EP1689837A1 - Methode pour valoriser des charges de craquage catalytique a l'aide d'un traitement presentant une solution d'acide sulfurique - Google Patents

Methode pour valoriser des charges de craquage catalytique a l'aide d'un traitement presentant une solution d'acide sulfurique

Info

Publication number
EP1689837A1
EP1689837A1 EP04812579A EP04812579A EP1689837A1 EP 1689837 A1 EP1689837 A1 EP 1689837A1 EP 04812579 A EP04812579 A EP 04812579A EP 04812579 A EP04812579 A EP 04812579A EP 1689837 A1 EP1689837 A1 EP 1689837A1
Authority
EP
European Patent Office
Prior art keywords
sulfuric acid
catalytic cracking
boiling range
acid solution
nitrogen
Prior art date
Legal status (The legal status 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 status listed.)
Withdrawn
Application number
EP04812579A
Other languages
German (de)
English (en)
Inventor
Mark A. Greaney
John N. Begasse
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
ExxonMobil Technology and Engineering Co
Original Assignee
ExxonMobil Research and Engineering Co
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 ExxonMobil Research and Engineering Co filed Critical ExxonMobil Research and Engineering Co
Publication of EP1689837A1 publication Critical patent/EP1689837A1/fr
Withdrawn legal-status Critical Current

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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
    • C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
    • C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
    • C10G67/14—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only including at least two different refining steps in the absence of hydrogen
    • 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
    • C10G17/00—Refining of hydrocarbon oils in the absence of hydrogen, with acids, acid-forming compounds or acid-containing liquids, e.g. acid sludge
    • C10G17/02—Refining of hydrocarbon oils in the absence of hydrogen, with acids, acid-forming compounds or acid-containing liquids, e.g. acid sludge with acids or acid-containing liquids, e.g. acid sludge
    • C10G17/04—Liquid-liquid treatment forming two immiscible phases
    • C10G17/06—Liquid-liquid treatment forming two immiscible phases using acids derived from sulfur or acid sludge thereof
    • 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
    • C10G21/00—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
    • C10G21/06—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents characterised by the solvent used
    • C10G21/08—Inorganic compounds only
    • 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
    • C10G47/00—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions
    • 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
    • C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
    • C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
    • C10G67/08—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only including acid treatment as the refining step in the absence of hydrogen

Definitions

  • the instant invention relates to an improved catalytic cracking method for hydrocarbon streams. More particularly, the present invention relates to the use of an acid treatment method to remove heterocyclic nitrogen- containing compounds from a feedstream and then subjecting the feedstream having a reduced amount of nitrogen-containing compounds to catalytic cracking.
  • the instant invention is directed at an improved catalytic cracking method involving removing nitrogen from a nitrogen-containing catalytic cracking boiling range feedstream.
  • the method comprises: a) providing a sulfuric acid solution containing greater than about 75 wt.% sulfuric acid; b) contacting a nitrogen-containing catalytic cracking boiling range feedstream with the sulfuric acid solution in a first reaction stage under effective conditions and at an acid solution volumetric treat rate greater than about 0.5 vol.%, based on the catalytic cracking boiling range feedstream, wherein greater than about 60 wt.% of the nitrogen compounds contained in said catalytic cracking boiling range feedstream is removed thereby producing a first reaction stage effluent comprising at least a catalytic cracking boiling range effluent and a used sulfuric acid solution; and c) conducting at least a portion of said first reaction stage effluent to a second reaction stage wherein said first reaction stage effluent is contacted under effective cracking conditions with a cracking catalyst.
  • the sulfuric acid solution is a spent sulfuric acid solution obtained from an alkylation process unit wherein the spent sulfuric acid solution is produced by: a) combining an olefmic hydrocarbon feedstream containing C olefms with isobutane to form a hydrocarbonaceous mixture; and a) contacting the hydrocarbonaceous mixture with sulfuric acid under conditions effective for producing at least an alkylate and a sulfuric acid solution having an acid concentration of at least about 75 wt.%.
  • cat cracker and “catalytic cracking” are used interchangeably herein. These terms are meant to encompass all catalytic cracking operations such as, for example, fluidized catalytic cracking, steam cracking, hydrocracking, etc.
  • the instant invention is an improved catalytic cracking method involving removing nitrogen compounds from nitrogen-containing catalytic cracking boiling range feedstreams.
  • the present method involves contacting a catalytic cracking boiling range feedstream in a first reaction stage with a sulfuric acid solution to reduce the nitrogen content of the catalytic cracking boiling range feedstream by at least about 60 wt.%.
  • the contacting of the catalytic cracking boiling range feedstream with the sulfuric acid solution produces a first reaction stage effluent comprising at least a catalytic cracking boiling range effluent and a used sulfuric acid solution.
  • At least a portion of the first reaction stage effluent is then conducted to a second reaction stage wherein the first reaction stage effluent is contacted under effective conditions with a cracking catalyst.
  • Feedstreams suitable for treatment with the present nitrogen reduction method include any conventional catalytic cracking operation feedstreams.
  • feedstreams typically include heavy hydrocarbonaceous feeds boiling in the range of about 430°F to about 1050°F (220-565°C), such as gas oils, heavy hydrocarbon oils comprising materials boiling above 1050°F (565°C); heavy and reduced petroleum crude oil; petroleum atmospheric distillation bottoms; petroleum vacuum distillation bottoms; pitch, asphalt, bitumen, other heavy hydrocarbon residues; tar sand oils; shale oil; liquid products derived from coal liquefaction processes; and mixtures thereof.
  • the cat cracker feedstream may also comprise recycled hydrocarbons, such as light or heavy cycle oils.
  • Preferred feeds for use in the presently disclosed method are vacuum gas oils boiling in the range above about 650°F (343°C).
  • the catalytic cracking boiling range feedstreams suitable for treatment with the present method also contain heterocyclic nitrogen- containing compounds.
  • the nitrogen content of such streams is about 10,000-100 wppm preferably about 5000-200 wppm, and more preferably about 3000-500 wppm.
  • the nitrogen compounds appears as both basic and non-basic nitrogen species.
  • basic nitrogen species include quinolines and substituted qumolines, benzo quinolines such as acridine, anilines, N-alkyl indoles, alkylarylamines and substituted derivatives thereof.
  • non-basic nitrogen species include indoles, carbazoles, benzocarbazoles, amides such as quinolone and substituted derivatives thereof.
  • Catalytic cracking boiling range feedstreams suitable for treatment with the present method also contain metals such as nickel, vanadium, copper, iron, and sodium.
  • the total metals concentration in the cat cracker boiling range feedstreams is typically from about 10 to about 1000 wppm, preferably about 50 to about 500 wppm, more preferably from about 100 wppm to about 300 wppm.
  • the above-defined catalytic cracking boiling range feedstreams are intimately contacted with a sulfuric acid solution in a first reaction stage to remove at least 60 wt.% of the nitrogen species, both basic and non-basic, thus producing a first reaction stage effluent comprising at least a catalytic cracking boiling range effluent and a used sulfuric acid solution.
  • Sulfuric acid solutions suitable for use herein contain at least about 75 wt.% sulfuric acid, based on the sulfuric acid solution, preferably greater than about 80 wt.%, more preferably greater than about 85 wt.%, most preferably from about 85 wt.% to about 93 wt.%.
  • the sulfuric acid solution may be obtained through any means known.
  • the sulfuric acid solution be a spent sulfuric acid solution obtained from an alkylation process unit and have a sulfuric acid concentration within the above-defined ranges.
  • a typical alkylation process involves combining an olefmic hydrocarbon feedstream containing C olefms with isobutane to produce a hydrocarbonaceous mixture. This hydrocarbonaceous mixture is subsequently contacted with sulfuric acid.
  • the sulfuric acid used for contacting the hydrocarbonaceous mixture is typically reagent grade sulfuric acid having an acid concentration of at least about 95 wt.%).
  • the sulfuric acid has a sulfuric acid concentration of greater than about 97 wt.%.
  • the hydrocarbonaceous mixture is contacted with the sulfuric acid under conditions effective at producing at least an alkylate and a sulfuric acid solution.
  • the sulfuric acid solution so produced comprises at least about 75 wt.%) sulfuric acid, about 0.5 to about 5 wt.% water, with the remaining balance being acid soluble hydrocarbons. It is more preferred that the effective conditions be selected such that the sulfuric acid solution so produced comprises between about 82 and 93 wt.% sulfuric acid, about 1 to about 4 wt.% water, with the remaining balance being acid soluble hydrocarbons. However, it is most preferred that the effective conditions be selected such that the sulfuric acid solution so produced comprises between about 85 and 93 wt.% sulfuric acid, about 1.5 to about 4 wt.% water, with the remaining balance being acid soluble hydrocarbons.
  • a suitable diluent preferably water
  • a sulfuric acid solution having the above-described concentration of sulfuric acid i.e. at least about 75 wt.% sulfuric acid, based on the sulfuric acid solution, preferably greater than about 75 wt.%, more preferably greater than about 85 wt.%, most preferably from about 85 wt.% to about 93 wt.%.
  • the sulfuric acid content and water content are measured by standard analytical techniques.
  • the catalytic cracking boiling range feedstream is contacted with the sulfuric acid solution under effective conditions and at an acid volumetric treat rate of greater than about 0.50 vol.%, based on the catalytic cracking boiling range feedstream, preferably about 0.5 to about 20 vol.%, more preferably about 0.5 to about 10 vol.%, and most preferably 0.50 to about 5 vol.%.
  • the contacting can be achieved by any suitable method including both dispersive and non-dispersive methods.
  • suitable dispersive methods include mixing valves, mixing tanks or vessels, propeller mixers, inline static mixers, and orifice plates.
  • Non-limiting examples of non-dispersive methods include packed beds of inert particles and fiber film contactors such as those sold by Merichem Company and described in United States Patent Number 3,758,404, which is hereby incorporated by reference, which involve contacting along a bundle of metallic fibers rather than a packed bed of inert particles.
  • the contacting methods are non-dispersive, and in another embodiment, the contacting methods are those that are classified as dispersive. [0016] As stated above, the contacting of the cat cracker boiling range feedstream with the sulfuric acid solution occurs under effective conditions.
  • effective conditions it is to be considered those conditions that allow the present method to achieve a reduction of nitrogen in the catalytic cracking boiling range feedstream of greater than about 60 wt.%, preferably greater than about 75 wt.% more preferably greater than about 90 wt.%.
  • Effective conditions are also to be considered those conditions that minimize yield losses during the sulfuric acid solution treatment to about to about 0.5 to about 30 wt.%, preferably about 0.5 to about 20 wt.% , more preferably about 0.5 to about 10 wt.%.
  • the contacting of the catalytic cracking boiling range feedstream with the sulfuric acid solution in the first reaction stage produces a first reaction stage effluent comprising at least a catalytic cracking boiling range effluent and a used sulfuric acid solution. At least a portion, preferably substantially all, of the first reaction stage effluent is thence conducted to a second reaction stage wherein it is contacted, under effective cracking conditions, with a cracking catalyst. However it is preferred to separate the first reaction stage effluent into at least a catalytic cracking boiling range effluent and a used sulfuric acid solution, which now contains the removed nitrogen species.
  • the used sulfuric acid solution and catalytic cracking boiling range effluent can be separated by any means known to be effective at separating an acid from a hydrocarbon stream.
  • suitable separation methods include gravity settling, electric field induced settling, centrifugation, microwave induced settling, and settling enhanced with coalescing surfaces.
  • the catalytic cracking boiling range effluent and the used sulfuric acid solution be separated, or allowed to separate, into layers in a separation device such as a settling tank or dram, coalescer, electrostatic precipitator, or other similar device.
  • a separation device such as a settling tank or dram, coalescer, electrostatic precipitator, or other similar device.
  • fiber-film contactors for separating the used sulfuric acid solution and the catalytic cracking boiling range effluent produced by the present method. At least a portion, preferably substantially all, of the catalytic cracking boiling range effluent can then be conducted to a suitable cracking operation.
  • the catalytic cracking boiling range effluent is typically greater than about 70 wt.% of the cat cracker feedstream, preferably greater than about 80 wt.%, more preferably greater than about 90 wt.%, with the remainder being contained in the used sulfuric acid solution separated from the catalytic cracking boiling range effluent.
  • the inventors hereof attribute the loss in yield to compounds such as coke precursors, 4-ring aromatics, and polar compounds. It should be noted that the amount of catalytic cracking boiling range effluent contained in the separated used sulfuric acid solution can also be recovered and combined with the catalytic cracking boiling range feedstream as a recycle stream, if desired.
  • the catalytic cracking boiling range effluent will typically contain less nitrogen, both basic and non-basic, than the initial catalytic cracking boiling range feedstream.
  • the nitrogen content of the catalytic cracking boiling range feedstream is reduced by greater than about 60 wt.%, preferably greater than about 75 wt.%, more preferably greater than about 90 wt.%.
  • catalytic cracking boiling range effluent will contain 60 wt.%, etc. less nitrogen that the catalytic cracking boiling range feedstream.
  • the catalytic cracking boiling range effluent will also typically have a lower total metals concentration, such as the sum of, for example, Ni, V, Fe, Cu, Na metals, than the initial catalytic cracking boiling range feedstream.
  • the total metals concentration in the catalytic cracking boiling range product typically ranges from about 20 wppm to about 1000 wppm, preferably from about 10 wppm to about 500 wppm, more preferably from about 5 wppm to about 30 wppm.
  • At least a portion of the first reaction stage effluent, or catalytic cracking boiling range effluent in preferred embodiments, is sent to a suitable catalytic cracking operation.
  • suitable catalytic cracking operations include fluidized catalytic cracking and hydrocracking.
  • any suitable cracking catalyst can be employed to obtain the desired product.
  • the conditions under which the first reaction stage effluent is contacted with the cracking catalyst are not critical to the instant invention and can be any conditions effective at producing the desired products, i.e. naphtha, diesel, etc.
  • the practitioner selects a cracking catalyst or catalysts, and then selects conditions that are effective for use with that particular catalyst or catalysts.
  • FCCU fluidized catalytic cracking
  • any FCCU catalyst can be used, and the FCCU reactor would be operated under effective conditions for that particular catalyst.
  • a suitable hydrocracking catalyst such as, for example a zeolite, can be selected and the hydrocracking reactor conditions such as, for example, hydrogen treat rate, liquid hourly space velocity, etc. would be selected from conditions known to be effective with that particular catalyst or catalysts.
  • the present nitrogen reduction method also benefit downstream catalytic processes such as desulfurization processes that are utilized on some products, such as naphtha and diesel boiling range products, that are produced by catalytic cracking operations.
  • the catalytic cracking boiling range effluent will also typically have a sulfur concentration lower than that of the nitrogen-containing catalytic cracking boiling range feedstream.
  • the contacting of the catalytic cracking boiling range feedstream with the sulfuric acid solution also reduces the sulfur content of the catalytic cracking boiling range effluent.
  • the catalytic cracking boiling range effluent will therefore have a sulfur content lower than the catalytic cracking boiling range feedstream.
  • the catalytic cracking boiling range effluent will have a sulfur content about 0.1 to about 25 % lower than the catalytic cracking boiling range feedstream, preferably about 0.1 to about 15% lower, more preferably about 0.1 to about 10% lower, and most preferably about preferably about 0.1 to about 5 % lower.
  • Example 2 The same virgin gas oil feedstream of Example 1 was treated according to the method outlined in Example 1 above.
  • the sulfuric acid solution mixed with the virgin gas oil was a spent sulfuric acid recovered from an alkylation process unit, referced to herein as acid solution #2.
  • the spent sulfuric acid had a composition of 90 wt.% sulfuric acid, 4 wt.%) water and 6 wt.% acid soluble hydrocarbon. This converts to an equivalent sulfuric acid strength as defined above of 96 wt.%.
  • the virgin gas oil feedstream was separately mixed with 1 ml (5 vol.% treat rate) and 20 ml (10 vol.%) treat rate) of sulfuric acid solution #1 and sulfuric acid solution #2, respectively. The results of this experiment are contained in Table 2 below, which compares the results of treatment with sulfuric acid solution #1 and #2.

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  • 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)
  • Inorganic Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

L'invention concerne l'utilisation d'une méthode de traitement à l'acide, pour supprimer des composés contenant de l'azote hétérocyclique d'une charge, et pour soumettre la charge présentant une quantité réduite de composés contenant de l'azote, à un craquage catalytique.
EP04812579A 2003-12-05 2004-12-01 Methode pour valoriser des charges de craquage catalytique a l'aide d'un traitement presentant une solution d'acide sulfurique Withdrawn EP1689837A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US52725603P 2003-12-05 2003-12-05
PCT/US2004/040092 WO2005056731A1 (fr) 2003-12-05 2004-12-01 Methode pour valoriser des charges de craquage catalytique a l'aide d'un traitement presentant une solution d'acide sulfurique

Publications (1)

Publication Number Publication Date
EP1689837A1 true EP1689837A1 (fr) 2006-08-16

Family

ID=34676723

Family Applications (1)

Application Number Title Priority Date Filing Date
EP04812579A Withdrawn EP1689837A1 (fr) 2003-12-05 2004-12-01 Methode pour valoriser des charges de craquage catalytique a l'aide d'un traitement presentant une solution d'acide sulfurique

Country Status (5)

Country Link
EP (1) EP1689837A1 (fr)
JP (1) JP2007513247A (fr)
AU (1) AU2004297562A1 (fr)
CA (1) CA2547193A1 (fr)
WO (1) WO2005056731A1 (fr)

Family Cites Families (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2800427A (en) * 1954-07-29 1957-07-23 Standard Oil Co Catalytic cracking of pretreated hydrocarbon oils
US2902430A (en) * 1955-02-21 1959-09-01 Exxon Research Engineering Co Removal of metal contaminants from catalytic cracking feed stocks with sulfuric acid
US3681233A (en) * 1967-03-11 1972-08-01 Sun Oil Co Making a cable oil by acid extraction and hydrofining
US3749666A (en) * 1970-10-30 1973-07-31 Cities Service Oil Co Method for the improvement of petroleum distillate
US3992156A (en) * 1975-07-23 1976-11-16 Merichem Company Mass transfer apparatus
GB2311789B (en) * 1996-04-01 1998-11-04 Fina Research Process for converting wax-containing hydrocarbon feedstocks into high-grade middle distillate products

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
See references of WO2005056731A1 *

Also Published As

Publication number Publication date
WO2005056731A1 (fr) 2005-06-23
JP2007513247A (ja) 2007-05-24
AU2004297562A1 (en) 2005-06-23
CA2547193A1 (fr) 2005-06-23

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