EP1463789B9 - Wasserdampfcracken eines fcc-benzins - Google Patents

Wasserdampfcracken eines fcc-benzins Download PDF

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Publication number
EP1463789B9
EP1463789B9 EP03712222A EP03712222A EP1463789B9 EP 1463789 B9 EP1463789 B9 EP 1463789B9 EP 03712222 A EP03712222 A EP 03712222A EP 03712222 A EP03712222 A EP 03712222A EP 1463789 B9 EP1463789 B9 EP 1463789B9
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EP
European Patent Office
Prior art keywords
weight
gasoline
component
naphtha
feedstock
Prior art date
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EP03712222A
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English (en)
French (fr)
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EP1463789B1 (de
EP1463789A2 (de
Inventor
François BOUVART
Robert Duchesnes
Claude Gutle
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Total Petrochemicals Research Feluy SA
TotalEnergies Marketing Services SA
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Total Petrochemicals Research Feluy SA
Total France SA
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Publication of EP1463789B1 publication Critical patent/EP1463789B1/de
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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/1037—Hydrocarbon fractions
    • C10G2300/104—Light gasoline having a boiling range of about 20 - 100 °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
    • C10G2300/1044—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
    • C10G2300/1081—Alkanes
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/20—Characteristics of the feedstock or the products
    • C10G2300/30—Physical properties of feedstocks or products
    • C10G2300/301—Boiling range
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/80—Additives
    • C10G2300/805—Water
    • C10G2300/807—Steam
    • 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
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S208/00—Mineral oils: processes and products
    • Y10S208/01—Automatic control

Definitions

  • the present invention relates to a process for the steam cracking of naphtha, a hydrocarbon composition suitable for steam cracking, a method for controlling a steam cracker, apparatus for controlling a steam cracker and a process for treating a sulfur gasoline feedstock.
  • olefins are mainly obtained by steam cracking charges obtained from refineries.
  • the available feedstocks are mainly naphtha feeds including paraffins, isoparaffins and aromatics.
  • a naphtha feedstock useful in steam cracking is known in the art as comprising a petroleum cutter whose lightest constituents have five carbon atoms and which has a final boiling point of about 200 ° C, the naphtha comprising high carbon components having a boiling point of at least 200 ° C.
  • Steam cracking of naphtha gives light olefins such as ethylene and propylene, and diolefins such as butadiene, as well as aromatics-containing gasolines.
  • the cracked product When a typical naphtha is subjected to steam cracking, the cracked product typically has the following composition (in% by weight) at the outlet of the oven: % in weight (approximate) Hydrogen 1 Methane 16 Acetylene 0.2 Ethylèue 22 Ethane 5 Methylacetylene, Propadiene 0.3 propylene 14 Propane 0.5 butadiene 4 C4 5 C5 4 Benzene 9 Toluene 5 Non-aromatic essence 2 Aromatic essence 6 oil 6 Total 100
  • the most interesting cuts in the cracked product are light olefins, namely ethylene and propylene.
  • Their yield is directly related to the presence of paraffins in the load. When straight chain paraffins are present, the formation of ethylene is favored. When isoparaffins are present, propylene formation is favored.
  • the relative yield of propylene is expressed as the ratio by weight of propylene to ethylene and is typically between 0.5 and 0.75.
  • DE-A-3708332 discloses a method of thermal cracking of ethylene in a steam cracker, wherein the ethylene is mixed with the naphtha so as to prepare a feedstock consisting essentially of naphtha and 10 to 80% by weight of ethylene, optionally containing , in addition to naphtha, fractions up to the fuel oil (boiling temperature up to 350 ° C) and / or by-products recycled from a petrochemical plant up to 50% of the naphtha.
  • This process has the disadvantage that it requires relatively large amounts of ethylene (at least 10%) in the raw materials and that then the ethylene (relative to ethylene feedstock) and propylene yields do not increase. are not particularly high.
  • US-A-3786110 describes a process for the production of unsaturated hydrocarbons obtained by pyrolysis, where the undesirable fractions are reduced by the addition to the products of the pyrolysis of a polymerization inhibitor containing asphaltic hydrocarbons.
  • a process for steam cracking of naphtha capable of providing a commercially acceptable yield of olefins, especially light olefins such as ethylene and propylene, while reducing the amount of paraffinic naphtha starting material required, is therefore necessary in the art. technical.
  • Ethane and propane are used as fillers for steam cracking, particularly in the United States, where natural gas, from which they are extracted, is abundant. These paraffins generate a large amount of ethylene (greater than 50%), when they are steam-cracked, which leads to treating these charges in specifically sized units for this type of charges.
  • Some refinery hydrocarbon gases, such as FCC gases contain substantial amounts of paraffins (ethane and propane) and olefins (ethylene, propylene).
  • FCC gases Some refinery hydrocarbon gases, such as FCC gases, contain substantial amounts of paraffins (ethane and propane) and olefins (ethylene, propylene).
  • FCC gases include substantial amounts of paraffins (ethane and propane) and olefins (ethylene, propylene).
  • Butane and propane are also used, either alone or mixed with naphtha, as steam cracker feedstocks. When attempting to use them exclusively, the problem of imbalance in the downstream section of a naphtha steam cracker is also apparent. Depending on the availability of the refinery or the market, these liquefied gases can be in excess and it is therefore interesting to use them as a steam cracker load.
  • DE-A-3708332 does not address the technical problem of producing an effluent whose composition corresponds to that produced by the steam-cracking of a naphtha.
  • the composition of the effluent particularly with respect to ethylene and propylene, is substantially altered compared to the cracking of naphtha. only under the same conditions, which can lead to significantly reduce the capacity of the steam-cracking unit.
  • the invention aims to at least partially satisfy these needs.
  • the invention provides a process for the steam-cracking of naphtha, which process comprises the passage in a steam-steam cracker of a hydrocarbon charge, which comprises a portion of a paraffinic naphtha modified with adding the combination of a first component, comprising a portion of gasoline, and a second component, comprising a portion of at least one hydrocarbon refinery gas, and a paraffin-rich feed comprising at least one paraffin selected from propane and butane or a mixture of both.
  • the invention also provides a hydrocarbon composition suitable for steam cracking, comprising a part of a paraffinic naphtha, modified by the addition of the combination of a first component, comprising one part of gasoline, and a second component, comprising a portion of at least one hydrocarbon refinery gas, and a paraffin-rich filler comprising at least one paraffin selected from propane and butane or a mixture of both.
  • the invention further provides a method for controlling a steam cracker, which process comprises supplying a steam cracker and a hydrocarbon feedstock comprising a part of a paraffinic naphtha, modified by the addition of the combination of a first component, comprising a portion of gasoline, and a second component, comprising a portion of at least one hydrocarbon refinery gas and a paraffin-rich feedstock comprising at least one paraffin selected from propane and butane or a mixture of both, and continuously controlling feed intakes. paraffinic naphtha, the second component and gasoline in the feed to give the effluent a desired target composition.
  • the invention also provides a process for treating a sulfur-containing gasoline charge, which process comprises the steps of: combining a sulfur-containing gasoline charge with a naphtha charge to provide a composite charge; passing the composite feed through a steam cracker, in the presence of steam, to produce an effluent, the effluent containing at least light olefins, the light olefins comprising at least one of C2 to C4 olefins, and C5 + hydrocarbons; and separating from the effluent a first fraction that is substantially free of sulfur and includes light olefins, and a second fraction that contains sulfur and includes C5 + hydrocarbons.
  • the invention is based on the surprising discovery by the Applicant that by selecting certain quantities and qualities of these gasolines and gaseous hydrocarbons and by using them as fillers in combination with naphtha, it is possible to steam crack the composite charge to thereby produce a composition for the cracked product (referred to in the "product palette" technique) that strongly resembles a pallet of products resulting from steam cracking, under similar conditions, of a paraffinic naphtha feedstock only.
  • the composition of the effluent produced according to the invention is within a range of ⁇ 20% by weight and preferably, ⁇ 10% by weight, for each component, relative to that of the effluent, when it is an unmodified paraffinic naphtha.
  • a part of the paraffinic naphtha feed is, according to the invention, replaced by a combination of a gasoline feedstock and a hydrocarbon refinery gas feedstock and / or feedstock. butane or propane or a mixture of both.
  • a process for the steam cracking of naphtha uses a filler of a hydrocarbon composition, which comprises a portion of a paraffinic naphtha, modified by a portion of a gasoline in combination with a portion of a gas hydrocarbon refinery and / or a portion of butane or propane or a mixture of both
  • the paraffinic naphtha for use in the process of the invention comprises from 10 to 60% by weight of n-paraffins, from 10 to 60% by weight of isoparaffins, from 0 to 35% by weight of naphthenes, from 0 to 1% by weight. % by weight of olefins and from 0 to 20% by weight of aromatics.
  • a typical paraffinic naphtha for use in the process of the invention comprises about 31% by weight of n-paraffins, 35% by weight of isoparaffins (giving a total paraffinic content of 66% by weight), 26% by weight of naphthenes. 0% by weight of olefins (typically 0.05% by weight of olefins) and 8% by weight of aromatics.
  • this starting paraffinic naphtha feed is modified by adding thereto a gasoline and a hydrocarbon refinery gas and / or butane or propane or a mixture of the two.
  • the gasoline is preferably a fraction from a fluidized-bed catalytic cracking (FCC) unit of an oil refinery (herein referred to as FCC gasoline), which advantageously has not has not been subjected to a hydrogenation treatment (referred to in the art as "hydrorefining"), which increases the paraffin content of gasoline by hydrogenating the unsaturated functions (such as those present in olefins and diolefins) of gasoline
  • FCC gasoline fluidized-bed catalytic cracking unit of an oil refinery
  • hydroorefining referred to in the art as "hydrorefining”
  • the advantage of using a non-hydrorefined FCC gasoline is that by avoiding a hydrogenation process, production costs are reduced by eliminating or reducing the use of hydrogen and avoiding the need for a hydrogenation process. additional hydrorefining capacity.
  • FCC gasoline is a slice or slice of the FCC unit typically having a distillation range of from 30 to 160 ° C, preferably a slice of cup or mixture of slices within the range of between 30 and 65 ° C, 65 to 105 ° C and 105 to 145 ° C.
  • the choice of the particular FCC gasoline or blend of it to be used may be determined based on the requirements at any time for the various cuts produced by the refinery. For example, some gasoline cuts have an octane deficit and could be better valued in a steam cracker than having to increase the octane number in the refinery.
  • the FCC gasoline to be used may have a sulfur content that would be too high for gasolines to be used in the automotive sector and that would require a desulphurization treatment with hydrogen, which is expensive because it consumes more fuel. hydrogen and requires the corresponding capacity on a desulfurization unit.
  • non-hydrorefined FCC gasoline it is preferred to use a non-hydrorefined FCC gasoline, because in the refinery, where there is a need for hydrorefined gasoline for other uses, this can cause bottlenecks in processing by the unit of hydroprocessing.
  • this can freeze appliances and appliances. hydrorefining units, thereby improving the flow management in the refinery, and also by reducing the need for hydrogen.
  • the non-hydrorefined FCC gasoline comprises from 0 to 30% by weight of n-paraffins, from 10 to 60% by weight of isoparaffins, from 0 to 80% by weight of naphthenes, from 5 to 80% by weight olefins and from 0 to 60% by weight of aromatics. More typically, the non-hydrorefined FCC gasoline comprises approximately 3.2% by weight of n-paraffins, 19.2% by weight of isoparaffins (giving a total paraffin content of 22.4% by weight), 18% by weight of naphthenes, 30% by weight of olefins and 29.7% by weight of aromatics.
  • this gas hydrocarbon is rich in C 2 and C 3 hydrocarbons, in particular paraffins (ethane and propane) and olefins (ethylene and propylene).
  • the refinery gas has the following compositional ranges: 0 to 5% by weight hydrogen, 0 to 40% by weight methane, 0 to 50% by weight ethylene, 0 to 80% by weight d ethane, 0 to 50% by weight of propylene, 0 to 80% by weight of propane and 0 to 30% by weight of butane.
  • a typical composition of a refinery gas of this type is approximately 1% by weight of hydrogen, 2% by weight of nitrogen, 0.5% by weight of carbon monoxide, 0% by weight of carbon dioxide. carbon, 10% by weight of methane, 15% by weight of ethylene, 32% by weight of ethane, 13% by weight of propylene, 14% by weight of propane, 2% by weight of isobutane, 4% by weight of weight of n-butane, 3% by weight of butene, 2% by weight of n-pentane, and 1.5% by weight of n-hexane.
  • this butane and / or propane or the mixture of both which is added to the paraffinic naphtha, in combination with the FCC gasoline and optionally the refinery gas, to produce a composite filler for steam cracking
  • this butane and / or this propane or the mixture of two may contain compounds olefins such as butenes and / or propylene, or saturated compounds such as butanes (normal and / or iso) and / or propane.
  • butane and / or propane or the mixture of both contain more than 50% by weight of saturated compounds to maximize the production of light olefins such as ethylene and propylene.
  • Butane and propane are preferably n-butane and n-propane.
  • the composite filler comprises from 5 to 95% by weight of naphtha, from 5 to 95% by weight of a mixture of refinery gas, butane or propane or a mixture of both, and gasoline.
  • the mixture of refinery gas, butane or propane or a mixture of both, and gasoline which is added to the naphtha comprises up to 60% by weight of refinery gas and / or butane or propane gas or a mixture of both, and at least 40% by weight of gasoline, more typically up to 50% by weight of refinery gas and / or butane or propane gas or a mixture of both, and up to 50% by weight of gasoline.
  • the composite naphtha comprises 80% by weight of naphtha, 7% by weight of refinery gas and / or butane or propane or a mixture of both, and 13% by weight of non-hydrorefined FCC gasoline. .
  • the composite filler of naphtha, gasoline, refinery gas and / or butane or propane or a mixture of both. is typically subjected to steam cracking under conditions similar to those known in the art, namely a temperature of between 780 and 880 ° C, preferably between 800 and 850 ° C.
  • the amount of steam may also fall within ranges known in the art, typically between 25 and 60% by weight based on the weight of the hydrocarbon feed.
  • the steam cracking unit for use in the method of the invention is schematically represented.
  • the steam cracking unit comprises a heating assembly consisting of ovens 4, which is provided with coils 6 having a first inlet 8 for the hydrocarbon feed to be cracked and a second inlet 10 for the steam.
  • An outlet pipe 12 of the set of Heating is connected to a primary fractionation column 14.
  • the primary fractionation column 14 comprises overhead gasoline reflux 15 and outlets for the various fractionated products, including an upper outlet 16 for light hydrocarbons and a lower outlet 18 for heavy hydrocarbons, which can be returned to 19 after cooling in line 12 to control the temperature or withdrawn at 17 in the form of heavy products called pyrolysis oil.
  • the entire composite feedstock of naphtha, refinery gas, and / or butane or propane or a mixture of both and gasoline may be fed from the common hydrocarbon inlet or alternatively, the four components of naphtha, FCC gasoline, refinery gas and / or butane or propane or a mixture of the two can be cracked separately in specific tubular coils.
  • the naphtha and the FCC gasoline, on the one hand, butane and / or propane or a mixture of both, and the refinery gas, on the other hand, are cracked separately.
  • naphtha and FCC gasoline are typically cracked at temperatures that are close to each other, typically in the range of 750 to 850 ° C, while butane, propane, refineries that contain ethane and propane must be cracked at higher temperatures, typically in the range of 800 to 900 ° C.
  • the two effluents can be combined at the outlet of the heating assembly before the primary fractionation column.
  • the process of the invention can operate continuously and has the advantage of eliminating excess gasoline from the refinery, and also reducing the need in the refinery for a desulphurization process.
  • Gasoline contains sulfur and, as a result of the steam cracking process, in which gasoline provides some of the composite filler, the most valuable light olefins in the effluent are sulfur free, while the sulfur remains concentrated in the game C5 + of the effluent stream. Therefore, the use of gasoline as part of a feed to be cracked to produce lighter olefins results in partial desulphurization of the gasoline portion of the feed because the sulfur is concentrated in the carbon number fraction. higher and commercially less attractive effluent, namely the C5 + current.
  • the invention provides a process for treating a sulfurized gasoline feedstock, the process comprising the steps of: combining a sulfur gasoline feedstock with a naphtha feedstock to provide a composite feedstock; passing the composite feed through a steam cracker, in the presence of steam, to produce an effluent, the effluent containing at least light olefins, the light olefins comprising at least one of C2 to C4 olefins, and C5 + hydrocarbons; and separating from the effluent a first fraction that is substantially free of sulfur and includes light olefins, and a second fraction that contains sulfur and includes C5 + hydrocarbons.
  • the sulfur is redistributed in the higher carbon number fraction, producing a lower sulfur-free olefinic fraction, which is an effective way of partially desulfurizing the gasoline charge.
  • the process has the advantage that the steam cracking process at least partially dehydrogenates the ethane present in the refinery gases, the dehydrogenation being carried out at a sufficiently high temperature to efficiently produce ethylene.
  • the invention also has the advantage that by adding to the naphtha feed, which contains no or only a small amount of olefins, a non-hydrorefined gasoline which contains a relatively high amount of olefins, typically from 5 to 80% by weight of olefins, the composite feedstock for steam cracking has a higher overall olefin content, compared with the single naphtha, and this translates into a lower energy expenditure for the production of light oliimes (that is, that is, ethylene and propylene) from this feed, as compared with the steam cracking of paraffins or paraffinic feedstocks to such light olefins.
  • light oliimes that is, that is, ethylene and propylene
  • software using linear or non-linear programming, is used continuously to control steam cracking conditions, in particular to control parts of paraffinic naphtha, refinery gas, butane and / or or propane or a mixture of both and the FCC gasoline in the feed, so that stirring presents the desired target composition.
  • the target composition may have substantially the same effluent composition for the important constituents, i.e., ⁇ 20% by weight, preferably ⁇ 10% by weight, relative to that of the unmodified filler.
  • the software can also control the shipment of refinery gas and / or control the quantities of FCC and / or butane or propane gasoline or the mixture of both, taken from the refinery, for example by shipping excess quantities to the refinery. storage tanks.
  • a composite feed comprising 80% by weight of naphtha and 20% of a mixture of refinery gas and non-hydrorefined FCC gasoline, in a weight ratio of one-third gas and two-thirds gasoline. , was subjected to steam cracking.
  • composition of the effluent of the composite filler of Example 1 is similar ( ⁇ 10% by weight for each constituent) to that of the only naphtha, but a part of the naphtha has been replaced by the addition of the gas of FCC refinery and gasoline for the reasons and with the benefits outlined above. It can be seen that high yields of ethylene and propylene are obtained according to the process of the invention, similar to those obtainable simply by steam-cracking of paraffinic naphtha.
  • Table 2 also shows, in contrast, the effluent compositions obtained by steam cracking of the single refinery gas and, separately, of the single FCC gasoline. It can be seen that the steam cracking of the non-hydrorefined FCC gasoline produces a low yield of ethylene and propylene and that the steam cracking of the refinery gas produces a high ethylene yield, but a low propylene yield. However, when the three feeds of naphtha, refinery gas, and non-hydrorefined FCC gasoline are combined, the composition of the effluent is very similar to that of a normal naphtha.
  • a composite filler comprising 60% by weight of naphtha and 40% by weight of a mixture of butane and non-hydrorefined FCC gasoline, in a ratio by weight of half gas and half gasoline, has was subjected to steam cracking.
  • the naphtha has the same starting composition as in the previous example.
  • butane is pure normal butane, such that it can be produced at the outlet of an alkylation unit in a refinery.
  • the non-hydrorefined FCC gasoline has the same starting composition as in the previous example.
  • composition of the effluent of the composite filler of Example 2 is similar ( ⁇ 10% by weight for each constituent) to that of the only naphtha, but part of the naphtha was replaced by the addition of butane and FCC gasoline for the reasons and with the benefits outlined above. It can be seen that high yields of ethylene and propylene are obtained according to the process of the invention, similar to those obtainable simply by steam-cracking of paraffinic naphtha.
  • Table 4 also shows, in contrast, the compositions of the effluents obtained by steam cracking of butane alone and, separately, of the sole essence of FCC. It can be seen that the steam cracking of non-hydrorefined FCC gasoline produces a low yield of ethylene and propylene and that steam cracking of butane produces high yields of ethylene, propylene and C4 and low yields of heavy products. However, when the three feeds of naphtha, butane and non-hydrorefined FCC gasoline are combined, the composition of the effluent is very similar to that of a normal naphtha.

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  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Liquid Carbonaceous Fuels (AREA)

Claims (20)

  1. Verfahren zum Steamcracken von Naphtha, wobei dieses Verfahren dadurch gekennzeichnet ist, dass es den Durchlauf, durch einen Steamcracker in Gegenwart von Wasserdampf, einer Kohlenwasserstoffbeladung umfasst, die 5 bis 95 Gewichts-% eines paraffinischen Naphthas und 95 - 5 Gewichts-% einer Mischung eines ersten Bestandteils, nämlich einem aus einer Einheit einer katalytischen Fluidbettcrackung (FCC) stammenden Benzin, und eines zweiten Bestandteils, der mindestens ein Kohlenwasserstoffraffineriegas und mindestens eine an Paraffinen reiche Beladung aufweist, umfasst, wobei das paraffinische Naphtha 10 bis 60 Gewichts-% n-Paraffine, 10 bis 60 Gewichts-% Isoparaffine, 0 bis 35 Gewichts-% Naphthene, 0 bis 1 Gewichts-% Olefine und 0 bis 20 Gewichts-% Aromaten umfasst, das FCC-Benzin ein nicht-hydriertes Benzin ist, das 0 bis 30 Gewichts-% n-Paraffine, 10 bis 60 Gewichts-% Isoparaffine, 0 bis 80 Gewichts-% Naphthene, 5 bis 80 Gewichts-% Olefine und 0 bis 60 Gewichts-% Aromaten umfasst, das Raffineriegas 0 bis 5 Gewichts-% Wasserstoff, 0 bis 40 Gewichts-% Methan, 0 bis 50 Gewichts-% Ethylen, 0 bis 80 Gewichts-% Ethan, 0 bis 50 Gewichts-% Propylen, 0 bis 80 Gewichts-% Propan und 0 bis 30 Gewichts-% Butane umfasst, und die an Paraffinen reiche Beladung mindestens 50 Gewichts-% gesättigte Kohlenwasserstoffe enthält, wobei die besagte Beladung mindestens Propan oder Butan umfasst.
  2. Verfahren gemäß Anspruch 1, bei dem die Mischung der ersten und zweiten Bestandteile bis 60 Gewichts-% des zweiten Bestandteils und mindestens 40 Gewichts-% Benzin umfasst.
  3. Verfahren gemäß Anspruch 2, bei dem die Mischung der ersten und zweiten Bestandteile bis 50 Gewichts-% des zweiten Bestandteils und mindestens 50 Gewichts-% Benzin umfasst.
  4. Verfahren gemäß Anspruch 2 oder 3, bei dem die Mischung der ersten und zweiten Bestandteile ungefähr ein Drittel Gew.-% des zweiten Bestandteils und ungefähr zwei Drittel Gew.-% Benzin umfasst.
  5. Verfahren gemäß irgendeinem der vorangehenden Ansprüche, bei dem die Beladung ungefähr 80 Gewichts-% Naphtha, ungefähr 7 Gewichts-% des zweiten Bestandteils und ungefähr 13 Gewichts-% Benzin umfasst.
  6. Verfahren gemäß einem der vorangehenden Ansprüche, bei dem das FCC-Benzin ein Verschnitt oder eine Mischung von Verschnitten einer FCC-Einheit darstellt, einen Destillationsbereich zwischen einschließlich 30 bis 160°C zeigend.
  7. Verfahren gemäß irgendeinem der Ansprüche 1 bis 6, bei dem der zweite Bestandteil aus mindestens Propan und Butan besteht.
  8. Verfahren gemäß irgendeinem der Ansprüche 1 bis 7, bei dem die sich aus Naphtha, Benzin und dem zweiten Bestandteil zusammensetzende Beladung einem Steamcracken unter Bedingungen unterzogen wird, die eine Temperatur von 780 bis 880°C einschließen.
  9. Verfahren gemäß irgendeinem der Ansprüche 1 bis 8, bei dem die Menge an Dampf 25 bis 60 Gewichts-%, gerechnet auf das Gewicht der Kohlenwasserstoffbeladung, beträgt.
  10. Kohlenwasserstoffzusammensetzung, die auf ein Steamcrackverfahren angepasst ist, wobei die Zusammensetzung 5 bis 95 Gewichts-% paraffinisches Naphtha und 95 bis 5 Gewichts-% einer Mischung eines ersten Bestandteils, nämlich einem aus einer Einheit einer katalytischen Fluidbettcrackung (FCC) stammenden Benzin, und eines zweiten Bestandteils, der mindestens ein Kohlenwasserstoffraffineriegas und mindestens eine an Paraffinen reiche Beladung aufweist, umfasst, wobei das paraffinische Naphtha 10 bis 60 Gewichts-% n-Paraffine, 10 bis 60 Gewichts-% Isoparaffine, 0 bis 35 Gewichts-% Naphthene, 0 bis 1 Gewichts-% Olefine und 0 bis 20 Gewichts-% Aromaten umfasst, das FCC-Benzin ein nicht-hydriertes Benzin ist, das 0 bis 30 Gewichts-% n-Paraffine, 10 bis 60 Gewichts-% Isoparaffine, 0 bis 80 Gewichts-% Naphthene, 5 bis 80 Gewichts-% Olefine und 0 bis 60 Gewichts-% Aromaten umfasst, das Raffineriegas 0 bis 5 Gewichts-% Wasserstoff, 0 bis 40 Gewichts-% Methan, 0 bis 50 Gewichts-% Ethylen, 0 bis 80 Gewichts-% Ethan, 0 bis 50 Gewichts-% Propylen, 0 bis 80 Gewichts-% Propan und 0 bis 30 Gewichts-% Butane umfasst, und die an Paraffinen reiche Beladung mindestens 50 Gewichts-% gesättigte Kohlenwasserstoffe enthält, wobei die besagte Beladung mindestens Propan oder Butan umfasst.
  11. Kohlenwasserstoffzusammensetzung gemäß Anspruch 10, bei der die Mischung der ersten und zweiten Bestandteile von Naphtha bis 60% des zweiten Bestandteils und mindestens 40 Gewichts-% Benzin umfasst.
  12. Kohlenwasserstoffzusammensetzung gemäß Anspruch 11, bei der die Mischung der ersten und zweiten Bestandteile bis 50% des zweiten Bestandteils und mindestens 50 Gewichts-% Benzin umfasst.
  13. Kohlenwasserstoffzusammensetzung gemäß Anspruch 11 oder 12, bei der die Mischung der ersten und zweiten Bestandteile ungefähr ein Drittel Gewichts-% des zweiten Bestandteils und ungefähr zwei Drittel Gewichts-% Benzin umfasst.
  14. Kohlenwasserstoffzusammensetzung gemäß Anspruch 13, bei der die Beladung ungefähr 80 Gewicht-% Naphtha, ungefähr 7 Gewichts-% des zweiten Bestandteils und ungefähr 13 Gewichts-% Benzin umfasst.
  15. Kohlenwasserstoffzusammensetzung gemäß irgendeinem der Ansprüche 10 bis 14, bei der der zweite Bestandteil mindestens aus Propan und Butan besteht.
  16. Verfahren zum Steuern eines Steamcrackens, wobei das Verfahren umfasst:
    - Beschickung mit einem Dampf-Steamcracker und einer Kohlenwasserstoffbeladung, die 5 bis 95 Gewichts-% eines paraffinischen Naphthas und 95 bis 5 Gewichts-% einer Mischung eines ersten Bestandteils, nämlich einem aus einer Einheit einer katalytischen Fluidbettcrackung (FCC) stammenden Benzin, und eines zweiten Bestandteils, der mindestens ein Kohlenwasserstoffraffineriegas und mindestens eine an Paraffinen reiche Beladung aufweist, umfasst, wobei das paraffinische Naphtha 10 bis 60 Gewichts-% n-Paraffine, 10 bis 60 Gewichts-% Isoparaffine, 0 bis 35 Gewichts-% Naphthene, 0 bis 1 Gewichts-% Olefine und 0 bis 20 Gewichts-% Aromaten umfasst, das FCC-Benzin ein nicht-hydriertes Benzin ist, das 0 bis 30 Gewichts-% n-Paraffine, 10 bis 60 Gewichts-% Isoparaffine, 0 bis 80 Gewichts-% Naphthene, 5 bis 80 Gewichts-% Olefine und 0 bis 60 Gewichts-% Aromaten umfasst, das Raffineriegas 0 bis 5 Gewichts-% Wasserstoff, 0 bis 40 Gewichts-% Methan, 0 bis 50 Gewichts-% Ethylen, 0 bis 80 Gewichts-% Ethan, 0 bis 50 Gewichts-% Propylen, 0 bis 80 Gewichts-% Propan und 0 bis 30 Gewichts-% Butane umfasst, und die an Paraffinen reiche Beladung mindestens 50 Gewichts-% gesättigte Kohlenwasserstoffe enthält, wobei die besagte Beladung mindestens Propan oder Butan umfasst,
    - und die kontinuierliche Steuerung der Einbringung des paraffinischen Naphthas, des zweiten Bestandteils und des Benzins in die Beladung, um dem Abgang eine gewünschte Zielzusammensetzung zu geben.
  17. Verfahren gemäß Anspruch 16, bei dem die Zielzusammensetzung im Wesentlichen die gleiche ist, d.h. ± 20 Gewichts-% für einen beliebig gegebenen Abgangsbestandteil, wie diejenige des Abgangs, der mit nicht-modifiziertem, paraffinischem Naphtha erhalten wird.
  18. Verfahren gemäß Anspruch 16 oder 17, bei dem der zweite Bestandteil und das Benzin beide direkt durch eine Raffinerie geliefert werden, und ferner umfassend die Fackelsteuerung der Liefermenge von überschüssigem zweiten Bestandteil und/oder die Steuerung der Menge an Benzin in der Raffinerie.
  19. Verfahren gemäß irgendeinem der Ansprüche 16 bis 18, bei dem die Beschickung der Bestandteile der Beladung in den Steamcracker über ein Programm geregelt wird.
  20. Verwendung des Verfahrens gemäß einem der Ansprüche 1 bis 16 zur Behandlung von schwefelhaltigem Benzin, dadurch gekennzeichnet, dass
    - das schwefelhaltige Benzin ein Benzin darstellt, das aus einer Einheit einer katalytischen Fluidbettcrackung stammt,
    - und der Abgang des Steamcrackers, der mindestens leichte Olefine, die mindestens ein C2- bis C4-Olefin umfassen, und Kohlenwasserstoffe mit C5+ enthält, getrennt wird in eine erste Fraktion, die praktisch schwefelfrei ist und die leichten Olefine umfasst, sowie eine zweite Fraktion, die Schwefel enthält und die Kohlenwasserstoffe mit C5+ umfasst.
EP03712222A 2002-01-10 2003-01-09 Wasserdampfcracken eines fcc-benzins Expired - Lifetime EP1463789B9 (de)

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FR0200244A FR2834515B1 (fr) 2002-01-10 2002-01-10 Vapocraquage de naphta modifie
FR0200244 2002-01-10
PCT/FR2003/000047 WO2003057802A2 (fr) 2002-01-10 2003-01-09 Vapocraquage de naphta modifie

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Families Citing this family (27)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US8775138B2 (en) * 2008-11-21 2014-07-08 Exxonmobil Chemical Patents Inc. Methods for handling withdrawal of streams from a linear programming model developed from a thermodynamically-based reference tool
CN101734990B (zh) * 2008-11-25 2013-09-04 中国石油天然气股份有限公司 一种管式裂解炉蒸汽裂解制乙烯的方法
EP2290045A1 (de) * 2009-07-27 2011-03-02 Total Petrochemicals Research Feluy Verfahren zur Herstellung von biologischem Rohbenzin aus komplexen Gemischen natürlich vorkommender Fette und Öle
AU2010313862B2 (en) * 2009-10-27 2014-10-23 Ignite Resources Pty Ltd Methods for producing hydrocarbon products from bio-oils and/or coal -oils
RU2627663C2 (ru) * 2012-08-09 2017-08-09 Линде Актиенгезелльшафт Способ получения олефинов путем термического парового крекинга
US9505677B2 (en) 2012-10-29 2016-11-29 China Petroleum & Chemical Corporation Steam cracking processes
ES2604654T3 (es) * 2012-11-08 2017-03-08 Linde Ag Procedimiento para la obtención de productos que contienen olefinas mediante disociación de vapor térmica
US20140275669A1 (en) * 2013-03-15 2014-09-18 Exxonmobil Research And Engineering Company Production of lubricant base oils from dilute ethylene feeds
US10041673B2 (en) 2013-07-25 2018-08-07 Honeywell International Inc. Flare stack monitoring
CN107056568A (zh) * 2017-05-10 2017-08-18 中石化上海工程有限公司 Mto工艺与石脑油及丙烷裂解前脱丙烷工艺耦合的方法
FI128839B (en) * 2018-04-10 2021-01-15 Neste Oyj Method for preparing a hydrocarbon mixture
FI128378B (en) * 2019-04-03 2020-04-15 Neste Oyj Process and input material for the production of hydrocarbons
WO2020242916A1 (en) * 2019-05-24 2020-12-03 Eastman Chemical Company Cracking a c4-c7 fraction of pyoil
EP3976732A4 (de) 2019-05-24 2023-05-17 Eastman Chemical Company Mischung von kleinen mengen von pyrolyseöl zu einem flüssigkeitsstrom, der zu einen gas-cracker verarbeitet wird
US20220186124A1 (en) * 2019-05-24 2022-06-16 Eastman Chemical Company Co-cracking pyoil with ethane
US20220281793A1 (en) * 2019-07-29 2022-09-08 Eastman Chemical Company Recycle content (c4)alkanal
US11319262B2 (en) 2019-10-31 2022-05-03 Eastman Chemical Company Processes and systems for making recycle content hydrocarbons
US11945998B2 (en) 2019-10-31 2024-04-02 Eastman Chemical Company Processes and systems for making recycle content hydrocarbons
US20220403254A1 (en) * 2019-10-31 2022-12-22 Eastman Chemical Company Processes and systems for formation of recycle-content hydrocarbon compositions
KR20220091563A (ko) * 2019-10-31 2022-06-30 이스트만 케미칼 컴파니 재활용물 탄화수소 조성물의 생성을 위한 방법 및 시스템
CN114650981A (zh) 2019-11-07 2022-06-21 伊士曼化工公司 回收成分α烯烃和脂肪醇
US11021422B1 (en) * 2019-12-04 2021-06-01 Saudi Arabian Oil Company Integrated processes to produce gasoline blending components from light naphtha
MX2022007131A (es) * 2019-12-23 2022-09-19 Chevron Usa Inc Economia circular para residuos plasticos en polipropileno a traves de unidad de craqueo catalitico de fluidos (fcc) de refineria.
CN114867825A (zh) * 2020-03-30 2022-08-05 雪佛龙美国公司 通过炼油厂fcc单元或fcc/烷基化单元将塑料废物转化为聚乙烯的循环经济
US11566182B2 (en) 2020-03-30 2023-01-31 Chevron U.S.A. Inc. Circular economy for plastic waste to polyethylene via refinery FCC feed pretreater and FCC units
US11306253B2 (en) 2020-03-30 2022-04-19 Chevron U.S.A. Inc. Circular economy for plastic waste to polyethylene via refinery FCC or FCC/alkylation units
CN114106867B (zh) * 2021-10-27 2023-05-23 中国石油化工股份有限公司 一种降低碳五馏分中硫含量的方法

Family Cites Families (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3511771A (en) * 1967-07-24 1970-05-12 Exxon Research Engineering Co Integrated hydrofining,hydrodesulfurization and steam cracking process
US3786110A (en) * 1972-05-19 1974-01-15 Marathon Oil Co Asphaltenes for inhibiting polymerization of pyrolysis products
US4257105A (en) * 1979-05-02 1981-03-17 Phillips Petroleum Company Control of a cracking furnace
ES2018664B3 (es) * 1986-06-25 1991-05-01 Naphtachimie Sa Procedimiento y horno de vapocraqueado de hidrocarburos destinados a la fabricación de olefinas y de diolefinas.
DE3708332A1 (de) * 1987-03-14 1988-09-22 Erdoelchemie Gmbh Verfahren zur thermischen umwandlung von ethylen
US4956509A (en) * 1989-10-16 1990-09-11 Mobil Oil Corp. Integrated paraffin upgrading and catalytic cracking processes
US5481052A (en) * 1992-04-22 1996-01-02 Bp Chemicals Limited Polymer cracking
CN1026594C (zh) * 1993-01-28 1994-11-16 化学工业部北京化工研究院 石油烃蒸汽裂解方法的改进
US5582714A (en) * 1995-03-20 1996-12-10 Uop Process for the removal of sulfur from petroleum fractions
FR2753717B1 (fr) 1996-09-24 1998-10-30 Procede et installation pour la production d'essences de craquage catalytique a faible teneur en soufre

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CN1615353A (zh) 2005-05-11
EP1463789B1 (de) 2006-06-14
KR101062768B1 (ko) 2011-09-06
DE60306105D1 (de) 2006-07-27
FR2834515A1 (fr) 2003-07-11
DE60306105T2 (de) 2007-01-04
CN1306011C (zh) 2007-03-21
WO2003057802A2 (fr) 2003-07-17
CA2471491A1 (fr) 2003-07-17
DK1463789T3 (da) 2006-10-16
EP1463789A2 (de) 2004-10-06
AU2003216795A1 (en) 2003-07-24
PT1463789E (pt) 2006-10-31
ES2266792T3 (es) 2007-03-01
US20060089518A1 (en) 2006-04-27
CA2471491C (fr) 2011-03-15
US7838712B2 (en) 2010-11-23

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