• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
  • 同族专利
  • 引用文献
  • 法律状态
  • 优先权
    • 专利摘要:
    The present invention relates to a process for the production of light olefins and BTX using a catalytic cracking unit NCC treating a naphtha feed, and an aromatic complex. It makes it possible to exploit synergies between these two units. The thermal balance of the NCC, which is intrinsically deficient in coke, is solved by the optimal use of the heat of the reforming furnaces in order to preheat the load of the NCC, and by the introduction in mixture with the naphtha of at least a part of the raffinate. derived from the aromatic complex.
    公开号:FR3019555A1
    申请号:FR1453076
    申请日:2014-04-07
    公开日:2015-10-09
    发明作者:Bertrand Fanget；Abdelhakim Koudil；Romain Corroyer；Alexandre Pagot；Joana Fernandes
    申请人:IFP Energies Nouvelles IFPEN；
    IPC主号:
    专利说明:

    [0001] FIELD OF THE INVENTION The interest in cracking paraffinic charges of the straight-run gasoline type in FCC units in order to upgrade them to propylene and ethylene is relatively recent. This interest stems from the need for light olefins, ethylene and propylene for petrochemicals, in addition to the traditional source of steam cracking. Gasoline or naphtha type cracking leads to a modification of the operating conditions of the FCC, and to the use of ZSM-5 type zeolite. Currently, the market price differential between light olefins and gasoline is at least in part an incentive to take better advantage of gasoline by turning it into these light olefins. In addition, the improvement of zeolitic catalysts allows more interesting yields in this transformation to light olefins. This new type of FCC unit is commonly called NCC for "Naphtha Catalytic Craking" which can be translated by catalytic cracking of naphtha. The cracking reactions, in addition to producing olefins, are accompanied by the formation of aromatic molecules which were generally not valued as such, since the cost of their separation would prove to be of little or no profit. Furthermore, the cracking of light cuts in the FCC process is a problem because this type of charge does not produce enough coke under the conditions of the FCC, and the thermal balance of the FCC can be reached only by external heat input. to the process. The present invention provides an original solution for solving this problem by exchange of flux with the aromatic complex. EXAMINATION OF THE PRIOR ART It is common to find documents which propose recycling to the regenerator of a catalytic cracking unit (FCC) cuts with high potential of coke of the "slurry" type.
    [0002] Other documents describe the cokant cutting recycle in the FCC stripper, or in a bypass capability of the stripper. The invention proposes recycling to the reactor of the NCC unit a coking cutoff from the aromatic complex itself. The NCC unit is also recycled to a non-aromatic raffinate to increase the production of light olefins. In summary, the catalytic cracking of a naphtha-type fraction allows an increase in yields of light olefins compared to an FCC working on conventional feeds, and the problem of the closure of the heat balance of the NCC is solved by the use of a heavy aromatics cut from the aromatic complex. SUMMARY DESCRIPTION OF THE FIGURES FIG. 1 shows the diagram of the method according to the invention in its basic version. In this version the raffinate from the aromatic complex (CA) is directly sent, at least in part, in admixture with the light naphtha from the separation unit (SPLIT1) placed upstream of the NCC to supply the NCC unit. Fractionation placed upstream of the NCC unit and noted (SPLIT1) makes it possible to separate the starting naphtha fraction into a light fraction called "light naphtha" which feeds the NCC, and a heavy fraction called "heavy naphtha" which feeds the feedstock. catalytic reforming. FIG. 2 represents a first variant of the process scheme according to the present invention in which the raffinate derived from the aromatic complex is sent to a separation column (SPLIT 2) which makes it possible to separate a first lighter raffinate (stream 13) which is introduced as a mixture with the light naphtha feed to the NCC unit, and a second heavier raffinate (feed 14) which is directed to the catalytic reforming unit. FIG. 3 represents a second variant of the process scheme according to the invention which, in addition to the modification of the first variant, introduces a recycling of light paraffinic hydrocarbons of the ethane, propane and butane type mixed with the light naphtha feedstock of the NCC (stream 15).
    [0003] FIG. 4 represents a third variant of the process scheme according to the invention which, in addition to the units already present in the preceding variants, introduces an oligomerization unit (OLG) of the C4 and C5 sections, so as to produce oligomers more easily crackable, and likely to produce even more propylene and ethylene.
    [0004] SUMMARY DESCRIPTION OF THE INVENTION The present invention describes a refinery and petrochemical process scheme that achieves integration between three units: the FCC processes a light naphtha-type feedstock, referred to as NCC, catalytic reforming which processes heavy naphtha, and the aromatic complex (CA) producing BTX. Integration between these three units is accomplished both by material flow exchanges, and also by the use of the convection zone of the reforming furnaces to preheat the NCC naphtha feedstock. The advantages of integration between the NCC unit and the aromatic complex (CA) can be summarized by the following points: Simultaneous production of light olefins and aromatics from a starting naphtha feedstock. The NCC unit benefits from the proximity of a very high charge to compensate for the coke deficiency of the light naphtha charge, and an additional charge in the form of the raffinate from the aromatic complex to produce more olefins. light. The integration of NCC into the aromatic complex provides a process scheme that ultimately reduces the outputs to fuel gas (H2 and C 1 essentially), light olefins (C2 = and C3 =) and BTX. The exhaustion cycle of the other effluents, such as the raffinate and the heavy aromatics fraction derived from the aromatic complex (CA), makes it possible both to increase the production of light olefins, ethylene and propylene, and to provide a balance sheet. thermal NCC. It is in this sense that we can speak of a real synergy between the NCC and the aromatic complex. The "heavy aromatics" flow of the aromatic complex (CA) is thus minimized or eliminated, to the benefit of coke produced during the catalytic cracking reaction, and burned at the regenerator of the NCC to ensure the thermal balance. The raffinate stream (12) from the aromatic complex is also minimized or eliminated to the benefit of light olefins produced by cracking in NCC. The load of the NCC is preheated by the furnaces of the catalytic reforming unit (FREF), preferably in the convection zone of the latter, which makes it possible to better balance the thermal balance of the NCC deficient in coke. More specifically, the present invention describes a process scheme for the simultaneous production of light olefins (mainly ethylene and propylene) and BTX using three synergistically operating units: one FCC unit treating a type charge. light naphtha called NCC, catalytic reforming (REF) of the heavy naphtha fraction, and a BTX-producing aromatic complex (CA). The scheme of the process according to the present invention can be described as follows: The process feedstock is a naphtha cut, the broadest definition of which is an initial point cut of at least 30 ° C and an end point at plus 220 ° C. Any cut having a distillation range within the wide range of 30 ° C-220 ° C is, in the context of the present invention, considered a naphtha. For simplicity, 30 ° C and 220 ° C will be retained as the typical initial and final points of a naphtha section.
    [0005] The naphtha feed (1) distillation range 30 ° C-220 ° C is sent to a hydrotreatment unit (HDT) that removes the sulfur compounds and nitrogen contained in it.
    [0006] The hydrotreated naphtha feedstock (2) is sent to a separating unit (SPLIT1) which makes it possible to separate a light fraction called light naphtha, with a distillation interval of 30 ° C., and a heavy fraction called heavy naphtha. of distillation TM ° C-220 ° C. The value of the cutting point TM ° C can vary depending on the desired yields of final products (ethylene and propylene and BTX). Generally the temperature Tm is between 80 and 160 ° C, and preferably between 100 ° C and 150 ° C, and more preferably between 110 ° C and 140 ° C. The light naphtha (3) is sent as a load of the NCC. The heavy naphtha (4) is sent as a feed to the catalytic reforming unit (REF). The effluents (6) of the NCC are separated in a fractionation unit (FRAC) which makes it possible to separate a light fraction (8) which is sent into a so-called cold box separation (SBF) which makes it possible to isolate the H2, the CH4 and C2 light paraffins, C3, C4, C5, and ethylene (C2 =) and propylene (C3 =). The heavy fraction (7) from the separator (FRAC) is sent in admixture with the effluents (5) of the catalytic reforming (REF) as feed (10) of the aromatic complex (CA). The aromatic complex (CA) extracts BTX, a raffinate (12), corresponding to the non-aromatic part of the effluents, which is sent at least in part as a mixture with the light naphtha (3) as the NCC feed, and a so-called heavy aromatic fraction (11) which is also mixed with the light naphtha (3) as a feedstock of the NCC to ensure by its coking power the heat balance of the latter.
    [0007] In a first variant of the process according to the invention, represented by FIG. 2, the raffinate effluent (12) of the aromatic complex (CA) is sent to a separation unit (SPLIT2) which makes it possible to separate a light fraction (13). which is mixed with the light naphtha feed (3) to the catalytic cracking unit (NCC), and a heavy fraction (14) which is mixed with the heavy naphtha feed (4) to the reforming unit catalytic converter (REF). In a second variant of the process according to the invention represented by FIG. 3, variant which can be combined with the first variant, light paraffins of C2 to C5 produced as effluents of the catalytic cracking unit (NCC) from the separation box (SBF) are mixed with the light naphtha feedstock (3) to the catalytic cracking unit (NCC) to increase the yield of light olefins, ethylene and propylene and improve transport and fluidization.
    [0008] In a third variant of the process according to the invention represented by FIG. 4, which variant can perfectly combine with the preceding variants, the light C 4 and C 5 molecules originating from the separation box (SBF) are sent to an oligomerization unit. (OLG), and the effluents of said oligomerization unit (OLG) are mixed with the light naphtha feedstock (3) in the catalytic cracking unit (NCC). Finally, in all the variants of the process according to the present invention, the fractional naphtha fraction (3) resulting from the fractionation (SPLIT1) is preferably preheated in the convection zone of the catalytic reforming furnaces (FREF) before being introduced as a feedstock. From the catalytic cracking unit (NCC). The process for producing light olefins and BTX according to the present invention preferably operates the NCC unit under severe cracking conditions, i.e. a reactor outlet temperature (ROT) of between 500 ° C. and 750 ° C, and a mass flow rate ratio of catalyst to mass flow rate (C / O) of 5 to 40.
    [0009] The process for the production of light olefins and BTX according to the present invention uses, for the NCC unit, a catalyst comprising a proportion of zeolite at least equal to 20%, and more particularly a proportion of ZSM-5 zeolite with less than 10% by weight relative to the total catalyst.
    [0010] DETAILED DESCRIPTION OF THE INVENTION An FCC unit generally processes a heavy cut from the vacuum distillation unit such as VGO (abbreviation of the English terminology Vacuum Gas Oil), or a vacuum residue, taken alone or as a mixture , or an atmospheric residue taken alone or in mixture. Sometimes, however, the load arriving at the FCC may be lighter due to prior pretreatment of the VGO for example, or because it comes from a conversion unit in which the initial charge has been enriched. hydrogen and has been freed from certain impurities. A recent adaptation of the FCC to even lighter loads, such as gasoline, also known as naphtha, aims to convert these streams to light olefins (ethylene and propylene), 20 high value-added products and starting points for the market. petrochemicals. An FCC unit dealing with naphtha type feeds is then called NCC. The major problem of cracking these naphtha type feeds is the low coke yield of the feed which makes it necessary to rethink the heat balance of the unit. In the present invention, this thermal balance problem of NCC is solved by synergism with an aromatic complex (CA). Figure 1 schematically depicts the aromatic complex with integration of a NCC unit, object of the present invention.
    [0011] The naphtha feed is a gasoline cut whose initial boiling point is greater than or equal to 30 ° C, and the final boiling point is generally less than or equal to 220 ° C. It is previously treated in a hydrotreatment unit (HDT) to rid it of sulfur compounds and nitrogen compounds likely to poison the downstream catalysts. The desulphurized / denitrogenated naphtha effluent is sent to a fractionation unit (SPLIT1). The light part resulting from this fractionation (stream 3) is sent to the NCC unit, while the heavy part (stream 4) is sent to the catalytic reforming unit (REF) after having been heated to the required level in a furnace. reforming (FREF). The downstream fractionation of the NCC unit is represented by the unit (FRAC) and can be adjusted to direct the production to more light olefins, or to more aromatics. The heavy stream (7) leaving the fractionation unit (FRAC) is directed to the aromatic complex (CA). The light stream (8) leaving the fractionation unit (FRAC) is directed to a separation unit (SBF) for separating the light olefins ethylene and propylene, hydrogen and methane, and propane and butane. The fractionated heavy stream (7) is mixed with the effluents of the catalytic reforming unit (5) to form the feedstock (10) of the aromatic complex (CA) from which the BTX is extracted, and an aromatic section. heavier corresponding to the flow (11). The non-aromatic fraction called raffinate corresponds to the flow (12) and, in the basic version of the scheme according to the invention, is mixed with the light fraction of the naphtha (3) as the feedstock of the NCC unit. The units involved in the present scheme, ie NCC, catalytic reforming (REF) and aromatic complex (CA) make it possible to produce ethylene from a starting naphtha. and propylene, and BTX. Some variants of the basic scheme can produce more propylene or ethylene. The aromatic complex (CA) makes it possible to produce benzene, toluene and xylenes (globally noted BTX), and especially para-xylene, a petrochemical base product. The heavy aromatics stream (stream 11) is recycled at least in part to the NCC as an additional feed, mixed with the light naphtha feedstock (3), and ensures the heat balance of the NCC. The flux called raffinate (12) corresponding to the non-aromatic portion of the aromatic complex (CA), is recycled at least in part to the NCC as an additional charge producing light olefins.
    [0012] According to the scheme shown in Figure 2, the raffinate (12) can be separated into two fractions in a separation unit noted (SPLIT2), the light part (13) going to the NCC to produce mainly olefins and a few aromatics, and the reforming heavy portion (14) (REF) to produce additional aromatics.
    [0013] The unit (NCC) after fractionation separation (FRAC) and the cold box (SBF) produces a C6 + flux (denoted 9) containing an appreciable quantity of aromatics which are introduced in admixture with the heavy fractionation fraction (FRAC). ) to form the flow (7) supplying the aromatic complex (CA) mixed with the effluents (10) of the catalytic reforming (REF). The non-aromatic fraction of the aromatic complex (AC) effluents, referred to as the raffinate (stream 12), is returned, in whole or in part, to the NCC forming an additional charge to the main charge (3) of the NCC. This additional charge makes it possible to increase the final yields of light olefins C2 = and C3 =. NCC products other than ethylene or propylene can be recycled in this unit. It is also possible to use the so-called "dry gas" part, excluding ethylene, and the so-called "LPG" part, excluding propylene, as fuel gas in the catalytic reforming furnaces (FREF).
    [0014] In FIG. 3, another variant is considered in which C2 and C3 paraffins as well as C4 and C5 cuts originating from cold box separation (SBF) are recycled to the NCC, in a mixture or separately.
    [0015] Another way to recycle C4 and C5 cuts from NCC is to first pass through an oligomerization unit (OLG) to produce oligomers more easily crackable, and likely to produce even more propylene and ethylene. This variant is illustrated in FIG.
    [0016] In all these schemes, the reforming heat exchange train is used to increase the temperature of the light naphtha (3) going to the NCC. This preheating of the NCC load saves the calories needed for the thermal balance of the NCC. The thermal balance of the NCC is ensured by the recycle of the heavy aromatics (HA) section, flow noted (11), leaving the aromatic complex (CA). This section of heavy aromatics can be defined as consisting of compounds with a carbon number greater than 8. This highly aromatic cut is a strongly cokantic cut which will make it possible to generate the quantity of coke necessary for the closure of the thermal balance of the carbon dioxide. NCC unit.
    [0017] The NCC unit is a naphtha catalytic cracking (NCC) unit having at least one main reactor operating either in riser flow or down flow. In the following we will talk about reactor without specifying the type of flow since the present invention covers the two possible flow modes. Alternatively, the NCC unit may have a secondary reactor, type "riser" or "downer" to crack recycles or additional flows separately. It has a separation-stripping section in which the catalyst is separated from the hydrocarbon effluents.
    [0018] It furthermore has a regeneration section of the catalyst in which the coke formed in the reaction and deposited on the catalyst is burned in order to recover in the form of sensible heat of the catalyst, part of the heat required in the reactor.
    [0019] The NCC unit has its own hydrocarbon effluent treatment section including a gas treatment section allowing a separation of light olefins (ethylene, propylene) from other gases: hydrogen, methane, ethane, propane. This separation section is represented by the assembly formed by the fractionation of the effluents (FRAC) and the cold box of separation of the light compounds (that is to say less than 5 carbon atoms) noted SBF. This set of fractionation unit well known to those skilled in the art will not be described in detail.
    [0020] The heavier portion of the hydrocarbon effluents is treated in a separation section (FRAC) comprising at least one fractionation unit for recovering the C6 + cut (stream 7) which is sent to the aromatic complex (CA). The intermediate portion comprising the hydrocarbons with 4 and 5 carbon atoms can be either recycled directly to the NCC, or sent to an oligomerization unit (OLG) to obtain polyC4 / C5 type cuts whose crackability (c '). that is, the cracking potential) in the NCC is significantly higher than that of the non-oligomerized compounds, or still be upgraded to dedicated pools.
    [0021] The NCC unit is operated preferably at high severity, that is to say with a high reactor output temperature (ROT) and a high C / O ratio (ratio of the catalyst flow rate to the feed rate entering the NCC the two flow rates being mass). The range of operating conditions is given in Table 1 below.
    [0022] Condition Min. Max ROT, ° C 500 750 C / O 5 Table 1- FCC unit (NCC) operating conditions range The catalyst can be any type of acid catalyst, with a preference for a catalyst containing some proportion of zeolite, preferably greater than 20% by weight of the total catalyst. A typical FCC catalyst comprising alumina, zeolite Y, and zeolite ZSM-5 is an example of a catalyst that could be used. EXAMPLES ACCORDING TO THE INVENTION Laboratory tests on a unit simulating NCC were conducted on a very paraffinic light naphtha section, on a light section taken at the outlet of the catalytic reforming unit, and on an aromatic section representative of flow called "heavy aromatics" (denoted HA) from the aromatic complex. The tests were carried out with high severity (temperature> 650 ° C and C / O> 15) in order to simulate as closely as possible the operating conditions of the NCC. These tests make it possible to establish yield structures for cracking a load of NCC. For reforming the naphtha, severity conditions for obtaining an RON around 95 were used.
    [0023] Example 1: Naphtha FCC unit (according to the prior art)) The first example makes it possible to justify the interest of the proximity of the aromatic complex and the NCC unit in order to extract the aromatics produced during the cracking of a charge type 5 straight-run gasoline. Table 2 below describes the chemical family structure of a paraffinic naphtha whose distillation range is between 55 ° C and 115 ° C. The following table 3 provides the yield structure of the products resulting from the cracking of this feedstock on a simulated riser unit with a short contact time and a high degree of severity. Composition (% by weight) N-Paraffins 28.10 I-Paraffins 29.98 Naphthenes 33.67 Olefins 1.03 Di-Olefins 0.13 Aromatics 7.08 Table 2 - Composition of FCC Naphtha per family of hydrocarbons. The cracking of this high-severity naphtha (T = 650 ° C, C / O = 15) leads to the following mass yields for the molecules of interest in our case: Yield (% wt) Ethylene 12.63 Propylene 18.01 Butenes 8.51 C6 Aromatic 4.31 C7 Aromatic 7.13 C8 Aromatic 2.25 Coke 0.14 Table 3 - Main yields of cracking.
    [0024] The yields of ethylene and propylene are significantly higher than for a conventional VGO FCC. On the other hand, the coke yield is much lower than for a conventional FCC. With this lower coke yield, an external supply of heat to the regenerator is necessary, it even represents 95% of the heat necessary to ensure a balance between the reactor and the regenerator. For a naphtha feedstock flow rate (Table 2) of 5000 ton / hour, the flow rates of the various cracking effluents are given in Table 4 below. Flow rate (ton / hour) Ethylene 631 Propylene 900 Butenes 426 C6 Aromatic 215 C7 Aromatic 357 C8 Aromatic 112 Coke 7 Table 4 - Flow rates of the main NCC compounds with a capacity of 5000 tonnes / hour. Example 2: NCC unit coupled to an aromatic complex with a large naphtha cut cut at 50-50. In order to illustrate the advantages of the present invention, we considered a total naphtha of initial point 55 ° C, and of end point 160 ° C. The distilled fraction corresponding to the first 50% by weight, and whose properties are given in Table 2, is sent to the NCC under the conditions of severity described in Example 1, while the 115 ° C + portion represents approximately 50%. weight of the total, is sent to a catalytic reforming unit.
    [0025] The effluents from the two units are arranged as described in the figure of the invention 1. The flow rates leaving the NCC units and the aromatic complex (CA) for a total naphtha flow rate of 10,000 ton / hour are given in Table 5. below. Flow rate (ton / hour) Ethylene 717 Propylene 1110 Butenes 515 C6 Aromatic 674 C7 Aromatic 1382 C8 Aromatic 1199 Coke 98 Table 5 - Flow rates of the main NCC compounds + aromatic complex for a capacity of 10,000 ton / hour (5000 ton / hour NCC and 5000 ton / hour for reforming Compared to the situation of Example 1 (cracking of naphtha alone), the flow rates of light olefins are significantly improved: ethylene increases from 631 to 717 ton / hour, propylene increases by 900 to 1110 ton / hour, Butenes increase from 426 to 674 ton / hour.
    [0026] The coke yield of the NCC is very significantly increased. It goes from 7 to 98 tons per hour. This coke yield almost equilibrates the thermal balance of the NCC since we go from 95% of the thermal looping brought by an external source to the regenerator to only 17%.
    [0027] Example 3: NCC unit coupled to an aromatic complex with a wide naphtha cut cut at 40-60. If it is desired to establish the thermal equilibrium of the NCC and increase the production of aromatics, 40% of the total naphtha (55 ° C - 160 ° C) can be sent to the NCC and the remaining 60% to reforming (REF) . The flow rates are then as follows: Flow rate (ton / hour) Ethylene 608 Propylene 972 Butenes 447 C6 Aromatic 723 C7 Aromatic 1516 C8 Aromatic 1394 Coke 115 Table 6 - Flow rates of the main NCC compounds + aromatic complex for a capacity of 10,000 ton / hour (4000 ton / hour NCC, and 6000 ton / hour for reforming.) The yield of light olefins (ethylene, propylene, butenes) has decreased compared to the previous case (Table 5), but remains higher than in the In the case of NCC alone (Table 4), except for ethylene or a slight decrease, the aromatics yields are markedly increased by the fact that more charge has been added to the reforming and aromatic complex. NCC coke continues to increase as more heavy aromatics are sent to the reactor.
    [0028] With the coke yield obtained, the thermal balance of the NCC loop without resorting to an external heat source, which represents a very significant advantage from the point of view of the operating cost of the process.
    权利要求:
    Claims (7)
    [0001]
    CLAIMS 1- A process for the production of light olefins and BTX from an naphtha section with an initial boiling point of greater than 30 ° C. and a boiling point of less than 220 ° C., said process comprising a cracking unit catalytic converter (NCC) treating a light naphtha feedstock (30-TM ° C), a catalytic reforming unit (REF) treating a so-called heavy naphtha feedstock (TM ° C-220 ° C), and an aromatic complex ( CA) supplied by the effluents of the catalytic reforming (REF) and the fraction 60+ of the NCC effluents, said process comprising the following sequence of operations: - The naphtha feedstock (1) of initial boiling point is sent at least equal at 30 ° C. and at a boiling point of at least 220 ° C. in a hydrotreating unit (HDT) which makes it possible to eliminate the sulfur and nitrogen compounds which it contains. - The hydrotreated naphtha feedstock is sent ( 2) is in a separation unit (SPLIT 1) which makes it possible to separate a light naphtha light reaction, distillation range 40-TM ° C, and a heavy fraction called heavy naphtha distillate range Tm-220 ° C with TM ° C between 80 ° C and 160 ° C, preferably included between 100 ° C and 150 ° C, and very preferably between 110 ° C and 140 ° C, - The light naphtha (3) is sent as a load of the NCC, - The heavy naphtha (4) is sent as a load of the catalytic reforming unit (REF), - The effluents (6) are separated from the NCC in a fractionation unit (FRAC) which separates a light fraction (8) which is sent into a so-called cold box separation (SBF) which allows to isolate H 2, CH 4 and C 2, C 3 and C 4 light paraffins on the one hand, and ethylene and propylene on the other hand, - the heavy fraction (7) coming from the separator (FRAC) is sent ) in admixture with the effluents (5) of the catalytic reforming (REF) as feed (10) of the aromatic complex (CA), - extracting the aromatic complex (CA) BTX, a raffinate (12) defined as the nonaromatic part of the effluents, which is sent at least partly in admixture with the light naphtha (3) as a NCC feed, and a so-called heavy aromatic fraction (11) which is also mixed with the light naphtha (3) as a load of the NCC.
    [0002]
    2- Process for producing light olefins and BTX from a catalytic cracking unit (NCC) treating a light naphtha feed (30-TM ° C), a catalytic reforming unit (REF) treating a so-called heavy naphtha (TM ° C-220 ° C), and an aromatic complex (CA) fed by the catalytic reforming effluents (REF) and the fraction 60+ of the NCC effluents, according to claim 1, in wherein the raffinate effluent (12) of the aromatic complex is fed to a separation unit (SPLIT2) which separates a light fraction (13) which is mixed with the light naphtha feedstock (3) to the cracking unit catalytic converter (NCC), and a heavy fraction (14) which is mixed with the heavy naphtha feedstock (4) to the catalytic reforming unit (REF).
    [0003]
    The process for producing light olefins and BTX from a catalytic cracking unit (NCC) according to claim 2, wherein the C2 to C5 light paraffins produced as NCC effluents from the separation box. (BF) are mixed with the light naphtha feedstock (3) to the NCC catalytic cracking unit.
    [0004]
    A process for producing light olefins and BTX from a catalytic cracking unit (NCC) according to claim 3, wherein the C4 and C5 light olefins are sent to an oligomerization unit (OLG), and the effluents of said oligomerization unit are mixed with the light naphtha feedstock (3) in the catalytic cracking unit (NCC).
    [0005]
    5- Process for producing light olefins and BTX from a catalytic cracking unit (NCC) treating a light naphtha feed (30-TM ° C), a catalytic reforming unit (REF) treating a feedstock said heavy naphtha (TM ° C-220 ° C), and an aromatic complex (CA) fed by the effluents of the catalytic reforming and the fraction 60+ of the NCC effluents, according to any one of claims 1 to 4, wherein the light fraction naphtha fraction (3) from the fractionation (SPLIT1) is preheated in the convection zone of the catalytic reforming furnaces (FREF) before being introduced as a feedstock of the catalytic cracking unit (NCC).
    [0006]
    A process for producing light olefins and BTX from a catalytic cracking unit (NCC) according to any one of claims 1 to 5, wherein the operating conditions of the NCC are as follows; reactor outlet temperature of between 500 ° C and 750 ° C, and ratio of mass flow rate of catalyst to mass flow rate (C / O) is between 5 and 40.
    [0007]
    A process for producing light olefins and BTX from a catalytic cracking unit (NCC) according to any one of claims 1 to 6, wherein the catalyst used in the NCC unit comprises a proportion of zeolite ZSM-5 at least equal to 10% by weight relative to the total catalyst.
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    WO2017009109A1|2017-01-19|Method for balancing the heat budget on a naphtha catalytic cracking unit referred to as ncc
    FR2984914A1|2013-06-28|PROCESS FOR MAXIMIZING AROMATIC PRODUCTION
    FR2983865A1|2013-06-14|Conversion of coal to aromatic compounds involves liquefying, separating light hydrocarbons, hydrocracking, separating naphtha and heavier fractions, reforming naphtha to give hydrogen and reformate with aromatic compounds, and separation
    同族专利:
    公开号 | 公开日
    US9796937B2|2017-10-24|
    RU2015110987A|2016-10-20|
    RU2015110987A3|2018-09-28|
    AR099954A1|2016-08-31|
    EP2930226A1|2015-10-14|
    EP2930226B1|2019-07-10|
    US20150284646A1|2015-10-08|
    KR20150116415A|2015-10-15|
    RU2674016C2|2018-12-04|
    JP2015199957A|2015-11-12|
    CN104974003A|2015-10-14|
    JP6543501B2|2019-07-10|
    FR3019555B1|2016-04-29|
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    法律状态:
    2015-04-14| PLFP| Fee payment|Year of fee payment: 2 |
    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 |
    2021-01-08| ST| Notification of lapse|Effective date: 20201205 |
    优先权:
    申请号 | 申请日 | 专利标题
    FR1453076A|FR3019555B1|2014-04-07|2014-04-07|PROCESS FOR PRODUCING LIGHT OLEFINS AND BTX USING A CATALYTIC CRACKING UNIT NCC PROCESSING A NAPHTHA-TYPE LOAD, A CATALYTIC REFORMING UNIT AND AN AROMATIC COMPLEX|FR1453076A| FR3019555B1|2014-04-07|2014-04-07|PROCESS FOR PRODUCING LIGHT OLEFINS AND BTX USING A CATALYTIC CRACKING UNIT NCC PROCESSING A NAPHTHA-TYPE LOAD, A CATALYTIC REFORMING UNIT AND AN AROMATIC COMPLEX|
    RU2015110987A| RU2674016C2|2014-04-07|2015-03-26|Method for preparing light olefins and btx, using catalytic cracking unit ncc, processing naphtha-type feedstock, catalytic reforming unit and aromatic complex|
    ARP150101018A| AR099954A1|2014-04-07|2015-04-01|PROCEDURE FOR THE PRODUCTION OF LIGHTWEIGHT AND BTX OLEFINS THAT USES A CATALYTIC CRACKING UNIT, NCC, THAT TREATES A LOAD OF A NAFTA TYPE, A CATALYTIC REFORMING UNIT AND AN AROMATIC COMPLEX|
    EP15305502.5A| EP2930226B1|2014-04-07|2015-04-03|Method for producing light olefins and btx using an ncc catalytic cracking unit treating a naphtha feedstock, with a catalytic reformer unit and an aromatic complex|
    US14/679,075| US9796937B2|2014-04-07|2015-04-06|Process for the production of light olefins and BTX using a catalytic cracking unit, NCC, processing a naphtha type feed, a catalytic reforming unit and an aromatics complex|
    KR1020150048566A| KR20150116415A|2014-04-07|2015-04-06|Process for the production of light olefins and btx using a catalytic cracking unit, ncc, processing a naphtha type feed, a catalytic reforming unit and an aromatics complex|
    JP2015077301A| JP6543501B2|2014-04-07|2015-04-06|Process for producing light olefins and BTX using a catalytic cracking unitprocessing a naphtha-based feed, a catalytic reforming unit and an aromatics complex|
    CN201510161535.1A| CN104974003A|2014-04-07|2015-04-07|Method For Producing Light Olefins And Btx Using An Ncc Catalytic Cracking Unit Treating A Naphtha Feedstock, With A Catalytic Reformer Unit And An Aromatic Complex|
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