US20160068760A1 - Process for treating a hydrocarbon-based heavy residue - Google Patents

Process for treating a hydrocarbon-based heavy residue Download PDF

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Publication number
US20160068760A1
US20160068760A1 US14/783,985 US201314783985A US2016068760A1 US 20160068760 A1 US20160068760 A1 US 20160068760A1 US 201314783985 A US201314783985 A US 201314783985A US 2016068760 A1 US2016068760 A1 US 2016068760A1
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process according
residue
heavy hydrocarbon
weight
based residue
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Giuseppe Belmonte
Alberto Maria Antonio MALANDRINO
Vincenzo Piccolo
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Eni SpA
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Eni SpA
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Assigned to ENI S.P.A. reassignment ENI S.P.A. ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: BELMONTE, GIUSEPPE, MALANDRINO, Alberto Maria Antonio, PICCOLO, VINCENZO
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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
    • C10G7/00—Distillation of hydrocarbon oils
    • C10G7/06—Vacuum distillation
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10C—WORKING-UP PITCH, ASPHALT, BITUMEN, TAR; PYROLIGNEOUS ACID
    • C10C3/00—Working-up pitch, asphalt, bitumen
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10C—WORKING-UP PITCH, ASPHALT, BITUMEN, TAR; PYROLIGNEOUS ACID
    • C10C3/00—Working-up pitch, asphalt, bitumen
    • C10C3/06—Working-up pitch, asphalt, bitumen by distillation
    • 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
    • C10G31/06—Refining of hydrocarbon oils, in the absence of hydrogen, by methods not otherwise provided for by heating, cooling, or pressure treatment
    • 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
    • C10G47/24—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions with moving solid particles
    • C10G47/30—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions with moving solid particles according to the "fluidised-bed" technique
    • 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
    • C10G49/04—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 containing nickel, cobalt, chromium, molybdenum, or tungsten metals, or compounds thereof
    • 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
    • C10G49/10—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 with moving solid particles
    • C10G49/12—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 with moving solid particles suspended in the oil, e.g. slurries
    • 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
    • C10G55/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process
    • 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
    • C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
    • C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
    • 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
    • C10G7/00—Distillation of hydrocarbon oils
    • C10G7/12—Controlling or regulating
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08L—COMPOSITIONS OF MACROMOLECULAR COMPOUNDS
    • C08L95/00—Compositions of bituminous materials, e.g. asphalt, tar, pitch
    • 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
    • C10G2300/107—Atmospheric residues having a boiling point of at least about 538 °C
    • 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
    • C10G2300/1077—Vacuum residues
    • 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
    • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
    • C10G2400/16—Residues

Definitions

  • the present invention relates to a process for treating a hydrocarbon-based residue.
  • the process and plant according to the invention are particularly suitable for treating and facilitating the use, management and disposal of hydrocarbon-based residues, in particular bituminous residues with a high asphaltene content, obtained as by-product in a previous conversion process of organic residues with a high molecular weight or in any case a high C/H ratio, such as, for example, oils or more generally heavy hydrocarbons, distillation residues possibly already partly deasphalted, bitumens from tar sands, oils deriving from coal and oil shales.
  • hydrocarbon-based residues in particular bituminous residues with a high asphaltene content, obtained as by-product in a previous conversion process of organic residues with a high molecular weight or in any case a high C/H ratio, such as, for example, oils or more generally heavy hydrocarbons, distillation residues possibly already partly deasphalted, bitumens from tar sands, oils deriving from coal and oil shales.
  • Conversion methods of high-molecular-weight organic residues such as for example, heavy oils such as distillation residues possibly already partly deasphalted, oils from tar sands, oils deriving from coal and oil shales, are currently known.
  • the conversion is effected by reducing the molecular weight of the residues to be treated, and increasing their H/C ratio. Examples of conversion methods that combine cracking and hydrogenation reactions of the reactive fragments in the presence of catalysts are described in documents U.S. Pat. No. 5,932,090, EP2158304, EP2155835, EP2291238.
  • bituminous residue is obtained as by-product from the conversion, which, under standard conditions, has the consistency of a viscous paste and is therefore extremely difficult to manage for transportation, sale, disposal or possible re-use on the same production site.
  • This bituminous residue contains an organic fraction normally having an even higher molecular weight, and an even more consistent fraction of coke and inorganic compounds with respect to the residue entering the catalytic hydrocracking process.
  • THFis i.e. the fraction of material insoluble in tetrahydrofuran.
  • bituminous residue is produced in considerable quantities: in a petrochemical plant capable of refining 200,000 barrels/day of crude oil, for example, the relative conversion plant of the organic residues by means of catalytic hydrocracking is capable of producing 60,000 barrels/day.
  • bituminous residue into higher-quality products that can be re-used, for example, as combustibles or commercial fuels, or into an inert product that is easier to manage, dispose of and is less harmful for the environment.
  • U.S. Pat. No. 3,928,170 describes a process (called EUREKA process) for the production of a pitch by means of thermal cracking in a stream of vapour of a bottom oil residue at a pressure within the range of 1.1-3 barg and a temperature in the reaction area of 350-450° C.; the reactor is preceded by a furnace, for preheating the charge, and is followed by a separation section of the products.
  • the pitch is extracted from the bottom of the cracking reactor which operates in semibatch to avoid the formation of coke during the preheating phase.
  • This process however is not satisfactory for treating bottom residues with a particularly high concentration of asphaltenes or residues insoluble in tetrahydrofuran.
  • U.S. Pat. No. 4,477,334 describes a process in which heavy hydrocarbons can be converted in a continuous cracking process, without the formation of coke, forming a pitch as by-product.
  • the solvent deasphalting process uses a solvent (generally propane or butane) under conditions close to those critical for separating the maltene component from the asphaltene component: the asphaltene fraction (which can also contain a certain percentage of solids) is recycled to the process, whereas the maltene fraction (rich in DAO, DeAsphalted Oils), after separating the solvent by extraction under a supercritical condition, forms a product.
  • this process represents the opposite of solvent deasphalting as it is the asphaltene component (rich in solid phase) that is to be extracted and the maltene component recycled.
  • the difficulty in applying this process consists in the use of more columns for managing the cycle of the solvent under supercritical conditions.
  • An objective of the present invention is therefore to overcome the above-mentioned drawbacks of the state of the art, in particular by providing a process for converting the bituminous and pasty residue of previous conversion processes of high-molecular-weight organic residues, into products that can be more easily and conveniently re-used and disposed of.
  • this objective is achieved with a process having the characteristics according to claim 1 .
  • FIG. 1 shows the scheme of a process for treating bituminous residues according to a particular embodiment of the invention
  • FIG. 2 shows a scheme of the ejector of the plant of FIG. 1 .
  • the expression “compound X prevalently containing the substance Y” unless otherwise specified should be interpreted as meaning that the compound X contains at least 50% by weight of the substance Y.
  • FIGS. 1 , 2 relate to a plant for treating a pitchy or bituminous residue obtained as by-product of a conversion process of organic residues having a high molecular weight or in any case a high C/H ratio, such as for example, heavy oils such as distillation residues possibly already partly deasphalted, bitumens from tar sands, oils deriving from coal and oil shales.
  • a pitchy or bituminous residue obtained as by-product of a conversion process of organic residues having a high molecular weight or in any case a high C/H ratio such as for example, heavy oils such as distillation residues possibly already partly deasphalted, bitumens from tar sands, oils deriving from coal and oil shales.
  • the reference number 1 indicates a feeding stream which is preferably a blow-down coming for example from the vacuum distillation column of a conversion plant of heavy oils described for example in the documents U.S. Pat. No. 5,932,090, EP2158304, EP2155835, EP2291238, or from other conversion processes of heavy oils by means of ebullated bed catalytic hydrocracking or other cracking processes.
  • the blow-down of the feeding stream 1 is a solid-liquid suspension, viscous but pumpable at suitable temperatures.
  • the content of C5 asphaltenes (asphaltenes insoluble in n-pentane) in said feeding stream ( 1 ) ranges from 20 to 45%, whereas the THFis range from 10 to 20%.
  • the catalyst of the possible conversion process by means of hydrocracking can, for example, be based on one or more transition metals such as Ni, Co, Mo, preferably molybdenum.
  • the feeding stream 1 can have a temperature ranging for example from 320-350° C., and more preferably 320-330° C., in order to facilitate the pumpability of the fluid.
  • the stream 1 is preferably heated and fluidified by introducing overheated water vapour 2 , for example a vapour flow-rate at about 350° C. The introduction of water vapour also prevents the formation of coke in the furnace.
  • the water vapour flow-rate preferably ranges from 0.5-2% by weight of the flow-rate of the blow-down 1 before being introduced, and preferably about 1% by weight of the blow-down flow-rate.
  • the feeding stream 1 ′ is preferably subsequently further heated to about 325-500° C. by introducing it, for example, into the furnace 3 .
  • the temperature of the stream 4 immediately before being introduced into the separator 6 , can be substantially the same as that inside the furnace 3 , and is preferably equal to or lower than 480° C.
  • the stream 4 can for example be a three-phase solid-liquid-vapour stream.
  • This pressure is preferably the same as the stream 4 immediately before undergoing the adiabatic expansion described hereunder.
  • the pressure values unless otherwise specified, should be considered as being absolute pressure values and not relating to atmospheric pressure.
  • the stream 4 leaving the furnace 3 is subjected to a substantially adiabatic expansion in an environment at a pressure equal to or lower than about 0.1 bara and at a temperature equal to or lower than 450° C. in order to separate a first less volatile fraction 17 , having a boiling point at atmospheric pressure equal to or higher than 540° C. and whose solid and/or anhydrous residue prevalently contains asphaltenes insoluble in pentane and/or other residues insoluble in tetrahydrofuran, from the heavy residue to be treated.
  • a second more volatile fraction 7 is also preferably separated from the heavy residue.
  • the substantially adiabatic expansion is preferably effected by means of substantially instantaneous expansion (flash) through a lamination valve.
  • the adiabatic expansion preferably takes place in a first separator 6 comprising a sealed container, in which there is the above pressure equal to or lower than 0.1 bara. More preferably, there is a pressure equal to or lower than 0.04 bara in the separator 6 .
  • the above-mentioned maximum temperature of 450° C. is an average value over the whole volume of the separator 6 .
  • the stream 4 is preferably subjected to a substantially adiabatic expansion in an environment at a temperature equal to or lower than 400° C., and more preferably equal to or lower than 390° C.
  • the flash or in any case adiabatic expansion advantageously takes place in the upper part of the sealed container or in any case in the first separator 6 , whereas a stripping stream 5 , preferably a stream of water vapour, is introduced into its lower part.
  • the asphaltene-THFi fraction in the heavy stream can vary from 75 to 94%.
  • the ratio between the stripping vapour 5 and blow-down flow-rate 1 ranges from 0.03 to 0.75, more preferably from 0.03 to 0.5.
  • the second more volatile fraction 7 together with most of the stripping stream 5 is preferably evacuated from the first separator 6 reaching the ejector 8 .
  • the ejector 8 is advantageously of the type of FIG. 2 , i.e. equipped with a Venturi tube which sucks the stream 7 , introduced into the narrow section of the Venturi tube, and expels it from the duct 8 depending on the flow-rate of a suitable motor fluid 9 , for example vapour, that enters the Venturi tube from the duct 9 ′. It is therefore possible to control the vacuum degree in the first separator 6 by acting on the flow-rate of the motor fluid 9 entering the Venturi tube.
  • the stream 10 containing the second more volatile fraction 7 , the stripping stream 5 and the motor fluid 9 , is subsequently cooled, for example by means of the heat exchanger 11 —in order to condense the heavier phases, and then reaches the second separator 13 .
  • the exchanger 11 operates at such a temperature that the stream 12 leaving it is preferably at 50° C.
  • the second separator 13 separates the following products from the stream 12 :
  • the first stream 14 can be advantageously reintroduced into the refining or conversion cycle of heavy oils upstream of the plant 100 , for example a vacuum distillation column.
  • the second gaseous stream can be sold, for example, as fuel, propellant or another commercial product.
  • the gaseous stream 15 after leaving the condensation system of the ejectors, can be sent to a blow-down.
  • the first less volatile fraction 17 enriched in asphaltenes and poor in maltenes and other lighter hydrocarbons, practically containing all the asphaltenes of the feedstock and having a composition of maltenes and other lighter hydrocarbons varying from 6 to 25%, depending on the operative conditions, after being collected on the bottom of the first separator 6 , can be poured by gravity, by means of an operating machine or repressurization lung, onto a cooled conveyor belt 18 and cooled thereon and transformed into a granular solid. After sudden cooling of the cooled belt 18 on the surface, the first less volatile fraction 17 solidifies very rapidly and disintegrates.
  • the surface of the cooled conveyor belt 18 is preferably kept at a temperature equal to or lower than about 100° C., and more preferably equal to or lower than about 50° C.
  • the first less volatile fraction 17 is preferably deposited on the conveyor belt 18 , or in any case discharged from the separator 6 , at a relatively high temperature, for example equal to or higher than 315° C. and even more preferably from 315 to 480° C.
  • the reference number 19 indicates the solidified bituminous residue, in the form of granules. As it is in the form of granules rather than a paste or sludge, the bituminous residue 19 can be packaged directly, for example in metal barrels, and commercialized, or in any case managed much more easily. The granular bituminous residue can be used directly, for example, as an inert product for road surfaces or as fuel for blast furnaces or other industrial furnaces.
  • the combination of the adiabatic expansion, preferably flash or in any case sufficiently rapid, and high vacuum degree of the environment in which the expansion takes place, allows residues of previous recovery treatment, having a particularly high content of asphaltenes and inorganic compounds, to be treated, enabling their extremely effective separation into a) a first fraction extremely rich in maltenes, liquid or gaseous hydrocarbons and extremely poor in asphaltenes and b) a second fraction solid at room temperature, considerably enriched in asphaltenes and inorganic residues and extremely poor in maltenes and liquid or gaseous hydrocarbons at standard temperature and pressure.
  • the process according to the invention is particularly suitable for treating residual blow-down streams from oil or hydrocarbon treatment processes, wherein said residues contain at least 30% by weight, and even over 50% by weight, of asphaltenes insoluble in pentane and/or other residues, not necessarily organic, insoluble in tetrahydrofuran.
  • the heavy residue to be treated may preferably have a content of C5-asphaltenes ranging from 20 to 45% by weight and a THFi content ranging from 10 to 20% by weight.
  • the content of solids insoluble in tetrahydrofuran and asphaltenes of the less volatile fraction 17 can easily reach and constantly maintain very high concentrations, for example ranging from 75% to 94% by weight, or in any case over 75% by weight.
  • the invention allows the second more volatile fraction 7 to become poorer in asphaltenes.
  • the separator 6 can comprise or consist of a vacuum column from which the heavy fraction can be extracted from the bottom and the light fraction laterally.
  • a stream containing water vapour and incondensable products is extracted from the head of the column, which is sent to the ejector 8 .
  • the stream based on heavy hydrocarbons 14 coming from the separation of the ejector 8 , can be joined with the side cut of the vacuum column (see paragraph 18 ).
  • the plant 100 was under the following conditions:
  • a process according to the invention is particularly suitable for treating blow-down streams 1 , residues based on hydrocarbons or other organic residues containing at least 30% by weight, and up to over 45-50% by weight, of asphaltenes insoluble in pentane and/or other residues insoluble in tetrahydrofuran.
  • the process according to the invention can bring the flows treated to temperatures well over 150° C., making them more fluid and easier to treat in a continuous process—as for example in the embodiments previously described—rather than batch, of the overall plant or some of its components.
  • the invention allows a more effective flushing to be obtained, and also to actuate the process in an extremely simple plant, as it is equipped with only one separator 6 , i.e. only one separation column.
  • the flows treated do not substantially exceed 450° C. in temperature and generally do not undergo excessively severe conditions
  • the process according to the invention does not degrade or substantially damage the more volatile components of the residue to be treated, increasing the quantity extracted, and on the other hand, avoids the formation of coke in the same plant, reducing the necessity of maintenance and increasing its operative life.
  • the pressure control in the first separator 6 by means of the flow of motor fluid 9 , in particular through a Venturi tube 8 , is suitable for being inserted in a plant functioning in continuous.
  • the embodiment examples previously described can undergo various modifications and variations, all included in the protection scope of the invention.
  • the cooled conveyor belt 18 for example, can be substituted more generally by other cooled conveyors or supports. All the details can be substituted by technically equivalent elements.
  • the materials used, for example, as also the dimensions, can vary according to technical requirements. It should be noted that an expression such as “A comprises B, C, D” also comprises and describes the particular case in which “A is composed of B, C, D”.
  • the examples and lists of possible variants of the present patent application should be considered as being non-limiting lists.

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  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Civil Engineering (AREA)
  • Structural Engineering (AREA)
  • Materials Engineering (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Processing Of Solid Wastes (AREA)
US14/783,985 2013-04-22 2013-04-22 Process for treating a hydrocarbon-based heavy residue Abandoned US20160068760A1 (en)

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CA (1) CA2908439C (zh)
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PT (1) PT2989182T (zh)
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US11149210B2 (en) * 2017-03-31 2021-10-19 Eni S.P.A. Method for the physical separation of refinery purge streams
CN115996798A (zh) * 2020-06-03 2023-04-21 E·丰特查·奎托斯 用于从罐和其它容器中选择性提取粘性烃的系统和方法

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CN106978209A (zh) * 2016-01-19 2017-07-25 肇庆市顺鑫煤化工科技有限公司 一种煤直接液化产物的分离方法和装置
CN105709445B (zh) * 2016-02-19 2018-04-27 中石化炼化工程（集团）股份有限公司 含固油气的脱固方法
CN105833550B (zh) * 2016-04-12 2018-06-29 中石化炼化工程（集团）股份有限公司 含固油气的脱固方法

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US11149210B2 (en) * 2017-03-31 2021-10-19 Eni S.P.A. Method for the physical separation of refinery purge streams
CN115996798A (zh) * 2020-06-03 2023-04-21 E·丰特查·奎托斯 用于从罐和其它容器中选择性提取粘性烃的系统和方法

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PT2989182T (pt) 2018-11-14
CA2908439C (en) 2020-04-28
TR201815716T4 (tr) 2018-11-21
PL2989182T3 (pl) 2019-01-31
ES2692947T3 (es) 2018-12-05
CN105143409A (zh) 2015-12-09
RU2015144506A (ru) 2017-05-26
WO2014174536A1 (en) 2014-10-30
RS57904B1 (sr) 2019-01-31
CA2908439A1 (en) 2014-10-30
EP2989182B1 (en) 2018-08-01
EP2989182A1 (en) 2016-03-02

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