The present invention discloses processes for producing normal alpha olefins, such as 1-hexene, 1-octene, 1-decene, and 1-dodecene in a multistep synthesis scheme from another normal alpha olefin. Also disclosed are reactions for converting aldehydes, primary alcohols, and terminal vicinal diols into normal alpha olefins.

The present invention discloses processes for producing normal alpha olefins, such as 1-hexene, 1-octene, 1-decene, and 1-dodecene in a multistep synthesis scheme from another normal alpha olefin. Also disclosed are reactions for converting aldehydes, primary alcohols, and terminal vicinal diols into normal alpha olefins.

The present invention discloses processes for producing normal alpha olefins, such as 1-hexene, 1-octene, 1-decene, and 1-dodecene in a multistep synthesis scheme from another normal alpha olefin. Also disclosed are reactions for converting aldehydes, primary alcohols, and terminal vicinal diols into normal alpha olefins.

Process scheme configurations are disclosed that enable conversion of crude oil feeds with several processing units in an integrated manner into petrochemicals. The designs utilize minimum capital expenditures to prepare suitable feedstocks for the steam cracker complex. The integrated process for converting crude oil to petrochemical products including olefins and aromatics, and fuel products, includes mixed feed steam cracking and gas oil steam cracking. Feeds to the mixed feed steam cracker include light products and naphtha from hydroprocessing zones within the battery limits, recycle streams from the C3 and C4 olefins recovery steps, and raffinate from a pyrolysis gasoline aromatics extraction zone within the battery limits. Feeds to the gas oil steam cracker include hydrotreated gas oil range intermediates from vacuum gas oil hydrotreating.

Process scheme configurations are disclosed that enable conversion of crude oil feeds with several processing units in an integrated manner into petrochemicals. The designs utilize minimum capital expenditures to prepare suitable feedstocks for the steam cracker complex. The integrated process for converting crude oil to petrochemical products including olefins and aromatics, and fuel products, includes mixed feed steam cracking and gas oil steam cracking. Feeds to the mixed feed steam cracker include light products and naphtha from hydroprocessing zones within the battery limits, recycle streams from the C3 and C4 olefins recovery steps, and raffinate from a pyrolysis gasoline aromatics extraction zone within the battery limits. Feeds to the gas oil steam cracker include hydrotreated gas oil range intermediates from vacuum gas oil hydrotreating.

Provided is a process for converting an alkane to an alkene. The process comprises (a) contacting the alkane and either (i) an oxidizing electrophile comprising a main group element in oxidized form, or (ii) an oxidant and a reduced form of the oxidizing electrophile, in a liquid medium comprising an oxygen acid and optionally one or more additives selected from a non-oxidizable liquid, a salt additive, a Lewis acid, and water, to provide an oxidized intermediate and a reduced form of the oxidizing electrophile; (b) optionally separating the oxidized intermediate and the reduced form of the oxidizing electrophile; and (c) performing an elimination reaction on the oxidized intermediate to provide the alkene and the oxygen acid.

Provided is a process for converting an alkane to an alkene. The process comprises (a) contacting the alkane and either (i) an oxidizing electrophile comprising a main group element in oxidized form, or (ii) an oxidant and a reduced form of the oxidizing electrophile, in a liquid medium comprising an oxygen acid and optionally one or more additives selected from a non-oxidizable liquid, a salt additive, a Lewis acid, and water, to provide an oxidized intermediate and a reduced form of the oxidizing electrophile; (b) optionally separating the oxidized intermediate and the reduced form of the oxidizing electrophile; and (c) performing an elimination reaction on the oxidized intermediate to provide the alkene and the oxygen acid.

Provided is a process for oxidizing an alkene. The process comprises contacting an alkene, and either an oxidizing electrophile comprising a main group element in oxidized form or an oxidant and a reduced form of the oxidizing electrophile, in a liquid medium comprising an oxygen acid and optionally one or more additives selected from a non-oxidizable liquid, a salt additive, a Lewis acid, and water, to provide an oxygenate and a reduced form of the oxidizing electrophile. The process optionally further comprises separating the oxygenate and the reduced form of the oxidizing electrophile. The oxygenate can be further hydrolyzed to form an alcohol, diol, or polyol.

Provided is a process for oxidizing an alkene. The process comprises contacting an alkene, and either an oxidizing electrophile comprising a main group element in oxidized form or an oxidant and a reduced form of the oxidizing electrophile, in a liquid medium comprising an oxygen acid and optionally one or more additives selected from a non-oxidizable liquid, a salt additive, a Lewis acid, and water, to provide an oxygenate and a reduced form of the oxidizing electrophile. The process optionally further comprises separating the oxygenate and the reduced form of the oxidizing electrophile. The oxygenate can be further hydrolyzed to form an alcohol, diol, or polyol.

A catalyst includes a zeolite, wherein the zeolite has: a CHA framework; a particle size less than or equal to 100 nanometers; and a silica to alumina mole ratio in the range of about 50:1 to about 150:1. The catalyst can include a metal dopant. The catalyst can be used for purifying a product by flowing a reactant across the catalyst to form the product; and condensing or separating the product. The product can be an olefin or alkenes with an increased carbon chain. The catalyst can be used for selective catalytic reduction of nitrogen oxide or a gas to liquid reaction. A method of producing the catalyst can include selecting the concentration of a crystal growth inhibitor based on the ratio of the silica precursor and an alumina precursor such that the zeolite crystals have a mean particle size less than or equal to 100 nanometers.