A process for the production of middle distillates by the catalytically promoted hydration of olefinic compounds having a carbon number ranging from 7 to 14 to convert the olefins to the corresponding mixed alcohols having a higher boiling point that is in the diesel range, the process being conducted in a continuous stirred tank reactor, e.g., an ebullated-bed reactor, utilizing catalysts that include soluble homogeneous acidic compounds and solid heterogeneous compounds such as resins, and amorphous or structured metal oxides containing elements selected from IUPAC Groups 4-10, 13 and 14, and having Lewis or Bronsted acid sites.

A process for the production of middle distillates by the catalytically promoted hydration of olefinic compounds having a carbon number ranging from 7 to 14 to convert the olefins to the corresponding mixed alcohols having a higher boiling point that is in the diesel range, the process being conducted in a continuous stirred tank reactor, e.g., an ebullated-bed reactor, utilizing catalysts that include soluble homogeneous acidic compounds and solid heterogeneous compounds such as resins, and amorphous or structured metal oxides containing elements selected from IUPAC Groups 4-10, 13 and 14, and having Lewis or Bronsted acid sites.

A method for optimising the operation of a facility for catalytic reforming, the facility including a multitude of reactors which have a catalyser and through which an operating gas including hydrocarbons and molecular hydrogen successively flows, wherein the composition of the operating gas in the reactors changes and wherein a product results at the outlet side of the last reactor. Specific constant characteristics as well as initial operating parameters that are present during the operation of the facility are acquired. A computational simulation of the chemical processes in the reactors then takes place, wherein results of a measurement of the chemical composition of the product at the outlet side of the last reactor is also included. A computational simulation of the chemical processes in the reactors with different varied operating parameters is subsequently carried out and set of optimised operating parameters is determined from the computed chemical composition.

A method for optimising the operation of a facility for catalytic reforming, the facility including a multitude of reactors which have a catalyser and through which an operating gas including hydrocarbons and molecular hydrogen successively flows, wherein the composition of the operating gas in the reactors changes and wherein a product results at the outlet side of the last reactor. Specific constant characteristics as well as initial operating parameters that are present during the operation of the facility are acquired. A computational simulation of the chemical processes in the reactors then takes place, wherein results of a measurement of the chemical composition of the product at the outlet side of the last reactor is also included. A computational simulation of the chemical processes in the reactors with different varied operating parameters is subsequently carried out and set of optimised operating parameters is determined from the computed chemical composition.

Process and apparatus for producing a naphtha stream is provided. The process comprises providing a kerosene stream to a hydrocracking reactor. The kerosene stream is hydrocracked in the presence of a hydrogen stream and a hydrocracking catalyst in the hydrocracking reactor at hydrocracking conditions comprising a hydrocracking pressure, a hydrocracking temperature, and a liquid hourly space velocity at a net conversion of at least about 90%, to provide a hydrocracked effluent stream comprising liquefied petroleum gas, heavy naphtha fraction and light naphtha fraction. One or more of the hydrocracking conditions are adjusted to maintain a ratio of the light naphtha fraction to the heavy naphtha fraction of at least about 2 by weight, suitably at least about 2.2 and preferably at least about 2.5 in the hydrocracked effluent stream while maintaining the net conversion of at least about 90%.

Process and apparatus for producing a naphtha stream is provided. The process comprises providing a kerosene stream to a hydrocracking reactor. The kerosene stream is hydrocracked in the presence of a hydrogen stream and a hydrocracking catalyst in the hydrocracking reactor at hydrocracking conditions comprising a hydrocracking pressure, a hydrocracking temperature, and a liquid hourly space velocity at a net conversion of at least about 90%, to provide a hydrocracked effluent stream comprising liquefied petroleum gas, heavy naphtha fraction and light naphtha fraction. One or more of the hydrocracking conditions are adjusted to maintain a ratio of the light naphtha fraction to the heavy naphtha fraction of at least about 2 by weight, suitably at least about 2.2 and preferably at least about 2.5 in the hydrocracked effluent stream while maintaining the net conversion of at least about 90%.

A refinery or petrochemical plant may include a fractionation column and related equipment, such as one or more condensers, receivers, reboilers, feed exchangers, and pumps. The equipment may have boundaries or thresholds of operating parameters based on existing limits and/or operating conditions. Illustrative existing limits may include mechanical pressures, temperature limits, hydraulic pressure limits, and operating lives of various components. There may also be relationships between operational parameters related to particular processes. For example, the boundaries on a naphtha reforming reactor inlet temperature may be dependent on a regenerator capacity and hydrogen-to-hydrocarbon ratio, which in turn may be dependent on a recycle compressor capacity. Operational parameters of a final product may be determined based on actual current or historical operation, and implemented in one or more models to determine adjustments for enhanced operational efficiency.

A refinery or petrochemical plant may include a fractionation column and related equipment, such as one or more condensers, receivers, reboilers, feed exchangers, and pumps. The equipment may have boundaries or thresholds of operating parameters based on existing limits and/or operating conditions. Illustrative existing limits may include mechanical pressures, temperature limits, hydraulic pressure limits, and operating lives of various components. There may also be relationships between operational parameters related to particular processes. For example, the boundaries on a naphtha reforming reactor inlet temperature may be dependent on a regenerator capacity and hydrogen-to-hydrocarbon ratio, which in turn may be dependent on a recycle compressor capacity. Operational parameters of a final product may be determined based on actual current or historical operation, and implemented in one or more models to determine adjustments for enhanced operational efficiency.

The present disclosure relates to the aromatization of hydrocarbons with an aromatization catalyst, including methods of aromatization comprising the use of a continuous catalyst regeneration type reformer.

A process and a system for reforming and upgrading a heavy naphtha feedstock may include dehydrogenating naphthenes in the heavy naphtha feedstock to form a first effluent stream comprising aromatics and then separating the aromatics via extraction from the produced first effluent stream to produce a second effluent stream containing raffinate paraffins. The process may then include subjecting the second effluent stream to cyclization reactions to produce a third effluent stream comprising aromatics and then combining the first effluent stream and the third effluent stream prior to extraction