Bp Chemicals Limited

Bp P.l.c.

Technip E&c Limited

Michael Keith Lee

Benjamin Patrick Gracey

Leslie William Bolton

Stephen Roy Partington

Craig Bailey

Peter Simpson Bell

Nigel Stewart Brown

Mark Julian Howard

The present invention provides a process for the preparation of ethene by vapor phase chemical dehydration of a feed comprising ethanol, said process comprising contacting the feed with a supported heteropolyacid catalyst in a reactor, wherein the feed temperature is at least 250&#xb0; C. and the pressure inside the reactor is at least 0.80 MPa but less than 1.80 MPa.

Process for preparing ethene

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

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 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 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).

Process for the conversion of hydrocarbons to alcohols

Process for converting a hydrocarbon feedstock into alcohol(s) wherein the hydrocarbons are first converted into syngas, which is converted into alcohols, by converting hydrocarbon feedstock in a steam reformer into stream A' of carbon oxide(s), hydrogen and water, feeding stream A&#x2032; with hydrocarbon and oxygen feedstocks into an auto-thermal reformer to produce stream A, converting stream A in an oxygenate synthesis reactor into stream B containing methanol, ethanol, propanol(s), H2, C1-C3 alkanes, CO, CO2 and water, separating stream B, into stream C containing CO, C1-C3 alkanes, H2 and methanol, stream D containing CO2, recovering stream B containing the ethanol, propanol(s) and water, treating stream C to separate into a stream comprising CO and a stream comprising H2 and C1-C3 alkanes, reintroducing part of stream C with the stream comprising CO into the oxygenate synthesis reactor. At least part of stream D is reintroduced into the steam reformer.

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Hull, United Kingdom

Michael Keith Lee