁÐÅÒÅÍÈß Ê ÏÀÒÅÍÒÓ (21), (22) Çà âêà: 2005127095/12, 15.01.2004 (30) Êîíâåíöèîííûé ïðèîðèòåò: 29.01.2003 EP 03001868.3 (73) Ïàòåíòîîáëàäàòåëü(è): ÌÅÒÀÍÎË ÊÀÑÀËÅ Ñ.À. (CH) (43) Äàòà ïóáëèêàöèè çà âêè: 27.02.2006 R U (24) Äàòà íà÷àëà îòñ÷åòà ñðîêà äåéñòâè ïàòåíòà: 15.01.2004 (72) Àâòîð(û): ÔÈËÈÏÏÈ Ýðìàííî (CH), ÐÈÖÖÈ Ýíðèêî (IT), ÒÀÐÎÖÖÎ Ìèðêî (CH) (45) Îïóáëèêîâàíî: 10.12.2008 Áþë. ¹ 34 2 3 4 0 3 9 1 (56) Ñïèñîê äîêóìåíòîâ, öèòèðîâàííûõ â îò÷åòå î ïîèñêå: US 5035867 À, 30.07.1991. US 4769220 À, 06.09.1988. SU 1058487 À, 30.11.1983. DE 2803945 À, 03.08.1978. DE 4120788 À, 07.01.1993. (85) Äàòà ïåðåâîäà çà âêè PCT íà íàöèîíàëüíóþ ôàçó: 29.08.2005 2 3 4 0 3 9 1 R U (87) Ïóáëèêàöè PCT: WO 2004/067163 (12.08.2004) C 2 C 2 (86) Çà âêà PCT: EP 2004/000232 (15.01.2004) Àäðåñ äë ïåðåïèñêè: 101000, Ìîñêâà, Ì.Çëàòîóñòèíñêèé ïåð., 10, êâ.15, "ÅÂÐÎÌÀÐÊÏÀÒ", ïàò.ïîâ. È.À.Âåñåëèöêîé, ðåã. ¹ 11 (54) ÏÑÅÂÄÎÈÇÎÒÅÐÌÈ×ÅÑÊÈÉ ÐÀÄÈÀËÜÍÛÉ ÐÅÀÊÒÎÐ (57) Ðåôåðàò: Óñòðîéñòâî ïðåäíàçíà÷åíî äë ïðîâåäåíè êàòàëèòè÷åñêèõ ðåàêöèé. Ïñåâäîèçîòåðìè÷åñêèé ðàäèàëüíûé õèìè÷åñêèé ðåàêòîð èìååò öèëèíäðè÷åñêèé êîðïóñ, çàêðûòûé ñ ïðîòèâîïîëîæíûõ êîíöîâ ïëîñêèìè äíèùàìè, è çîíó ðåàêöèè.  çîíå ðåàêöèè ...

接触反応装置

(57)【要約】本公報は電子出願前の出願データであるた め要約のデータは記録されません。

SYNTHESIS REACTOR, IN PARTICULAR FOR THE CATALYTIC SYNTHESIS OF AMMONIA AND METHANOL

Use of steam eductor to supply oxygen for oxidative reheating in dehydrogenation of C3 + hydrocarbons

A dehydrogenation process, where a hydrocarbon feed is dehydrogenated in a dehydrogenation zone and then oxidatively reheated by the combustion of hydrogen in an oxidation zone containing an oxidation catalyst, is improved by using a stream of dilution steam as an educing fluid to draw oxygen into contact with the effluent from the dehydrogenation zone ahead of the oxidation zone. A stream of dilution steam is often combined with the dehydrogenation zone effluent in order to control the oxygen concentration ahead of the oxidation zone and to lower the hydrogen partial pressure. Educing the oxygen-containing gas for the oxidation zone into the process by using the dilution steam an an educing fluid eliminates the need for compression of the oxygen-containing gas and prevents oxygen from contacting the dehydrogenation zone effluent before the dilution steam is admixed therewith. This process is particularly beneficial in the dehydrogenation of ethylbenzene to produce styrene.

Method and device for reducing the nox and n2o of gases

The method comprises the following steps: conduction of the gas containing N 2 O and NO x over a series of two catalyst beds consisting of one or more zeolites charged with iron; addition of a reduction agent for NO x between the catalyst beds; setting of a temperature of less than 500 °C in the first and second catalyst bed; setting of a gas pressure of at least 2 bar in the two catalyst beds; and the selection of a space velocity in the first and second catalyst bed that achieves a degradation of the N 2 O content of the gas in the first catalyst bed by a maximum of up to 90 %, in relation to the N 2 O content at the entrance to the catalyst bed and an additional degradation of the N 2 O content of the gas in the second catalyst bed by at least 30 % in relation to the N 2 O content at the entrance to the second catalyst bed. The first reaction zone is used to degrade the N 2 O and the second reaction zone reduces the NO x and breaks down at least part of the remaining N 2 O. The inventive device comprises at least one radially traversed catalyst bed.

Apparatus and process for reacting over two catalyst beds

Disclosed is a process for reacting feed in and an apparatus comprising a radial flow reactor (10) including a first catalyst bed disposed between an outer wall (14) and a centerpipe (36) of the vessel (12) and a second catalyst bed disposed within a centerpipe (36). Also disclosed is a method of loading catalyst into the radial flow reactor (10).

Reactor with an annular adsorptively active bed and an annular inert bed

A reactor has a jacket (1), and two annular beds (6). One bed has a chemically and or adsorptively active material (active bed) and one bed (7) has a material which is inert with respect to the chemical reaction that is to be carried out in the reactor (inert bed). The first bed (6) surrounds the second bed (7). The beds are separated from one another by a gas-permeable and or liquid-permeable barrier. A gas feed gas exhaust space (4) is between the jacket and the active bed (6) or optionally between the jacket and an inert bed surrounding the active bed. Gas feed gas exhaust in the form of a hollow central column (2) is provided where the inert bed (7) partially fills a space between and adjacent to the hollow central column and the active bed. The active bed has an inner entry or exit area of a predetermined height and the inert bed extends over 10% of the predetermined height of the inner entry or exit. The inert bed extends over the entire predetermined height of the inner entry or exit area of the active bed.

Reactor and apparatus for purifying by adsorption

The case 2 of the container 1 having a vertical axis X-X contains two adsorbent beds 3,4 in the form of sleeves retained by three cylindrical grates 5, 6, 7. The intermediate grate 6 is axially rigid and radially flexible while the innermost and outermost grates 5,7 are axially flexible and radially rigid. This enables the container and the adsorbent beds to support without damage the successive heating and cooling stages in the course of the adsorbent regeneration stages. Application to the purification of large amounts of air intended to be distilled.

Air cleaning reactor vessel

A vertically disposed cylindrical reactor vessel, containing two coaxial cylinders (4,5) between which a bed (3A,3B) of permeable particles is formed. These cylinders are free to expand axially but are kept rigid in a radial direction by a number of retaining rings.

Method and device for reducing the NOX and N2O of gases

The disclosure involves a method for reducing the content of NO x and N 2 O in gases. The method includes the conduction of a gas containing N 2 O and NO X over a series of two catalyst beds containing of one or more zeolites charged with iron followed by the: addition of a reduction agent for NO X between the catalyst beds. The first catalyst bed reaction zone is used to degrade the N 2 O and the catalyst bed second reaction zone reduces the NO X and breaks down at least part of the remaining N 2 O. The inventive device comprises at least one radially traversed catalyst bed.

Apparatus and process for reacting over two catalyst beds

Disclosed is a process for reacting feed in and an apparatus comprising a radial flow reactor including a first catalyst bed disposed between an outer wall and a centerpipe of the vessel and a second catalyst bed disposed within a centerpipe. Also disclosed is a method of loading catalyst into the radial flow reactor.

Process for reacting over two catalyst beds

A process for reacting feed in and an apparatus comprising a radial flow reactor including a first catalyst bed disposed between an outer wall and a centerpipe of the vessel and a second catalyst bed disposed within a centerpipe. Also disclosed is a method of loading catalyst into the radial flow reactor.

Reactor with an annular adsorptively active bed and an annular inert bed

Es wird ein Reaktor für chemische Reaktionen und/oder adsorptive Trennverfahren beschrieben, a) aufweisend einen Mantel (1), b) aufweisend zwei im Wesentlichen ringförmige Schüttungen (6, 6', 7, 7', 7"), c) wobei eine Schüttung (6, 6') aus einem chemisch und/oder adsorptiv aktivem Material (Aktiv-Schüttung) und eine Schüttung (7, 7', 7") aus einem im Hinblick auf die in dem Reaktor zu realisierende chemische Reaktion inerten Material (Inert-Schüttung) besteht, d) wobei die Schüttungen (6, 6', 7, 7', 7") mittels eines gas- und/oder flüssigkeitsdurchlässigen Korbes voneinander getrennt sind, e) aufweisend einen Gaszuführ- bzw. Gasabführbereich (4) zwischen dem Mantel (1) und der Aktiv-Schüttung (6, 6') und f) aufweisend einen Gaszuführ- bzw. Gasabführbereich in Form eines Kernrohres (2, 2'). A reactor for chemical reactions and / or adsorptive separation processes is described, a) comprising a jacket (1), b) having two substantially annular beds (6, 6 ', 7, 7', 7 "), c) wherein a bed (6, 6 ') of a chemically and / or adsorptively active material (active bed) and a bed (7, 7', 7 ") of a to be realized in the reactor chemical reaction inert material (inert bed), d) wherein the beds (6, 6 ', 7, 7', 7 ") are separated from one another by means of a gas- and / or liquid-permeable basket, e) comprising a Gaszuführ- or Gasabführbereich (4) between the jacket (1) and the active bed (6, 6 ') and f) comprising a Gaszuführ- or Gasabführbereich in the form of a core tube (2, 2 '). Erfindungsgemäß füllt die Inert-Schüttung (7, 7', 7") den zwischen dem Kernrohr (2, 2') und der Aktiv-Schüttung (6, 6') verbleibenden Raum zumindest teilweise aus. According to the invention, the inert bed (7, 7 ', 7 ") at least partially fills the space remaining between the core tube (2, 2') and the active bed (6, 6 ').

FLUID TREATMENT PLANT COMPRISING SEVERAL BEDS OF PARTICLES SUPPORTED BY A SEPARATION GRID

L'invention concerne une installation de traitement de fluide, notamment de gaz, comprenant au moins un récipient (R) de traitement, par exemple un ou plusieurs adsorbeurs ou réacteurs catalytiques, contenant un premier lit (L1) de particules (P1) ayant une première granulométrie (g1), et un deuxième lit (L2) de particules (P2) ayant une deuxième granulométrie. Les premier et deuxième lits (L1, L2) de particules (P1, P2) sont adjacents et séparés par une structure de séparation (G), telle une grille ou une tôle ajourée, comportant des orifices de passage (OG) de fluide ayant une dimension (d), avec : g1 > d > g2. Les premier et deuxième lit de particules peuvent constitués de particules adsorbantes et/ ou catalytiques, notamment de type zéolite, alumine, hopcalite ou analogues. Utilisation d'une installation selon l'invention pour séparer, purifier ou convertir un ou des constituants d'un flux gazeux, tels l'air, les gaz de synthèse ou les hydrocarbures, notamment les oléfines. The invention relates to an installation for treating fluid, in particular gas, comprising at least one treatment vessel (R), for example one or more adsorbers or catalytic reactors, containing a first bed (L1) of particles (P1) having a first particle size (g1), and a second bed (L2) of particles (P2) having a second particle size. The first and second beds (L1, L2) of particles (P1, P2) are adjacent and separated by a separation structure (G), such as a grid or a perforated sheet, comprising passage orifices (OG) of fluid having a dimension (d), with: g1> d> g2. The first and second bed of particles may consist of adsorbent and / or catalytic particles, in particular of zeolite, alumina, hopcalite or the like type. Use of an installation according to the invention for separating, purifying or converting one or more constituents of a gas stream, such as air, synthesis gases or hydrocarbons, in particular olefins.

Enhanced bed separation in a styrene monomer reactor using milled plates

An apparatus for use in radial flow reactors is presented. The apparatus includes a plate of sufficient thickness to impart strength in supporting a solid particle bed, and is milled to have narrow slots allowing the flow of fluid through the plate, while preventing the passage of catalyst through the plate.

Method and apparatus for reducing NOx and N₂O of gases

본 발명의 방법은 철 담지된 하나 이상의 제올라이트로 이루어진 일련의 2개의 촉매층 위로 N 2 O 및 NO x 를 함유하는 가스를 통과시키는 단계; 촉매층들 사이에 NO x 용 환원제를 가하는 단계; 제1 촉매층 및 제2 촉매층에서의 온도를 500℃ 미만으로 설정하는 단계; 2개의 촉매층에서의 기압을 2bar 이상으로 설정하는 단계; 및 제1 촉매층 및 제2 촉매층에서의 공간 속도를, 촉매층의 입구에서의 N 2 O 함량을 기준으로 하여, 제1 촉매층 중의 가스의 N 2 O 함량이 최대 90% 이하 저하되도록, 그리고 제2 촉매층의 입구에서의 N 2 O 함량을 기준으로 하여, 제2 촉매층 중의 가스의 N 2 O 함량이 30% 이상 추가로 저하되도록 선택하는 단계를 포함한다. 제1 반응 영역은 N 2 O를 분해시키는 데 사용되고, 제2 반응 영역은 NO x 를 환원시키고 잔류하는 N 2 O의 적어도 일부를 분해하는 데 사용된다. 본 발명의 장치는 하나 이상의 방사상 선회 촉매층을 포함한다. The process of the present invention comprises the steps of passing a gas containing N 2 O and NO x over a series of two catalyst beds of iron-supported one or more zeolites; Adding a reducing agent for NO x between the catalyst layers; Setting a temperature in the first catalyst layer and the second catalyst layer to less than 500 ° C .; Setting the air pressure in the two catalyst beds to at least 2 bar; And the space velocity at the first catalyst and the second catalyst layer, based on the N 2 O content in the catalyst layer inlet, so that the N 2 O content of the gas in the first catalyst layer decreases up to 90% or less, and the second catalyst layer Based on the N 2 O content at the inlet of, selecting to further reduce the N 2 O content of the gas in the second catalyst layer by 30% or more. The first reaction zone is used to decompose N 2 O and the second reaction zone is used to reduce NO x and to decompose at least a portion of the remaining N 2 O. The apparatus of the present invention comprises one or more radial swirl catalyst layers. 촉매층, N2O, NOx, 공간 속도, 환원제, 철 담지된 제올라이트, 암모니아 Catalyst bed, N2O, NOx, space velocity, reducing agent, iron-supported zeolite, ammonia

Process for carrying out heterogenous exothermal synthesis and reactor for practising thereof

In a process for exothermic and heterogeneous synthesis, for example of ammonia, in which the synthesis gas is reacted in several catalytic beds (6, 7, 13) with axial-radial or only radial flow, said reaction gas is collected at the outlet from the last catalytic bed but one (7) and is transferred to a system for heat recovery (SAC) external to the reactor, and is re-introduced into the last catalytic bed (13).

多相催化合成放热反应用反应器

一种用于多相合成的反应器，其中 ——筒形壳体与催化框基本上相互独立， ——至少将第一个顶部框安装在中间框上面，而该中间框又被装在与所述筒形壳体成一体的密封圈上，所述两个结合在一起的框的底部曲面与反应器底部曲面方向相反， ——所述第一个顶部床中，有一个收集器装在框外壁与筒壳体内壁之间， ——所述的中间床中，有一个骤冷收集器装在构成框的圆筒形内壁内， ——一个气/气热交换器，至少位于最靠近反应器中反应后热气体出口的那个催化框的圆筒形壁内的中心部位。

Multi-bed catalytic converter

A multi-bed catalytic converter comprising: a plurality of catalytic beds (4, 5, 6) which are traversed in series by a process gas, sequentially from a first catalytic bed (4) to a last catalytic bed (6) of said plurality, and at least one inter-bed heat exchanger (7) positioned between a first catalytic bed (4) and a second catalytic bed (5) of said plurality, wherein at least the last catalytic bed (6) of said plurality is adiabatic and is made of fine catalyst with a particle size not greater than 2 mm.

Способ модернизации реактора для гетерогенного экзотермического синтеза и способ повышения его эффективности

Способ модернизации реактора для гетерогенного экзотермического синтеза, включающего внешний корпус, в котором расположен по крайней мере один каталитический слой, соединенный с внешним бойлером для генерации пара высокого давления посредством сопла для выхода прореагировавшего газа и трубопровода, расположенного в сопле, образуя тем самым кольцевой воздушный зазор. В качество преимущества воздушный зазор задает выходной путь для потока газов, охлажденных в бойлере, который предотвращает перегрев сопла.

Process and reactor for heterogeneous exothermic synthesis of formaldehyde

FIELD: industrial organic synthesis. SUBSTANCE: multistage process is conducted in reactors with several in-series connected adiabatic catalytic layers. Gaseous reagents containing methanol and excess oxygen are fed into the first catalytic layer and then passed through adiabatic catalytic layers to achieve partial oxidation of methanol, at least one of layers being passed by regents in radial direction. Reactor for this process is also described. EFFECT: increased productivity of process, reduced explosion hazard, and reduced power consumption. 15 cl, 2 dwg босс пы Го (19) РОССИЙСКОЕ АГЕНТСТВО ПО ПАТЕНТАМ И ТОВАРНЫМ ЗНАКАМ ВИ “” 2 150 995 ' В 01 4 $/04, С 07 С 451/38, (51) МПК? 13) СЛ 471052 12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ РОССИЙСКОЙ ФЕДЕРАЦИИ (21), (22) Заявка: 97118856/04, 09.04.1996 (24) Дата начала действия патента: 09.04.1996 (30) Приоритет: 11.04.1995 СН 1042/95-8 (46) Дата публикации: 20.06.2000 (56) Ссылки: Ц$ 2504502 А, 18.04.1950. ЗЦ 267621 А, 03.07.1970. ЗЧ 448705 А, 02.06.1978. СВ 2122102 А, 11.01.1984. ЕР 0327343 АС, 09.08.1989. СВ 2055606 А, 11.03.1981. (85) Дата перевода заявки РСТ на национальную фазу: 11.11.1997 (86) Заявка РСТ: ЕР 96/01516 (09.04.1996) (87) Публикация РСТ: М/О 96/32189 (17.10.1996) (98) Адрес для переписки: 101000, Москва, Малый Златоустинский пер. 10, кв.15, "Евромаркпат", Веселицкой И.А. (71) Заявитель: Флпориалл Холдингс Лимитед (Е) (72) Изобретатель: Джанкарло СЬОЛИ (1Т) (73) Патентообладатель: Фпориалл Холдингс Лимитед (Е) (54) СПОСОБ И РЕАКТОР ДЛЯ ГЕТЕРОГЕННОГО ЭКЗОТЕРМИЧЕСКОГО СИНТЕЗА ФОРМАЛЬДЕГИДА (57) Реферат: Описывается способ гетерогенного экзотермического синтеза формальдегида в реакторах с несколькими соединенными последовательно адиабатическими каталитическими слоями, включающий следующие стадии: подачу в первый каталитический слой газообразных реагентов, содержащих метанол и избыточное количество кислорода; прохождение газообразн ых реагентов через адиабатические каталитические слои, в процессе которого ...

Method of modification of heterogeneous exothermic synthesis reactor, synthesis reactor for realization of this method and method of conducting heterogeneous exothermic synthesis reactions

FIELD: modification of heterogeneous exothermic synthesis reactors. SUBSTANCE: proposed method includes stages of ensuring first and second catalytic layers in upper and lower parts of reactor, ensuring lowest catalytic layer whose reaction volume is lesser than reaction volume of second catalytic layer and loading lowest catalytic layer with catalyst possessing higher activity as compared with catalyst loaded in other layers. EFFECT: high fractional conversion of reactor. 11 cl, 2 dwg _ ОСД сс ПЧ сэ РОССИЙСКОЕ АГЕНТСТВО ПО ПАТЕНТАМ И ТОВАРНЫМ ЗНАКАМ ЗВО‘” 2 217 230‘ (51) МПК? 13) С2 В 01 4 8/04 12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ РОССИЙСКОЙ ФЕДЕРАЦИИ (21), (22) Заявка: 98121322/12, 25.11.1998 (24) Дата начала действия патента: 25.11.1998 (30) Приоритет: 28.11.1997 ЕР 97203724.6 (43) Дата публикации заявки: 21.09.2000 (46) Дата публикации: 27.11.2003 (56) Ссылки: 4$ 5585074 АЛ, 17.12.1996. $ 4755362 АЛ, 05.07.1988. $Ц 1095980 АЛ, 07.06.1984. $Ц 13083771 АЛ, 07.05.1987. КЦ 2035989 СЛ, 27.05.1995. КУ 2045330 СЛ, 10.10.1995. 4$ 2646391 АЛ, 21.07.1953. $ 2415855 СЛ, 12.07.1949. (98) Адрес для переписки: 103062, Москва, ул. Покровка, д.27, стр.1 АГ, Кооперативное агентство интеллектуальной собственности "ИНТЭЛС", О.М.Дьяконовой (72) Изобретатель: ПАГАНИ Джорджио (СН), ФИЛИППИ Урманно (СН) (73) Патентообладатель: АММОНИА КАЗАЛИ С.А. (СН) (74) Патентный поверенный: Дьяконова Ольга Михайловна (54) СПОСОБ МОДИФИКАЦИИ ГЕТЕРОГЕННОГО ЭКЗОТЕРМИЧЕСКОГО РЕАКТОРА СИНТЕЗА, РЕАКТОР СИНТЕЗА И СПОСОБ ОСУЩЕСТВЛЕНИЯ ГЕТЕРОГЕННЫХ ЭКЗОТЕРМИЧЕСКИХ РЕАКЦИЙ СИНТЕЗА (57) Способ модификации гетерогенного экзотермического реактора синтеза включает стадии обеспечения, по крайней мере, первого и, по крайней мере, второго каталитического слоя в верхней и, соответственно, нижней части реактора, обеспечения дополнительно самого нижнего каталитического слоя в нижней части реактора, имеющего реакционный объем меньший, чем реакционный объем второго каталитического слоя, и загрузки самого нижнего ...

SYSTEMS AND METHODS FOR OXIDATIVE COMBINATIONS OF METHANE

РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2020 102 298 A (51) МПК C07C 2/84 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ЗАЯВКА НА ИЗОБРЕТЕНИЕ (21)(22) Заявка: 2020102298, 09.07.2018 (71) Заявитель(и): ЛЮММУС ТЕКНОЛОДЖИ ЛЛС (US) Приоритет(ы): (30) Конвенционный приоритет: (43) Дата публикации заявки: 10.08.2021 Бюл. № 22 (85) Дата начала рассмотрения заявки PCT на национальной фазе: 07.02.2020 US 2018/041322 (09.07.2018) (87) Публикация заявки PCT: A WO 2019/010498 (10.01.2019) Адрес для переписки: 190900, BOX 1125, Санкт-Петербург, Нилова Мария Иннокентьевна R U (57) Формула изобретения 1. Способ получения олефина, включающий: а) обеспечение реактора, имеющего изотермическую секцию, причем указанная изотермическая секция содержит катализатор, способный стимулировать реакцию окислительного сочетания метана (ОСМ), и находится в тепловом контакте с теплопередающей средой; и б) введение газовой смеси в изотермическую секцию реактора, причем указанная газовая смесь содержит кислород (O2) и метан (CH4), в результате чего по меньшей мере примерно 75 мол. % O2 вступает в реакцию с CH4 с образованием выходящего потока, содержащего углеводородные соединения, имеющие два или более атомов углерода (соединения C2+), и не содержащие соединения C2+ примеси. 2. Способ по п. 1, в котором реакция ОСМ имеет селективность по соединениям C2+ по меньшей мере примерно 50% при 700°C. 3. Способ по п. 1, в котором реакция ОСМ имеет селективность по соединениям C2+ по меньшей мере примерно 60% при 750°C. 4. Способ по п. 1, в котором реакция ОСМ имеет селективность по соединениям C2+ по меньшей мере примерно 65% при 800°C. Стр.: 1 A 2 0 2 0 1 0 2 2 9 8 (54) СИСТЕМЫ И СПОСОБЫ ОКИСЛИТЕЛЬНОГО СОЧЕТАНИЯ МЕТАНА 2 0 2 0 1 0 2 2 9 8 (86) Заявка PCT: (72) Автор(ы): ЦИЦЕРОН, Джоэль (US), ШЕРИДАН, Дэвид (US), ТЮРК, Грегори Дж. (US), ЛАКХАПАТРИ, Сатиш (US), ФЭНЬ, Жун (US), РАДЕЛЛИ, Гвидо (US), МАРТЕНС, Францискус Дж.А. (CA), МАККОРМИК, Джарод (US), РОЗЕНБЕРГ, Дэниел (US), ЦУРКЕР, ...

Method of mass exchange between a liquid and a gaseous phases, column with a filler for the method realization and a method of upgrading the column for mass exchange

FIELD: mass exchange between a liquid and a gaseous phases. SUBSTANCE: the invention presents a method of mass exchange between a liquid and a gaseous phases, a column with a filler for the method realization and a method of upgrading the column for mass exchange. The method of a mass exchange between a liquid and a gaseous phases in the filler column, that has an outer housing, inside which there are several filled sections located one over another, cross-section of which is less than cross-section of the housing, provides, that a liquid and a gas phases are fed into the column with the filler. The liquid phase passes through some sections mainly in the axial direction, and the gas phase passes through some sections mainly in a radial direction. The liquid phase is collected and distributed between the adjacent sections. Then the liquid and the gas phases are removed from the column with the filler. The invention allows to increase efficiency of the mass exchange at low investments and operational costs. EFFECT: the invention allows to increase efficiency of the mass exchange at low investments and operational costs. 42 cl, 6 dwg сссессс ПЧ сэ РОССИЙСКОЕ АГЕНТСТВО ПО ПАТЕНТАМ И ТОВАРНЫМ ЗНАКАМ (19) ВИ "” 2 229 333. (51) МПК? 13) С2 В 01 + 19/00 12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ РОССИЙСКОЙ ФЕДЕРАЦИИ (21), (22) Заявка: 2000124539/15, 23.02.1999 (24) Дата начала действия патента: 23.02.199911.1-42 (30) Приоритет: 25.02.1998 ЕР 98200587.8 (43) Дата публикации заявки: 27.08.2002 (46) Дата публикации: 27.05.2004 (56) Ссылки: КУ 2056163 СЛ, 20.03.1996. ЗЧ 1426607 АЛ, 30.09.1988. КЦ 2049542 СЛ, 10.12.1995. ОЕ 1243143 АЛ, 29.06.1967. ($ 42566174 АЛ, 17.03.1981. ЕР 0386692 АЛ, 12.09.1990. (85) Дата перевода заявки РСТ на национальную фазу: 25.09.2000 (86) Заявка РСТ: ЕР 99/01275 (23.02.1999) (87) Публикация РСТ: МГО 99/43428 (02.09.1999) (98) Адрес для переписки: 101000, Москва, М.Златоустинский пер., 10, кв.15, "ЕВРОМАРКПАТ", пат.пов. И.А.Веселицкой (72) Изобретатель: ...

Method of modification of reactor for heterogeneous exothermic synthesis and method of enhancing its efficiency

Использование: изобретение относится к модернизации реакторов. Способ модернизации реактора для гетерогенного экзотермического синтеза, типа, включающего внешний корпус, в котором расположен по крайней мере один каталитический слой, соединенный с внешним бойлером для генерации пара высокого давления посредством сопла для выхода прореагировавшего газа и трубопровода, расположенного в сопле, образуя тем самым кольцевой воздушный зазор. Воздушный зазор задает выходной путь для потока газов, охлажденных в бойлере, который предотвращает перегрев сопла. Изобретение позволяет восстанавливать более высокий термальный уровень реакционного тепла. 2 с. и 6 з.п. ф-лы, 3 ил. 9% с Пы ГЭ РОССИЙСКОЕ АГЕНТСТВО ПО ПАТЕНТАМ И ТОВАРНЫМ ЗНАКАМ (19) ВИ "” 2 137 538. (51) МПК 13) Сл В 01 + 8/04 12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ РОССИЙСКОЙ ФЕДЕРАЦИИ (21), (22) Заявка: 94039279/25, 28.10.1994 (24) Дата начала действия патента: 28.10.1994 (30) Приоритет: 29.10.1993 СН 3257/93 (46) Дата публикации: 20.09.1999 (56) Ссылки: ЕР 386692 А2, 12.09.90. ЗЦ 1773236 АЗ, 30.10.92. 4$ 4935210 А, 19.06.90. 4$ 5254316 А, 19.10.93. СН 666197 АЪ, 15.07.88. ЕР 0142170 АД, 22.05.85. (98) Адрес для переписки: 103735, Москва, ул.Ильинка 5/2, Союзпатент, пат.поверенному Томской Е.В. (71) Заявитель: Аммониа Казале С.А. (СН), Умберто Зарди (1Т) (72) Изобретатель: Умберто Зарди (1Т), Джорджо Пагани (1Т), Филиппи Эрманно (1Т) (73) Патентообладатель: Аммониа Казале С.А. (СН), Умберто Зарди (1Т) (54) СПОСОБ МОДЕРНИЗАЦИИ РЕАКТОРА ДЛЯ ГЕТЕРОГЕННОГО ЭКЗОТЕРМИЧЕСКОГО СИНТЕЗА И СПОСОБ ПОВЫШЕНИЯ ЕГО ЭФФЕКТИВНОСТИ (57) Реферат: Использование: изобретение относится к модернизации реакторов. Способ модернизации реактора для гетерогенного экзотермического синтеза, типа, включающего внешний корпус, в котором расположен по крайней мере один каталитический слой, соединенный с внешним бойлером для генерации пара высокого давления посредством сопла для выхода прореагировавшего газа и трубопровода, расположенного в сопле, образуя тем ...

A kind of combined type fixed bed reactors and the device formed by it

本发明提供了一种组合式固定床反应器，包括，壳体、等温反应床层、绝热反应床层和气体分布器，气体分布器、等温反应床层、绝热反应床层依次套设，且彼此间设有间隙；所述等温反应床层内设置有换热结构，其包括沿轴向贯穿所述等温反应床层的若干换热件；还包括导气结构。使得工艺气进入催化剂床层后，沿径向流动，这种外扩式的流动方式，对于气体量增加的反应而，避免了气体流速的提高，延长了工艺气在催化剂床层内的停留时间，促进反应能够完全进行，提高了催化剂的利用率。同时由于绝热反应床层设置在等温反应床层的外部，有利于吸收等温反应床层的热量，一方面减少了换热量，另一方面促进了绝热反应的进行。

DEVICE FOR TREATING AT LEAST ONE FLUID, APPLICATION FOR TREATING AN AIR FLOW AND METHOD FOR FILLING SUCH A DEVICE WITH A MASS OF GRAIN MATERIAL

Method and apparatus for multiple loading of adsorbent for radial flow vessels

Method for heterogeneous synthesis

Improved process for heterogeneous synthesis and related reactors according to which the synthesis catalyst is distributed in three catalytic beds (C1, C22, C3) either axial-radial or radial, control of the temperature between beds being effected by means of fresh quench gas (4) between the first and the second bed and by means of indirect cooling with an exchanger (S2) between the second and the third bed of the gas leaving the second bed, using fresh gas which is heated inside the tubes of said exchanger.

Process for effecting mass transfer between liquid phase and gaseous phase

在填充型交换柱内进行液相和气相之间物质转移的方法,交换柱具有外壳,用以容纳至少一个填料盛篮,上述两相通过它时引起产生反向形式的流动,该方法包括以下步骤:通过网篮的透气表面供给气相至上述至少一个网篮,网篮的透气表面大于网篮的横截面,气相最好主要沿径向流动。

Steam reformer with internal heat recovery

The inventive apparatus for the execution of endothermic reactions between gaseous reactants at heightened temperature and increased pressure encompasses the following main components: an inner isolating hull (33) for conveying the feed substances from their inlet (E) along the clearance between the pressure wall (31) of the apparatus and said hull; a tube-bundle heat exchanger (39'), placed within said hull for the internal heat recovery, whereby the feed substances are outside of the tubes (39) of said heat exchanger; a catalyst material, disposed in the lower part of said heat exchanger and/or after it in flowing direction; heating means (37, 37'') arranged within said catalyst material for the supply of heat energy to the reactants at the region of the final conversion, whereby the reaction products proceed inside of the said tubes, with heat delivery to the entering feed substances to the outlet of the apparatus. All said parts are arranged within a pressure vessel (31). Processes for producing a hydrogen-rich gas may be carried out by using an apparatus as indicated. For that the necessary amount of feed substances in form of steam and hydrocarbons and the necessary heat-energy in form of electrical energy and/or oxygen-containing gas for the partial oxidation of the reducing components in the feed substances are fed into said apparatus and the hydrogen-rich reaction products are withdrawn therefrom. Such processes are useful for the production of the feed stock to be used in the NH3- and/or CH3OH-synthesis.

Split-flow contactor

FIELD: machine building. SUBSTANCE: split-flow contactor includes housing having the first head and the second head located on it, two or more separate fixed beds located in the housing cross section, one or more flow passages for bypass of each fixed bed, which have no obstacles, and one or more partition walls located between fixed beds. Each fixed bed includes one or more catalysts, one or more ion exchange resins, one or more absorbents, one or more adsorbents or any of their combinations. According to the tank modernisation method, two or more supporting sieves are arranged inside the tank; at that, each sieve is located separately; one or more obstacle-free flow passages through each of the above supporting sieves is formed, and one or more partition walls are arranged between adjacent supporting sieves. Besides, one or more partition walls are mainly perpendicular to flow passages. According to the method for bringing into contact of one or more fluid media and one or more solid products, the supplied material is introduced to contactor, the first portion of the supplied material is passed through the first fixed bed so that the first effluent is obtained; the second portion of the supplied material is passed through one or more flow passages bypassing the first fixed bed. After that, the second portion is passed through the second fixed bed so that the second effluent is obtained; the first effluent is passed through one or more flow passages bypassing the second fixed bed and the first and the second effluents are combined. According to the other version, split-flow contactor includes the housing having the first head and the second head located on it, two or more separate fixed beds located in the housing cross section and mixing volume located between beds. Each fixed bed includes one or more catalysts, one or more ion exchange resins, one or more absorbents, one or more adsorbents or any of their combinations, and each bed includes one or more circular ...

PSEUDOISOTHERMAL RADIAL REACTOR

ÐÎÑÑÈÉÑÊÀß ÔÅÄÅÐÀÖÈß (19) RU (11) 2005 127 095 (13) A (51) ÌÏÊ B01J 8/04 (2006.01) ÔÅÄÅÐÀËÜÍÀß ÑËÓÆÁÀ ÏÎ ÈÍÒÅËËÅÊÒÓÀËÜÍÎÉ ÑÎÁÑÒÂÅÍÍÎÑÒÈ, ÏÀÒÅÍÒÀÌ È ÒÎÂÀÐÍÛÌ ÇÍÀÊÀÌ (12) ÇÀßÂÊÀ ÍÀ ÈÇÎÁÐÅÒÅÍÈÅ (21), (22) Çà âêà: 2005127095/12, 15.01.2004 (71) Çà âèòåëü(è): ÌÅÒÀÍÎË ÊÀÑÀËÅ Ñ.À. (CH) (30) Ïðèîðèòåò: 29.01.2003 EP 03001868.3 (43) Äàòà ïóáëèêàöèè çà âêè: 27.02.2006 Áþë. ¹ 6 (86) Çà âêà PCT: EP 2004/000232 (15.01.2004) (74) Ïàòåíòíûé ïîâåðåííûé: Âåñåëèöêà Èðèíà Àëåêñàíäðîâíà Àäðåñ äë ïåðåïèñêè: 101000, Ìîñêâà, Ì.Çëàòîóñòèíñêèé ïåð., 10, êâ.15, "ÅÂÐÎÌÀÐÊÏÀÒ", ïàò.ïîâ. È.À.Âåñåëèöêîé, ðåã. ¹ 11 R U (57) Ôîðìóëà èçîáðåòåíè 1. Ïñåâäîèçîòåðìè÷åñêèé ðàäèàëüíûé õèìè÷åñêèé ðåàêòîð äë ïðîâåäåíè êàòàëèòè÷åñêèõ ðåàêöèé, èìåþùèé ïî ñóùåñòâó öèëèíäðè÷åñêèé êîðïóñ (2), çàêðûòûé ñ ïðîòèâîïîëîæíûõ êîíöîâ ñîîòâåòñòâóþùèìè ïëîñêèìè äíèùàìè (3 è 4), è çîíó (8) ðåàêöèè, â êîòîðîé íàõîäèòñ ñëîé (11) ñîîòâåòñòâóþùåãî êàòàëèçàòîðà è ìíîæåñòâî ðàñïîëîæåííûõ â íåì òåïëîîáìåííèêîâ (22), îòëè÷àþùèéñ òåì, ÷òî îí èìååò ïî ìåíüøåé ìåðå îäíó âòîðóþ çîíó (26) ðåàêöèè, â êîòîðîé íàõîäèòñ ñëîé (29) ñîîòâåòñòâóþùåãî êàòàëèçàòîðà è ìíîæåñòâî ðàñïîëîæåííûõ â íåì òåïëîîáìåííèêîâ (36) è êîòîðà ñîîáùàåòñ ñ ïåðâîé çîíîé (8) ðåàêöèè. 2. Õèìè÷åñêèé ðåàêòîð ïî ï.1, îòëè÷àþùèéñ òåì, ÷òî ïåðâà è âòîðà çîíû (8 è 26) ðåàêöèè ðàñïîëîæåíû ïîñëåäîâàòåëüíî. 3. Õèìè÷åñêèé ðåàêòîð ïî ï.2, îòëè÷àþùèéñ òåì, ÷òî òåïëîîáìåííèêè (22), ðàñïîëîæåííûå ïî ìåíüøåé ìåðå â îäíîé èç çîí (8, 26) ðåàêöèè, ñîåäèíåíû ñ òðóáîïðîâîäàìè, âûõîä ùèìè èç ðåàêòîðà íàðóæó. 4. Õèìè÷åñêèé ðåàêòîð ïî ï.3, îòëè÷àþùèéñ òåì, ÷òî òåïëîîáìåííèêè (22, 36), ðàñïîëîæåííûå â äâóõ çîíàõ (8, 26) ðåàêöèè, ñîîáùàþòñ äðóã ñ äðóãîì. 5. Õèìè÷åñêèé ðåàêòîð ïî ï.4, îòëè÷àþùèéñ òåì, ÷òî ïî ìåíüøåé ìåðå îäèí èç òåïëîîáìåííèêîâ (22, 36) âûïîëíåí â âèäå ïëîñêîãî ïîëîãî ïð ìîóãîëüíèêà. 6. Õèìè÷åñêèé ðåàêòîð ïî ï.5, îòëè÷àþùèéñ òåì, ÷òî òåïëîîáìåííèêè (22) ðàñïîëîæåíû ðàäèàëüíî âîêðóã îñè (À-À) ðåàêòîðà. 7. Ñïîñîá îïòèìèçàöèè ïñåâäîèçîòåðìè÷åñêèõ êàòàëèòè÷åñêèõ ðåàêöèé, ...

Method and reactor for heterogeneous exothermic synthesis of formaldehyde

FIELD: method and reactors for heterogeneous exothermic synthesis of formaldehyde. SUBSTANCE: method of heterogeneous exothermic synthesis of formaldehyde in reactor with several successively connected adiabatic layers of catalyst provides for supply into reactor of gaseous reagents containing methanol and excessive amount of oxygen, and passage of gaseous reagents through adiabatic layers to partially oxidized methanol. In this case, methanol supplied to reactor is separated into several parts. The first part comprising the larger part amounting to about 82% of total quantity of methanol supplied to synthesis reactor is supplied to the first catalytic bed and, at least, the second part is supplied to the second catalytic bed located behind the first catalytic bed. Reactor (its versions) is offered for embodiment of claimed method. EFFECT: higher process efficiency, reduced possibility of reagent explosion, simplified design of reactor. 17 cl, 2 dwg, 3 ex оэгэбгс пы сэ (19) РОССИЙСКОЕ АГЕНТСТВО ПО ПАТЕНТАМ И ТОВАРНЫМ ЗНАКАМ ВИ "” 2 156 160 ' В 01 4 $/04, С 07 С 451/38, (51) МПК? 13) С2 471052 12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ РОССИЙСКОЙ ФЕДЕРАЦИИ (21), (22) Заявка: 97118855/04, 09.04.1996 (24) Дата начала действия патента: 09.04.1996 (30) Приоритет: 11.04.1995 СН 1041/95-6 (46) Дата публикации: 20.09.2000 (56) Ссылки: Ц$ 2504402 А, 18.04.1950. ЗЦ 448705 А, 02.06.1978. ЕР 0327343 А2, 09.08.1989. $Ц 1058487 А, 30.11.1983. 5Ц 14231148 АЛ, 15.09.1988. КЦ 21352174 СЛ, 27.08.1999. КЦ 2136359 СЛ, 10.09.1999. (85) Дата перевода заявки РСТ на национальную фазу: 11.11.1997 (86) Заявка РСТ: ЕР 96/01517 (09.04.1996) (87) Публикация РСТ: М/О 96/32190 (17.10.1996) (98) Адрес для переписки: 101000, Москва, Малый Златоустинский пер., д.10, кв.15, "ЕВРОМАРКПАТ", Веселицкой И.А. (71) Заявитель: ФЛОРИАЛЛ ХОЛДИНГС ЛИМИТЕД (Е) (72) Изобретатель: Джанкарло СЬОЛИ (1Т) (73) Патентообладатель: ФЛОРИАЛЛ ХОЛДИНГС ЛИМИТЕД (Е) (54) СПОСОБ И РЕАКТОР ДЛЯ ГЕТЕРОГЕННОГО ЭКЗОТЕРМИЧЕСКОГО СИНТЕЗА ...

Hydrogen generator and hydrogenation apparatus

本发明的目的在于提高脱氢反应或氢化反应的效率。本发明的氢发生装置是在催化剂的存在下，通过有机氢化物的脱氢反应产生氢的装置，该装置具有多管结构的反应器(10)，该反应器(10)具备下述两个区域，即供给用于产生脱氢反应所必须的热的燃料、具有该燃料的燃烧所利用的燃烧催化剂的区域(12)；和具有脱氢反应所必须的脱氢催化剂的区域(11)；这两个区域以壁为间隔，在直径方向上相邻。本发明的氢化反应装置是在催化剂的存在下，通过不饱和烃和氢的氢化反应合成有机氢化物的装置，该装置具有多管结构的反应器(10)，该反应器(10)具备下述两个区域，即除去氢化反应中产生的热的区域(12)；和具有氢化反应所必须的氢化催化剂的区域(11)，这两个区域以壁为间隔，在直径方向上相邻。

Heterogeneous synthetic improving one's methods and reactor

多相合成改进方法及其反应器，其中将合成催化 剂分布在三个轴向一径向或径向催化剂床中，温度控 制是在第一和第二床层之间用新鲜气进行骤冷并在 第二和第三床层之间借助换热器用其管中被加热的 新鲜气间接冷却离开第二床层的气体。

Reactor

一种反应器(3)，包括反应部分(32a、32b)和去除部分(33a、33b)。反应部分(32a、32b)配置成借助于未反应的物质的反应而产生至少两种产物。所述去除部分(33a、33b)配置成从所述至少两种产物选择性地吸留至少一种产物，以便分离和去除该至少一种产物。所述去除部分(33a、33b)包括吸收剂(330a、330b)和冷却单元(35a、35b)。所述吸收剂(330a、330b)在选择性地吸留所述至少一种产物时释放热量。所述冷却单元(35a、35b)配置成去除由吸收剂(330a、330b)所释放的热量。

Multilayer catalytic converter with interlayer cooling

Изобретение относится к многослойным каталитическим конвертерам с межслойным охлаждением, к комбинациям конструктивных элементов конвертера, и способу охлаждения газового потока данным устройством. Многослойный каталитический конвертер, включающий по меньшей мере первый каталитический слой, второй каталитический слой и теплообменник, расположенный между первым слоем и вторым слоем и приспособленный для передачи тепла от горячего исходящего потока первого слоя хладагенту, причем теплообменник содержит несколько сложенных пакетом круглых пластин, представляющих собой сплошные круглые пластины или кольцевые пластины, при этом между соседними пластинами образованы промежутки, а исходящий поток первого каталитического слоя и хладагент подаются, соответственно, в чередующиеся промежутки. Способ осуществляется в процессе работы устройства. Технический результат – повышение эффективности теплопередачи и компактности конструкции. 2 н. и 21 з.п. ф-лы, 9 ил. РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2 746 734 C1 (51) МПК B01J 8/04 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (52) СПК B01J 8/00 (2021.02); B01J 8/04 (2021.02) (21)(22) Заявка: 2019139379, 21.02.2018 (24) Дата начала отсчета срока действия патента: (73) Патентообладатель(и): КАСАЛЕ СА (CH) Дата регистрации: 19.04.2021 11.05.2017 EP 17170546.0 (45) Опубликовано: 19.04.2021 Бюл. № 11 (85) Дата начала рассмотрения заявки PCT на национальной фазе: 11.12.2019 (86) Заявка PCT: 2 7 4 6 7 3 4 R U (87) Публикация заявки PCT: WO 2018/206167 (15.11.2018) Адрес для переписки: 105082, Москва, пер. Спартаковский, 2, стр. 1, секция 1, этаж 3, ЕВРОМАРКПАТ (54) МНОГОСЛОЙНЫЙ КАТАЛИТИЧЕСКИЙ КОНВЕРТЕР С МЕЖСЛОЙНЫМ ОХЛАЖДЕНИЕМ (57) Реферат: Изобретение относится к многослойным содержит несколько сложенных пакетом круглых каталитическим конвертерам с межслойным пластин, представляющих собой сплошные охлаждением, к комбинациям конструктивных круглые пластины или кольцевые пластины, при ...

Reactor plant with extraction of intermediate product

FIELD: process engineering. SUBSTANCE: invention relates to reactor plant with several interconnected catalyst layers and discharge device that serves to extract product from between two adjacent catalyst layers. Said reactor plant comprises several interconnected reactors including, at least, two reactors separated by intermediate chamber. Reactor plant comprises stock feed line to feed flow of starting reagents to inlets of several reactors. Reactor plant comprises discharge device communicated with intermediate chamber to direct first portion of flow outcoming from first reactor of aforesaid two rectors into first chamber and to direct second portion of flow to inlet of another reactor of said two reactors. First chamber makes product extraction chamber that can separate product components. EFFECT: higher yield of finished product. 9 cl, 3 dwg, 4 tbl, 2 ex РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) 2 444 402 (13) C2 (51) МПК B01J 19/24 (2006.01) B01J 8/00 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (21)(22) Заявка: 2009104699/05, 15.06.2007 (24) Дата начала отсчета срока действия патента: 15.06.2007 (73) Патентообладатель(и): ЮОП ЛЛК (US) (43) Дата публикации заявки: 20.08.2010 Бюл. № 23 2 4 4 4 4 0 2 (45) Опубликовано: 10.03.2012 Бюл. № 7 (56) Список документов, цитированных в отчете о поиске: WO 2006012150 А2, 02.02.2006. US 6454932 В1, 24.09.2002. US 5689014 A, 18.11.1997. US 5211838 A, 18.05.1993. US 4975178 A, 04.12.1992. RU 2205181 C2, 27.05.2003. 2 4 4 4 4 0 2 R U (86) Заявка PCT: US 2007/071363 (15.06.2007) C 2 C 2 (85) Дата начала рассмотрения заявки PCT на национальной фазе: 12.02.2009 (87) Публикация заявки РСТ: WO 2008/008597 (17.01.2008) Адрес для переписки: 109012, Москва, ул. Ильинка, 5/2, ООО "Союзпатент" (54) РЕАКТОРНАЯ УСТАНОВКА С ИЗВЛЕЧЕНИЕМ ПРОМЕЖУТОЧНОГО ПРОДУКТА (57) Реферат: Изобретение относится к реактору с несколькими слоями катализатора, соединенными друг с другом и с отводящим устройством, ...

Reactor system with interstage product removal

본 발명은 (1) 유체 유동 연통되게 연결되고, 단계간 위치(33)에 의해 분리되는 한쌍 이상의 반응기(12a, b)를 갖는 복수의 반응기(12); (2) 복수의 반응기(12a, b)의 하나 초과의 주입구(21)로 반응물 공급물 스트림을 분리하여 주입하는 라인(25); 및 (3) 단계간 위치(33)와 유체 연통되며, 상기 반응기 쌍(12a, b) 중 하나의 반응기(12a)로 배출되는 생성물 스트림(32a)의 첫번째 분획을 제1 위치(40)로 유도시키며, 생성물 스트림의 두번째 분획을 상기 반응쌍(12a, b) 중 다른 반응기(12b)의 주입구(21b)로 유도시킬 수 있는 전환기(30)를 갖는 것인 반응기 시스템(10)를 제공한다. 유체 유동, 단계간 위치, 반응기 시스템, 단계간 생성물 제거 (1) a plurality of reactors (12) connected in fluid flow communication and having at least one pair of reactors (12a, b) separated by an interstage position (33); (2) a line 25 for separately injecting a reactant feed stream into one or more inlets 21 of a plurality of reactors 12a, b; And (3) directing the first fraction of the product stream (32a) in fluid communication with the interstage location (33) and exiting the reactor (12a) of one of the reactor pairs (12a, b) And a diverter 30 capable of leading a second fraction of the product stream to the inlet 21b of the other of the reaction pairs 12a, b. Fluid flow, interstage location, reactor system, stepwise product removal

Catalyst bed reactor

FIELD: chemistry. SUBSTANCE: disclosed is a catalyst bed for a chemical reactor, having a radial-cylindrical geometry and comprising at least one manifold made in the form of a gas-permeable cylindrical wall, comprising at least a first catalyst and a second catalyst, wherein the particle size of the second catalyst is smaller than that of the first catalyst, and a catalyst layer is formed from the first catalyst, adjacent to the manifold and in contact with it. EFFECT: use of a catalyst with a particularly small particle size in a catalytic chemical reactor without adversely affecting the operation and reliability of the catalyst bed. 22 cl, 4 dwg РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2 769 913 C2 (51) МПК B01J 8/02 (2006.01) C01C 1/04 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (52) СПК B01J 8/02 (2022.01); C01C 1/04 (2022.01) (21)(22) Заявка: 2019141229, 23.05.2018 (24) Дата начала отсчета срока действия патента: (73) Патентообладатель(и): КАСАЛЕ СА (CH) Дата регистрации: 08.04.2022 02.06.2017 EP 17174266.1 (43) Дата публикации заявки: 09.07.2021 Бюл. № 19 (45) Опубликовано: 08.04.2022 Бюл. № 10 (85) Дата начала рассмотрения заявки PCT на национальной фазе: 09.01.2020 2 7 6 9 9 1 3 Приоритет(ы): (30) Конвенционный приоритет: (56) Список документов, цитированных в отчете о поиске: WO 1999020384 A1, 29.04.1999. WO 2001023080 A1, 05.04.2001. DE 69504179 T2, 12.05.1999. RU 2283174 C1, 10.09.2006. RU 2674950 C1, 13.12.2018. SU 1114458 A1, 23.09.1984. R U 23.05.2018 (72) Автор(ы): РИЦЦИ Энрико (IT) EP 2018/063478 (23.05.2018) C 2 C 2 (86) Заявка PCT: (87) Публикация заявки PCT: R U 2 7 6 9 9 1 3 WO 2018/219731 (06.12.2018) Адрес для переписки: 105082, Москва, Спартаковский пер., д. 2, стр. 1, секция 1, этаж 3, "ЕВРОМАРКПАТ", Веселицкий Максим Борисович (54) РЕАКТОР СО СЛОЕМ КАТАЛИЗАТОРА (57) Реферат: Предложен слой катализатора для химического реактора, имеющий радиальноцилиндрическую геометрию и включающий по ...

Membrane reactor for producing CO- and CO2 -free hydrogen

In a reactor and a method for the conversion of methanol to hydrogen wherein the reactor comprises first and second chambers divided by a membrane which is permeable for hydrogen and CO but not for CO 2 , the methanol is converted in the first chamber by a catalyst disposed therein to a gas mixture comprising hydrogen, carbon monoxide and carbon dioxide, and the hydrogen and carbon monoxide pass through the membrane into the second chamber wherein the CO is converted by another catalyst disposed therein to methane.

Integrated hydrocarbon reforming system and controls

A hydrocarbon reformer system including a first reactor configured to generate hydrogen-rich reformate by carrying out at least one of a non-catalytic thermal partial oxidation, a catalytic partial oxidation, a steam reforming, and any combinations thereof, a second reactor in fluid communication with the first reactor to receive the hydrogen-rich reformate, and having a catalyst for promoting a water gas shift reaction in the hydrogen-rich reformate, and a heat exchanger having a first mass of two-phase water therein and configured to exchange heat between the two-phase water and the hydrogen-rich reformate in the second reactor, the heat exchanger being in fluid communication with the first reactor so as to supply steam to the first reactor as a reactant is disclosed. The disclosed reformer includes an auxiliary reactor configured to generate heated water/steam and being in fluid communication with the heat exchanger of the second reactor to supply the heated water/steam to the heat exchanger.

Systems and methods for carbon monoxide production by reduction of carbon dioxide with elemental sulfur

Thermoneutral systems and methods for producing carbon monoxide (CO) and sulfur dioxide (SO 2 ) are disclosed. The systems can include a first reaction zone and a second reaction zone, where heat generated in the first reaction zone is sufficient to drive a carbon dioxide gas (CO 2 (g)) and elemental sulfur gas (S(g)) reaction to produce a product stream that includes CO(g) and SO 2 (g).

A kind of metaformaldehyde manufacturing technique method and extractive reaction tower

本发明公开了一种三聚甲醛生产工艺方法及萃取反应塔，其中萃取反应塔包括设在底部的萃取剂进口、设在顶部的反应物采出口和从下至上依次设置的多级萃取反应单元，相邻萃取反应单元通过带孔塔板隔开，且相邻萃取反应单元之间还设有降液管，所述萃取反应单元内还设有固体酸催化剂。本发明具有超过45％的甲醛转化率，且具有反应过程蒸汽消耗量小，设备投入下等特点。

Method and apparatus for multiple packing of adsorbent for radial flow type vessel

(57)【要約】 【課題】 容器に、半径方向に同中心に配置された、異 なる粒状物材料の少なくとも２つの別個の層を充填する ための改良方法及び装置を提供すること。 【解決手段】 隔壁６０１が回転アームの所望される界 面位置の直上位置から伸延される。隔壁６０１は回転ア ーム２３０と一体化されあるいは回転アームから垂下さ れ得、回転アーム内の孔を出た粒状材料が円錐状に拡散 するのを抑制するとともに、回転アームから吸着剤床面 に自由落下するに際しての２つの吸着剤の混合を減少さ せる。