EP1866389A1 - Improved short contact time pcc process - Google Patents
Improved short contact time pcc processInfo
- Publication number
- EP1866389A1 EP1866389A1 EP06737614A EP06737614A EP1866389A1 EP 1866389 A1 EP1866389 A1 EP 1866389A1 EP 06737614 A EP06737614 A EP 06737614A EP 06737614 A EP06737614 A EP 06737614A EP 1866389 A1 EP1866389 A1 EP 1866389A1
- Authority
- EP
- European Patent Office
- Prior art keywords
- catalyst
- aromatics
- stream containing
- contact time
- saturates
- 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- Withdrawn
Links
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
- C10G25/00—Refining of hydrocarbon oils in the absence of hydrogen, with solid sorbents
-
- 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
- C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
- C10G11/14—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts
- C10G11/18—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts according to the "fluidised-bed" technique
-
- 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
-
- 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
- C10G31/00—Refining of hydrocarbon oils, in the absence of hydrogen, by methods not otherwise provided for
- C10G31/11—Refining of hydrocarbon oils, in the absence of hydrogen, by methods not otherwise provided for by dialysis
-
- 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
- C10G2300/40—Characteristics of the process deviating from typical ways of processing
- C10G2300/44—Solvents
-
- 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
-
- 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
- FCC fluidized catalytic cracking
- coking In the FCC process, high molecular weight feeds are contacted with fluidized catalyst particles in the riser reactor of the FCC unit. The contacting between feed and catalyst is controlled according to the type of product desired. In catalytic cracking of the feed, reactor conditions such as temperature and contact time are controlled to maximize the products desired and minimize the formation of less desirable products such as light gases and coke.
- SCT FCC has been widely implemented as a means to decrease nonselective reactions, suppress undesirable hydrogen transfer reactions and yield a more valuable product slate.
- High conversion of feed is in part due to control of reaction parameters such as reactor temperature, catalyst activity, catalyst circulation rate or some combination thereof.
- Recent improvements to the SCT FCC process have focused on catalysts and hardware.
- One method for improving the SCT FCC process involves forming a falling curtain of FCC catalyst that is then contacted with feed.
- Other improvements involve hardware modifications such as dual risers.
- Still other improvements are directed to process modifications.
- There is still a need to improve the SCT FCC process which improvement can be implemented using existing catalysts and without the need for extensive modifications to the FCC unit itself.
- One embodiment of the invention relates to a fluid catalytic cracking process which comprises:
- step (e) passing the stream containing saturates and 1- and 2-ring aromatics to step (a) wherein hydrocarbon feed and the stream containing saturates and 1- and 2-ring aromatics are separately contacted with regenerated catalyst.
- the separation zone for separating spent catalyst particles from reactor effluent may employ separation devices such as cyclones.
- Spent catalyst particles are stripped of strippable hydrocarbons using a stripping agent such as steam.
- the stripped catalyst particles are then sent to a regeneration zone in which any remaining hydrocarbons are stripped and coke is removed.
- coked catalyst particles are contacted with an oxidizing medium, usually air, and coke is oxidized (burned) at high temperatures such as 650 0 C to 760°C.
- the regenerated catalyst particles are then passed back to the riser reactor.
- FCC catalysts may be amorphous, e.g., silica-alumina, crystalline, e.g., molecular sieves including zeolites, or mixtures thereof.
- a preferred catalyst particle comprises: (a) an amorphous, porous solid acid matrix, such as alumina, silica-alumina, silica-magnesia, silica-zirconia, silica- thoria, silica-beryllia, silica- titania, silica-alumina-rare earth and the like; and (b) a zeolite such as faujasite.
- the primary catalyst zeolite component includes zeolites which are iso- structural to zeolite Y. These include the ion-exchanged forms such as the rare- earth hydrogen and ultrastable (USY) form.
- the zeolite may range in crystallite size from 0.1 to 10 microns, preferably from 0.3 to 3 microns.
- the relative concentrations of zeolite component and matrix on an anhydrous basis may vary widely, with the zeolite content ranging from 1 to 100, preferably 10 to 99, more usually from 10 to 80, percent by weight of the dry composite.
- the amount of zeolite component in the catalyst particle will generally range from 1 to 60 wt.%, preferably from 5 to 60 wt.%, and more preferably from 10 to 50 wt.%, based on the total weight of the catalyst.
- the catalyst is typically in the form of a catalyst particle contained in a composite.
- the catalyst particle size will range from 10 to 300 microns in diameter, with an average particle diameter of 60 microns.
- the surface area of the matrix material after artificial deactivation in steam will be ⁇ 350 m 2 /g, preferably 50 to 200 m 2 /g, more preferably from 50 to 100 m 2 /g.
- the surface area of the catalysts will be dependent on such things as type and amount of zeolite and matrix components used, it will usually be less than 500 m 2 /g, preferably from 50 to 300 m 2 /g, more preferably from 50 to 250 m 2 /g, and most preferably from 100 to 250 m 2 /g.
- the short contact time reaction step can be achieved using any of the known processes.
- a close coupled cyclone system effectively separates the catalyst from the reacted hydrocarbon to quench the cracking reaction. See, for example, Exxon's United States Patent Number 5,190,650, Tammera, et al., of which the detailed description is incorporated herein by reference.
- the second fraction containing predominantly aromatics having three or more rings is the net bottoms stream from the process.
- predominantly is meant the concentration of 3+ ring aromatics and polar species is greater than 75 wt.% and preferably greater than 95 wt.% of the stream.
- solvent extraction One means of separating saturates and 1- and 2-ring aromatics from 3+ ring aromatics is solvent extraction.
- Preferred solvents include dimethyl sulfoxide, dimethyl formamide, n-methyl pyrrolidone (NMP), phenol and furfural, especially dimethyl sulfoxide.
- NMP n-methyl pyrrolidone
- the solvent extraction process selectively dissolves the aromatic components in an extract phase while leaving the more paraffinic components in a raffinate phase. Naphthenes are distributed between the extract and raffinate phases.
- This example relates to a short contact time FCC riser reactor. Vapor residence times in the riser are in the range of 3 to 4 seconds. Process performance data collected during a commercial monitoring test period were used to tune FCC model software program for representing base case operation. Selected feedstock inspections are listed in Table 1 :
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
Description
Claims
Applications Claiming Priority (3)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US66589905P | 2005-03-28 | 2005-03-28 | |
US66853205P | 2005-04-05 | 2005-04-05 | |
PCT/US2006/008453 WO2006104661A1 (en) | 2005-03-28 | 2006-03-10 | Improved short contact time pcc process |
Publications (1)
Publication Number | Publication Date |
---|---|
EP1866389A1 true EP1866389A1 (en) | 2007-12-19 |
Family
ID=36586066
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP06737614A Withdrawn EP1866389A1 (en) | 2005-03-28 | 2006-03-10 | Improved short contact time pcc process |
Country Status (10)
Country | Link |
---|---|
US (1) | US20060231458A1 (en) |
EP (1) | EP1866389A1 (en) |
JP (1) | JP2008534737A (en) |
CN (1) | CN101151350B (en) |
AU (1) | AU2006229739B2 (en) |
CA (1) | CA2603717A1 (en) |
MX (1) | MX2007010782A (en) |
SG (1) | SG158890A1 (en) |
TW (1) | TW200704765A (en) |
WO (1) | WO2006104661A1 (en) |
Families Citing this family (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
RU2497933C2 (en) * | 2008-03-13 | 2013-11-10 | Чайна Петролеум & Кемикал Корпорейшн | Method for conversion of low-grade raw feedstock to high-quality oil fuel |
US8128879B2 (en) | 2010-03-31 | 2012-03-06 | Uop Llc | Apparatus for increasing weight of olefins |
US8471084B2 (en) | 2010-03-31 | 2013-06-25 | Uop Llc | Process for increasing weight of olefins |
CN101972638B (en) * | 2010-11-12 | 2012-07-04 | 南开大学 | Deep denitrification method for fuel oil |
US9828309B2 (en) | 2011-05-24 | 2017-11-28 | Jx Nippon Oil & Energy Corporation | Method for producing monocyclic aromatic hydrocarbons |
FR2984917B1 (en) | 2011-12-23 | 2014-01-10 | Total Raffinage Marketing | METHOD FOR OPTIMIZING THE PRODUCTION OF DISTILLATES COMPRISING A CATALYTIC CRACKING STEP. |
Family Cites Families (22)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US733862A (en) * | 1903-02-02 | 1903-07-14 | John A Miller | Steam-generator. |
GB698332A (en) * | 1950-07-04 | 1953-10-14 | Standard Oil Co | Improvements in or relating to the refining and catalytic cracking of hydrocarbons |
BE515752A (en) * | 1951-11-30 | |||
US2790753A (en) * | 1954-12-29 | 1957-04-30 | Gulf Research Development Co | Quality of slurry oil recycle in fluid catalytic cracking |
US2850431A (en) * | 1955-12-30 | 1958-09-02 | Texas Co | Solvent deasphalting |
US3182011A (en) * | 1961-06-05 | 1965-05-04 | Sinclair Research Inc | Cracking a plurality of hydrocarbon stocks |
US3193489A (en) * | 1962-09-13 | 1965-07-06 | Phillips Petroleum Co | Solvent extraction process |
US3164542A (en) * | 1962-10-08 | 1965-01-05 | Phillips Petroleum Co | Catalytic process for the cracking of hydrocarbon oils containing metallic contaminants |
US3303123A (en) * | 1964-10-16 | 1967-02-07 | Phillips Petroleum Co | Catalytic cracking of residuum oils containing metal contaminants in several stages |
US3639228A (en) * | 1969-10-28 | 1972-02-01 | Gulf Research Development Co | Fcc process utilizing divided catalyst injection |
US4388175A (en) * | 1981-12-14 | 1983-06-14 | Texaco Inc. | Hydrocarbon conversion process |
JPS6031594A (en) * | 1983-07-30 | 1985-02-18 | Jgc Corp | Catalytic reforming of residual oil of distillation |
US5976355A (en) * | 1984-03-09 | 1999-11-02 | Stone & Webster Engineering Corp. | Low residence time catalytic cracking process |
US4606810A (en) * | 1985-04-08 | 1986-08-19 | Mobil Oil Corporation | FCC processing scheme with multiple risers |
US4784748A (en) * | 1987-10-28 | 1988-11-15 | Mobil Oil Corporation | FCC unit combined with a circulating fluid bed combustor |
US4985136A (en) * | 1987-11-05 | 1991-01-15 | Bartholic David B | Ultra-short contact time fluidized catalytic cracking process |
US4976868A (en) * | 1989-10-16 | 1990-12-11 | Exxon Research And Engineering Company | Polyester membranes for aromatics/saturates separation |
US5254795A (en) * | 1992-10-07 | 1993-10-19 | Exxon Research And Engineering Company | Removal of 2-ring aromatics from low boiling streams containing low concentrations of same using membranes |
CA2103230C (en) * | 1992-11-30 | 2004-05-11 | Paul E. Eberly, Jr. | Fluid catalytic cracking process for producing light olefins |
US5824208A (en) * | 1994-05-27 | 1998-10-20 | Exxon Research & Engineering Company | Short contact time catalytic cracking process |
FR2771418B1 (en) * | 1997-11-25 | 2001-02-02 | Inst Francais Du Petrole | PROCESS FOR SEPARATING A C5-C8 LOAD OR AN INTERMEDIATE LOAD, INTO THREE EFFLUENTS RESPECTIVELY RICH IN LINEAR, SINGLE-BRANCHED AND MULTI-BRANCHED PARAFFINS |
US6110356A (en) * | 1998-05-06 | 2000-08-29 | Uop Llc | Slurry circulation process and system for fluidized particle contacting |
-
2006
- 2006-02-14 US US11/354,701 patent/US20060231458A1/en not_active Abandoned
- 2006-03-10 MX MX2007010782A patent/MX2007010782A/en unknown
- 2006-03-10 AU AU2006229739A patent/AU2006229739B2/en not_active Ceased
- 2006-03-10 EP EP06737614A patent/EP1866389A1/en not_active Withdrawn
- 2006-03-10 JP JP2008504076A patent/JP2008534737A/en active Pending
- 2006-03-10 WO PCT/US2006/008453 patent/WO2006104661A1/en active Application Filing
- 2006-03-10 CN CN2006800099928A patent/CN101151350B/en not_active Expired - Fee Related
- 2006-03-10 CA CA002603717A patent/CA2603717A1/en not_active Abandoned
- 2006-03-10 SG SG201000286-3A patent/SG158890A1/en unknown
- 2006-03-13 TW TW095108475A patent/TW200704765A/en unknown
Non-Patent Citations (1)
Title |
---|
See references of WO2006104661A1 * |
Also Published As
Publication number | Publication date |
---|---|
SG158890A1 (en) | 2010-02-26 |
CA2603717A1 (en) | 2006-10-05 |
MX2007010782A (en) | 2007-11-07 |
US20060231458A1 (en) | 2006-10-19 |
CN101151350A (en) | 2008-03-26 |
AU2006229739B2 (en) | 2011-05-12 |
AU2006229739A1 (en) | 2006-10-05 |
TW200704765A (en) | 2007-02-01 |
WO2006104661A1 (en) | 2006-10-05 |
JP2008534737A (en) | 2008-08-28 |
CN101151350B (en) | 2012-02-08 |
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Legal Events
Date | Code | Title | Description |
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PUAI | Public reference made under article 153(3) epc to a published international application that has entered the european phase |
Free format text: ORIGINAL CODE: 0009012 |
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17P | Request for examination filed |
Effective date: 20070928 |
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AK | Designated contracting states |
Kind code of ref document: A1 Designated state(s): AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HU IE IS IT LI LT LU LV MC NL PL PT RO SE SI SK TR |
|
DAX | Request for extension of the european patent (deleted) | ||
17Q | First examination report despatched |
Effective date: 20090525 |
|
RIN1 | Information on inventor provided before grant (corrected) |
Inventor name: COOK, BRUCE, R. Inventor name: MON, EDUARDO Inventor name: SWAN, GEORGE, A., III Inventor name: LOWENTHAL, STEVEN, S. |
|
STAA | Information on the status of an ep patent application or granted ep patent |
Free format text: STATUS: THE APPLICATION IS DEEMED TO BE WITHDRAWN |
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18D | Application deemed to be withdrawn |
Effective date: 20131001 |