• 专利附录
  • 专利说明
  • 权利要求
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    • 专利摘要:
    The present invention relates to FCC units treating hydrogen-enriched heavy charges, such as for example a highly hydrotreated VGO, or the unconverted part resulting from a hydrocracking of the same type of VGO charge, charges which present the characteristic of cracking light olefins such as ethylene and propylene. The integration of an FCC with an aromatic complex allows the recovery by the aromatic complex of the BTX formed in the FCC, and the recovery by the FCC of the bottom flow of the aromatic heavy column of the aromatic complex.
    公开号:FR3019554A1
    申请号:FR1453075
    申请日:2014-04-07
    公开日:2015-10-09
    发明作者:Bertrand Fanget；Abdelhakim Koudil；Alexandre Pagot；Romain Corroyer；Joana Fernandes
    申请人:IFP Energies Nouvelles IFPEN；
    IPC主号:
    专利说明:

    [0001] FIELD OF THE INVENTION 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.
    [0002] The present invention describes means for restoring a balanced thermal balance by exchange of material flow between the FCC and the aromatic complex (CA). EXAMINATION OF THE PRIOR ART It is known in the prior art that the cracking of highly hydrogenated sections in FCC processes poses certain problems for thermal loopback, because these charges are not good precursors of coke and imply that the Thermal balance of these units can only be achieved by external heat input to the process. It is common to find inventions that offer to burn in the regenerator very heavy loads rich in carbon of the "torch oil" type. Other inventions describe the recycle of a coker cutter in the stripper or in a bypass capability of the stripper. The present invention proposes to recycle to the FCC unit a coking cut from the aromatic complex. 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. It is not in the practice of a person skilled in the art to link processes making it possible to recover the BTXs formed in the FCC units, since these high-added-value molecules are embedded in effluents from which it is difficult to remove them. extract at low cost. The integration of FCC with the aromatic complex proposes the recycle of the light cracked naphtha fraction, called "LCN" cut formed in the FCC, to the aromatic complex (CA) to extract aromatics of commercial interest.
    [0003] 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.
    [0004] 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. Furthermore, 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.
    [0005] SUMMARY DESCRIPTION OF THE FIGURES FIG. 1 represents a diagram of the method according to the present invention in its basic version. The following abbreviations have been used to denote the main units: HCV for hydroconversion, HDT for hydrotreating, FCC for catalytic cracking, RC for catalytic reforming of gasoline, CA for the aromatic complex. FIG. 2 represents a first variant of the basic scheme in which the raffinate stream from the aromatic complex is divided into two streams, a light stream that is mixed with the FCC feedstock and a heavy stream that is mixed with the charge of the catalytic reforming of gasolines.
    [0006] FIG. 3 represents a second variant of the basic scheme in which a stream composed mainly of C4 and C5 olefins is isolated at the level of the cold box separation (SBF) downstream of the FCC to be sent to an oligomerization unit (OLG) to produce longer olefins fed to the FCC unit mixed with the main charge. SUMMARY DESCRIPTION OF THE INVENTION The present invention can be defined as a process for the production of 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 of gasoline (RC). These three units work in synergy in the sense that they exchange both material and heat streams. The so-called LCN feedstock from the catalytic cracking unit (FCC) 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, i.e., ranging from 150 ° C to 170 ° C. This definition of the LCN cut remains valid for the whole of this text. For simplicity we continue to note PI-160 ° 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 admixture with the charge (2) of the FCC unit, where it provides, by its power, the heat necessary for the closure of the heat balance.
    [0007] Finally, 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. More specifically, the present invention can be defined as a process for the production of light olefins and BTX from a first hydrotreated VGO or unconverted oil (UCO) feedstock resulting from a hydroconversion process, or from any mixture of these two feeds, and a second naphtha feedstock, an initial boiling point of greater than 30 ° C and a boiling point of less than 220 ° C, said process comprising a cracking unit Catalyst (FCC) treating the hydrotreated VGO feed or the unconverted oil (UCO), a catalytic reforming unit (RC) treating the so-called naphtha feed (30 ° C-220 ° C), and an aromatic complex ( CA) fed by the catalytic reforming (CR) effluents, and the so-called LCN fraction (PI-160 ° C) of the FCC effluents, said process comprising the following sequence of operations: - The hydrotreated VGO feedstock or the unconverted UCO (2) oil, or any mixture of the two x charges, in an FCC unit that produces effluents (6) that are sent to a fractionation unit (FRAC) from which a light fraction (8), an LCN cut (PI-160 ° C), a HCN cut is extracted (160 ° C-220 ° C), and a heavy fraction (220 ° C +), - The light fraction (8) is sent to a separation box, called cold box (BF), for separating the light olefins, ethylene and propylene, the dry gases (H2 and CH4), and the light paraffins in C2, C3 and C4, the gasoline cut (PI-160 ° C), called LCN (9), is sent to the aromatic complex (CA) in mixing with the effluents (5) of the catalytic reforming (RF) to form the charge (10) of the aromatic complex (CA), - the HCN cut (160 ° C-220 ° C) is upgraded as such, - the heavy fraction (220 ° C +) initial boiling point greater than 220 ° C which in this case has a significant cracking potential, is recycled to the FCC - is sent hydrotreated naphtha (4) as a feedstock catalytic reforming unit (REF), - The BTX is extracted from the aromatic complex (CA), a raffinate (12) defined as the non-aromatic part of the effluents, which is sent at least partially in mixture with the feed ( 2) of the FCC, and a so-called heavy aromatic fraction (11) which is also sent in admixture with the FCC charge (2). According to a first variant of the process of the present invention, 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).
    [0008] According to a second variant of the process according to the invention, 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).
    [0009] According to a third variant of the process according to the invention, 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). In the end, the advantages that are provided by the present invention can be summarized in the following points: 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 aromatics recoverable in petrochemicals derived from the aromatic complex (BTX) are 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 thermal balance.
    [0010] 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.
    [0011] 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 reforming unit, which further improves the thermal balance of the FCC. DETAILED DESCRIPTION OF THE INVENTION An FCC unit generally processes a heavy cut from the vacuum distillation unit 15 such as VGO (abbreviation for "vacuum gas oil" terminology), or an atmospheric residue alone or in admixture. However, 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. Such a filler has, because of its high hydrogen content (greater than 13.5% by weight of the filler), a high potential for light olefins, in particular propylene (C 3), butenes (C 4), but also ethylene. (C2 =). This filler also has the advantage of containing few nitrogenous and sulfur-containing 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 into mixing with an ex-reforming charge. This LCN feed may optionally be blended with a steam cracker gasoline feed to be hydrotreated prior to going to the aromatic complex.
    [0012] 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.
    [0013] The flexibility of the FCC also allows secondary loads to be treated in relation to the main load. These secondary feedstocks generally represent less than 10% by weight of the main feedstock 10 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. In the context of the present invention, i.e., the proximity of the FCC unit and the aromatic complex (CA), it is easy to recycle the raffinate stream to the FCC unit as secondary charge. The heavier effluents from the aromatic complex (CA), generally aromatic with 10 or more carbon atoms, have the advantage of being very cokant during a catalytic cracking. 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 to increase the BTX yield of the aromatic complex. Figure 1 shows a diagram of the sequence according to the present invention. The feedstock entering the hydroconversion unit (HCV) is a heavy feedstock generally from vacuum distillation.
    [0014] It is most often a vacuum distillate, noted VGO, whose initial boiling point is generally greater than 340 ° C, and whose end point may be variable, but is generally less than 700 ° C.
    [0015] For example, it is possible to have a light vacuum distillate (LVGO) or a HVGO heavy vacuum distillate, depending on the intermediate cutting point adopted. At the output of the conversion unit (HCV), the unconverted part, the so-called 340 ° C + portion, (denoted UCO) is purified with very little sulfur and nitrogen compared to the original charge, but Above all, it has been significantly enriched in hydrogen, reaching levels above 13.5% and a relatively low residual carbon of less than 0.5%. It is all or part of this unconverted oil that is sent to FCC catalytic cracking.
    [0016] In summary, 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 (HDT) 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. The desaturation of the molecules produces hydrogen which is accompanied by an enrichment of the essence fraction in aromatics. This aromatic-rich fraction is then sent to the aromatic complex (CA) for extraction / production of aromatics including benzene, toluene and xylenes (BTX).
    [0017] FIG. 1 shows how the FCC is connected to the reforming (RC) complex-aromatic complex (CA) by two flows: a first stream consisting of the so-called LCN effluent (PI-160 ° C.) resulting from FCC, which is sent to the aromatic complex, in admixture with the main charge of said aromatic complex (CA). - A second stream is constituted by the heavy aromatic effluent from the aromatic complex, which can be defined as the set of molecules of more than 10 carbon atoms and which is sent to the FCC mixed with the charge of said FCC. 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 about 25% -35%. % of the 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. Thus, this heavy aromatics stream (11) will convert to yielding BTX aromatics and additional coke (relative to the highly hydrogenated feed) permitting the closure of the overall heat balance of the FCC unit. For improved FCC production of light olefins, the raffinate is recycled to the raffinate from the aromatic complex so that it is predominantly cracked with propylene, butenes and ethylene. In the other direction, the FCC contributes to a higher production of BTX aromatics, since the lightly cracked LCN gasoline portion, which is almost free of sulfur and other impurities due to the heavy load hydroconversion stage, is sent to the aromatic complex (CA) to extract and process the aromatics to produce a maximum of benzene, toluene and para-xylene. This implementation between the two complexes, allows very significant synergies.
    [0018] Figure 2 shows a variant of the present invention wherein 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. In addition, 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) from the fractionation of the FCC can be preferably 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 the thermal balance of the FCC unit. FIG. 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 to be further separated and thus allow to isolate the fraction C4 and C5 for recycling into the reaction section of the FCC or send it in an oligomerization unit (OLG) and then send the oligomerate thus formed in the FCC reactor, increasing yields of light olefins. Naturally, the variants of FIGS. 2 and 3 can perfectly be implemented separately or combined. Optionally, the FCC can be equipped in addition to the main reactor treating the highly hydrogenated feed 25, another reactor, called secondary, dedicated to various light cuts whose cracking conditions can be more severe. FCC + CA Complex Flux Characteristics The first feedstock (1) entering the FCC-Petrochemical Unit is an unconverted oil from a VGO hydrocracking unit or highly hydrotreated VGO. Table 1 gives property ranges for such a type of load.
    [0019] Typical load Min / Max Nitrogen compounds mg / kg 7.84 1 - 50 Conradson carbon <0.2% <1 P (0.50%) ° C 244.1> 240 mp (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 / m 4.9 2 - 10 Resins% m / m 0.7 <5 Vanadium (FX) mg / kg <2 <5 Nickel (FX) mg / kg <2 <5 Sulfur (FX) ppm 54.6 <100 Table 1 - Characteristic of the main FCC charge 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 FCC liquid effluents is a hydrocarbon fraction whose initial boiling point (P1) is 220 ° C. This stream concentrates most of the sulfur and nitrogen compounds initially present in the feedstock, 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 virtually aromatic-free cut. 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. Operating Conditions of the FCC Unit The FCC unit is a catalytic cracking unit of highly hydrotreated VGO 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 in riser flow or down flow. 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 burnt in a flow of air generating combustion fumes and making it possible to recover most of the heat. necessary for the reactor in the form of sensible heat of the catalyst itself. The FCC unit has its own hydrocarbon effluent treatment section with in particular a plant gas allowing a separation of the light olefins (ethylene, propylene, butenes) from the other gases: hydrogen, methane, ethane, propane. The heavier portion 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). The intermediate portion comprising the hydrocarbons with 4 and 5 carbon atoms can be either recycled directly to the FCC or preferably sent to an oligomerization unit in order to obtain a polyC4 / C5 oligomer whose crackability in catalytic cracking processes is significantly higher than that of non-oligomerized compounds, either to be upgraded to their dedicated pool. The FCC unit is operated preferably at high severity (high riser output temperature, strong catalyst ratio on charge: C / O). The range of operating conditions is given in Table 2 below. Condition Min Max TSR, ° C 500 650 C / O, kg / kg Table 2 - Operating Temperature Range of the FCC Unit The catalyst can 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 of ZSM-5, or may even be composed of 100% ZSM-5.
    [0020] EXAMPLES Laboratory tests with commercial FCC catalysts with or without ZSM-5 additives were conducted to validate the results of the present invention. The tests were conducted under high severity conditions for simulating the FCC unit: TSR = 605 ° C ± 5 ° C and C / O = 15 ± 1 kg / kg. Example 1: Cracking of a Highly Hydrogenated Heavy Load (Not in Accordance with the Invention) This example shows the separate yields of one FCC unit treating a converted hydrocracker type feedstock of a vacuum distillate whose composition type is given in Table 3 below, and those of an aromatic complex allowing the recovery of BTX, without integration of the FCC units and the aromatic complex. FCC load Nitrogen compounds mg / kg 7.84 Conradson carbon <0.2% PI (0.50%) ° C 244.1 PF (99.50%) ° C 649.4 Hydrogen (NMR)% m / m 14 , 2 SPGR 15 ° C kg / m3 844.8 Saturated% m / m 92.1 Aromatic% m / m 4.9 Resins% m / m 0.7 Vanadium (FX) mg / kg <2 Nickel (FX) mg / kg <2 Sulfur (FX) ppm 54.6 Table 3 - Characteristic of the FCC cracked load. The yield structure given in Table 4 was obtained during the cracking of this typical feed at a high severity: Temperature = 607 ° C at the output Riser, C / O = 16. Compound / Cut% wt C2 = 2, 8 C3 = 22.4 C4 = 23.1 LCN (PI-160 ° C) 28.7 HCN (160-220 ° C) 3.8 Heavy fraction (220 + ° C) 3.3 Coke 3.1 PI Details -160 ° C 28.7% wt NormalParaffins 1.2 Iso-Paraffins 6.7 Naphthenes 0.6 Olefins 16 Di-Olefins 0.1 Aromatic 4.1 C6 Aromatic 0.6 C7 Aromatic 0.8 C8 Aromatic 2.4 Table 4 - Crude compound / crack yield of unconverted hydrocracking effluent. In the case of a commercial unit of 10,000 tons / day of hydrogenated heavy load, we obtain the following flow rates for the main components of interest for petrochemicals: Flow rate (ton / day) Ethylene 280 Propylene 2240 Butenes 2310 C6 Aromatic 60 C7 Aromatic 80 C8 Aromatic 240 Coke 310 Table 5 - FCC Output Rates of the Compounds of Interest.
    [0021] Under the operating conditions of the FCC, and in total combustion with the regenerator, a deficiency in heating power of 20% to the regenerator is observed. This deficit is only recoverable in an FCC unit by the burning in the regenerator of a "torch oil" type cut or any other type of fuel. For a commercial gasoline reforming unit that processes 6000 tonnes / day of an initial point naphtha at 85 ° C and a final point at 180 ° C, and for a moderate reformer severity giving an RON of 95, the following flow rates of aromatics and fluxes with the FCC: Flow rate (ton / day) C6 Aromatic 372 C7 Aromatic 1134 C8 Aromatic 1272 Heavy aromatics 426 Raffinate 1326 Table 6 - Some flows out of an aromatic complex treating a flow Example 2: Cracking of a heavy aromatic charge from an aromatic complex in addition to the highly hydrogenated heavy charge Under the same operating conditions as for Example 1 Example 2 implements the synergies between the FCC and the aromatic complex according to the scheme of Figure 1, by sending to the reaction section of the FCC, the heavy aromatics feedstock (11) which is an effluent of aromatic compounds. (CA) whose initial point of distillation (5%) is about 190 ° C. This heavy aromatic charge (11) is composed of 100% aromatics; the majority (70% 25 m / m) are compounds with 11 or 12 carbon atoms; the remaining 30% by weight are aromatics with 10 carbon atoms.
    [0022] The treatment of this secondary charge is done in a mixture with the main charge of the FCC defined in Example 1.
    [0023] The main effluents are then as follows: Flow rate (ton / day) Ethylene 285 Propylene 2245 Butenes 2312 C6 Aromatic 476 C7 Aromatic 1287 C8 Aromatic 1535 Coke 384 Table 7 - Output flow rates of the compounds of interest after integration of the FCC with the aromatic complex.
    [0024] This improves the production of coke for the FCC and with the increase of the inlet temperature of the FCC charge, the thermal balance of the FCC is correctly achieved, while Example 1 showed a deficit of 20% of the FCC. thermal balance of the FCC unit.
    [0025] For the aromatic complex (CA), the production of aromatics is significantly improved due to the LCN feed from the FCC. The yields of BTX are thus increased by 28% benzene, 13% (toluene) and 21% (xylenes), respectively, compared to one unit without the proximity of an FCC.20
    权利要求:
    Claims (4)
    [0001]
    CLAIMS 1- A process for the production of light olefins and BTX from a first hydrotreated VGO or unconverted oil (UCO) feedstock resulting from hydrocracking, or from any mixture of these two feeds, and from a second naphtha feedstock having an initial boiling point of greater than 30 ° C and boiling point of less than 220 ° C, said process comprising a catalytic cracking unit (FCC) treating the hydrotreated VGO feed or the oil unconverted, a catalytic reforming unit (REF) treating a so-called naphtha filler (30 ° C-220 ° C), and an aromatic complex (CA) fed by catalytic reforming effluents (REF) and the so-called LCN fraction (PI-160 ° C) FCC effluent, said process comprising the following sequence of operations: - The hydrotreated VGO feedstock or unconverted UCO oil (2) or any mixture of both is sent to an FCC unit which produces effluents (6) which are sent in a Fractionation unit (FRAC) from which a light fraction (8), an LCN cut (PI-160 ° C), an HCN cut (160 ° C-220 ° C), and a heavy fraction (220 ° C +) are extracted. The light fraction (8) is sent to a cold box (BF) separating the light olefins, ethylene and propylene, the dry gases (H2 and CH4), and the C2, C3 and C2 light paraffins. C4, - The gasoline (PI-160 ° C) called LCN (9) is sent to the aromatic complex (CA) mixed with the effluents (5) of the catalytic reforming (RF) to form the charge (10) of the aromatic complex (CA), - the HCN cut (160 ° C-220 ° C) is recovered as such, - the heavy fraction (220 ° C +) of initial boiling point above 220 ° C, is recycled to the FCC - The hydrotreated naphtha (4) is fed as a feedstock for the catalytic reforming unit (REF). The BTX is extracted from the aromatic complex (CA), a raffinate (12) defined as the non-aromatic part of the effluents. which is sent at least partly in admixture with the FCC charge (2), and a so-called heavy aromatic fraction (11) which is also mixed with the FCC charge (2).
    [0002]
    2) - Process for the production of light olefins and BTX according to claim 1, wherein 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).
    [0003]
    A process for producing light olefins and BTX from a catalytic cracking unit (FCC) according to claim 1, wherein the C4 and C5 light olefins from the separation box (BF) are sent to an oligomerization unit (OLG), and the effluents of said oligomerization unit (16) are mixed with the feedstock (2) in the catalytic cracking unit (FCC).
    [0004]
    The process for the production of light olefins and BTX according to any one of claims 1 to 3, wherein the charge (2) of the FCC unit is preheated in the convection zone of catalytic reforming furnaces (FREF). before being introduced as a feedstock of the catalytic cracking unit (FCC).
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    FR3038904A1|2017-01-20|METHOD FOR REALIZING THE THERMAL BALANCE CLOSURE ON A CATALYTIC CRACKING UNIT OF NAPHTHA DITE NCC
    WO2020249498A1|2020-12-17|Process for the production of olefins, comprising hydrotreatment, deasphalting, hydrocracking and steam cracking
    同族专利:
    公开号 | 公开日
    JP2015199956A|2015-11-12|
    CN104974791A|2015-10-14|
    US20150284644A1|2015-10-08|
    RU2015112094A3|2018-10-12|
    EP2930224A1|2015-10-14|
    FR3019554B1|2017-10-27|
    RU2672913C2|2018-11-21|
    RU2015112094A|2016-10-20|
    US9650579B2|2017-05-16|
    KR20150116412A|2015-10-15|
    JP6539475B2|2019-07-03|
    CN104974791B|2018-11-06|
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    法律状态:
    2016-04-20| PLFP| Fee payment|Year of fee payment: 3 |
    2017-04-26| PLFP| Fee payment|Year of fee payment: 4 |
    2018-04-13| PLFP| Fee payment|Year of fee payment: 5 |
    2019-04-25| PLFP| Fee payment|Year of fee payment: 6 |
    2020-04-29| PLFP| Fee payment|Year of fee payment: 7 |
    2021-04-27| PLFP| Fee payment|Year of fee payment: 8 |
    优先权:
    申请号 | 申请日 | 专利标题
    FR1453075A|FR3019554B1|2014-04-07|2014-04-07|PROCESS FOR PRODUCING LIGHT OLEFINS AND BTX USING AN FCC UNIT FOR VERY HYDROTREATED VGO-TYPE HEAVY LOAD, COUPLED WITH A CATALYTIC REFORMING UNIT AND AN AROMATIC COMPLEX PROCESSING A NAPHTHA-TYPE LOAD|FR1453075A| FR3019554B1|2014-04-07|2014-04-07|PROCESS FOR PRODUCING LIGHT OLEFINS AND BTX USING AN FCC UNIT FOR VERY HYDROTREATED VGO-TYPE HEAVY LOAD, COUPLED WITH A CATALYTIC REFORMING UNIT AND AN AROMATIC COMPLEX PROCESSING A NAPHTHA-TYPE LOAD|
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    EP15305501.7A| EP2930224A1|2014-04-07|2015-04-03|Method for producing light olefins and btx using an fcc unit treating a highly hydrotreated vgo heavy feedstock, coupled with a catalytic reformer unit and an aromatic complex treating a naphtha feedstock|
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    US14/680,542| US9650579B2|2014-04-07|2015-04-07|Process for production of light olefins and BTX using an FCC unit processing a heavy feedstock of the highly hydrotreated VGO type, coupled with a catalytic reforming unit and an aromatic complex processing a naphtha-type feedstock|
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