Micro-interface enhanced oxidation system and oxidation method for preparing hydrogen peroxide
US-12090458-B2 · Sep 17, 2024 · US
US2016214913A1 · US · A1
| Field | Value |
|---|---|
| Publication number | US-2016214913-A1 |
| Application number | US-201414916377-A |
| Country | US |
| Kind code | A1 |
| Filing date | Aug 29, 2014 |
| Priority date | Sep 6, 2013 |
| Publication date | Jul 28, 2016 |
| Grant date | — |
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A reactor and process for removing unsaturated alkynes and diolefinic impurities from olefins and oxygenates is described.
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1 . A reactor suitable for use in a hydrogenation process, the reactor comprising: a. a catalyst bed comprising a tube for cooling the catalyst bed; b. a plurality of inlets for conveying a feed material to the catalyst bed; and c. one or more outlets, wherein the catalyst bed comprises a catalyst having a surface area of from about 15 m 2 /g to about 650 m 2 /g, and wherein the reactor can provide a space velocity of from about 500/h to about 50,000/h for hydrogenation reactions. 2 . The reactor of claim 1 , further comprising one or more distributors for distributing the feed material uniformly or substantially uniformly across the catalyst bed. 3 . The reactor of claim 1 , wherein the catalyst bed is a fixed bed comprising a selective hydrogenation catalyst. 4 . The reactor of claim 1 , wherein the catalyst bed is positioned in contact with one or more catalyst bed supports. 5 . The reactor of claim 1 , being a hydrogenation reactor comprising a plurality of inlets for an olefin feed, an oxygenate feed, or a combination thereof. 6 . The reactor of claim 1 , further comprising a drip trap for recovering a condensate and/or a green oil. 7 . The reactor of claim 1 , further comprising one or more thermowells disposed between an exterior surface of the reactor and the catalyst bed. 8 . (canceled) 9 . (canceled) 10 . (canceled) 11 . The reactor of claim 1 , wherein the catalyst has a surface area of from about 30 m 2 /g to about 650 m 2 /g. 12 . The reactor of claim 1 , having a space velocity of at least about 25,000/h. 13 . The reactor of claim 1 , having a high space velocity, a low pressure drop, a uniform distribution of feed material across the catalyst bed, or a combination thereof, as compared to a conventional hydrogenation and/or dehydrogenation reactor. 14 . A reactor system comprising a plurality of the reactors of claim 1 , arranged in a series configuration. 15 . A reactor system comprising a plurality of the reactors of claim 1 , arranged in a parallel configuration. 16 . (canceled) 17 . (canceled) 18 . (canceled) 19 . A method for a hydrogenation process, the method comprising introducing a feed material to the reactor of claim 1 through the plurality of inlets, such that the feed material uniformly or substantially uniformly contacts the catalyst bed to produce a hydrogenation reaction product. 20 . The method of claim 19 , wherein the feed material comprises acetylene, and wherein the reaction product comprises an alkene. 21 . (canceled) 22 . (canceled) 23 . (canceled) 24 . The method of claim 19 , wherein the reactor exhibits a pressure drop of from about 0.05 to about 100 bar. 25 . (canceled) 26 . The method of claim 19 , wherein the reactor provides improved control over runaway reactions, as compared to a conventional reactor. 27 . (canceled) 28 . The method of claim 19 , wherein a plurality of reactors are connected in a series configuration to provide a front-end acetylene removal system. 29 . (canceled) 30 . The method of claim 19 , wherein a plurality of reactors are connected in a parallel configuration to provide a back-end acetylene removal system.
Details of the reactor or of the particulate material; Processes to increase or to retard the rate of reaction (B01J8/0285, B01J8/067, B01J8/087, B01J8/1836 take precedence) · CPC title
to carbon-to-carbon double bonds · CPC title
Feeding reactive fluids (for solid material B01J8/0015) · CPC title
Flow distribution elements · CPC title
Feeding reactive fluids (for solid material, see B01J8/0015) · CPC title
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