Abstract: A method is provided for producing gasoline that includes separating a cracked naphtha feed into a light catalytic naphtha fraction and a heavy naphtha fraction; and exposing the light catalytic naphtha fraction to a catalyst under effective conversion conditions to reduce sulfur content of the light catalytic naphtha fraction while also reducing a Reid vapor pressure and an olefin content of the light catalytic naphtha fraction, wherein the effective conversion conditions comprise a pressure of less than about 500 psig and a temperature of at least about 550° F. (288° C.).

Abstract: A method is provided for upgrading a hydrocarbon feed. The method may include contacting a hydrocarbon feed with a catalyst in a fluidized bed reactor; directing a portion of the catalyst from the fluidized bed reactor to a regeneration zone, such that the portion of the catalyst flows in a first direction through the regeneration zone; directing combustion air into the regeneration zone in a counter-flow direction to the first direction, wherein the combustion air is provided at a rate of about 100.05% or less of the stoichiometric air requirement for combusting coke present on the portion of catalyst; regenerating the portion of the catalyst in the regeneration zone to produce regenerated catalyst; and directing a portion of the hydrocarbon feed to combine with the regenerated catalyst downstream of the regeneration zone and lift the regenerated catalyst back to the fluidized bed reactor.

Abstract: Systems and methods are provided for the conversion of methanol to gasoline. Such methods may be performed be the sequential conversion of methanol to dimethyl ether, the conversion of dimethyl ether (and unconverted methanol, if present) to an intermediate olefin-rich product, and the oligomerization of the olefin-rich product to gasoline boiling range hydrocarbons.

Abstract: Methods and systems are provided for making gasoline. The method includes converting a resid-containing feed to a first fuel gas and a fluid coke in a fluidized bed reactor; gasifying the fluid coke with steam and air to produce a second fuel gas, said second fuel gas comprising a syngas; contacting the first fuel gas with a first conversion catalyst under first effective conversion conditions to form an effluent comprising C5+ hydrocarbon compounds; and converting the syngas to gasoline boiling range hydrocarbons by converting the syngas to a methanol intermediate product.

Abstract: Systems and methods are provided for catalyst regeneration using a stoichiometric amount or less air for coke combustion.

Abstract: In a process for the catalytic conversion of organic oxygenates to hydrocarbons, a feed comprising at least one organic oxygenate is contacted with a zeolite catalyst under conditions effective to produce a hydrocarbon product comprising aromatics, olefins and paraffins. At least a fraction of the hydrocarbon product containing C4+ hydrocarbons, including at least part of the olefins, is then contacted with hydrogen in the presence of a hydrogenation catalyst under conditions effective to saturate at least part of the olefins in the C4+-containing fraction and produce a hydrogenated effluent containing less than 1 wt % olefins. The hydrogenated effluent is useful as a diluent for heavy crude oils.

Abstract: Apparatuses and processes for converting an oxygenate feedstock, such as methanol and dimethyl ether, in a fluidized bed containing a catalyst to hydrocarbons, such as gasoline boiling components, olefins and aromatics are provided herein.

Abstract: An FCC unit enables the normal regenerator to be eliminated by carrying out catalyst regeneration in the reactor section of the unit using air, oxygen-enriched air or even relatively pure oxygen as the stripping medium in the stripping section of the reactor while maintaining overall reducing conditions so that sulfur and nitrogen are produced in the form of hydrogen sulfide, ammonia and other reduced species. The combustion gases from the stripper are sent from the reactor with the cracking vapors to the FCC main fractionator, wet gas compressor and gas plant to process the by-products of the coke combustion along with the FCC reactor effluent. The principle is applicable to grass-roots FCC units with its potential for elimination of a major unit component but it also has potential for application to existing units to reduce the load on the regenerator or eliminate the need for the existing regenerator so that an existing regenerator may be converted to a parallel or auxiliary reactor system.

Abstract: Systems and methods are provided for hydroconversion of a heavy oil feed under slurry hydroprocessing conditions and/or solvent assisted hydroprocessing conditions. The systems and methods for slurry hydroconversion can include the use of a configuration that can allow for improved separation of catalyst particles from the slurry hydroprocessing effluent. In addition to allowing for improved catalyst recycle, an amount of fines in the slurry hydroconversion effluent can be reduced or minimized. This can facilitate further processing or handling of any “pitch” generated during the slurry hydroconversion. The systems and methods for solvent assisted hydroprocessing can include processing of a heavy oil feed in conjunction with a high solvency dispersive power crude.

Abstract: The invention relates to the production of aromatic hydrocarbon by the conversion of a feed comprising saturated hydrocarbon. At least a portion of the saturated hydrocarbon is converted to olefinic hydrocarbon. Aromatic hydrocarbon is produced from at least a portion of the olefinic hydrocarbon using at least one dehydrocyclization catalyst comprising dehydrogenation and molecular sieve components.

Abstract: A method for utilizing the heating value of clarified shiny oil (CSO) by in which clarified slurry oil from the settler of a fluid catalytic cracking unit is introduced as feed to the gasifier of a Flexicoking unit where it is reacted at high temperature with the air and steam to produce additional heat. In this way, the heating value of the CSO is better utilized as refinery fuel gas and plant economics are enhanced.

Abstract: Methods are provided for producing lubricant base stocks from deasphalted oils formed by sequential deasphalting. The deasphalted oil can be exposed a first deasphalting process using a first solvent that can provide a lower severity of deasphalting and a second deasphalting process using a second solvent that can provide a higher severity of deasphalting. This can result in formation of at least a deasphalted oil and a resin fraction. The resin fraction can represent a fraction that traditionally would have been included as part of a deasphalter rock fraction.

Abstract: The invention relates to the production of aromatic hydrocarbon by the conversion of a feed comprising saturated hydrocarbon. At least a portion of the saturated hydrocarbon is converted to olefinic hydrocarbon. Aromatic hydrocarbon is produced from at least a portion of the olefinic hydrocarbon using at least one dehydrocyclization catalyst comprising dehydrogenation and molecular sieve components.

Abstract: Processes and systems for converting an oxygenate feedstock to a hydrocarbon product, selectivated catalysts and processes for reducing off-spec gasoline production during start-up are provided herein.

Abstract: Systems and methods are provided for producing diesel boiling range compounds from an olefin-containing feed. The olefin-containing feed can include a refinery fuel gas and/or a naphtha feed. The olefin-containing feed can be exposed to a first set of conversion conditions that can include a low pressure to produce an oligomerized olefin effluent. The oligomerized olefin effluent can be exposed to a second set of conversion conditions that include a higher pressure than the first set of conversion conditions to produce a product effluent that includes diesel boiling range compounds.

Abstract: Systems and methods are provided for producing naphtha boiling range fractions having a reduced or minimized amount of sulfur and an increased and/or desirable octane rating and suitable for incorporation into a naphtha fuel product. A naphtha boiling range feed can be separated to form a lower boiling portion and a higher boiling portion. The lower boiling portion, containing a substantial amount of olefins, can be exposed to an acidic catalyst without the need for providing added hydrogen in the reaction environment. Additionally, during the exposure of the lower boiling portion to the acidic catalyst, a stream of light olefins (such as C2-C4 olefins) can be introduced into the reaction environment. Adding such light olefins can enhance the C5+ yield and/or improve the removal of sulfur from thiophene and methyl-thiophene compounds in the naphtha feed.

Abstract: A potentially heat-deficient fluid catalytic cracking process for effecting a bulk boiling point conversion of a high boiling point petroleum feed to lower boiling products in which the overall enthalpy balance between the endothermic cracking and exothermic regeneration is maintained by combustion of a supplemental fuel in the middle or upper region of the dense bed in the regenerator (including the region immediately above the dense phase bed). There is a direct economic benefit from operation of the cracking process in this way since the preferred supplemental fuel is methane (natural gas) which is currently a low cost fuel while liquid products are higher value. Use of natural gas as a supplemental fuel will allow re-optimization of the catalyst and operations separately from the heat balance demand.

Abstract: An FCC unit enables the normal regenerator to be eliminated by carrying out catalyst regeneration in the reactor section of the unit using air, oxygen-enriched air or even relatively pure oxygen as the stripping medium in the stripping section of the reactor while maintaining overall reducing conditions so that sulfur and nitrogen are produced in the form of hydrogen sulfide, ammonia and other reduced species. The combustion gases from the stripper are sent from the reactor with the cracking vapors to the FCC main fractionator, wet gas compressor and gas plant to process the by-products of the coke combustion along with the FCC reactor effluent. The principle is applicable to grass-roots FCC units with its potential for elimination of a major unit component but it also has potential for application to existing units to reduce the load on the regenerator or eliminate the need for the existing regenerator so that an existing regenerator may be converted to a parallel or auxiliary reactor system.

Abstract: An integrated process for converting light (C2-C5) paraffins to hydrocarbon products in the gasoline and distillate boiling range in which a light paraffin fraction is subjected to steam cracking under conditions to maximize weight of C5+ molecules plus a multiple of the weight of C4? olefins. This multiple is preferably between 0.7-1 to result in maximum volume of gasoline and distillate production in the overall conversion to products. Light (C2-C5) olefins are oligomerized in a zeolite-catalyzed fluidized bed oligomerization at elevated temperature to produce oligomerized products in the gasoline and middle distillate boiling range.

Abstract: In a process for the catalytic conversion of organic oxygenates to hydrocarbons, a feed comprising at least one organic oxygenate is contacted with a zeolite catalyst under conditions effective to produce a hydrocarbon product comprising aromatics, olefins and paraffins. At least a fraction of the hydrocarbon product containing C4+ hydrocarbons, including at least part of the olefins, is then contacted with hydrogen in the presence of a hydrogenation catalyst under conditions effective to saturate at least part of the olefins in the C4+-containing fraction and produce a hydrogenated effluent containing less than 1 wt % olefins. The hydrogenated effluent is useful as a diluent for heavy crude oils.