EP2751230A2 - Utilisation de fluide supercritique dans l'hydrotraitement d'hydrocarbures lourds - Google Patents

Utilisation de fluide supercritique dans l'hydrotraitement d'hydrocarbures lourds

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Publication number
EP2751230A2
EP2751230A2 EP12762124.1A EP12762124A EP2751230A2 EP 2751230 A2 EP2751230 A2 EP 2751230A2 EP 12762124 A EP12762124 A EP 12762124A EP 2751230 A2 EP2751230 A2 EP 2751230A2
Authority
EP
European Patent Office
Prior art keywords
solvent
comprised
component
solvent component
supercritical
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.)
Withdrawn
Application number
EP12762124.1A
Other languages
German (de)
English (en)
Inventor
Stephen Harold Brown
Teh C. Ho
Jane Chi-Ya Cheng
Hyung Suk Woo
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
ExxonMobil Technology and Engineering Co
Original Assignee
ExxonMobil Research and Engineering Co
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by ExxonMobil Research and Engineering Co filed Critical ExxonMobil Research and Engineering Co
Publication of EP2751230A2 publication Critical patent/EP2751230A2/fr
Withdrawn legal-status Critical Current

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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
    • C10G47/00—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions
    • C10G47/32—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions in the presence of hydrogen-generating compounds
    • C10G47/34—Organic compounds, e.g. hydrogenated hydrocarbons
    • 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
    • C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
    • C10G45/02—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing
    • 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
    • C10G47/00—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions
    • 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
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/20—Characteristics of the feedstock or the products
    • C10G2300/201—Impurities
    • C10G2300/205—Metal content
    • 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
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/20—Characteristics of the feedstock or the products
    • C10G2300/201—Impurities
    • C10G2300/205—Metal content
    • C10G2300/206—Asphaltenes
    • 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
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/20—Characteristics of the feedstock or the products
    • C10G2300/30—Physical properties of feedstocks or products
    • C10G2300/301—Boiling range
    • 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
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/20—Characteristics of the feedstock or the products
    • C10G2300/30—Physical properties of feedstocks or products
    • C10G2300/308—Gravity, density, e.g. API
    • 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
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/40—Characteristics of the process deviating from typical ways of processing
    • C10G2300/44—Solvents

Definitions

  • This invention is directed to a process for producing a hvdroprocessed product from residua or heavy hydrocarbon feeds. More specifically, this invention is directed to a process for producing a hvdroprocessed product from a heavy hydrocarbon oil, using a supercritical fluid or solvent.
  • Crude oil is typically distilled to produce a variety of components that can be used directly as fuels or that are used as feedstocks for further processing or upgrading.
  • a heavy residuum is produced typically that has an initial boiling point of about 650°F (343°C). This residuum is typically referred to as atmospheric residuum or as an atmospheric residuum fraction.
  • Atmospheric residuum fractions tend to collect a relatively high quantity of various metals, sulfur components and nitrogen components relative to the lighter distillation fractions as a result of the distillation process. Because these metal sulfur and nitrogen components are relatively undesirable in various fuels, they are typically removed by various catalytic hydroprocessing techniques.
  • the atmospheric residuum is further distilled under vacuum, i.e., at a pressure below atmospheric pressure, to recover additional distillation fractions.
  • additional lighter fractions can be recovered without adding to various problems encountered in atmospheric distillation such as coking of the heavy fraction components.
  • the heavy residuum recovered in vacuum distillation of the atmospheric residuum is typically referred to as vacuum residuum or a vacuum residuum fraction, and typically has an initial boiling point of about 1 050°F (566°C).
  • This vacuum residuum is generally higher in metals, sulfur components and nitrogen components than atmospheric residuum, and as was the case with atmospheric residuum, removal of these components is typically carried out by catalytic hydroprocessing.
  • Catalytic hydroprocessing of atmospheric and vacuum residua, including other heavy oils such as bitumen from oil sand, is carried out in the presence of hydrogen, using a hydroprocessing catalyst.
  • hydroprocessing of heavy oil or residua is carried out bv adding a diluent or solvent.
  • Hydroprocessing of residua or other heavy oil can also include a cracking activity in which the heavv carbon components are "cracked” into smaller or lower molecular weight components. This is typically referred to as upgrading, with the upgraded product including higher volumes of fuel components.
  • U.S. Patent No. 3,617,525 discloses a process for removing sulfur from a hydrocarbon fraction having a boiling point above about 650°F (343 °C).
  • the hydrocarbon fraction is separated into a gas oil fraction having a boiling point between about 650°F (343 °C) and about 1050°F (566°C), and a heavy residuum fraction boiling above about 1050°F (566°C).
  • the gas oil fraction is catalytically hydrodesulfurized until the gas oil fraction contains less than 1 percent sulfur.
  • the hydrodesulfurized gas oil is then used to dilute the heavy residuum fraction, and the diluted heavy residuum fraction is catalytically hydrodesulfurized, producing fuels or fuel blending components reduced in sulfur content.
  • the process is considered to provide an increased catalyst life and to use a smaller reactor volume compared to typical processes.
  • U.S. Patent No. 4,302,323 discloses a process for upgrading a residual petroleum fraction in which the residual fraction is mixed with a light cycle oil and hydrogen and the mixture sent through a catalytic hydrotreating zone containing a hydrotreating catalyst and then a hydrocrackmg zone containing a hydrocrackmg catalyst. Upgraded products are then separated from the effluent of the hydrocrackmg zone.
  • the light cycle oil boils in the range of from 400°F (204°C) to 700°F (371 °C), has a high aromatic content, and is high in nitrogen. It is considered that the light cycle oil acts more as a diluent rather than as a hydrogen donor and that the addition of the light cycle oil resulted in a substantial increase in the yield of premium products such as distillate fuels.
  • the feedstock can be atmospheric residuum or vacuum residuum, which is mixed with a solvent that is a recycled distillate boiling at about 400°F-700°F (204°C-371 °C), considered to be equivalent to a FCC light cycle oil.
  • the process uses a mixture of large pore and small pore catalysts such as large and small pore sulfided Ni-W catalysts. The process converts the higher boiling point residua to lower boiling point hydrocarbons by forming distillate and naphtha while removing heteroatoms, metals and carbon residuals from the higher boiling point residua.
  • Supercritical fluids have typically been used in the hydrocarbon processing industries to provide enhanced solubilization or extracting power for many complex organic molecules.
  • a fluid at both a temperature and pressure that exceeds its critical temperature and pressure is considered a supercritical fluid.
  • a supercritical fluid exists in a form in which its liquid and gaseous states are indistinguishable from one another,
  • the critical temperature of a fluid is the temperature above which the fluid cannot be liquefied by an increase in pressure,
  • the critical pressure of a fluid is the vapor pressure of the fluid at its critical temperature. It has been shown that not only does the solubility of heavy materials in the supercritical fluid increase generally with temperature, but also that above the critical temperature the solubility increases with pressure, often by an order of magnitude.
  • U.S. Patent No. 5,496,464 discloses a process for hydrotreating a heavy hydrocarbon oil containing a substantial portion of material that boils above 524°C to form lower boiling materials.
  • the process comprises adding to the heavy hydrocarbon oil as solvent a paraffmic, isoparaffinic or cyclic paraffmic hydrocarbon that is hydrogen-rich and has a critical temperature of less than 500°C.
  • the addition of the solvent to the heavy hydrocarbon oil forms a diluted feedstock mixture and the feedstock mixture is hydrotreated in the presence of activated carbon catalyst at a temperature and pressure substantially at or greater than the critical temperature and pressure of the solvent.
  • the supercritical solvent is considered to act as a hydrogen-rich diluent to decrease the probability of recombination and condensation of asphaltene molecules, and to enhance the degree of breakup of coke precursor "micelles," and to enhance diffusivity of the reactant molecules into and out of the pores of the activated carbon catalyst.
  • the sol ent in conjunction with the activated carbon act in a unique way to transfer gaseous hydrogen to the heavy hydrogen-deficient feedstock.
  • This invention provides a process for producing hydroprocessed product.
  • the hydroprocessed products are lighter hydrocarbon oils, which can be used to produce fuel grade products.
  • the process provides an advantage of having a long catalyst run length.
  • a process for producing a hydroprocessed product includes a step of sending to a hydroprocessing zone (preferably located in a reactor vessel) a combined feed comprised of a heavy hydrocarbon oil component, wherein the heavy hydrocarbon oil component has a ASTM D86 10% distillation point of at least 650°F (343°C), and a solvent component in which a majority of the solvent component is comprised of at least one supercritical hydrocarbon compound having a critical temperature and pressure.
  • the combined feed is contacted with a hydroprocessing catalyst in the hydroprocessing zone in the presence of hydrogen at a temperature and pressure above the critical, temperature and pressure of the at least one supercritical hydrocarbon compound to form the hydroprocessed product.
  • the heavy hydrocarbon oil component has an initial ASTM D86 boiling point of 650°F (343°C) or greater.
  • the heavy hydrocarbon oil can contain at least 0.0001 grams of Ni/V/Fe, on a total elemental basis of nickel vanadium and iron.
  • the combined feed is comprised of from 30 wt% to 90 wt% of the heavy hydrocarbon oil component and from 10 wt% to 70 wt% of the solvent component, based on total weight of the combined feed.
  • the contacting of the combined feed with a hydroprocessing catalyst in the presence of hydrogen is carried out at a hydrogen partial pressure from 550 psig (3792 kPa-g) to 3000 psig (20684 kPa-g).
  • the solvent component is comprised of more than one supercritical hydrocarbon compound and contacting of the combined feed with the hydroprocessing catalyst, in the presence of hydrogen is carried out at a total pressure that is higher than the critical pressure of the highest-boiling point supercritical hydrocarbon compound in the solvent component.
  • the solvent component is comprised of more than one supercritical hydrocarbon compound and contacting of the supercritical hydrocarbon compound with the combined feed and the hydroprocessing catalyst in the presence of hydrogen is carried out at a temperature that is higher than the critical temperature of the highest-boiling point supercritical
  • the contacting is carried out at a total pressure and at a temperature at which the combined feed and the
  • hydroprocessed products are comprised of no more than one vapor and one liquid phase during contact
  • the solvent component is comprised of at least one supercritical solvent compound selected from the group consisting of benzene, toluene, xylene, ethyl benzene, iso-propyl benzene, trimefhylbenzene and tetramethylbenzene.
  • the solvent component can be comprised of a mixture of aromatic molecules having boiling points of from 200°F (93 ° €) to 750°F (399°C).
  • the solvent component can be comprised of a mixture of aromatic and hydroa.rom.atic molecules having boiling points of from 200°F (93°C) to 750°F (399°C).
  • the solvent component has an ASTM D86 10% distillation point of at least 250°F (120°C).
  • the solvent component can be a petroleum fraction with an API gravity of at most 35°.
  • the contacting is carried out at a temperature of from 320°F (160°C) to 900°F (482°C).
  • the contacting can also be carried out at a pressure of from 600 psig (4137 kPa-g) to 3000 psig (20684 kPa-g).
  • the solvent component is comprised of trimethylbenzene.
  • the solvent component is comprised of at least 50 wt % trimethylbenzene, based o total weight of the solvent component.
  • the heavy hydrocarbon oil component and the solvent component are combined prior to entering the liydroprocessing zone although in embodiments of the invention, the heavy hydrocarbon oil component and the solvent component may be combined in the hydroprocessing zone.
  • at least a portion, of the solvent component can be injected separately into an intermediate section of the hydroprocessing zone as an interbed quench.
  • the hydroprocessing zone contains the catalyst in a fixed bed.
  • FIG URE 1 shows a comparative example of hydroprocessing of 100% Basrah resid.
  • FIGURE 2 shows a specific example of the invention regarding hydroprocessing of 60/40 resid/trimethylbenzene feed.
  • FIGURE 3 shows a comparative example of hydroprocessing of resid methylnaphihalene feed.
  • This invention provides a process for producing a hvdroprocessed product.
  • the process is capable of treating residua or heavy hydrocarbon oils to produce a hvdroprocessed oil product that has reduced sulfur, nitrogen, metals and " 1050°F+ (566°C+) fraction" components (i.e., components that boil at 1050°F (566°C) and above) relative to the heavy oil.
  • 1050°F+ (566°C+) fraction i.e., components that boil at 1050°F (566°C) and above
  • a majority of the solvent component is comprised of supercritical hydrocarbon compounds in which the supercritical hydrocarbon compounds have a critical temperature and pressure.
  • the heavy hydrocarbon oil feed material and solvent co-feed are hydroprocessed by contacting the combined feed with hydroprocessing catalyst in the presence of hydrogen at a temperature and pressure above the critical temperature and pressure of the supercritical hydrocarbon compounds to form a hydroprocessed product.
  • the hydroprocessed product has reduced sulfur, nitrogen, metals and 1050°F+ (566°C+) fraction components (i.e., components that boil at 1050°F (566°C) and above) relative to the heavy hydrocarbon oil feed component.
  • the hydroprocessed product is produced from a heavy hydrocarbon oil component.
  • heavy hydrocarbon oils include, but are not limited to, heavy crude oils, distillation residues, heavy oils coming from catalytic treatment (such as fluid catalytic cracking), tars (such as oils from visbreaking or similar thermal processes), oils (such as bitumen) from oil sands and heavy oils derived from coal.
  • Heavy hydrocarbon oils can be liquid, semi-solid, and/or solid at atmospheric conditions. Additional examples of heavy oils that can be hydroprocessed, treated or upgraded according to this invention include
  • Heavy hydrocarbon oil examples include residuum from refinery distillation processes, including atmospheric and vacuum distillation processes.
  • Such heavy hydrocarbon oils can have an initial ASTM D86 boiling point of 650°F (343°C) or greater.
  • the heavy hydrocarbon oil will have an ASTM D86 10% distillation point of at least 650°F (343°C),
  • Heavy hydrocarbon oils can be relatively high in total acid number (TAN),
  • TAN total acid number
  • heavy hydrocarbon oils that can be hydroprocessed according to this invention have a TAN of at least 0.1 , at least 0.3, or at least 1.
  • the density, or weight per volume, of the heavy hydrocarbon can be determined according to ASTM 0287-92(2006) Standard Test Method for API Gravity of ( ' rude Petroleum and Petroleum. Products (Hydrometer Method), and is provided in terms of API gravity. In general, the higher the API gravity, the less dense the oil. API gravity is at most 20° in. one embodiment, at most 15° in another embodiment, and at most 10° in another embodiment.
  • Heavy hydrocarbon oils can be high in metals.
  • the heavy hydrocarbon oil can be high in total nickel, vanadium and iron contents.
  • the heavy hydrocarbon oil will contain at least 0.00005 grams of Ni/V/Fe (50 ppm) or at least 0.0002 grams of Ni/V/Fe (200 ppm) per gram of heavy hydrocarbon oil, on a total elemental basis of nickel, vanadium and iron.
  • Contaminants such as nitrogen and sulfur are found in heavy hydrocarbon oils, often in organically-bound form.
  • Nitrogen content can range from about 50 wppm to about 5000 wppm elemental nitrogen, or about 75 wppm to about 800 wppm elemental nitrogen, or about 100 wppm to about 700 wppm, based on total weight of the heavy hydrocarbon component.
  • the nitrogen containing compounds can be present as basic or non-basic nitrogen species. Examples of basic nitrogen species include quinolines and substituted quinolines. Examples of non-basic nitrogen species include carbazoles and substituted carbazoles,
  • Sulfur content of heavy hydrocarbon oils generally ranges from about 500 wppm to about 100,000 wppm elemental sulfur, or from about 1000 wppm to about 50,000 wppm, or from about 1000 wppm to about 30,000 wppm, based on total weight of the heavy hydrocarbon component.
  • Sulfur will usually be present as organically bound sulfur.
  • examples of such sulfur compounds include the class of heterocyclic sulfur compounds such as thiophenes, tetrahydrothiophenes, benzothiophenes and their higher homologs and analogs
  • Other organically bound sulfur compounds include aliphatic, naphthenic, and aromatic mercaptans, sulfides, di- and polysulfides.
  • Heavy hydrocarbon oils can be high in n-pentane asphaltenes.
  • the heavy hydrocarbon oil will contain at 5 wt% or at least 15 wt% n-pentane asphaltene s .
  • the solvent component that is used according to this invention is comprised of at least one supercritical solvent compound, in which a
  • supercritical solvent compound is defined as a compound, i.e., hydrocarbon compound, having a critical point, such as a critical temperature and critical pressure.
  • a hydrocarbon compound is defined as a compound having at least one hydrogen atom and at least one carbon atom.
  • a critical point is the temperature and pressure at which a phase boundary of the hydrocarbon ceases to exist.
  • a preferred supercritical solvent compound of this invention is a hydrocarbon oil solvent that has a vapor-liquid critical point below the operating temperature and pressure at which the hydroprocessing process is being carried out.
  • the solvent component can include supercritical solvent compounds as well as hydrocarbons that are not considered supercritical solvent compounds.
  • a majority (i.e., at least 50 wt % based on total solvent weight) of the solvent component is comprised of one or more supercritical compounds.
  • the solvent can be comprised of at least 60 wt% or 70 wt% or 80 wt% or 90 wt%, based on total solvent weight, of supercritical compounds.
  • the supercritical solvent compounds contained in the solvent composition preferably have a critical temperature of at least 300°F (149°C).
  • the compounds can be hydrocarbons or organic derivatives of hydrocarbons and other organic compounds that have a critical temperature of at least 300°F (149°C).
  • these compounds Preferably, these compounds have a critical temperature of not greater than 840°F (449°C).
  • the supercritical compounds have a critical temperature of at least 350°F (177°C), or at least 480°F (249°C), or at least 6G0°F (316°C), and not greater than 750°F (399°C).
  • the supercritical solvent compounds contained in the solvent component preferably have a critical pressure of not greater than 500 psig (3447 kPa-g). More preferably, the supercritical solvent compounds contained in the solvent component have a critical pressure of not greater than 400 psig (2750 kPa ⁇ g), alternatively 350 psig (2413 kPa-g), alternatively not greater than 300 psig (2068 kPa-g), or alternatively not greater than 250 psig (1724 kPa-g).
  • the supercritical solvent compounds contained in the solvent component have a critical pressure of at least 50 psig (345 kPa-g), or at least 100 psi (389 kPa-g), or at least 150 psig (1034 kPa-g).
  • the supercritical solvent compounds contained in the solvent composition have boiling points of not greater than 750°F (399°C). In a preferred embodiment, none of the supercritical solvent compounds contained in the solvent composition has a boiling point of greater than 600°F (316°C), or greater than 550°F (288°C), or greater than 500°F (260°C), or greater than 450°F i232°C), or greater than 400°F (204°C).
  • the supercritical solvent compounds At the hydroprocessing temperature, i.e., the temperature in the contacting zone in which the combined heavy hydrocarbon oil and the solvent co-feed contact the hydroprocessing catalyst, the supercritical solvent compounds will be in a supercritical or near-supercritical state. Under hydroprocessing conditions, the solvent components should be much less reactive than residual oils. Preferably, the supercritical compounds undergo no greater than 30 percent decomposition, particularly no greater than 20 percent decomposition, during hydroprocessing.
  • Suitable supercritical compounds that can be used as the solvent of this invention include aromatic hydrocarbons having one, two or three rings, hydroaromatic compounds, alicyclic compounds and aliphatic compounds or mixtures thereof.
  • the solvent component can be comprised of a mixture of aromatic molecules having boiling points of from 200 F (93 °C) to 750°F (399°C), or from 240°F (1 16°C) to 710°F (377°C), or from 260°F
  • aromatic hydrocarbon includes aromatic hydrocarbons having a single benzene ring and preferably not more than 4 carbon atoms in substituent groups.
  • aromatic hydrocarbons include, but are not limited to, benzene, toluene, xylene, ethyl benzene, iso-propyi benzene, trimethylbenzene, and tetramethylbenzene.
  • a solvent feedstream containing at least a majority of one or more of these compounds can be used in the hydroprocessmg at the predetermined hydroprocessing temperatures further described below.
  • Aromatic hydrocarbons having two aromatic rings can also be used as supercritical solvent compounds. Since these compounds tend to have higher critical temperatures, hydroprocessing can be carried out at higher temperatures such as at the predetermined temperatures further described below . Examples of these compounds include, but are not limited to naphthalene, methyl
  • the solvent component can be comprised of a mixture of aromatic and hydroaromatic molecules.
  • the solvent component can be comprised of a mixture of aromatic and hydroaromatic molecules having boiling points of from 200°F (93 C) to 750°F (399°C), or from 250°F (121°C) to 660°F (349°C), or from 300°F (149°C) to 600°F (316°C).
  • Hydroaromatic compounds having at least two rings are representative of preferred supercritical solvent compounds.
  • the preferred hydroaromatic compounds are two ring hydrocarbon compounds in which one ring is saturated and one is unsaturated. Examples of these compounds include, but are not limited to, tetralin and methyl tetralin.
  • hydrocarbons can also be employed as supercritical solvent compounds.
  • Such compounds include, but are not limited to, alicyclic
  • hydrocarbons having at least five carbon atoms such as cyclopentane, cyclohexane, cis- and transdecalin and alkylated derivatives thereof.
  • the alicyclic hydrocarbons have no more than 12 carbon atoms.
  • Additional examples include naphthenic-containing fractions of kerosene such as those fractions having an initial and final boiling points in the range of 200°F (93°C) to 750°F (399°C) and a naphthenic concentration of at least 10 wt % or at least 1 5 wt%, based on the total weight of the solvent feedstream.
  • Aliphatic hydrocarbons having at least five carbon atoms, but not more than 16 carbon atoms can also be employed. Examples of such
  • hydrocarbons include, but are not limited to, pentanes, hexanes, octanes, dodecanes and hexadecanes,
  • the solvent component has an ASTM D86 10% distillation point of at least 250°F (120°C).
  • the solvent component has an ASTM D86 10% distillation point of at least 275°F f 135°C) or at least 300°F (149°C).
  • the solvent component preferably has an ASTM D86 90% distillation point of not greater than 575°F (302°C).
  • the solvent component has an ASTM D86 90% distillation point of not greater than 550°F (288°C) or not greater than 500°F (260°C), or not greater than 450°F (232°C), or not greater than 400°F (204°C).
  • the density of the solvent component can also be determined according to ASTM D287-92(2006) Standard Test Method for API Gravity of Crude Petroleum and Petroleum Products (Hydrometer Method) in terms of API gravity.
  • API gravity of the solvent component is at most 35° in one
  • hydrocarbon oil component to produce a combined feedstock for the contacting zone of a hydroprocessing reactor.
  • a feedstock is comprised of from 30 wt% to 95 wt% of the heavy hydrocarbon oil component and from 5 wt% to 70 wt% of the solvent component, based on the total weight of the combined feed.
  • the combined feedstock is comprised of from 40 wt% to 80 wt% of the heavy hydrocarbon oil component and from 10 wt% to 60 wt% of the solvent component, based on total weight of the combined feed.
  • the solvent can be combined with the heavy hydrocarbon oil within the hydroprocessing vessel or hydroprocessing zone.
  • the solvent and heavy hydrocarbon oil can be supplied as separate streams and combined into one feed stream prior to entering the hydroprocessing vessel or
  • Suitable hydroprocessing catalysts for use in the present invention can include conventional hydroprocessing catalysts and particularly those that comprise at least one Group VIII non-noble metal, preferably Fe, Co, and/or Ni, such as Co and/or Ni; and at least one Group VI metal, preferably Mo and/or W,
  • Such hydroprocessing catalysts optionally include transition metal sulfides that are impregnated or dispersed on a refractory support or carrier such as alumina and/or silica.
  • the support or carrier itself typically has no
  • Substantially carrier- or support-free catalysts commonly referred to as bulk catalysts, generally have higher volumetric activities than their supported counterparts.
  • the catalysts used in the present invention can either be in bulk form or in supported form, in addition to alumina and/or silica, other suitable support/carrier materials can include, but are not limited to, zeolites, titania, silica-titania, and titania-alumina. It is within the scope of the present invention that more than one type of hydroprocessing catalyst can be used in one or multiple reaction vessels,
  • the at least one Group VIII non-noble metal in oxide form can typically be present in an amount ranging from about 2 wt% to about 30 wt%, preferably from about 4 wt% to about 15 wt%.
  • the at least one Group VI metal, in oxide form can typically be present in an amount ranging from about 2 wt% to about 60 wt%, preferably trom about (5 wt% to about 40 wt% or from about 10 wt% to about 30 wt%. These weight percents are based on the total weight of the catalyst.
  • a vessel or hydroprocessing zone in which catalytic activity occurs can include one or more hydroprocessing catalysts.
  • Such catalysts can be mixed or stacked, with the catalyst preferably being in a fixed bed in the vessel or hydroprocessing zone.
  • the support can be impregnated with the desired metals to form the hydroprocessing catalyst.
  • the support is heat treated at temperatures in a range of from 400°C to 1200°C, or from 450°C to 1000°C, or from 600°C to 900°C, prior to impregnation with the metals.
  • the hydroprocessing catalyst is comprised of shaped extrudates.
  • the extrudate diameters range from l/32nd to l/8 th inch, from l/20 th to I / 10 th inch, or from 120 th to l/16 lh inch.
  • the extrudates can be cylindrical or shaped. Non-limiting examples of extnidate shapes include trilobes and quadralobes.
  • the process of this invention can be effectively carried out using a hydroprocessing catalyst having any median pore diameter effective for hydroprocessing the heavy oil component.
  • the median pore diameter can be in a range of from 30 to 1000 A (Angstroms), or 50 to 500 A, or 60 to 300 A. Pore diameter is preferably determined according to ASTM
  • the hydroprocessing catalyst has a median pore diameter in a range of from 50 to 200 A.
  • the hydroprocessing catalyst has a median pore diameter in a range of from 50 to 200 A.
  • hydroprocessing catalyst has a median pore diameter in a range of from 90 to 180 A, or 100 to 140 A, or 1 10 to 130 A.
  • the hydroprocessing catalyst has a median pore diameter ranging from 50 A to 150 A.
  • the hydroprocessing catalyst has a median pore diameter in a range of from 60 A to 135 A, or from 70 A to 120 A.
  • the process of this invention is also effective with hydroprocessing catalysts having a larger median pore diameter.
  • the process can be effective using a hydroprocessing catalyst having a median pore diameter in a range of from. 180 to 500 A, or 200 to 300 A, or 230 to 250 A.
  • the hydroprocessing catalyst have a pore size distribution that is not so great as to negatively impact catalyst activity or selectivity.
  • the hydroprocessing catalyst can have a pore size distribution in which at least 60% of the pores have a pore diameter within 45 A, 35A, or 25 A of the median pore diameter.
  • the catalyst has a median pore diameter in a range of from 50 to 180 A, or from 60 to 150 A, with at least 60% of the pores having a pore diameter within 45 A, 35 A, or 25 A of the median pore diameter.
  • Pore volume should be sufficiently large to further contribute to catalyst activity or selectivity.
  • the hydroprocessing catalyst can have a pore volume of at least 0.3 cnrV ' g, at least 0.7 cm g, or at least 0.9 cnrVg, In certain embodiments, pore volume can range from 0.3-0.99 cm7g, 0.4-0.8 cm g, or 0.5-0.7 cm ' Vg.
  • the catalyst exists in shaped forms, for example, pellets, cylinders, and/or extrudates.
  • the catalyst typically has a flat plate crush strength in a range of from 50-500 N/cm, or 60-400 N/cm, or 100- 350 N/cm, or 200-300 N/cm, or 220-280 N/cm.
  • Hydroprocessing is carried out in the presence of hydrogen.
  • a hydrogen stream is, therefore, fed or injected into a vessel or reaction zone (or "hydroprocessing zone") in which the hydroprocessing catalyst is located.
  • Treat gas which is contained in a hydrogen "treat gas,” is provided to the reaction zone.
  • Treat gas can be either pure hydrogen or a hydrogen-containing gas, which is a gas stream containing hydrogen i an amount that is sufficient for the intended reaction(s), optionally including one or more other gases (e.g., nitrogen and light hydrocarbons such as methane), and which will not adversely interfere with or affect either the reactions or the products.
  • gases e.g., nitrogen and light hydrocarbons such as methane
  • Impurities such as H 2 S and NH 3 are undesirable and would typically be removed from the treat gas before it is conducted to the reactor.
  • the treat gas stream introduced into a reaction stage will preferably contain at least about 50 vol. % and more preferably at least about 75 vol. % hydrogen.
  • Hydrogen-containing treat gas can be supplied at a rate of from 300 SCF/B (standard cubic feet of hydrogen per barrel of feed) (53 S rrrVnr') to 5000 SCF/'B (891 S m7m 3 ).
  • the treat gas is provided in a range of from 1000 SCF/B (178 S mVm 3 ) to 3000 SCF/B (534 S m 3 /m 3 ).
  • Hydrogen-containing treat gas can be supplied co-currently with the heavy hydrocarbon oil and/or solvent or separately via a separate gas conduit to the hydroprocessing zone. The contact of the heavy hydrocarbon oil and solvent with the hydroprocessing catalyst and the hydrogen treat gas produces a total product that includes a hydroprocessed oil product, and, in some embodiments, gas.
  • Hydroprocessing generally refers to treating or upgrading the heavy hydrocarbon oil component that contacts the hydroprocessing catalyst
  • Hydroprocessing particularly refers to any process that is carried out in the presence of hydrogen, including, but not limited to, hydroconversion, hydrocracking, hydrogenation, hydrotreating,
  • hydroprocessing reaction is carried out in a vessel or a hydroprocessing zone in which heavy hydrocarbon and solvent contact the hydroprocessing catalyst in the presence of hydrogen,
  • Contacting conditions in the hydroprocessing zone can include, but are not limited to, temperature, pressure, hydrogen flow, hydrocarbon feed flow, or combinations thereof. Contacting conditions in some embodiments are controlled to yield a product with specific properties.
  • Temperature in the contacting zone is higher than the critical temperature of the supercritical solvent compound in the solvent component that has the highest critical temperature of all supercritical solvent compounds present in the solvent component.
  • the temperature in the contacting zone is at least 10°C, or at least 30°C, or at least 50°C higher than the critical temperature of the supercritical solvent compound in the solvent component that has the highest critical temperature of all supercritical solvent compounds present in the solvent component.
  • the temperature in the contacting zone can range from 320°F (160°C) to 900°F (482°C), or from 350°F (177°C) to 800°F (427°C), or from 500°F (260°C) to 700°F (371 °C), or from 550°F i288°C) to 650°F (343 °C). in some
  • temperature in the contacting zone can range from 560°F (293°C) to 850°F (454 C), or 660°F (349°C) to 790°F (421°C), or 680°F (360°C) to 750°F (399°C).
  • Total pressure in the contacting zone is higher than the critical pressure of the supercritical solvent compound in the solvent component that has the highest critical pressure of all supercritical solvent compounds present in the solvent component.
  • the total pressure in the contacting zone is at least 10 psig (69 kPa-g), or at least 20 psig (138 kPa-g), or at least 30 psig (207 kPa-g) higher than the critical pressure of the supercritical solvent compound in the solvent component that has the highest critical pressure of all supercritical solvent compounds present in the solvent component.
  • the total pressure in the contacting zone can range from 600 psig (4137 kPa-g) to 3000 psig (20684 kPa-g), more preferably from 650 psig (4482 kPa-g) to 2000 psig (13790 kPa-g), and most preferably from 800 psig (5516 kPa-g) to 1500 psig (10342 kPa-g).
  • Liquid hourly space velocity (LHS V) of the combined heavy hydrocarbon oil and solvent components will generally range from 0.1 to 30 h ! , or 0.4 IT 1 to 25 IT', or 0.5 to 20 h "J . In some embodiments, LHSV is at least 15 h " 1 , or at least 10 h "1 , or at least 5 IT 1 .
  • Partial pressure of hydrogen in the contacting zone can range from 550 psig (3792 kPa-g) to 3000 psig (20684 kPa-g),
  • the contacting of - zz ⁇ the combined feed with hydroprocessmg catalyst in the presence of hydrogen is carried out at a hydrogen partial pressure of from 650 psig (4482 kPa-g) to 2000 psig (13790 kPa-g), and more preferably from 800 psig (55 16 kPa-g) to 1500 psig (10342-g).
  • the hydroprocessed product will be a material or crude product that exhibits reductions in such properties as average molecular weight, boiling point range, density and/or concentration of sulfur, nitrogen, oxygen, and metals.
  • contacting the heavy hydrocarbon oil and solvent with the hydroprocessmg catalyst in the presence of hydrogen to produce a hydroprocessed product is carried out in a single contacting zone. In another embodiment, contacting is carried out in two or more contacting zones.
  • the total hydroprocessed product can be separated to form one or more particularly desired liquid products and one or more gas products.
  • the liquid product is blended with a
  • hydrocarbon feedstock that is the same as or different from the heavy
  • the liquid hydroprocessed product can be combined with a hydrocarbon oil having a different viscosity, resulting in a blended product having a viscosity that is between the viscosity of the liquid hydroprocessed product and the viscosity of the heavy hydrocarbon oil component.
  • the hydroprocessed product and/or the blended product are transported to a refinery and distilled to produce one or more distillate fractions.
  • the distillate fractions can be catalytically processed to produce commercial products such as transportation fuels, lubricants, or chemicals.
  • the hydroprocessed product has a total Ni/V/Fe content of at most 50%, or at most 10%, or at most 5%, or at most 3%, or at most 1 % of the total Ni/V/Fe content of the heavy hydrocarbon oil component.
  • the fraction of the hydroprocessed product that has a boiling point of 650°F (343°C) and higher i.e., 650°F+ (343°C+) product fraction
  • the 650°F+ (343°C+) product fraction has not greater than 4x ] () grams of Ni/V/Fe (40 ppm).
  • the hydroprocessed product has an API gravity that is 100- 160%, or 1 10-140% of that of the heavy hydrocarbon oil component.
  • API gravity of the hydroprocessed product is from 10°-40 °, or 12°-35°, or 14°-30°.
  • the hydroprocessed product has a viscosity of at most 90%, or at most 80%, or at most 70% of that of the heavy hydrocarbon oil component. In some embodiments, the viscosity of the hydroprocessed product is at most 90% of the viscosity of the heavy hydrocarbon oil component, while the API gravity of the hydroprocessed product is 100-160%, or 105-155%, or 1 10-150% of that of the heavy hydrocarbon oil component.
  • the 650°F+ (343°C+) product fraction can have a viscosity at 100°C of 10 to 150 est, or 15 to 120 est, or 20- 100 est. Most atmospheric resids of crude oils range from 40 to 200 est. In certain embodiments, 650°F+ (343°C+) product fraction lias a viscosity of at most 90%, or at most 50%, or at most 5% of that of the heavy hydrocarbon oil component.
  • the hydroprocessed product has a total heteroatom (i.e., S/N/O) content of at most 50%, or at most 10%, or at most 5% of the total heteroatom content of the heavy hydrocarbon oil component.
  • a total heteroatom i.e., S/N/O
  • the sulfur content of the hydroprocessed product is at most 50%, or at most 10%, or at most 5% of the sulfur content of the heavy hydrocarbon feedstock.
  • hydroprocessed product is at most 50%, or at most 10%, or at most 5% of that of the heavy hydrocarbon feedstock, and the hydroprocessed product has a total oxygen content that is at most 75%, or at most 50%, or at most 30%, or at most 10%, or at most 5% of the total oxygen content of the heavy hydrocarbon oil component.
  • a fixed bed, downflow reactor was constructed from 3/8 ih inch stainless steel tubing. Two 50 cm brass half cylinders were bolted onto the 3/8* inch tube. The volume of the hot zone inside the brass cylinder was 16.0 cc's.
  • the reactor was loaded with 5 cc of a supported NiMo hydroprocessing catalyst on top of 8 cc of an unsupported NiMoW hydroprocessing catalyst.
  • the supported NiMo catalyst was used primarily for removing metals from heavy oil feedstocks.
  • the catalyst system was sulfided using a feedstock comprised of 80 wt% 130-neutral lube oil/20 wt% ethyl-disulfide.
  • the feedstock was fed at 3000 SCF/B (standard cubic feet of hydrogen per barrel of feed), 644°F (340°C), 0.2 LHSV, and 1000 psig (6895 kPa-g) for 48 hours.
  • the feedstock was then switched to 60 wt% Athabasca bitumen/40 wt% trimethylbenzene (TMB).
  • TMB trimethylbenzene
  • Reaction conditions were changed to 800 psig (5516 kPa-g), 5 cc/lir liquid feed, and 1 100 SCF/B hydrogen (197 S m 3 /m J ).
  • the reactor temperature was varied between 689°F (365°C) and 780°F (416°C).
  • the Athabasca bitumen had the following properties: 4.8 wt% S, 5000 ppm N, 55% 450°F (232°C) to 1050°F(566°C), 45 wt% 1050°F+ (566°C+) fraction, 0.9950 specific gravity at 60°F, 67 wppm Ni, 166 wppm V, and 13 wppm Fe.
  • the hydrodesulfurization and hydrodemetallization levels were typically held between 60 and 70% through temperature adjustment.
  • the deposition of metals in the reactor was tracked with time. For example, at the time that the catalyst had accumulated 5 wt% metals, the conditions were 800 psig (5516 kPa-g) and 725°F (385°C). Less than 1 wt% of the TMB was hydrogenated and/or hydrocracked.
  • the catalyst was run for 150 days. Its FIDS activity dropped by less than 1% over a 3-week period at a temperature as high as 780°F (416°C). The run was voluntarily terminated to enable examination of the metals distribution on the catalyst before metal loading filled any more of the catalyst void volume.
  • the total metal loading on the catalyst was 14 wt%.
  • the catalysts were analyzed for vanadium profile in the extrudates.
  • the vanadium deposit across whole extrudates was found to be evenly deposited throughout the extrudate on both catalysts, indicative of insignificant pore mouth plugging.
  • Analysis of the spent catalysts showed that the metals uptake of both catalysts were similar- close to 0.14 g metal/cc of catalyst.
  • This example demonstrates that upgrading of Athabasca bitumen in the presence of TMB at a moderate pressure of 800 psig (5516 kPa-g) can be achieved for an extended period of time without reactor plugging problems. Moreover, there is little metal buildup inside catalyst pores.
  • TMB is a supercritical fluid. As such, it helps reduce oil viscosity and hence accelerate diffusion rate inside catalyst particles.
  • a supercritical solvent also changes the phase behavior around the catalyst particles by reducing the tendency of forming two incompatible liquid phases during the reaction, thus mitigating the deposition and accumulation of carbonaceous species on the catalyst.
  • the feedstock and catalyst used in Examples 2-4 were a Basrah atmospheric resid and a supported Co-Mo catalyst.
  • the following solvents were used: trimethyibenzene (TMB) and methyinaphthalene (MN).
  • TMB trimethyibenzene
  • MN methyinaphthalene
  • Table 1 shows the properties of the Basrah atmospheric resii ⁇ able 1
  • a base case run was conducted with neat Basrah resid (i.e., 100% resid, no solvent) as described above for this Example.
  • Figure 1 shows the performance of the catalyst.
  • the catalyst was on stream for 18 days with decreasing activities for 1050°F+ (566°C+) fraction conversion, HDM, ITDS, and HDN. After 18 days, the run was forced to shut down due to excessive reactor pressure drop.
  • Example 3
  • TMB trimethylbenzene
  • the reactor temperature was raised to 752°F (400°C) after 40 days and then to 797°F (425°C) after 62 days.
  • the consequent increases in ! 050°F+ (566°C+) fraction conversion, HDM, HDS, and HDM can be seen in Fig. 2.
  • the reactor temperature was further increased to 842 °F (450°C). After 3 days at this temperature, the ran was terminated due to reactor plugging.
  • Figure 2 also shows the catalyst performance with the 60/40 resid/TMB feed. This run was on stream for 82 days, much longer than the base case ran as shown in Example 2.
  • the TMB-as-solvent experiment permits scanning a temperature range of 725°F (385°C) to 842°F (450°C), whereas the no-solvent run (Example 2) was restricted to 725°F (385°C) due to operability problem.
  • the results disclosed in Examples 1 -3 show that the presence of a supercritical solvent significantly increases a catalyst's productivity by prolonging its run length.
  • part of the solvent may be fed to the reactor via interbed quench zones. This would allow the solvent to help control reaction exothermicity (adiabatic temperature rise) and improve the liquid flow distribution in the reactor bed.
  • the use of the appropriate light aromatic solvent has the additional benefit because of relatively straightforward separation and solvent recycle.

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  • Engineering & Computer Science (AREA)
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  • General Chemical & Material Sciences (AREA)
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Abstract

Cette invention concerne un procédé de production d'un produit hydrotraité. L'invention est particulièrement avantageuse en ce qu'elle permet d'atteindre une longueur d'exploitation supérieure à celle des méthodes d'hydrotraitement classiques. Cet avantage est atteint grâce à l'utilisation d'un solvant particulier tel qu'un composant de co-charge, notamment, le composant solvant étant constitué d'au moins un ou plusieurs composés solvants supercritiques.
EP12762124.1A 2011-08-31 2012-08-30 Utilisation de fluide supercritique dans l'hydrotraitement d'hydrocarbures lourds Withdrawn EP2751230A2 (fr)

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WO2013033298A3 (fr) 2013-04-25

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