Patent Publication Number: US-11384294-B1

Title: Systems and processes for treating disulfide oil

Description:
TECHNICAL FIELD 
     Embodiments of the present disclosure generally relate to upgrading petroleum-based compositions, and more specifically relate to supercritical reactor systems, methods, and uses for upgrading petroleum-based compositions. 
     BACKGROUND 
     Petroleum is an indispensable source of energy; however, most petroleum is heavy or sour petroleum, meaning that it contains a high amount of impurities (including sulfur and coke, a high carbon petroleum residue). Heavy petroleum must be upgraded before it is a commercially valuable product, such as fuel. Supercritical water has been known to be an effective reaction medium for heavy oil upgrading without external supply of hydrogen, at least because supercritical water upgrading reactions are highly selective towards breaking of heavy fractions to produce middle distillate oils without coke generation. 
     SUMMARY 
     Although supercritical water has been known to be an effective reaction medium for heavy oil upgrading without an external supply of hydrogen, the upgraded product from a supercritical water process has a greater aromaticity and olefinicity than the hydrocarbon feed, which has negative effect on the stability of the products. Nuclear magnetic resonance (NMR) analysis has shown that the asphaltene content of supercritical water treated oil decreased to a large extent, while saturate, olefin, and aromatic content increased. Additionally, the extent of hydrocarbon upgrading in conventional supercritical water upgrading processes may be limited. The high temperature of supercritical water reactor induces thermal cracking of chemical bonds such as carbon-sulfur bonds and carbon-carbon bonds. Broken bonds should be filled with other atoms, preferably hydrogen, to avoid intermolecular condensation and generation of olefins and polycondensed aromatics. Although olefins are very valuable chemicals, the low stability of unsaturated bonds can degrade products by forming gums. The hydrogen inherently present in the water molecules can participate in the cracking reaction, but the extent of hydrogen donation from water is quite limited in supercritical water conditions due to high hydrogen-oxygen bond energy. 
     Accordingly, a need exists for a hydrocarbon upgrading process that incorporates the benefits of conventional supercritical water upgrading processes, while decreasing the large hydrocarbon radicals and olefins that are hydrothermally generated by supercritical water. The present disclosure addresses this need by incorporating hydrogen addition into the supercritical water hydrocarbon upgrading process. 
     Hydrogen addition into the supercritical water process provides additional yields of middle distillate oils but at improved stability by saturating heavy hydrocarbon radicals and olefins that have potential to generate gums. In addition, the supercritical water process breaks large asphaltene aggregates, such as aggregates with a size from 1 to 800 microns (μm), to much smaller scattered radical aggregates, such as aggregates with a size from 0.1 to 300 nanometers (nm) that can readily be saturated by hydrogen due to its small size (1.06-1.20 angstrom). This in turn reduces the asphaltene content in the oil by converting them into lighter fractions. Therefore, supercritical water facilitates the hydrogenation of heavy hydrocarbon radicals including olefin and alphaltene radicals and prevents their combination reactions that terminate the upgrading reaction mechanism. In other words, the hydrogen addition to the supercritical water process passivates the combination reactions of large hydrocarbon radicals and olefins that are hydrothermally generated by supercritical water, thereby preventing gum, asphaltene, and coke generation, which allows for increasing process severity for additional oil upgrading. 
     In accordance with one embodiment of the present disclosure, a process for treating a disulfide oil composition is provided. The process includes combining a supercritical water stream, a hydrogen stream, and a disulfide oil composition in a mixing device to create a combined disulfide feed stream; introducing the combined disulfide feed stream into a supercritical water hydrogenation reactor operating at a temperature greater than a critical temperature of water and a pressure greater than a critical pressure of water; and at least partially converting the combined disulfide feed stream to an upgraded disulfide product. 
    
    
     
       BRIEF DESCRIPTION OF THE DRAWINGS 
       The following detailed description of specific embodiments of the present disclosure can be best understood when read in conjunction with the following drawings, in which: 
         FIG. 1  is a schematic view of a process for upgrading a hydrocarbon-based composition, according to the present embodiments; and 
         FIG. 2  is a schematic view of a process for treating a disulfide oil composition, according to the present embodiments. 
     
    
    
     DETAILED DESCRIPTION 
     Embodiments of the present disclosure are directed to processes for upgrading hydrocarbon streams in a supercritical water hydrogenation reactor. 
     As used throughout the disclosure, “supercritical” refers to a substance at or above a pressure and a temperature greater than or equal to that of its critical pressure and temperature, such that distinct phases do not exist and the substance may exhibit the fast diffusion of a gas while dissolving materials like a liquid. As such, supercritical water is water having a temperature and pressure greater than or equal to the critical temperature and the critical pressure of water. At a temperature and pressure greater than or equal to the critical temperature and pressure, the liquid and gas phase boundary of water disappears, and the fluid has characteristics of both liquid and gaseous substances. Supercritical water is able to dissolve organic compounds like an organic solvent and has excellent diffusibility like a gas. Regulation of the temperature and pressure allows for continuous “tuning” of the properties of the supercritical water to be more liquid-like or more gas-like. Supercritical water has reduced density and lesser polarity, as compared to liquid-phase subcritical water, thereby greatly extending the possible range of chemistry that can be carried out in water. Water above its critical condition is neither a liquid nor gas but a single fluid phase that converts from being polar to non-polar. 
     As used throughout the disclosure, “upgrade” means to increase the API gravity, decrease the amount of impurities, such as sulfur, nitrogen, and metals, decrease the amount of asphaltene, and increase the amount of the light fraction. 
     Supercritical water has various unexpected properties as it reaches supercritical boundaries. Supercritical water has very high solubility toward organic compounds and has an infinite miscibility with gases. Furthermore, radical species can be stabilized by supercritical water through the cage effect (that is, a condition whereby one or more water molecules surrounds the radical species, which then prevents the radical species from interacting). Without being limited to theory, stabilization of radical species helps prevent inter-radical condensation and thereby reduces the overall coke production in the current embodiments. For example, coke production can be the result of the inter-radical condensation. In certain embodiments, supercritical water generates hydrogen gas through a steam reforming reaction and water-gas shift reaction, which is then available for the upgrading reactions. 
     Moreover, the high temperature and high pressure of supercritical water may give supercritical water a density of 0.123 grams per milliliter (g/mL) at 27 MPa and 450° C. Contrastingly, if the pressure was reduced to produce superheated steam, for example, at 20 MPa and 450° C., the superheated steam would have a density of only 0.079 g/mL. At that density, the hydrocarbons may interact with superheated steam to evaporate and mix into the vapor phase, leaving behind a heavy fraction that may generate coke upon heating. The formation of coke or coke precursor may plug the lines and must be removed. Therefore, supercritical water is superior to steam in some applications. 
     Specific embodiments will now be described with references to the figures. Whenever possible, the same reference numerals will be used throughout the drawings to refer to the same or like parts. 
       FIG. 1  schematically depicts a process  100  for upgrading a hydrocarbon-based composition  105 , according to embodiments described herein. 
     The hydrocarbon-based composition  105  may refer to any hydrocarbon source derived from petroleum, coal liquid, or biomaterials. Possible sources for hydrocarbon-based composition may include crude oil, distilled crude oil, reduced crude oil, residue oil, topped crude oil, product streams from oil refineries, product streams from steam cracking processes, liquefied coals, liquid products recovered from oil or tar sands, bitumen, oil shale, asphaltene, biomass hydrocarbons, and the like. Many compositions are suitable for the hydrocarbon-based composition. In some embodiments, the hydrocarbon-based composition  105  may comprise heavy crude oil or a fraction of heavy crude oil. In other embodiments, the hydrocarbon-based composition  105  may include atmospheric residue (AR), atmospheric distillates, vacuum gas oil (VGO), vacuum distillates, or vacuum residue (VR), or cracked product (such as light cycle oil or coker gas oil). In some embodiments, the hydrocarbon-based composition may be combined streams from a refinery, produced oil, or other hydrocarbon streams, such as from an upstream operation. The hydrocarbon-based composition  105  may be decanted oil, oil containing 10 or more carbons (C10+ oil), or hydrocarbon streams from an ethylene plant. The hydrocarbon-based composition  105  may, in some embodiments, be liquefied coal or biomaterial-derivatives, such as bio fuel oil. In some embodiments, used lubrication (lube) oil or brake fluids may be used. 
     The hydrocarbon-based composition  105  may, in some embodiments, be naphtha or kerosene or diesel fractions. Such fractions may be used but may not be upgraded as efficiently by the supercritical water. Contaminated hydrocarbon fractions may also be used. In some embodiments, fractions with saltwater contamination may be used as the hydrocarbon-based composition  105 . For instance, crude oil in market typically has a salt content below about 10 PTB (pounds of salt per 1000 barrels of oil). The salt in saltwater may be precipitated by the supercritical water to produce a desalted product, which may be desirable in some embodiments. 
     The hydrocarbon-based composition  105  may have a T 5  true boiling point (TBP) of less than 500° C., of less than 450° C., of less than 400° C., of less than 380° C., or of less than 370° C. In embodiments, the hydrocarbon-based composition  105  may have a T 5  TBP of from 200° C. to 500° C., from 200° C. to 450° C., from 200° C. to 425° C., from 200° C. to 400° C., from 200° C. to 380° C., from 200° C. to 370° C., from 250° C. to 500° C., from 250° C. to 450° C., from 250° C. to 425° C., from 250° C. to 400° C., from 250° C. to 380° C., from 250° C. to 370° C., from 260° C. to 500° C., from 260° C. to 450° C., from 260° C. to 425° C., from 260° C. to 400° C., from 260° C. to 380° C., from 260° C. to 370° C., from 300° C. to 500° C., from 300° C. to 450° C., from 300° C. to 425° C., from 300° C. to 400° C., from 300° C. to 380° C., from 300° C. to 370° C., from 325° C. to 500° C., from 325° C. to 450° C., from 325° C. to 425° C., from 325° C. to 400° C., from 325° C. to 380° C., from 325° C. to 370° C., from 350° C. to 500° C., from 350° C. to 450° C., from 350° C. to 425° C., from 350° C. to 400° C., from 350° C. to 380° C., from 350° C. to 370° C., or approximately 367° C. The hydrocarbon-based composition  105  may have a T 90  TBP of less than or equal to 750° C., less than or equal to 700° C., or less than or equal to 650° C. In embodiments, the hydrocarbon-based composition  105  may have a T 90  TBP from 500° C. to 750° C., from 500° C. to 700° C., from 500° C. to 675° C., from 500° C. to 650° C., from 540° C. to 750° C., from 540° C. to 700° C., from 540° C. to 675° C., from 540° C. to 650° C., from 600° C. to 750° C., from 600° C. to 700° C., from 600° C. to 675° C., from 600° C. to 650° C., from 625° C. to 750° C., from 625° C. to 700° C., from 625° C. to 675° C., from 625° C. to 650° C., where the T 90  TBP is greater than the T 5  TBP previously described. The hydrocarbon-based composition  105  may have an API gravity from 5° to 23°, from 5° to 20°, from 5° to 19°, from 5° to 15°, from 5° to 12°, from 8° to 23°, from 8° to 20°, from 8° to 19°, from 8° to 15°, from 8° to 12°, from 10° to 23°, from 10° to 20°, from 10° to 19°, from 10° to 15°, from 10° to 12°, or approximately 11°. The hydrocarbon-based composition  105  may include greater than 2.7 weight percent (wt. %) or greater than 1.7 wt. % total sulfur content by weight of the hydrocarbon-based composition  105 . In embodiments, the hydrocarbon-based composition  105  may include from 0.1 wt. % to 5 wt. %, from 0.1 wt. % to 4 wt. %, from 0.1 wt. % to 3.5 wt. %, from 0.5 wt. % to 5 wt. %, from 0.5 wt. % to 4 wt. %, from 0.5 wt. % to 3.5 wt. %, from 1.0 wt. % to 5 wt. %, from 1.0 wt. % to 4 wt. %, from 1.0 wt. % to 3.5 wt. %, from 1.3 wt. % to 5 wt. %, from 1.3 wt. % to 4 wt. %, from 1.3 wt. % to 3.5 wt. %, from 1.6 wt. % to 5 wt. %, from 1.6 wt. % to 4 wt. %, from 1.6 wt. % to 3.5 wt. %, from 1.8 wt. % to 5 wt. %, from 1.8 wt. % to 4 wt. %, from 1.8 wt. % to 3.5 wt. %, from 2.0 wt. % to 5 wt. %, from 2.0 wt. % to 4 wt. %, from 2.0 wt. % to 3.5 wt. %, from 2.3 wt. % to 5 wt. %, from 2.3 wt. % to 4 wt. %, from 2.3 wt. % to 3.5 wt. %, from 2.6 wt. % to 5 wt. %, from 2.6 wt. % to 4 wt. %, from 2.6 wt. % to 3.5 wt. %, from 2.8 wt. % to 5 wt. %, from 2.8 wt. % to 4 wt. %, from 2.8 wt. % to 3.5 wt. %, from 3.0 wt. % to 5 wt. %, from 3.0 wt. % to 4 wt. %, from 3.0 wt. % to 3.5 wt. %, or approximately 3.4 wt. % wt. % total sulfur content by weight of the hydrocarbon-based composition  105 . The hydrocarbon-based composition  105  may include greater than 0.9 wt. % or greater than 0.3 wt. % wt. % total nitrogen content by weight of the hydrocarbon-based composition  105 . In embodiments, the hydrocarbon-based composition  105  may include from 0.01 wt. % to 2 wt. %, from 0.01 wt. % to 1.3 wt. %, from 0.1 wt. % to 2 wt. %, from 0.1 wt. % to 1.3 wt. %, from 0.2 wt. % to 2 wt. %, from 0.2 wt. % to 1.3 wt. %, from 0.4 wt. % to 2 wt. %, from 0.4 wt. % to 1.3 wt. %, from 0.6 wt. % to 2 wt. %, from 0.6 wt. % to 1.3 wt. %, from 0.8 wt. % to 2 wt. %, from 0.8 wt. % to 1.3 wt. %, from 1.0 wt. % to 2 wt. %, from 1.0 wt. % to 1.3 wt. %, or approximately 1.2 wt. % wt. % total nitrogen content by weight of the hydrocarbon-based composition  105 . The hydrocarbon-based composition  105  may include greater than 1.7 wt. % or greater than 0.3 wt. % asphaltene (heptane-insoluble) by weight of the hydrocarbon-based composition  105 . In embodiments, the hydrocarbon-based composition  105  may include from 0.01 wt. % to 6 wt. %, from 0.01 wt. % to 5 wt. %, from 0.01 wt. % to 4.9 wt. %, from 0.1 wt. % to 6 wt. %, from 0.1 wt. % to 5 wt. %, from 0.1 wt. % to 4.9 wt. %, from 0.2 wt. % to 6 wt. %, from 0.2 wt. % to 5 wt. %, from 0.2 wt. % to 4.9 wt. %, from 0.4 wt. % to 6 wt. %, from 0.4 wt. % to 5 wt. %, from 0.4 wt. % to 4.9 wt. %, from 0.6 wt. % to 6 wt. %, from 0.6 wt. % to 5 wt. %, from 0.6 wt. % to 4.9 wt. %, from 0.8 wt. % to 6 wt. %, from 0.8 wt. % to 5 wt. %, from 0.8 wt. % to 4.9 wt. %, from 1.0 wt. % to 6 wt. %, from 1.0 wt. % to 5 wt. %, from 1.0 wt. % to 4.9 wt. %, from 1.6 wt. % to 6 wt. %, from 1.6 wt. % to 5 wt. %, from 1.6 wt. % to 4.9 wt. %, from 1.8 wt. % to 6 wt. %, from 1.8 wt. % to 5 wt. %, from 1.8 wt. % to 4.9 wt. %, from 2.0 wt. % to 6 wt. %, from 2.0 wt. % to 5 wt. %, from 2.0 wt. % to 4.9 wt. %, from 2.5 wt. % to 6 wt. %, from 2.5 wt. % to 5 wt. %, from 2.5 wt. % to 4.9 wt. %, from 3.0 wt. % to 6 wt. %, from 3.0 wt. % to 5 wt. %, from 3.0 wt. % to 4.9 wt. %, from 4.7 wt. % to 6 wt. %, from 4.7 wt. % to 5 wt. %, from 4.7 wt. % to 4.9 wt. %, or approximately 4.8 wt. % asphaltene (heptane-insoluble) by weight of the hydrocarbon-based composition  105 . The hydrocarbon-based composition  105  may include greater than 9 parts per million (ppm) or greater than 4 ppm metals. In embodiments, the metals may be vanadium, nickel, or both. In embodiments, the hydrocarbon-based composition may include from 1 ppm to 100 ppm, from 1 ppm to 83 ppm, from 5 ppm to 100 ppm, from 5 ppm to 83 ppm, from 10 ppm to 100 ppm, from 10 ppm to 83 ppm, from 50 ppm to 100 ppm, from 50 ppm to 83 ppm, or approximately 82 ppm metals. The hydrocarbon-based composition  105  may have a viscosity at 50° C. of greater than 27 centiStokes (cSt) or greater than 89 cSt. In embodiments, the hydrocarbon-based composition  105  may have a viscosity at 50° C. from 5 cSt to 1000 cSt, from 5 cSt to 700 cSt, from 5 cSt to 650 cSt, from 10 cSt to 1000 cSt, from 10 cSt to 700 cSt, from 10 cSt to 650 cSt, from 100 cSt to 1000 cSt, from 100 cSt to 700 cSt, from 100 cSt to 650 cSt, from 300 cSt to 1000 cSt, from 300 cSt to 700 cSt, from 300 cSt to 650 cSt, from 500 cSt to 1000 cSt, from 500 cSt to 700 cSt, from 500 cSt to 650 cSt, or approximately 640 cSt. 
     As shown in  FIG. 1 , the hydrocarbon-based composition  105  may be pressurized in hydrocarbon pump  112  to create pressurized hydrocarbon-based composition  116 . The pressure of pressurized hydrocarbon-based composition  116  may be at least 22.1 megapascals (MPa), which is approximately the critical pressure of water. Alternatively, the pressure of the pressurized hydrocarbon-based composition  116  may be between 23 MPa and 35 MPa, or between 24 MPa and 30 MPa. For instance, the pressure of the pressurized hydrocarbon-based composition  116  may be between 25 MPa and 29 MPa, 26 MPa and 28 MPa, 25 MPa and 30 MPa, 26 MPa and 29 MPa, or 24 MPa and 28 MPa. 
     The pressurized hydrocarbon-based composition  116  may then be heated in one or more hydrocarbon pre-heaters  120  to form pressurized, heated hydrocarbon-based composition  124 . In one embodiment, the pressurized, heated hydrocarbon-based composition  124  has a pressure greater than the critical pressure of water and a temperature greater than 75° C. Alternatively, the temperature of the pressurized, heated hydrocarbon-based composition  124  is between 10° C. and 300° C., or between 50° C. and 250° C., or between 75° C. and 225° C., or between 100° C. and 200° C., or between 125° C. and 175° C., or between 140° C. and 160° C. According to embodiments, the pressurized, heated hydrocarbon-based composition  124  should not be heated above about 350° C., and in some embodiments, the pressurized, heated hydrocarbon-based composition should not be heated above 300° C. to avoid the formation of coking products. See Hozuma, U.S. Pat. No. 4,243,633, which is incorporated by reference in its entirety. While some coke or coke precursor products may be able to pass through process lines without slowing or stopping the process  100 , the formation of these potentially problematic compounds should be avoided if possible. 
     Embodiments of the hydrocarbon pre-heater  120  may include a natural gas fired heater, heat exchanger, or an electric heater or any type of heater known in the art. In some embodiments, not shown, the pressurized, heated hydrocarbon-based composition  124  may be heated in a double pipe heat exchanger. For example, and not by way of limitation, the double pipe heat exchanger may heat the pressurized, heated hydrocarbon-based composition  124  after it has combined with a heated water stream  126  and/or a heated hydrogen stream  129  to form a combined feed stream  132 . 
     The water stream  110  may be any source of water, such as a water stream having conductivity of less than 1 microSiemens (μS)/centimeters (cm), such as less than 0.1 μS/cm. The water stream  110  may also include demineralized water, distilled water, boiler feed water (BFW), and deionized water. In at least one embodiment, water stream  110  is a boiler feed water stream. Water stream  110  is pressurized by water pump  114  to produce pressurized water stream  118 . The pressure of the pressurized water stream  118  is at least 22.1 MPa, which is approximately the critical pressure of water. Alternatively, the pressure of the pressurized water stream  118  may be between 23 MPa and 35 MPa, or between 24 MPa and 30 MPa. For instance, the pressure of the pressurized water stream  118  may be between 25 MPa and 29 MPa, 26 MPa and 28 MPa, 25 MPa and 30 MPa, 26 MPa and 29 MPa, or 24 MPa and 28 MPa. 
     The pressurized water streams  118 ,  218 , and  318  may then be heated in a water pre-heater  122  to create heated water stream  126 . According to embodiments, the temperature of the heated water stream  126  is greater than 100° C. In embodiments, the temperature of the heated water stream  126  may be from 100° C. to 370° C., from 100° C. to 350° C., from 100° C. to 300° C., from 100° C. to 250° C., from 100° C. to 200° C., from 100° C. to 150° C., from 150° C. to 370° C., from 150° C. to 350° C., from 150° C. to 300° C., from 150° C. to 250° C., from 150° C. to 200° C., from 200° C. to 370° C., from 200° C. to 350° C., from 200° C. to 300° C., from 200° C. to 250° C., from 250° C. to 370° C., from 250° C. to 350° C., from 250° C. to 300° C., from 300° C. to 370° C., from 300° C. to 350° C., or from 350° C. to 370° C. 
     Similar to hydrocarbon pre-heater  120 , suitable water pre-heaters  122  may include a natural gas fired heater, a heat exchanger, and an electric heater. The water pre-heater  122  may be a unit separate and independent from the hydrocarbon pre-heater  120 . 
     The hydrogen stream  127  may be any source of hydrogen. The hydrogen stream  127  may be heated in a hydrogen pre-heater  128  to create heated hydrogen stream  129 . According to embodiments, the temperature of the heated hydrogen stream  129  is greater than 100° C. In embodiments, the temperature of the heated hydrogen stream  129  may be from 100° C. to 370° C., from 100° C. to 350° C., from 100° C. to 300° C., from 100° C. to 250° C., from 100° C. to 200° C., from 100° C. to 150° C., from 150° C. to 370° C., from 150° C. to 350° C., from 150° C. to 300° C., from 150° C. to 250° C., from 150° C. to 200° C., from 200° C. to 370° C., from 200° C. to 350° C., from 200° C. to 300° C., from 200° C. to 250° C., from 250° C. to 370° C., from 250° C. to 350° C., from 250° C. to 300° C., from 300° C. to 370° C., from 300° C. to 350° C., or from 350° C. to 370° C. 
     Similar to hydrocarbon pre-heater  120  and water pre-heater  122 , suitable hydrogen pre-heaters  128  may include a natural gas fired heater, a heat exchanger, and an electric heater. The hydrogen pre-heater  128  may be a unit separate and independent from the hydrocarbon pre-heater  120  and the water pre-heater  122 . 
     The heated water stream  126 , the heated hydrogen stream  129 , and the pressurized, heated hydrocarbon-based composition  124  may then be mixed in a feed mixer  130  to produce a combined feed stream  132 . The feed mixer  130  can be any type of mixing device capable of mixing the heated water stream  126  and the pressurized, heated hydrocarbon-based composition  124 . In one embodiment, the feed mixer  130  may be a mixing tee. The feed mixer  130  may be an ultrasonic device, a small continuous stir tank reactor (CSTR), or any suitable mixer. The volumetric flow ratio of each component fed to the feed mixer  130  may vary. It should also be understood that in one or more embodiments, which are not shown, multiple feed mixers may be used to individually mix the pressurized, heated hydrocarbon-based composition  124 , the heated hydrogen stream  129 , and the heated water stream  126  in any combination. In embodiments, the volumetric flow ratio of the heated hydrocarbon-based composition  124  to the heated water stream  126  may be from 1:10 to 1:1, from 1:10 to 1:5, from 1:10 to 1:2, from 1:5 to 1:1, from 1:5 to 1:2, or from 1:2 to 1:1 at standard ambient temperature and ambient pressure (SATP). In embodiments it is desirable that the volumetric flow rate of water is greater than the volumetric flow rate of hydrocarbons. Without being bound by any particular theory, it is believed that heavy oils such as residual and bituminous types are rich in fractions that contain asphaltenes and heavy polycondensed aromatic molecules. These fractions yield a high viscosity. Mixing hot compressed water, such as supercritical water, reduces the viscosity and improves the oil&#39;s mobility through the developed mixed oil/water phase. Therefore, having a water flow rate that is higher than an oil flow rate improves the mixture mobility especially for highly viscous oils. Furthermore, increasing the water-to-oil ratio improves the caging effect of water molecules surrounding the asphaltenic and polycondensed aromatic molecules and increases the distance between them to prevent their propagation and association. In embodiments, the hydrogen-to-oil volumetric flow can be from 10 to 5000 cubic feet of heated hydrogen stream  129  to one barrel of heated hydrocarbon-based composition  124 , at SATP. 
     The combined feed stream  132  may then be introduced to the supercritical water hydrogenation reactor  150  that is configured to upgrade the combined feed stream  132 . The supercritical water hydrogenation reactor  150  may be an upflow, downflow, or horizontal flow reactor. An upflow, downflow or horizontal reactor refers to the direction the supercritical water and hydrocarbon-based composition flow through the supercritical water hydrogenation reactor  150 . An upflow, downflow, or horizontal flow reactor may be chosen based on the desired application and system configuration. Without intending to be bound by any theory, in downflow supercritical reactors, heavy hydrocarbon fractions may flow very quickly due to having a greater density, which may result in shortened residence times (known as channeling). This may hinder upgrading, as there is less time for reactions to occur. Upflow supercritical reactors have a uniform increased residence time distribution (no channeling), but may experience difficulties due to undissolved portion of heavy fraction and large particles, such as carbon-containing compounds in the heavy fractions, accumulating in the bottom of the reactor. This accumulation may hinder the upgrading process and plug the reactor. Upflow reactors typically utilize catalysts to provide increased contact with the reactants; however, the catalysts may break down due to the harsh conditions of supercritical water, forming insoluble aggregates, which may generate coke. Horizontal reactors may be useful in applications that desire phase separation or that seek to reduce pressure drop, however; the control of hydrodynamics of internal fluid is difficult. Each type of reactor flow has positive and negative attributes that vary based on the applicable process; however, in some embodiments, an upflow or downflow reactor may be favored. 
     The supercritical water hydrogenation reactor  150  may operate at a temperature greater than the critical temperature of water and a pressure greater than the critical pressure of water. In one or more embodiments, the supercritical water hydrogenation reactor  150  may have a temperature of between 380° C. to 480° C., or between 390° C. to 450° C. The supercritical water hydrogenation reactor  150  may be an isothermal or non-isothermal reactor. The reactor may be a tubular-type vertical reactor, a tubular-type horizontal reactor, a vessel-type reactor, a tank-type reactor having an internal mixing device, such as an agitator, or a combination of any of these reactors. Moreover, additional components, such as a stirring rod or agitation device may also be included in the supercritical water hydrogenation reactor  150 . 
     The supercritical water hydrogenation reactor  150  may have dimensions defined by the equation L/D, where L is a length of the supercritical water hydrogenation reactor  150  and D is the diameter of the supercritical water hydrogenation reactor  150 . In one or more embodiments, the L/D value of the supercritical water hydrogenation reactor  150  may be sufficient to achieve a superficial velocity of fluid greater than 0.5 meter (m)/minute (min), or an L/D value sufficient to achieve a superficial velocity of fluid between 1 m/min and 5 m/min. Such relatively high fluid velocity is desired to attain full turbulence of the internal fluid. The desired Reynolds number (a measurement of fluid flow) is greater than 5000. Reynolds number is given by the relationship: 
             Re   =     uD   v           
where u is the superficial velocity, D is the diameter of the supercritical upgrading reactor, and v is the kinematic viscosity. If that equation is rewritten as
 
             u   =       v   ⁢   R   ⁢   e     D           
it can be observed from this relationship that by decreasing the reactor diameter (D) the superficial velocity (u) is increased (because u and D are indirectly proportional to each other (
 
                 (     u   ⁢   α   ⁢     1   D       )     )     .         
For a fixed reactor length at a reference case, decreasing the reactor diameter (D) will increase the ratio (L/D). Furthermore, by increasing the superficial velocity (u), Reynolds Number (Re) is increased (because u and Re are directly proportional to each other (u α Re). Therefore, from the above rationale, in order to maintain the flow in high flow turbulence regime (Re&gt;5000), it is required to increase the superficial velocity, and/or decrease the reactor&#39;s diameter, and by decreasing the reactor&#39;s diameter, the ratio (L/D) is also increased.
 
     In some embodiments, the residence time of the internal fluid in the supercritical water hydrogenation reactor  150  may be longer than 5 seconds, such as longer than 1 minute. In some embodiments, the residence time of the internal fluid in the supercritical water hydrogenation reactor  150  may be from 1 to 30 minutes, from 1 to 20 minutes, from 1 to 15 minutes, from 1 to 12 minutes, from 1 to 10 minutes, from 1 to 8 minutes, from 1 to 5 minutes, from 1 to 2 minutes, from 2 to 30 minutes, from 2 to 20 minutes, from 2 to 15 minutes, from 2 to 12 minutes, from 2 to 10 minutes, from 2 to 8 minutes, from 2 to 5 minutes, from 5 to 30 minutes, from 5 to 20 minutes, from 5 to 15 minutes, from 5 to 12 minutes, from 5 to 10 minutes, from 5 to 8 minutes, from 8 to 30 minutes, from 8 to 20 minutes, from 8 to 15 minutes, from 8 to 12 minutes, from 8 to 10 minutes, from 10 to 30 minutes, from 10 to 20 minutes, from 10 to 15 minutes, from 10 to 12 minutes, from 12 to 30 minutes, from 12 to 20 minutes, from 12 to 15 minutes, from 15 to 30 minutes, from 15 to 20 minutes, or from 20 to 30 minutes. In embodiments, the residence time may be no greater than 15 minutes and no less than 2 minutes. 
     The supercritical water upgrading process is aided by the addition of the heated hydrogen stream  129  to convert a greater amount of heavy hydrocarbons into lighter hydrocarbons. The supercritical water upgrading process and the addition of the heated hydrogen stream have a synergistic effect because the supercritical water dissolves the oil; maximizes mixing of the combined feed stream  130  (oil, water, and hydrogen components); ruptures hydrocarbon and heteroatom chemical bonds; cages asphaltenes and large hydrocarbon radicals (preventing their polymerization); and provides high pressure that brings hydrogen to hydrocarbon and heteroatom radicals&#39; moieties to further rupture chemical bonds and saturate the free hydrocarbon and heteroatom radicals; and the hydrogen addition facilitates rupturing hydrocarbon and heteroatom chemical bonds and saturates the free hydrocarbon and heteroatom radicals generated by the combined effect of supercritical water and the added hydrogen. Specifically, the hydrogen addition may suppress gummy olefin, asphaltene, and coke generation; increase the conversion of the heavy fraction (hydrocarbons having a T 5  of greater than 540° C. and/or an API gravity of less than 17°) in the combined feed stream  130  to lighter fractions; allow for increasing operating severity by either increasing temperature or reducing flow rate, thereby increasing the heavy fraction conversion; and provide hydrotreating to the combined feed stream  130  by converting heteroatoms such as sulfur to H 2 S. 
     Thermal processes are temperature driven chemical processes that convert and upgrade petroleum heavy hydrocarbons via radical mechanism. The typical thermal cracking processes temperature range is between 495 and 540° C. and typical pressure is in the range of 10 and 40 atmospheres. The severities of thermal processes determine the extent of feed conversion. Process severity refers to the levels of operating conditions in terms of combinations of temperature and space times. Thermal processes utilize heat to crack heavy hydrocarbons into lighter end products, thereby reducing the oil viscosity without catalyst addition. However, the presence of asphaltenes in the heavy hydrocarbons limits upgradability. The amount of asphaltene in the hydrocarbon stream is directly related to its affinity to form coke, due to asphaltene condensation reactions. See Yan, T. Y.,  Characterization of visbreaker feeds . Fuel, 1990. 69(8): p. 1062-1064. The reactions taking place in thermal processes are a combination of endothermic reactions that proceed according to free radical mechanisms. The chemistry of thermal cracking is rather complex, and the degree of complexity increases with the increase in process severity for heavier feedstocks. Through thermal cracking, chemical bonds of different species present in the oil are subjected to endothermic homolytic dissociation reactions. During this bond cleavage procedure, the asphaltene solvating appendages are detached and the aliphatic bridges, connecting the polyaromatic clusters within the asphaltene molecules, are broken. This makes the asphaltene aggregates prone to precipitation in a less peptizing environment. In addition, dehydrogenation reactions of asphaltene aggregates result in increasing C/H ratios, which increase the molecular weight of the asphaltene molecules. Thermal processes proceed by initiation reactions where a portion of feed hydrocarbon molecules (M) break into multiple hydrocarbon radicals (R.), by homolytic cleavage of the C—C bonds. As a result, free radicals are accumulated until reaching a steady-stable concentration that allows the thermal cracking propagation reactions to continue. The generated free radicals shown by Equation 1 below drive the rest of the reactions.
 
M→R.+R n .  (1)
 
     The above reaction step is followed by a chain of reactions, which includes hydrogen abstraction and addition, and radical cracking and recombination. The produced free radicals abstract hydrogen from nearby molecules, as shown by Equation 2.
 
R.+M→R 1 .+RH  (2)
 
     Generated radicals are also dealkylated, simultaneously, to produce smaller alkane radicals, as shown by Equation 3.
 
R 1 →R 2 .+R 3 .  (3)
         where, R 1 &gt;R 2 &gt;R 3 , meaning that the R 1  radical is larger than the R 2  radical, which is larger than the R 3  radical.       

     Under constant flow, reactions 1-3 continue to take place unless interrupted by major change in feedstock properties or operating conditions. If the temperature or space time increases beyond the stability limit, heavy free radical combination reactions escalate to produce larger and heavier molecules. These combination reactions terminate the reaction mechanism and cause asphaltene condensation, hence called condensation reactions, as shown by Equation 4.
 
R.+R.→M  (4)
 
     The combinations resulting from termination reactions may produce heavier compounds than the ones present originally in the feedstock. The cleavage of C—C bond in alkanes requires lower energy than the cleavage of C—H and H—H bonds. For example while the cleavage of the C—C bond in ethane (CH 3 —CH 3 ) requires dissociation energy of 360 KJ/mole, the cleavage of the C—H bond (C 2 H 5 —H) requires dissociation energy of 410 KJ/mole, as shown Table 1. The same observation is noticed for the bond energy of H-Aromatics, which is higher than the bond energy of C-Aromatics. The data in Table 1 are given at standard ambient temperature and ambient pressure (SATP) (see Raseev, S., Thermal and catalytic processes in petroleum refining, page 37, 2003: CRC Press, 1 st  ed.) 
     
       
         
           
               
             
               
                 TABLE 1 
               
             
            
               
                   
               
               
                 Chemical Bond Dissociation  
               
               
                 Energies for Different Hydrocarbons. 
               
            
           
           
               
               
               
            
               
                   
                   
                 Dissociation  
               
               
                   
                 Bond 
                 Energy (kJ/mole) 
               
               
                   
                   
               
               
                   
                 H—H 
                 435 
               
               
                   
                 CH 2 —H 
                 356 
               
               
                   
                 CH 3 —H 
                 431 
               
               
                   
                 C 2 H 5 —H 
                 410 
               
               
                   
                 n-C 3 H 7 —H 
                 398 
               
               
                   
                 i-C 3 H 7 —H 
                 394 
               
               
                   
                 n-C 4 H 9 —H 
                 394 
               
               
                   
                 i-C 4 H 9 —H 
                 390 
               
               
                   
                 CH 3 —CH 3   
                 360 
               
               
                   
                 C 2 H 5 —CH 3   
                 348 
               
               
                   
                 n-C 4 H 9 —C 2 H 5   
                 322 
               
               
                   
                 C 6 H 5 —C 6 H 5   
                 415 
               
               
                   
                 (C 6 H 5 ) 3 C—C(C 6 H 5 ) 3   
                  46 
               
               
                   
                   
               
               
                   
                 
                   
                     
                     
                         
                         
                     
                   
                 
                 364             423 
               
               
                   
                   
               
            
           
         
       
     
     It is also observed from Table 1 that the dissociation energy of the C—H bond in alkanes tends to decrease as the alkane molecular size increases. This indicates that lower molecular weight hydrocarbon species are kinetically more stable than heavier ones. 
     The dissociation energies at different temperatures, such as at supercritical temperatures, may be calculated from thermodynamics starting from the tabulated dissociation enthalpies at 298K. For example, to estimate the oxygen-hydrogen bond (O—H) dissociation enthalpy starting from 298K at a fixed pressure, the following expression estimates the bond dissociation enthalpy at a supercritical temperature of 450° C. (723K): ΔH (723K) =ΔH (298K) +ΔC p ΔT. After finding the heat capacities (ΔC P ) from thermodynamic data references such as Brunner, G.,  Hydrothermal and supercritical water processes . Vol. 5. 2014: Elsevier, at the required temperature, the bond dissociation enthalpy at 723K is estimated to be 442 KJ/mol. 
     Non-carbon rejection processes, at relatively higher operating cost such as hydrocracking, upgrade oil to produce stable products distant from, gummy olefin generation, asphaltene precipitation, and/or coke formation reactions. These products are believed to retain sufficient H/C ratios to preserve their stability. Hydrogen based routes include hydrocracking (a hydrogenolysis process), operated at around 200 bars and 350 to 400° C., allows refiner to produce hydrocarbons having a lower molecular weight with higher H/C ratios and a lower yield of coke. The mechanism of hydrogenolysis is basically similar to that of thermal cracking, but the cracking is promoted by high hydrogen partial and catalyst with concurrent hydrogenation. Hydrotreating is a mild hydrogen based process that operates at 30 to 130 bars and 300 to 400° C., allows reducing impurities from the oil like sulfur and metals without major cracking to the oil. Overall, olefins and coke formation is very low in hydrogenous processes since the large hydrocarbon radicals&#39; combination reactions and the formation of coke precursors are suppressed as the hydrogen pressure is increased. Oil upgrading and quality improvements by hydrogenous processes have been vastly practiced in industry to generate light products (hydrocracking) and/or to remove impurities (hydrotreating). Hydrogen-based upgrading processes typically utilize bi-metallic catalysts and hydrogen at different pressures, which result in high operating costs due to high hydrogen partial pressure requirement and catalyst and related regeneration Testing and Inspection (T&amp;I) costs. Furthermore, hydrocracking is a catalytic process that necessitates treating the feedstock ahead of the process to prevent catalyst poisoning. Therefore, hydrocracker feed is usually treated by catalytic hydrotreating at lower pressures to remove sulfur, nitrogen, metals, and other catalyst poisoning materials. This hydrotreating step adds to the cost of the catalytic hydrocracking process. In addition to hydrogen consumption of 1200 to 2400 standard cubic foot per oil barrel (SCFB), hydrocracking process conventionally requires high hydrogen partial pressure of around 200 bars to facilitate cracking the hydrocarbon molecules. 
     Water above its critical condition (about 374° C. and about 221 bar), termed supercritical water, is neither a liquid nor gas but a single fluid phase that converts from being polar to non-polar. Supercritical water can diffuse through semi-solid materials that are insusceptible to penetration otherwise at lower conditions, such as polynuclear aromatics and asphaltenes. Supercritical water completely dissolves hydrocarbon oils, and therefore, both phases become totally miscible. The distinctive characteristics of water in supercritical state improve liquid yield and properties of cracking, desulfurization, and demetallization reactions. Hydrocarbon oil cracking via supercritical water proceeds by a similar free radical mechanism as that of thermal cracking, and is highly selective towards breaking of heavy fractions to produce middle distillate oils without coke generation. Furthermore, during upgrading, supercritical water molecules isolate and separate the most heavy oil fraction molecules by the caging effect, which extends the upgrading reaction at the expense of condensation reactions. NMR analysis has revealed that the asphaltene content of supercritical water treated oil decreased to a large extent, while saturate, olefin, and aromatic content increased. When supercritical water is mixed with oil it dissolves all the oil constituents, including asphaltene. The dissolution takes place by swelling and breaching the asphaltene aggregates, thereby reducing the asphaltene aggregate particles size from about 1 to 800 microns to much smaller molecules having a particle size of from 0.1 to 300 nanometers (nm) that are distributed throughout the water/oil mixture. These relatively smaller asphaltene molecules are caged by water molecules surrounding them, which prevent them from association, aggregation, and deposition during the upgrading reactions. 
     As stated above, processes using supercritical water can generate olefins and polycondensed aromatics, which can lead to gumming. As stated previously, the high temperature of the supercritical water reactor induces thermal cracking of chemical bonds that may be filled with hydrogen to avoid intermolecular condensation and generation of olefins and polycondensed aromatics. Although the hydrogen inherently present in the water molecules can participate in the cracking reaction, the extent of hydrogen donation from water is quite limited in supercritical water conditions due to high hydrogen-oxygen bond energy. The hydrogen-oxygen dissociation energy at supercritical conditions can be calculated as provided above. Thus, the upgraded product from a supercritical water process has a greater aromaticity and olefinicity than the hydrocarbon feed, which has a negative effect on the stability of the products. 
     Supercritical water prevents the asphaltenes and heavy molecules from association and precipitation by breaking the large molecules into smaller ones and by caging the polycondensed aromatic clusters (asphaltenes) molecules and breaking bridging bonds (such as carbon-sulfur-carbon) between large polyaromatic compounds and keeping them apart. Moreover, the supercritical water fully dissolves and converts the kinetically active hydrocarbon species such as large molecules. The upgrading reaction mechanism involves hydrocarbon and hydrogen abstraction reactions, which generates numerous free radicals. Appreciable portion of these generated radicals are subjected to cracking reactions, reforming reactions, combination reactions, addition reactions, substitution reactions, and others. The overall result of these reactions is the generation of new improved quality product fractions that improves the overall supercritical water product quality including API and asphaltenes reduction. However, after departing from the water supercritical conditions, and after cooling and pressure let down, some of the molecules and light hydrocarbon radicals that require longer time to complete their conversion reactions tend to associate and/or form double bonds to fulfill their unpaired electrons in the absence of hydrogen. These species are generated by hydrogen and light hydrocarbon abstraction reactions, which increase their C/H ratios. This increase is translated by increase in aromaticity, which is the conversion of cyclic hydrocarbons (having no double bonds or a single double bond) and to some extent straight chain hydrocarbons into aromatics, and by cleavage of alkyl appendages that are cross linking different smaller aromatics. Once their alkyl appendages are cleaved, the different smaller aromatic radicals combines into larger aromatic clusters, which also increases the oil aromaticity. Similarly, hydrogen abstraction reactions in a supercritical water process generates radicals, which tend to form double bond species (olefins) in the absence of hydrogen. Availing enough hydrogen during upgrading saturates these molecules that then require increased time for conversion into valuable products, which minimizes their interaction and limits their double bond formation. This issue may be addressed by using a catalyst in the supercritical water process, but no catalysts have been used in a supercritical water process due to the harsh conditions of supercritical water that makes most catalysts unstable in the presence of supercritical water. The disintegration of heterogeneous catalysts is frequently observed in the presence of supercritical water. Additionally, homogeneous catalysts, such as organometallic compounds, can be transformed to an inactive form under supercritical water conditions. Conventionally, this problem has been addressed by adding catalysts to be used in a separate process downstream from the supercritical water process as a post treatment option. However, using a downstream process requires major capital investment for dedicated infrastructure, such as reactor(s), pumps and compressor, and cooler(s) and heat exchanger(s) in addition to catalyst catalysts with its costs of purchasing, replacement, and regenerating due to deactivation. 
     Consequently, the processes described in this disclosure do not use a catalyst. Supercritical water processes hydrothermally crack the hydrocarbon molecules under high operating pressures, as previously described, which are greater than conventional hydrocracking pressures. Under this high pressure range, hydrogenation can suppress gummy olefin generation, heavy hydrocarbon radical polymerization, and condensation reactions that lead to coke formation in thermal cracking. The supercritical water process high pressure can be exploited by adding a low amount of hydrogen to the supercritical water at hydrogen partial pressure of 1-30 bar, more specifically at 2-6 bar (based on oil type). The hydrogen partial pressure may be dependent on the hydrocarbons present. For example, highly viscous oils such as residual and bituminous oils require relatively greater amounts of hydrogen because they are highly deficient in hydrogen content (very high C/H ratio) because they contain an abundance of heavy hydrocarbon molecules. In order to generate lighter hydrocarbon fractions out of these heavy oils, their generated free radicals must be saturated with abundant hydrogen. In addition to forming double bond species, the generated free radicals, especially the heavy ones, in the absence of hydrogen, tend to associate and form bigger and heavier molecules and aggregates that are prone to precipitation. The hydrogen-to-oil volumetric flow may be between (10 to 5000 ft 3 ) H 2  to one barrel of oil, at standard ambient temperature and ambient pressure (SATP). 
     In addition to rupturing different types of bonds in the oil, supercritical water facilitates hydrogen availability in the vicinities of the cracked hydrocarbon and heteroatoms moieties, through hydrogen, water, and oil mixing in high pressure environments. Therefore, in addition to hydrothermally generated free hydrocarbon and heteroatoms radicals by supercritical water, the added hydrogen facilitates further cracking of hydrocarbon and heteroatoms molecule into free radicals and saturates the overall generated radicals including heteroatoms (for example converts S to H 2 S), simultaneously, under the supercritical water process conditions. The disclosed process combines carbon rejection and non-carbon rejection processes in a single process that combines the benefits of operating at lower cost than conventional hydrocracking processes to produce more stable products than thermal cracking. In this disclosure, the non-catalytically produced free large hydrocarbon radicals by the combined effect of supercritical water hydrothermal and hydrogenolysis are saturated and prevented from combination reactions that terminate the upgrading reaction mechanism and lead to gummy olefin, asphaltene, and coke formations. Furthermore, the presence of hydrogen in the supercritical water hydrogenation process will treat the oil by saturating the generated free heteroatoms radicals, such as converting sulfur to H 2 S. 
     Hydrogenolysis processes such as hydrocracking require high hydrogen partial pressure and catalysts to rupture the carbon-sulfur and carbon-carbon, and carbon-metal bonds. In the present disclosure, the supercritical water hydrogenation reactions rupture hydrocarbon and heteroatom bonds and provide the required high pressure for hydrogenation reactions at low hydrogen partial pressure. It is contemplated that low hydrogen partial pressure is desirable because it eliminates the need for dedicated gas compressors and thereby reduces maintenance and utilities costs. Additionally, in embodiments, low hydrogen partial pressure eliminates high hydrogen consumption that is needed to maintain high hydrogen partial pressure. Under the supercritical water hydrogenation process conditions, the relatively lower molecular weight hydrocarbon species of C 1  to C 7  hydrocarbons (paraffins, cycloparaffins, and aromatics) are kinetically more stable than the heavier ones. Therefore, supercritical water hydrogenation process is highly selective towards breaking of heavy fractions to produce middle distillate oils without gummy olefin, asphaltene, and coke generation. Furthermore, during upgrading, supercritical water molecules isolate and separate the most heavy oil fraction molecules by the caging effect, which extends the upgrading reaction at the expense of condensation reactions, thereby decreasing condensation reactions. 
     Hydrogen addition into the supercritical water process provides additional yields of middle distillate oils but at improved stability by saturating heavy hydrocarbon radicals and olefins that has potential to generate gums. In addition, the supercritical water process breaks large asphaltene aggregates of size 1 to 800 microns to much smaller scattered radical aggregates of size 0.1 to 300 nm that can readily be approached and saturated by hydrogen due to its small size (1.06-1.20 angstrom). This in turn reduces the asphaltene content in the oil by converting them into lighter fractions. Therefore, supercritical water facilitates the hydrogenation of heavy hydrocarbon radicals including olefin and asphaltene radicals and prevents their combination reactions that terminate the upgrading reaction mechanism. In other words, the hydrogen addition to the supercritical water process passivates the combination reactions of large hydrocarbon radicals and olefins that are hydrothermally generated by supercritical water, thereby preventing gum, asphaltene, and coke generation, which allows for increasing process severity for additional oil upgrading. 
     Large hydrocarbon molecules cracking and radicals&#39; saturation reactions in supercritical water hydrogenation are favored by high operating pressure; therefore, increasing process severity in terms of higher pressures will facilitate large hydrocarbon and heteroatom bonds rupturing and hydrogenation of the generated radicals as well as increasing oil conversion. Furthermore, supercritical water processes have been reported to desulfurize and demetalize hydrocarbon oil. Adding hydrogen to the supercritical water process will further enhance the sulfur and metals removal by hydrogenating the heteroatoms (hydrotreating). Therefore, adding hydrogen to the supercritical water process will expand the application of the supercritical water technology for treating sulfur rich streams (such as disulfide oils) besides upgrading by facilitating C—S and S—S bond rupturing and hydrogenating the sulfur radicals in supercritical water to generate hydrogen sulfide and light hydrocarbons, as shown by equation 5.
 
CH 3 —S—S—CH 3 +2H 2 →CH 3 —CH 3 +2H 2 S  (5)
 
     Therefore, there exists recognizable synergy between supercritical water and added hydrogen to upgrade and improve hydrocarbon oils. It is contemplated that the supercritical water hydrogenation reactor  150  may dissolve the hydrocarbons and hydrogen in supercritical water and break the M-S bonds (having a bond energy of approximately 290 kJ/mol), M-M bonds, H—H bonds, and MS-SM bonds (having a bond energy of approximately 260 kJ/mol), and hydrogenate the generated hydrocarbon and heteroatom radicals. Within the supercritical water hydrogenation reactor  150 , it is contemplated that large hydrocarbon molecules (including asphaltene aggregates) are dissolved, broken, dispersed, and hydrogenated in the oil medium, in addition to hydrocarbon upgrading by improving properties such as API gravity and reducing properties such as density, viscosity, and heteroatoms (including metals). 
     Upon exiting the supercritical water hydrogenation reactor  150 , the upgraded product  152  may have a T 5  true boiling point (TBP) of less than 500° C., of less than 400° C., of less than 350° C., of less than 325° C., of less than 310° C., or of less than 300° C. In embodiments, the upgraded product  152  may have a T 5  TBP of from 25° C. to 350° C., from 25° C. to 325° C., from 25° C. to 300° C., from 25° C. to 275° C., from 25° C. to 250° C., from 25° C. to 225° C., from 25° C. to 200° C., from 25° C. to 175° C., from 25° C. to 150° C., from 25° C. to 125° C., from 25° C. to 100° C., from 25° C. to 75° C., from 25° C. to 50° C., from 50° C. to 350° C., from 50° C. to 325° C., from 50° C. to 300° C., from 50° C. to 275° C., from 50° C. to 250° C., from 50° C. to 225° C., from 50° C. to 200° C., from 50° C. to 175° C., from 50° C. to 150° C., from 50° C. to 125° C., from 50° C. to 100° C., from 50° C. to 75° C., from 75° C. to 350° C., from 75° C. to 325° C., from 75° C. to 300° C., from 75° C. to 275° C., from 75° C. to 250° C., from 75° C. to 225° C., from 75° C. to 200° C., from 75° C. to 175° C., from 75° C. to 150° C., from 75° C. to 125° C., from 75° C. to 100° C., from 100° C. to 350° C., from 100° C. to 325° C., from 100° C. to 300° C., from 100° C. to 275° C., from 100° C. to 250° C., from 100° C. to 225° C., from 100° C. to 200° C., from 100° C. to 175° C., from 100° C. to 150° C., from 100° C. to 125° C., from 125° C. to 350° C., from 125° C. to 325° C., from 125° C. to 300° C., from 125° C. to 275° C., from 125° C. to 250° C., from 125° C. to 225° C., from 125° C. to 200° C., from 125° C. to 175° C., from 125° C. to 150° C., from 150° C. to 350° C., from 150° C. to 325° C., from 150° C. to 300° C., from 150° C. to 275° C., from 150° C. to 250° C., from 150° C. to 225° C., from 150° C. to 200° C., from 150° C. to 175° C., from 175° C. to 350° C., from 175° C. to 325° C., from 175° C. to 300° C., from 175° C. to 275° C., from 175° C. to 250° C., from 175° C. to 225° C., from 175° C. to 200° C., from 200° C. to 350° C., from 200° C. to 325° C., from 200° C. to 300° C., from 200° C. to 275° C., from 200° C. to 250° C., from 200° C. to 225° C., from 225° C. to 350° C., from 225° C. to 325° C., from 225° C. to 300° C., from 225° C. to 275° C., from 225° C. to 250° C., from 250° C. to 350° C., from 250° C. to 325° C., from 250° C. to 300° C., from 250° C. to 275° C., from 275° C. to 350° C., from 275° C. to 325° C., from 275° C. to 300° C., from 300° C. to 350° C., from 300° C. to 325° C., or from 325° C. to 350° C. The upgraded product  152  may have a T 90  TBP of less than or equal to 650° C., less than or equal to 610° C., or less than or equal to 600° C. In embodiments, upgraded product  152  may have a T 90  TBP from 200° C. to 650° C., from 200° C. to 600° C., from 200° C. to 575° C., from 200° C. to 550° C., from 200° C. to 540° C., from 200° C. to 530° C., from 200° C. to 525° C., from 200° C. to 500° C., from 200° C. to 450° C., from 200° C. to 400° C., from 200° C. to 300° C., from 300° C. to 650° C., from 300° C. to 600° C., from 300° C. to 575° C., from 300° C. to 550° C., from 300° C. to 540° C., from 300° C. to 530° C., from 300° C. to 525° C., from 300° C. to 500° C., from 300° C. to 450° C., from 300° C. to 400° C., from 400° C. to 650° C., from 400° C. to 600° C., from 400° C. to 575° C., from 400° C. to 550° C., from 400° C. to 540° C., from 400° C. to 530° C., from 400° C. to 525° C., from 400° C. to 500° C., from 450° C. to 650° C., from 450° C. to 600° C., from 450° C. to 575° C., from 450° C. to 550° C., from 450° C. to 540° C., from 450° C. to 530° C., from 450° C. to 525° C., from 450° C. to 500° C., from 500° C. to 650° C., from 500° C. to 600° C., from 500° C. to 575° C., from 500° C. to 550° C., from 500° C. to 540° C., from 500° C. to 530° C., from 500° C. to 525° C., from 525° C. to 650° C., from 525° C. to 600° C., from 525° C. to 575° C., from 525° C. to 550° C., from 525° C. to 540° C., from 525° C. to 530° C., from 530° C. to 650° C., from 530° C. to 600° C., from 530° C. to 575° C., from 530° C. to 550° C., from 530° C. to 540° C., from 540° C. to 650° C., from 540° C. to 600° C., from 540° C. to 575° C., from 540° C. to 550° C., from 550° C. to 650° C., from 550° C. to 600° C., from 550° C. to 575° C., from 575° C. to 650° C., from 575° C. to 600° C., or from 600° C. to 650° C., where the T 90  TBP is greater than the T 5  TBP previously described. The upgraded product  152  may have an API gravity from 12° to 45°, from 12° to 35°, from 12° to 30°, from 12° to 27°, from 12° to 25°, from 12° to 23°, from 12° to 21°, from 12° to 20°, from 15° to 45°, from 15° to 35°, from 15° to 30°, from 15° to 27°, from 15° to 25°, from 15° to 23°, from 15° to 21°, from 15° to 20°, from 18° to 45°, from 18° to 35°, from 18° to 30°, from 18° to 27°, from 18° to 25°, from 18° to 23°, from 18° to 21°, from 18° to 20, from 20° to 45°, from 20° to 35°, from 20° to 30°, from 20° to 27°, from 20° to 25°, from 20° to 23°, from 20° to 21°, from 21° to 45°, from 21° to 35°, from 21° to 30°, from 21° to 27°, from 21° to 25°, from 21° to 23°, from 23° to 45°, from 23° to 35°, from 23° to 30°, from 23° to 27°, from 23° to 25°, approximately 20°, or approximately 19.8°. The upgraded product  152  may include less than 3.4 wt. % total sulfur content by weight of the upgraded product  152 . In embodiments, the upgraded product  152  may include from 0.1 wt. % to 5 wt. %, from 0.1 wt. % to 4 wt. %, from 0.1 wt. % to 3.3 wt. %, from 0.1 wt. % to 3.0 wt. %, from 0.1 wt. % to 2.8 wt. %, from 0.1 wt. % to 2.6 wt. %, from 0.1 wt. % to 2.3 wt. %, from 0.1 wt. % to 2.0 wt. %, from 0.1 wt. % to 1.8 wt. %, from 0.1 wt. % to 1.6 wt. %, from 0.1 wt. % to 1.3 wt. %, from 0.1 wt. % to 1.0 wt. %, from 0.1 wt. % to 0.5 wt. %, from 0.5 wt. % to 5 wt. %, from 0.5 wt. % to 4 wt. %, from 0.5 wt. % to 3.3 wt. %, from 0.5 wt. % to 3.0 wt. %, from 0.5 wt. % to 2.8 wt. %, from 0.5 wt. % to 2.6 wt. %, from 0.5 wt. % to 2.3 wt. %, from 0.5 wt. % to 2.0 wt. %, from 0.5 wt. % to 1.8 wt. %, from 0.5 wt. % to 1.6 wt. %, from 0.5 wt. % to 1.3 wt. %, from 0.5 wt. % to 1.0 wt. %, from 1.0 wt. % to 5 wt. %, from 1.0 wt. % to 4 wt. %, from 1.0 wt. % to 3.3 wt. %, from 1.0 wt. % to 3.0 wt. %, from 1.0 wt. % to 2.8 wt. %, from 1.0 wt. % to 2.6 wt. %, from 1.0 wt. % to 2.3 wt. %, from 1.0 wt. % to 2.0 wt. %, from 1.0 wt. % to 1.8 wt. %, from 1.0 wt. % to 1.6 wt. %, from 1.0 wt. % to 1.3 wt. %, from 1.3 wt. % to 5 wt. %, from 1.3 wt. % to 4 wt. %, from 1.3 wt. % to 3.3 wt. %, from 1.3 wt. % to 3.0 wt. %, from 1.3 wt. % to 2.8 wt. %, from 1.3 wt. % to 2.6 wt. %, from 1.3 wt. % to 2.3 wt. %, from 1.3 wt. % to 2.0 wt. %, from 1.3 wt. % to 1.8 wt. %, from 1.3 wt. % to 1.6 wt. %, from 1.6 wt. % to 5 wt. %, from 1.6 wt. % to 4 wt. %, from 1.6 wt. % to 3.3 wt. %, from 1.6 wt. % to 3.0 wt. %, from 1.6 wt. % to 2.8 wt. %, from 1.6 wt. % to 2.6 wt. %, from 1.6 wt. % to 2.3 wt. %, from 1.6 wt. % to 2.0 wt. %, from 1.6 wt. % to 1.8 wt. %, from 1.8 wt. % to 5 wt. %, from 1.8 wt. % to 4 wt. %, from 1.8 wt. % to 3.3 wt. %, from 1.8 wt. % to 3.0 wt. %, from 1.8 wt. % to 2.8 wt. %, from 1.8 wt. % to 2.6 wt. %, from 1.8 wt. % to 2.3 wt. %, from 1.8 wt. % to 2.0 wt. %, from 2.0 wt. % to 5 wt. %, from 2.0 wt. % to 4 wt. %, from 2.0 wt. % to 3.3 wt. %, from 2.0 wt. % to 3.0 wt. %, from 2.0 wt. % to 2.8 wt. %, from 2.0 wt. % to 2.6 wt. %, from 2.0 wt. % to 2.3 wt. %, from 2.3 wt. % to 5 wt. %, from 2.3 wt. % to 4 wt. %, from 2.3 wt. % to 3.3 wt. %, from 2.3 wt. % to 3.0 wt. %, from 2.3 wt. % to 2.8 wt. %, from 2.3 wt. % to 2.6 wt. %, from 2.6 wt. % to 5 wt. %, from 2.6 wt. % to 4 wt. %, from 2.6 wt. % to 3.3 wt. %, from 2.6 wt. % to 3.0 wt. %, from 2.6 wt. % to 2.8 wt. %, from 2.8 wt. % to 5 wt. %, from 2.8 wt. % to 4 wt. %, from 2.8 wt. % to 3.3 wt. %, from 2.8 wt. % to 3.0 wt. %, from 3.0 wt. % to 5 wt. %, from 3.0 wt. % to 4 wt. %, from 3.0 wt. % to 3.3 wt. %, or approximately 2.7 wt. % wt. % total sulfur content by weight of the upgraded product  152 . The upgraded product  152  may include less than 1.2 wt. % wt. % total nitrogen content by weight of the upgraded product  152 . In embodiments, the upgraded product  152  may include from 0.01 wt. % to 2 wt. %, from 0.01 wt. % to 1.1 wt. %, from 0.01 wt. % to 1.0 wt. %, from 0.01 wt. % to 0.8 wt. %, from 0.01 wt. % to 0.6 wt. %, from 0.01 wt. % to 0.4 wt. %, from 0.01 wt. % to 0.2 wt. %, from 0.01 wt. % to 0.1 wt. %, from 0.1 wt. % to 2 wt. %, from 0.1 wt. % to 1.1 wt. %, from 0.1 wt. % to 1.0 wt. %, from 0.1 wt. % to 0.8 wt. %, from 0.1 wt. % to 0.6 wt. %, from 0.1 wt. % to 0.4 wt. %, from 0.1 wt. % to 0.2 wt. %, from 0.2 wt. % to 2 wt. %, from 0.2 wt. % to 1.1 wt. %, from 0.2 wt. % to 1.0 wt. %, from 0.2 wt. % to 0.8 wt. %, from 0.2 wt. % to 0.6 wt. %, from 0.2 wt. % to 0.4 wt. %, from 0.4 wt. % to 2 wt. %, from 0.4 wt. % to 1.1 wt. %, from 0.4 wt. % to 1.0 wt. %, from 0.4 wt. % to 0.8 wt. %, from 0.4 wt. % to 0.6 wt. %, from 0.6 wt. % to 2 wt. %, from 0.6 wt. % to 1.1 wt. %, from 0.6 wt. % to 1.0 wt. %, from 0.6 wt. % to 0.8 wt. %, from 0.8 wt. % to 2 wt. %, from 0.8 wt. % to 1.1 wt. %, from 0.8 wt. % to 1.0 wt. %, from 1.0 wt. % to 2 wt. %, from 1.0 wt. % to 1.1 wt. %, or approximately 0.9 wt. % wt. % total nitrogen content by weight of the upgraded product  152 . The upgraded product  152  may include less than 4.8 wt. % asphaltene (heptane-insoluble) by weight of the upgraded product  152 . In embodiments, the upgraded product  152  may include from 0.01 wt. % to 6 wt. %, from 0.01 wt. % to 5 wt. %, from 0.01 wt. % to 4.7 wt. %, from 0.01 wt. % to 4.0 wt. %, from 0.01 wt. % to 3.0 wt. %, from 0.01 wt. % to 2.5 wt. %, from 0.01 wt. % to 2.0 wt. %, from 0.01 wt. % to 1.8 wt. %, from 0.01 wt. % to 1.6 wt. %, from 0.01 wt. % to 1.0 wt. %, from 0.01 wt. % to 0.8 wt. %, from 0.01 wt. % to 0.6 wt. %, from 0.01 wt. % to 0.4 wt. %, from 0.01 wt. % to 0.2 wt. %, from 0.01 wt. % to 0.1 wt. %, from 0.1 wt. % to 6 wt. %, from 0.1 wt. % to 5 wt. %, from 0.1 wt. % to 4.7 wt. %, from 0.1 wt. % to 4.0 wt. %, from 0.1 wt. % to 3.0 wt. %, from 0.1 wt. % to 2.5 wt. %, from 0.1 wt. % to 2.0 wt. %, from 0.1 wt. % to 1.8 wt. %, from 0.1 wt. % to 1.6 wt. %, from 0.1 wt. % to 1.0 wt. %, from 0.1 wt. % to 0.8 wt. %, from 0.1 wt. % to 0.6 wt. %, from 0.1 wt. % to 0.4 wt. %, from 0.1 wt. % to 0.2 wt. %, from 0.2 wt. % to 6 wt. %, from 0.2 wt. % to 5 wt. %, from 0.2 wt. % to 4.7 wt. %, from 0.2 wt. % to 4.0 wt. %, from 0.2 wt. % to 3.0 wt. %, from 0.2 wt. % to 2.5 wt. %, from 0.2 wt. % to 2.0 wt. %, from 0.2 wt. % to 1.8 wt. %, from 0.2 wt. % to 1.6 wt. %, from 0.2 wt. % to 1.0 wt. %, from 0.2 wt. % to 0.8 wt. %, from 0.2 wt. % to 0.6 wt. %, from 0.2 wt. % to 0.4 wt. %, from 0.4 wt. % to 6 wt. %, from 0.4 wt. % to 5 wt. %, from 0.4 wt. % to 4.7 wt. %, from 0.4 wt. % to 4.0 wt. %, from 0.4 wt. % to 3.0 wt. %, from 0.4 wt. % to 2.5 wt. %, from 0.4 wt. % to 2.0 wt. %, from 0.4 wt. % to 1.8 wt. %, from 0.4 wt. % to 1.6 wt. %, from 0.4 wt. % to 1.0 wt. %, from 0.4 wt. % to 0.8 wt. %, from 0.4 wt. % to 0.6 wt. %, from 0.6 wt. % to 6 wt. %, from 0.6 wt. % to 5 wt. %, from 0.6 wt. % to 4.7 wt. %, from 0.6 wt. % to 4.0 wt. %, from 0.6 wt. % to 3.0 wt. %, from 0.6 wt. % to 2.5 wt. %, from 0.6 wt. % to 2.0 wt. %, from 0.6 wt. % to 1.8 wt. %, from 0.6 wt. % to 1.6 wt. %, from 0.6 wt. % to 1.0 wt. %, from 0.6 wt. % to 0.8 wt. %, from 0.8 wt. % to 6 wt. %, from 0.8 wt. % to 5 wt. %, from 0.8 wt. % to 4.7 wt. %, from 0.8 wt. % to 4.0 wt. %, from 0.8 wt. % to 3.0 wt. %, from 0.8 wt. % to 2.5 wt. %, from 0.8 wt. % to 2.0 wt. %, from 0.8 wt. % to 1.8 wt. %, from 0.8 wt. % to 1.6 wt. %, from 0.8 wt. % to 1.0 wt. %, from 1.0 wt. % to 6 wt. %, from 1.0 wt. % to 5 wt. %, from 1.0 wt. % to 4.7 wt. %, from 1.0 wt. % to 4.0 wt. %, from 1.0 wt. % to 3.0 wt. %, from 1.0 wt. % to 2.5 wt. %, from 1.0 wt. % to 2.0 wt. %, from 1.0 wt. % to 1.8 wt. %, from 1.0 wt. % to 1.6 wt. %, from 1.6 wt. % to 6 wt. %, from 1.6 wt. % to 5 wt. %, from 1.6 wt. % to 4.7 wt. %, from 1.6 wt. % to 4.0 wt. %, from 1.6 wt. % to 3.0 wt. %, from 1.6 wt. % to 2.5 wt. %, from 1.6 wt. % to 2.0 wt. %, from 1.6 wt. % to 1.8 wt. %, from 1.8 wt. % to 6 wt. %, from 1.8 wt. % to 5 wt. %, from 1.8 wt. % to 4.7 wt. %, from 1.8 wt. % to 4.0 wt. %, from 1.8 wt. % to 3.0 wt. %, from 1.8 wt. % to 2.5 wt. %, from 1.8 wt. % to 2.0 wt. %, from 2.0 wt. % to 6 wt. %, from 2.0 wt. % to 5 wt. %, from 2.0 wt. % to 4.7 wt. %, from 2.0 wt. % to 4.0 wt. %, from 2.0 wt. % to 3.0 wt. %, from 2.0 wt. % to 2.5 wt. %, from 2.5 wt. % to 6 wt. %, from 2.5 wt. % to 5 wt. %, from 2.5 wt. % to 4.7 wt. %, from 2.5 wt. % to 4.0 wt. %, from 2.5 wt. % to 3.0 wt. %, from 3.0 wt. % to 6 wt. %, from 3.0 wt. % to 5 wt. %, from 3.0 wt. % to 4.7 wt. %, from 3.0 wt. % to 4.0 wt. %, from 4.0 wt. % to 6 wt. %, from 4.0 wt. % to 5 wt. %, or approximately 1.7 wt. % asphaltene (heptane-insoluble) by weight of the upgraded product  152 . The upgraded product  152  may include less than 83 parts per million (ppm) metals. In embodiments, the metals may be vanadium, nickel, or both. In embodiments, the upgraded product  152  may include from 1 ppm to 100 ppm, from 1 ppm to 82 ppm, from 1 ppm to 50 ppm, from 1 ppm to 25 ppm, from 1 ppm to 15 ppm, from 1 ppm to 10 ppm, from 1 ppm to 8 ppm, from 1 ppm to 5 ppm, from 1 ppm to 3 ppm, from 3 ppm to 100 ppm, from 3 ppm to 82 ppm, from 3 ppm to 50 ppm, from 3 ppm to 25 ppm, from 3 ppm to 15 ppm, from 3 ppm to 10 ppm, from 3 ppm to 8 ppm, from 3 ppm to 5 ppm, from 5 ppm to 100 ppm, from 5 ppm to 82 ppm, from 5 ppm to 50 ppm, from 5 ppm to 25 ppm, from 5 ppm to 15 ppm, from 5 ppm to 10 ppm, from 5 ppm to 8 ppm, from 8 ppm to 100 ppm, from 8 ppm to 82 ppm, from 8 ppm to 50 ppm, from 8 ppm to 25 ppm, from 8 ppm to 15 ppm, from 8 ppm to 10 ppm, from 10 ppm to 100 ppm, from 10 ppm to 82 ppm, from 10 ppm to 50 ppm, from 10 ppm to 25 ppm, from 10 ppm to 15 ppm, from 15 ppm to 100 ppm, from 15 ppm to 82 ppm, from 15 ppm to 50 ppm, from 15 ppm to 25 ppm, or approximately 9 ppm metals. The upgraded product  152  may have a viscosity at 50° C. of less than 640 centiStokes (cSt). In embodiments, the upgraded product  152  may have a viscosity at 50° C. from 10 to 639 cSt, from 10 cSt to 600 cSt, from 10 cSt to 400 cSt, from 10 cSt to 200 cSt, from 10 cSt to 150 cSt, from 10 cSt to 100 cSt, from 10 cSt to 90 cSt, from 10 cSt to 88 cSt, from 10 cSt to 70 cSt, from 10 cSt to 50 cSt, from 10 cSt to 35 cSt, from 10 cSt to 28 cSt, from 10 cSt to 26 cSt, from 10 cSt to 20 cSt, from 20 cSt to 639 cSt, from 20 cSt to 600 cSt, from 20 cSt to 400 cSt, from 20 cSt to 200 cSt, from 20 cSt to 150 cSt, from 20 cSt to 100 cSt, from 20 cSt to 90 cSt, from 20 cSt to 88 cSt, from 20 cSt to 70 cSt, from 20 cSt to 50 cSt, from 20 cSt to 35 cSt, from 20 cSt to 28 cSt, from 20 cSt to 26 cSt, from 26 cSt to 639 cSt, from 26 cSt to 600 cSt, from 26 cSt to 400 cSt, from 26 cSt to 200 cSt, from 26 cSt to 150 cSt, from 26 cSt to 100 cSt, from 26 cSt to 90 cSt, from 26 cSt to 88 cSt, from 26 cSt to 70 cSt, from 26 cSt to 50 cSt, from 26 cSt to 35 cSt, from 26 cSt to 28 cSt, from 28 cSt to 639 cSt, from 28 cSt to 600 cSt, from 28 cSt to 400 cSt, from 28 cSt to 200 cSt, from 28 cSt to 150 cSt, from 28 cSt to 100 cSt, from 28 cSt to 90 cSt, from 28 cSt to 88 cSt, from 28 cSt to 70 cSt, from 28 cSt to 50 cSt, from 28 cSt to 35 cSt, from 35 cSt to 639 cSt, from 35 cSt to 600 cSt, from 35 cSt to 400 cSt, from 35 cSt to 200 cSt, from 35 cSt to 150 cSt, from 35 cSt to 100 cSt, from 35 cSt to 90 cSt, from 35 cSt to 88 cSt, from 35 cSt to 70 cSt, from 35 cSt to 50 cSt, from 50 cSt to 639 cSt, from 50 cSt to 600 cSt, from 50 cSt to 400 cSt, from 50 cSt to 200 cSt, from 50 cSt to 150 cSt, from 50 cSt to 100 cSt, from 50 cSt to 90 cSt, from 50 cSt to 88 cSt, from 50 cSt to 70 cSt, from 70 cSt to 639 cSt, from 70 cSt to 600 cSt, from 70 cSt to 400 cSt, from 70 cSt to 200 cSt, from 70 cSt to 150 cSt, from 70 cSt to 100 cSt, from 70 cSt to 90 cSt, from 70 cSt to 88 cSt, from 88 cSt to 639 cSt, from 88 cSt to 600 cSt, from 88 cSt to 400 cSt, from 88 cSt to 200 cSt, from 88 cSt to 150 cSt, from 88 cSt to 100 cSt, from 88 cSt to 90 cSt, or approximately 89 cSt. 
     The upgraded product  152  may then be cooled by cooler  154  to a temperature from 150° C. to 250° C., from 150° C. to 225° C., from 150° C. to 200° C., from 150° C. to 175° C., from 175° C. to 250° C., from 175° C. to 225° C., from 175° C. to 200° C., from 200° C. to 250° C., from 200° C. to 225° C., or from 225° C. to 250° C. to form a cooled, upgraded product  156 . Various cooling devices are contemplated for the cooler  154 , such as a heat exchanger. 
     Referring again to  FIG. 1 , upon exiting the cooler  154 , the pressure of the cooled, upgraded product  156  may be reduced MPa to create a depressurized, upgraded product  159 , which may have a pressure from 0.01 MPa to 1.0 MPa, from 0.01 MPa to 0.8 MPa, from 0.01 MPa to 0.5 MPa, from 0.01 MPa to 0.3 MPa, from 0.01 MPa to 0.1 MPa, from 0.01 MPa to 0.08 MPa, from 0.01 MPa to 0.05 MPa, from 0.01 MPa to 0.03 MPa, from 0.03 MPa to 1.0 MPa, from 0.03 MPa to 0.8 MPa, from 0.03 MPa to 0.5 MPa, from 0.03 MPa to 0.3 MPa, from 0.03 MPa to 0.1 MPa, from 0.03 MPa to 0.08 MPa, from 0.03 MPa to 0.05 MPa, from 0.05 MPa to 1.0 MPa, from 0.05 MPa to 0.8 MPa, from 0.05 MPa to 0.5 MPa, from 0.05 MPa to 0.3 MPa, from 0.05 MPa to 0.1 MPa, from 0.05 MPa to 0.08 MPa, from 0.08 MPa to 1.0 MPa, from 0.08 MPa to 0.8 MPa, from 0.08 MPa to 0.5 MPa, from 0.08 MPa to 0.3 MPa, from 0.08 MPa to 0.1 MPa, from 0.1 MPa to 1.0 MPa, from 0.1 MPa to 0.8 MPa, from 0.1 MPa to 0.5 MPa, from 0.1 MPa to 0.3 MPa, from 0.3 MPa to 1.0 MPa, from 0.3 MPa to 0.8 MPa, from 0.3 MPa to 0.5 MPa, from 0.5 MPa to 1.0 MPa, from 0.5 MPa to 0.8 MPa, or from 0.8 MPa to 1.0 MPa. The depressurizing can be achieved by many devices, for example, a valve  158  as shown in  FIGS. 1 and 2 . 
     The depressurized, upgraded product  159  may then be passed to a gas/oil/water separator  160 . The gas/water separator  160  may separate the depressurized, upgraded product  159  into a first gas fraction  164 , a liquid oil fraction  162 , and a first water fraction  166 . The gas/water separator  160  may be any separator known in the industry. While the gas/oil/water separator  160  may separate the depressurized, upgraded product  159  into at least a first gas fraction  164  comprising CO, CO 2 , NH 3 , H 2 , H 2 S, C 1 , C 2 , C 3 , C 4 , C 5 , C 6 , or combinations thereof; a liquid oil fraction  162 ; and a first water fraction  166 , it should be appreciated that additional fractions may also be produced. In embodiments, the first gas fraction  164  may include from 0.5 wt. % to 3 wt. %, from 0.5 wt. % to 2 wt. %, from 0.5 wt. % to 1.5 wt. %, 0.5 wt. % to 1.2 wt. %, from 0.8 wt. % to 3 wt. %, from 0.8 wt. % to 2 wt. %, from 0.8 wt. % to 1.5 wt. %, from 0.8 wt. % to 1.2 wt. %, or approximately 1 wt. % H 2  by weight of the first gas fraction  164 . In embodiments, the first gas fraction  164  may include from 2 wt. % to 50 wt. %, from 2 wt. % to 25 wt. %, from 5 wt. % to 50 wt. %, from 5 wt. % to 25 wt. %, from 5 wt. % to 15 wt. %, from 5 wt. % to 13 wt. %, from 8 wt. % to 50 wt. %, from 8 wt. % to 25 wt. %, from 8 wt. % to 15 wt. %, from 8 wt. % to 13 wt. %, from 10 wt. % to 50 wt. %, from 10 wt. % to 25 wt. %, from 10 wt. % to 15 wt. %, from 10 wt. % to 13 wt. %, from 11 wt. % to 50 wt. %, from 11 wt. % to 25 wt. %, from 11 wt. % to 15 wt. %, from 11 wt. % to 13 wt. %, or approximately 12 wt. % C 1  by weight of the first gas fraction  164 . In embodiments, the first gas fraction  164  may include from 2 wt. % to 50 wt. %, from 2 wt. % to 25 wt. %, from 5 wt. % to 50 wt. %, from 5 wt. % to 25 wt. %, from 5 wt. % to 15 wt. %, from 5 wt. % to 12 wt. %, from 8 wt. % to 15 wt. %, from 8 wt. % to 12 wt. %, from 10 wt. % to 15 wt. %, from 10 wt. % to 12 wt. %, or approximately 11 wt. % C 2  by weight of the first gas fraction  164 . In embodiments, the first gas fraction  164  may include from 2 wt. % to 50 wt. %, from 2 wt. % to 25 wt. %, from 2 wt. % to 15 wt. %, from 5 wt. % to 50 wt. %, from 5 wt. % to 25 wt. %, from 5 wt. % to 15 wt. %, from 5 wt. % to 13 wt. %, from 5 wt. % to 11 wt. %, from 7 wt. % to 15 wt. %, from 7 wt. % to 13 wt. %, from 7 wt. % to 11 wt. %, from 9 wt. % to 15 wt. %, from 9 wt. % to 13 wt. %, from 9 wt. % to 11 wt. %, or approximately 10 wt. % C 3  by weight of the first gas fraction  164 . In embodiments, the first gas fraction  164  may include from 1 wt. % to 50 wt. %, from 1 wt. % to 25 wt. %, from 3 wt. % to 15 wt. %, from 3 wt. % to 12 wt. %, from 3 wt. % to 10 wt. %, from 5 wt. % to 15 wt. %, from 5 wt. % to 12 wt. %, from 5 wt. % to 10 wt. %, from 8 wt. % to 15 wt. %, from 8 wt. % to 12 wt. %, from 8 wt. % to 10 wt. %, or approximately 9 wt. % C 4  by weight of the first gas fraction  164 . In embodiments, the first gas fraction  164  may include from 0 wt. % to 50 wt. %, from 0 wt. % to 25 wt. %, from 0 wt. % to 10 wt. %, from 0 wt. % to 5 wt. %, from 0 wt. % to 1 wt. %, from 1 wt. % to 15 wt. %, from 1 wt. % to 10 wt. %, from 1 wt. % to 8 wt. %, from 3 wt. % to 10 wt. %, from 3 wt. % to 8 wt. %, from 5 wt. % to 15 wt. %, from 5 wt. % to 12 wt. %, from 5 wt. % to 10 wt. %, from 5 wt. % to 8 wt. %, from 6 wt. % to 10 wt. %, from 6 wt. % to 8 wt. %, or approximately 7 wt. % C 5  by weight of the first gas fraction  164 . The first gas fraction  164  may include from 0 wt. % to 25 wt. %, from 0 wt. % to 10 wt. %, from 0 wt. % to 1 wt. %, from 1 wt. % to 25 wt. %, from 1 wt. % to 10 wt. %, from 1 wt. % to 7 wt. %, from 1 wt. % to 5 wt. %, from 2 wt. % to 10 wt. %, from 2 wt. % to 7 wt. %, from 2 wt. % to 5 wt. %, from 3 wt. % to 10 wt. %, from 3 wt. % to 7 wt. %, from 3 wt. % to 5 wt. %, or approximately 4 wt. % C 6  by weight of the first gas fraction  164 . In embodiments, the first gas fraction  164  may include from 0 wt. % to 15 wt. %, from 1 wt. % to 10 wt. %, from 1 wt. % to 5 wt. %, from 1 wt. % to 3 wt. %, or approximately 2 wt. % CO by weight of the first gas fraction  164 . In embodiments, the first gas fraction  164  may include from 0 wt. % to 25 wt. %, from 0 wt. % to 10 wt. %, from 0 wt. % to 1 wt. %, from 1 wt. % to 25 wt. %, from 1 wt. % to 10 wt. %, from 1 wt. % to 7 wt. %, from 1 wt. % to 5 wt. %, from 2 wt. % to 10 wt. %, from 2 wt. % to 7 wt. %, from 2 wt. % to 5 wt. %, from 3 wt. % to 10 wt. %, from 3 wt. % to 7 wt. %, from 3 wt. % to 5 wt. %, or approximately 4 wt. % CO 2  by weight of the first gas fraction  164 . In embodiments, the first gas fraction  164  may include from 1 wt. % to 50 wt. %, from 1 wt. % to 35 wt. %, from 1 wt. % to 30 wt. %, from 1 wt. % to 26 wt. %, from 10 wt. % to 50 wt. %, from 10 wt. % to 35 wt. %, from 10 wt. % to 30 wt. %, from 10 wt. % to 26 wt. %, from 15 wt. % to 50 wt. %, from 15 wt. % to 35 wt. %, from 15 wt. % to 30 wt. %, from 15 wt. % to 26 wt. %, from 20 wt. % to 50 wt. %, from 20 wt. % to 35 wt. %, from 20 wt. % to 30 wt. %, from 20 wt. % to 26 wt. %, from 23 wt. % to 50 wt. %, from 23 wt. % to 35 wt. %, from 23 wt. % to 30 wt. %, from 23 wt. % to 26 wt. %, from 25 wt. % to 50 wt. %, from 25 wt. % to 35 wt. %, from 25 wt. % to 30 wt. %, from 25 wt. % to 26 wt. %, or approximately 25.6 wt. % H 2 S by weight of the first gas fraction  164 . In embodiments, the first gas fraction  164  may include from 1 wt. % to 50 wt. %, from 1 wt. % to 25 wt. %, from 1 wt. % to 20 wt. %, from 1 wt. % to 15 wt. %, from 5 wt. % to 50 wt. %, from 5 wt. % to 25 wt. %, from 5 wt. % to 20 wt. %, from 5 wt. % to 15 wt. %, from 10 wt. % to 50 wt. %, from 10 wt. % to 25 wt. %, from 10 wt. % to 20 wt. %, from 10 wt. % to 15 wt. %, from 12 wt. % to 50 wt. %, from 12 wt. % to 25 wt. %, from 12 wt. % to 20 wt. %, from 12 wt. % to 15 wt. %, from 14 wt. % to 50 wt. %, from 14 wt. % to 25 wt. %, from 14 wt. % to 20 wt. %, from 14 wt. % to 15 wt. %, or approximately 14.6 wt. % NH 3  by weight of the first gas fraction  164 . In embodiments, the first gas fraction  164  may include no C 5  or C 6  components. In embodiments, the liquid oil fraction  162  may have a T 5  true boiling point (TBP) of less than 500° C., of less than 400° C., of less than 350° C., of less than 325° C., of less than 300° C., of less than 275° C., or of less than 260° C. In embodiments, the liquid oil fraction  162  may have a T 5  TBP of from 25° C. to 350° C., from 25° C. to 325° C., from 25° C. to 300° C., from 25° C. to 275° C., from 25° C. to 250° C., from 25° C. to 225° C., from 25° C. to 200° C., from 25° C. to 175° C., from 25° C. to 150° C., from 25° C. to 125° C., from 25° C. to 100° C., from 25° C. to 75° C., from 25° C. to 50° C., from 50° C. to 350° C., from 50° C. to 325° C., from 50° C. to 300° C., from 50° C. to 275° C., from 50° C. to 250° C., from 50° C. to 225° C., from 50° C. to 200° C., from 50° C. to 175° C., from 50° C. to 150° C., from 50° C. to 125° C., from 50° C. to 100° C., from 50° C. to 75° C., from 75° C. to 350° C., from 75° C. to 325° C., from 75° C. to 300° C., from 75° C. to 275° C., from 75° C. to 250° C., from 75° C. to 225° C., from 75° C. to 200° C., from 75° C. to 175° C., from 75° C. to 150° C., from 75° C. to 125° C., from 75° C. to 100° C., from 100° C. to 350° C., from 100° C. to 325° C., from 100° C. to 300° C., from 100° C. to 275° C., from 100° C. to 250° C., from 100° C. to 225° C., from 100° C. to 200° C., from 100° C. to 175° C., from 100° C. to 150° C., from 100° C. to 125° C., from 125° C. to 350° C., from 125° C. to 325° C., from 125° C. to 300° C., from 125° C. to 275° C., from 125° C. to 250° C., from 125° C. to 225° C., from 125° C. to 200° C., from 125° C. to 175° C., from 125° C. to 150° C., from 150° C. to 350° C., from 150° C. to 325° C., from 150° C. to 300° C., from 150° C. to 275° C., from 150° C. to 250° C., from 150° C. to 225° C., from 150° C. to 200° C., from 150° C. to 175° C., from 175° C. to 350° C., from 175° C. to 325° C., from 175° C. to 300° C., from 175° C. to 275° C., from 175° C. to 250° C., from 175° C. to 225° C., from 175° C. to 200° C., from 200° C. to 350° C., from 200° C. to 325° C., from 200° C. to 300° C., from 200° C. to 275° C., from 200° C. to 250° C., from 200° C. to 225° C., from 225° C. to 350° C., from 225° C. to 325° C., from 225° C. to 300° C., from 225° C. to 275° C., from 225° C. to 250° C., from 250° C. to 350° C., from 250° C. to 325° C., from 250° C. to 300° C., from 250° C. to 275° C., from 275° C. to 350° C., from 275° C. to 325° C., from 275° C. to 300° C., from 300° C. to 350° C., from 300° C. to 325° C., or from 325° C. to 350° C. The liquid oil fraction  162  may have a T 90  TBP of less than or equal to 650° C., less than or equal to 600° C., less than or equal to 575° C., or less than or equal to 550° C. In embodiments, the liquid oil fraction  162  may have a T 90  TBP from 200° C. to 650° C., from 200° C. to 600° C., from 200° C. to 575° C., from 200° C. to 550° C., from 200° C. to 540° C., from 200° C. to 530° C., from 200° C. to 525° C., from 200° C. to 500° C., from 200° C. to 450° C., from 200° C. to 400° C., from 200° C. to 300° C., from 300° C. to 650° C., from 300° C. to 600° C., from 300° C. to 575° C., from 300° C. to 550° C., from 300° C. to 540° C., from 300° C. to 530° C., from 300° C. to 525° C., from 300° C. to 500° C., from 300° C. to 450° C., from 300° C. to 400° C., from 400° C. to 650° C., from 400° C. to 600° C., from 400° C. to 575° C., from 400° C. to 550° C., from 400° C. to 540° C., from 400° C. to 530° C., from 400° C. to 525° C., from 400° C. to 500° C., from 450° C. to 650° C., from 450° C. to 600° C., from 450° C. to 575° C., from 450° C. to 550° C., from 450° C. to 540° C., from 450° C. to 530° C., from 450° C. to 525° C., from 450° C. to 500° C., from 500° C. to 650° C., from 500° C. to 600° C., from 500° C. to 575° C., from 500° C. to 550° C., from 500° C. to 540° C., from 500° C. to 530° C., from 500° C. to 525° C., from 525° C. to 650° C., from 525° C. to 600° C., from 525° C. to 575° C., from 525° C. to 550° C., from 525° C. to 540° C., from 525° C. to 530° C., from 530° C. to 650° C., from 530° C. to 600° C., from 530° C. to 575° C., from 530° C. to 550° C., from 530° C. to 540° C., from 540° C. to 650° C., from 540° C. to 600° C., from 540° C. to 575° C., from 540° C. to 550° C., from 550° C. to 650° C., from 550° C. to 600° C., from 550° C. to 575° C., from 575° C. to 650° C., from 575° C. to 600° C., or from 600° C. to 650° C., where the T 90  TBP is greater than the T 5  TBP previously described. The liquid oil fraction  162  may have an API gravity from 12° to 45°, from 12° to 35°, from 12° to 30°, from 12° to 27°, from 12° to 25°, from 15° to 45°, from 15° to 35°, from 15° to 30°, from 15° to 27°, from 15° to 25°, from 18° to 45°, from 18° to 35°, from 18° to 30°, from 18° to 27°, from 18° to 25°, from 20° to 45°, from 20° to 35°, from 20° to 30°, from 20° to 27°, from 20° to 25°, from 21° to 45°, from 21° to 35°, from 21° to 30°, from 21° to 27°, from 21° to 25°, from 23° to 45°, from 23° to 35°, from 23° to 30°, from 23° to 27°, from 23° to 25°, or approximately 24°. The liquid oil fraction  162  may include less than 3.4 wt. % or less than 2.7 wt. % total sulfur content by weight of the liquid oil fraction  162 . In embodiments, the liquid oil fraction  162  may include from 0.1 wt. % to 5 wt. %, from 0.1 wt. % to 4 wt. %, from 0.1 wt. % to 3.3 wt. %, from 0.1 wt. % to 3.0 wt. %, from 0.1 wt. % to 2.8 wt. %, from 0.1 wt. % to 2.6 wt. %, from 0.1 wt. % to 2.3 wt. %, from 0.1 wt. % to 2.0 wt. %, from 0.1 wt. % to 1.8 wt. %, from 0.1 wt. % to 1.6 wt. %, from 0.1 wt. % to 1.3 wt. %, from 0.1 wt. % to 1.0 wt. %, from 0.1 wt. % to 0.5 wt. %, from 0.5 wt. % to 5 wt. %, from 0.5 wt. % to 4 wt. %, from 0.5 wt. % to 3.3 wt. %, from 0.5 wt. % to 3.0 wt. %, from 0.5 wt. % to 2.8 wt. %, from 0.5 wt. % to 2.6 wt. %, from 0.5 wt. % to 2.3 wt. %, from 0.5 wt. % to 2.0 wt. %, from 0.5 wt. % to 1.8 wt. %, from 0.5 wt. % to 1.6 wt. %, from 0.5 wt. % to 1.3 wt. %, from 0.5 wt. % to 1.0 wt. %, from 1.0 wt. % to 5 wt. %, from 1.0 wt. % to 4 wt. %, from 1.0 wt. % to 3.3 wt. %, from 1.0 wt. % to 3.0 wt. %, from 1.0 wt. % to 2.8 wt. %, from 1.0 wt. % to 2.6 wt. %, from 1.0 wt. % to 2.3 wt. %, from 1.0 wt. % to 2.0 wt. %, from 1.0 wt. % to 1.8 wt. %, from 1.0 wt. % to 1.6 wt. %, from 1.0 wt. % to 1.3 wt. %, from 1.3 wt. % to 5 wt. %, from 1.3 wt. % to 4 wt. %, from 1.3 wt. % to 3.3 wt. %, from 1.3 wt. % to 3.0 wt. %, from 1.3 wt. % to 2.8 wt. %, from 1.3 wt. % to 2.6 wt. %, from 1.3 wt. % to 2.3 wt. %, from 1.3 wt. % to 2.0 wt. %, from 1.3 wt. % to 1.8 wt. %, from 1.3 wt. % to 1.6 wt. %, from 1.6 wt. % to 5 wt. %, from 1.6 wt. % to 4 wt. %, from 1.6 wt. % to 3.3 wt. %, from 1.6 wt. % to 3.0 wt. %, from 1.6 wt. % to 2.8 wt. %, from 1.6 wt. % to 2.6 wt. %, from 1.6 wt. % to 2.3 wt. %, from 1.6 wt. % to 2.0 wt. %, from 1.6 wt. % to 1.8 wt. %, or approximately 1.7 wt. % total sulfur content by weight of the liquid oil fraction  162 . The liquid oil fraction  162  may include less than 1.2 wt. % or less than 0.9 wt. % total nitrogen content by weight of the liquid oil fraction  162 . In embodiments, the liquid oil fraction  162  may include from 0.01 wt. % to 2 wt. %, from 0.01 wt. % to 1.1 wt. %, from 0.01 wt. % to 1.0 wt. %, from 0.01 wt. % to 0.8 wt. %, from 0.01 wt. % to 0.6 wt. %, from 0.01 wt. % to 0.4 wt. %, from 0.01 wt. % to 0.2 wt. %, from 0.01 wt. % to 0.1 wt. %, from 0.1 wt. % to 2 wt. %, from 0.1 wt. % to 1.1 wt. %, from 0.1 wt. % to 1.0 wt. %, from 0.1 wt. % to 0.8 wt. %, from 0.1 wt. % to 0.6 wt. %, from 0.1 wt. % to 0.4 wt. %, from 0.1 wt. % to 0.2 wt. %, from 0.2 wt. % to 2 wt. %, from 0.2 wt. % to 1.1 wt. %, from 0.2 wt. % to 1.0 wt. %, from 0.2 wt. % to 0.8 wt. %, from 0.2 wt. % to 0.6 wt. %, from 0.2 wt. % to 0.4 wt. %, from 0.4 wt. % to 2 wt. %, from 0.4 wt. % to 1.1 wt. %, from 0.4 wt. % to 1.0 wt. %, from 0.4 wt. % to 0.8 wt. %, from 0.4 wt. % to 0.6 wt. %, or approximately 0.3 wt. % total nitrogen content by weight of the liquid oil fraction  162 . The liquid oil fraction  162  may include less than 4.8 wt. % or less than 1.7 wt. % asphaltene (heptane-insoluble) by weight of the liquid oil fraction  162 . In embodiments, the liquid oil fraction  162  may include from 0.01 wt. % to 6 wt. %, from 0.01 wt. % to 5 wt. %, from 0.01 wt. % to 4.7 wt. %, from 0.01 wt. % to 4.0 wt. %, from 0.01 wt. % to 3.0 wt. %, from 0.01 wt. % to 2.5 wt. %, from 0.01 wt. % to 2.0 wt. %, from 0.01 wt. % to 1.8 wt. %, from 0.01 wt. % to 1.6 wt. %, from 0.01 wt. % to 1.0 wt. %, from 0.01 wt. % to 0.8 wt. %, from 0.01 wt. % to 0.6 wt. %, from 0.01 wt. % to 0.4 wt. %, from 0.01 wt. % to 0.2 wt. %, from 0.01 wt. % to 0.1 wt. %, from 0.1 wt. % to 6 wt. %, from 0.1 wt. % to 5 wt. %, from 0.1 wt. % to 4.7 wt. %, from 0.1 wt. % to 4.0 wt. %, from 0.1 wt. % to 3.0 wt. %, from 0.1 wt. % to 2.5 wt. %, from 0.1 wt. % to 2.0 wt. %, from 0.1 wt. % to 1.8 wt. %, from 0.1 wt. % to 1.6 wt. %, from 0.1 wt. % to 1.0 wt. %, from 0.1 wt. % to 0.8 wt. %, from 0.1 wt. % to 0.6 wt. %, from 0.1 wt. % to 0.4 wt. %, from 0.1 wt. % to 0.2 wt. %, from 0.2 wt. % to 6 wt. %, from 0.2 wt. % to 5 wt. %, from 0.2 wt. % to 4.7 wt. %, from 0.2 wt. % to 4.0 wt. %, from 0.2 wt. % to 3.0 wt. %, from 0.2 wt. % to 2.5 wt. %, from 0.2 wt. % to 2.0 wt. %, from 0.2 wt. % to 1.8 wt. %, from 0.2 wt. % to 1.6 wt. %, from 0.2 wt. % to 1.0 wt. %, from 0.2 wt. % to 0.8 wt. %, from 0.2 wt. % to 0.6 wt. %, from 0.2 wt. % to 0.4 wt. %, from 0.4 wt. % to 6 wt. %, from 0.4 wt. % to 5 wt. %, from 0.4 wt. % to 4.7 wt. %, from 0.4 wt. % to 4.0 wt. %, from 0.4 wt. % to 3.0 wt. %, from 0.4 wt. % to 2.5 wt. %, from 0.4 wt. % to 2.0 wt. %, from 0.4 wt. % to 1.8 wt. %, from 0.4 wt. % to 1.6 wt. %, from 0.4 wt. % to 1.0 wt. %, from 0.4 wt. % to 0.8 wt. %, from 0.4 wt. % to 0.6 wt. %, or approximately 0.3 wt. % asphaltene (heptane-insoluble) by weight of the liquid oil fraction  162 . The upgraded product stream  152  may include less than 83 parts per million (ppm) or less than 9 ppm metals. In embodiments, the metals may be vanadium, nickel, or both. In embodiments, the upgraded product stream  152  may include from 1 ppm to 100 ppm, from 1 ppm to 82 ppm, from 1 ppm to 50 ppm, from 1 ppm to 25 ppm, from 1 ppm to 15 ppm, from 1 ppm to 10 ppm, from 1 ppm to 8 ppm, from 1 ppm to 5 ppm, from 1 ppm to 3 ppm, from 3 ppm to 100 ppm, from 3 ppm to 82 ppm, from 3 ppm to 50 ppm, from 3 ppm to 25 ppm, from 3 ppm to 15 ppm, from 3 ppm to 10 ppm, from 3 ppm to 8 ppm, from 3 ppm to 5 ppm, or approximately 4 ppm metals. The liquid oil fraction  162  may have a viscosity at 50° C. of less than 640 centiStokes (cSt) or less than 89 cSt. In embodiments, the liquid oil fraction  162  may have a viscosity at 50° C. from 10 cSt to 639 cSt, from 10 cSt to 600 cSt, from 10 cSt to 400 cSt, from 10 cSt to 200 cSt, from 10 cSt to 150 cSt, from 10 cSt to 100 cSt, from 10 cSt to 90 cSt, from 10 cSt to 88 cSt, from 10 cSt to 70 cSt, from 10 cSt to 50 cSt, from 10 cSt to 35 cSt, from 10 cSt to 28 cSt, from 10 cSt to 26 cSt, from 10 cSt to 20 cSt, from 20 cSt to 639 cSt, from 20 cSt to 600 cSt, from 20 cSt to 400 cSt, from 20 cSt to 200 cSt, from 20 cSt to 150 cSt, from 20 cSt to 100 cSt, from 20 cSt to 90 cSt, from 20 cSt to 88 cSt, from 20 cSt to 70 cSt, from 20 cSt to 50 cSt, from 20 cSt to 35 cSt, from 20 cSt to 28 cSt, from 20 cSt to 26 cSt, from 26 cSt to 639 cSt, from 26 cSt to 600 cSt, from 26 cSt to 400 cSt, from 26 cSt to 200 cSt, from 26 cSt to 150 cSt, from 26 cSt to 100 cSt, from 26 cSt to 90 cSt, from 26 cSt to 88 cSt, from 26 cSt to 70 cSt, from 26 cSt to 50 cSt, from 26 cSt to 35 cSt, from 26 cSt to 28 cSt, or approximately 27 cSt. 
     As shown in  FIG. 1 , the first gas fraction  164  may be passed to a gas storage tank  165 , the liquid oil fraction  162  may be passed to an oil storage tank  163 , and the first water fraction  166  may be passed to a water storage tank  167 . 
       FIG. 2  schematically depicts a process  200  for treating a disulfide oil composition  205 , according to embodiments described. For the reference numbers and descriptions of the process  200  that correlate with previous reference numbers and descriptions for process  100 , it is intended that all previous description for process  100  relevant to the reference numbers used in process  200  should be incorporated. For example, and not by way of limitation, water stream  110  in process  200  is meant to correspond and incorporate all previous descriptions of water stream  110  in process  100 . 
     The disulfide oil composition  205  may refer to any disulfide composition. In embodiments, it is contemplated that the disulfide oil composition  205  may be the product of a naphtha and LPG mercaptan oxidation unit  203 , which is a refining technology that selectively removes mercaptans sulfur by caustic extraction and generates disulfide oil (RSSR), by oxidizing sulfur rich caustic solution, as byproduct. In embodiments, the disulfide composition  205  may include dimethyl disulfide, methyl ethyl disulfide, methyl isopropyl disulfide, diethyl disulfide, methyl n-propyl disulfide, ethyl isopropyl disulfide, ethyl n-propyl disulfide, di-isopropyl disulfide, ethyl n-butyl disulfide, dipropyl disulfide, dimethyl trisulfide, diethyl trisulfide, methyl propyl trisulfide, di-isopropyl trisulfide, or combinations thereof. It is noted that different components may have different names but the same chemical formula. 
     The disulfide oil composition  205  may include from 5 wt. % to 50 wt. %, from 5 wt. % to 25 wt. %, from 5 wt. % to 20 wt. %, from 5 wt. % to 18 wt. %, from 5 wt. % to 15 wt. %, from 5 wt. % to 13 wt. %, from 5 wt. % to 10 wt. %, from 5 wt. % to 8 wt. %, from 8 wt. % to 50 wt. %, from 8 wt. % to 25 wt. %, from 8 wt. % to 20 wt. %, from 8 wt. % to 18 wt. %, from 8 wt. % to 15 wt. %, from 8 wt. % to 13 wt. %, from 8 wt. % to 10 wt. %, from 10 wt. % to 50 wt. %, from 10 wt. % to 25 wt. %, from 10 wt. % to 20 wt. %, from 10 wt. % to 18 wt. %, from 10 wt. % to 15 wt. %, from 10 wt. % to 13 wt. %, from 13 wt. % to 50 wt. %, from 13 wt. % to 25 wt. %, from 13 wt. % to 20 wt. %, from 13 wt. % to 18 wt. %, from 13 wt. % to 15 wt. %, from 15 wt. % to 50 wt. %, from 15 wt. % to 25 wt. %, from 15 wt. % to 20 wt. %, from 15 wt. % to 18 wt. %, from 18 wt. % to 50 wt. %, from 18 wt. % to 25 wt. %, from 18 wt. % to 20 wt. %, from 20 wt. % to 50 wt. %, from 20 wt. % to 25 wt. %, from 25 wt. % to 50 wt. %, or approximately 14 wt. % C 2 H 6 S 2  by weight of the disulfide oil composition  205 . In embodiments, C 2 H 6 S 2  may include dimethyl disulfide. 
     The disulfide oil composition  205  may include from 10 wt. % to 50 wt. %, from 10 wt. % to 40 wt. %, from 10 wt. % to 35 wt. %, from 10 wt. % to 30 wt. %, from 10 wt. % to 28 wt. %, from 10 wt. % to 25 wt. %, from 10 wt. % to 23 wt. %, from 10 wt. % to 20 wt. %, from 10 wt. % to 15 wt. %, from 15 wt. % to 50 wt. %, from 15 wt. % to 40 wt. %, from 15 wt. % to 35 wt. %, from 15 wt. % to 30 wt. %, from 15 wt. % to 28 wt. %, from 15 wt. % to 25 wt. %, from 15 wt. % to 23 wt. %, from 15 wt. % to 20 wt. %, from 20 wt. % to 50 wt. %, from 20 wt. % to 40 wt. %, from 20 wt. % to 35 wt. %, from 20 wt. % to 30 wt. %, from 20 wt. % to 28 wt. %, from 20 wt. % to 25 wt. %, from 20 wt. % to 23 wt. %, from 23 wt. % to 50 wt. %, from 23 wt. % to 40 wt. %, from 23 wt. % to 35 wt. %, from 23 wt. % to 30 wt. %, from 23 wt. % to 28 wt. %, from 23 wt. % to 25 wt. %, from 25 wt. % to 50 wt. %, from 25 wt. % to 40 wt. %, from 25 wt. % to 35 wt. %, from 25 wt. % to 30 wt. %, from 25 wt. % to 28 wt. %, from 28 wt. % to 50 wt. %, from 28 wt. % to 40 wt. %, from 28 wt. % to 35 wt. %, from 28 wt. % to 30 wt. %, from 30 wt. % to 50 wt. %, from 30 wt. % to 40 wt. %, from 30 wt. % to 35 wt. %, from 35 wt. % to 50 wt. %, from 35 wt. % to 40 wt. %, from 40 to 50 wt. %, or approximately 24 wt. % C 3 H 8 S 2  by weight of the disulfide oil composition  205 . In embodiments, C 3 H 8 S 2  may include methyl ethyl disulfide. 
     The disulfide oil composition  205  may include from 10 wt. % to 50 wt. %, from 10 wt. % to 40 wt. %, from 10 wt. % to 35 wt. %, from 10 wt. % to 30 wt. %, from 10 wt. % to 28 wt. %, from 10 wt. % to 26 wt. %, from 10 wt. % to 23 wt. %, from 10 wt. % to 20 wt. %, from 10 wt. % to 15 wt. %, from 15 wt. % to 50 wt. %, from 15 wt. % to 40 wt. %, from 15 wt. % to 35 wt. %, from 15 wt. % to 30 wt. %, from 15 wt. % to 28 wt. %, from 15 wt. % to 26 wt. %, from 15 wt. % to 23 wt. %, from 15 wt. % to 20 wt. %, from 20 wt. % to 50 wt. %, from 20 wt. % to 40 wt. %, from 20 wt. % to 35 wt. %, from 20 wt. % to 30 wt. %, from 20 wt. % to 28 wt. %, from 20 wt. % to 26 wt. %, from 20 wt. % to 23 wt. %, from 23 wt. % to 50 wt. %, from 23 wt. % to 40 wt. %, from 23 wt. % to 35 wt. %, from 23 wt. % to 30 wt. %, from 23 wt. % to 28 wt. %, from 23 wt. % to 26 wt. %, from 26 wt. % to 50 wt. %, from 26 wt. % to 40 wt. %, from 26 wt. % to 35 wt. %, from 26 wt. % to 30 wt. %, from 26 wt. % to 28 wt. %, from 28 wt. % to 50 wt. %, from 28 wt. % to 40 wt. %, from 28 wt. % to 35 wt. %, from 28 wt. % to 30 wt. %, from 30 wt. % to 50 wt. %, from 30 wt. % to 40 wt. %, from 30 wt. % to 35 wt. %, from 35 wt. % to 50 wt. %, from 35 wt. % to 40 wt. %, from 40 to 50 wt. %, or approximately 27 wt. % C 4 H 10 S 2  by weight of the disulfide oil composition  205 . In embodiments, C 4 H 10 S 2  may include methyl isopropyl disulfide, diethyl disulfide, methyl n-propyl disulfide, or combinations thereof. 
     The disulfide oil composition  205  may include from 5 wt. % to 50 wt. %, from 5 wt. % to 25 wt. %, from 5 wt. % to 23 wt. %, from 5 wt. % to 20 wt. %, from 5 wt. % to 18 wt. %, from 5 wt. % to 16 wt. %, from 5 wt. % to 14 wt. %, from 5 wt. % to 12 wt. %, from 5 wt. % to 10 wt. %, from 10 wt. % to 50 wt. %, from 10 wt. % to 25 wt. %, from 10 wt. % to 23 wt. %, from 10 wt. % to 20 wt. %, from 10 wt. % to 18 wt. %, from 10 wt. % to 16 wt. %, from 10 wt. % to 14 wt. %, from 10 wt. % to 12 wt. %, from 12 wt. % to 50 wt. %, from 12 wt. % to 25 wt. %, from 12 wt. % to 23 wt. %, from 12 wt. % to 20 wt. %, from 12 wt. % to 18 wt. %, from 12 wt. % to 16 wt. %, from 12 wt. % to 14 wt. %, from 14 wt. % to 50 wt. %, from 14 wt. % to 25 wt. %, from 14 wt. % to 23 wt. %, from 14 wt. % to 20 wt. %, from 14 wt. % to 18 wt. %, from 14 wt. % to 16 wt. %, from 16 wt. % to 50 wt. %, from 16 wt. % to 25 wt. %, from 16 wt. % to 23 wt. %, from 16 wt. % to 20 wt. %, from 16 wt. % to 18 wt. %, from 18 wt. % to 50 wt. %, from 18 wt. % to 25 wt. %, from 18 wt. % to 23 wt. %, from 18 wt. % to 20 wt. %, from 20 wt. % to 50 wt. %, from 20 wt. % to 25 wt. %, from 20 wt. % to 23 wt. %, from 23 wt. % to 50 wt. %, from 23 wt. % to 25 wt. %, from 25 wt. % wt. % to 50 wt. %, or approximately 15 wt. % C 5 H 12 S 2  by weight of the disulfide oil composition  205  by weight of the disulfide oil composition  205 . In embodiments, C 5 H 12 S 2  may include ethyl n-propyl disulfide, ethyl isopropyl disulfide, or both. 
     The disulfide oil composition  205  may include from 1 wt. % to 20 wt. %, from 1 wt. % to 15 wt. %, from 1 wt. % to 10 wt. %, from 1 wt. % to 8 wt. %, from 1 wt. % to 6 wt. %, from 1 wt. % to 4 wt. %, from 1 wt. % to 2 wt. %, from 2 wt. % to 20 wt. %, from 2 wt. % to 15 wt. %, from 2 wt. % to 10 wt. %, from 2 wt. % to 8 wt. %, from 2 wt. % to 6 wt. %, from 2 wt. % to 4 wt. %, from 4 wt. % to 20 wt. %, from 4 wt. % to 15 wt. %, from 4 wt. % to 10 wt. %, from 4 wt. % to 8 wt. %, from 4 wt. % to 6 wt. %, from 6 wt. % to 20 wt. %, from 6 wt. % to 15 wt. %, from 6 wt. % to 10 wt. %, from 6 wt. % to 8 wt. %, from 8 wt. % to 20 wt. %, from 8 wt. % to 15 wt. %, from 8 wt. % to 10 wt. %, from 10 wt. % to 20 wt. %, from 10 wt. % to 15 wt. %, from 15 wt. % to 20 wt. %, or approximately 5 wt. % C 6 H 14 S 2  by weight of the disulfide oil composition  205 . In embodiments, C 6 H 14 S 2  may include di-isopropyl disulfide, di-propyl disulfide, ethyl n-butyl disulfide, or combinations thereof. 
     The disulfide oil composition  205  may include from 1 wt. % to 30 wt. %, from 1 wt. % to 25 wt. %, from 1 wt. % to 20 wt. %, from 1 wt. % to 18 wt. %, from 1 wt. % to 16 wt. %, from 1 wt. % to 14 wt. %, from 1 wt. % to 12 wt. %, from 1 wt. % to 10 wt. %, from 1 wt. % to 5 wt. %, from 5 wt. % to 30 wt. %, from 5 wt. % to 25 wt. %, from 5 wt. % to 20 wt. %, from 5 wt. % to 18 wt. %, from 5 wt. % to 16 wt. %, from 5 wt. % to 14 wt. %, from 5 wt. % to 12 wt. %, from 5 wt. % to 10 wt. %, from 10 wt. % to 30 wt. %, from 10 wt. % to 25 wt. %, from 10 wt. % to 20 wt. %, from 10 wt. % to 18 wt. %, from 10 wt. % to 16 wt. %, from 10 wt. % to 14 wt. %, from 10 wt. % to 12 wt. %, from 12 wt. % to 30 wt. %, from 12 wt. % to 25 wt. %, from 12 wt. % to 20 wt. %, from 12 wt. % to 18 wt. %, from 12 wt. % to 16 wt. %, from 12 wt. % to 14 wt. %, from 14 wt. % to 30 wt. %, from 14 wt. % to 25 wt. %, from 14 wt. % to 20 wt. %, from 14 wt. % to 18 wt. %, from 14 wt. % to 16 wt. %, from 16 wt. % to 30 wt. %, from 16 wt. % to 25 wt. %, from 16 wt. % to 20 wt. %, from 16 wt. % to 18 wt. %, from 18 wt. % to 30 wt. %, from 18 wt. % to 25 wt. %, from 18 wt. % to 20 wt. %, from 20 wt. % to 30 wt. %, from 20 wt. % to 25 wt. %, from 25 wt. % wt. % to 30 wt. %, or approximately 15 wt. % NaOH and water combined by weight of the disulfide oil composition  205 . 
     As shown in  FIG. 2 , the disulfide oil composition  205  may be pressurized in disulfide pump  212  to create pressurized disulfide oil composition  216 . The pressure of pressurized disulfide oil composition  216  may be at least 22.1 megapascals (MPa), which is approximately the critical pressure of water. Alternatively, the pressure of the pressurized disulfide oil composition  216  may be between 23 MPa and 35 MPa, or between 24 MPa and 30 MPa. For instance, the pressure of the pressurized disulfide oil composition  216  may be between 25 MPa and 29 MPa, 26 MPa and 28 MPa, 25 MPa and 30 MPa, 26 MPa and 29 MPa, or 24 MPa and 28 MPa. 
     The pressurized disulfide oil composition  216  may then be heated in one or more disulfide pre-heaters  220  to form pressurized, heated disulfide oil composition  224 . In one embodiment, the pressurized, heated disulfide oil composition  224  has a pressure greater than the critical pressure of water and a temperature greater than 75° C. The temperature of the pressurized, heated disulfide oil composition  224  may be between 10° C. and 300° C., or between 50° C. and 250° C., or between 75° C. and 225° C., or between 100° C. and 200° C., or between 140° C. and 200° C., or between 160° C. and 200° C. The temperature of the pressurized, heated disulfide oil composition  224  may be from 100° C. to 300° C., from 100° C. to 250° C., from 100° C. to 200° C., from 100° C. to 190° C., from 100° C. to 180° C., from 100° C. to 170° C., from 100° C. to 160° C., from 100° C. to 150° C., from 150° C. to 300° C., from 150° C. to 250° C., from 150° C. to 200° C., from 150° C. to 190° C., from 150° C. to 180° C., from 150° C. to 170° C., from 150° C. to 160° C., from 160° C. to 300° C., from 160° C. to 250° C., from 160° C. to 200° C., from 160° C. to 190° C., from 160° C. to 180° C., from 160° C. to 170° C., from 170° C. to 300° C., from 170° C. to 250° C., from 170° C. to 200° C., from 170° C. to 190° C., from 170° C. to 180° C., from 180° C. to 300° C., from 180° C. to 250° C., from 180° C. to 200° C., from 180° C. to 190° C., from 190° C. to 300° C., from 190° C. to 250° C., from 190° C. to 200° C., from 200° C. to 300° C., from 200° C. to 250° C., or from 250° C. to 300° C. Without intending to be bound by theory, the disulfide oil is a light material and does not require high heat to be mixed with water; therefore, it may be desirable to heat it at or below 180° C. Heating above 180° C. may consume unnecessary energy and may cause undesirable evaporation of the disulfide oil before it is mixed with water and cause operation difficulties. It is contemplated that it may be important to keep the oil and water in liquid phase for better mixing. Heating below 100° C. may result in difficult mixing and induce oil and water phase separation. It is important to heat up the combined feedstock stream  232  after the mixer  130  close to water critical temperature (374° C.) by heat exchanger, or an electric heater or any type of heater (not shown in the  FIG. 2 ) to avoid quenching the inlet of the supercritical water hydrogenation reactor  150  and to assure that the reactions inside the reactor  150  are taking place at water supercritical conditions. 
     Similar to water pre-heater  122  and hydrogen pre-heaters  128 , suitable disulfide pre-heaters  220  may include a natural gas fired heater, a heat exchanger, and an electric heater. The disulfide pre-heater  220  may be a unit separate and independent from the water pre-heater  122  and the hydrogen pre-heater  128 . 
     The heated water stream  126 , the heated hydrogen stream  129 , and the pressurized, heated disulfide oil composition  224  may then be mixed in feed mixer  130  to produce a combined disulfide feed stream  232 . The feed mixer  130  can be any type of mixing device capable of mixing the heated water stream  126  and the pressurized, heated disulfide oil composition  224 . In one embodiment, the feed mixer  130  may be a mixing tee. The feed mixer  130  may be an ultrasonic device, a small continuous stir tank reactor (CSTR), or any suitable mixer. The volumetric flow ratio of each component fed to the feed mixer  130  may vary. In embodiments, the volumetric flow ratio of the heated disulfide oil composition  224  to the heated water stream  126  may be from 1:10 to 1:1, from 1:10 to 1:5, from 1:10 to 1:2, from 1:5 to 1:1, from 1:5 to 1:2, or from 1:2 to 1:1 at standard ambient temperature and ambient pressure (SATP). In embodiments, the hydrogen-to-oil volumetric flow can be from 10 to 5000 cubic feet of heated hydrogen stream  129  to one barrel of heated disulfide oil composition  224 , at SATP. 
     The combined disulfide feed stream  232  may then be introduced to the supercritical water hydrogenation reactor  150  configured to upgrade the combined feed stream  232 . The supercritical water hydrogenation reactor  150  may be substantially similar to the supercritical water hydrogenation reactor  150  as previously described. In the supercritical water hydrogenation reactor  150  the disulfide oil and hydrogen are dissolved in the supercritical water where C—S, H—H, and S—S bonds are broken and the generated hydrocarbon and heteroatoms radicals are saturated. 
     Referring to  FIG. 2 , upon exiting the supercritical water hydrogenation reactor  150 , the upgraded disulfide product  252  may be cooled by cooler  154  to a temperature from 20° C. to 50° C., from 20° C. to 40° C., from 20° C. to 30° C., from 30° C. to 50° C., from 30° C. to 40° C., or from 40° C. to 50° C. to form a cooled, upgraded disulfide product  256 . 
     Upon exiting the cooler  154 , the pressure of the cooled, upgraded disulfide product  256  may be reduced to create a depressurized, upgraded disulfide product  259 , which may have a pressure from 0.01 MPa to 1.0 MPa, from 0.01 MPa to 0.8 MPa, from 0.01 MPa to 0.5 MPa, from 0.01 MPa to 0.3 MPa, from 0.01 MPa to 0.1 MPa, from 0.01 MPa to 0.08 MPa, from 0.01 MPa to 0.05 MPa, from 0.01 MPa to 0.03 MPa, from 0.03 MPa to 1.0 MPa, from 0.03 MPa to 0.8 MPa, from 0.03 MPa to 0.5 MPa, from 0.03 MPa to 0.3 MPa, from 0.03 MPa to 0.1 MPa, from 0.03 MPa to 0.08 MPa, from 0.03 MPa to 0.05 MPa, from 0.05 MPa to 1.0 MPa, from 0.05 MPa to 0.8 MPa, from 0.05 MPa to 0.5 MPa, from 0.05 MPa to 0.3 MPa, from 0.05 MPa to 0.1 MPa, from 0.05 MPa to 0.08 MPa, from 0.08 MPa to 1.0 MPa, from 0.08 MPa to 0.8 MPa, from 0.08 MPa to 0.5 MPa, from 0.08 MPa to 0.3 MPa, from 0.08 MPa to 0.1 MPa, from 0.1 MPa to 1.0 MPa, from 0.1 MPa to 0.8 MPa, from 0.1 MPa to 0.5 MPa, from 0.1 MPa to 0.3 MPa, from 0.3 MPa to 1.0 MPa, from 0.3 MPa to 0.8 MPa, from 0.3 MPa to 0.5 MPa, from 0.5 MPa to 1.0 MPa, from 0.5 MPa to 0.8 MPa, or from 0.8 MPa to 1.0 MPa. The depressurizing can be achieved by many devices, for example, a valve  158  as shown in  FIGS. 1 and 2 . 
     The depressurized, upgraded disulfide product  259  may then be passed to a gas/water separator  160 . The gas/water separator  160  may separate the depressurized, upgraded disulfide product  259  into a second gas fraction  264  and a second water fraction  266 . The gas/water separator  160  may be any separator known in the industry. While the gas/water separator  160  may separate the depressurized, upgraded disulfide product  259  into at least a second gas fraction  264  and a second water fraction  266 , it should be appreciated that additional fractions may also be produced. The second gas fraction  264  may be passed to the gas storage tank  165  and the second water fraction  266  may be passed to the water storage tank  167 . In embodiments, the percent conversion of the disulfide oil composition  205  may be from 50% to 99%, from 50% to 95%, from 50% to 90%, from 50% to 85%, from 50% to 82%, from 60% to 99%, from 60% to 95%, from 60% to 90%, from 60% to 85%, from 60% to 82%, from 70% to 99%, from 70% to 95%, from 70% to 90%, from 70% to 85%, from 70% to 82%, from 75% to 99%, from 75% to 95%, from 75% to 90%, from 75% to 85%, from 75% to 82%, from 78% to 99%, from 78% to 95%, from 78% to 90%, from 78% to 85%, from 78% to 82%, or approximately 80%. 
     In embodiments, the second gas fraction  264  may include H 2 , C 2 H 6 , C 3 H 8 , C 4 H 10 , C 5 H 12 , C 6 H 14 , CH 3 SH, C 2 H 5 SH, C 4 H 9 SH, C 5 H 11 SH, H 2 S, C 2 H 6 S 2 , C 3 H 8 S 2 , C 4 H 10 S 2 , C 5 H 12 S 2 , C 6 H 14 S 2 , or combinations thereof. 
     The second gas fraction  264  may include from 0.1 wt. % to 0.5 wt. %, from 0.1 wt. % to 0.4 wt. %, from 0.1 wt. % to 0.3 wt. %, from 0.1 wt. % to 0.2 wt. %, from 0.2 wt. % to 0.5 wt. %, from 0.2 wt. % to 0.4 wt. %, from 0.2 wt. % to 0.3 wt. %, from 0.3 wt. % to 0.5 wt. %, from 0.3 wt. % to 0.4 wt. %, from 0.4 wt. % to 0.5 wt. %, or approximately 0.3 wt. % H 2  by weight of the second gas fraction  264 . 
     The second gas fraction  264  may include from 1 wt. % to 13 wt. %, from 1 wt. % to 10 wt. %, from 1 wt. % to 7 wt. %, from 1 wt. % to 5 wt. %, from 1 wt. % to 3 wt. %, from 1 wt. % to 2 wt. %, from 2 wt. % to 13 wt. %, from 2 wt. % to 10 wt. %, from 2 wt. % to 7 wt. %, from 2 wt. % to 5 wt. %, from 2 wt. % to 3 wt. %, from 3 wt. % to 13 wt. %, from 3 wt. % to 10 wt. %, from 3 wt. % to 7 wt. %, from 3 wt. % to 5 wt. %, from 5 wt. % to 13 wt. %, from 5 wt. % to 10 wt. %, from 5 wt. % to 7 wt. %, from 7 wt. % to 13 wt. %, from 7 wt. % to 10 wt. %, from 10 wt. % to 13 wt. %, or approximately 4 wt. % C 2 H 6  by weight of the second gas fraction  264 . 
     The second gas fraction  264  may include from 5 wt. % to 20 wt. %, from 5 wt. % to 18 wt. %, from 5 wt. % to 15 wt. %, from 5 wt. % to 13 wt. %, from 5 wt. % to 11 wt. %, from 5 wt. % to 8 wt. %, from 8 wt. % to 20 wt. %, from 8 wt. % to 18 wt. %, from 8 wt. % to 15 wt. %, from 8 wt. % to 13 wt. %, from 8 wt. % to 11 wt. %, from 11 wt. % to 20 wt. %, from 11 wt. % to 18 wt. %, from 11 wt. % to 15 wt. %, from 11 wt. % to 13 wt. %, from 13 wt. % to 20 wt. %, from 13 wt. % to 18 wt. %, from 13 wt. % to 15 wt. %, from 15 wt. % to 20 wt. %, from 15 wt. % to 18 wt. %, from 18 wt. % to 20 wt. %, or approximately 12 wt. % C 3 H 8  by weight of the second gas fraction  264 . 
     The second gas fraction  264  may include from 5 wt. % to 30 wt. %, from 5 wt. % to 23 wt. %, from 5 wt. % to 20 wt. %, from 5 wt. % to 18 wt. %, from 5 wt. % to 16 wt. %, from 5 wt. % to 14 wt. %, from 5 wt. % to 12 wt. %, from 5 wt. % to 10 wt. %, from 10 wt. % to 30 wt. %, from 10 wt. % to 23 wt. %, from 10 wt. % to 20 wt. %, from 10 wt. % to 18 wt. %, from 10 wt. % to 16 wt. %, from 10 wt. % to 14 wt. %, from 10 wt. % to 12 wt. %, from 12 wt. % to 30 wt. %, from 12 wt. % to 23 wt. %, from 12 wt. % to 20 wt. %, from 12 wt. % to 18 wt. %, from 12 wt. % to 16 wt. %, from 12 wt. % to 14 wt. %, from 14 wt. % to 30 wt. %, from 14 wt. % to 23 wt. %, from 14 wt. % to 20 wt. %, from 14 wt. % to 18 wt. %, from 14 wt. % to 16 wt. %, from 16 wt. % to 30 wt. %, from 16 wt. % to 23 wt. %, from 16 wt. % to 20 wt. %, from 16 wt. % to 18 wt. %, from 18 wt. % to 30 wt. %, from 18 wt. % to 23 wt. %, from 18 wt. % to 20 wt. %, from 20 wt. % to 30 wt. %, from 20 wt. % to 23 wt. %, from 23 wt. % to 30 wt. %, or approximately 15 wt. % C 4 H 10  by weight of the second gas fraction  264 . 
     The second gas fraction  264  may include from 1 wt. % to 20 wt. %, from 1 wt. % to 15 wt. %, from 1 wt. % to 10 wt. %, from 1 wt. % to 8 wt. %, from 1 wt. % to 6 wt. %, from 1 wt. % to 4 wt. %, from 1 wt. % to 2 wt. %, from 2 wt. % to 20 wt. %, from 2 wt. % to 15 wt. %, from 2 wt. % to 10 wt. %, from 2 wt. % to 8 wt. %, from 2 wt. % to 6 wt. %, from 2 wt. % to 4 wt. %, from 4 wt. % to 20 wt. %, from 4 wt. % to 15 wt. %, from 4 wt. % to 10 wt. %, from 4 wt. % to 8 wt. %, from 4 wt. % to 6 wt. %, from 6 wt. % to 20 wt. %, from 6 wt. % to 15 wt. %, from 6 wt. % to 10 wt. %, from 6 wt. % to 8 wt. %, from 8 wt. % to 20 wt. %, from 8 wt. % to 15 wt. %, from 8 wt. % to 10 wt. %, from 10 wt. % to 20 wt. %, from 10 wt. % to 15 wt. %, from 15 wt. % to 20 wt. %, or approximately 5 wt. % C 5 H 12  by weight of the second gas fraction  264 . 
     The second gas fraction  264  may include from 0.5 wt. % to 5 wt. %, from 0.5 wt. % to 3.5 wt. %, from 0.5 wt. % to 3.0 wt. %, from 0.5 wt. % to 2.5 wt. %, from 0.5 wt. % to 2.2 wt. %, from 0.5 wt. %, to 1.8 wt. %, from 0.5 wt. % to 1.5 wt. %, from 0.5 wt. % to 1.0 wt. %, from 1.0 wt. % to 5 wt. %, from 1.0 wt. % to 3.5 wt. %, from 1.0 wt. % to 3.0 wt. %, from 1.0 wt. % to 2.5 wt. %, from 1.0 wt. % to 2.2 wt. %, from 1.0 wt. %, to 1.8 wt. %, from 1.0 wt. % to 1.5 wt. %, from 1.5 wt. % to 5 wt. %, from 1.5 wt. % to 3.5 wt. %, from 1.5 wt. % to 3.0 wt. %, from 1.5 wt. % to 2.5 wt. %, from 1.5 wt. % to 2.2 wt. %, from 1.5 wt. %, to 1.8 wt. %, from 1.8 wt. % to 5 wt. %, from 1.8 wt. % to 3.5 wt. %, from 1.8 wt. % to 3.0 wt. %, from 1.8 wt. % to 2.5 wt. %, from 1.8 wt. % to 2.2 wt. %, from 2.2 wt. % to 5 wt. %, from 2.2 wt. % to 3.5 wt. %, from 2.2 wt. % to 3.0 wt. %, from 2.2 wt. % to 2.5 wt. %, from 2.5 wt. % to 5 wt. %, from 2.5 wt. % to 3.5 wt. %, from 2.5 wt. % to 3.0 wt. %, from 3.0 wt. % to 5 wt. %, from 3.0 to 3.5 wt. %, from 3.5 to 5 wt. %, or approximately 2 wt. % C 6 H 14  by weight of the second gas fraction  264 . 
     The second gas fraction  264  may include from 8 to 58 wt. %, from 8 to 50 wt. %, from 8 to 40 wt. %, from 8 to 30 wt. %, from 8 to 20 wt. %, from 8 to 15 wt. %, from 8 to 10 wt. %, from 10 to 58 wt. %, from 10 to 50 wt. %, from 10 to 40 wt. %, from 10 to 30 wt. %, from 10 to 20 wt. %, from 10 to 15 wt. %, from 15 to 58 wt. %, from 15 to 50 wt. %, from 15 to 40 wt. %, from 15 to 30 wt. %, from 15 to 20 wt. %, from 20 to 58 wt. %, from 20 to 50 wt. %, from 20 to 40 wt. %, from 20 to 30 wt. %, from 30 to 58 wt. %, from 30 to 50 wt. %, from 30 to 40 wt. %, from 40 to 58 wt. %, from 40 to 50 wt. %, from 50 to 58 wt. %, or approximately 35 wt. % H 2 S by weight of the second gas fraction  264 . 
     The second gas fraction  264  may include from 1 wt. % to 5 wt. %, from 1 wt. % to 4 wt. %, from 1 wt. % to 3.5 wt. %, from 2 wt. % to 5 wt. %, from 2 wt. % to 4 wt. %, from 2 wt. % to 3.5 wt. %, from 2.5 wt. % to 5 wt. %, from 2.5 wt. % to 4 wt. %, from 2.5 wt. % to 3.5 wt. %, or approximately 3 wt. % CH 3 SH by weight of the second gas fraction  264 . 
     The second gas fraction  264  may include from 0.5 wt. % to 4 wt. %, from 0.5 wt. % to 3 wt. %, from 0.5 wt. % to 2.5 wt. %, from 1 wt. % to 4 wt. %, from 1 wt. % to 3 wt. %, from 1 wt. % to 2.5 wt. %, from 1.5 wt. % to 4 wt. %, from 1.5 wt. % to 3 wt. %, from 1.5 wt. % to 2.5 wt. %, or approximately 2 wt. % C 2 H 5 SH by weight of the second gas fraction  264 . 
     The second gas fraction  264  may include from 0.25 wt. % to 2 wt. %, from 0.25 wt. % to 1.5 wt. %, from 0.25 wt. % to 1.25 wt. %, from 0.5 wt. % to 2 wt. %, from 0.5 wt. % to 1.5 wt. %, from 0.5 wt. % to 1.25 wt. %, from 0.75 wt. % to 2 wt. %, from 0.75 wt. % to 1.5 wt. %, from 0.75 wt. % to 1.25 wt. %, or approximately 1 wt. % C 4 H 9 SH by weight of the second gas fraction  264 . 
     The second gas fraction  264  may include from 0.25 wt. % to 2 wt. %, from 0.25 wt. % to 1.5 wt. %, from 0.25 wt. % to 1.25 wt. %, from 0.5 wt. % to 2 wt. %, from 0.5 wt. % to 1.5 wt. %, from 0.5 wt. % to 1.25 wt. %, from 0.75 wt. % to 2 wt. %, from 0.75 wt. % to 1.5 wt. %, from 0.75 wt. % to 1.25 wt. %, or approximately 1 wt. % C 5 H 11 SH by weight of the second gas fraction  264 . 
     The second gas fraction  264  may include from 1 wt. % to 5 wt. %, from 1 wt. % to 4 wt. %, from 1 wt. % to 3.5 wt. %, from 2 wt. % to 5 wt. %, from 2 wt. % to 4 wt. %, from 2 wt. % to 3.5 wt. %, from 2.5 wt. % to 5 wt. %, from 2.5 wt. % to 4 wt. %, from 2.5 wt. % to 3.5 wt. %, or approximately 3 wt. % C 2 H 6 S 2  by weight of the second gas fraction  264 . 
     The second gas fraction  264  may include from 1 wt. % to 10 wt. %, from 1 wt. % to 8 wt. %, from 1 wt. % to 7 wt. %, from 3 wt. % to 10 wt. %, from 3 wt. % to 8 wt. %, from 3 wt. % to 7 wt. %, from 5 wt. % to 10 wt. %, from 5 wt. % to 8 wt. %, from 5 wt. % to 7 wt. %, or approximately 6 wt. % C 3 H 8 S 2  by weight of the second gas fraction  264 . 
     The second gas fraction  264  may include from 1 wt. % to 10 wt. %, from 1 wt. % to 8 wt. %, from 1 wt. % to 7 wt. %, from 3 wt. % to 10 wt. %, from 3 wt. % to 8 wt. %, from 3 wt. % to 7 wt. %, from 5 wt. % to 10 wt. %, from 5 wt. % to 8 wt. %, from 5 wt. % to 7 wt. %, or approximately 6 wt. % C 4 H 10 S 2  by weight of the second gas fraction  264 . 
     The second gas fraction  264  may include from 1 wt. % to 5 wt. %, from 1 wt. % to 4 wt. %, from 1 wt. % to 3.5 wt. %, from 2 wt. % to 5 wt. %, from 2 wt. % to 4 wt. %, from 2 wt. % to 3.5 wt. %, from 2.5 wt. % to 5 wt. %, from 2.5 wt. % to 4 wt. %, from 2.5 wt. % to 3.5 wt. %, or approximately 3 wt. % C 5 H 12 S 2  by weight of the second gas fraction  264 . 
     The second gas fraction  264  may include from 0.25 wt. % to 2 wt. %, from 0.25 wt. % to 1.5 wt. %, from 0.25 wt. % to 1.25 wt. %, from 0.5 wt. % to 2 wt. %, from 0.5 wt. % to 1.5 wt. %, from 0.5 wt. % to 1.25 wt. %, from 0.75 wt. % to 2 wt. %, from 0.75 wt. % to 1.5 wt. %, from 0.75 wt. % to 1.25 wt. %, or approximately 1 wt. % C 6 H 14 S 2  by weight of the second gas fraction  264 . 
     In embodiments, the second gas fraction  264  may have a similar composition to liquefied petroleum gas (LPG), due to the presence of butane and propane. In embodiments, the second gas fraction  264  may have a composition similar to LPG+, meaning that the second gas fraction  264  includes components present in LPG (butane and propane) along with additional liquid components, such as a pentane and hexane. Therefore, the process  200  as shown in  FIG. 2  may be used to convert hazardous waste, such as disulfide oil, into desirable products, such as Hz, C 2  to C 6  hydrocarbons, H 2 S, or combinations thereof. 
     EXAMPLES 
     Example 1 
     An example process for upgrading a hydrocarbon-based composition  105  according to embodiments described herein was run. The hydrocarbon-based composition  105  had the properties shown in Table 2. 
     
       
         
           
               
             
               
                 TABLE 2 
               
             
            
               
                   
               
               
                 Properties of Feed and Product 
               
            
           
           
               
               
               
               
            
               
                   
                 Hydro 
                   
                   
               
               
                   
                 carbon- 
                   
                 Liquid 
               
               
                   
                 based 
                 Upgraded 
                 Oil  
               
               
                   
                 composition 
                 Product 
                 Fraction 
               
               
                 Properties 
                 (105) 
                 (152) 
                 (162) 
               
               
                   
               
            
           
           
               
               
               
               
            
               
                 Mass Flow (kg/hr) 
                 49 
                 48.1 
                 45.6 
               
               
                 API° 
                 11 
                 19.8 
                 24 
               
               
                 Hydrogen Flow (kg/hr) 
                 0.4 
                 0.0 
                 0.0 
               
            
           
           
               
               
               
               
               
            
               
                 Distillation (TBP) 
                  5% 
                 367 
                 297 
                 256 
               
               
                   
                 10% 
                 395 
                 337 
                 300 
               
               
                   
                 30% 
                 465 
                 420 
                 374 
               
               
                   
                 50% 
                 526 
                 464 
                 415 
               
               
                   
                 70% 
                 587 
                 519 
                 461 
               
               
                   
                 90% 
                 647 
                 592 
                 538 
               
               
                   
                 95% 
                 671 
                 632 
                 568 
               
            
           
           
               
               
               
               
            
               
                 Total Sulfur Content 
                 3.4 
                 2.7 
                 1.7 
               
               
                 (wt. %) 
                   
                   
                   
               
               
                 Total Nitrogen Content 
                 1.2 
                 0.9 
                 0.3 
               
               
                 (wt. %) 
                   
                   
                   
               
               
                 Viscosity (cSt) at 50° C. 
                 640 
                 89 
                 27 
               
               
                 Asphaltene (Heptane- 
                   
                   
                   
               
               
                 insoluble) (wt. %) 
                 4.8 
                 1.7 
                 0.3 
               
               
                 Metals (V and Ni) (wtppm) 
                 83 
                 9 
                 4 
               
               
                 Water (wt. %) 
                 0 
                 0.2 
                 0 
               
               
                   
               
               
                 kg/hr 
               
               
                 Sulfur in Feed = 1.7 
               
               
                 Nitrogen in Feed = 0.6 
               
               
                 Sulfur in Liquid Product = 0.8 
               
               
                 Nitrogen in Liquid Product = 0.1 
               
            
           
         
       
     
     A water stream  110  included demineralized water having a conductivity of less than 0.1 μS/cm 2 . The hydrocarbon-based composition  105 , the water stream  110 , and a hydrogen stream  127  were fed at rates of 50 L/hr, 100 L/hr, and 157 ft 3 /hr, respectively, at a process pressure of 3,600 psig. 
     As shown in  FIG. 1 , the hydrocarbon-based composition  105  and the water stream  110  are fed to pumps  112  and  114 , respectively, to increase their pressure to 3600 psig. The pressurized hydrocarbon-based composition  116 , pressurized water stream  118 , and hydrogen stream  127  are heated to about 350° C. by heaters  120 ,  122 , and  128 , respectively. The pressurized, heated hydrocarbon-based composition  124 , the heated water stream  126 , and the heated hydrogen stream  129  exiting the heaters were routed to a static mixer  130 , where the hydrogen, oil, and water are mixed vigorously to generate combined feed stream  132 . The combined feed stream  132  is then routed to the supercritical water hydrogenation reactor  150  that is configured to upgrade the combined feed stream  132  that is maintained at 440° C. and 3600 psig. The upgraded product  152  having the properties shown in Table 2 was routed to cooler  154  to form a cooled, upgraded product  156 . The cooled, upgraded product  156  was depressurized by valve  158  to reduce the mixture pressure to 1 atm to form a depressurized, upgraded product  159 . The depressurized, upgraded product  159  was then sent to a gas/oil/water separator  160  to separate the depressurized, upgraded product  159  into a first gas fraction  164 , a liquid oil fraction  162 , and a first water fraction  166 . The liquid oil fraction  162  had the properties shown in Table 2. The liquid oil fraction  162  was then collected in an oil storage tank  163 . The composition of the first gas fraction  164  is shown in Table 3: 
     
       
         
           
               
             
               
                 TABLE 3 
               
             
            
               
                   
               
               
                 First Gas Fraction 164 
               
               
                 First Gas Fraction 164 
               
            
           
           
               
               
               
               
            
               
                   
                 Concentration 
                 MW 
                   
               
            
           
           
               
               
               
               
               
            
               
                 Species 
                 (wt. %) 
                 (kg/kmol) 
                 kg/hr 
                 kmol/hr 
               
               
                   
               
            
           
           
               
               
               
               
               
            
               
                 H 2   
                 1.0 
                 2.0 
                 0.04 
                 0.02 
               
               
                 CH 4   
                 11.9 
                 16.0 
                 0.45 
                 0.03 
               
               
                 C 2 H 6   
                 10.9 
                 30.1 
                 0.41 
                 0.01 
               
               
                 C 3 H 8   
                 10.0 
                 44.1 
                 0.38 
                 0.01 
               
               
                 C 4 H 10   
                 9.0 
                 58.1 
                 0.34 
                 0.01 
               
               
                 C 5 H 12   
                 7.0 
                 72.2 
                 0.26 
                 0.00 
               
               
                 C 6 H 14   
                 4.0 
                 86.2 
                 0.15 
                 0.00 
               
               
                 CO 
                 2.0 
                 28.0 
                 0.08 
                 0.00 
               
               
                 CO 2   
                 4.0 
                 44.0 
                 0.15 
                 0.00 
               
               
                 H 2 S 
                 25.6 
                 34.1 
                 0.97 
                 0.03 
               
               
                 NH 3   
                 14.6 
                 17.0 
                 0.55 
                 0.03 
               
               
                   
               
               
                 kg/hr 
               
               
                 Sulfur in Gas Product = 0.9 
               
               
                 Nitrogen in Gas Product = 0.5 
               
            
           
         
       
     
     Example 2 
     An example process for treating disulfide oil according to embodiments described herein was run. A disulfide oil stream of 180 kg/hr exiting LPG Merox is hydrotreated in supercritical water to remove the sulfur in the form of H 2 S. The disulfide oil composition  205  had the composition shown in Table 4: 
     
       
         
           
               
             
               
                 TABLE 4 
               
             
            
               
                   
               
               
                 Disulfide Oil Composition 205 
               
            
           
           
               
               
               
               
               
            
               
                   
                 Concentration  
                   
                 MW  
                   
               
               
                 Species 
                 (wt. %) 
                 kg/hr 
                 (kg/kmol) 
                 kmol/hr 
               
               
                   
               
            
           
           
               
               
               
               
               
            
               
                 C 2 H 6 S 2   
                 14 
                 23 
                 94 
                 0.24 
               
               
                 C 3 H 8 S 2   
                 24 
                 39 
                 108 
                 0.36 
               
               
                 C 4 H 10 S 2   
                 27 
                 44 
                 122 
                 0.36 
               
               
                 C 5 H 12 S 2   
                 15 
                 24 
                 136 
                 0.18 
               
               
                 C 6 H 14 S 2   
                 5 
                 8 
                 150 
                 0.05 
               
               
                 NaOH + water 
                 15 
                 24 
                   
                   
               
               
                 Total 
                 100 
                 162 
                   
                   
               
            
           
           
               
               
               
               
            
               
                 Total Feed  
                   
                   
                   
               
               
                 (Excluding NaOH + water) (kg/hr) = 
                 139 
               
               
                   
               
            
           
         
       
     
     The disulfide oil composition  205  included 2.4 kilomoles per hour (kmol/hr) of sulfur. The flow rate of the total feed excluding NaOH and water was 139 kilograms per hour (kg/hr). The water stream  110  was demineralized water having a conductivity lower than 0.1 μS/cm 2 . The disulfide oil composition  205  and the water stream  110  were fed to pumps  212  and  114 , respectively, to increase their pressure to a pressure of 3600 psi to form pressurized disulfide composition  216  and pressurized water stream  118 , respectively. The pressurized disulfide oil composition  216 , the pressurized water stream  118 , and the hydrogen stream  127  were fed to the process at rates of 162 kg/hr, 360 L/hr, and 500 ft 3 /hr, respectively. The pressurized disulfide oil composition  216 , the pressurized water stream  118 , and the hydrogen stream  127  were preheated by heaters  220 ,  122 , and  128 , respectively, to a temperature of 180° C., to form pressurized, heated disulfide oil composition  224 , heated water stream  126 , and heated hydrogen stream  129 . The heated water stream  126 , the heated hydrogen stream  129 , and the pressurized, heated disulfide oil composition  224  were then mixed in a static mixer  130  to produce a combined disulfide feed stream  232 . The combined disulfide feed stream  232  was then introduced to the supercritical water hydrogenation reactor  150 . The disulfide oil was then hydrotreated in the supercritical water hydrogenation reactor  150  at 450° C. and 3600 psig (24.8 MPa) to form upgraded disulfide product  252 . Upon exiting the supercritical water hydrogenation reactor  150 , the upgraded disulfide product  252  was cooled by water cooler  154  to 35° C. to form cooled, upgraded disulfide product  256 . The cooled, upgraded disulfide product  256  was then depressurized to 1 atm by back pressure regulator valve  158  to form depressurized, upgraded disulfide product  259 . The depressurized, upgraded disulfide product  259  was then sent to the gas/water separator  160  to separate the depressurized, upgraded disulfide product  259  into the second water fraction  266  and the second gas fraction  264 . The gas/water separator  160  was operated at 1 atmosphere and a maximum of 90° C. The percent conversion of disulfide oil was 80%. The second gas fraction  264  collected in the gas storage tank  165  was a mixture of light paraffins, thiols, un-converted disulfide oil and hydrogen, and hydrogen sulfide. The composition of the second gas fraction  264  is shown in Table 5: 
     
       
         
           
               
             
               
                 TABLE 5 
               
             
            
               
                   
               
               
                 Properties of the second gas fraction 264 
               
            
           
           
               
               
            
               
                 Second gas fraction 264 
                 Sulfur in 
               
            
           
           
               
               
               
               
               
               
            
               
                   
                 Concentration 
                   
                 MW 
                   
                 Product 
               
               
                 Species 
                 (wt. %) 
                 kg/hr 
                 (kg/kmol) 
                 kmol/hr 
                 kmol/hr 
               
               
                   
               
            
           
           
               
               
               
               
               
               
            
               
                 H 2   
                 0.3 
                 0.3 
                 2 
                 0.17 
                 0.6 
               
               
                 C 2 H 6   
                 4 
                 4.5 
                 30 
                 0.15 
                   
               
               
                 C 3 H 8   
                 12 
                 13.4 
                 44 
                 0.30 
                   
               
               
                 C 4 H 10   
                 15 
                 16.7 
                 58 
                 0.29 
                   
               
               
                 C 5 H 12   
                 5 
                 5.6 
                 72 
                 0.08 
                   
               
               
                 C 6 H 14   
                 2 
                 2.2 
                 86 
                 0.03 
                   
               
               
                 CH 3 SH 
                 3 
                 3.3 
                 48 
                 0.07 
                   
               
               
                 C 2 H 5 SH 
                 2 
                 2.2 
                 62 
                 0.04 
                   
               
               
                 C 4 H 9 SH 
                 1 
                 1.1 
                 90 
                 0.01 
                   
               
               
                 C 5 H 11 SH 
                 1 
                 1.1 
                 104 
                 0.01 
                   
               
               
                 H 2 S 
                 35 
                 60.6 
                 34 
                 1.78 
                   
               
               
                 C 2 H 6 S 2   
                 3 
                 4.5 
                 94 
                 0.05 
                   
               
               
                 C 3 H 8 S 2   
                 6 
                 7.8 
                 108 
                 0.07 
                   
               
               
                 C 4 H 10 S 2   
                 6 
                 8.8 
                 122 
                 0.07 
                   
               
               
                 C 5 H 12 S 2   
                 3 
                 4.9 
                 136 
                 0.04 
                   
               
               
                 C 6 H 14 S 2   
                 1 
                 1.6 
                 150 
                 0.01 
                   
               
            
           
           
               
               
               
               
               
            
               
                 Total 
                 100 
                 139 
                 Total Sulfur Out (kg/hr) = 
                 76 
               
               
                   
               
            
           
         
       
     
     It should be apparent to those skilled in the art that various modifications and variations may be made to the embodiments described within without departing from the spirit and scope of the claimed subject matter. Thus, it is intended that the specification cover the modifications and variations of the various embodiments described within provided such modifications and variations come within the scope of the appended claims and their equivalents. 
     As used throughout the disclosure, the singular forms “a,” “an” and “the” include plural referents unless the context clearly dictates otherwise. Thus, for example, reference to “a” component includes aspects having two or more such components, unless the context clearly indicates otherwise. 
     Having described the subject matter of the present disclosure in detail and by reference to specific embodiments thereof, it is noted that the various details disclosed within should not be taken to imply that these details relate to elements that are essential components of the various embodiments described within, even in cases where a particular element is illustrated in each of the drawings that accompany the present description. Further, it should be apparent that modifications and variations are possible without departing from the scope of the present disclosure, including, but not limited to, embodiments defined in the appended claims. More specifically, although some aspects of the present disclosure are identified as particularly advantageous, it is contemplated that the present disclosure is not necessarily limited to these aspects.