WO2011051434A2 - Procédé de craquage - Google Patents

Procédé de craquage Download PDF

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Publication number
WO2011051434A2
WO2011051434A2 PCT/EP2010/066450 EP2010066450W WO2011051434A2 WO 2011051434 A2 WO2011051434 A2 WO 2011051434A2 EP 2010066450 W EP2010066450 W EP 2010066450W WO 2011051434 A2 WO2011051434 A2 WO 2011051434A2
Authority
WO
WIPO (PCT)
Prior art keywords
product
separating
carbon atoms
fractions
gas
Prior art date
Application number
PCT/EP2010/066450
Other languages
English (en)
Other versions
WO2011051434A3 (fr
Inventor
John William Harris
Original Assignee
Shell Internationale Research Maatschappij B.V.
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Shell Internationale Research Maatschappij B.V. filed Critical Shell Internationale Research Maatschappij B.V.
Publication of WO2011051434A2 publication Critical patent/WO2011051434A2/fr
Publication of WO2011051434A3 publication Critical patent/WO2011051434A3/fr

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • 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

Definitions

  • the present invention relates to catalytic cracking of hydrocarbon feedstock.
  • Catalytic cracking processes are well known in the art. A more recent development is to further crack part of the product obtained thereby to obtain lower olefins besides the conventional cracking products. We now have found an improved process for separating the products obtained thereby into the different fractions.
  • the present invention relates to a process for converting a hydrocarbon feed which process comprises
  • step (b) separating the mixture obtained in step (a) into spent catalyst and hydrocarbon product
  • step (c) separating the hydrocarbon product of step (b) into two or more fractions
  • step (d) further catalytically cracking at least one of the fractions obtained in step (c) ,
  • step (e) separating the mixture obtained in step (d) into used catalyst and hydrocarbon product
  • step (h) separating hydrocarbons comprising 3 carbon atoms from the product of step (g) to obtain propane-lean product
  • step (i) separating the propane-lean product obtained in step (h) into a fraction containing hydrocarbons
  • hydrocarbons comprising 5 or 6 carbon atoms and a heavy fraction, in which process the fraction containing hydrocarbons comprising 5 or 6 carbon atoms obtained in step (i) is sent as feed to step (d) .
  • butane-lean means that the liquid in question contains a limited amount only of butane and butene
  • propane-lean means that the liquid in question contains a limited amounts only of propane and propene
  • the feed to be used in the present invention can be any feed conventionally used in fluid catalytic cracking.
  • the feed preferably boils in the gasoil boiling range or higher, more specifically in the range of from 210 to 750 °C, more preferably above the gas oil boiling range, more specifically of from 350 to 650 °C.
  • step (a) the feed is preferably contacted with cracking catalyst at a temperature of from 450 to 650 °C to yield a hydrocarbon product and spent catalyst.
  • This cracking step is preferably carried out in a riser reactor .
  • the mixture obtained is typically separated in a separator/stripper to separate the spent catalyst from the hydrocarbon product.
  • a separator/stripper to separate the spent catalyst from the hydrocarbon product.
  • steam is added to the mixture during separation.
  • step (a) preferably regenerated with an oxygen-containing gas to obtain regenerated catalyst, with at least part of the regenerated catalyst used again as cracking catalyst in step (a) .
  • the hydrocarbon product obtained in step (b) is separated into two or more fractions.
  • At least one of the fractions obtained in step (c) is cracked further in order to obtain lower olefins which are desirable starting compounds for many different products.
  • the fraction to be cracked further preferably comprises at least 70 %wt of hydrocarbons comprising of from 5 to 9 carbon atoms, more preferably at least
  • the lower olefins typically are hydrocarbons comprising of from 2 to 4 carbon atoms.
  • the fraction to be subjected to further cracking in step (d) preferably contains
  • Used catalyst is separated from the mixture obtained in step (d) to obtain hydrocarbon product.
  • the used catalyst contains a limited amount of coke and still has sufficiently high temperature which makes that it can be used as cracking catalyst in step (a) .
  • the hydrocarbon product separated off in step (e) is separated in combination with one or more fractions obtained in step (c) .
  • the separation is preferably carried out by fractional distillation.
  • the temperature at the bottom of the fractionator preferably is of from 210 to 280 °C, more specifically of from 230 to 270 °C, most specifically of from 240 to 260 °C.
  • the pressure applied generally will be of from 1 to 10 bar, more specifically of from 1 to 5 bar.
  • step (f) a gas as top fraction, a gas oil as middle fraction and a residue as bottom fraction.
  • a gas oil as middle fraction
  • a residue as bottom fraction.
  • only a limited amount of product is separated as gas oil specifically less than 8 %wt, based on amount of product separated, more
  • the efficient work-up section requires to increase the pressure of the gas separated off in step (f) . This is suitably done in a number of steps whereby the gas is partly converted into a liquid which can be introduced separately into the separation column of step (h) .
  • the pressure of the gas generally will be increased to of from 10 to 40 bar, more specifically to of from 15 to 30 bar.
  • step (h) preferably is carried out by divided wall fractional distillation, more
  • step (h) specifically divided wall fractional distillation which is carried out in a column containing a wall dividing the column in the longitudinal direction to form a first upper region, a second upper region and lower common region.
  • the dividing wall extends to the top of the column thereby preventing fluid communication between the first and second upper region in the upper part of the column.
  • each of the upper regions has their separate reflux, i.e. withdraw gas at the top and recycle part thereof as reflux to the upper region from which it was withdrawn.
  • (f) generally is of from 10 to 50 bar, more specifically of from 15 to 30 bar.
  • step (h) The propane-lean product obtained in step (h) is separated further in step (i) preferably by divided wall fractional distillation, more specifically divided wall fractional distillation which is carried out in a column containing a wall dividing the column in the longitudinal direction to form a first middle region and a second middle region.
  • the column for use in step (i) preferably comprises an upper common region and a lower common region.
  • the pressure in the separation column of step (i) generally is of from 1 to 20 bar, more specifically of from 5 to 20 bar.
  • the fractions separated in step (i) mainly contain hydrocarbons comprising the number of carbon atoms mentioned but further hydrocarbons can be present as well.
  • Each of the fractions preferably contains at least 80 %wt of hydrocarbons comprising the number of carbon atoms mentioned, more preferably at least 90 %wt .
  • fraction containing hydrocarbons comprising 5 or
  • 6 carbon atoms can be mixed with fresh feed or with a fraction obtained in step (c) before being cracked further in step (d) .
  • hydrocarbon feed is sent to the cracking process via line 1 and regenerated catalyst is added via line 2. Additionally, used catalyst can be added via line 32 if required.
  • the mixture of feed and catalyst flows upwardly through riser reactor 3. Via line 4, the mixture of spent catalyst and hydrocarbon product is sent to stripper/seperator 5.
  • Spent catalyst will generally be separated from hydrocarbon product with the help of a first cyclone 7, after which the gas separated off in the first cyclone 7 can be sent to a second cyclone 8. If desired, the gas separated off in the second cyclone 8 can be sent to a third means for separating solid partices. Catalyst particles which have been separated off, flow via a so-called dipleg to a regeneration zone.
  • the separated catalyst particles flow via line 10 to regenerator 11 where oxygen-containing gas is added via line 13 and waste gas is removed via line 12. Solids can be removed from the gas flowing upwards with the help of cyclone 14 which feeds into cyclone 15. Gas which is substantially free from solids can further flow upwards via line 16. Regenerated catalyst can be used again in riser reactor 3.
  • stripper/separator 5 is sent via line 6 to the main fractionator 17 where gas is removed via line 20, gas oil is removed via line 19 and the further compounds are removed via line 18.
  • the gas removed via line 20 has a pressure of from 1 to 4 bar, which pressure is increased in several steps to of from 20 to 25 bar.
  • pressurised gas is sent to divided wall column 21 which is operated at 20 bar.
  • Gas containing propane and/or propene is removed via line 22 and a propane-lean liquid is sent via line 23 to divided wall column 24 which is operated at a pressure of from 2 to 10 bar.
  • a fraction containing hydrocarbons comprising 5 or 6 carbon atoms is removed via line 27 and a heavy fraction is removed via line 26.
  • This heavy fraction is preferably hydrotreated and the hydrotreated product is separated further at atmospheric pressure in a divided wall column (not shown) .
  • Part or all of the fraction containing hydrocarbons comprising 5 or 6 carbon atoms is sent via line 27 to a further cracking reactor 30 together with regenerated catalyst supplied via line 27 and a fraction separated in the main fractionator 17 via line 28.
  • the product is sent via line 27 to a further cracking reactor 30 together with regenerated catalyst supplied via line 27 and a fraction separated in the main fractionator 17 via line 28.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

L'invention concerne un procédé de conversion de charge hydrocarbonée, consistant à (a) soumettre la charge à un craquage catalytique, (b) séparer le mélange obtenu à l'étape (a) en catalyseur usé et produit hydrocarboné, (c) séparer le produit hydrocarboné de l'étape (b) en deux fractions ou plus, (d) continuer à soumettre au moins l'une des fractions obtenues à l'étape (c) à un craquage catalytique, (e) séparer le mélange obtenu à l'étape (d) en catalyseur usé et produit hydrocarboné, (f) soumettre une ou plusieurs fractions obtenues à l'étape (c) et le produit hydrocarboné de l'étape (e) à une séparation de manière à obtenir un gaz et une ou plusieurs fractions liquides, (g) augmenter la pression du gaz obtenu à l'étape (f), (h) séparer les hydrocarbures comprenant trois atomes de carbone du produit de l'étape (g) pour obtenir un produit pauvre en propane, et (i) séparer le produit pauvre en propane obtenu à l'étape (h) en une fraction contenant des hydrocarbures comportant quatre atomes de carbone, une fraction contenant des hydrocarbures comprenant cinq ou six atomes de carbone, et une fraction lourde, dans ce procédé, la fraction contenant des hydrocarbures comprenant cinq ou six atomes de carbone obtenue à l'étape (i) est envoyée en tant que charge à l'étape (d).
PCT/EP2010/066450 2009-11-02 2010-10-29 Procédé de craquage WO2011051434A2 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
EP09174736 2009-11-02
EP09174736.0 2009-11-02

Publications (2)

Publication Number Publication Date
WO2011051434A2 true WO2011051434A2 (fr) 2011-05-05
WO2011051434A3 WO2011051434A3 (fr) 2011-07-14

Family

ID=42026548

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/EP2010/066450 WO2011051434A2 (fr) 2009-11-02 2010-10-29 Procédé de craquage

Country Status (1)

Country Link
WO (1) WO2011051434A2 (fr)

Family Cites Families (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4090949A (en) * 1974-07-31 1978-05-23 Mobil Oil Corportion Upgrading of olefinic gasoline with hydrogen contributors
US3974062A (en) * 1974-10-17 1976-08-10 Mobil Oil Corporation Conversion of full range crude oils with low molecular weight carbon-hydrogen fragment contributors over zeolite catalysts
US5087349A (en) * 1988-11-18 1992-02-11 Stone & Webster Engineering Corporation Process for selectively maximizing product production in fluidized catalytic cracking of hydrocarbons
DE69007649T2 (de) * 1989-02-06 1994-08-25 Stone & Webster Eng Corp Verfahren zur katalytischen Krackung von Kohlenwasserstoffen.
CN100448953C (zh) * 2000-02-16 2009-01-07 印度石油股份有限公司 由重烃原料以高产率生产中间馏分产品的多级选择性催化裂化方法和系统

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
None

Also Published As

Publication number Publication date
WO2011051434A3 (fr) 2011-07-14

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