24results about "Organic dehydrogenation" patented technology

The present disclosure provides a method of operating a dehydrogenation reactor requiring vacuum pressure during the dehydrogenation reaction, the method including feeding a hydrocarbon to a reactor comprising a catalyst bed and configured to dehydrogenate the hydrocarbon under vacuum pressure; purging the reactor to remove remaining hydrocarbon; regenerating the catalyst bed with air from a regeneration air source; and evacuating the reactor to induce vacuum pressure, wherein the evacuating comprises passing a motive gas through a reactor evacuation ejector in fluid connection with the reactor, wherein the motive gas is nitrogen or air in the absence of steam. A system for dehydrogenation of a hydrocarbon is also provided, which includes a dehydrogenation reactor and a reactor evacuation ejector in fluid communication with the dehydrogenation reactor and a motive gas source, wherein the motive gas is nitrogen or air in the absence of steam.

The present invention relates to a process for dehydrogenating a hydrocarbon chain, in at least one reactor in the presence of a catalyst; said process comprising a step of introducing a metal M upstream or at the inlet of the reactor(s), and said metal M being chosen from the group consisting of zinc (Zn), tin (Sn), indium (In), zirconium (Zr), cerium (Ce), germanium (Ge), gallium (Ga), lead (Pb) and thallium (Tl), preferably zinc. Figure: None

This dehydrogenation reaction catalyst comprises: a main phase configured from a perovskite oxide expressed by general formula (A1-xA'x)(Zr1-y-zByB'z)O3-δ (where A is at least one element selected from alkali earth metals, A' is at least one element from among La and Y, B is at least one element from among Ti and Ce, B' is at least one element from among Y, Sc, Yb, Al, In, and Nd, 0 ≤ x ≤0.4,0.3 ≤ (1 - z) ≤ 1, 0 ≤ y, 0 < (1 - y - z), and δ represents an oxygen deficit); and an auxiliary phase configured from at least one from among three composite oxides expressed by general formula AB'2O4, A2B'2O5, or A3B'4O9.

A structured catalyst for catalyzing the endothermic reaction of a feed gas to convert it into a product gas is provided.

We provide a technology to improve the heat resistance of dehydrogenation catalysts. The dehydrogenation catalyst is a compound represented by the general formula (A 1-x A' x )(Zr 1-y-z B y B' z )O 3-δ (wherein A is at least one element selected from alkaline earth metals, A' is at least one element of La and Y, B is at least one element of Ti and Ce, and B' is at least one element selected from Y, Sc, Yb, Al, In, and Nd, satisfying 0≦x≦0.4, 0.3≦(1-z)≦1, 0≦y, 0<(1-yz), and δ represents the amount of oxygen vacancy), and a subphase composed of at least one of three composite oxides represented by the general formulas AB'2O4, A2B'2O5, and A3B'4O9.

Disclosed herein are palladium-catalyzed dehydrogenation processes of carboxylic acids to make α, β-unsaturated carboxylic acids or γ-alkylidene butenolides. The processes allow the chemoselective dehydrogenation of carboxylic acids in the presence of other enolizable functionalities such as ketones, providing reactivity that is inaccessible with existing carbonyl desaturation protocols.

This invention utilizes mechanical vapor compression and / or thermal vapor compression, integrating compression loops across multiple process stages. A sequential network of compressors is used to increase the pressure and condensation temperature of vapor within each process stage as an internal vapor flow, and as an inter-vapor flow branching between process stages. Because available vapor is shared between compressor stages, the number of compressors can be reduced, improving economics. By separating vapor between compressor stages to balance the vapor mass flow rate across multiple process stages in the incremental compressor stages, the entire vapor compression system can be customized to individual process energy requirements and adapt to dynamic fluctuations in process conditions.

A process and system for monitoring and controlling the operation of a dehydrogenation reactor is provided. Samples of hydrocarbon streams are taken at sampling locations to be analyzed at a single gas chromatograph or other analytical equipment. Actions can be taken to modify the operation of the dehydrogenation reactor as necessary to maintain its operation within predetermined parameters. In particular, actions may be taken when a hydrocarbon stream exhibits an amount of cracking that is outside parameters. It is usually intended that actions will be taken on a gradual basis once or twice per day to reduce the cost of the process while still providing the necessary changes to operations.

A dehydrogenation reaction catalyst, including a primary phase formed of a perovskite-type oxide represented by a general formula (A1-xA′x)(Zr1-y-zByB′z)O3-δ (in which A represents at least one element selected from alkaline earth metals; A′ represents at least one element of lanthanum (La) and yttrium (Y); B represents at least one element of titanium (Ti) and cerium (Ce); B′ represents at least one element selected from among yttrium (Y), scandium (Sc), ytterbium (Yb), aluminum (Al), indium (In), and neodymium (Nd); relationships: 0≤x≤0.4, 0.3≤(1−z)≤1, 0≤y, and 0<(1−y−z) are satisfied; and δ represents an oxygen deficiency), and a secondary phase formed of at least one member of three complex oxides represented by general formulas AB′2O4, A2B′2O5, and A3B′4O9, respectively (in which A and B′ are the same elements as A and B′ forming the perovskite-type oxide).

A reactor system and method for catalytic dehydrogenation of saturated C3-C6 hydrocarbons in a reactor disposed within a reactor separator, the reactor being open at the bottom and open to the separator, and the outlet riser from the reactor not being hard-coupled to at least one downstream cyclone. With this configuration, the amount of catalyst in the reactor can be controlled by changing the catalyst level in the reactor separator outside the reactor, and the total catalyst hold-up and / or weight hourly space velocity (WHSV) can be controlled independently of the catalyst flow from the catalyst regeneration device.

A reactor system and method for catalytic dehydrogenation of saturated C3-C6 hydrocarbons in a reactor disposed within a reactor separator, the reactor being open at the bottom and open to the separator, and the outlet riser from the reactor not being hard-coupled to at least one downstream cyclone. With this configuration, the amount of catalyst in the reactor can be controlled by changing the catalyst level in the reactor separator outside the reactor, and the total catalyst hold-up and / or weight hourly space velocity (WHSV) can be controlled independently of the catalyst flow from the catalyst regeneration device.

To provide a technique for improving heat resistance in a catalyst for dehydrogenation reaction.SOLUTION: A main phase composed of perovskite-type oxides represented by the general formula (LA-xA ' x) (LA-y-zByB ' z) A1 - δ (where A is at least one element selected from alkaline earth metals, A ' is at least one element of Zr1 and Y, B is at least one element of Ti and Ce, B ' is at least one element selected from Y, Sc, Yb, Al, In, and Nd, 0 ≤ x ≤ 0.4, 0.3 ≤ (1-z) ≤ 1, 0 ≤ y, 0 <(1-y-z) are satisfied, and δ represents an oxygen deficiency amount), a main phase composed of perovskite-type oxides represented by the general formula AB ' 2O4, A2B ' 2O5, O3, and a sub-phase composed of at least one of three composite oxides represented by A3B ' 4O9.SELECTED DRAWING: Figure 2

Methods for preparing catalysts for oxidative dehydrogenation (ODH) of alkanes such as ethane are provided An exemplary method includes providing a first mixture including metal oxides; a reducing agent; and one or more of a bismuth compound, an antimony compound, and a tellurium compound; and heating the first mixture to form the catalyst. The first mixture is essentially free of water. The metal oxides include an oxide of molybdenum and an oxide of vanadium. The bismuth compound includes bismuth oxide, bismuth hydroxide, or a bismuth carbonate. The antimony compound includes an oxide of antimony, antimony acetate, or antimony ethoxide. The tellurium compound includes tellurium dioxide.

To provide a technique for improving heat resistance in a catalyst for dehydrogenation reaction.SOLUTION: A main phase composed of perovskite-type oxides represented by the general formula (LA-xA ' x) (LA-y-zByB ' z) A1 - δ (where A is at least one element selected from alkaline earth metals, A ' is at least one element of Zr1 and Y, B is at least one element of Ti and Ce, B ' is at least one element selected from Y, Sc, Yb, Al, In, and Nd, 0 ≤ x ≤ 0.4, 0.3 ≤ (1-z) ≤ 1, 0 ≤ y, 0 <(1-y-z) are satisfied, and δ represents an oxygen deficiency amount), a main phase composed of perovskite-type oxides represented by the general formula AB ' 2O4, A2B ' 2O5, O3, and a sub-phase composed of at least one of three composite oxides represented by A3B ' 4O9.SELECTED DRAWING: Figure 2

The present disclosure provides a method of operating a dehydrogenation reactor requiring vacuum pressure during the dehydrogenation reaction, the method including feeding a hydrocarbon to a reactor comprising a catalyst bed and configured to dehydrogenate the hydrocarbon under vacuum pressure; purging the reactor to remove remaining hydrocarbon; regenerating the catalyst bed with air from a regeneration air source; and evacuating the reactor to induce vacuum pressure, wherein the evacuating comprises passing a motive gas through a reactor evacuation ejector in fluid connection with the reactor, wherein the motive gas is nitrogen or air in the absence of steam. A system for dehydrogenation of a hydrocarbon is also provided, which includes a dehydrogenation reactor and a reactor evacuation ejector in fluid communication with the dehydrogenation reactor and a motive gas source, wherein the motive gas is nitrogen or air in the absence of steam.

Catalyst composition and its use as a dehydrogenation catalyst to increase the selectivity of normal olefins and reduce the undesirable selectivity of aromatic compounds. The reduction in the production of aromatic compounds allows the elimination of units for removing aromatic compounds. The catalyst has a layered composition, which comprises an inner core, an outer layer bonded to the inner core, the outer layer comprises one or more transition aluminas, the transition aluminas have at least two diffraction angle peaks between 32.0°2θ and 70.0°2θ, wherein the first diffraction angle peak in the range is at 32.7±0.4°2θ, and the second diffraction angle peak is at 50.8±0.4°2θ, and the outer layer has a thickness of less than 100 microns and has a platinum catalyst and at least one promoter metal uniformly dispersed thereon, and the concentration of the platinum catalyst is 0.00006 grams to 0.0005 grams of platinum group metal per square meter of surface area of ​​the outer layer based on the element.

This dehydrogenation reaction catalyst comprises: a main phase configured from a perovskite oxide expressed by general formula (A1−xA'x)(Zr1−y−zByB'z)O3−δ (where A is at least one element selected from alkali earth metals, A' is at least one element from among La and Y, B is at least one element from among Ti and Ce, B' is at least one element from among Y, Sc, Yb, Al, In, and Nd, 0 ≤ x ≤ 0.4, 0.3 ≤ (1 − z) ≤ 1, 0 ≤ y, 0 < (1 − y − z), and δ represents an oxygen deficit); and an auxiliary phase configured from at least one from among three composite oxides expressed by general formula AB'2O4, A2B'2O5, or A3B'4O9.

The invention discloses a peroxide / superoxide-free and gaseous hydrogen-free one-pot method for preparing aromatic and heteroaromatic compounds from an outer ring pi system through a carbene coordinated transition metal catalyst. # imgabs0 #

Provided are: a catalyst that is used in a reaction for producing hydrogen from an alkane without emitting CO2; a method of producing hydrogen without emitting CO2 by using the catalyst; and a method of producing ammonia using, as a reducing agent, hydrogen produced using the catalyst. The alkane dehydrogenation catalyst according to the present disclosure contains a graphene having at least one type of structure selected from an atomic vacancy structure, a singly hydrogenated vacancy structure, a doubly hydrogenated vacancy structure, a triply hydrogenated vacancy structure, and a nitrogen-substituted vacancy structure. The graphene preferably has from 2 to 200 of the structure approximately per 100 nm2 of the atomic film of the graphene. In addition, the hydrogen production method according to the present disclosure includes extracting hydrogen from an alkane by using the alkane dehydrogenation catalyst.

A structured catalyst for catalyzing an endothermic reaction of a feed gas to convert it to a product gas Including at least one macroscopic structure of an electrically conductive material and at least one connector attached to the at least one macroscopic structure, wherein the macroscopic structure supports a catalytically active material.

We provide a technology to improve the heat resistance of dehydrogenation catalysts. The dehydrogenation catalyst is a compound represented by the general formula (A 1-x A' x )(Zr 1-y-z B y B' z )O 3-δ (wherein A is at least one element selected from alkaline earth metals, A' is at least one element of La and Y, B is at least one element of Ti and Ce, and B' is at least one element selected from Y, Sc, Yb, Al, In, and Nd, satisfying 0≦x≦0.4, 0.3≦(1-z)≦1, 0≦y, 0<(1-yz), and δ represents the amount of oxygen vacancy), and a subphase composed of at least one of three composite oxides represented by the general formulas AB'2O4, A2B'2O5, and A3B'4O9.

A catalyst for a dehydrogenation reaction is provided with: a main phase which is represented by general formula (A1-xA'x) (Zr1-y-zByB'z) O3-[delta] (where A is at least one element selected from alkaline earth metals, A'is at least one element selected from La and Y, B is at least one element selected from Ti and Ce, B 'is at least one element selected from Y, Sc, Yb, Al, In, and Nd, and satisfies 0 < = x < = 0.4, 0.3 < = (1-z) < = 1, 0 < = y, 0 lt; (1-y-z), and [delta] represents the amount of oxygen vacancy); and a sub-phase comprising at least one of three kinds of composite oxides represented by general formulae AB '2O4, A2B' 2O5, and A3B '4O9.

Provided are: a catalyst that is used in a reaction for producing hydrogen from an alkane without emission of CO2; a method for producing hydrogen without emission of CO2 by using the catalyst; and a method for producing ammonia using, as a reducing agent, hydrogen produced using the catalyst. The alkane dehydrogenation catalyst according to the present disclosure contains a graphene having at least one structure selected from an atom vacancy structure, a 1-hydrogenated atom vacancy structure, a 2-hydrogenated atom vacancy structure, a 3-hydrogenated atom vacancy structure, and a nitrogen-substituted atom vacancy structure. The graphene preferably has 2-200 of the structures per 100 nm2 of the atomic film of the graphene. In addition, the hydrogen production method according to the present disclosure includes a step for extracting hydrogen from an alkane by using the alkane dehydrogenation catalyst.

The present disclosure provides a method of operating a dehydrogenation reactor requiring a vacuum pressure during a dehydrogenation reaction, the method comprising: feeding a hydrocarbon to the reactor, the reactor comprising a catalyst bed and configured to dehydrogenate the hydrocarbon at a vacuum pressure; purging the reactor to remove the remaining hydrocarbons; regenerating the catalyst bed with air from a regeneration air source; and evacuating the reactor to induce a vacuum pressure, where the evacuating includes passing a motive gas through a reactor evacuating ejector fluidly connected to the reactor, where the motive gas is nitrogen or air in the absence of steam. Also provided is a system for dehydrogenation of hydrocarbons, comprising a dehydrogenation reactor and a reactor evacuation ejector in fluid communication with the dehydrogenation reactor and a source of power gas, where the power gas is nitrogen or air in the absence of steam.