EP2930224A1 - Verfahren zur herstellung von leichtolefinen und btx unter verwendung einer fcc-anlage, in der ein schweres einsatzmaterial vom typ vgo mit starkem hydrotreating aufbereitet wird, gekoppelt mit einer katalytischen reforming-einheit und einem aromakomplex, die zur aufbereitung eines schweren einsatzmaterials vom typ erdöl verwendet werden - Google Patents

Verfahren zur herstellung von leichtolefinen und btx unter verwendung einer fcc-anlage, in der ein schweres einsatzmaterial vom typ vgo mit starkem hydrotreating aufbereitet wird, gekoppelt mit einer katalytischen reforming-einheit und einem aromakomplex, die zur aufbereitung eines schweren einsatzmaterials vom typ erdöl verwendet werden Download PDF

Info

Publication number
EP2930224A1
EP2930224A1 EP15305501.7A EP15305501A EP2930224A1 EP 2930224 A1 EP2930224 A1 EP 2930224A1 EP 15305501 A EP15305501 A EP 15305501A EP 2930224 A1 EP2930224 A1 EP 2930224A1
Authority
EP
European Patent Office
Prior art keywords
fcc
unit
feedstock
aromatic
fraction
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Withdrawn
Application number
EP15305501.7A
Other languages
English (en)
French (fr)
Inventor
Bertrand Fanget
Abdelhakim Koudil
Alexandre Pagot
Romain Corroyer
Joana Fernandes
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
IFP Energies Nouvelles IFPEN
Original Assignee
IFP Energies Nouvelles IFPEN
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by IFP Energies Nouvelles IFPEN filed Critical IFP Energies Nouvelles IFPEN
Publication of EP2930224A1 publication Critical patent/EP2930224A1/de
Withdrawn legal-status Critical Current

Links

Images

Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G63/00—Treatment of naphtha by at least one reforming process and at least one other conversion process
    • C10G63/02—Treatment of naphtha by at least one reforming process and at least one other conversion process plural serial stages only
    • C10G63/04—Treatment of naphtha by at least one reforming process and at least one other conversion process plural serial stages only including at least one cracking step
    • 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
    • C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G11/14—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts
    • C10G11/18—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts 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
    • C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G11/14—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts
    • C10G11/18—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts according to the "fluidised-bed" technique
    • C10G11/182—Regeneration
    • 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
    • C10G35/00—Reforming naphtha
    • 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
    • C10G69/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process
    • C10G69/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only
    • C10G69/04—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only including at least one step of catalytic cracking in the absence of hydrogen
    • 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
    • C10G69/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process
    • C10G69/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only
    • C10G69/08—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only including at least one step of reforming naphtha
    • 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
    • C10G2300/1044—Heavy gasoline or naphtha having a boiling range of about 100 - 180 °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
    • C10G2300/1037—Hydrocarbon fractions
    • C10G2300/1048—Middle distillates
    • C10G2300/1059—Gasoil having a boiling range of about 330 - 427 °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
    • C10G2300/1074—Vacuum distillates
    • 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
    • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
    • C10G2400/20—C2-C4 olefins
    • 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
    • C10G2400/30—Aromatics
    • 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
    • C10G69/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process
    • C10G69/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only
    • C10G69/12—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only including at least one polymerisation or alkylation step
    • C10G69/126—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only including at least one polymerisation or alkylation step polymerisation, e.g. oligomerisation

Definitions

  • the invention is in the field of refining and petrochemical processes and achieves extensive integration between the FCC unit and the aromatic complex (CA).
  • the present invention relates more particularly to the case of FCC units treating heavy loads but highly hydrotreated, and thus having a hydrogen content greater than 13.5% by weight. During catalytic cracking, these charges have a coke deficit, which adversely affects the thermal balance of the FCC.
  • the present invention describes means for restoring a balanced thermal balance by exchange of material flow between the FCC and the aromatic complex (CA).
  • This fraction derived from the aromatic complex (CA) is recycled to the FCC reactor that can operate both in riser flow and downflow, and its conversion allows an increase in BTX yield. more than improving the thermal balance of the FCC unit.
  • the prior art also proposes recycle FCC effluents into an additional reactor in order to exhaust the potential of these unconverted sections such as the C4 fraction for example.
  • the present invention taking advantage of the immediate proximity of the FCC and the aromatic complex, proposes in addition to conventional recycles from the FCC, recycle the heavy aromatics flux from the aromatic complex initially dedicated to the gasoline pool.
  • the present invention also describes the possibility of preheating the FCC charge by recovering the heat from the furnaces of the catalytic reforming units.
  • the present invention thus proposes to recover a portion of the available heat in the convection zone of the preheating furnaces of the catalytic reforming feed in order to preheat the FCC feed.
  • the present invention can be defined as a process for producing C 2, C 3 and C 4 light olefins and BTX (benzene, toluene, xylenes) using a catalytic cracking unit (FCC) and an aromatic complex (CA) including a catalytic reforming unit for gasoline (RC).
  • FCC catalytic cracking unit
  • CA aromatic complex
  • RC catalytic reforming unit for gasoline
  • LCN feedstock from the catalytic cracking unit is defined by its distillation range (PI-160 ° C), PI (initial distillation point) ranging from 30 ° C to 60 ° C, and PF (final point of distillation) being defined at plus or minus 10 ° C, that is to say ranging from 150 ° C to 170 ° C.
  • the LCN feed is introduced in admixture with the charge (5) of the aromatic complex (CA).
  • the so-called heavy aromatic charge (11) produced by the aromatic complex (CA) is composed of aromatics with more than 10 carbon atoms. This heavy aromatic charge is sent in mixture with the charge (2) of the FCC unit where it brings by its power coquant the calories necessary for the closure of the thermal balance.
  • the charge (2) of the FCC unit is preheated in the furnaces of the catalytic reforming unit (RF), preferably in the convection zone of the latter.
  • the raffinate effluent (12) of the aromatic complex is sent to a separation unit (SPLIT2) which makes it possible to separate a light fraction (13) which is mixed with the feedstock ( 2) to the catalytic cracking unit (FCC), and a heavy fraction (14) which is mixed with the hydrotreated naphtha feedstock (4) to the catalytic reforming unit (REF).
  • SPLIT2 separation unit
  • the C4 and C5 light olefins originating from the separation box (BF), denoted stream 15, are sent to an oligomerization unit (OLG), and the effluents (16) of said oligomerization unit (15) are mixed with the feedstock (2) in the catalytic cracking unit (FCC).
  • OLG oligomerization unit
  • FCC catalytic cracking unit
  • the charge (2) of the FCC unit is preheated in the convection zone of the catalytic reforming furnaces (FREF) before being introduced as a feedstock of the catalytic cracking unit. (FCC).
  • FREF catalytic reforming furnaces
  • the FCC allows the production of a BTX recoverable flux in the aromatic complex.
  • the flow rate of light olefins produced by the FCC is increased.
  • the FCC benefits from a substantial coke input thanks to the recycling of at least a portion of the aromatic heavy fraction derived from the aromatic complex, which makes it possible to complete the heat balance.
  • the integration of the aromatic complex and FCC provides a process flow that optimizes and makes flexible the production and recovery of high value-added compounds, such as light olefins and BTX.
  • the heavy aromatics flux from the aromatic complex (11) is minimized or eliminated to the benefit of coke produced and useful for the thermal balance of the FCC, and BTX produced by cracking in the FCC.
  • the FCC charge can be preheated by the furnaces of the catalytic reformer unit, further improving the thermal balance of the FCC.
  • An FCC unit generally processes a heavy cut from the vacuum distillation unit such as VGO (abbreviation of "vacuum gas oil” terminology), or an atmospheric residue alone or in admixture.
  • VGO abbreviation of "vacuum gas oil” terminology
  • the load arriving at the FCC for example a VGO, may be significantly lighter due to pretreatment, usually a more or less advanced hydrotreatment, or because it comes from a conversion unit. wherein the initial charge has been greatly enriched in hydrogen.
  • This filler also has the advantage of containing few nitrogen and sulfur impurities, which leads to an LCN (abbreviation for "light cracked naphtha”) cut from catalytic cracking which can be oriented towards the entry of the aromatic complex generally in a mixture. with an ex-reforming charge.
  • LCN abbreviation for "light cracked naphtha”
  • This LCN feed may optionally be mixed with a steam cracker type feed to be hydrotreated before going to the aromatic complex.
  • the cracking reactions in the FCC also lead to the production of aromatic compounds and especially high value-added compounds such as benzene, toluene and xylene (especially para-xylene), noted overall BTX, that it will be possible to value in the FCC-Complexe Aromatique sequence.
  • the flexibility of the FCC also allows secondary loads to be treated in relation to the main load.
  • These secondary charges generally represent less than 10% by weight of the main charge and are recycles of available effluents, effluents which have a significant potential for light olefins. This is particularly the case of the so-called "raffinate" flow from the aromatic complex which is a low flux of aromatic compounds.
  • the FCC recycle of this type of highly cokant charge makes it possible to benefit from an additional source of coke, thus to balance the coke deficient thermal balance from a hydrogen-enriched main charge, and to be able to, at the same time , increase the BTX yield of the aromatic complex.
  • the figure 1 represents a diagram of the sequence according to the present invention.
  • the feedstock entering the hydroconversion unit is a heavy feedstock generally derived from vacuum distillation.
  • VGO vacuum distillate
  • the feed to the FCC can be any mixture of hydrotreated VGO feedstock and UCO feedstock in the previously defined sense.
  • the naphtha feedstock for hydrotreatment is a gasoline cut whose initial boiling point is generally above 30 ° C and the final boiling point is generally below 220 ° C. It is treated in a hydrotreating unit in order to rid it of sulfur compounds, so as to reach an S content of less than 0.5 ppm.
  • the desulfurized gasoline effluent (30-220 ° C) is sent to the catalytic reforming unit (RC) after being heated in an exchange train comprising furnaces.
  • Another factor of integration of the FCC with the aromatic complex is achieved by the use of reforming furnaces as a means of preheating the charge of said FCC, preferably in the convection zone of these furnaces, which generally corresponds to approximately 25% -35%. total heating power. This preheating contributes to the achievement of the thermal balance of FCC made deficient in coke because of its highly hydrogenated charge.
  • the heavy aromatics flux from the aromatic complex (CA) is recycled to the FCC, not by burning it in the regenerator, but by treating it as a mixture with the feedstock in the FCC reactor.
  • this heavy aromatics stream (11) will be converted into BTX aromatics and additional coke (with respect to the highly hydrogenated feedstock) allowing the closure of the overall thermal balance of the FCC unit.
  • the raffinate is recycled to the raffinate from the aromatic complex so that it is predominantly cracked with propylene, butenes and ethylene.
  • the FCC contributes to a higher production of BTX aromatics, because the lightly cracked LCN gasoline fraction, almost free of sulfur and other impurities due to the hydroconversion stage of the heavy load, is sent aromatic complex (CA) to extract and process aromatics to produce a maximum of benzene, toluene and para-xylene.
  • CA aromatic complex
  • the figure 2 shows a variant of the present invention in which the raffinate from the aromatic complex is divided in two; the light part goes to the FCC, while the heavy part is recycled to the aromatic complex.
  • it may be desired to extract even more valuable aromatics from the assembly by sending the HCN heavy cracking gasoline into the starting naphtha stream so that said HCN feed undergoes a hydrotreatment before entering the aromatic complex ( IT).
  • the heavy fraction (16) resulting from the fractionation of the FCC may be recycled in part or in whole to the FCC reactor to make even more olefins and aromatics, as well as for the production of additional essential coke at the same time. thermal balance of the FCC unit.
  • the figure 3 shows another variant of the present invention which consists in separating from the C5 cut at the outlet of the FCC reactor so as to send in the cold box a part comprising the dry gases, the LPGs as well as the compounds with five carbon atoms for be further separated and thus make it possible to isolate the fraction C4 and C5 to recycle it into the reaction section of the FCC or send it to an oligomerization unit (OLG) and then send the oligomerate thus formed to the FCC reactor, which increases the yields of light olefins.
  • OLG oligomerization unit
  • the FCC can be equipped in addition to the main reactor treating highly hydrogenated feed, another reactor, called secondary, dedicated to various light cuts whose cracking conditions may be more severe.
  • the first feedstock (1) entering the FCC-Petrochemical Unit is an unconverted oil from a VGO hydrocracking unit or a highly hydrotreated VGO.
  • Table 1 gives property ranges for such a type of load. ⁇ b> Table 1 - Main FCC Load Characteristic ⁇ / b> Typical load Min / Max Nitrogen compounds mg / kg 7.84 1 - 50 Conradson Carbon ⁇ 0.2% ⁇ 1 PI (0.50%) ° C 244.1 > 240 PF (99.50%) ° C 649.4 ⁇ 700 Hydrogen (NMR) % m / m 14.2 13.5 - 14.5 SPGR 15 ° C kg / m3 844.8 800 - 920 saturated % m / m 92.1 85 - 98 aromatic % m / 4.9 2 - 10 resins % m / 0.7 ⁇ 5 Vanadium (FX) mg / kg ⁇ 2 ⁇ 5 Nickel (FX) mg / kg ⁇ 2 ⁇ 5
  • the light cracked gasoline stream (9) noted as LCN from the FCC is recycled to the aromatic complex (CA). It is a depentanized cut whose initial boiling point (PI) is greater than 30 ° C.
  • the boiling point (PF) is usually 160 ° C.
  • the heavy cracked gasoline stream (17) denoted HCN from the FCC is generally richer in aromatics than the LCN fraction, with an initial point (PI) corresponding to the final cut point of the LCN and a final cut point ( PF) generally not exceeding 220 ° C.
  • This HCN cut is often richer in sulfur than the light fraction of FCC gasoline. Under severe cracking conditions, its yield is low, but it concentrates the sulfur compounds of the total FCC gasoline.
  • the heavy fraction stream (16) from the fractionation of the liquid effluents of the FCC is a hydrocarbon fraction whose initial boiling point (PI) is 220 ° C. This stream concentrates most of the sulfur and nitrogen compounds initially present in the feed, and can be wholly or partly recycled to the FCC reactor.
  • the heavy aromatic stream (11) derived from the aromatic complex and recycled to the FCC reactor is composed mainly of aromatic compounds whose carbon number is greater than or equal to 10.
  • the initial distillation temperature (PI) of this stream (11) is generally greater than 190 ° C.
  • the raffinate stream (12) from the aromatic complex is a cut almost free of aromatic compounds.
  • the initial boiling point (PO) of this cup is above 30 ° C, and its boiling end point (PF) is variable, but is normally between 150 ° C and 220 ° C.
  • the raffinate stream (12) can optionally be split into two fractions with an intermediate point between 75 ° C and 150 ° C.
  • the FCC unit is a highly hydrotreated VGO catalytic cracking unit or unconverted oil from VGO hydro-conversion units.
  • the FCC unit in the context of the present invention has at least one main reactor operating, either upflow ("riser”) or downflow (“downer”).
  • the FCC unit has a separator-stripper section in which the catalyst is separated from the hydrocarbon effluents.
  • the FCC unit furthermore has a regeneration section of the catalyst in which the coke formed during the reaction and deposited on the catalyst is burned in a flow of air generating combustion fumes and recovering most of the heat required by the reactor in the form of sensible heat of the catalyst itself.
  • the FCC unit has its own hydrocarbon effluent treatment section including a plant gas allowing a separation of light olefins (ethylene, propylene, butenes) from the other gases: hydrogen, methane, ethane, propane.
  • a plant gas allowing a separation of light olefins (ethylene, propylene, butenes) from the other gases: hydrogen, methane, ethane, propane.
  • the heavier part of the hydrocarbon effluents is treated in a separation section comprising at least one fractionation unit (FRAC) for recovering the typical distillation range cut [30 ° C - 160 ° C], called LCN cut, which is recycled to the aromatic complex (CA).
  • FRAC fractionation unit
  • the intermediate portion comprising the hydrocarbons with 4 and 5 carbon atoms can be either recycled directly to the FCC or preferentially be sent to an oligomerization unit to obtain a polyC4 / C5 oligomer whose crackability in catalytic cracking processes is clearly greater than that of non-oligomerized compounds, or be upgraded to their dedicated pool.
  • the FCC unit is preferably operated at high severity (high riser output temperature, high catalyst to load ratio: C / O).
  • the range of operating conditions is given in Table 2 below. ⁇ b> Table 2 - Operating Conditions of the FCC Unit ⁇ / b> Condition Low Max TSR, ° C 500 650 C / O, kg / kg 5 30
  • the catalyst may be any type of catalyst preferably containing a high proportion of zeolite. This can be a common catalyst for FCC. It may be additive or not ZSM-5, or may even be composed of 100% ZSM-5.
  • Example 1 cracking of a heavy load highly hydrogenated (not according to the invention)
  • This example shows the separate yields of one FCC unit treating a converted no-feed hydrocracker feedstock of a vacuum distillate whose typical composition is given in Table 3 below, and those of an aromatic complex allowing recovery of BTX, without integration of FCC units and aromatic complex.
  • Table 3 Table 3 - Characteristic of FCC cracked load.
  • Example 2 implements the synergies between the FCC and the aromatic complex according to the scheme of the invention.
  • figure 1 by sending to the reaction section of the FCC, the heavy aromatic charge (11) which is an aromatic compound (CA) effluent having an initial distillation point (5%) of about 190 ° C.
  • CA aromatic compound
  • This heavy aromatic charge (11) is composed of 100% aromatics; the majority (70% w / w) are compounds with 11 or 12 carbon atoms; the remaining 30% by weight are aromatics with 10 carbon atoms.
  • CA aromatic complex

Landscapes

  • 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)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Catalysts (AREA)
EP15305501.7A 2014-04-07 2015-04-03 Verfahren zur herstellung von leichtolefinen und btx unter verwendung einer fcc-anlage, in der ein schweres einsatzmaterial vom typ vgo mit starkem hydrotreating aufbereitet wird, gekoppelt mit einer katalytischen reforming-einheit und einem aromakomplex, die zur aufbereitung eines schweren einsatzmaterials vom typ erdöl verwendet werden Withdrawn EP2930224A1 (de)

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
FR1453075A FR3019554B1 (fr) 2014-04-07 2014-04-07 Procede de production d'olefines legeres et de btx utilisant une unite fcc traitant une charge lourde de type vgo tres hydrotraite, couplee avec une unite de reformage catalytique et un complexe aromatique traitant une charge de type naphta.

Publications (1)

Publication Number Publication Date
EP2930224A1 true EP2930224A1 (de) 2015-10-14

Family

ID=50976909

Family Applications (1)

Application Number Title Priority Date Filing Date
EP15305501.7A Withdrawn EP2930224A1 (de) 2014-04-07 2015-04-03 Verfahren zur herstellung von leichtolefinen und btx unter verwendung einer fcc-anlage, in der ein schweres einsatzmaterial vom typ vgo mit starkem hydrotreating aufbereitet wird, gekoppelt mit einer katalytischen reforming-einheit und einem aromakomplex, die zur aufbereitung eines schweren einsatzmaterials vom typ erdöl verwendet werden

Country Status (7)

Country Link
US (1) US9650579B2 (de)
EP (1) EP2930224A1 (de)
JP (1) JP6539475B2 (de)
KR (1) KR102375080B1 (de)
CN (1) CN104974791B (de)
FR (1) FR3019554B1 (de)
RU (1) RU2672913C2 (de)

Families Citing this family (17)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
KR102374847B1 (ko) * 2014-02-25 2022-03-16 사우디 베이식 인더스트리즈 코포레이션 촉매적 분해를 이용하여 혼합 탄화수소 급원으로부터 btx를 생산하는 방법
WO2017108476A1 (en) * 2015-12-22 2017-06-29 Sabic Global Technologies B.V. Process for converting mixed hydrocarbon streams to lpg and btx
JP7075612B2 (ja) * 2017-09-26 2022-05-26 日立金属株式会社 窒化ケイ素焼結基板
CN111479905B (zh) 2017-12-15 2023-09-01 沙特基础全球技术有限公司 用于在石脑油催化裂化工艺中预热石脑油的方法
KR102420209B1 (ko) * 2017-12-29 2022-07-12 루머스 테크놀로지 엘엘씨 중질 연료유의 화학제품으로의 전환
WO2020021356A1 (en) 2018-07-27 2020-01-30 Sabic Global Technologies B.V. Process of producing light olefins and aromatics from wide range boiling point naphtha
KR102188532B1 (ko) 2019-02-15 2020-12-09 에쓰대시오일 주식회사 다환 방향족 탄화수소로부터 경방향족 탄화수소 제조를 위한 분자크기 선택성 수소화 분해 반응용 촉매
SG11202109648PA (en) * 2019-03-04 2021-10-28 China Petroleum & Chem Corp Process and system for producing light olefins from inferior oils
FR3104605B1 (fr) * 2019-12-16 2022-04-22 Ifp Energies Now Dispositif et procédé de production d’oléfines légères par craquage catalytique et vapocraquage.
US11248173B2 (en) 2020-02-13 2022-02-15 Saudi Arabian Oil Company Process and system for catalytic conversion of aromatic complex bottoms
EP3901237B1 (de) 2020-04-21 2023-09-06 Indian Oil Corporation Limited Verfahrenskonfiguration zur herstellung von petrochemischen rohstoffen
FR3113061B1 (fr) * 2020-07-30 2023-04-21 Ifp Energies Now Procede de traitement d’huiles de pyrolyse de plastiques incluant un hydrocraquage en une etape
US11473022B2 (en) 2021-01-07 2022-10-18 Saudi Arabian Oil Company Distillate hydrocracking process with an n-paraffins separation step to produce a high octane number isomerate stream and a steam pyrolysis feedstock
US11807818B2 (en) * 2021-01-07 2023-11-07 Saudi Arabian Oil Company Integrated FCC and aromatic recovery complex to boost BTX and light olefin production
US11820949B2 (en) 2021-01-15 2023-11-21 Saudi Arabian Oil Company Apparatus and process for the enhanced production of aromatic compounds
US11965136B2 (en) * 2021-01-15 2024-04-23 Saudi Arabian Oil Company Cyclization and fluid catalytic cracking systems and methods for upgrading naphtha
US11591526B1 (en) * 2022-01-31 2023-02-28 Saudi Arabian Oil Company Methods of operating fluid catalytic cracking processes to increase coke production

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5685972A (en) * 1995-07-14 1997-11-11 Timken; Hye Kyung C. Production of benzene, toluene, and xylene (BTX) from FCC naphtha
US20080156696A1 (en) * 2006-12-29 2008-07-03 Niccum Phillip K FCC process for converting C3/C4 feeds to olefins and aromatics
US20080223754A1 (en) * 2007-03-15 2008-09-18 Anand Subramanian Systems and methods for residue upgrading
US20080264829A1 (en) * 2007-04-30 2008-10-30 Eng Curtis N Method for adjusting yields in a light feed fcc reactor

Family Cites Families (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
RU2052490C1 (ru) * 1993-08-24 1996-01-20 Брускин Юрий Александрович Способ получения низших олефинов и бензола
JP4409977B2 (ja) * 2004-02-03 2010-02-03 株式会社ジャパンエナジー 石油精製における廃油処理方法
CN100487080C (zh) * 2004-03-08 2009-05-13 中国石油化工股份有限公司 一种生产低碳烯烃和芳烃的化工型炼油方法
BRPI0514218A (pt) * 2004-08-10 2008-06-03 Shell Internationale Rsearch M processo e aparelho para fabricar destilado médio e olefinas inferiores
JP4866579B2 (ja) * 2005-08-02 2012-02-01 Ｊｘ日鉱日石エネルギー株式会社 石油精製における廃油処理方法
US20100331590A1 (en) * 2009-06-25 2010-12-30 Debarshi Majumder Production of light olefins and aromatics
CN102795958B (zh) * 2011-05-27 2015-03-18 中国石油化工股份有限公司 一种以石脑油为原料生产芳烃和乙烯的方法
CN103772123B (zh) * 2012-10-25 2015-07-08 中国石油化工股份有限公司 增产btx芳烃的方法

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5685972A (en) * 1995-07-14 1997-11-11 Timken; Hye Kyung C. Production of benzene, toluene, and xylene (BTX) from FCC naphtha
US20080156696A1 (en) * 2006-12-29 2008-07-03 Niccum Phillip K FCC process for converting C3/C4 feeds to olefins and aromatics
US20080223754A1 (en) * 2007-03-15 2008-09-18 Anand Subramanian Systems and methods for residue upgrading
US20080264829A1 (en) * 2007-04-30 2008-10-30 Eng Curtis N Method for adjusting yields in a light feed fcc reactor

Also Published As

Publication number Publication date
CN104974791B (zh) 2018-11-06
KR102375080B1 (ko) 2022-03-15
US9650579B2 (en) 2017-05-16
RU2015112094A (ru) 2016-10-20
RU2015112094A3 (de) 2018-10-12
JP6539475B2 (ja) 2019-07-03
US20150284644A1 (en) 2015-10-08
CN104974791A (zh) 2015-10-14
KR20150116412A (ko) 2015-10-15
RU2672913C2 (ru) 2018-11-21
FR3019554B1 (fr) 2017-10-27
JP2015199956A (ja) 2015-11-12
FR3019554A1 (fr) 2015-10-09

Similar Documents

Publication Publication Date Title
EP2930224A1 (de) Verfahren zur herstellung von leichtolefinen und btx unter verwendung einer fcc-anlage, in der ein schweres einsatzmaterial vom typ vgo mit starkem hydrotreating aufbereitet wird, gekoppelt mit einer katalytischen reforming-einheit und einem aromakomplex, die zur aufbereitung eines schweren einsatzmaterials vom typ erdöl verwendet werden
KR102243952B1 (ko) 방향족 컴플렉스 버텀(aromatic complex bottom)으로부터 가솔린 및 디젤을 회수하는 공정
EP2930226B1 (de) Verfahren zur herstellung von leichtolefinen und btx unter verwendung einer katalytischen ncc-crack-einheit zur aufbereitung eines einsatzmaterials vom typ erdöl, einer einheit zum katalytischen reforming und eines aromakomplexes
CN108884395B (zh) 通过回收和处理重质裂化器残余物来增加烯烃产量的整合方法
CN109593552B (zh) 将炼厂重质渣油提质为石化产品的方法
KR102339046B1 (ko) 원유를 에틸렌 수율이 향상된 석유화학물질로 변환시키기 위한 방법 및 장치
EP3577199B1 (de) Verfahren zur integriertes hydrobehandlungs- und dampfpyrolyseverfahren zur direkten verarbeitung eines rohöls zur herstellung von olefinischen und aromatischen petrochemikalien
WO2019014012A1 (en) MULTI-STAGE HYDROCARBON PYROLYSIS TAR ASSESSMENT
JP6415588B2 (ja) 高沸点炭化水素供給原料をより軽沸点の炭化水素生成物に転換する方法
EP3339401B1 (de) Anlage und integriertes verfahren für hydrotreatment und hydrokonvertierung mit gemeinsamer fraktionierung
EP3110918B1 (de) Verfahren zur aufwertung von schweren raffineriekohlenwasserstoffen in petrochemikalien
US9458390B2 (en) Process and system for preparation of hydrocarbon feedstocks for catalytic cracking
KR101717827B1 (ko) 개질기를 갖는 파라핀 이성체화 유닛의 병렬 작동에 의한 개선된 공정
JP2017511829A (ja) 高沸点炭化水素供給原料をより軽沸点の炭化水素生成物へ転換する方法
FR2895417A1 (fr) Procede de desulfurisation comprenant une etape de transformation et une etape d'extraction des composes soufres
EP2426189B1 (de) Verfahren zur Herstellung von Kerosin- und Dieselkraftstoffen aus leichten ungesättigten und reichen aromatischen BTX-Anteilen
CN112601801A (zh) 在蒸汽裂解焦油的改质过程中维持再循环溶剂的高溶解力的方法
CN101617026B (zh) 使用改性原料的延迟焦化法
RU2799453C2 (ru) Конфигурация производства олефинов и ароматических соединений
WO2020249498A1 (fr) Procede de production d'olefines comprenant un hydrotraitement, un desasphaltage, un hydrocraquage et un vapocraquage
FR3038904A1 (fr) Procede permettant de realiser le bouclage du bilan thermique sur une unite de craquage catalytique de naphta dite ncc

Legal Events

Date Code Title Description
PUAI Public reference made under article 153(3) epc to a published international application that has entered the european phase

Free format text: ORIGINAL CODE: 0009012

AK Designated contracting states

Kind code of ref document: A1

Designated state(s): AL AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC MK MT NL NO PL PT RO RS SE SI SK SM TR

AX Request for extension of the european patent

Extension state: BA ME

17P Request for examination filed

Effective date: 20160414

RBV Designated contracting states (corrected)

Designated state(s): AL AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC MK MT NL NO PL PT RO RS SE SI SK SM TR

RAP1 Party data changed (applicant data changed or rights of an application transferred)

Owner name: IFP ENERGIES NOUVELLES

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: EXAMINATION IS IN PROGRESS

17Q First examination report despatched

Effective date: 20190919

GRAP Despatch of communication of intention to grant a patent

Free format text: ORIGINAL CODE: EPIDOSNIGR1

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: GRANT OF PATENT IS INTENDED

INTG Intention to grant announced

Effective date: 20200707

GRAS Grant fee paid

Free format text: ORIGINAL CODE: EPIDOSNIGR3

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: GRANT OF PATENT IS INTENDED

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: THE APPLICATION IS DEEMED TO BE WITHDRAWN

18D Application deemed to be withdrawn

Effective date: 20201118