Bp Chemicals Limited

Bp P.l.c.

University of Southern Mississippi

Lubrizol Adibis Holdings (uk) Limited

Technip E&c Limited

Bp International Limited

Benjamin Patrick Gracey

Leslie William Bolton

Michael Keith Lee

Berian John Daniel

Stephen Roy Partington

John Glenn Sunley

Craig Bailey

Jon Michael Stewart Deeley

Martin Philip Atkins

Barry Hudson

Christopher Hallett

Cong Rong Li

Jon Michael Deeley

David J Moreton

Peter Simpson Bell

Peter S Williams

Nicholas John Hazel

Stephen Robert Hodge

Gordon John Haining

Ian D Dobson

Mark R Smith

Robert Paul Klaasen

David Lyons

Thakor Kikabhai

James Noel Martin Hegarty

Norbert Walter Josef Kamp

David Robert Alston

Carl A Avison

Process for producing alkene(s) from an oxygenate feedstock in a reactor by dehydration in the presence of a supported heteropolyacid catalyst. The pore volume of the supported heteropolyacid catalyst satisfies the following formula:0.6&#x2212;0.3[loading/Surface Area of Dried Catalyst]where;

Process for producing alkenes oxygenates by using supported heteropolyacid catalysts

Process for the conversion of carbon oxide(s) and hydrogen containing feedstocks into alcohols in the presence of a particulate catalyst.

Process for the conversion of synthesis gas to oxygenates containing C2+ alcohols

The present invention relates to an improved process for the production of ethanol from a carbonaceous feedstock; wherein the carbonaceous feedstock is first converted to synthesis gas which is then converted to ethanoic acid, which is then esterified and which is then hydrogenated to produce ethanol.

Process for the production of alcohol from a carbonaceous feedstock

Process for the production of ethene by the vapor phased chemical dehydration of a feed containing ethanol, water and ethoxyethane in a reactor at elevated temperature and pressure in the presence of a bed of catalyst comprising a supported heteropolytungstic acid, by maintaining or configuring the reactor so that it operates in a regime which satisfies the following parameters:0.05&#x3c;())/(8&#xd7;10&#xd7;GHSV+0.75)&#x2003;&#x2003;(1)and&#x2212;20&#x3c;&#x2212;40&#xd7;+40&#xd7;&#x3c;+80&#x2003;&#x2003;(2)wherein P, Pand P, GHSV, T, T, Pand Pare as defined in the specification.

Process for preparing ethene

Process for the preparation of alcohol(s) from alkyl ester(s) by bringing hydrogen, carbon monoxide and at least one alkyl ester into contact with a hydrogenation catalyst including copper and manganese in a reaction zone to produce at least one alcohol. The molar ratio of hydrogen to carbon monoxide in the reaction zone is in the range of from 100:1 to 1:10.

Process for hydrogenating alkyl ester(s) in the presence of carbon monoxide

Process for removing water from an ethylene stream containing water, by introducing an ethylene stream containing water into, and circulating the ethylene stream through, a separation vessel. A liquid diethyl ether stream is introduced into, and circulated through, the separation vessel so that the liquid diethyl ether stream and the ethylene stream containing water are brought into contact, and an ethylene stream having a reduced water content is recovered from the separation vessel.

Process for treatment of ethylene

Process for producing propylene from a propanol feedstock Aby reacting the propanol feedstock Ain a vapor phase dehydration reactor wherein the propanol is convened at a temperature comprised between 160 and 270&#xb0; C. and at a pressure of above 0.1 MPa but less than 4.5 MPa, into a product stream Bcontaining propylene, propyl ethers, water and unconverted and/or isomerized propanols, cooling the product stream B, disengaging the cooled product stream Bin a separation unit to give a first stream Ccontaining propylene and propyl ethers, and a second product stream Dcontaining water, propyl ethers and unconverted and/or isomerized propanols, feeding the product stream Dto a dewatering unit wherein the water stream Fis separated from the propyl ethers and unconverted and/or isomerised propanols stream E, recycling the stream Einto the dehydration reactor, cooling the product stream C, feeding the cooled product stream Cto a purification unit wherein the propyl ethers stream Gis separated from the propylene stream H, and optionally, recycling the propyl ethers stream Gto either the dewatering unit or directly to dehydration reactor.

Process for producing propylene

Process for the conversion of ethanoic acid into ethanol by (a) introducing ethanoic acid and Hinto a primary hydrogenation unit in the presence of a precious metal-based catalyst to produce ethanol and ethyl ethanoate and (b) introducing ethyl ethanoate, from step (a), together with Hinto a secondary hydrogenation unit in the presence of a copper-based catalyst to produce ethanol. Ethanol from step (b) is recovered.

Process for producing mono-olefins(s) from a feedstock A containing ethanol and propanol, wherein ethanol and propanol are dehydrated into the corresponding same carbon number olefins. The process is performed by 1. reacting feedstock A in a vapor phase dehydration reactor wherein the ethanol and propanol alcohols are converted into a product stream B comprising ethylene, propylene, ethers, water and unconverted alcohols, 2. cooling the product stream B, 3. disengaging the cooled product stream B in a separation unit to give a first stream C containing ethylene, propylene and ethers, and a second product stream D containing water, ethers and unconverted alcohols, 4. feeding the product stream D to a dewatering column wherein the water stream F is separated from the ethers and unconverted alcohols stream E, 5. recycling the stream E into the dehydration reactor of step 1, and 6. cooling the product stream C. In a step 7, the cooled product stream C is fed to a purification unit wherein the ethers stream G is separated from the ethylene and propylene stream H, and in an optional step 8, the ethers stream G is recycled to either the dewatering column of step 4 and/or directly to dehydration reactor of step 1.

Process for producing olefins

Process for producing ethylene from an ethanol feedstock A by (1) reacting the ethanol feedstock A in a vapor phase reactor wherein the ethanol is converted at a temperature between 160 and 270&#xb0; C. and at a pressure of above 0.1 MPa but less than 4.5 MPa, into a product stream B containing ethylene, diethyl ethers, water and unconverted ethanol, (2) cooling the product stream B, (3) disengaging the cooled product stream B in a separation unit to give a first stream C containing ethylene and diethyl ethers, and a second product stream D containing water, diethyl ethers and unconverted ethanol, (4) feeding the product stream D to a dewatering unit wherein the water stream F is separated from the diethyl ethers and unconverted ethanol stream E, (5) recycling the stream E into the dehydration reactor of step 1, (6) cooling the product stream C, and (7) feeding the cooled product stream C to a purification unit wherein the diethyl ethers stream G is separated from the ethylene stream H. Optionally, the ethyl ethers stream G is recycled to either the dewatering unit of step (4) or directly to dehydration reactor of step (1).

Process for producing ethylene

Process for homologation of alcohol(s), by 1 introducing alcohol(s) into an etherification unit to produce alkyl ether(s), 2, introducing at least a part of the alkyl ether(s) from step 1, together with CO and optionally H, into a carbonylation unit, in the presence of an acidic homogeneous or heterogeneous carbonylation catalyst, to produce alkyl ester(s), and 3, introducing at least a part of the alkyl ester(s) from step 2, together with H, into a hydrogenation unit, to produce homologated alcohol(s). Optionally, at least a part of the homologated alcohol(s) from step 3 is recycled into the etherification unit of step 1. Alcohol(s) from the hydrogenation unit of step 3 are recovered.

Process for the conversion of alcohol (s) into alcohol (s) with increased carbon-chain

Process for producing alkene(s) from a feedstock containing at least one monohydric aliphatic paraffinic alcohol having from 2 to 5 carbon atoms. The process is carried out by 1 converting the monohydric aliphatic paraffinic alcohol(s) containing 2 to 5 carbon atoms in a reactive distillation column at elevated pressure and temperature into a heads stream having the corresponding same carbon number alkene(s) and ether(s), 2 separating the heads stream from step 1 into an ether(s) enriched stream and an alkene(s) enriched stream, 3 recycling at least part of the ether(s) enriched stream from step 2 as a reflux return to the reactive distillation column, 4 simultaneously separating the alkene(s) enriched stream from step 2 into alkene(s) and ether(s), and 5 recycling at least part of the separated ether(s) from step 4 into the reactive distillation column. An alkene(s) stream from step 4 is then recovered.

Reactive distillation for the dehydration of mixed alcohols

Process for converting a hydrocarbon feedstock into alcohol(s), wherein the hydrocarbons are first converted into syngas, which is subsequently converted into alcohols. The process comprises the consecutive steps of 1) converting a hydrocarbon feedstock, in a syngas reactor, into a stream A, comprising essentially of a mixture of carbon oxide(s) and hydrogen, 2) converting at least part of stream A, in the presence of a catalyst in a oxygenate synthesis reactor under a temperature comprised between 150 and 400&#xb0; C. and a pressure of 20 to 200 bar, into an alcohols stream B, comprising essentially methanol, ethanol, propanol(s), H2, C1-03 alkanes, CO, CO2 and water, 3) separating stream B, into a stream C containing the CO, C1-C3 alkanes, H2 and methanol; a stream D containing the CO2; and recovering a stream E containing the ethanol, propanol(s) and water, 4) treating a fraction of stream C in order to separate said fraction into a stream comprising CO, and a stream comprising H2 and the C1-C3 alkanes, 5) reintroducing at least part of stream C together with the stream comprising CO from step 4 into the oxygenate synthesis reactor of step 2, and 6) reintroducing at least part of stream D into the syngas reactor of step 1.

Process for the conversion of hydrocarbons to oxygenates

Process for converting a hydrocarbon feedstock into alcohol(s), wherein the hydrocarbons are first converted into syngas, which is subsequently converted into alcohols. The process is carried out by performing the steps of (1) converting a hydrocarbon feedstock, together with an oxygen feedstock, in a auto-thermal reactor (ATR), into a stream A, containing a mixture of carbon oxide(s) and hydrogen, (2) converting at least part of stream A, in the presence of a catalyst in a oxygenate synthesis reactor under a temperature between 150 and 400&#xb0; C. and a pressure of 20 to 200 bar, into an alcohols stream B containing methanol, ethanol, propanol, H2, C1-C3 alkanes, CO, CO2 and water, (3) separating stream B, into a stream C containing the CO, C1-C3 alkanes, H2 and methanol; a stream D containing the CO2; and recovering a stream E containing the ethanol, propanol(s) and water, (4) treating a fraction of stream C in order to separate the fraction into a stream containing CO, and a stream containing H2 and the C1-C3 alkanes, (5) reintroducing at least part of stream C together with the stream containing CO from step 4 into the oxygenate synthesis reactor of step 2, and (6) reintroducing at least part of stream D into the auto-thermal reactor of step (1).

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Hull, United Kingdom

Benjamin Patrick Gracey