EP0758014A2 - Externes geschlossenes Druck-Cyclon für FCC-Anlage - Google Patents

Externes geschlossenes Druck-Cyclon für FCC-Anlage Download PDF

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Publication number
EP0758014A2
EP0758014A2 EP96112454A EP96112454A EP0758014A2 EP 0758014 A2 EP0758014 A2 EP 0758014A2 EP 96112454 A EP96112454 A EP 96112454A EP 96112454 A EP96112454 A EP 96112454A EP 0758014 A2 EP0758014 A2 EP 0758014A2
Authority
EP
European Patent Office
Prior art keywords
catalyst
catalyst particles
cyclone
primary
stripping vessel
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Withdrawn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
EP96112454A
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English (en)
French (fr)
Other versions
EP0758014A3 (de
Inventor
Phillip K. Niccum
Philip E. Glasgow
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.)
MW Kellogg Co
Original Assignee
MW Kellogg 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 MW Kellogg Co filed Critical MW Kellogg Co
Publication of EP0758014A2 publication Critical patent/EP0758014A2/de
Publication of EP0758014A3 publication Critical patent/EP0758014A3/de
Withdrawn legal-status Critical Current

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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
    • 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
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
    • B04C—APPARATUS USING FREE VORTEX FLOW, e.g. CYCLONES
    • B04C9/00—Combinations with other devices, e.g. fans, expansion chambers, diffusors, water locks
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
    • B04C—APPARATUS USING FREE VORTEX FLOW, e.g. CYCLONES
    • B04C5/00—Apparatus in which the axial direction of the vortex is reversed
    • B04C5/02—Construction of inlets by which the vortex flow is generated, e.g. tangential admission, the fluid flow being forced to follow a downward path by spirally wound bulkheads, or with slightly downwardly-directed tangential admission

Definitions

  • the present invention relates to a fluid catalytic cracking (FCC) unit, and more particularly a pressurized, closed-cyclone apparatus useful in an FCC unit.
  • FCC fluid catalytic cracking
  • staged cyclone separators are enclosed in a disengagement vessel and effluent from the riser is fed directly to the primary cyclone.
  • Gaseous effluent from the primary cyclone is directly introduced to a secondary cyclone (and any additional cyclone stages) which are directly connected by conduit without any additional reaction residence time in the disengagement vessel.
  • the conduits (or plenums) between stages have vents to permit stripping steam to enter.
  • the separated catalyst particles travel down diplegs of the cyclone stages for accumulation in the disengagement vessel and feed to a catalyst regeneration stage. See also Peterson U. S. Patent 5,370,844 which is hereby incorporated herein by reference.
  • the cyclone stages have not been pressurized independently from the disengagement vessel in which they have been housed. To permit the introduction of stripping steam into the cyclone plenum inlets from the disengagement vessel, the cyclone stages have been maintained totally enclosed within the pressurized catalyst disengagement vessel.
  • U. S. Patent 4,455,220 to Parker et al. describes the separation of catalyst and hydrocarbon vapors in a cyclone zone attached to the discharge of a riser wherein a vortex stabilizing means separates the cyclone zone from a stripping zone and allows stripping gas in the stripping zone to be passed therethrough to the cyclone zone countercurrent to the downward flow of the catalyst.
  • U. S. Patent 4,721,603 to Krug et al. describes a specific baffle arrangement within a catalytic reactor which improves the separation of gaseous hydrocarbon reaction products from catalyst within the reactor vessel.
  • a pressurized, externally disposed, closed-cyclone apparatus of the present invention has a vent line for introducing stripping steam and hydrocarbon vapor from a catalyst stripping stage to a catalyst disengaging stage, and diplegs for discharging separated catalyst particles from the catalyst disengaging stage to the stripping stage for rapidly disengaging catalyst from the cracked hydrocarbon effluent of an FCC riser.
  • the present invention provides an apparatus for disengaging catalyst particles from a cracked hydrocarbon gas in a fluidized catalytic cracking (FCC) unit.
  • a pressure-containing primary cyclone is provided for receiving cracked hydrocarbon gas containing suspended catalyst particles from an FCC riser and disengaging a major portion of the catalyst particles therefrom to form a gas stream of reduced catalyst content.
  • a plenum is provided for passing the gas stream from the primary cyclone to pressure-containing secondary cyclone(s) adapted to disengage residual catalyst particles and form an essentially catalyst-free hydrocarbon stream.
  • Primary and secondary diplegs are provided for gravity-feeding disengaged catalyst particles from the respective primary and secondary cyclones into a stripping vessel.
  • a steam distributor is provided for countercurrently contacting catalyst particles in the stripping vessel with steam. Lines are provided for venting steam and hydrocarbon vapors from the stripping vessel to the plenum and for withdrawing stripped catalyst particles from the stripping vessel.
  • the cyclones have refractory linings comprising high density vibration cast refractory.
  • the primary cyclone is preferably supported atop the stripping vessel with the primary dipleg descending from the primary cyclone coaxially into the stripping vessel.
  • the stripping vessel preferably includes an annular catalyst disengagement zone between a stripper bed and an outlet to the steam venting line.
  • the stripping vessel preferably includes a baffled section between the bottom of the primary dipleg and the steam injection distributor.
  • the secondary dipleg is preferably connected to the stripping vessel adjacent the bottom of the primary dipleg.
  • the primary and secondary cyclones have an exterior surface exposed to ambient conditions.
  • the present invention provides a method for disengaging catalyst particles from a cracked hydrocarbon gas in a fluidized catalytic cracking (FCC) unit.
  • FCC fluidized catalytic cracking
  • cracked hydrocarbon gas containing catalyst particles is passed involutely through a pressurized primary cyclone to disengage catalyst particles and form a catalyst-lean stream.
  • the catalyst-lean stream is passed from the primary cyclone into a sealed plenum. Steam is introduced into the stripper to countercurrently contact the catalyst particles. Steam and hydrocarbon vapors from an overhead vapor space in the stripper are passed into the plenum.
  • the catalyst-lean stream, steam and hydrocarbon vapors from the plenum are passed involutely through a pressurized secondary cyclone(s) to disengage residual catalyst particles and form an essentially catalyst-free stream.
  • the disengaged catalyst particles from the secondary cyclone are passed into the stripper. Stripped catalyst particles from the stripper are recovered.
  • the primary and secondary cyclones are preferably operated with walls exposed to ambient conditions.
  • the primary cyclone is preferably supported coaxially atop the stripping vessel.
  • the stripping vessel is preferably supported coaxially atop or adjacent a regenerator and the recovered catalyst particles are passed from the stripper into the regenerator.
  • Fig. 1 is a schematic representation of a side view of an embodiment of an FCC reaction unit showing a pressurized, closed-cyclone apparatus of the present invention externally mounted to the side of a regeneration vessel.
  • Fig. 2 is a schematic representation of a side view of another embodiment of an FCC reaction unit showing the pressurized, close-cyclone apparatus externally mounted from above the regeneration vessel.
  • An externally mounted, closed-cyclone separation apparatus of the present invention is independently pressurized to permit elimination of an enclosing disengagement vessel without decreasing the efficiency of catalyst disengagement and recovery of hydrocarbons from spent catalyst particles.
  • embodiments 10 , 100 of a fluidized catalytic cracking (FCC) reaction unit of the present invention have a pressurized, two-stage closed-cyclone disengagement apparatus 12 mounted externally with respect of a regeneration vessel 14 either from the side as seen in Fig. 1 or from above as seen in Fig. 2 to rapidly disengage catalyst particles from the riser 16 effluent.
  • a regeneration vessel 14 either from the side as seen in Fig. 1 or from above as seen in Fig. 2 to rapidly disengage catalyst particles from the riser 16 effluent.
  • Use of the present cyclone apparatus 12 minimizes undesirable side reactions to maximize yield of desired products without lowering the efficiency of catalyst disengagement.
  • the relatively high cost and complexity of installing and maintaining cyclones within an enclosing disengagement vessel in the prior art is eliminated.
  • the cracking of heavy hydrocarbons such as petroleum oils into lighter hydrocarbons such as gasoline, light cycle oil (LCO), and olefins by FCC is well known.
  • the process employs finely divided fluidized catalyst particles which are continuously circulated between a reaction zone in the riser 16 and a regeneration zone in the regeneration vessel 14 .
  • long chain hydrocarbons are split into shorter chain molecules and carbon deposits form on the catalyst particles.
  • Carbon-coated catalyst also referred to in the art as spent catalyst, is then disengaged from the effluent hydrocarbons by the closed-cyclone apparatus 12 and circulated to a regeneration zone in the regeneration vessel 14 .
  • a cracked hydrocarbon stream essentially free of catalyst is withdrawn from the cyclone apparatus 12 for the recovery of heat and hydrocarbon products.
  • Hot exhaust gas produced by catalyst regeneration is preferably separated from the entrained catalyst by a disengagement stage comprising cyclones 19 internally disposed in the regeneration vessel 14 .
  • the cyclones 19 are operated conventionally and have diplegs 20 extending into a bed 22 of regenerated catalyst to seal the diplegs 22 from exhaust gas. Gas discharged from the cyclones 19 is withdrawn for the recovery of heat (e. g. steam generation) prior to disposal.
  • a fluidized hydrocarbon/catalyst reaction medium is maintained in a reaction zone of the riser 16 at an elevated temperature and pressure for a suitable length of time necessary to maximize the desired mix of cracked hydrocarbon products in the reaction effluent.
  • the riser reaction zone is preferably maintained in a plug-flow mass transport regime and backmixing is minimized as the reaction medium circulates up the riser 16 for discharge into the present closed-cyclone catalyst disengagement apparatus 12 .
  • the riser 16 is maintained in pressurized fluid communication with a primary disengagement stage of the present closed-cyclone disengagement apparatus 12 via a conduit 23 transversely oriented thereto.
  • the riser effluent stream 23 is introduced to an upper end of an involutely-shaped primary cyclone 24 wherein a major portion of the suspended catalyst is conventionally disengaged from the riser effluent stream 23 and removed by gravity down a dipleg 25 to a catalyst accumulation and stripping zone.
  • Discharged gas from the primary cyclone 24 is passed through a discharge duct 26 and gathered into a plenum 28 disposed at an inlet to a secondary disengagement stage comprising one or more secondary cyclones 30 .
  • Gas from the plenum is roughly evenly distributed to an upper involute end of the secondary cyclone(s) 30 via a duct 32 .
  • the secondary cyclone(s) 30 substantially disengages all the remaining suspended catalyst particles from the discharge gas 26 . Separated catalyst particles are subsequently removed by gravity down a dipleg 34 to the catalyst accumulation and stripping zone.
  • the diplegs 25 , 34 have openings (not shown) extending below an upper surface of a spent catalyst bed 38 accumulated in a stripping vessel 40 to seal the diplegs 25 , 34 from stripping steam introduced via one or more steam spargers 39.
  • the stripping vessel 40 is integrally connected to the primary cyclone 24 so that the dipleg 25 is coaxially received therein.
  • the cyclone apparatus 12 and stripping vessel 40 together can be positioned to maximize layout efficiency of the reaction units 10 , 100 without the necessity of housing in a disengagement vessel.
  • the stripping vessel could be positioned to the side of the cyclone 24 and the dipleg 25 could be inclined in a fashion similar to cyclone 30 and dipleg 34 .
  • Steam is preferably countercurrently distributed through the bed 38 to enhance the stripping of hydrocarbons from the catalyst particles.
  • several steam distribution baffles 42 are preferably disposed within the catalyst bed 38 to ensure suitable countercurrent distribution of steam therein.
  • a vent line 44 is used to introduce a stream comprising hydrocarbon vapor and steam accumulating in the stripping vessel 40 to the secondary cyclone stage of the present closed-cyclone apparatus 12 .
  • the vent line 44 preferably extends from an upper end 46 of the vessel 40 to the plenum 28 to facilitate disengagement of the catalyst particles from the steam/hydrocarbon mixture in the secondary cyclone(s) 30 .
  • a discharge gas which is substantially free of suspended particles is withdrawn from the secondary cyclone(s) 30 via duct(s) 48 .
  • Catalyst particles which have been substantially stripped of volatile hydrocarbons are circulated to the regenerator vessel 14 via standpipe 50 .
  • the present closed-cyclone apparatus 12 in combination with the stripping vessel 40 can be mounted externally atop the catalyst regenerator 14 .
  • Catalyst accumulating in the stripping vessel 40 is preferably passed into the regenerator 14 through a standpipe 104 extending therein.
  • the standpipe 104 can extend into a spent catalyst distributor 105 connected to a gas inlet line 106 so that catalyst particles from the standpipe 104 are fluidized by the gas.
  • Catalyst in the regenerator 14 can be cooled by one or more external bayonet type exchangers 110 as known in the art.
  • Catalyst solids enter the exchanger 110 through line 112 for heat exchange with a cooling medium flowing through internal tubes (not shown) such as boiler feedwater to generate steam.
  • the exchanger 110 is vented to the regenerator 14 via line 114 .
  • the cooled catalyst solids are discharged to the regenerator 14 via standpipe 116 . Cooled, regenerated catalyst is circulated back to the riser 16 via standpipe 118 .
  • the standpipe 118 has a catalyst flow control valve 120 to maintain a suitable catalyst circulation rate to the riser 16 .
  • Exhaust gas is withdrawn via line 122 .
  • the closed-cyclone apparatus 12 of the present invention pressurized independently from any disengagement vessel, is preferably made by pressure vessel techniques used for withstanding the stresses of a pressurized fluid at elevated operating temperatures and erosion due to high velocity particulate flows.
  • the cyclone walls are preferably internally lined with refractory. Both cold wall and hot wall refractory lining designs can be used.
  • a suitable hot wall construction includes an insulated exterior surface having an approximately 2.5 cm thick interior erosion resistant refractory lining supported in hexsteel.
  • a preferred cold wall construction includes an uninsulated exterior surface and an interior surface lined with a thicker vibration cast refractory up to about 13 cm (5 inches) thick.
  • An equipment cost estimation is made to compare the costs of an internal cyclone system (and disengager vessel) against an external cyclone arrangement (including stripping vessel) of the present invention designed for operation at a pressure in the range of 15-25 psi above atmospheric.
  • Basis for sizing the equipment is a 25,000 barrels per day FCC unit charge rate. Standard cost estimating techniques are employed and the results are presented in the Table with a ⁇ 25% accuracy.
  • a pressurized closed-cyclone catalyst disengaging apparatus for use in an FCC unit A closed-cyclone apparatus of the present invention independently pressurized in the absence of a disengager vessel has a line for venting stripping steam and hydrocarbon vapor from a catalyst stripping stage to a catalyst disengaging stage for rapidly disengaging catalyst particles from an FCC reaction hydrocarbon effluent.

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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)
  • Physics & Mathematics (AREA)
  • Fluid Mechanics (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Cyclones (AREA)
  • Catalysts (AREA)
EP96112454A 1995-08-09 1996-08-01 Externes geschlossenes Druck-Cyclon für FCC-Anlage Withdrawn EP0758014A3 (de)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US51287095A 1995-08-09 1995-08-09
US512870 1995-08-09

Publications (2)

Publication Number Publication Date
EP0758014A2 true EP0758014A2 (de) 1997-02-12
EP0758014A3 EP0758014A3 (de) 1997-04-02

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EP96112454A Withdrawn EP0758014A3 (de) 1995-08-09 1996-08-01 Externes geschlossenes Druck-Cyclon für FCC-Anlage

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EP (1) EP0758014A3 (de)
JP (1) JPH09143479A (de)
KR (1) KR970009895A (de)
CA (1) CA2180686A1 (de)
MX (1) MX9603320A (de)

Families Citing this family (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US7736501B2 (en) 2002-09-19 2010-06-15 Suncor Energy Inc. System and process for concentrating hydrocarbons in a bitumen feed
CA2400258C (en) 2002-09-19 2005-01-11 Suncor Energy Inc. Bituminous froth inclined plate separator and hydrocarbon cyclone treatment process
CA2455011C (en) 2004-01-09 2011-04-05 Suncor Energy Inc. Bituminous froth inline steam injection processing
CA2827237C (en) 2005-11-09 2016-02-09 Suncor Energy Inc. Mobile oil sands mining system
CA2526336C (en) 2005-11-09 2013-09-17 Suncor Energy Inc. Method and apparatus for oil sands ore mining
US8168071B2 (en) 2005-11-09 2012-05-01 Suncor Energy Inc. Process and apparatus for treating a heavy hydrocarbon feedstock
CA2689021C (en) 2009-12-23 2015-03-03 Thomas Charles Hann Apparatus and method for regulating flow through a pumpbox

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3261776A (en) * 1962-05-23 1966-07-19 Exxon Research Engineering Co Conversion of hydrocarbons
US4502947A (en) * 1984-05-21 1985-03-05 Mobil Oil Corporation Closed cyclone FCC catalyst separation method and apparatus
EP0236055A2 (de) * 1986-02-24 1987-09-09 Engelhard Corporation Verfahren zur Behandlung von Kohlenwasserstoffen
EP0613935A1 (de) * 1993-03-01 1994-09-07 The M.W. Kellogg Company FCC-Phasenauslösungsapparatur

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3261776A (en) * 1962-05-23 1966-07-19 Exxon Research Engineering Co Conversion of hydrocarbons
US4502947A (en) * 1984-05-21 1985-03-05 Mobil Oil Corporation Closed cyclone FCC catalyst separation method and apparatus
EP0236055A2 (de) * 1986-02-24 1987-09-09 Engelhard Corporation Verfahren zur Behandlung von Kohlenwasserstoffen
EP0613935A1 (de) * 1993-03-01 1994-09-07 The M.W. Kellogg Company FCC-Phasenauslösungsapparatur

Also Published As

Publication number Publication date
EP0758014A3 (de) 1997-04-02
MX9603320A (es) 1997-03-29
JPH09143479A (ja) 1997-06-03
KR970009895A (ko) 1997-03-27
CA2180686A1 (en) 1997-02-10

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