EP0022883B1 - Katalytisches Krack- und Hydroraffinierverfahren zur Herstellung von Benzin aus schwefelhaltiger Beschickung - Google Patents

Katalytisches Krack- und Hydroraffinierverfahren zur Herstellung von Benzin aus schwefelhaltiger Beschickung Download PDF

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EP0022883B1
EP0022883B1 EP19790301428 EP79301428A EP0022883B1 EP 0022883 B1 EP0022883 B1 EP 0022883B1 EP 19790301428 EP19790301428 EP 19790301428 EP 79301428 A EP79301428 A EP 79301428A EP 0022883 B1 EP0022883 B1 EP 0022883B1
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product
fraction
range
cracked naphtha
cat
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EP0022883A1 (de
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William Edward Winter
William Lee Schuette
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ExxonMobil Technology and Engineering Co
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Exxon Research and Engineering Co
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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
    • C10G51/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more cracking processes only
    • C10G51/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more cracking processes only plural serial stages only
    • C10G51/026—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more cracking processes only plural serial stages only only catalytic cracking steps
    • 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
    • C10G2400/02—Gasoline

Definitions

  • the present invention relates to a catalytic cracking and hydrotreating process for gasoline production from sulfur-containing hydrocarbon feedstocks.
  • the catalyst in such unit, is regenerated in a separate vessel, i.e., a regenerator, by burning off the coke to restore its activity.
  • a regenerator i.e., a regenerator
  • the catalyst is continuously cycled between the reactor and regenerator as a moving bed without shutdown of either unit.
  • the economics of the catalytic cracking unit in a refinery determines the product slate which will be produced by a refinery.
  • Products from the catalytic cracking unit thus provide feed for other units, e.g., alkylation and polymerization units.
  • Cat cycle stocks are used to make lubes, and gas is employed as fuel in the refinery.
  • a major portion of the product of the catalytic cracking units of a given refinery are blended directly in gasoline blending pools which serve as supplies of motor gasoline.
  • Cat cracking feed stocks are provided by atmospheric and vacuum stills, phenol extraction plants and hydrotreaters.
  • the usual feed to a commercial catalytic cracking unit is comprised of a gas oil boiling below about 565.6°C (565.6°C-) (1050°F (1050°F-)), typically a virgin gas oil boiling between about 315.6°C (600°F) and 565.6°C (1050°F).
  • thermally cracked materials are often used as cat cracking feeds.
  • the activity and activity-maintenance of the catalysts are suppressed due to the presence of sulfur.
  • the catalytic converters emit sulfate, either as a sulfuric acid aerosol or as particulates caused by sulfuric acid corrosion of the metal portions of the exhaust train.
  • the sulfur in gasoline which is typically present in amounts of about 300 ppm, is oxidized in the combustion chamber of the engine to sulfur dioxide.
  • the catalytic converter which is required for lowering the emissions of CO and HC, is thus responsible for the oxidation of sulfur dioxide in the exhaust gas to produce sulfur trioxide which immediately hydrates due to the presence of water vapor, one of the combustion products, to form a sulfuric acid aerosol or acid particulates, neither of which is environmentally acceptable.
  • US-A-3950242 describes and claims a method for producing a gasoline boiling range product which comprises cracking a petroleum fraction boiling from about 400°F (204.4°C) to 1100°F (593.3°C) in the presence of a crystalline zeolite cracking catalyst under conditions of temperature, pressure, space velocity and catalyst to oil ratio providing a conversion level of at least 45 vol.% of said fraction to produce a material having a 90% ASTM boiling point of 400°F (204.4°C) and comprising not more than 15 wt.% olefins in the depentanised gasoline product thereof, and contacting the depentanised gasoline of restricted olefin content with a ZSM-5 type crystalline zeolite conversion catalyst at a temperature within the range of 500 to 800°F (260.0 to 426.7°C) to produce a higher octane product.
  • the present invention provides a process for the production of high octane gasoline comprising the following steps in combination:
  • the present invention provides a process having as an essential feature the step of recracking a cracked naphtha feed containing up to 60 percent, suitably from 20 to 40 percent olefins over a crystalline alumino-silicate zeolite catalyst to further crack the naphtha and saturate at least 50 percent of the olefins, preferably from 80 percent to 100 percent of the olefins, based on the weight of said cracked naphtha feed.
  • the cracked naphtha feed is contacted and reacted over the catalyst, without dilution of said feed, at a temperature ranging from 426.7 to 593.3°C (800°F to 1100°F), preferably from 482.2 to 554.4°C (900°F to 1030°F), and at a gauge pressure ranging from 0 to 344.75 kPa (0 to 50 pounds per square inch gauge (psig)), preferably from 43.475 to 137.9 kPa (5 psig to 20 psig). Reaction at such conditions not only produces significant saturation of the olefins, but also significant hydrodenitrogenation and hydrodesulfurization of said cat naphtha feed.
  • the process is one wherein a conventional sulfur-bearing cat cracker feed, suitably a gas oil, is catalytically cracked, at conventional conditions, in an initial or first stage to provide a cat naphtha product containing generally from 10 to 60 percent, preferably from 20 to 40 percent olefins.
  • the cat naphtha product in whole or in part is then recracked, as an undiluted feed, in a subsequent or second catalytic cracking zone over a crystalline aluminosilicate zeolite catalyst.
  • the cat naphtha product of the initial or first stage is split into fractions inclusive of a low octane, highly olefinic intermediate fraction having a low end boiling point ranging from 48.9 to 121.1 °C (120°F to 250°F), preferably from 82.2 to 104.4°C (180°F to about 220°F), and a high end boiling point ranging from 121.1 to 193.3°C (250°F to about 380°F), preferably from 132.2°C to 176.7°C (270°F to 350°F).
  • a low octane, highly olefinic intermediate fraction having a low end boiling point ranging from 48.9 to 121.1 °C (120°F to 250°F), preferably from 82.2 to 104.4°C (180°F to about 220°F), and a high end boiling point ranging from 121.1 to 193.3°C (250°F to about 380°F), preferably from 132.2°C to 176.7°C (270°F to 350°F).
  • a higher boiling fraction having a low end boiling point range from 121.1 to 193.3°C (250°F to 380°F), preferably from 132.2 to 176.7°C (270°F to 350°F), and a higher end boiling point range from 176.7°C to 232.2°C (350°F to 450°F), preferably from 204.4 to 221.1 °C (400°F to 430°F) can also be obtained.
  • the intermediate or higher boiling fraction, or a composition which includes both, may be utilized as feed and further catalytically cracked, or recracked, in a subsequent stage over a crystalline aluminosilicate zeolite catalyst sufficient to produce significant saturation of the olefins, and hydrodenitrogenation and hydrodesulfurization of said cat cracked naphtha fraction, or fractions.
  • the recracked product is then hydrotreated, or hydrofined, at mild hydrotreating conditions to provide a low sulfur gasoline of improved octane.
  • the higher boiling fraction or fraction typically having a low end boiling point ranging from 121.1 to 193.3°C (250°F to 380°F) and a high end boiling point ranging from 176.7 to 232.2°C (350°F to 450°F) is not recracked because it is generally of relatively high octane and upgrading of this fraction is not required.
  • the intermediate fraction per se preferably, is utilized as a feed and further catalytically cracked, or recracked, in a subsequent stage over a crystalline aluminosilicate zeolite catalyst sufficient to produce significant saturation of the olefins, and hydrodenitrogenation and hydrodesulfurization of said cat cracked naphtha fraction.
  • the recracked product thereof is then hydrotreated, or hydrofined, at mild hydrotreating conditions, and then reformed over a conventional catalyst at conventional reforming (hydroforming) conditions to provide a low olefin gasoline of improved octane.
  • recracking of the cracked naphtha in this manner prior to hydrotreatment of the cracked naphtha to eliminate olefins minimizes mercaptan reversion reactions wherein olefins normally react with by-product hydrogen sulfide to form mercaptans, any significant amount of which simply cannot be tolerated in a reformer feed.
  • Suitable cracking catalysts can be used in cracking the gas oil feed, or feed to the first stage catalytic cracker.
  • Suitable cracking catalysts include conventional silica-based materials. Exemplary of such catalysts are, e.g. amorphous silica-alumina; silica-magnesia; silica-zirconia; conventional clay cracking catalysts, and the like.
  • the amorphous gel silica-metal oxide cracking catalyst may further be composited with kaolin in amounts of 10 to 40 wt.% (based on total weight of the composited catalyst) and up to 20 wt.% or more crystalline alumino-silicate zeolite, such as faujasite.
  • a crystalline alumino- silicate zeolite catalyst is required in the second stage catalytic cracker, i.e., for cracking the cat cracked naphtha, or fraction thereof, from the first stage.
  • These catalysts are well known and commercially available.
  • the catalyst utilized, particularly in the second stage catalytic cracker is an amorphous silica-alumina catalyst containing from 5 to 16 weight percent v-type faujasite, and, optionally 15 to 40 percent kaolin.
  • the first and second stage catalytic crackers are operated at about the same absolute conditions of temperature, pressure, space velocity, and catalyst/oil ratio, the runs being initiated by adjusting the feed and catalyst rates, and the temperature and pressure of the reactor to operating conditions.
  • the catalytic cracking operation in both stages of cracking is continued at conditions by adjustment of the major process variables, within the ranges described below:
  • the product of the first stage catalytic cracker is characterized as a cracked naphtha having an olefin content ranging from 10 percent to 60 percent, more typically from 20 percent to 40 percent (by weight) and boiling within the gasoline range, typically from 18.3 °C (65°F) to 221.1 °C (430°F) (i.e., Cs to 221.1 °C, C 5/ 430°F).
  • All or a portion of the cat cracked naphtha, preferably an intermediate or heavy fraction, or composition which includes both fractions, as previously defined, is split from the product of said first stage, fed into, and recracked, without dilution, over the crystalline aluminosilicate zeolite catalyst in the second stage catalytic cracker.
  • the recracked product is then subjected to a mild hydrotreatment by contact, with a catalyst comprising a composite of an inorganic oxide base, suitably alumina, and a Group VI-B or Group VIII metal, or both, e.g., a cobalt molybdenum ("moly”)/alumina catalyst, at conditions given as follows, to provide a gasoline suitable for addition to a gasoline blending pool, to wit:
  • the recracked product is subjected to the following mild hydrotreating conditions so as to provide a naphtha suitable as a feed to a reforming process:
  • the product from the hydrofiner is subjected to reforming, at reforming conditions, by contact with a sulfur-sensitive, noble metal reforming catalyst to produce a satisfactory high octane gasoline.
  • the reforming run is initiated by injection of hydrogen into the reforming reactor (or zone) with the feed at the desired .hydrogen and feed rates, with adjustment of the temperature and pressure to operating conditions.
  • the run is continued at optimum reforming conditions by adjustment of the major process variables, within the ranges described below:
  • the catalyst employed in reforming is one comprising a refractory or inorganic oxide support material, particularly alumina, which is composited with a Group VIII noble metal hydrogenation- dehydrogenation component, notably platinum, to which may be added an additional metal, or metals, to promote the activity and selectivity of the catalysts, particularly iridium or rhenium, or both, or component selected from the Group IV metals, Group VI metals, Group VII metals, and Group VIII metals, e.g., germanium, tin, lead, osmium, ruthenium, rhodium or the like.
  • a halogen component suitably chlorine, is generally added to provide the desired acidity.
  • These components can be added to a support by any of the conventional methods, e.g., by impregnation prior to, following or simultaneously with the impregnation of the noble metal, or halogen components.
  • the metal hydrogenation-dehydragenation components, or promoters are added to a support in concentration ranging about 0.01 to 3 percent, preferably from about 0.05 to about 1 percent, based on the weight of the catalyst.
  • a suitable support can contain, e.g., one or more of alumina, bentonite, clay, diatomaceous earth, zeolite, silica, activated carbon, magnesia, zirconia, thoria, and the like; though the most preferred support is alumina to which, if desired, can be added a suitable amount of other refractory carrier materials such as silica, zirconia, magnesia, titania, etc., usually in a range of about 1 to 20 percent, based on the weight of the support.
  • a preferred support is one having a surface area of more than 50 m 2 /g, preferably from 100 to 300 m 2 /g, a bulk density of 0.3 to 1.0 g/ml, preferably 0.4 to 0.8 g/ml, an average pore volume of 0.2 to 1.1 ml/g, preferably 0.3 to 0.8 ml/g, and an average pore diameter of 30 to 300A (3 to 30 nm).
  • Feedstock A a cat cracked naphtha, hereinafter referred to as Feedstock A, the complete feedstock inspections of which are given in Table I, below.
  • Feedstock A was hydrofined in a reactor at 287.8°C (550°F), 2758 kPa gauge (400 psig), and 142.5 litres H 2 /litre feedstock (800 SCF/B) over a cobalt moly-on-alumina catalyst to produce a low sulfur gasoline blending component having a Bromine number of about 5 and 20 wppm sulfur, this requiring about 96.5% hydrodesulfurization.
  • the product has a research octane number (RONC) at 77.3 and a motor octane number (MONC) of 73.0, this representing a loss of 5.5 RONC and a 2.2 loss of MONC as a result of the hydrofining.
  • Feedstock A was recracked in a reactor at 498.9°C (930°F), 101.36 kPa absolute (14.7 psia), 13.7 WHSV and at a catalyst/oil ratio of 9.2 over a conventional commercial zeolite cracking catalyst containing crystalline aluminosilicate zeolite, silica alumina gel and clays, and the product then fractionated to provide a light ends cut, and three fractions, i.e., a low boiling 18.3/93.3°C (65/200°F) fraction, an intermediate 93.3/221.1 °C (200/430°F) fraction and a high boiling 221.1 °C+ (430°F+) fraction, the low boiling and intermediate boiling fractions being characterized in Table II.
  • the 93.3/221.1 °C (200/430°F) fraction is then hydrofined at 287.8°C (550°F), 2758 kPa gauge (400 psig), 142.5 litres H/litre naphtha fraction (800 SCF/Bbl) over a cobalt moly-on-alumina catalyst as in Example 1 to produce a low sulfur gasoline blending component having Bromine No. of about 1 and containing 11 wppm sulfur, this requiring about 95.5% hydrodesulfurization.
  • the resulting product has octane ratings of 89.4 RONC and 80.9 MONC.
  • the loss in octane rating for this low sulfur gasoline blending component is nil as relates to the motor octane number rating, and only 1 octane number as relates to research octane number.
  • the resultant product has an octane number of 88.7 RONC and 80.6 MONC, contains only 20 wppm of sulfur, and represents 80.8 vol. percent recovered product, based on the original feed.
  • Octane loss as a result of hydrofining is estimated at about 0.5 RONC, or less.
  • Feedstock A was split into three fractions, a 18.3/93.3°C (65/200°F) fraction, a 93.3/165.6°C (200/330°F) fraction, and a 165.6°C+ (330°F+) fraction as defined in Table III.
  • the 18.3/93.3°C (65/200°F) fraction is then treated in a Merox * process, after admixture with light ends from the 93.3/165.6°C (200/330°F) fraction which is recracked as defined hereafter, to produce a product of 87.5 RONC and 79.2 MONC with 50 ppm sulfur.
  • the 93.3/165.6°C (200/330°F) fraction is recracked in a reactor at 498.9°C (930°F), 101.36 kPa absolute (14.7 psia), 13.7 WHSV at a catalyst/oil ratio of 9.2 over a conventional commercial zeolite, silica-alumina gel and clays, and the product then fractionated to provide a 18.3/93.3°C (65/200°F) fraction which is blended with the 18.3/93.3°C (65/200°F) fraction to Merox, a 93.3/221.1°C (200/430°F) fraction, and a 221.1°C+ (430°F+) fraction.
  • the 18.3/93.3°C (65/200°F) and 93.3/221.1 °C (200/430°F) fractions are characterized in Table IV.
  • the 165.6°C+ (330°F+) fraction characterized in Table III, is combined with the 93.3/221.1 °C (200/430°F) and 221.1 °C+ (430°F+) recracked fractions, then hydrofined over a cobalt moly-on-alumina catalyst at 287.8°C (550°F), 2758 kPa gauge (400 psig) and 142.5 litres H2/litre naphtha fractions (800 SCR/B).
  • the feed entering the hydrofiner (H/F Feed), the product therefrom (H/F Product), and the final product formed by combining the hydrofined product and product from Merox * is characterized in Table V.
  • Feedstock A was recracked in a reactor at 498.9°C (930°F), 101.36 kPa absolute (14.7 psia), 13.7 WHSV and at a catalyst/oil ratio of 9.2 over a conventional commercial zeolite cracking catalyst containing crystalline aluminosilicate zeolite, silicate alumina gel and clays, and the product then fractionated to provide three fractions, i.e., a low boiling 18.3/93.3°C (65/200°F) fraction, an intermediate 93.3/176.7°C (200/350°F) fraction and a high boiling 176.7/221.1°C (350/430°F) fraction, as characterized in Table VI.
  • the 93.3/176.7°C (200/350°F) fraction is then hydrofined over a cobalt moly-on-alumina catalyst at conditions just sufficient to produce a suitable reforming feed, this requiring 98.9% hydrodesulfurization, 50% hydrodenitrogenation, and 70% saturation of the olefins to provide a product of 89 RONC with less than 1 ppm sulfur, less than 1 ppm nitrogen and a bromine number of less than 1.
  • a hydrogen consumption of 3.562 litres H/litre feed (20 SCF/Bbl) is required.
  • the hydrofined fraction is then reformed over an iridium-promoted platinum catalyst at 498.9°C (930°F), 1.0 W/Hr/W, 1379 kPa gauge (200 psig) at a hydrogen to oil ratio of 855 litres/litre (4800 SCF/Bbl) to produce 100 RONC gasoline.
  • the recracking of Feedstock A is thus shown to drastically reduce the amount of hydrotreating required to produce a reformer feed, and it achieves this at far less severity and with far less consumption of hydrogen. Moreover, assuming first order desulfurization kinetics, 20% less reactor volume is required to achieve 98.8% hydrodesulfurization for the intermediate fraction of recracked Feedstock A than is required to produce 99.6% hydrodesulfurization for the intermediate fraction of raw Feedstock A. It also reduces reforming severity, or the severity required to produce 100 RONC gasoline.
  • the 93.3/176.7°C (200/350°F) fraction is then hydrofined over a cobalt moly-on-alumina catalyst at conditions just sufficient to produce a suitable reforming feed, this requiring 98.8% hydrodesulfurization, 67% hydrodenitrogenation, and 63% saturation of the olefins to provide a product of 89.6 RONC with less than 1 ppm sulfur, less than 1 ppm nitrogen and a bromine number of less than one.
  • a hydrogen consumption of 3.562 to 5.343 litres H 2 /litre oil (20 to 30 SCF/Bbl) is required.
  • the hydrofined fraction is then reformed over an iridium promoted platinum catalyst at 498.9°C (930°F), 1.0 W/Hr/W, 1379 kPa (gauge (200 psig) at a hydrogen to oil ratio of 855 litres H 2 /litre oil (4800 SCB/Bbl) to produce 100 RONC gasoline.
  • the preferred embodiment as represented by Example 5, also provides higher selectivity for other relatively high value products vis-a-vis the embodiment of Example 4; or, conversely, lower selectivity for products of lesser value vis-a-vis the embodiment of Example 4.
  • Table IX presents comparative data illustrative of the product of such relatively low value by-products as coke, light gases, inclusive of hydrogen and C 1 and C 2 hydrocarbons, and 221.1°C+ (430°F+) hydrocarbons, in the preceding runs wherein, as in Example 4, the whole of Feedstock A is recracked, and in Example 5 an intermediate boiling feedstock is recracked.
  • the Table also presents the yields of C 3 and C 4 hydrocarbons which were obtained, these products being nearly as valuable as gasoline.
  • the first column of Table IX identifies the by-product, the second column gives the percent yield of the by-product, based on the amount of recracked feed which was treated, and the third column gives the percent yield, based on the amount of original Feedstock A.
  • Temperatures expressed in °F are converted to °C by subtracting 32 and dividing by 1.8.
  • SCF Standard Cubic Feet
  • Liquid Volumes in Barrels (B or Bbl) are converted to litres by multiplying by 159.0.
  • Mass in pounds (lbs) is converted to kilograms by dividing by 2.20462.

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  • Engineering & Computer Science (AREA)
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Claims (13)

1. Verfahren zur Herstellung von Benzin mit hoher Oktanzahl, bei dem
(a) ein Kohlenwasserstoffeinsatzprodukt in einer ersten Crackzone über einem ersten Crackkatalysator gecrackt wird, um ein katalytisch gecracktes Nphthaprodukt zu erhalten,
(b) das katalytisch gecrackte Naphthaprodukt aus der ersten Crackzone abgezogen wird und
(c) das katalytisch gecrackte Naphthaprodukt oder eine oder mehrere Fraktionen desselben ohne Verdünnung mit anderen Kohlenwasserstoffen über einem kirstallinen Aluminiumsilikatzeolithkatalysator in einer zweiten Crackzone erneut gecrackt wird, um mindestens einen Teil des Olefingehaltes desselben abzusättigen, dadurch gekennzeichnet, daß das Kohlenwasserstoffeinsatzprodukt ein schwefelhaltiges Kohlenwasserstoffeinsatzprodukt ist, das katalytische Cracken in Stufe (a) zu einem katalytisch gecrackten Naphthaprodukt mit einem Olefingehalt im Bereich von 10 bis 60%, bezogen auf das Gewicht des Naphthaproduktes, führt, in Stufe (c) das Naphthaprodukt oder mindestens eine Fraktion desselben entschwefelt wird und mindestens 50% der Olefine, bezogen auf das Gewicht des katalytisch gecrackten Naphthaprodukts oder der Fraktion desselben, gesättigt werden und in der zusätzlichen Stufe (d) mindestens eine Fraktion des erneut gecrackten Produkts aus Stufe (c) einer Wasserstoffbehandlung unterworfen oder hydrofiniert wird, um ein Benzin oder eine Mischungskomponente für Benzin mit oher Oktanzahl und geringem Schwefelgehalt zu erzeugen.
2. Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß mindestens eine der Fraktionen des katalytisch gecrackten Naphthaprodukts eine Zwischenfraktion mit einem unteren Siedepunkt im Bereich von 48,9 bis 121°C und einem oberen Siedepunkt im Bereich von 121,1 °C bis 193,3°C enthält.
3. Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß mindestens eine der Fraktionen des katalytisch gecrackten Naphthaprodukts eine Fraktion mit einem unteren Siedepunkt im Bereich von 82,2°C bis 104,4°C und einem oberen Siedepunkt im Bereich von 204,4°C bis 221,1°C enthält.
4. Verfahren nach Anspruch 2, dadurch gekennzeichnet, daß mindestens eine andere Fraktion des katalytisch gecrackten Naphthaprodukts einen unteren Siedepunkt im Bereich von 121,1 °C bis 193,3°C und einen oberen Siedepunkt im Bereich von 176,7°C bis 232,2°C besitzt.
5. Verfahren nach Anspruch 2, dadurch gekennzeichnet, daß eine Fraktion des katalytisch gecrackten Naphthaprodukts mit einem unteren Siedepunkt im Bereich von 121,1 °C bis 193,3°C und einem oberen Siedepunkt im Bereich von 176,7°C bis 232,2°C in Stufe (c) nicht erneut gecrackt wird.
6. Verfahren nach jedem der Ansprüche 2 bis 5, dadurch gekennzeichnet, daß das in Stufe (d) erhaltene Produkt reformiert wird.
7. Verfahren nach jedem der Ansprüche 1 bis 6, dadurch gekennzeichnet, daß der Olefingehalt des gecrackten Naphthaprodukts im Bereich von 20 bis 40 Gew. %, bezogen auf das Gewicht des Naphthaprodukts, liegt.
8. Verfahren nach jedem der Ansprüche 1 bis 7, dadurch gekennzeichnet, daß die Bedingungen der Wasserstoffbehandlung oder des Hydrofinierens in Stufe (d) innerhalb der folgenden Bereiche ausgewählt sind, so daß ein für die Zugabe zu einem Benzinmischpool geeignetes Produkt resultiert:
Figure imgb0017
9. Verfahren nach jedem der Ansprüche 1 bis 7, dadurch gekennzeichnet, daß die Bedingungen der Wasserstoffbehandlung oder des Hydrofinierens in Stufe (d) in den folgenden Bereichen gewählt sind, so daß ein zum Reformieren über einem schwefelempfindlichen Edelmetallreformierkatalysator geeignetes Produkt resultiert:
Figure imgb0018
10. Verfahren nach jedem der Ansprüche 1 bis 9, dadurch gekennzeichnet, daß das in die erste Crackzone eingeleitete schwefelhaltige Kohlenwasserstoffeinsatzprodukt ein Gasöl ist, das unter 565,5°C siedet.
11. Verfahren nach jedem der Ansprüche 1 bis 10, dadurch gekennzeichnet, daß 80 bis 100% der Olefine im katalytisch gecrackten Naphthaeinsatzprodukt, das in die zweite Crackzone eingeleitet wird, in der zweiten Crackzone gesättigt werden.
12. Verfahren nach jedem der Ansprüche 1 bis 11, dadurch gekennzeichnet, daß das in die zweite Crackzone eingeleitete katalytisch gecrackte Naphthaeinsatzprodukt bei einer Temperatur im Bereich von 426 bis 593°C und einem Überdruck im Bereich von 0 bis 344,75 kPa umgesetzt wird.
13. Verfahren nach jedem der Ansprüche 1 bis 12, dadurch gekennzeichnet, daß das in die zweite Crackzone eingeleitete katalytisch gecrackte Naphthaeinsatzprodukt bei einer Temperatur im Bereich von 482,2 bis 554,4°C umgesetzt wird.
EP19790301428 1979-07-18 1979-07-18 Katalytisches Krack- und Hydroraffinierverfahren zur Herstellung von Benzin aus schwefelhaltiger Beschickung Expired EP0022883B1 (de)

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EP19790301428 EP0022883B1 (de) 1979-07-18 1979-07-18 Katalytisches Krack- und Hydroraffinierverfahren zur Herstellung von Benzin aus schwefelhaltiger Beschickung
DE7979301428T DE2966422D1 (en) 1979-07-18 1979-07-18 Catalytic cracking and hydrotreating process for producing gasoline from hydrocarbon feedstocks containing sulfur

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
EP19790301428 EP0022883B1 (de) 1979-07-18 1979-07-18 Katalytisches Krack- und Hydroraffinierverfahren zur Herstellung von Benzin aus schwefelhaltiger Beschickung

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EP0022883A1 EP0022883A1 (de) 1981-01-28
EP0022883B1 true EP0022883B1 (de) 1983-11-23

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EP19790301428 Expired EP0022883B1 (de) 1979-07-18 1979-07-18 Katalytisches Krack- und Hydroraffinierverfahren zur Herstellung von Benzin aus schwefelhaltiger Beschickung

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EP (1) EP0022883B1 (de)
DE (1) DE2966422D1 (de)

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US6803494B1 (en) 1998-05-05 2004-10-12 Exxonmobil Chemical Patents Inc. Process for selectively producing propylene in a fluid catalytic cracking process

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DE69223809T2 (de) * 1991-08-15 1998-04-23 Mobil Oil Corp Verfahren zur verbesserung der qualität von kohlenwasserstoffen
US5773676A (en) * 1996-08-06 1998-06-30 Phillips Petroleum Company Process for producing olefins and aromatics from non-aromatics
US6602403B1 (en) 1998-05-05 2003-08-05 Exxonmobil Chemical Patents Inc. Process for selectively producing high octane naphtha
US6455750B1 (en) 1998-05-05 2002-09-24 Exxonmobil Chemical Patents Inc. Process for selectively producing light olefins
US6315890B1 (en) * 1998-05-05 2001-11-13 Exxonmobil Chemical Patents Inc. Naphtha cracking and hydroprocessing process for low emissions, high octane fuels
AU1374201A (en) * 1999-11-04 2001-05-14 Concordia University Method and apparatus for selective deep catalytic cracking of hydrocarbons
US7135602B1 (en) 1999-11-04 2006-11-14 Valorbec Societe En Commandite Method and apparatus for selective deep catalytic cracking of hydrocarbons
CN100425675C (zh) * 2005-08-09 2008-10-15 中国石油化工股份有限公司 一种生产催化重整原料的加氢方法

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GB682309A (en) * 1948-01-10 1952-11-05 Anglo Iranian Oil Co Ltd Improvements relating to the catalytic desulphurisation of petroleum hydrocarbons
US2981674A (en) * 1955-10-24 1961-04-25 Shell Oil Co Production of gasoline by thermal cracking, catalytic cracking and reforming
US3784463A (en) * 1970-10-02 1974-01-08 Texaco Inc Catalytic cracking of naphtha and gas oil
US3761391A (en) * 1971-07-26 1973-09-25 Universal Oil Prod Co Process for the production of gasoline and low molecular weight hydrocarbons
US3950242A (en) * 1974-04-02 1976-04-13 Mobil Oil Corporation Fluid catalytic cracking plus selective upgrading of cracked gasoline
US3891540A (en) * 1974-04-02 1975-06-24 Mobil Oil Corp Combination operation to maximize fuel oil product of low pour
US4090949A (en) * 1974-07-31 1978-05-23 Mobil Oil Corportion Upgrading of olefinic gasoline with hydrogen contributors
US3997427A (en) * 1975-12-24 1976-12-14 Exxon Research And Engineering Company Reducing hydrogen consumption in hydrotreating petroleum fractions

Cited By (1)

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Publication number Priority date Publication date Assignee Title
US6803494B1 (en) 1998-05-05 2004-10-12 Exxonmobil Chemical Patents Inc. Process for selectively producing propylene in a fluid catalytic cracking process

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EP0022883A1 (de) 1981-01-28
DE2966422D1 (en) 1983-12-29

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