EP3535355A1 - Process for producing lighter distillates - Google Patents
Process for producing lighter distillatesInfo
- Publication number
- EP3535355A1 EP3535355A1 EP17867017.0A EP17867017A EP3535355A1 EP 3535355 A1 EP3535355 A1 EP 3535355A1 EP 17867017 A EP17867017 A EP 17867017A EP 3535355 A1 EP3535355 A1 EP 3535355A1
- Authority
- EP
- European Patent Office
- Prior art keywords
- metal
- catalyst
- reactor
- separator
- hydroprocessing
- 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.)
- Pending
Links
Classifications
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- 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
- C10G45/14—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 with moving solid particles
- C10G45/16—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 with moving solid particles suspended in the oil, e.g. slurries
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- 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
- C10G47/02—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions characterised by the catalyst used
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- 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
- C10G25/00—Refining of hydrocarbon oils in the absence of hydrogen, with solid sorbents
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- 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
- C10G31/10—Refining of hydrocarbon oils, in the absence of hydrogen, by methods not otherwise provided for with the aid of centrifugal force
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- 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
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- 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
- C10G45/04—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 characterised by the catalyst used
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- 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
- C10G45/04—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 characterised by the catalyst used
- C10G45/06—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 characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof
- C10G45/08—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 characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof in combination with chromium, molybdenum, or tungsten metals, or compounds thereof
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- 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
- C10G45/04—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 characterised by the catalyst used
- C10G45/10—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 characterised by the catalyst used containing platinum group metals or compounds thereof
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- 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
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- 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
- C10G47/02—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions characterised by the catalyst used
- C10G47/10—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions characterised by the catalyst used with catalysts deposited on a carrier
- C10G47/12—Inorganic carriers
- C10G47/14—Inorganic carriers the catalyst containing platinum group metals or compounds thereof
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- 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
- C10G49/00—Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups C10G45/02, C10G45/32, C10G45/44, C10G45/58 or C10G47/00
- C10G49/02—Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups C10G45/02, C10G45/32, C10G45/44, C10G45/58 or C10G47/00 characterised by the catalyst used
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- 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
- C10G2300/10—Feedstock materials
- C10G2300/1037—Hydrocarbon fractions
- C10G2300/1048—Middle distillates
- C10G2300/1055—Diesel having a boiling range of about 230 - 330 °C
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- 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
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- 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
- C10G2300/4093—Catalyst stripping
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- 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
- C10G2300/70—Catalyst aspects
- C10G2300/706—Catalytic metal recovery
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- 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
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/02—Gasoline
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- 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
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/04—Diesel oil
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- 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
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/06—Gasoil
Definitions
- the present subject matter relates to hydroprocessing and, in particular, to a process for hydroprocessing distillates in the range of naphtha to vacuum gas oils in slurry phase.
- Hydroprocessing is widely used to improve quality of products obtained during crude oil refining. For instance, hydrotreating is carried out to remove Sulfur and Nitrogen from hydrocarbon feedstock in treating units. Similarly, hydrocracking is carried out to convert heavy hydrocarbons into lighter and more valuable hydrocarbons. Hydrotreating and hydrocracking reactions are generally carried out in fixed bed reactors. Solid catalysts of different shapes are loaded into the fixed bed reactors to form number of beds separated by a quench system to carry out the reactions for Hydroprocessing.
- Figure 1 illustrates a block diagram of a hydroprocessing unit, in accordance with an example of the present subject matter.
- Figure 2 illustrates a block diagram of a hydroprocessing unit, in accordance with another example of the present subject matter.
- Figure 3 illustrates a block diagram of a hydroprocessing unit, in accordance with yet another example of the present subject matter.
- Figure 4 illustrates a block diagram of a hydroprocessing unit, in accordance with yet another example of the present subject matter.
- Figure 5 illustrates a method for producing lighter distillates in a hydroprocessing unit, in accordance with yet another example of the present subject matter.
- the present subject matter describes a process of producing lighter distillates.
- the process includes hydroprocessing of hydrocarbons in the range of naphtha to vacuum gas oils in slurry phase.
- the lighter distillates are produced by performing hydrotreating and/or hydrocracking reactions in a hydroprocessing unit.
- the hydroprocessing unit is to carry out hydroprocessing reactions in a slurry phase with active catalysts in dispersed mode.
- the active catalyst may be an organometallic based catalyst comprising a metal selected from a predetermined group of metals.
- the organometallic based catalyst may comprise a metal selected from the group consisting of titanium, molybdenum, vanadium, chromium, manganese, iron, cobalt, nickel, zirconium, tungsten, ruthenium, rhodium, tin, tantalum, rhenium, and iridium.
- the amount of metal in the catalyst used for hydroprocessing of the hydrocarbons may be in the range of 0.001% to 10% by weight.
- the hydroprocessing unit includes a reactor system, a feed vessel for providing feed to the reactor system, a catalyst storage tank for providing a catalyst to the feed vessel, separators for separation of gaseous and liquid products obtained from the reactor system, and a fractionator for separation of different fractions of the product.
- the reactor system can be selected from a group consisting of continuous stirred tank reactor, ebullated bed reactor, slurry bubble column reactor or combinations thereof.
- the reactor system comprises of reactors in a configuration selected from the group consisting of series, parallel and series-parallel.
- a predetermined amount of the organometallic based catalyst may be mixed with a predetermined amount of the hydrocarbon feed present in the feed vessel.
- the mix of organometallic based catalyst and the hydrocarbon feed may then be provided along with Hydrogen gas to the reactor system at a predetermined pressure.
- the hydrocarbon feed and the Hydrogen gas is then allowed to react in presence of the active metals in the catalysts at a predetermined temperature and pressure, for a predetermined time period.
- the products, thus obtained are processed by the separators to separate gaseous and liquid products and further remove dissolved gases from the liquid products. Subsequently, the liquid products are provided to the fractionator for fractionation to obtain different products.
- metal capture units can be used to capture and re-use the metal from the catalyst, as will be described in detail with reference to the figures.
- the present subject matter thus provides a process of producing lighter distillates in the range of naphtha to vacuum gas oils in slurry phase.
- the distillates are produced in a hydroprocessing unit that facilitates hydroprocessing of hydrocarbon feedstocks in a slurry phase with active catalysts in dispersed mode.
- Hydroprocessing the feedstock in a slurry phase instead of a fixed bed reactor helps in providing efficient reaction between the hydrocarbon feedstock and the hydrogen gas in the presence of the active metal in the active catalyst.
- the active catalyst is dispersed in the liquid hydrocarbon feedstock to form a slurry, the feedstock is efficiently able to come in contact with the metal.
- FIG. 1 illustrates a block diagram of a hydroprocessing unit 102, in accordance with an example of the present subject matter.
- the hydroprocessing unit 102 includes a catalyst storage tank 104, a feed vessel 106, a reactor system 108, a first separator 110, a second separator 112, and a fractionator 114.
- the hydroprocessing unit 102 may include various other intermediate sub-units that may be utilized for hydroprocessing, however, for the sake of brevity and not as a limitation, only the aforementioned sub-units are described and shown in the figure.
- the reactor system 108 is in fluid connection with the feed vessel 106 and the first separator 110.
- the first separator 110 is a high- pressure separator and the second separator 112 is a low-pressure separator.
- a hydrogen gas supply unit 116 may be connected to the reactor system 108 for providing the hydrogen for hydroprocessing.
- the hydroprocessing unit 102 may be implemented for performing hydrotreating and/or hydrocracking reactions of hydrocarbon feedstock ranging from naphtha to vacuum gas oil.
- the hydrocarbon feed comprises of hydrocarbons boiling above 60 °C.
- the hydroprocessing unit 102 may use an organometallic based catalyst comprising a metal selected from the group consisting of titanium, molybdenum, vanadium, chromium, manganese, iron, cobalt, nickel, zirconium, tungsten, ruthenium, rhodium, tin, tantalum, rhenium, and iridium.
- the amount of metal in the catalyst used for hydrotreating the hydrocarbons may be in the range of 0.001 % to 10% by weight. Further, the metal content in the catalyst may range from 1% to 35 %.
- the hydroprocessing unit 102 may be operated at a temperature in the range of 100 °C to 450 °C depending on the feed and the catalyst.
- the hydroprocessing unit 102 may be operated at a pressure in the range of 10 bar to 250 bar depending on the feed and the catalyst.
- a predetermined amount of an organometallic based catalyst is obtained from the catalyst storage tank 104 and mixed with a predetermined amount of feed obtained from the feed vessel 106.
- the catalyst and the feed may be mixed in one of a static line mixer (not shown in the figure) or a mixing tank (not shown in the figure) before the mix enters into the reactor system 108.
- the mix of catalyst and the feed may then be transferred to the reactor system 108.
- the hydrogen gas may be fed to the reactor system 108 at a predetermined pressure.
- the feed and the hydrogen gas subsequently react in the presence of the catalyst at a predetermined temperature for a predetermined time period.
- the reaction may be carried out under hydrogen atmosphere at a temperature in the range of 100 °C to 450 °C and at a pressure in the range of 10 bar to 250 bar for a time ranging from 15 minutes to 4 hours.
- the organometallic catalyst decomposes to release the active metal.
- the metal in the reactant mixture acts as the catalyst for hydroprocessing resulting in the cracking of heavy hydrocarbons into lighter distillates.
- a product stream having the products obtained as a result of the reaction is subsequently transferred to the first separator 110 to separate gas products and liquid products.
- the separation happens by virtue of Thermodynamic flash at predetermined temperature and pressure maintained within the first separator 110.
- the first separator is operated in a temperature range of 200 to 250 deg C and in a Pressure range of 180-200 bar.
- the gas products may include dry gas and LPG. Dry gas may be routed to hydrogen recovery section for hydrogen separation. The recovered hydrogen may be recycled back to the reaction zone.
- the liquid products are further transferred to the second separator 112 to remove dissolved gases from the liquid products. The gases, thus obtained, are then removed from the second separator 112 for further treatment, while the liquid products are moved to the fractionator 114.
- the separation in the second separator 112 happens by virtue of Thermodynamic flash at predetermined temperature and pressure maintained within the second separator 112.
- the second separator 112 is operated in a temperature range of 25 to 30 deg C and in a Pressure range of 1-2 bar.
- the fractionator 114 may perform fractionation to separate product fractions from the liquid product based on their boiling point range to obtain various fractions of the product.
- the products obtained from fractionator may be mixtures of Naphtha, Kerosene, Diesel, and Vacuum Gas Oil.
- the operating conditions of the fractionator can be appropriately selected depending on the products to be obtained, as will be understood.
- the metal from the catalyst remains in the liquid product streams that are taken out from the different separators.
- the present subject matter provides for metal capture, such as using adsorption or centrifugation, for separating out the metals from the hydroprocessed products.
- the metals adsorbed on the adsorbents may be further put to re-use as a catalyst in the reactor leading to a reduction in the requirement of make-up catalyst. Further, the amount of metal discarded as waste is substantially reduced.
- Various example schemes for metal capture will now be described.
- FIG. 2 illustrates a block diagram of the hydroprocessing unit 102, in accordance with another example of the present subject matter.
- the hydroprocessing unit 102 in accordance with the current embodiment further includes a metal capture unit 202 coupled to the reactor system 108.
- the metal capture unit 202 is provided to remove metals from the products obtained from the reactor system 108.
- a predetermined amount of a catalyst is obtained from the catalyst storage tank 104 and mixed with a predetermined amount of feed obtained from the feed vessel 106.
- the mix of catalyst and the feed may then be transferred to the reactor system 108.
- the hydrogen gas may be transferred to the reactor system 108 at a predetermined pressure.
- the feed and the hydrogen gas may then be allowed to react in the presence of the catalyst at a predetermined temperature for a predetermined time period.
- a product stream having the products obtained as a result of the reaction is subsequently transferred to the metal capture unit 202.
- the metal capture unit 202 may implement a separation process for separating metals from the product stream.
- the separation process may be one of an adsorption process and a centrifugal process.
- the metal capture unit 202 may be implemented as a centrifuge.
- the metal capture unit 202 may thus perform the separation process such that the product stream is separated into a lighter portion stream and a heavier portion stream.
- the heavier portion stream that includes the metals may be transferred back to the reactor system 108 while the lighter portion stream is transferred to the first separator 110 for the separation of gas and liquid products.
- the metal capture unit 202 may be implemented as an adsorption unit employing an adsorption bed with active adsorbents. As the product stream is received by the metal capture unit 202, the metals are adsorbed on the adsorbents. The adsorption may occur as a result of one or both of physical adsorption and chemical adsorption.
- a relatively metal free hydrocarbon product stream, thus obtained, is transferred to the first separator 110.
- a metal loaded stream of adsorbents obtained owing to the adsorption may be transferred to the reactor system 108 as an additional catalyst for the reactions.
- a portion of the metal loaded stream of adsorbents may be recycled to the reactor while the other portion may be sent for metal recovery.
- the ratio of the metal loaded stream recycled may depend on the extent of adsorption which occurs and can be changed suitably as will be understood.
- the metal from the metal loaded adsorbents may be leached away, for example, by contact with a hydrocarbon. In one example, the leaching may be performed using fresh diesel. The recovered metal may be again used in the reaction or may be used as reclaimed metal.
- the product stream from the reactor 108 may be sent to a filtration system (not shown in diagram) to remove spent adsorbents, i.e., metal loaded adsorbents, before transferring to metal capture unit 202, which is filled with fresh adsorbents. Alternatively, the metal loaded adsorbents may be regenerated to reclaim metals without being transferred to the reactor system 108.
- the adsorbent employed in the metal capture unit may employ any commercial adsorbent that can adsorb the metals and can be selected from a group consisting of activated carbon derived from hard woods, soft woods and rice husks, functionalized activated carbon obtained from refinery residues like delayed coker pitch, slurry hydrocracking pitch and Bituminous tar, lignite coal, ion-exchange resins, carbon nanotubes, graphene, carbon black, functionalized carbon obtained after carbonization of rubber tires and coconut coir, zeolites, alumino-silicates, silica light, ZSM-5, modernite, carbon molecular sieves and clays such as bentonite and kaolin.
- any commercial adsorbent that can adsorb the metals and can be selected from a group consisting of activated carbon derived from hard woods, soft woods and rice husks, functionalized activated carbon obtained from refinery residues like delayed coker pitch, slurry
- the first separator 110 processes the product stream to separate gas products and liquid products.
- the liquid products are further transferred to the second separator 112 to remove dissolved gases from the liquid products.
- the gases, thus obtained, are then removed from the second separator 112 for further treatment, while the liquid products are moved to the fractionator 114.
- the fractionator 114 may perform fractionation to separate product fractions from the liquid product based on their boiling point range to obtain various distillates.
- the operating conditions of the various units, such as reactor, separators, and fractionator may be similar to those described earlier.
- FIG 3 illustrates a block diagram of the hydroprocessing unit 102, in accordance with yet another example of the present subject matter.
- the hydroprocessing unit 102 in accordance with the current embodiment, further includes the metal capture unit 202 coupled to the first separator 110 and the reactor system 108.
- the metal capture unit 202 is provided to remove metals from the liquid products obtained from the first separator 110.
- FIG. 4 illustrates a block diagram of the hydroprocessing unit 102, in accordance with yet another example of the present subject matter.
- the hydroprocessing unit 102 in accordance with the current embodiment, further includes the metal capture unit 202 coupled to the second separator 112, the reactor system 108, and the fractionator 114.
- the metal capture unit 202 is provided to remove metals from the liquid products obtained from the second separator 112.
- metal capture is conducted after the further separation of the lighter fractions from the hydroprocessed products. Metal removal is done here after most of the volatile or lighter fractions have been separated out from the heavier portion left behind.
- the operating conditions of the various units, such as reactor, separators, and fractionator, may be similar to those described earlier.
- Figure 5 illustrates a method 500 for producing lighter distillates in a hydroprocessing unit, in accordance with yet another example of the present subject matter.
- the order in which the method 500 is described is not intended to be construed as a limitation, and any number of the described method blocks may be combined in any order to implement the aforementioned methods, or an alternative method. Further, the method may be performed in a hydroprocessing unit, such as the hydroprocessing unit 102.
- an organometallic based catalyst and a predetermined amount of feed are mixed to obtain a first mix.
- the organometallic based catalyst comprising a metal selected from the group consisting of titanium, molybdenum, vanadium, chromium, manganese, iron, cobalt, nickel, zirconium, tungsten, ruthenium, rhodium, tin, tantalum, rhenium, and iridium.
- the feed may be a hydrocarbon feed.
- the catalyst and the feed may be mixed in one of a static line mixer (not shown in the figure) or a mixing tank (not shown in the figure).
- the first mix and hydrogen gas are fed in a reactor system.
- the hydrogen may be mixed with the first mix before entering into the reactor system.
- the hydrogen gas and the feed are allowed to react in the presence of the catalyst at a predetermined temperature to obtain reaction products.
- the temperature may be maintained in the range of 100 °C to 450 °C.
- a product stream having the reaction products is transferred to separators to obtain gaseous and liquid products.
- the liquid products are further processed to separate gas dissolved in the liquid products.
- metal may be captured from at least one of the product stream and one or more liquid product streams, for example, as per the schemes described in figures 2-4 earlier.
- the liquid products are transferred to a fractionator for fractionation.
- the fractionator may perform fractionation to separate product fractions from the liquid product to obtain lighter distillates including Naphtha, Kerosene, Diesel, and Vacuum Gas Oil.
- Example 1 Slurry phase diesel hydrotreating with no catalyst
- the example 1 illustrates the slurry phase hydrotreating of sour diesel in the presence of hydrogen without catalyst.
- 300ml of sour diesel was taken in a batch reactor.
- the reactor was purged with nitrogen to remove any air trapped inside and later it was pressurized with Hydrogen to attain a pressure of 40 bar.
- the reaction mixture was heated to 340 °C, under continuous stirring at 500 rpm.
- the reaction temperature was maintained for 1 hour.
- chilled water was circulated to bring down the temperature to 30°C.
- the gaseous products were collected in a gas bomb.
- the liquid sample was collected and analyzed in Micro Distillation Unit as per ASTM D-7345. Density measurement and Sulphur analysis was also conducted for both the feed diesel as well as the products.
- Tables 1 and 2 as shown herein:
- Example 2 Slurry phase diesel hydrotreating at 40 bar Pressure of Hydrogen with Iron-based catalyst
- the example 2 illustrates the slurry phase hydrotreating of sour diesel in the presence of hydrogen using SCAT- 106 * as a catalyst precursor which is an Iron-based organometallic catalyst.
- SCAT- 106 * as a catalyst precursor which is an Iron-based organometallic catalyst.
- 300ml of sour diesel and 1000 ppm of SCAT- 106 were taken in a batch reactor.
- the reactor was purged with nitrogen to remove any air trapped inside and later it was pressurized with Hydrogen to attain a pressure of 40 bar.
- the reaction mixture was heated to 340 °C, under continuous stirring at 500 rpm. Heating was continued for 1 hour. After 1 hour, the reaction was quenched by circulating chilled water to bring down the temperature to 30°C.
- the gaseous products were collected in a gas bomb.
- Example 3 Slurry phase diesel hvdrotreating at 60 bar Pressure of Hydrogen with Molybdenum-based catalyst
- the example 3 illustrates the slurry phase hydrotreating of sour diesel in the presence of hydrogen using SOSCAT-9 as a catalyst which is a Molybdenum- based organometallic catalyst.
- SOSCAT-9 a catalyst which is a Molybdenum- based organometallic catalyst.
- 50 grams of sour diesel, 10000 ppm of SOSCAT-9 and 0.5 g of Dimethyl disulfide (for sulfiding of the catalyst) was taken in a batch reactor.
- the reactor was purged with nitrogen to remove any air trapped inside and later it was pressurized with Hydrogen to attain a pressure of 60 bar.
- the reactor with the reaction mixture was heated to a temperature of about 320 °C.
- the reaction mixture was then cooled down and the reactor was de-pressurized.
- Example 4 Slurry phase diesel hydrotreating of partially hydrotreated diesel
- the example 4 illustrates the slurry phase hydrotreating of partially hydrotreated diesel in the presence of hydrogen using SOSCAT-9 as a catalyst which is a Molybdenum-based organometallic catalyst.
- SOSCAT-9 a catalyst which is a Molybdenum-based organometallic catalyst.
- 50 grams of sour diesel, 10000 ppm of SOSCAT-9 and 0.5 g of Dimethyl disulfide (for sulfiding of the catalyst) was taken in a batch reactor. The reactor was purged with nitrogen to remove any air trapped inside and later it was pressurized with Hydrogen to attain a pressure of 60 bar. Pre-sulfidation of the catalyst was conducted at 340 °C. The reaction mixture was then cooled down and the reactor was de-pressurized.
- Example 5 Slurry phase diesel hydrotreating of diesel along with adsorption for metal capture
- the example 5 illustrates the slurry phase hydrotreating of sour diesel in the presence of hydrogen using Iron-based organometallic catalyst followed by adsorption operation with Alumina powder.
- 250 grams of sour diesel and 50000 ppm of Iron-based organometallic catalyst was taken in a batch reactor. The reactor was purged with nitrogen to remove any air trapped inside and later it was pressurized with Hydrogen to attain a pressure of 60 bar. The reaction mixture was then heated to 340 °C, under continuous stirring at 500 rpm. Heating was continued for 1 hour. After 1 hour, the reaction was quenched by circulating chilled water to bring down the temperature to 30°C. The gaseous products were collected in a gas bomb. The liquid sample was collected and analyzed for metals using ICP-MS.
- Alumina powder was then taken in a batch reactor followed by addition of the liquid sample which was collected after reaction. This was done for metal capture by adsorption, for example, as per the process of Figure 3 described earlier.
- the liquid sample with Alumina powder was heated to 340 °C, under continuous stirring at 500 rpm. Heating was continued for 1 hour. After 1 hour, the reaction was quenched by circulating chilled water to bring down the temperature to 30°C.
- the liquid product was collected and analyzed for metals using ICP-MS.
- Table 9 The results of the experiment of example 5 are summarized in Table 9, as shown herein:
Abstract
Description
Claims
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PCT/IN2017/050514 WO2018083715A1 (en) | 2016-11-07 | 2017-11-07 | Process for producing lighter distillates |
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US3165463A (en) * | 1962-07-02 | 1965-01-12 | Universal Oil Prod Co | Hydrorefining of crude oil and catalyst therefor |
US3622503A (en) * | 1970-03-02 | 1971-11-23 | Universal Oil Prod Co | Hydrogen transfer agents for slurry processing of hydrocarbonaceous black oils |
US3720602A (en) * | 1971-02-26 | 1973-03-13 | Exxon Research Engineering Co | Water injection in a hydrodesulfurization process |
US4066530A (en) * | 1976-07-02 | 1978-01-03 | Exxon Research & Engineering Co. | Hydroconversion of heavy hydrocarbons |
US4578181A (en) * | 1984-06-25 | 1986-03-25 | Mobil Oil Corporation | Hydrothermal conversion of heavy oils and residua with highly dispersed catalysts |
US5028313A (en) * | 1987-07-23 | 1991-07-02 | Uop | Process for treating a temperature-sensitive hydrocarbonaceous stream containing a non-distillable component to produce a distillable hydrocarbonaceous product |
US4943548A (en) * | 1988-06-24 | 1990-07-24 | Uop | Method of preparing a catalyst for the hydroconversion of asphaltene-containing hydrocarbonaceous charge stocks |
US4888104A (en) * | 1988-09-06 | 1989-12-19 | Intevep, S.A. | Catalytic system for the hydroconversion of heavy oils |
US5171727A (en) * | 1991-08-26 | 1992-12-15 | Uop | Method of preparing a catalyst for the hydroconversion of asphaltene-containing hydrocarbonaceous charge stocks |
US5298152A (en) * | 1992-06-02 | 1994-03-29 | Chevron Research And Technology Company | Process to prevent catalyst deactivation in activated slurry hydroprocessing |
US6162350A (en) * | 1997-07-15 | 2000-12-19 | Exxon Research And Engineering Company | Hydroprocessing using bulk Group VIII/Group VIB catalysts (HEN-9901) |
JP2003247028A (en) * | 2001-11-21 | 2003-09-05 | Shipley Co Llc | Method for recovering catalytic metal |
WO2005056728A2 (en) * | 2003-12-05 | 2005-06-23 | Exxonmobil Research And Engineering Company | Two-stage hydrotreating process for diesel fuel |
ES2585891T3 (en) * | 2004-04-28 | 2016-10-10 | Headwaters Heavy Oil, Llc | Boiling bed hydroprocessing methods and systems |
US8372266B2 (en) * | 2005-12-16 | 2013-02-12 | Chevron U.S.A. Inc. | Systems and methods for producing a crude product |
US8097149B2 (en) * | 2008-06-17 | 2012-01-17 | Headwaters Technology Innovation, Llc | Catalyst and method for hydrodesulfurization of hydrocarbons |
US7897035B2 (en) * | 2008-09-18 | 2011-03-01 | Chevron U.S.A. Inc. | Systems and methods for producing a crude product |
US9284494B2 (en) * | 2008-11-15 | 2016-03-15 | Uop Llc | Solids management in slurry hydroprocessing |
US8178461B2 (en) * | 2008-12-30 | 2012-05-15 | Chevron U.S.A. Inc | Thermal treatment processes for spent hydroprocessing catalyst |
EP2404981A1 (en) * | 2010-07-06 | 2012-01-11 | Total Raffinage Marketing | Slurry catalyst and slurry flakes valorization |
US9163183B2 (en) * | 2012-11-21 | 2015-10-20 | Reg Synthetic Fuels, Llc | Removal of solubilized metals from Fischer-Tropsch products |
WO2014199389A1 (en) * | 2013-06-14 | 2014-12-18 | Hindustan Petroleum Corporation Limited | Hydrocarbon residue upgradation process |
US10857532B2 (en) * | 2015-03-30 | 2020-12-08 | Council Of Scientific & Industrial Research | Slurry phase organic-inorganic fused hybrid catalyst for residue hydroprocessing and process for preparation thereof |
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- 2017-11-07 US US16/347,785 patent/US20190330543A1/en active Pending
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WO2018083715A1 (en) | 2018-05-11 |
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