An integrated process for maximizing recovery of LPG is provided. The process comprises providing a hydrocarbonaceous feed comprising naphtha, and a hydrogen stream to a reforming zone. The hydrocarbonaceous feed is reformed in the reforming zone in the presence of the hydrogen stream and a reforming catalyst to provide a reformate effluent stream. At least a portion of the reformate effluent stream and at least one stream comprising C6- hydrocarbons from one or more of a hydrocracking zone, an isomerization zone, and a transalkylation zone is passed to a debutanizer column of the reforming zone to provide a fraction comprising liquid petroleum gas (LPG) and a debutanizer column bottoms stream.

A naphtha reforming reactor system comprising a first reactor comprising a first inlet and a first outlet, wherein the first reactor is configured to operate as an adiabatic reactor, and wherein the first reactor comprises a first naphtha reforming catalyst; and a second reactor comprising a second inlet and a second outlet, wherein the second inlet is in fluid communication with the first outlet of the first reactor, wherein the second reactor is configured to operate as an isothermal reactor, and wherein the second reactor comprises a plurality of tubes disposed within a reactor furnace, a heat source configured to heat the interior of the reactor furnace; and a second naphtha reforming catalyst disposed within the plurality of tubes, wherein the first naphtha reforming catalyst and the second naphtha reforming catalyst are the same or different.

L'invention concerne un procédé de production de composés aromatiques C6-C7 à partir d'une charge hydrocarbonée de type naphta comprenant une étape de fractionnement (2) de la charge pour obtenir un flux supérieur et un flux inférieur, une étape de reformage catalytique du flux supérieur (6) et du flux inférieur (9), une étape de recombinaison (15) des effluents de reformat obtenus, une étape de recontactage (16) et une étape de stabilisation (19) des effluents de reformat stabilisé et une étape de séparation (22) du raffinat pour récupérer des composés hydrocarbonés en C6 et C7.

Optimizing power generation from waste heat in large industrial facilities such as petroleum refineries by utilizing a subset of all available hot source streams selected based, in part, on considerations for example, capital cost, ease of operation, economics of scale power generation, a number of ORC machines to be operated, operating conditions of each ORC machine, combinations of them, or other considerations are described. Recognizing that several subsets of hot sources can be identified from among the available hot sources in a large petroleum refinery, subsets of hot sources that are optimized to provide waste heat to one or more ORC machines for power generation are also described. Further, recognizing that the utilization of waste heat from all available hot sources in a mega-site such as a petroleum refinery and aromatics complex is not necessarily or not always the best option, hot source units in petroleum refineries from which waste heat can be consolidated to power the one or more ORC machines are identified.

Configurations and related processing schemes of direct or indirect inter-plants (or both) heating systems synthesized for grassroots medium grade crude oil semi-conversion refineries to increase energy efficiency from specific portions of low grade waste heat sources are described. Configurations and related processing schemes of direct or indirect inter-plants (or both) heating systems synthesized for integrated medium grade crude oil semi-conversion refineries and aromatics complex for increasing energy efficiency from specific portions of low grade waste sources are also described.

Configurations and related processing schemes of direct or indirect (or both) intra-plants and thermally coupled heating systems synthesized for grassroots medium grade crude oil semi-conversion refineries to increase energy efficiency from specific portions of low grade waste heat sources are described. Configurations and related processing schemes of direct or indirect (or both) intra-plants and thermally coupled heating systems synthesized for integrated medium grade crude oil semi-conversion refineries and aromatics complex for increasing energy efficiency from specific portions of low grade waste sources are also described.

Configurations and related processing schemes of specific inter-plants and hybrid, intra- and inter- plants waste heat recovery schemes for thermal energy consumption reduction in integrated refining-petrochemical facilities synthesized for grassroots medium grade crude oil semi-conversion refineries to increase energy efficiency from specific portions of low grade waste heat sources are described. Configurations and related processing schemes of specific inter-plants and hybrid, intra- and inter- plants waste heat recovery schemes for thermal energy consumption reduction in integrated refining-petrochemical facilities synthesized for integrated medium grade crude oil semi-conversion refineries and aromatics complex for increasing energy efficiency from specific portions of low grade waste sources are also described.

Described herein is a two-stage reforming process using a unique configuration which allows the reforming unit to operate at a higher naphtha feed rate as compared to conventional reforming configurations. In the unique reforming process described herein, a naphtha feedstock undergoes a distillation step prior to the first reforming stage. The distillation step separates the naphtha feedstock into a top light C₆/C₇ stream, which typically accounts for between 5 and 20 percent of the overall feedstock, and a C₈+ stream. The C₈+ stream undergoes reforming in a first stage consisting of at least one reactor containing conventional metallic reforming catalyst, under conditions sufficient to convert the C₈+ stream into a first intermediate reformate. The C₆/C₇ stream, bypasses the first stage and is combined with the intermediate reformate, and reformed in the second stage, at lower pressure than in the first stage, over a reforming catalyst containing a medium pore zeolite.

Described herein is a two-stage reforming process using a unique configuration which allows the reforming unit to operate at a higher naphtha feed rate as compared to conventional reforming configurations. In the unique reforming process described herein, a naphtha feedstock undergoes a distillation step prior to the first reforming stage. The distillation step separates the naphtha feedstock into a top light a C₇ stream, which typically accounts for between 5 and 20 percent of the overall feedstock, and a C₈+ stream. The C₈+ stream undergoes reforming in a first stage consisting of at least one reactor containing conventional metallic reforming catalyst, under conditions sufficient to convert the C₈+ stream into a first intermediate reformate. The C₇ stream, bypasses the first stage and is combined with the intermediate reformate, and reformed in the second stage, at lower pressure than in the first stage, over a reforming catalyst containing a medium pore zeolite.