US20170210998A1 - Process for fractionating hydrocarbon feeds using a device comprising switchable bottom zones - Google Patents

Process for fractionating hydrocarbon feeds using a device comprising switchable bottom zones Download PDF

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Publication number
US20170210998A1
US20170210998A1 US15/329,665 US201515329665A US2017210998A1 US 20170210998 A1 US20170210998 A1 US 20170210998A1 US 201515329665 A US201515329665 A US 201515329665A US 2017210998 A1 US2017210998 A1 US 2017210998A1
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Prior art keywords
zone
fractionation
zones
fractionation zone
feed
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US15/329,665
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English (en)
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Thomas Bruneau
Jerome Majcher
Frederic Feugnet
Jean Francois LE COZ
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IFP Energies Nouvelles IFPEN
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IFP Energies Nouvelles IFPEN
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Assigned to IFP Energies Nouvelles reassignment IFP Energies Nouvelles ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: MAJCHER, JEROME, FEUGNET, FREDERIC, BRUNEAU, THOMAS, LE COZ, JEAN-FRANCOIS
Publication of US20170210998A1 publication Critical patent/US20170210998A1/en
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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
    • C10G7/02—Stabilising gasoline by removing gases by fractioning
    • 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
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/14—Fractional distillation or use of a fractionation or rectification column
    • 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
    • C10G53/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes
    • C10G53/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes 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
    • C10G53/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes
    • C10G53/16—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural parallel 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
    • 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
    • C10G75/00—Inhibiting corrosion or fouling in apparatus for treatment or conversion of hydrocarbon oils, in general
    • 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
    • C10G99/00—Subject matter not provided for in other groups of this subclass

Definitions

  • the invention relates to the field of fractionating hydrocarbon feeds, and more precisely to the distillation of hydrocarbon feeds.
  • feeds are generally feeds comprising olefinic fractions, asphaltenes and/or sulphur-containing and metallic impurities or any other chemical entity which is capable of giving rise to a deposit of sediments, or to the formation of coke and/or gum on the fractionation devices.
  • Equipment for distilling hydrocarbon feeds usually has a basic configuration which consists of using a single distillation unit.
  • certain hydrocarbon feeds such as, for example, crude oil feeds or effluents from feeds obtained from conversion processes, are rich in impurities, sediments and/or asphaltenes.
  • deposits of sediments, coke and/or gum form on the internals of the columns which may be plates and/or a structured or unstructured packing, the edges of the device and/or heating devices such as column bottom reboilers, thereby modifying the column traffic as well as the heat transfer from the heating system.
  • One aim of the present invention is to extend the operability of the process for fractionating hydrocarbon feeds.
  • the Applicant has developed a process for fractionating hydrocarbon feeds employing at least one fractionation zone provided with separator internals, and at least two switchable bottom zones which can be connected to the bottom of the fractionation zone in a manner such that at least a first of the bottom zones operates with said fractionation zone, in alternation, for a period at most equal to a plugging period, in a manner such that when at least the first of the bottom zones becomes plugged or before it becomes plugged, it is disconnected from the fractionation zone in order to be cleaned while the feed fractionation process continues with at least one other of the bottom zones.
  • a process of this type has the advantage of being capable of operating continuously without stopping to clean the bottom zones. This results in a substantial increase in productivity and separation efficiency compared with known fractionation processes of the prior art.
  • FIGS. 1 and 2 describe an embodiment of the process carried out with a device comprising one fractionation zone and two bottom zones disposed in parallel and operating in a cyclic and successive manner.
  • FIGS. 3 to 6 describe an embodiment of the process carried out with a device comprising one fractionation zone and two bottom zones disposed in series and operating in a cyclic and successive manner.
  • the invention concerns a process for fractionating hydrocarbon feeds employing at least one fractionation zone provided with separator internals, and at least two switchable bottom zones which can be connected to the bottom of the fractionation zone in a manner such that at least a first of the bottom zones operates with said fractionation zone, in alternation, for a period at most equal to a plugging period, in a manner such that when at least the first of the bottom zones becomes plugged or before it becomes plugged, it is disconnected from the fractionation zone in order to be cleaned while the feed fractionation process continues with at least one other of the bottom zones.
  • fractionation zone is intended to mean any separation means which is known to the person skilled in the art which exploits the differences in volatility and molecular weight of the fractions of the feed to be separated.
  • the fractionation zone in accordance with the invention comprises at least one distillation column of any type provided with separator internals such as plates and/or structured or unstructured packing or any other device which is known to the person skilled in the art.
  • the temperature of the theoretical plate at the bottom of the fractionation zone is lower than the temperature for the formation of sediments, coke and/or gum in the feed to be treated.
  • a limitation of this type prevents the formation of sediments, coke and/or gum at the bottom of the fractionation zone.
  • This temperature may vary as a function of the feed to be treated and may be determined by the person skilled in the art using known methods, non-exhaustive examples of which are: the Carbon Conradson content for coking feeds (ASTM D189/D482), the Maleic Anhydride Value (UOP326-08) and the Bromine Index (ASTM D1159) for feeds with gum-forming potential linked to olefins and/or diolefins, IP375 and IP390 for unstable feeds leading to the formation of sediments.
  • the fractionation zone comprises at least one distillation column.
  • the fractionation zone can be used to separate, for example:
  • the bottom zones in accordance with the invention advantageously correspond to a plurality of switchable bottom zones which are capable of receiving bottom fractions from the feed with a boiling point which is higher than the temperature of the theoretical plate at the bottom of the fractionation zone.
  • the term “bottom fraction” means any fraction at the foot of the fractionation zone.
  • the bottom fractions of the feed have a boiling point which is at least more than 40° C., preferably more than 150° C., more preferably more than 220° C. and yet more preferably more than 300° C. under pressure conditions corresponding to atmospheric pressure.
  • the switchable bottom zones in accordance with the invention are used in a cyclic manner and are connected to the bottom of the fractionation zone, advantageously by means of conduits provided with valves, in a manner such that a first of the bottom zones operates with said fractionation zone, in alternation, for a period at most equal to a plugging period, such that when at least the first of the bottom zones becomes plugged, it is disconnected from the fractionation zone for cleaning while the feed fractionation process continues with at least one other of the bottom zones.
  • the bottom zones are preferably also connected together by means of conduits provided with valves.
  • the operator does not have to await complete plugging of a bottom zone before rendering it non-operational by disconnecting it from the fractionation zone and/or the other bottom zones.
  • the plugging period may correspond to a time selected by the operator.
  • the bottom zones in accordance with the invention are advantageously provided with separator internals such as plates, or structured or unstructured packing which are known to the person skilled in the art, in order to ensure separation of the compounds by contact with liquid and vapour fractions.
  • the bottom zones are disposed in parallel with respect to each other.
  • at least a first of the bottom zones is connected to the bottom of the fractionation zone in a manner such as to be able to operate with said fractionation zone in a cyclic and successive manner for a period at most equal to their plugging period, in a manner such that before at least one of the bottom zones becomes plugged, it is disconnected for cleaning while the feed fractionation process continues with at least one other bottom zone.
  • the switchable bottom zones are disposed and connected in series.
  • the bottom zones are connected together in series, and at least one first bottom zone is connected to the bottom of the fractionation zone in a manner such as to be able to operate in a cyclic and successive manner for a period at most equal to the plugging period of the bottom zone furthest from the fractionation zone in accordance with an operating protocol wherein, when the bottom zone furthest from the fractionation zone becomes plugged or before it becomes plugged, it is disconnected for cleaning, while the feed fractionation process continues with the other bottom zone or zones preceding said bottom zone, and when cleaning of said bottom zone is finished, it is rendered operational and connected directly to the head of the series, the operating protocol being repeated each time the bottom zone furthest from the fractionation zone becomes plugged or before it becomes plugged.
  • the bottom zones are connected (linked) together, preferably via conduits provided with valves and capable of conveying the bottom fractions from one bottom zone to another.
  • the in-series embodiment can be used to optimize the use of the bottom zones because, apart from the period for cleaning the bottom zone furthest from the fractionation zone, all of the bottom zones are used in series, thus meaning that all of the theoretical separation stages can be used and not those of a single bottom zone as in the “in-parallel” embodiment.
  • This embodiment can also be employed to operate the bottom zones in accordance with the “in-parallel” embodiment, in alternation as required.
  • the bottom zone furthest from the fractionation zone is rendered operational and connected directly to the head of the series, advantageously to the bottom of the fractionation zone and to the head of the first bottom zone which was previously connected to the bottom of the fractionation zone.
  • head of the series assumes that a system of conduits and valves, known to the person skilled in the art, is present so that said furthest bottom zone can be connected to the fractionation zone and to the other bottom zones, in particular to the first bottom zone which was previously connected to the bottom of the fractionation zone.
  • the bottom fractions advantageously undergo stripping using a stream of gas.
  • the gas stream is injected as a counter-current into the bottom zones in a manner such as to entrain the light fractions towards the fractionation zone.
  • These gas streams can in fact be used to recover the light fractions entrained in the bottom fraction which have not been separated in the fractionation zone and return them to the fractionation zone.
  • the gas stream may be any chemical cut which vaporizes under the temperature and pressure conditions at the point of injection into the bottom zone.
  • the gas stream in accordance with the invention is advantageously selected from steam, hydrogen, nitrogen or a gas stream obtained from reboiling the bottom of the fractionation zone.
  • the gas stream is injected as a counter-current into the bottom zone furthest from the fractionation zone, then the resulting stream of gas is subsequently sent to the other bottom zones before being returned to the fractionation zone.
  • the feeds for the process in accordance with the invention may be obtained from what is known as conventional crude oil (API degree>20°), heavy crude oil (API degree in the range 10 to 20°) or extra heavy (API degree ⁇ 10°).
  • the density of the feed in accordance with the invention is advantageously greater than 0.6, preferably greater than 0.85, more preferably greater than 0.88.
  • the feeds for the process in accordance with the invention are advantageously selected from crude oil feeds, or from feed effluents obtained from the distillation of crude oil and/or from refining processes, or from feeds obtained from the direct liquefaction of coal (H-CoalTM) or obtained from the direct liquefaction of lignocellulosic biomass, alone or as a mixture with coal.
  • They may in particular be selected from effluents from feeds obtained from thermal or catalytic conversion processes with or without hydrogen, atmospheric residues, vacuum residues, deasphalted oils, pitches, asphalts mixed with an aromatic distillate, coal hydrogenates, heavy oils of any origin and in particular obtained from bituminous sand or oil shale, or mixtures thereof.
  • the conversion processes may be ebullated bed hydroconversion processes, fluid catalytic cracking units, fixed bed hydrotreatment units, cokers, delayed cokers or visbreaking and hydrovisbreaking units.
  • the feeds in accordance with the invention preferably comprise asphaltenes and sulphur-containing and metallic impurities and may have a boiling point of more than 20° C., preferably more than 180° C., more preferably more than 200° C., yet more preferably more than 250° C.
  • the feed treated by the process in accordance with the invention may have a metals content of more than 10 ppm (parts per million, expressed as the mass of metals with respect to the mass of feed), which is preferably more than 20 ppm, more preferably more than 50 ppm.
  • the fractionation process in accordance with the invention is carried out with feeds which may have a C7 asphaltenes content of more than 0.5% m/m (percentage expressed as the mass of C7 asphaltenes with respect to the mass of feed, measured in accordance with the NF T60-115 method), preferably more than 2% m/m, more preferably more than 5% m/m;
  • the feeds in accordance with the invention may be feed effluents obtained from thermal cracking processes, in particular gasolines obtained from catalytic cracking, fluid catalytic cracking (FCC), from a coking process, from a visbreaking process, or from a pyrolysis process.
  • feeds comprise unsaturated species such as monoolefins and diolefins, which are gum precursors and which run a high risk of fouling the fractionation equipment.
  • FIGS. 1 to 6 Several embodiments of the process of the invention are illustrated in FIGS. 1 to 6 for better comprehension. These embodiments are given by way of example and are not limiting in nature. These illustrations of the process of the invention do not include details of all of the components necessary for carrying it out. Only the elements necessary to understanding the invention are represented therein; the person skilled in the art will be able to complete the picture in order to make and implement the invention.
  • FIGS. 1 and 2 describe an embodiment of the process carried out with a device comprising a fractionation zone and two bottom zones.
  • the bottom zones are disposed in parallel and operate in a cyclic and successive manner.
  • FIG. 1 describes operational mode 1 ( 2 a + 2 b ) of this embodiment in which the fractionation zone and the two bottom zones operate in parallel.
  • the feed is sent to the fractionation zone 2 a via the conduit 1 and fractionated therein into several fractions of interest as a function of their boiling point (represented by the arrows A, B, C and D). These fractions are generally fractions such as a gaseous fraction, a gasoline cut, a gas oil cut, or a heavy gas oil cut.
  • the bottom fraction leaving from the bottom of the fractionation zone 2 a via the conduit 2 is sent to the bottom zone 2 b via the conduit 4 provided with the open valve 3 .
  • the bottom fraction obtained from the bottom zone 2 b is sent directly via the conduit 5 provided with the open valve 9 then via the conduit 10 for evacuation via the conduit 15 .
  • the zone 2 c is advantageously not connected to the bottom of the fractionation zone.
  • the bottom fractions advantageously undergo stripping by means of a gas stream injected into said bottom zone 2 b as a counter-current to the bottom fraction.
  • the gas stream injected as a counter-current into the bottom zone 2 b produces a gas stream charged with light fractions which is returned to the fractionation zone via the conduit 11 and the conduit 14 provided with the open valve 12 .
  • the bottom zone 2 b is disconnected from the zone 2 a. It is isolated from the remainder of the device by closing the valves 3 , 9 and 12 , for cleaning ( FIG. 2 ). During this period, the device of the process continues to operate in accordance with operational mode 2 of the embodiment of the process ( 2 a + 2 c ) ( FIG. 2 ).
  • FIG. 2 has the same nomenclature as that for FIG. 1 . Because the bottom zone 2 b has been disconnected, the bottom fraction leaving the bottom of the fractionation zone 2 a via the conduit 2 is sent to the bottom zone 2 c by means of the conduit 4 ′ provided with the open valve 3 ′.
  • the bottom fraction obtained from the bottom zone 2 c is sent directly via the conduit 8 provided with the open valve 9 ′ then via the conduit 10 ′ for evacuation via the conduit 15 .
  • injection of the gas stream into said zone is advantageously stopped.
  • the bottom fractions advantageously undergo stripping by means of a gas stream injected into said bottom zone 2 c as a counter-current to the bottom fraction.
  • the gas stream injected into the bottom zone 2 c as a counter-current produces a gas stream charged with light fractions which is returned to the fractionation zone via the conduit 11 ′ and the conduit 14 ′ provided with the open valve 12 ′.
  • the bottom zone 2 b When cleaning of the bottom zone 2 b is finished, the bottom zone 2 b is rendered operational and connected directly to the bottom of the fractionation zone 2 a in order to once again operate in accordance with operational mode 1 of the embodiment of the process ( 2 a + 2 b ) described above with reference to FIG. 1 and the operating protocol is then repeated each time the bottom zone which is operating is plugged or before it becomes plugged.
  • the zone 2 c is advantageously disconnected from the bottom of the fractionation zone during operational mode 1 of the embodiment of the process ( 2 a + 2 b ) and cleaned.
  • FIGS. 1 and 2 In this first operational embodiment described in FIGS. 1 and 2 , two bottom zones are shown in parallel. However, the invention does not exclude operating a plurality of bottom zones disposed in parallel.
  • FIGS. 3 to 6 describe an embodiment of the process carried out with a device comprising a fractionation zone and two bottom zones.
  • the bottom zones are disposed and connected in series and operate in a cyclic and successive manner.
  • FIG. 3 describes operational mode 1 of the embodiment of the process in which the fractionation zone and the two bottom zones operate in series in accordance with the operational mode: 2 a + 2 b + 2 c.
  • the feed is sent to the fractionation zone 2 a via the conduit 1 in which it is fractionated into several light fractions of interest depending on their boiling point (represented by the arrows A, B, C and D). These fractions are generally fractions such as a gaseous fraction, a gasoline cut, a gas oil cut, or a heavy gas oil cut.
  • the bottom fraction leaving from the bottom of the fractionation zone 2 a via the conduit 2 is sent to the bottom zone 2 b by means of the conduit 4 provided with the open valve 3 . After passing through the bottom zone 2 b, said bottom fraction passes into the bottom zone 2 c by means of the conduit 7 provided with the open valve 6 and the conduit 4 ′.
  • the bottom fraction obtained from the bottom zone 2 c then passes via the conduit 8 provided with the open valve 9 ′ then via the conduit 10 ′ for evacuation via the conduit 15 .
  • the bottom fractions advantageously undergo stripping by means of a gas stream injected into said bottom zones as a counter-current to the bottom fraction.
  • said gas stream is only injected as a counter-current into the bottom zone 2 c in a manner such as to produce a gas stream charged with light fractions which is sent towards the bottom zone 2 b via the conduit 11 ′ and the conduit 13 ′ provided with the open valve 16 ′.
  • said gas stream entrains more light fractions and is then returned to the fractionation zone via the conduit 11 and the conduit 14 provided with the open valve 12 .
  • the bottom zone 2 c is disconnected. This latter is isolated from the remainder of the device by closing the valves 6 , 9 ′ and 16 ′, for cleaning. During this period, the device of the process continues to operate in accordance with operational mode 2 of the embodiment of the process ( 2 a + 2 b ) ( FIG. 4 ).
  • FIG. 4 has the same nomenclature as that for FIG. 3 . Because the bottom zone 2 c has been disconnected, the bottom fraction obtained from the bottom zone 2 b is sent directly via the conduit 5 provided with the open valve 9 then via the conduit 10 for evacuation via the conduit 15 . During cleaning of the bottom zone 2 c, injection of the gas stream into said zone is advantageously stopped.
  • the bottom zone 2 c When cleaning of the bottom zone 2 c has finished, the bottom zone 2 c is rendered operational and connected directly to the bottom of the fractionation zone 2 a in order to operate in accordance with operational mode 3 of the embodiment of the process ( 2 a + 2 c + 2 b ) ( FIG. 5 ).
  • the bottom fraction leaving the bottom of the fractionation zone 2 a via the conduit 2 is sent to the bottom zone 2 c via the conduit 4 ′ provided with the open valve 3 ′.
  • said bottom fraction passes into the bottom zone 2 b via the conduit 7 ′ provided with the open valve 6 ′ and the conduit 4 .
  • the bottom fraction obtained from the bottom zone 2 b then passes via the conduit 5 provided with the open valve 9 and subsequently via the conduit 10 for evacuation via the conduit 15 .
  • the bottom fractions advantageously undergo stripping by means of a gas stream injected into said bottom zones as a counter-current to the bottom fraction.
  • said gas stream is injected only as a counter-current into the bottom zone 2 b in a manner such as to produce a gas stream charged with light fractions which is sent to the bottom zone 2 c via the conduit 11 and the conduit 13 provided with the open valve 16 .
  • said gas stream entrains more of the light fractions and is sent to the fractionation zone via the conduit 11 ′ and the conduit 14 ′ provided with the open valve 12 ′.
  • FIG. 6 has the same nomenclature as that for FIG. 5 . Because the bottom zone 2 b is disconnected, the bottom fraction obtained from the bottom zone 2 c passes directly via the conduit 8 provided with the open valve 9 ′ then via the conduit 10 ′ for evacuation via the conduit 15 . During cleaning of the bottom zone 2 b, injection of the gas stream into said zone is advantageously stopped.
  • the bottom zone 2 b When cleaning of the bottom zone 2 b is finished, the bottom zone 2 b is rendered operational and connected directly to the bottom of the fractionation zone 2 a in order to operate again in accordance with operational mode 1 of the embodiment ( 2 a + 2 b + 2 c ) of the process as described in FIG. 3 above and the operating protocol is then repeated each time that the bottom zone furthest from the fractionation zone becomes plugged.
  • a feed obtained from a process for ebullated bed hydroconversion (RHCK EB) of a vacuum residue (RSV) was sent for fractionation to an atmospheric distillation column (ADU).
  • the atmospheric distillation column (ADU) clogged up after 12 months and had to be stopped for cleaning for a period of 1.5 months.
  • ADU atmospheric distillation column
  • a conventional unit operating with a conventional atmospheric distillation column (ADU) operates 89% of the time with the atmospheric distillation column (ADU) running, and 11% of the time with the atmospheric distillation column stopped (for cleaning).
  • Fractionation of the feed was carried out in accordance with two embodiments of the process in accordance with the invention (the “in-parallel” embodiment and the “in-series” embodiment) and a comparative conventional embodiment in accordance with the prior art.
  • the device employed comprised a distillation column connected to two switchable bottom zones.
  • the device was operated continuously.
  • the two switchable bottom zones were disposed in parallel.
  • At least a first of the bottom zones was connected to the bottom of the distillation column so as to be able to operate with said distillation column in a cyclic and successive manner for a period at most equal to their plugging period, so that before the first bottom zone plugged, it was disconnected for cleaning while the feed fractionation process continued with the second bottom zone.
  • the number of plates for the separation device was equal to 20.
  • the device employed comprised a distillation column connected to two switchable bottom zones connected in series via conduits provided with valves. The device was operated continuously.
  • At least one first bottom zone was connected to the bottom of the distillation column so as to be able to operate in a cyclic and successive manner for a period at most equal to the plugging period for the bottom zone furthest from the distillation column in accordance with an operating protocol such that when the bottom zone furthest from the distillation column was plugged or before it became plugged, it was disconnected for cleaning, while the feed fractionation process continued with only the first bottom zone.
  • an operating protocol such that when the bottom zone furthest from the distillation column was plugged or before it became plugged, it was disconnected for cleaning, while the feed fractionation process continued with only the first bottom zone.
  • cleaning of said bottom zone was finished, it was rendered operational and connected directly as the head of the series to the bottom of the distillation column and as the head of said first bottom zone which as a consequence became the bottom zone furthest from the distillation column; the operating protocol was repeated each time the bottom zone furthest from the distillation column became plugged or before it plugged.
  • the number of plates for the separation device was equal to 20.
  • the device employed comprised just one traditional atmospheric distillation column. Periodically, the column was cleaned, involving stopping it and stopping the upstream hydroconversion unit. Table 2 provides the comparative elements between the three separations.
  • the Net Present Value refers to the sum of the current values for the cash flow associated with a project.
  • the Internal Rate of Return is the maximum rate of return from a project that is required to return the capital invested.
  • the Pay Out Time is the amount of time for revenue from a project to generate cash flow to recover the initial investment costs.
  • the invention allows for an increase in operability by avoiding total stoppage of the unit and ensuring a substantial economic advantage.

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  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Engineering & Computer Science (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
US15/329,665 2014-07-30 2015-06-25 Process for fractionating hydrocarbon feeds using a device comprising switchable bottom zones Abandoned US20170210998A1 (en)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
FR14-57373 2014-07-30
FR1457373A FR3024459B1 (fr) 2014-07-30 2014-07-30 Procede de fractionnement de charges d'hydrocarbures mettant en œuvre un dispositif comprenant des zones de fond permutables
PCT/EP2015/064386 WO2016015930A1 (fr) 2014-07-30 2015-06-25 Procede de fractionnement de charges d'hydrocarbures mettant en œuvre un dispositif comprenant des zones de fond permutables

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US20170210998A1 true US20170210998A1 (en) 2017-07-27

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EP (1) EP3174958B1 (zh)
CN (1) CN107075387B (zh)
CA (1) CA2954551A1 (zh)
FR (1) FR3024459B1 (zh)
MX (1) MX2017000876A (zh)
PL (1) PL3174958T3 (zh)
RU (1) RU2680847C2 (zh)
SG (1) SG11201700502YA (zh)
WO (1) WO2016015930A1 (zh)

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US3248316A (en) * 1963-05-01 1966-04-26 Standard Oil Co Combination process of hydrocracking and isomerization of hydrocarbons with the addition of olefins in the isomerization zone
US3256178A (en) * 1965-05-25 1966-06-14 Union Oil Co Hydrocracking process
US4017382A (en) * 1975-11-17 1977-04-12 Gulf Research & Development Company Hydrodesulfurization process with upstaged reactor zones
US5250234A (en) * 1992-10-08 1993-10-05 Koch Engineering Company, Inc. Liquid distributor apparatus and method for high viscosity liquids
US6168709B1 (en) * 1998-08-20 2001-01-02 Roger G. Etter Production and use of a premium fuel grade petroleum coke
US6312586B1 (en) * 1999-09-27 2001-11-06 Uop Llc Multireactor parallel flow hydrocracking process
US20060213809A1 (en) * 2005-03-09 2006-09-28 Karin Barthelet Hydrocracking process with recycle, comprising adsorption of polyaromatic compounds from the recycled fraction on an adsorbant based on silica-alumina with a controlled macropore content
US20070108036A1 (en) * 2005-11-14 2007-05-17 Michael Siskin Continuous coking process

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GB251363A (en) * 1925-02-04 1926-05-04 V L Oil Processes Ltd Improvements in methods for the vacuum distillation of lubricating oils and the like
SU889684A1 (ru) * 1978-09-25 1981-12-15 Ново-Горьковский Нефтеперерабатывающий Завод Им.Хх1У Съезда Кпсс Производственного Объединения "Горькнефтеоргсинтез" Способ получени нефт ных фракций
FR2784687B1 (fr) * 1998-10-14 2000-11-17 Inst Francais Du Petrole Procede d'hydrotraitement d'une fraction lourde d'hydrocarbures avec reacteurs permutables et introduction d'un distillat moyen
EP1090663A1 (en) * 1999-10-05 2001-04-11 SOLVAY (Société Anonyme) Process for the manufacture of concentrated solutions
CA2432022A1 (fr) * 2000-12-11 2002-06-20 Institut Francais Du Petrole Procede d'hydrotraitement d'une fraction lourde d'hydrocarbures avec des reacteurs permutables et des reacteurs court-circuitables
FR2940313B1 (fr) * 2008-12-18 2011-10-28 Inst Francais Du Petrole Procede d'hydrocraquage incluant des reacteurs permutables avec des charges contenant 200ppm poids-2%poids d'asphaltenes
US8535516B2 (en) * 2009-04-23 2013-09-17 Bechtel Hydrocarbon Technology Solutions, Inc. Efficient method for improved coker gas oil quality
RU2448145C1 (ru) * 2010-12-02 2012-04-20 Общество С Ограниченной Ответственностью "Проминтех" Способ замедленного коксования
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US2436496A (en) * 1946-01-11 1948-02-24 Adsorptive Process Company Process for the catalytic treatment of hydrocarbon oil
US3248316A (en) * 1963-05-01 1966-04-26 Standard Oil Co Combination process of hydrocracking and isomerization of hydrocarbons with the addition of olefins in the isomerization zone
US3256178A (en) * 1965-05-25 1966-06-14 Union Oil Co Hydrocracking process
US4017382A (en) * 1975-11-17 1977-04-12 Gulf Research & Development Company Hydrodesulfurization process with upstaged reactor zones
US5250234A (en) * 1992-10-08 1993-10-05 Koch Engineering Company, Inc. Liquid distributor apparatus and method for high viscosity liquids
US6168709B1 (en) * 1998-08-20 2001-01-02 Roger G. Etter Production and use of a premium fuel grade petroleum coke
US6312586B1 (en) * 1999-09-27 2001-11-06 Uop Llc Multireactor parallel flow hydrocracking process
US20060213809A1 (en) * 2005-03-09 2006-09-28 Karin Barthelet Hydrocracking process with recycle, comprising adsorption of polyaromatic compounds from the recycled fraction on an adsorbant based on silica-alumina with a controlled macropore content
US20070108036A1 (en) * 2005-11-14 2007-05-17 Michael Siskin Continuous coking process

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PL3174958T3 (pl) 2019-01-31
SG11201700502YA (en) 2017-03-30
CN107075387A (zh) 2017-08-18
CA2954551A1 (fr) 2016-02-04
CN107075387B (zh) 2019-08-16
RU2017106171A3 (zh) 2018-10-19
FR3024459A1 (fr) 2016-02-05
RU2017106171A (ru) 2018-08-28
MX2017000876A (es) 2017-05-01
WO2016015930A1 (fr) 2016-02-04
FR3024459B1 (fr) 2018-04-13
RU2680847C2 (ru) 2019-02-28
EP3174958B1 (fr) 2018-05-16
EP3174958A1 (fr) 2017-06-07

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