US20080099374A1 - Reactor and process for upgrading heavy hydrocarbon oils - Google Patents
Reactor and process for upgrading heavy hydrocarbon oils Download PDFInfo
- Publication number
- US20080099374A1 US20080099374A1 US11/555,211 US55521106A US2008099374A1 US 20080099374 A1 US20080099374 A1 US 20080099374A1 US 55521106 A US55521106 A US 55521106A US 2008099374 A1 US2008099374 A1 US 2008099374A1
- Authority
- US
- United States
- Prior art keywords
- water
- reaction zone
- reactor
- hydrocarbon
- reaction
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Abandoned
Links
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G31/00—Refining of hydrocarbon oils, in the absence of hydrogen, by methods not otherwise provided for
- C10G31/08—Refining of hydrocarbon oils, in the absence of hydrogen, by methods not otherwise provided for by treating with water
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J3/00—Processes of utilising sub-atmospheric or super-atmospheric pressure to effect chemical or physical change of matter; Apparatus therefor
- B01J3/008—Processes carried out under supercritical conditions
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J4/00—Feed or outlet devices; Feed or outlet control devices
- B01J4/001—Feed or outlet devices as such, e.g. feeding tubes
- B01J4/002—Nozzle-type elements
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/54—Improvements relating to the production of bulk chemicals using solvents, e.g. supercritical solvents or ionic liquids
Definitions
- the present invention relates to upgrading of hydrocarbons, especially heavy hydrocarbons such as whole heavy oil, bitumen, and the like using supercritical water.
- Oil produced from a significant number of oil reserves around the world is simply too heavy to flow under ambient conditions. This makes it challenging to bring remote, heavy oil resources closer to the markets.
- One typical example is the Hamaca field in Venezuela.
- the diluent may be naphtha, or any other stream with a significantly higher API gravity (i.e., much lower density) than the heavy oil.
- diluted crude oil is sent from the production wellhead via pipeline to an upgrading facility.
- Two key operations occur at the upgrading facility: (1) the diluent stream is recovered and recycled back to the production wellhead in a separate pipeline, and (2) the heavy oil is upgraded with suitable technology known in the art (coking, hydrocracking, hydrotreating, etc.) to produce higher-value products for market.
- suitable technology known in the art (coking, hydrocracking, hydrotreating, etc.) to produce higher-value products for market.
- Some typical characteristics of these higher-value products include lower sulfur content, lower metals content, lower total acid number (TAN), lower residuum content, higher API gravity, and lower viscosity.
- Most of these desirable characteristics are achieved by reacting the heavy oil with hydrogen gas at high temperatures and pressures in the presence of a catalyst.
- the upgraded crude is sent further to the end-users via tankers.
- Hydrogen-addition processes such as hydrotreating or hydrocracking require significant investments in capital and infrastructure.
- Hydrogen-addition processes also have high operating costs, since hydrogen production costs are highly sensitive to natural gas prices. Some remote heavy oil reserves may not even have access to sufficient quantities of low-cost: natural gas to support a hydrogen plant. These hydrogen-addition processes also generally require expensive catalysts and resource intensive catalyst handling techniques, including catalyst regeneration.
- the refineries and/or upgrading facilities that are located closest to the production site may have neither the capacity nor the facilities to accept the heavy oil.
- Coking is often used at refineries or upgrading facilities. Significant amounts of by-product solid coke are rejected during the coking process, leading to lower liquid hydrocarbon yield. In addition, the liquid products from a coking plant often need further hydrotreating. Further, the volume of the product from the coking process is significantly less than the volume of the feed crude oil.
- a process according to the present invention overcomes these disadvantages by using supercritical water to upgrade a heavy hydrocarbon feedstock into an upgraded hydrocarbon product or syncrude with highly desirable properties (low sulfur content, low metals content, lower density (higher API), lower viscosity, lower residuum content, etc.).
- the process neither requires external supply of hydrogen nor must it use catalysts. Further, the process in the present invention does not produce an appreciable coke by-product.
- advantages that may be obtained by the practice of the present invention include a high liquid hydrocarbon yield; no need for externally-supplied hydrogen; no need to provide catalyst; significant increases in API gravity in the upgraded hydrocarbon product; significant viscosity reduction in the upgraded hydrocarbon product; and significant reduction in sulfur, metals, nitrogen, TAN, and MCR (micro-carbon residue) in the upgraded hydrocarbon product.
- U.S. Pat. No. 4,840,725 discloses a process for conversion of high boiling liquid organic materials to lower boiling materials using supercritical water in a tubular continuous reactor.
- the water and hydrocarbon are separately preheated and mixed in a high-pressure feed pump just before being fed to the reactor.
- U.S. Pat. No. 5,914,031 discloses a three zone reactor design so that the reactant activity, reactant solubility and phase separation of products can be optimized separately by controlling temperature and pressure. However, all the examples given in the patent were obtained using batch operation.
- U.S. Pat. No. 6,887,369 discloses a supercritical water pretreatment process using hydrogen or carbon monoxide preferably carried out in a deep well reactor to hydrotreat and hydrocrack carbonaceous material.
- the deep well reactor is adapted from underground oil wells, and consists of multiple, concentric tubes.
- the deep well reactor described in the patent is operated by introducing feed streams in the core tubes and returning reactor effluent in the outer annular section.
- heavy oil upgrading using supercritical water may be considered similar in some respects to waste treatment using supercritical water, and can be implemented using various elements of reactors designed for waste treatment, there are significant differences in requirement for reactor design for heavy hydrocarbon upgrading from that for waste treatment. Specifically, the following are among the many issues to be addressed in designing a reactor in which to conduct an effective process for heavy oil upgrading using supercritical water:
- the present invention relates to an apparatus for upgrading a hydrocarbon by reaction with a fluid comprising water under supercritical water conditions comprising; means for dispersing and mixing the fluid comprising water and the hydrocarbon under conditions which disfavor thermal cracking and formation of coke; means for injecting a dispersed water-hydrocarbon mixture into a reaction zone under supercritical water conditions; a reaction zone having means for maintaining a uniform temperature within said reaction zone, means for controlling the residence time in the reaction zone within determined limits and means for avoiding the settling of inorganic solids within the reaction zone; and means for recovering an upgraded hydrocarbon.
- FIG. 1 is a process flow diagram of one embodiment of a process employing an apparatus of the present invention.
- FIG. 2 is a process flow diagram of another embodiment of a process employing an apparatus of the present invention.
- FIG. 3 is a process flow diagram of another embodiment of a process employing an apparatus of the present invention.
- FIG. 4 is a process flow diagram of another embodiment of a process employing an apparatus of the present invention.
- FIG. 5 is a process flow diagram of another embodiment of a process employing an apparatus of the present invention.
- Water and hydrocarbons, preferably heavy hydrocarbons are the two reactants employed in a process according to the present invention.
- Any hydrocarbon can be suitably upgraded by a process according to the present invention.
- the preferred heavy hydrocarbons are heavy crude oil, heavy hydrocarbons extracted from tar sands, commonly called tar sand bitumen, such as Athabasca tar sand bitumen obtained from Canada, heavy petroleum crude oils such as Venezuelan Orinoco heavy oil belt crudes Boscan heavy oil, heavy hydrocarbon fractions obtained from crude petroleum oils particularly heavy vacuum gas oils, vacuum residuum as well as petroleum tar, tar sands and coal tar.
- Other examples of heavy hydrocarbon feedstocks which can be used are oil shale, shale oil, and asphaltenes.
- Sources of water include but are not limited to drinking water, treated or untreated wastewater, river water, lake water, seawater, produced water or the like.
- the heavy hydrocarbon feed and a fluid comprising water that has been heated to a temperature higher than its critical temperature are contacted in a mixing zone prior to entering the reaction zone.
- mixing may be accomplished in many ways and is preferably accomplished by a technique that does not employ mechanical moving parts. Such means of mixing may include, but are not limited to, use of static mixers, spray nozzles, sonic or ultrasonic agitation, or thermal siphons.
- the oil and water should be heated and mixed so that the combined stream will reach supercritical conditions in the reaction zone.
- One aspect of this invention is to employ a heating sequence so that the temperature and pressure of the hydrocarbons and water will reach supercritical reaction conditions in a controlled manner. This will avoid excessive local heating of oil, which will lead to solid formation and lower quality product.
- the oil should only be heated up with sufficient amount of water present and around the hydrocarbon molecules. This requirement can be met by mixing oil with water before heating.
- water is heated to a temperature higher than its critical temperature, and then mixed with oil.
- the temperature of heavy oil feed should be kept in the range of about 100° C. to 200° C. to avoid thermal cracking but still high enough to maintain a reasonable pressure drop.
- the water stream temperature should be high enough to make sure that after mixing with oil, the temperature of the oil-water mixture is still higher than the water supercritical temperature.
- the oil is actually heated up by water. An abundance of water molecules surrounding the hydrocarbon molecules will significantly suppress condensation reactions and therefore reduce formation of coke and solid product.
- the required temperature of the supercritical water stream, T SCW can be estimated based on reaction temperature, T R , and water to oil ratio. Since the heat capacity of water changes significantly in the range near its critical conditions, for a given reaction temperature, the required temperature for the supercritical water stream increases almost exponentially with decreasing water-to-oil ratio. The lower the water-to-oil ratio, the higher the T SCW . The relationship, however, is very nonlinear since higher T SCW leads to a lower heat capacity (far away from the critical point).
- water is heated up to supercritical conditions. Then the supercritical water mixed with heavy oil feed in a mixer.
- the temperature of heavy oil feed should be kept in the range of about 100° C. to 200° C. to avoid thermal cracking but still high enough to maintain reasonable pressure drop.
- the temperature of the water-oil mixture would be lower than critical temperature of water; therefore a second heater is needed to raise the temperature of the mixture stream to above the critical temperature of water.
- the heavy oil is first partially heated up by water, and then the water-oil mixture is heated to supercritical conditions by the second heater.
- reaction zone in which they are allowed to react under temperature and pressure conditions of supercritical water, i.e. supercritical water conditions, in the absence of externally added hydrogen, for a residence time sufficient to allow upgrading reactions to occur.
- the reaction is preferably allowed to occur in the absence of externally added catalysts or promoters, although the use of such catalysts and promoters is permissible in accordance with the present invention.
- Hydrogen as used herein in the phrase, “in the absence of externally added hydrogen” means hydrogen gas. This phrase is not intended to exclude all sources of hydrogen that are available as reactants. Other molecules such as saturated hydrocarbons may act as a hydrogen source during the reaction by donating hydrogen to other unsaturated hydrocarbons. In addition, H 2 may be formed in-situ during the reaction through steam reforming of hydrocarbons and water-gas-shift reaction.
- the reaction zone preferably comprises a reactor, which is equipped with a means for collecting the reaction products (syncrude, water, and gases), and a section, preferably at the bottom, where any metals or solids (the “dreg stream”) may accumulate.
- Supercritical water conditions include a temperature from 374° C. (the critical temperature of water) to 1000° C., preferably from 374° C. to 600° C. and most preferably from 374° C. to 400° C., a pressure from 3,205 (the critical pressure of water) to 10,000 psia, preferably from 3,205 psia to 7,200 psia and most preferably from 3,205 to 4,000 psia, an oil/water volume ratio from 1:0.1 to 1:10, preferably from 1:0.5 to 1:3 and most preferably about 1:1 to 1:2.
- the reactants are allowed to react under these conditions for a sufficient time to allow upgrading reactions to occur.
- the residence time will be selected to allow the upgrading reactions to occur selectively and to the fullest extent without having undesirable side reactions of coking or residue formation.
- Reactor residence times may be from 1 minute to 6 hours, preferably from 8 minutes to 2 hours and most preferably from 20 to 40 minutes.
- a reactor designed for heavy oil upgrading using supercritical water in accordance with the present invention will preferably include the following features:
- the reactor will have means for adequate oil-water mixing and dispersion. Contrary to the conventional thermal cracking in an uncontrolled fashion that will lead to excessive formation of light hydrocarbon and therefore lower liquid hydrocarbon yield at the temperature and pressure under supercritical water conditions, heavy hydrocarbons will hydrothermally crack into lighter components. Furthermore, hydrocarbon radicals formed from thermal cracking will also recombine and polymerize and eventually become coke. Water molecules, especially under supercritical conditions, can quench and stabilize hydrocarbon radicals and therefore prevent them from over cracking and polymerization. To avoid over cracking into light hydrocarbons and coke formation, the heavy hydrocarbon molecules are preferably surrounded by water molecules to the greatest practical extent. Therefore, the reactor includes means to assure adequate mixing of oil with water for the purpose of achieving a high yield of liquid hydrocarbons.
- Such means should be chosen so as to be able to handle heavy oil feed which has low API gravity and high viscosity at high oil to water ratio.
- such means can include, among others (a) nozzles; (b) static mixer; (c) stirring vessel; (d) micro-channel device; and sonic and ultrasonic device.
- reaction zone in accordance with the present invention will preferably:
- the present invention also employs a separation zone for product recovery.
- the effluent stream from the reaction zone contains liquid hydrocarbon product, gas, water under supercritical conditions and solids.
- the liquid hydrocarbons are generally separated from other components to achieve high yield.
- the preferred way is to remove the solid first, and then bring the fluid phase containing hydrocarbon products, supercritical water and gas byproducts out of supercritical condition by lowing temperature, pressure or both so that hydrocarbon product and water will condense into liquid phase.
- the solids are primarily inorganic materials formed during the reactions and can be separated from the supercritical fluid phase using separation techniques known in the art, which could be a disengaging zone in the reactor or a separate device such as settling vessel, filter, cyclone etc.
- Another option for separating the solids is to bring the product stream out of supercritical regime by lowing temperature or pressure or both. Then the solid will precipitate.
- a potential disadvantage of this option is that some of the inorganic components in the solid may dissolve in water, which may contaminate the liquid hydrocarbon product. It should be noted that depending on the specific applications, a reactor for heavy oil upgrading using supercritical water in accordance with the present invention may have more than one of each of the three components listed above.
- FIG. 1 shows an embodiment of the present invention, which has been used in a laboratory.
- An inline mixer is used for mixing heavy oil with water.
- it is a static mixer.
- the reaction zone comprises a spiral tube reactor with large length to diameter ratio to attain high velocity inside the reactor, which is helpful to maintain oil-water dispersion.
- This design also makes the fluid flow inside the reactor close to plug flow and therefore achieves narrow residence time distribution for selective conversion to desired liquid hydrocarbons. Inorganic solids in the feed and formed during the reaction will not dissolve in supercritical water. High velocity inside the reactor also prevents settling of those inorganic solids.
- the small diameter of the reactor body also provides large specific surface area for heat transfer to maintain uniform temperature distribution inside the reactor.
- the length of the reactor can be designed based on residence time needed for specific conversion.
- a second vessel is added to settle the solids.
- the temperature and pressure is maintained at the same values as those in the spiral tube so that the fluid in the second vessel is still at supercritical water conditions. Due to the larger cross-sectional area of the second vessel the fluid velocity is much lower.
- inorganic materials separated from the fluid will settle down in the vessel, and can be removed from the system.
- the fluid containing hydrocarbon products, supercritical water and gas byproducts is cooled while maintaining at the same pressure as in the reactor, and hydrocarbon products and water are condensed in the high pressure separator.
- a spiral tube with a high length to diameter ratio which may be from 50 to 10,000, preferably from 100 to 4,000 may be used as reactor body.
- Use of such a reactor has the advantages of high velocity, narrow residence time distribution, and large surface for heat transfer.
- the length to diameter ratio is a useful parameter to determine preferred reactor configurations.
- the diameter may be determined by velocity needed to avoid solids precipitation and then the length can be selected to provide the desired residence time.
- Other reactor configurations known to those in the art can be used to achieve similar effects such as a serpentine reactor.
- the separation zone for removing solid and recovering hydrocarbon products is a vessel with a dip tube.
- Other fluid solid separation devices known in the art can be used to achieve the separation effect, which includes, but not limited to, cyclone, filter, ceramic membrane, settling tank, etc.
- the mixer, reaction and separation zones are separated.
- Such arrangement is convenient for laboratory research, and is used as an illustrative example. It is within the scope of the present invention and in some applications will be beneficial to integrate these three functions into one vessel.
- the reactor may include more than one piece of each function devices.
- FIG. 2 shows an example.
- heavy hydrocarbon molecules are preferably surrounded by sufficient water molecules.
- high water to oil ratio will be helpful to maintain the desired environment.
- high water to oil ratio also means high equipment and operating cost.
- the embodiment shown in FIG. 2 can achieve high water to oil ratio locally without increasing overall water to feed ratio. Instead of mixing all the feed oil with water at reactor inlet, this embodiment uses multiple injections of oil to maintain a desired water to oil ratio. Such a design is also helpful to control reaction temperature. By distributing feed oil more uniformly through the reactor length, reaction temperature will not increase too much due to the exothermic nature of the reactions.
- FIG. 2 Only two injections were shown in FIG. 2 This is not intended as a limitation. A reactor with multiple injections may also be used. In addition, one or more settling vessels can be added to a reactor with a multiple injection configuration to achieve solid separation under supercritical conditions.
- FIG. 3 shows yet another embodiment with more than one mixing and reaction zones.
- a second mixer which may or may not be the same as the first mixer, is added between reaction zone to enhance the oil/supercritical water mixing. Again, multiple mixers and reaction zones can be used.
- the upgrading reaction is exothermic.
- a reactor with a large surface area helps to maintain uniform temperature distribution inside the reactor.
- heat exchange through the surface area provided by the reactor may or may not be enough. Water can be used to quench the reaction stream and thereby control the reaction temperature.
- FIG. 4 shows an embodiment of using water to quench the reaction stream between two reaction zones.
- the amount of water used for quenching should be enough to bring down the reaction temperature while the reaction stream after quenching still maintain supercritical conditions. Multiple reaction zones and water quenching may be necessary for some feeds.
- the quenching water can also be used to for product recovery, as shown in FIG. 5 .
- the product stream is quenched by liquid water.
- the solid will be washed out by the water, and: due to the temperature reduction caused by quenching water and the hydrocarbons will condense as liquid.
- a single phase reaction product is withdrawn from the reaction zone, cooled, and separated into gas, effluent water, and upgraded hydrocarbon phases.
- This separation is preferably done by cooling the stream and using ones or more two-phase separators, three-phase separators or other gas-oil-water separation device known in the art.
- any method of separation can be used in accordance with the invention.
- composition of gaseous product obtained by treatment of the heavy hydrocarbons in accordance with the process of the present invention will depend on feed properties and typically comprises light hydrocarbons, water vapor, acid gas (CO 2 and H 2 S), methane and hydrogen.
- the effluent water may be used, reused or discarded. It may be recycled to e.g. the feed water tank, the feed water treatment system or to the reaction zone.
- the upgraded hydrocarbon product which is sometimes referred to as “syncrude” herein may be upgraded further or processed into other hydrocarbon products using methods that are known in the hydrocarbon processing art.
- the process of the present invention may be carried out either as a continuous or semi-continuous process or a batch process or as a continuous process.
- the entire system operates with a feed stream of oil and a separate feed stream of supercritical water and reaches a steady state; whereby all the flow rates, temperatures, pressures, and composition of the inlet, outlet and recycle streams do not vary appreciably with time.
- the exact pathway may depend on the reactor operating conditions (temperature, pressure, O/W volume ratio), reactor design (mode of contact/mixing, sequence of heating), and the hydrocarbon feedstock.
- Oil and supercritical water are contacted in a mixer prior to entering the reactor.
- the reactor is equipped with air inner tube for collecting the products (syncrude, excess water, and gas), and a bottom section where any metals or solids comprising a “dreg stream” of indeterminate properties or composition may accumulate.
- the shell-side of the reactor is kept isothermal during the reaction with a clamshell furnace and temperature controller.
- Preferred reactor residence times are 20-40 minutes, with preferred oil/water volume ratios on the order of 1:3.
- Preferred temperatures are around 374°-400° C., with the pressure at 3200-4000 psig.
- the reactor product stream leaves as a single phase, and is cooled and separated into gas, syncrude, and effluent water. The effluent water is recycled back to the reactor. Sulfur from the original feedstock accumulates in the dreg stream for the most part, with lesser amounts primarily in the form of H 2 S found in the gas phase and water phase.
- Elimination of the dreg stream means that a greater degree of hydrocarbon is recovered as syncrude, but it also means that metals and sulfur will accumulate elsewhere, such as in the water and gas streams.
- a Hamaca crude oil was diluted with a diluent hydrocarbon at a ratio of 5:1 (20 vol % of diluent:).
- the diluted Hamaca crude oil properties were measured before reacting it with the supercritical water process as referred to in Example 1 and FIG. 2 .
- the properties of the crude were as follows, 12.8 API gravity at 60/60; 1329 CST viscosity @40° C.; 7.66 wt % C/H ratio, 13.04 wt % MCRT; 3.54 wt % sulfur; 0.56 wt % nitrogen, 3.05 mg KOH/gm acid number; 1.41 wt % water; 371 ppm Vanadium; and 86 ppm Nickel.
- the diluted Hamaca crude oil after the super critical water treatment was converted into a syncrude with the following properties: 24.1 API gravity at 60/60: 5.75 CST viscosity @40° C., 7.40 wt % C/H ratio; 2.25 wt % MCRT; 2.83 wt % sulfur; 0.28 wt % nitrogen; 1.54 mg KOH/gm acid number; 0.96 wt % water; 24 ppm. Vanadium; and 3 ppm Nickel. Substantial reductions in metals and residues were observed, with simultaneous increase in the API gravity and a significant decrease in the viscosity of the original crude oil feedstock. There were modest reductions in the Total Acid number, sulfur concentration, and nitrogen concentration which could be improved with further optimization of the reaction conditions.
- the product syncrude had the following properties; 14.0 API gravity at 60.60; 1:88 CST viscosity @40° C.; 8.7 wt % MCRT; 3.11 wt % sulfur; 267 ppm Vanadium; and 59 ppm Nickel. This comparison demonstrates the, importance of the heating sequence of the present invention.
- Undiluted Boscan crude oil properties were measured before reacting it with the supercritical water process of the present invention.
- the properties of the crude were as follows: 9 API gravity at 60/60; 1,140 CST viscosity @40° C.; 8.0 wt % C/H ratio; 16 wt % MCRT; 5.8 wt % Sulfur;, and 1,280 ppm Vanadium;.
- the undiluted Boscan crude oil after the super critical water treatiment was converted into a syncrude with the following properties: 22 API: gravity at 60/60; 9 CST viscosity @40° C.; 7 . 6 wt % C/H ratio, 2.5 wt % MCRT; 4.6% sulfur; and 130 ppm Vanadium.
- the syncrudes contain a higher fraction of lower-boiling fractions, 51% of the diluted Hamaca crude boils across a range of temperatures of less than 1000° F., while employing a process according to the present invention using supercritical water depending on process configurations, between 79 to 94% of the synrcrude boils across a range of temperatures of less than 1000° F. 40% of the undiluted Boscan crude boils across a range of temperatures of less than 1000° F., while employing a process according to the present invention using supercritical water, 93% of the syncrude boils across a range of temperatures of less than 1000° F.
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- General Chemical & Material Sciences (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Priority Applications (5)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US11/555,211 US20080099374A1 (en) | 2006-10-31 | 2006-10-31 | Reactor and process for upgrading heavy hydrocarbon oils |
EA200970437A EA200970437A1 (ru) | 2006-10-31 | 2007-10-30 | Реактор и способ повышения качества тяжелых углеводородных нефтей |
PCT/US2007/082992 WO2008055152A1 (en) | 2006-10-31 | 2007-10-30 | Reactor and process for upgrading heavy hydrocarbon oils |
CA002666390A CA2666390A1 (en) | 2006-10-31 | 2007-10-30 | Reactor and process for upgrading heavy hydrocarbon oils |
CNA2007800403157A CN101558136A (zh) | 2006-10-31 | 2007-10-30 | 对重质烃油进行改质的反应器和方法 |
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US11/555,211 US20080099374A1 (en) | 2006-10-31 | 2006-10-31 | Reactor and process for upgrading heavy hydrocarbon oils |
Publications (1)
Publication Number | Publication Date |
---|---|
US20080099374A1 true US20080099374A1 (en) | 2008-05-01 |
Family
ID=39328836
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
US11/555,211 Abandoned US20080099374A1 (en) | 2006-10-31 | 2006-10-31 | Reactor and process for upgrading heavy hydrocarbon oils |
Country Status (5)
Country | Link |
---|---|
US (1) | US20080099374A1 (zh) |
CN (1) | CN101558136A (zh) |
CA (1) | CA2666390A1 (zh) |
EA (1) | EA200970437A1 (zh) |
WO (1) | WO2008055152A1 (zh) |
Cited By (40)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US20090145805A1 (en) * | 2007-11-28 | 2009-06-11 | Saudi Arabian Oil Company | Process for upgrading heavy and highly waxy crude oil without supply of hydrogen |
US20090145808A1 (en) * | 2007-11-30 | 2009-06-11 | Saudi Arabian Oil Company | Catalyst to attain low sulfur diesel |
US20090230026A1 (en) * | 2008-02-21 | 2009-09-17 | Saudi Arabian Oil Company | Catalyst To Attain Low Sulfur Gasoline |
US20110003901A1 (en) * | 2008-12-30 | 2011-01-06 | Chevron U.S.A. Inc. | Ft water treating and recovery |
US20110024330A1 (en) * | 2006-12-06 | 2011-02-03 | Saudi Arabian Oil Company | Composition and Process for the Removal of Sulfur from Middle Distillate Fuels |
US20110147266A1 (en) * | 2009-12-21 | 2011-06-23 | Saudi Arabian Oil Company | Petroleum Upgrading Process |
US20110163011A1 (en) * | 2010-12-23 | 2011-07-07 | Stephen Lee Yarbro | Using supercritical fluids to refine hydrocarbons |
US20110203973A1 (en) * | 2010-02-23 | 2011-08-25 | Chevron U.S.A., Inc. | Process for upgrading hydrocarbons and device for use therein |
US8142646B2 (en) | 2007-11-30 | 2012-03-27 | Saudi Arabian Oil Company | Process to produce low sulfur catalytically cracked gasoline without saturation of olefinic compounds |
US8444843B2 (en) | 2010-04-15 | 2013-05-21 | Saudi Arabian Oil Company | Electrocatalytic dissociation of water for hydrodesulfurization of hydrocarbon feedstock |
US20130206645A1 (en) * | 2010-12-23 | 2013-08-15 | Stephen Lee Yarbro | Using supercritical fluids to refine hydrocarbons |
US8535518B2 (en) | 2011-01-19 | 2013-09-17 | Saudi Arabian Oil Company | Petroleum upgrading and desulfurizing process |
JP2013540855A (ja) * | 2010-09-14 | 2013-11-07 | サウジ アラビアン オイル カンパニー | 超臨界水処理とその次の水素化による重質炭化水素供給原料からのイオウ除去 |
US20140109465A1 (en) * | 2012-10-22 | 2014-04-24 | Applied Research Associates, Inc. | High rate reactor system |
WO2014138208A1 (en) * | 2013-03-05 | 2014-09-12 | Saudi Arabian Oil Company | Process to upgrade and desulfurize crude oil by supercritical water |
US9005432B2 (en) | 2010-06-29 | 2015-04-14 | Saudi Arabian Oil Company | Removal of sulfur compounds from petroleum stream |
US9039889B2 (en) | 2010-09-14 | 2015-05-26 | Saudi Arabian Oil Company | Upgrading of hydrocarbons by hydrothermal process |
US20150203768A1 (en) * | 2014-01-20 | 2015-07-23 | Applied Research Associates, Inc. | High Efficiency Pour Point Reduction Process |
US20150284642A1 (en) * | 2011-04-27 | 2015-10-08 | Saudi Arabian Oil Company | Sulfone cracking using supercritical water |
US9802176B2 (en) | 2015-03-24 | 2017-10-31 | Saudi Arabian Oil Company | Method for mixing in a hydrocarbon conversion process |
US9920258B2 (en) | 2015-12-15 | 2018-03-20 | Saudi Arabian Oil Company | Supercritical reactor systems and processes for petroleum upgrading |
US9926497B2 (en) | 2015-10-16 | 2018-03-27 | Saudi Arabian Oil Company | Method to remove metals from petroleum |
US10011790B2 (en) | 2015-12-15 | 2018-07-03 | Saudi Arabian Oil Company | Supercritical water processes for upgrading a petroleum-based composition while decreasing plugging |
US10066172B2 (en) | 2015-12-15 | 2018-09-04 | Saudi Arabian Oil Company | Supercritical water upgrading process to produce paraffinic stream from heavy oil |
US10066176B2 (en) | 2015-12-15 | 2018-09-04 | Saudi Arabian Oil Company | Supercritical water upgrading process to produce high grade coke |
US10106748B2 (en) | 2017-01-03 | 2018-10-23 | Saudi Arabian Oil Company | Method to remove sulfur and metals from petroleum |
US10113122B2 (en) | 2015-08-31 | 2018-10-30 | University Of New Brunswick | Process for upgrading heavy hydrocarbon liquids |
US10526552B1 (en) | 2018-10-12 | 2020-01-07 | Saudi Arabian Oil Company | Upgrading of heavy oil for steam cracking process |
EP3481919A4 (en) * | 2016-07-08 | 2020-01-22 | Applied Research Associates, Inc. | SUPERCRITICAL WATER SEPARATION PROCESS |
US10577546B2 (en) | 2017-01-04 | 2020-03-03 | Saudi Arabian Oil Company | Systems and processes for deasphalting oil |
US10703999B2 (en) | 2017-03-14 | 2020-07-07 | Saudi Arabian Oil Company | Integrated supercritical water and steam cracking process |
US10752847B2 (en) | 2017-03-08 | 2020-08-25 | Saudi Arabian Oil Company | Integrated hydrothermal process to upgrade heavy oil |
US10815434B2 (en) | 2017-01-04 | 2020-10-27 | Saudi Arabian Oil Company | Systems and processes for power generation |
US10920158B2 (en) * | 2019-06-14 | 2021-02-16 | Saudi Arabian Oil Company | Supercritical water process to produce bottom free hydrocarbons |
US20210069732A1 (en) * | 2019-09-09 | 2021-03-11 | Xtrudx Technologies, Inc. | Supercritical hydrocyclotron and related methods |
US11021659B2 (en) | 2018-02-26 | 2021-06-01 | Saudi Arabia Oil Company | Additives for supercritical water process to upgrade heavy oil |
WO2021127243A1 (en) * | 2019-12-17 | 2021-06-24 | Saudi Arabian Oil Company | Production of liquid hydrocarbons from polyolefins by supercritical water |
US11162035B2 (en) * | 2020-01-28 | 2021-11-02 | Saudi Arabian Oil Company | Catalytic upgrading of heavy oil with supercritical water |
US11345861B2 (en) * | 2020-06-22 | 2022-05-31 | Saudi Arabian Oil Company | Production of linear olefins from heavy oil |
US11866447B2 (en) | 2022-02-03 | 2024-01-09 | Saudi Arabian Oil Company | Reactive deasphalting process |
Families Citing this family (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US9567530B2 (en) * | 2014-11-26 | 2017-02-14 | Saudi Arabian Oil Company | Process for heavy oil upgrading in a double-wall reactor |
CN111665164B (zh) * | 2019-03-05 | 2023-07-18 | 中国石油化工股份有限公司 | 测定co2在油水间传质系数的实验装置、系统及方法 |
CN114561229A (zh) * | 2022-02-28 | 2022-05-31 | 中海油天津化工研究设计院有限公司 | 一种节能的超临界水改质油品的方法 |
Citations (25)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3353924A (en) * | 1965-07-16 | 1967-11-21 | Shell Oil Co | Bed reactor with quench deck |
US3948755A (en) * | 1974-05-31 | 1976-04-06 | Standard Oil Company | Process for recovering and upgrading hydrocarbons from oil shale and tar sands |
US3948754A (en) * | 1974-05-31 | 1976-04-06 | Standard Oil Company | Process for recovering and upgrading hydrocarbons from oil shale and tar sands |
US3960706A (en) * | 1974-05-31 | 1976-06-01 | Standard Oil Company | Process for upgrading a hydrocarbon fraction |
US3983027A (en) * | 1974-07-01 | 1976-09-28 | Standard Oil Company (Indiana) | Process for recovering upgraded products from coal |
US3988238A (en) * | 1974-07-01 | 1976-10-26 | Standard Oil Company (Indiana) | Process for recovering upgraded products from coal |
US3989618A (en) * | 1974-05-31 | 1976-11-02 | Standard Oil Company (Indiana) | Process for upgrading a hydrocarbon fraction |
US4005005A (en) * | 1974-05-31 | 1977-01-25 | Standard Oil Company (Indiana) | Process for recovering and upgrading hydrocarbons from tar sands |
US4151068A (en) * | 1974-05-31 | 1979-04-24 | Standard Oil Company (Indiana) | Process for recovering and upgrading hydrocarbons from oil shale |
US4402709A (en) * | 1982-04-27 | 1983-09-06 | Texaco Inc. | Simultaneous production of clean dewatered and clean saturated streams of synthesis gas |
US4528100A (en) * | 1983-10-31 | 1985-07-09 | General Electric Company | Process for producing high yield of gas turbine fuel from residual oil |
US4557820A (en) * | 1984-05-24 | 1985-12-10 | The Standard Oil Company | Conversion of high boiling organic materials to low boiling materials |
US4559127A (en) * | 1984-05-24 | 1985-12-17 | The Standard Oil Company | Conversion of high boiling organic materials to low boiling materials |
US4594141A (en) * | 1984-12-18 | 1986-06-10 | The Standard Oil Company | Conversion of high boiling organic materials to low boiling materials |
US4840725A (en) * | 1987-06-19 | 1989-06-20 | The Standard Oil Company | Conversion of high boiling liquid organic materials to lower boiling materials |
US5384051A (en) * | 1993-02-05 | 1995-01-24 | Mcginness; Thomas G. | Supercritical oxidation reactor |
US5560823A (en) * | 1994-12-21 | 1996-10-01 | Abitibi-Price, Inc. | Reversible flow supercritical reactor and method for operating same |
US5567698A (en) * | 1995-02-15 | 1996-10-22 | Bristol-Myers Squibb Company | Pyridinium thiomethyl substituted chepholosporin derivatives |
US5611915A (en) * | 1994-03-09 | 1997-03-18 | Exxon Research And Engineering Company | Process for removal of heteroatoms under reducing conditions in supercritical water |
US5914031A (en) * | 1994-12-06 | 1999-06-22 | L'electrolyse | Process in a reducing medium of chemically transforming complex chemical structures in a supercritical fluid |
US6168771B1 (en) * | 1997-02-19 | 2001-01-02 | Hitachi, Ltd. | Supercritical oxidation process and apparatus |
US6264844B1 (en) * | 1991-06-28 | 2001-07-24 | Modell Environmental Corporation | Supercritical water oxidation process and apparatus of organics with inorganics |
US20050016733A1 (en) * | 2001-01-09 | 2005-01-27 | Dawson Jeffrey C. | Well treatment fluid compositions and methods for their use |
US6887389B2 (en) * | 2002-10-23 | 2005-05-03 | Wendell Judd | Method and apparatus for recycling sewage sludge utilizing spent water-softener lime |
US7264710B2 (en) * | 2002-03-08 | 2007-09-04 | Hitachi, Ltd. | Process and apparatus for treating heavy oil with supercritical water and power generation system equipped with heavy oil treating apparatus |
Family Cites Families (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2003025098A2 (en) * | 2001-09-17 | 2003-03-27 | Southwest Research Institute | Pretreatment processes for heavy oil and carbonaceous materials |
US7144498B2 (en) * | 2004-01-30 | 2006-12-05 | Kellogg Brown & Root Llc | Supercritical hydrocarbon conversion process |
-
2006
- 2006-10-31 US US11/555,211 patent/US20080099374A1/en not_active Abandoned
-
2007
- 2007-10-30 WO PCT/US2007/082992 patent/WO2008055152A1/en active Application Filing
- 2007-10-30 CA CA002666390A patent/CA2666390A1/en not_active Abandoned
- 2007-10-30 EA EA200970437A patent/EA200970437A1/ru unknown
- 2007-10-30 CN CNA2007800403157A patent/CN101558136A/zh active Pending
Patent Citations (26)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3353924A (en) * | 1965-07-16 | 1967-11-21 | Shell Oil Co | Bed reactor with quench deck |
US3948755A (en) * | 1974-05-31 | 1976-04-06 | Standard Oil Company | Process for recovering and upgrading hydrocarbons from oil shale and tar sands |
US3948754A (en) * | 1974-05-31 | 1976-04-06 | Standard Oil Company | Process for recovering and upgrading hydrocarbons from oil shale and tar sands |
US3960706A (en) * | 1974-05-31 | 1976-06-01 | Standard Oil Company | Process for upgrading a hydrocarbon fraction |
US3989618A (en) * | 1974-05-31 | 1976-11-02 | Standard Oil Company (Indiana) | Process for upgrading a hydrocarbon fraction |
US4005005A (en) * | 1974-05-31 | 1977-01-25 | Standard Oil Company (Indiana) | Process for recovering and upgrading hydrocarbons from tar sands |
US4151068A (en) * | 1974-05-31 | 1979-04-24 | Standard Oil Company (Indiana) | Process for recovering and upgrading hydrocarbons from oil shale |
US3983027A (en) * | 1974-07-01 | 1976-09-28 | Standard Oil Company (Indiana) | Process for recovering upgraded products from coal |
US3988238A (en) * | 1974-07-01 | 1976-10-26 | Standard Oil Company (Indiana) | Process for recovering upgraded products from coal |
US4402709A (en) * | 1982-04-27 | 1983-09-06 | Texaco Inc. | Simultaneous production of clean dewatered and clean saturated streams of synthesis gas |
US4528100A (en) * | 1983-10-31 | 1985-07-09 | General Electric Company | Process for producing high yield of gas turbine fuel from residual oil |
US4559127A (en) * | 1984-05-24 | 1985-12-17 | The Standard Oil Company | Conversion of high boiling organic materials to low boiling materials |
US4557820A (en) * | 1984-05-24 | 1985-12-10 | The Standard Oil Company | Conversion of high boiling organic materials to low boiling materials |
US4594141A (en) * | 1984-12-18 | 1986-06-10 | The Standard Oil Company | Conversion of high boiling organic materials to low boiling materials |
US4840725A (en) * | 1987-06-19 | 1989-06-20 | The Standard Oil Company | Conversion of high boiling liquid organic materials to lower boiling materials |
US6264844B1 (en) * | 1991-06-28 | 2001-07-24 | Modell Environmental Corporation | Supercritical water oxidation process and apparatus of organics with inorganics |
US5384051A (en) * | 1993-02-05 | 1995-01-24 | Mcginness; Thomas G. | Supercritical oxidation reactor |
US5558783A (en) * | 1993-02-05 | 1996-09-24 | Mcguinness; Thomas G. | Supercritical oxidation reactor |
US5611915A (en) * | 1994-03-09 | 1997-03-18 | Exxon Research And Engineering Company | Process for removal of heteroatoms under reducing conditions in supercritical water |
US5914031A (en) * | 1994-12-06 | 1999-06-22 | L'electrolyse | Process in a reducing medium of chemically transforming complex chemical structures in a supercritical fluid |
US5560823A (en) * | 1994-12-21 | 1996-10-01 | Abitibi-Price, Inc. | Reversible flow supercritical reactor and method for operating same |
US5567698A (en) * | 1995-02-15 | 1996-10-22 | Bristol-Myers Squibb Company | Pyridinium thiomethyl substituted chepholosporin derivatives |
US6168771B1 (en) * | 1997-02-19 | 2001-01-02 | Hitachi, Ltd. | Supercritical oxidation process and apparatus |
US20050016733A1 (en) * | 2001-01-09 | 2005-01-27 | Dawson Jeffrey C. | Well treatment fluid compositions and methods for their use |
US7264710B2 (en) * | 2002-03-08 | 2007-09-04 | Hitachi, Ltd. | Process and apparatus for treating heavy oil with supercritical water and power generation system equipped with heavy oil treating apparatus |
US6887389B2 (en) * | 2002-10-23 | 2005-05-03 | Wendell Judd | Method and apparatus for recycling sewage sludge utilizing spent water-softener lime |
Cited By (87)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US8323480B2 (en) | 2006-12-06 | 2012-12-04 | Saudi Arabian Oil Company | Composition and process for the removal of sulfur from middle distillate fuels |
US20110024330A1 (en) * | 2006-12-06 | 2011-02-03 | Saudi Arabian Oil Company | Composition and Process for the Removal of Sulfur from Middle Distillate Fuels |
US20090145805A1 (en) * | 2007-11-28 | 2009-06-11 | Saudi Arabian Oil Company | Process for upgrading heavy and highly waxy crude oil without supply of hydrogen |
US20090178952A1 (en) * | 2007-11-28 | 2009-07-16 | Saudi Arabian Oil Company | Process to upgrade highly waxy crude oil by hot pressurized water |
US10010839B2 (en) | 2007-11-28 | 2018-07-03 | Saudi Arabian Oil Company | Process to upgrade highly waxy crude oil by hot pressurized water |
US8815081B2 (en) | 2007-11-28 | 2014-08-26 | Saudi Arabian Oil Company | Process for upgrading heavy and highly waxy crude oil without supply of hydrogen |
US9656230B2 (en) | 2007-11-28 | 2017-05-23 | Saudi Arabian Oil Company | Process for upgrading heavy and highly waxy crude oil without supply of hydrogen |
US20090145808A1 (en) * | 2007-11-30 | 2009-06-11 | Saudi Arabian Oil Company | Catalyst to attain low sulfur diesel |
US8142646B2 (en) | 2007-11-30 | 2012-03-27 | Saudi Arabian Oil Company | Process to produce low sulfur catalytically cracked gasoline without saturation of olefinic compounds |
US9636662B2 (en) | 2008-02-21 | 2017-05-02 | Saudi Arabian Oil Company | Catalyst to attain low sulfur gasoline |
US10252247B2 (en) | 2008-02-21 | 2019-04-09 | Saudi Arabian Oil Company | Catalyst to attain low sulfur gasoline |
US10596555B2 (en) | 2008-02-21 | 2020-03-24 | Saudi Arabian Oil Company | Catalyst to attain low sulfur gasoline |
US20090230026A1 (en) * | 2008-02-21 | 2009-09-17 | Saudi Arabian Oil Company | Catalyst To Attain Low Sulfur Gasoline |
US20110003901A1 (en) * | 2008-12-30 | 2011-01-06 | Chevron U.S.A. Inc. | Ft water treating and recovery |
US20110147266A1 (en) * | 2009-12-21 | 2011-06-23 | Saudi Arabian Oil Company | Petroleum Upgrading Process |
US8394260B2 (en) | 2009-12-21 | 2013-03-12 | Saudi Arabian Oil Company | Petroleum upgrading process |
US8197670B2 (en) | 2010-02-23 | 2012-06-12 | Chevron U.S.A. Inc. | Process for upgrading hydrocarbons and device for use therein |
WO2011106217A3 (en) * | 2010-02-23 | 2011-11-24 | Chevron U.S.A. Inc. | Process for upgrading hydrocarbons and device for use therein |
WO2011106217A2 (en) * | 2010-02-23 | 2011-09-01 | Chevron U.S.A. Inc. | Process for upgrading hydrocarbons and device for use therein |
US20110203973A1 (en) * | 2010-02-23 | 2011-08-25 | Chevron U.S.A., Inc. | Process for upgrading hydrocarbons and device for use therein |
US8444843B2 (en) | 2010-04-15 | 2013-05-21 | Saudi Arabian Oil Company | Electrocatalytic dissociation of water for hydrodesulfurization of hydrocarbon feedstock |
US9005432B2 (en) | 2010-06-29 | 2015-04-14 | Saudi Arabian Oil Company | Removal of sulfur compounds from petroleum stream |
JP2013540855A (ja) * | 2010-09-14 | 2013-11-07 | サウジ アラビアン オイル カンパニー | 超臨界水処理とその次の水素化による重質炭化水素供給原料からのイオウ除去 |
US9957450B2 (en) | 2010-09-14 | 2018-05-01 | Saudi Arabian Oil Company | Petroleum upgrading process |
US9382485B2 (en) | 2010-09-14 | 2016-07-05 | Saudi Arabian Oil Company | Petroleum upgrading process |
US9039889B2 (en) | 2010-09-14 | 2015-05-26 | Saudi Arabian Oil Company | Upgrading of hydrocarbons by hydrothermal process |
US8894846B2 (en) * | 2010-12-23 | 2014-11-25 | Stephen Lee Yarbro | Using supercritical fluids to refine hydrocarbons |
US9051521B2 (en) * | 2010-12-23 | 2015-06-09 | Stephen Lee Yarbro | Using supercritical fluids to refine hydrocarbons |
US20130206645A1 (en) * | 2010-12-23 | 2013-08-15 | Stephen Lee Yarbro | Using supercritical fluids to refine hydrocarbons |
US20110163011A1 (en) * | 2010-12-23 | 2011-07-07 | Stephen Lee Yarbro | Using supercritical fluids to refine hydrocarbons |
US8535518B2 (en) | 2011-01-19 | 2013-09-17 | Saudi Arabian Oil Company | Petroleum upgrading and desulfurizing process |
US9951283B2 (en) | 2011-01-19 | 2018-04-24 | Saudi Arabian Oil Company | Petroleum upgrading and desulfurizing process |
US9550948B2 (en) * | 2011-04-27 | 2017-01-24 | Saudi Arabian Oil Company | Sulfone cracking using supercritical water |
US20150284642A1 (en) * | 2011-04-27 | 2015-10-08 | Saudi Arabian Oil Company | Sulfone cracking using supercritical water |
US9353318B2 (en) * | 2011-04-27 | 2016-05-31 | Saudi Arabian Oil Company | Sulfone cracking using supercritical water |
US20160272900A1 (en) * | 2011-04-27 | 2016-09-22 | Saudi Arabian Oil Company | Sulfone cracking using supercritical water |
EP2908942B1 (en) * | 2012-10-22 | 2020-08-12 | Applied Research Associates, Inc. | High-rate reactor system |
US20140109465A1 (en) * | 2012-10-22 | 2014-04-24 | Applied Research Associates, Inc. | High rate reactor system |
WO2014138208A1 (en) * | 2013-03-05 | 2014-09-12 | Saudi Arabian Oil Company | Process to upgrade and desulfurize crude oil by supercritical water |
JP2016515151A (ja) * | 2013-03-05 | 2016-05-26 | サウジ アラビアン オイル カンパニー | 超臨界水流によって原油の品質を上げ、かつ脱硫するプロセス |
KR101818317B1 (ko) * | 2013-03-05 | 2018-01-12 | 사우디 아라비안 오일 컴퍼니 | 초임계수에 의해 원유를 업그레이드하고 탈황하는 공정 |
US9914885B2 (en) | 2013-03-05 | 2018-03-13 | Saudi Arabian Oil Company | Process to upgrade and desulfurize crude oil by supercritical water |
US20150203768A1 (en) * | 2014-01-20 | 2015-07-23 | Applied Research Associates, Inc. | High Efficiency Pour Point Reduction Process |
US10961469B2 (en) * | 2014-01-20 | 2021-03-30 | Applied Research Associates, Inc. | High efficiency pour point reduction process |
US9802176B2 (en) | 2015-03-24 | 2017-10-31 | Saudi Arabian Oil Company | Method for mixing in a hydrocarbon conversion process |
US10113122B2 (en) | 2015-08-31 | 2018-10-30 | University Of New Brunswick | Process for upgrading heavy hydrocarbon liquids |
US10202552B2 (en) | 2015-10-16 | 2019-02-12 | Saudi Arabian Oil Company | Method to remove metals from petroleum |
US9926497B2 (en) | 2015-10-16 | 2018-03-27 | Saudi Arabian Oil Company | Method to remove metals from petroleum |
US10995281B2 (en) | 2015-12-15 | 2021-05-04 | Saudi Arabian Oil Company | Supercritical reactor systems and processes for petroleum upgrading |
US11021660B2 (en) | 2015-12-15 | 2021-06-01 | Saudi Arabian Oil Company | Supercritical reactor systems and processes for petroleum upgrading |
JP2019002012A (ja) * | 2015-12-15 | 2019-01-10 | サウジ アラビアン オイル カンパニーSaudi Arabian Oil Company | 石油改良のための超臨界反応器システム及びプロセス |
JP2019006996A (ja) * | 2015-12-15 | 2019-01-17 | サウジ アラビアン オイル カンパニーSaudi Arabian Oil Company | 石油改良のための超臨界反応器システム及びプロセス |
US10119081B2 (en) | 2015-12-15 | 2018-11-06 | Saudi Arabian Oil Company | Supercritical reactor systems and processes for petroleum upgrading |
JP2019505609A (ja) * | 2015-12-15 | 2019-02-28 | サウジ アラビアン オイル カンパニーSaudi Arabian Oil Company | 石油改良のための超臨界反応器システム及びプロセス |
US10066172B2 (en) | 2015-12-15 | 2018-09-04 | Saudi Arabian Oil Company | Supercritical water upgrading process to produce paraffinic stream from heavy oil |
US10344228B2 (en) | 2015-12-15 | 2019-07-09 | Saudi Arabian Oil Company | Supercritical water upgrading process to produce high grade coke |
US10384179B2 (en) | 2015-12-15 | 2019-08-20 | Saudi Arabian Oil Company | Supercritical reactor systems and processes for petroleum upgrading |
CN108993317A (zh) * | 2015-12-15 | 2018-12-14 | 沙特阿拉伯石油公司 | 用于石油升级的超临界反应器系统和工艺 |
US10011790B2 (en) | 2015-12-15 | 2018-07-03 | Saudi Arabian Oil Company | Supercritical water processes for upgrading a petroleum-based composition while decreasing plugging |
US10543468B2 (en) | 2015-12-15 | 2020-01-28 | Saudi Arabian Oil Company | Supercritical reactor systems and processes for petroleum upgrading |
US9920258B2 (en) | 2015-12-15 | 2018-03-20 | Saudi Arabian Oil Company | Supercritical reactor systems and processes for petroleum upgrading |
US10066176B2 (en) | 2015-12-15 | 2018-09-04 | Saudi Arabian Oil Company | Supercritical water upgrading process to produce high grade coke |
US10640715B2 (en) | 2015-12-15 | 2020-05-05 | Saudi Arabian Oil Company | Supercritical reactor systems and processes for petroleum upgrading |
EP3481919A4 (en) * | 2016-07-08 | 2020-01-22 | Applied Research Associates, Inc. | SUPERCRITICAL WATER SEPARATION PROCESS |
US10941355B2 (en) | 2016-07-08 | 2021-03-09 | Applied Research Associates, Inc. | Supercritical water separation process |
US10703988B2 (en) | 2017-01-03 | 2020-07-07 | Saudi Arabian Oil Company | System to remove sulfur and metals from petroleum |
US10106748B2 (en) | 2017-01-03 | 2018-10-23 | Saudi Arabian Oil Company | Method to remove sulfur and metals from petroleum |
US10815434B2 (en) | 2017-01-04 | 2020-10-27 | Saudi Arabian Oil Company | Systems and processes for power generation |
US10577546B2 (en) | 2017-01-04 | 2020-03-03 | Saudi Arabian Oil Company | Systems and processes for deasphalting oil |
US10752847B2 (en) | 2017-03-08 | 2020-08-25 | Saudi Arabian Oil Company | Integrated hydrothermal process to upgrade heavy oil |
US11149216B2 (en) | 2017-03-08 | 2021-10-19 | Saudi Arabian Oil Company | Integrated hydrothermal process to upgrade heavy oil |
US11149218B2 (en) | 2017-03-14 | 2021-10-19 | Saudi Arabian Oil Company | Integrated supercritical water and steam cracking process |
US10703999B2 (en) | 2017-03-14 | 2020-07-07 | Saudi Arabian Oil Company | Integrated supercritical water and steam cracking process |
US11479729B2 (en) | 2018-02-26 | 2022-10-25 | Saudi Arabian Oil Company | Additives for supercritical water process to upgrade heavy oil |
US11021659B2 (en) | 2018-02-26 | 2021-06-01 | Saudi Arabia Oil Company | Additives for supercritical water process to upgrade heavy oil |
US10975317B2 (en) | 2018-10-12 | 2021-04-13 | Saudi Arabian Oil Company | Upgrading of heavy oil for steam cracking process |
US10526552B1 (en) | 2018-10-12 | 2020-01-07 | Saudi Arabian Oil Company | Upgrading of heavy oil for steam cracking process |
US11230675B2 (en) | 2018-10-12 | 2022-01-25 | Saudi Arabian Oil Company | Upgrading of heavy oil for steam cracking process |
US11149215B2 (en) * | 2019-06-14 | 2021-10-19 | Saudi Arabian Oil Company | Supercritical water process to produce bottom free hydrocarbons |
US10920158B2 (en) * | 2019-06-14 | 2021-02-16 | Saudi Arabian Oil Company | Supercritical water process to produce bottom free hydrocarbons |
US20210069732A1 (en) * | 2019-09-09 | 2021-03-11 | Xtrudx Technologies, Inc. | Supercritical hydrocyclotron and related methods |
WO2021127243A1 (en) * | 2019-12-17 | 2021-06-24 | Saudi Arabian Oil Company | Production of liquid hydrocarbons from polyolefins by supercritical water |
US11124707B2 (en) | 2019-12-17 | 2021-09-21 | Saudi Arabian Oil Company | Production of liquid hydrocarbons from polyolefins by supercritical water |
CN114829547A (zh) * | 2019-12-17 | 2022-07-29 | 沙特阿拉伯石油公司 | 用超临界水从聚烯烃生产液态烃 |
US11162035B2 (en) * | 2020-01-28 | 2021-11-02 | Saudi Arabian Oil Company | Catalytic upgrading of heavy oil with supercritical water |
US11345861B2 (en) * | 2020-06-22 | 2022-05-31 | Saudi Arabian Oil Company | Production of linear olefins from heavy oil |
US11866447B2 (en) | 2022-02-03 | 2024-01-09 | Saudi Arabian Oil Company | Reactive deasphalting process |
Also Published As
Publication number | Publication date |
---|---|
CA2666390A1 (en) | 2008-05-08 |
CN101558136A (zh) | 2009-10-14 |
EA200970437A1 (ru) | 2009-10-30 |
WO2008055152A1 (en) | 2008-05-08 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
US20080099374A1 (en) | Reactor and process for upgrading heavy hydrocarbon oils | |
US20080099378A1 (en) | Process and reactor for upgrading heavy hydrocarbon oils | |
US20080099376A1 (en) | Upgrading heavy hydrocarbon oils | |
US20080099377A1 (en) | Process for upgrading heavy hydrocarbon oils | |
US20090166262A1 (en) | Simultaneous metal, sulfur and nitrogen removal using supercritical water | |
US20090166261A1 (en) | Upgrading heavy hydrocarbon oils | |
EP2588569B1 (en) | Removal of sulfur compounds from petroleum stream | |
JP5346036B2 (ja) | 水素の供給を用いない重質及び高ワックス質原油のアップグレード法 | |
US9951283B2 (en) | Petroleum upgrading and desulfurizing process | |
US20180171240A1 (en) | Method to remove metals from petroleum | |
US20090159498A1 (en) | Intergrated process for in-field upgrading of hydrocarbons | |
CA2790617C (en) | Process for upgrading hydrocarbons and device for use therein | |
CN111788283A (zh) | 使用超临界水的转化工艺 | |
KR20240031339A (ko) | 탄화수소계 중질 공급원료를 유기 첨가제와 예비혼합하는 것을 포함하는, 탄화수소계 중질 공급원료의 하이브리드 비등-동반 층 수소화전환 | |
CN117616104A (zh) | 包括将重质烃原料与有机添加剂预混合的所述原料的浆态床加氢转化 | |
CN117651754A (zh) | 包括将重质烃原料与包含有机添加剂的催化剂前体混合的所述原料的浆态床加氢转化 | |
EA041150B1 (ru) | Способ модернизации реактора с кипящим слоем для незначительного загрязнения осадком |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
AS | Assignment |
Owner name: CHEVRON U.S.A. INC., CALIFORNIA Free format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNORS:HE, ZUNQING;LI, LIN;LI, LIXIONG;AND OTHERS;REEL/FRAME:018819/0483;SIGNING DATES FROM 20070115 TO 20070124 |
|
STCB | Information on status: application discontinuation |
Free format text: ABANDONED -- FAILURE TO RESPOND TO AN OFFICE ACTION |