A process and apparatus for making aromatics are described. The process includes reforming a naphtha stream in a reforming zone to form a reformer effluent comprising aromatic compounds and non-aromatic compounds, wherein at least a portion of the aromatic compounds contain alkyl groups. The reformer effluent is heated and passed directly to an acid cracking reaction zone. The non-aromatic compounds are selectively cracked and at least a portion of the alkyl groups on the aromatic compounds are selectively dealkylated in the presence of an acid cracking catalyst to form a cracked reformer effluent comprising the aromatic compounds and cracked olefins.

A process for reducing the environmental contaminants in a ISO 8217 compliant Feedstock Heavy Marine Fuel Oil, the process involving: mixing a quantity of the Feedstock Heavy Marine Fuel Oil with a quantity of Activating Gas mixture to give a feedstock mixture; contacting the feedstock mixture with one or more catalysts to form a Process Mixture from the feedstock mixture; separating the Product Heavy Marine Fuel Oil liquid components of the Process Mixture from the gaseous components and by-product hydrocarbon components of the Process Mixture and, discharging the Product Heavy Marine Fuel Oil. The Product Heavy Marine Fuel Oil is compliant with ISO 8217 for residual marine fuel oils and the sulfur and Specific Contaminants have concentration less than 0.5 wt %., wherein the Specific Contaminates are selected from the group consisting of: vanadium, sodium, aluminum, silicon, calcium, zinc, phosphorus, nickel, iron and combinations thereof. The Product Heavy Marine Fuel Oil can be used as or as a blending stock for an ISO 8217 compliant, IMO MARPOL Annex VI (revised) compliant low sulfur or ultralow sulfur heavy marine fuel oil.

The invention relates to a process (100) for deriving polymerizable aromatic compounds having nine carbon atoms (S) in which a component mixture (B) is formed at least partially by steam cracking, in which the component mixture (B) is subjected to a workup (2, 3, 4, 5) comprising a gasoline removal (5) and thereafter is a compression (8) and a fractionation (10), and wherein one or more pyrolysis gasoline fractions (H, L) is or are formed in the gasoline removal (5) and/or the compression (8). The invention provides that a separation feed is formed which comprises predominantly exclusively pyrolysis gasoline from the or at least one of the pyrolysis gasoline fractions (H, L) and that the separation feed is subjected to a separation (7), wherein in the separation (7) at least one fraction (P) enriched in aromatic compounds having nine carbon atoms compared to the separation feed is formed. A corresponding plant likewise forms part of the subject matter of the invention.

A multi-stage process for the production of an ISO8217 compliant Product Heavy Marine Fuel Oil from ISO 8217 compliant Feedstock Heavy Marine Fuel Oil involving a core process under reactive conditions in a Reaction System composed of one or more reaction vessels, wherein one or more of the reaction vessels contains one or more catalysts in the form of a structured catalyst bed and is operated under reactive distillation conditions. The Product Heavy Marine Fuel Oil has a sulfur level has a maximum sulfur content (ISO 14596 or ISO 8754) between the range of 0.05 mass % to 1.0 mass. A process plant for conducting the process for conducting the process is disclosed.

According to embodiments, a process of forming a catalyst for aromatizing hydrocarbons may include enhancing a mesoporosity of a zeolite support by a base-leaching treatment, an acid-leaching treatment, or both to form a zeolite support having enhanced mesoporosity, mixing the zeolite support having enhanced mesoporosity with a solution containing zinc or gallium to disperse the zinc or gallium on the zeolite support having enhanced mesoporosity, and calcining the zeolite support having enhanced mesoporosity with zinc or gallium dispersed thereon to form a zinc- or gallium-doped zeolite catalyst having a mesopore volume of greater than 0.09 cm.sup.3/g and less than 0.20 cm.sup.3/g.

The present disclosure provides a method for producing a clean gasoline and a system for producing the same, the method includes: a full range gasoline is subjected to a directional sulfur transfer reaction, then is cut to obtain a light gasoline fraction, a medium gasoline fraction and a heavy gasoline fraction; the light gasoline fraction is treated to obtain an esterified light gasoline; the medium gasoline fraction is treated to obtain a raffinate oil and an extracted oil; the raffinate oil is treated to obtain an esterified medium gasoline; the heavy gasoline fraction is mixed with the extracted oil to obtain a mixed oil, and a one-stage hydrodesulfurization reaction, a two-stage hydrodesulfurization reaction, H.sub.2S-removal and a hydrocarbon isomerization/aromatization reaction are carried out successively to obtain a treated heavy gasoline; blending the esterified light gasoline, the esterified medium gasoline and the treated heavy gasoline to obtain a clean gasoline.

A molecular separation method can include: passing a deasphalted oil stream through a reactor containing an active substrate, wherein the catalytic active substrate adsorbs heteroatom species from the deasphalted oil stream and produces a pretreated hydrocarbon feed stream essentially free of 4+ ring aromatic molecules (ARC 4+ species), metal species, and heteroatom species; and chromatographically separating with a simulated moving bed apparatus or a true moving bed apparatus (SMB/TMB) the pretreated hydrocarbon feed stream into a saturate fraction and an aromatics fraction.

Embodiments disclosed herein relate to systems and processes for producing olefins and/or dienes. The systems and processes may include thermally cracking a C1-C4 hydrocarbon containing feed to produce a cracked hydrocarbon effluent containing a mixture of olefins and paraffins. The systems and processes may also include dehydrogenating the cracked hydrocarbon effluent to produce a dehydrogenated hydrocarbon effluent containing additional olefins and/or dienes.

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 one or more naphtha fractions from hydroprocessing zones within the battery limits, including vacuum residue hydrocracking, 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. Feed to the gas oil steam cracker in certain embodiments includes gas oil range intermediates from the vacuum residue hydrocracking zone. In addition, a base oil production center is integrated to provide base oils product used for production of synthetic lubes or corresponding lube oil feedstocks

A method of separating hydrocarbons containing three or more carbon atoms from an off-gas stream is provided. This method includes separating a light ends stream from a fractionator, thereby producing a stream rich in hydrocarbons containing three or more carbon atoms, and a stream lean in hydrocarbons containing three or more carbon atoms, separating the stream lean in hydrocarbons containing three or more carbon atoms in a membrane unit, thereby producing a permeate stream enriched in hydrocarbons containing three or more carbon atoms and a retentate stream, and separating the stream rich in hydrocarbons containing three or more carbon atoms in one or more separation columns, thereby producing one or more streams selected from the group consisting of a propylene stream, a propane stream, a butane stream, a light cat naptha stream, and a heavy cat naptha stream.