Back to results
US 11,884,888 B2Granted
Processes and systems for producing aromatic products and hydrogen carriers
AssigneeSaudi Arabian Oil Company
InventorOmer Refa Koseoglu
Life of this patent
Estimating the term…
Abstract
The present disclosure is directed to refinery processes and systems for producing petrochemicals including aromatic products, and hydrogen carriers. Embodiments include those with increased naphtha production, increasing reformer feed. An aromatic rich stream is separated in an aromatic recovery complex to produce BTX, and all or a portion of BTX products subjected to hydrogenation to produce cyclohexanes.
Claims20
An integrated refinery process comprising:
- catalytically reforming naphtha-range hydrocarbons to produce reformate containing C6-C8 aromatic hydrocarbons, wherein the naphtha-range hydrocarbons are obtained from a source within the refinery selected from the group consisting of
- a first naphtha source consisting of naphtha-range hydrocarbons derived from naphtha hydrotreating of straight run naphtha,
- a second naphtha source consisting of naphtha-range hydrocarbons derived from hydrocracking of straight run middle distillates,
- a third naphtha source consisting of naphtha-range hydrocarbons derived from treatment of vacuum gas oil by (a) hydrocracking of vacuum gas oil or (b) fluid catalytic cracking of vacuum gas oil,
- a fourth naphtha source consisting of naphtha-range hydrocarbons derived from treatment of vacuum residue by (a) residue hydrotreating of vacuum residue followed by hydrocracking of hydrotreated vacuum residue, (b) residue hydrotreating of vacuum residue followed by fluid catalytic cracking of hydrotreated vacuum residue, or (c) coking of vacuum residue,
- combinations comprising of two or more of the foregoing, and
- combinations comprising one or more of the foregoing and an additional deeply hydrotreated naphtha source;
- and
- reacting all or a portion of the reformate in the presence of a hydrogenation catalyst containing 0.01-5 wt % of one or more active metal components selected from Pt, Pd, Re and a combination comprising at least two of Pt, Pd or Re, on a catalyst support, at conditions including at a reactor temperature (° C.) in the range of from about 250-320, at a hydrogen partial pressure (bar) in the range of from about 40-100, at a hydrogen gas feed rate (standard liters per liter of hydrocarbon feed, SLt/Lt) of up to about 500-3000, and at a liquid hourly space velocity (h−1), on a fresh feed basis relative to the hydrogenation catalysts, in the range of from about 0.1-5.0, the catalyst and conditions being effective to produce a liquid hydrogenation effluent hydrogen carrier in which at least about 95-99.9 wt % of C6-C8 aromatic hydrocarbons in the reformate are converted to cyclohexanes.
6 more elements
An integrated refinery process comprising:
- separating crude oil by atmospheric distillation into at least straight run naphtha, middle distillates, and atmospheric residue;
- separating atmospheric residue by vacuum distillation into at least vacuum gas oil and vacuum residue;
- hydrotreating the straight run naphtha to produce hydrotreated naphtha as a first naphtha source;
- hydrocracking the middle distillates to produce at least naphtha-range hydrocarbons as a second naphtha source;
- treating at least a portion of the vacuum gas oil to produce at least naphtha-range hydrocarbons as a third naphtha source, wherein treating is by hydrocracking or fluid catalytic cracking;
- optionally subjecting one or more of the first, second and third naphtha sources deep hydrodesulfurization and deep hydrodenitrogenation;
- catalytically reforming all or a portion of naphtha from the first, second and third naphtha sources, optionally subjected to deep hydrodesulfurization and deep hydrodenitrogenation, to produce reformate;
- and
- reacting all or a portion of the reformate in the presence of a hydrogenation catalyst containing 0.01-5 wt % of one or more active metal components selected from Pt, Pd, Re and a combination comprising at least two of Pt, Pd or Re, and on a support containing zeolite at a concentration range of 0.1-20 wt %, at conditions including at a reactor temperature (° C.) in the range of from about 250-320, at a hydrogen partial pressure (bar) in the range of from about 40-100, at a hydrogen gas feed rate (standard liters per liter of hydrocarbon feed, SLt/Lt) of up to about 500-3000, and at a liquid hourly space velocity (h−1), on a fresh feed basis relative to the hydrogenation catalysts, in the range of from about 0.1-5.0, the catalyst and conditions being effective to produce a liquid hydrogenation effluent hydrogen carrier in which at least about 95-99.9 wt % of C6-C8 aromatic hydrocarbons in the reformate are converted to cyclohexanes.
6 more elements
An integrated refinery process comprising:
- catalytically reforming naphtha-range hydrocarbons to produce reformate containing C6-C8 aromatic hydrocarbons, wherein the naphtha-range hydrocarbons are obtained from a source within the refinery selected from the group consisting of
- a first naphtha source consisting of naphtha-range hydrocarbons derived from naphtha hydrotreating of straight run naphtha,
- a second naphtha source consisting of naphtha-range hydrocarbons derived from hydrocracking of straight run middle distillates,
- a third naphtha source consisting of naphtha-range hydrocarbons derived from treatment of vacuum gas oil by (a) hydrocracking of vacuum gas oil or (b) fluid catalytic cracking of vacuum gas oil,
- a fourth naphtha source consisting of naphtha-range hydrocarbons derived from treatment of vacuum residue by (a) residue hydrotreating of vacuum residue followed by hydrocracking of hydrotreated vacuum residue, (b) residue hydrotreating of vacuum residue followed by fluid catalytic cracking of hydrotreated vacuum residue, or (c) coking of vacuum residue,
- combinations comprising of two or more of the foregoing, and
- combinations comprising one or more of the foregoing and an additional deeply hydrotreated naphtha source;
- and
- reacting all or a portion of the reformate in the presence of a hydrogenation catalyst containing wt % of one or more active metal components selected from Pt, Pd, Re and a combination comprising at least two of Pt, Pd or Re, on a catalyst support comprising non-acidic amorphous alumina and about 0.1-15 wt % of a modified USY zeolite having one or more of Ti, Zr and/or Hf substituting aluminum atoms constituting the zeolite framework thereof, at conditions including at a reactor temperature (° C.) in the range of from about 250-320, at a hydrogen partial pressure (bar) in the range of from about 20-100, at a hydrogen gas feed rate (standard liters per liter of hydrocarbon feed, SLt/Lt) of up to about 500-3000, and at a liquid hourly space velocity (h−1), on a fresh feed basis relative to the hydrogenation catalysts, in the range of from about 0.1-5.0, the catalyst and conditions being effective to produce a liquid hydrogenation effluent in which at least about 95-99.9 wt % of C6-C8 aromatic hydrocarbons in the reformate are converted to cyclohexanes.
6 more elements
Dependencies are inferred from the claim text.