A process for the production of high octane number gasoline from light refinery olefins and benzene-containing aromatic streams such as reformate. Light olefins including ethylene and propylene are extracted from refinery off-gases, typically from the catalytic cracking unit, into a light aromatic stream such as reformate containing benzene and other single ring aromatic compounds which is then reacted with the light olefins to form a gasoline boiling range product containing akylaromatics. The alkylation reaction is carried out in the liquid phase with a catalyst which preferably comprises a member of the MWW family of zeolites such as MCM-22 using a fixed catalyst bed.

Liquid phase aromatics alkylation process

The disclosed invention relates to a process, comprising: flowing a first reactant feed stream (314) comprising a reactant substrate and a second reactant feed stream (342) comprising an alkylating agent, an acylating agent or a mixture thereof, in a process microchannel (310) in contact with each other to form a product (316) comprising at least one alkylation product, at least one acylation product, or a mixture thereof; transferring heat from the process microchannel to a heat sink (320); and removing the product (316) from the process microchannel.

Process using microchannel technology for conducting alkylation or acylation reaction

Systems and methods for processing hydrocarbons are provided. A hydrocarbon can be distilled to provide a distillate, a gas oil, and a residue. The residue can include, but is not limited to asphaltenes and non-asphaltenes. The residue can be mixed with a solvent to provide a mixture. The asphaltenes can be selectively separated from the mixture to provide a deasphalted oil. At least a portion of the deasphalted oil and at least a portion of the gas oil can be hydroprocessed to provide a hydroprocessed hydrocarbon. At least a portion of the distillate and at least a portion of the hydroprocessed hydrocarbon can be cracked in a first reaction zone to provide a first cracked product comprising C2 hydrocarbons, C3 hydrocarbons, C4 hydrocarbons, and naphtha.

Systems and methods for residue upgrading

A process for the production of high octane number gasoline from light refinery olefins, typically from the catalytic cracking unit, and benzene-containing aromatic streams such as reformate. A portion of the light olefins including ethylene and propylene is polymerized to form a gasoline boiling range product and another portion is used to alkylate the light aromatic stream. The alkylation step may be carried out in successive stages with an initial low temperature stage using a catalyst comprising an MWW zeolite followed by a higher temperature stage using a catalyst comprising an intermediate pore size zeolite such as ZSM-5. Using this staged approach, the alkylation may be carried out in the vapor phase. Alternatively, the alkylation may be carried out in the liquid phase using the heavier olefins (propylene, butene) dissolved into the aromatic stream by selective countercurrent extraction; a separate alkylation step using the ethylene not taken up in the extraction is carried out at a higher temperature.

Gasoline production by olefin polymerization with aromatics alkylation

A splitter system is disclosed that produces a product stream from a mixed stream of two materials. A multi-stage heat pump compressor is used in combination with a bottoms reboiler and an intermediate reboiler resulting in reduced utility consumption. The intermediate reboiler enables use of a lower temperature heat source relative to the bottoms reboiler heat source. The first stage of the multi-stage heat pump compressor delivers pressurized overhead vapor to the intermediate reboiler and the second stage provides pressurized overhead vapor to the bottoms reboiler. The disclosed design and method lessens the heat pump compressor power consumption and trim condenser duty for a propylene/propane splitter system by over 20%. A third stage of compression upstream of the overhead trim condenser may be used for purposes of making the column pressure and temperatures independent of the trim condenser temperature.

Splitter with multi-stage heat pump compressor and inter-reboiler

A unified process which couples a unique in-situ catalyst regeneration process with a continuous reactive distillation under pressure for the alkylation of light aromatic hydrocarbons such as benzene with C2-C30 olefins using a solid acid alkylation catalyst supported in the reflux zone (21) of a distillation column (section A). Periodic regeneration of the catalyst (sections E, F and G) is carried out with a countercurrent injection of a C4-C16 paraffin (35) below the benzene rectification zone at the top of the column, but above the catalyst zone while the aromatic hydrocarbon reaction feedstock (17) is injected continuously at a point above a rectification zone at the base of the column where the aromatic compound is separated from the paraffin and by-products washed from the catalyst. The use of the C4-C16 paraffin with the aromatic at a mole fraction in the range of 40 to 90% enables a regeneration temperature of about 175 - 250°C. to be achieved and maintained by adjusting the column pressure and aromatic reflux rate. Significantly lower pressures, on the order of 125 to 370 psig, are required to achieve regeneration temperature than would be otherwise required with the use only of the aromatic hydrocarbon to dilute and wash the by-products from the catalyst surfaces.

A reactive distillation alkylation process including in situ catalyst regeneration

A unified process for reactive distillation under pressure for the alkylation of light aromatic hydrocarbons such as benzene and cumene with straight chain C6- C18 olefins using a solid acid alkylation catalyst supported in the reflux zone of the distillation column (column 2). The process is continuous, using a reactive distillation configuration such that at least a portion of the olefin (7) is injected below the benzene rectification zone at the top of the column. The aromatic hydrocarbon (17) is injected continuously at a low rate above the rectification zone (H) at the base of the column and above the reboiler (40). The alkylation reaction takes place primarily in the liquid phase on the solid acid catalyst and is characterized in that the molar ratio is adjustable up to about 100/1, through adjustment of the internal column operating pressure, the benzene reflux rate, the amount of benzene removed from the reflux condenser to storage or from the reboiler with the distillation column operated at or near total aromatic hydrocarbon reflux. The unexpectedly high liquid phase aromatic hydrocarbon to olefin molar ratios achieved in the reactive distillation column increases the selectivity to mono-alkylated aromatics and helps stabilize catalyst lifetime.

Murray Joy L

Papers

A reactive distillation alkylation process including in situ catalyst regeneration

A reactive distillation process for the alkylation of aromatic hydrocarbons