Abstract: An integrated process for hydrogenating olefins wherein the hydrogen stream is generated from electrolysis of water is described. Water is derived from a first reaction step wherein a first feed stream comprising oxygenated hydrocarbons is reacted to produce a first reacted product stream comprising olefins and a second reacted product stream comprising water. The second reacted product stream is electrolyzed to produce an electrolyzer product stream comprising hydrogen. Hydrogen is used to hydrogenate olefins. A paraffin stream can be obtained from the hydrogenated effluent.

Abstract: An integrated process for hydrogenating olefins wherein the hydrogen stream is generated from electrolysis of water is described. Water is derived from a first reaction step wherein a first feed stream comprising oxygenated hydrocarbons is reacted to produce a first reacted product stream comprising olefins and a second reacted product stream comprising water. The second reacted product stream is electrolyzed to produce an electrolyzer product stream comprising hydrogen. Hydrogen is used to hydrogenate olefins. A paraffin stream can be obtained from the hydrogenated effluent.

Abstract: A process for dehydration of an ethanol feed stream comprising sending said ethanol feed stream and steam to a radial flow reactor to contact a catalyst under reaction conditions and produce an effluent comprising ethylene. The use of a radial flow reactor eliminates concerns about pressure drops that may occur with conventional fixed bed downflow reactors.

Abstract: A process of converting an ethanol feed stream to ethylene comprising sending portions of said ethanol feed stream to two reactors in parallel and then sending the combined product to a third reactor that is operated at a higher temperature to prevent the formation of ethers such as diethyl ether.

Abstract: A process for dimerizing and oligomerizing olefins to distillate fuels which utilizes a solid acid catalyst for ethylene oligomerization in a first stage and a metal catalyst for further oligomerization in a second stage. Distillate fuels can be produced from the process. Oligomerized olefins may be recycled to the first stage oligomerization reaction to ensure sufficient oligomerization of smaller olefins.

Abstract: A process for dehydration of ethanol to produce ethylene is provided. Ethanol is dehydrated to produce ethylene and the subsequent conversion of ethylene to longer chain olefins and then their hydrogenation to produce long chain paraffins. In some embodiments, a split feed is employed to improve efficiency and a caustic wash column is eliminated. The advantages of the process include a lower requirement for steam and a reduction in the combined reactor volume of 30-40% when two reactors are used as compared to a single reactor.

Abstract: A process for dimerizing and oligomerizing olefins to distillate fuels which manages the dimerization exotherm by diluting it with paraffins which are inert in the dimerization. The olefin stream can also be split and fed to multiple dimerization reactors to further reduce the heat generated. The ethylene feed can also be cooled before entering the dimerization reactor. The paraffins can be obtained from saturating oligomerized effluent.

Abstract: A process for oligomerizing an olefin stream with an oligomerization catalyst to produce an oligomerized olefin stream. Oligomerization may comprise a first stage ethylene oligomerization step followed by a second stage oligomerization of the first stage oligomerized olefin to higher olefins. The oligomerized olefin stream can be separated into jet and diesel fuel streams. The olefin stream may be obtained by converting oxygenates to olefins with an MTO catalyst.

Abstract: A process for producing olefins from methanol with an MTO catalyst and oligomerizing a resulting olefin stream with an oligomerization catalyst to produce an oligomerized olefin stream. Oligomerization may comprise a first stage ethylene and/or propylene oligomerization step followed by a second stage oligomerization step of the first stage oligomerized olefin stream to higher olefins. The oligomerized olefin stream can be separated into jet and diesel fuel streams.

Abstract: A catalytic composite comprises a first component selected from Group VIII noble metal components and mixtures thereof, a second component selected from one or more of alkali and alkaline earth metal components, and a third component selected from one or more of tin, germanium, lead, indium, gallium, and thallium, all supported on an alumina support comprising delta alumina having an X-ray diffraction pattern comprising at least three 2? diffraction angle peaks between 32.0° and 70.0°. The at least three 2? diffraction angle peaks comprise a first 2? diffraction angle peak of 32.7°±0.4°, a second 2? diffraction angle peak of 50.8°±0.4°, and a third 2? diffraction angle peak of 66.7°±0.8°, wherein the second 2? diffraction angle peak has an intensity of less than about 0.06 times the intensity of the third 2? diffraction angle peak.

Abstract: New/fresh catalyst is added to a dehydrogenation unit and aged catalyst is removed from the dehydrogenation unit on a continuous or semi-continuous basis while the dehydrogenation unit is in operation. The conversion achieved by the higher activity catalyst results in the production rate of olefin product being maintained at near start-of-run production for longer, with a slower rate of decline. The higher activity catalyst extends run time, reduces feed consumption for each unit of olefin product, and minimizes fresh catalyst expenses.

Abstract: Catalysts and processes for a selective conversion of hydrocarbons. The catalyst comprises: a first component selected from the group consisting of Group VIII noble metals and mixtures thereof, a modifier selected from the group consisting of alkali metals or alkaline-earth metals and mixtures thereof, and a third component selected from the group consisting of tin, germanium, lead, indium, gallium, thallium and mixtures thereof; and a support forming a catalyst particle comprising a plurality of pores. The catalyst has a modifier profile index in a range of 1 to 1.4 across the catalyst particle.

Abstract: A catalytic composite comprises a first component selected from Group VIII noble metal components and mixtures thereof, a second component selected from one or more of alkali and alkaline earth metal components, and a third component selected from one or more of tin, germanium, lead, indium, gallium, and thallium, all supported on an alumina support comprising delta alumina having an X-ray diffraction pattern comprising at least three 2? diffraction angle peaks between 32.0° and 70.0°. The at least three 2? diffraction angle peaks comprise a first 2? diffraction angle peak of 32.7°±0.4°, a second 2? diffraction angle peak of 50.8°±0.4°, and a third 2? diffraction angle peak of 66.7°±0.8°, wherein the second 2? diffraction angle peak has an intensity of less than about 0.06 times the intensity of the third 2? diffraction angle peak.

Abstract: Catalysts and processes for a selective conversion of hydrocarbons. The catalyst comprises: a first component selected from the group consisting of Group VIII noble metals and mixtures thereof, a modifier selected from the group consisting of alkali metals or alkaline-earth metals and mixtures thereof, and a third component selected from the group consisting of tin, germanium, lead, indium, gallium, thallium and mixtures thereof; and a support forming a catalyst particle comprising a plurality of pores. The catalyst has a modifier profile index in a range of 1 to 1.4 across the catalyst particle.

Abstract: A catalyst for a selective conversion of hydrocarbons. The catalyst includes a first component selected from the group consisting of Group VIII noble metals and mixtures thereof, a second component selected from the group consisting of alkali metals or alkaline-earth metals and mixtures thereof, and a third component selected from the group consisting of tin, germanium, lead, indium, gallium, thallium and mixtures thereof. The catalyst is a support formed as a spherical catalyst particle with an average pore diameter between 200 to 350 Angstroms, a porosity of at least 75% and an apparent bulk density between 0.60 and 0.3 g/cc. Also, a process of using such a catalyst for a selective hydrocarbon conversion reaction and a process for regenerating such a catalyst by removing coke from same.

Abstract: A catalyst for a selective conversion of hydrocarbons. The catalyst includes a first component selected from the group consisting of Group VIII noble metals and mixtures thereof, a second component selected from the group consisting of alkali metals or alkaline-earth metals and mixtures thereof, and a third component selected from the group consisting of tin, germanium, lead, indium, gallium, thallium and mixtures thereof. The catalyst is a support formed as a spherical catalyst particle with a median diameter between 1.6 mm and 2.5 mm and an apparent bulk density between 0.6 and 0.3 g/cc. Also a process of using such a catalyst for a selective hydrocarbon conversion reaction and a process for regenerating such a catalyst by removing coke from same.

Abstract: A catalyst for a selective conversion of hydrocarbons. The catalyst includes a first component selected from the group consisting of Group VIII noble metals and mixtures thereof, a second component selected from the group consisting of alkali metals or alkaline-earth metals and mixtures thereof, and a third component selected from the group consisting of tin, germanium, lead, indium, gallium, thallium and mixtures thereof. The catalyst is a support formed as a spherical catalyst particle with an average pore diameter between 200 to 350 Angstroms, a porosity of at least 75% and an apparent bulk density between 0.60 and 0.3 g/cc. Also, a process of using such a catalyst for a selective hydrocarbon conversion reaction and a process for regenerating such a catalyst by removing coke from same.

Abstract: Processes for dehydrogenation of a hydrocarbon feedstock are described. The process can be run at lower H2/HC ratios and lower RITs while maintaining coke production at the same level as operation at higher H2/HC ratios and higher RITs without decreasing the yield per pass. Acceptable levels of coke were achieved when operating the process at low hydrogen to hydrocarbon molar ratio in the range of 0.01 to 0.40 and reactor inlet temperatures in the range of 500°-645° C. The process uses a low coke catalyst.

Abstract: A catalyst for a selective conversion of hydrocarbons. The catalyst includes a first component selected from the group consisting of Group VIII noble metals and mixtures thereof, a second component selected from the group consisting of alkali metals or alkaline-earth metals and mixtures thereof, and a third component selected from the group consisting of tin, germanium, lead, indium, gallium, thallium and mixtures thereof. The catalyst is a support formed as a spherical catalyst particle with a median diameter between 1.6 mm and 2.5 mm and an apparent bulk density between 0.6 and 0.3 g/cc. Also a process of using such a catalyst for a selective hydrocarbon conversion reaction and a process for regenerating such a catalyst by removing coke from same.

Abstract: Large pill dehydrogenation catalysts and large screens slot width are combined in dehydrogenation units to reduce the pressure drop across the catalyst bed and reactor screens compared to conventional screen and catalyst size combinations. The catalyst has an average pill diameter in the range of 1.6 mm to 3.0 mm, and the slot width of the screen is in the range of about 30% to about 60% of the pill diameter.