WO2015119598A1 - Procédés et appareils de traitement de combustible pour améliorer un courant d'huile de pyrolyse et un courant d'hydrocarbures - Google Patents

Procédés et appareils de traitement de combustible pour améliorer un courant d'huile de pyrolyse et un courant d'hydrocarbures Download PDF

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Publication number
WO2015119598A1
WO2015119598A1 PCT/US2014/014806 US2014014806W WO2015119598A1 WO 2015119598 A1 WO2015119598 A1 WO 2015119598A1 US 2014014806 W US2014014806 W US 2014014806W WO 2015119598 A1 WO2015119598 A1 WO 2015119598A1
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WIPO (PCT)
Prior art keywords
stream
pyrolysis oil
hydrocarbon
oil stream
hydrocarbon stream
Prior art date
Application number
PCT/US2014/014806
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English (en)
Inventor
Lance Awender Baird
Paolo Palmas
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Uop Llc
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 Uop Llc filed Critical Uop Llc
Priority to PCT/US2014/014806 priority Critical patent/WO2015119598A1/fr
Publication of WO2015119598A1 publication Critical patent/WO2015119598A1/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
    • C10G3/00—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
    • C10G3/42—Catalytic treatment
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/005—Separating solid material from the gas/liquid stream
    • B01J8/0055—Separating solid material from the gas/liquid stream using cyclones
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
    • B01J8/26—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with two or more fluidised beds, e.g. reactor and regeneration installations
    • 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
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P30/00—Technologies relating to oil refining and petrochemical industry
    • Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock

Definitions

  • the technical field generally relates to methods and fuel processing apparatuses for upgrading a pyrolysis oil stream and a hydrocarbon stream. More particularly, the technical field relates to methods and fuel processing apparatuses for cataly tically cracking a mixture of a pyrolysis oil stream and a hydrocarbon stream.
  • Fluid catalytic cracking is a well-known process for the conversion of relatively high boiling point hydrocarbons to lower boiling point hydrocarbons in the heating oil or gasoline (or lighter) range. Such processes are commonly referred to in the art as “upgrading" processes.
  • FCC units are generally provided that have one or more reaction chambers, with a hydrocarbon stream contacted in the one or more reaction chambers with a particulate cracking catalyst.
  • the particulate cracking catalyst is maintained in a fluidized state under conditions that are suitable for the conversion of the relatively high boiling point hydrocarbons to lower boiling point hydrocarbons.
  • Biofuels encompass various types of combustible fuels that are derived from organic biomass, and one particular type of biofuel is pyrolysis oil, which is also commonly referred to as biomass-derived pyrolysis oil.
  • Pyrolysis oil is produced through pyrolysis, including through recently-developed fast pyrolysis processes.
  • Fast pyrolysis is a process during which organic biomass, such as wood waste, agricultural waste, etc., is rapidly heated to 450°C to 600°C in the absence of air using a pyrolysis unit. Under these conditions, a pyrolysis vapor stream including organic vapors, water vapor, and pyrolysis gases is produced, along with char (which includes ash and combustible hydrocarbon solids).
  • Pyrolysis oil is a complex, highly oxygenated organic liquid that typically contains 20-30% by weight water with high acidity (TAN >150).
  • pyrolysis oils Due to the high oxygen content of the pyrolysis oils, pyrolysis oils are generally immiscible with hydrocarbon streams.
  • Prior attempts to co-process pyrolysis oil streams and hydrocarbon streams have involved deoxygenation of the pyrolysis oil followed by combining the deoxygenated pyrolysis oil stream and hydrocarbon stream prior to FCC processing.
  • Such approaches add unit operations, along with added capital costs, to the upgrading process.
  • clogging of feed lines may still remain a concern even after deoxygenating the pyrolysis oils, and feed lines that facilitate introduction of a pyrolysis oil stream into a reaction zone where FCC processing is conducted are prone to clogging.
  • feed lines that contain mixtures of a hydrocarbon stream and a pyrolysis oil stream are also generally prone to clogging due to the presence of the pyrolysis oil stream in the feed lines.
  • a method for upgrading a pyrolysis oil stream and a hydrocarbon stream includes providing a pyrolysis oil stream and providing a hydrocarbon stream separate from the pyrolysis oil stream.
  • the pyrolysis oil stream and the hydrocarbon stream are mixed in a mixing zone and in the absence of a particulate cracking catalyst.
  • the pyrolysis oil stream and the hydrocarbon stream are introduced in a substantially common direction into the mixing zone to form a mixture of the pyrolysis oil stream and the hydrocarbon stream.
  • the mixture of the pyro lysis oil stream and the hydrocarbon stream are catalytically cracked in the presence of the particulate cracking catalyst.
  • a method for upgrading a pyrolysis oil stream and a hydrocarbon stream is conducted in a fluid catalytic cracking unit
  • the fluid catalytic cracking unit includes a reaction chamber and a feed distributor mat is in fluid
  • the method includes providing the hydrocarbon stream separate from the pyrolysis oil stream to the feed distributor.
  • the feed distributor includes a pyrolysis oil feed line and a hydrocarbon feed line mat have respective outlets into a mixing zone for separately supporting flow of the hydrocarbon stream and the pyrolysis oil stream into the mixing zone.
  • the pyrolysis oil feed line and the hydrocarbon feed line extend in a substantially common direction to the respective outlets.
  • the hydrocarbon stream and the pyrolysis oil stream are mixed in the mixing zone and in the absence of a particulate cracking catalyst to form a mixture of the pyrolysis oil stream and the hydrocarbon stream.
  • the mixture of the pyrolysis oil stream and the hydrocarbon stream are introduced into a reaction zone within the reaction chamber, and the mixture of the pyrolysis oil stream and the hydrocarbon stream are catalytically cracked in the presence of the particulate cracking catalyst in the reaction zone within the reaction chamber.
  • a fuel processing apparatus includes a pyrolysis unit for pyrolyzing a biomass stream to produce a pyrolysis oil stream.
  • the fluid processing apparatus further includes a fluid catalytic cracking unit, and the fluid catalytic cracking unit includes a reaction chamber and a feed distributor.
  • the reaction chamber has a reaction zone within which particulate cracking catalyst is contacted with a mixture of a hydrocarbon stream and the pyrolysis oil stream.
  • the feed distributor is adapted to receive the pyrolysis oil stream and the hydrocarbon stream.
  • the feed distributor includes a pyrolysis oil feed line and a hydrocarbon feed line that have respective outlets into a mixing zone for separately supporting flow of the hydrocarbon stream and the pyrolysis oil stream into the mixing zone.
  • the pyrolysis oil feed line and the hydrocarbon feed line extend in a substantially common direction to the respective outlets.
  • FIG. 1 is a schematic diagram of a fuel processing apparatus and a method for preparing upgraded pyrolysis oil in accordance with an exemplary embodiment
  • FIG. 2 is a schematic diagram of a portion of the schematic diagram of FIG. 1 showing an embodiment of a feed distributor in greater detail;
  • FIG. 3 is a partial schematic view of the schematic diagram of FIG. 2 shown features of the feed distributor in greater detail.
  • Upgrading processes generally render a hydrocarbon stream and a pyrolysis oil stream suitable for use as a transportation fuel.
  • a mixture of the pyrolysis oil stream and the hydrocarbon stream are catalytically cracked in a reaction zone in the presence of a particulate cracking catalyst.
  • the reaction zone as referred to herein, is an area or space where particulate cracking catalyst is comingled along with the pyrolysis oil stream and/or the hydrocarbon stream.
  • Catalytic cracking is conducted at temperatures in excess of 100 °C, and the hydrocarbon stream is generally provided at temperatures in excess of 100 °C.
  • pyrolysis oil generally polymerizes at temperatures in excess of 100 °C and forms deposits within the apparatuses. Deposit formation is less of a concern in the reaction zone than in feed lines that lead to the reaction zone. In particular, deposit formation in the reaction zone generally results in deposited compounds forming on the particulate cracking catalyst.
  • the particulate cracking catalyst may be regenerated through conventional processes even with high amounts of deposited compounds present thereon, operation of the fuel processing apparatuses is not materially affected by formation of deposited compounds on the particulate cracking catalyst.
  • deposit formation in the feed lines that lead to the reaction zone may result in clogging, which requires shutdown of the fuel processing apparatuses and cleanout of the clogged feed lines. Therefore, to minimize deposit formation attributable to polymerization within the pyrolysis oil stream in the feed lines that lead to the reaction zone, the methods and fuel processing apparatuses that are described herein are adapted to minimize temperature rise of the pyrolysis oil stream until the pyrolysis oil stream is clear of structure upon which deposit formation could cause clogging.
  • the pyrolysis oil stream and the hydrocarbon stream are mixed in a mixing zone in the absence of a particulate cracking catalyst.
  • the pyrolysis oil stream and the hydrocarbon stream are introduced in a substantially common direction, optionally in the presence of a carrier gas, into the mixing zone to form a mixture of the pyrolysis oil stream and the hydrocarbon stream.
  • inertial flow of the mixture of the pyrolysis oil stream and the hydrocarbon stream into the reaction zone from the mixing zone minimizes contact time between the pyrolysis oil stream and the hydrocarbon stream before entry into the reaction zone to thereby minimize temperature rise of the pyrolysis oil stream from the hotter hydrocarbon stream.
  • the fuel processing apparatus 10 includes a pyrolysis unit 12 and a fluid catalytic cracking (FCC) unit 14.
  • the pyrolysis unit 12 provides a pyrolysis oil stream 16 by pyrolyzing a biomass stream 18 to produce the pyrolysis oil stream 16, such as through recently-developed fast pyrolysis.
  • Fast pyrolysis is a process during which the biomass stream 18, such as wood waste, agricultural waste, biomass that is purposely grown and harvested for energy, and the like, is rapidly heated to 450°C to 600°C in the absence of air in the pyrolysis unit 12.
  • a pyrolysis vapor stream including organic vapors, water vapor, and pyrolysis gases is produced, along with char (which includes ash and combustible hydrocarbon solids).
  • a portion of the pyrolysis vapor stream is condensed in a condensing system within the pyrolysis unit 12 to produce the pyrolysis oil stream 16.
  • the pyrolysis oil stream 16 is a complex, organic liquid having an oxygen content, and may also contain water.
  • the oxygen content of the pyrolysis oil stream 16 can be from 30 to 60 weight %, such as from 40 to 55 weight %, based on the total weight of the pyrolysis oil stream 16.
  • Water can be present in the pyrolysis oil stream 16 in an amount of from 10 to 35 weight %, such as from 20 to 32 weight %, based on the total weight of the pyrolysis oil stream 16. It is to be appreciated that in other embodiments, although not shown, the pyrolysis oil stream 16 may be provided from any source of pyrolysis oil such as a vessel that contains the pyrolysis oil stream 16, and the methods described herein are not limited to providing the pyrolysis oil stream 16 from any particular source.
  • the pyrolysis oil stream 16 is provided from the pyrolysis unit 12 at a temperature of less than or equal to 100 °C, such as less than or equal to 80 °C, to minimize polymerization of the pyrolysis oil stream 16 that could lead to deposit formation after leaving the pyrolysis unit 12.
  • hydrocarbon stream 20 refers to a petroleum-based source of hydrocarbons.
  • the hydrocarbon stream 20 is provided separate from the pyrolysis oil stream 16, with the pyrolysis oil stream 16 and hydrocarbon stream 20 later mixed in a mixing zone 22 as described in further detail below.
  • the hydrocarbon stream 20 can include a fresh stream of hydrocarbons, or can include a refined stream of hydrocarbons from other refinement operations.
  • the hydrocarbon stream 20 is vacuum gas oil, which is a common hydrocarbon stream 20 that is upgraded in FCC units.
  • the hydrocarbon stream 20 may be provided from any source, and the methods described herein are not limited to providing the hydrocarbon stream 20 from any particular source.
  • the hydrocarbon stream 20 is provided at a higher temperature than the pyrolysis oil stream 16 because little risk of deposit formation from the hydrocarbon stream 20 exists due to elevated temperatures and because elevated temperatures of the hydrocarbon stream 20 promote catalytic cracking.
  • the hydrocarbon stream 20 is provided at a temperature of at least 100 °C, such as from 100 to 425 °C, for example from 200 to 300 °C.
  • an exemplary embodiment of the FCC unit 14 contemplated herein includes a reaction chamber 24 and a feed distributor 26 that is adapted to receive the pyrolysis oil stream 16 and the hydrocarbon stream 20.
  • the reaction chamber 24 has a reaction zone 28 within which a particulate cracking catalyst 30 is contacted with a mixture 46 of the hydrocarbon stream 20 and the pyrolysis oil stream 16.
  • the feed distributor 26 is in fluid communication with the reaction chamber 24 for providing the pyrolysis oil stream 16 and the hydrocarbon stream 20 into the reaction chamber 24 and, more particularly, into the reaction zone 28. As shown in FIG.
  • the feed distributor 26 includes a pyrolysis oil feed line 32 and a hydrocarbon feed line 34 that have respective outlets 36, 38 into the mixing zone 22 for separately supporting flow of the hydrocarbon stream 20 and the pyrolysis oil stream 16 into the mixing zone 22.
  • the exemplary method continues with providing the hydrocarbon stream 20 separate from the pyrolysis oil stream 16 to the feed distributor 26.
  • the pyrolysis oil stream 16 and the hydrocarbon stream 20 remain separated by flowing through the pyrolysis oil feed line 32 and the hydrocarbon feed line 34, respective.
  • a temperature rise of the pyrolysis oil stream 16 can be controlled and a temperature of the pyrolysis oil stream 16 can be maintained at less than or equal to 100 °C.
  • the pyrolysis oil stream 16 and the hydrocarbon stream 20 are introduced in a substantially common direction 40 into the mixing zone 22, as alluded to above.
  • substantially common direction means that both the pyrolysis oil stream 16 and the hydrocarbon stream 20 have a directional flow toward the mixing zone 22 with the individual directional flows offset by an angle of less than or equal to 60°, such as an offset of 0°.
  • the pyrolysis oil stream 16 and the hydrocarbon stream 20 are introduced in the same direction 40 into the mixing zone 22 with no offset angle between the individual directional flows, that is, their flows are parallel.
  • the hydrocarbon feed line 34 is concentric the pyrolysis oil feed line
  • the pyrolysis oil feed line 32 and concentrically disposed hydrocarbon feed line 34 introduce the pyrolysis oil stream 16 and the hydrocarbon stream 20, respectively, into the mixing zone 22 in the same direction 40 with no offset angle between the individual directional flows.
  • the pyrolysis stream and the hydrocarbon stream flow in an at least substantially coaxial manner, that is, offset by an angle of 0°.
  • the pyrolysis oil feed line 32 and the hydrocarbon feed line 34 are at least substantially parallel to each other such that the pyrolysis stream and the hydrocarbon stream flow in an at least substantially parallel manner, that is, offset by an angle of 0°.
  • the exemplary method continues with mixing the pyrolysis oil stream 16 and the hydrocarbon stream 20 in the mixing zone 22, in the absence of the particulate cracking catalyst 30, to form a mixture 46 of the pyrolysis oil stream 16 and the hydrocarbon stream 20.
  • the mixing zone 22, as referred to herein, represents a location where the pyrolysis oil stream 16 and the hydrocarbon stream 20 are first brought into physical contact with each other.
  • the mixing zone 22 is located outside of the reaction chamber 24.
  • the mixing zone 22 is located within the feed distributor 26. In this embodiment and as shown in FIG.
  • the outlets 36, 38 of the pyrolysis oil feed line 32 and (he hydrocarbon feed line 34 are located within the feed distributor 26, with the mixing zone 22 of the feed distributor 26 located within a nozzle 42 of the feed distributor 26.
  • the feed distributor 26 optionally includes a spray head 44 for conveying the mixture 46 of the pyrolysis oil stream 16 and the hydrocarbon stream 20 from the mixing zone 22.
  • the mixing zone 22 may be present within the reaction chamber 24 but outside of the reaction zone 28.
  • the particulate cracking catalyst 30 may be introduced into the reaction chamber 24 at an outlet that is downstream of the mixing zone in the reaction chamber 24, with the mixture 46 of the pyrolysis oil stream 16 and the hydrocarbon stream 20 introduced into the reaction zone 28 separate from the particulate cracking catalyst 30.
  • the outlets of the pyrolysis oil feed line 32 and the hydrocarbon feed line 34 are disposed directly within the reaction chamber 24.
  • the pyrolysis oil stream 16 produced from pyrolyzing the biomass stream 18 is mixed with the hydrocarbon stream 20 in the absence of intervening upgrading processing of the pyrolysis oil stream 16.
  • Intervening upgrading processes include, but are not limited to, deoxygenation, cracking, hydrotreating, and the like.
  • the pyrolysis oil stream 16 is provided directly as a condensed product stream from the pyrolysis unit 12.
  • Deposit formation from the pyrolysis oil stream 16 is attributable to a temperature rise of the pyrolysis oil stream 16 above 100 °C.
  • the pyrolysis oil stream 16 is maintained at a temperature of less than or equal to 100 °C, such as less than or equal to 80 °C, up to introduction into the mixing zone 22, i.e., prior to mixing with the hydrocarbon stream 20.
  • the pyrolysis oil stream 16 and the hydrocarbon stream 20 are comingled for a period of less than or equal to 2 seconds, such as less than or equal to 1.4 seconds, upon mixing in the mixing zone 22 before catalytically cracking the mixture 46 of the pyrolysis oil stream 16 and the hydrocarbon stream 20.
  • the methods described herein are effective for minimizing deposit formation from the pyrolysis oil stream 16 prior to introducing the pyrolysis oil stream 16 into the reaction zone 28, independent of a ratio of the pyrolysis oil stream 16 to the hydrocarbon stream 20, excessive deposit formation on the particulate cracking catalyst 30 may be avoided by adjusting the ratio at which the pyrolysis oil stream 16 and the hydrocarbon stream 20 are mixed.
  • the pyrolysis oil stream 16 and the hydrocarbon stream 20 are mixed at a weight ratio of the pyrolysis oil stream 16 to the hydrocarbon stream 20 of from 0.005: 1 to 0.2:1, such as from 0.01:1 to 0.05: 1.
  • the pyrolysis oil stream 16 is sufficiently dilute within the mixture 46 of the pyrolysis oil stream 16 and the hydrocarbon stream 20 to avoid excessive deposit formation on the particulate cracking catalyst 30, thereby avoiding impact on flow dynamics of the particulate cracking catalyst 30 within the fluid catalytic cracking unit 14, catalyst activity and selectivity, and FCC heat balance.
  • the nozzle 42 of the feed distributor 26 contemplated herein houses a portion of the pyrolysis oil feed line 32 and a portion of the hydrocarbon feed line 34, and also houses the mixing zone 22 and the spray head 44.
  • the nozzle 42 may be removable and may be attached to a main body 48 of the feed distributor 26 through a coupling ring (not shown), to thereby enable the nozzle 42 to be quickly removed for providing access to clean an interior of the feed distributor 26.
  • a coupling ring not shown
  • the nozzle 42 can be removed to enable the deposits to be cleaned from the feed distributor 26 or to enable a replacement nozzle 42 to be installed.
  • catalytically cracking the mixture 46 of the pyrolysis oil stream 16 and the hydrocarbon stream 20 in the presence of the particulate cracking catalyst 30.
  • catalytically cracking the mixture 46 of the pyrolysis oil stream 16 and the hydrocarbon stream 20 includes comingling the particulate cracking catalyst 30 and the mixture 46 of the pyrolysis oil stream 16 and the hydrocarbon stream 20 in the reaction zone 28.
  • the particulate cracking catalyst 30 is generally introduced into the reaction chamber 24 at a temperature that is sufficient to facilitate catalytic cracking of the mixture 46 of the pyrolysis oil stream 16 and the hydrocarbon stream 20, and because the hydrocarbon stream 20 is also generally provided at temperatures that facilitate catalytic cracking in the presence of the particulate cracking catalyst 30, catalytic cracking generally commences when the particulate cracking catalyst 30 is comingled with the mixture 46 of the pyrolysis oil stream 16 and the hydrocarbon stream 20. To facilitate catalytic cracking, the mixture 46 of the pyrolysis oil stream 16 and the hydrocarbon stream 20 is introduced into the reaction zone 28 within the reaction chamber 24.
  • the mixture 46 of the pyrolysis oil stream 16 and the hydrocarbon stream 20 is introduced from outside of the reaction chamber 24 into the reaction chamber 24.
  • the pyrolysis oil stream 16 and the hydrocarbon stream 20 are mixed in the mixing zone 22 of the feed distributor 26 as shown in FIGS. 2 and 3, and the mixture 46 of the pyrolysis oil stream 16 and the hydrocarbon stream 20 is introduced into the reaction chamber 24 from the mixing zone 22 in the feed distributor 26 that is outside of the reaction chamber 24.
  • the mixing zone 22 is contained in the feed distributor 26, and the mixture 45 of the pyrolysis oil stream 16 and the hydrocarbon stream 20 do not enter the reaction chamber until dispensed through the spray head 44.
  • the spray head 44 of the feed distributor 26 is disposed adjacent an inlet into the reaction chamber 24 for introducing the mixture 46 of the pyrolysis oil stream 16 and the hydrocarbon stream 20 into the reaction chamber 24.
  • the particulate cracking catalyst 30 may be introduced into the reaction chamber 24 upstream of the mixture 46 of pyrolysis oil stream 16 and the hydrocarbon stream 20 such that the particulate cracking catalyst 30 is present within the reaction chamber 24 at a location where the mixture 46 of the pyrolysis oil stream 16 and the hydrocarbon stream 20 is introduced into the reaction chamber 24.
  • the mixing zone 22 is present within the reaction chamber 24 but outside of the reaction zone 28, and the particulate cracking catalyst 30 may be introduced into the reaction chamber 24 downstream of the mixing zone 22 in the reaction chamber 24, with the mixture 46 of the pyrolysis oil stream 16 and the hydrocarbon stream 20 introduced into the reaction zone 28 separate from the particulate cracking catalyst 30.
  • the particulate cracking catalyst 30 is not present in the mixing zone 22, but is rather introduced into the reaction chamber 24 downstream of the mixing zone 22 such that the mixing zone 22 within the reaction chamber 24 is distinct from the reaction zone 28.
  • the mixture 46 of the pyrolysis oil stream 16 and the hydrocarbon stream 20 may be introduced into the reaction chamber 24 in the substantially common direction 40 in which the pyrolysis oil stream 16 and the hydrocarbon stream 20 are introduced into the mixing zone 22
  • the exemplary method includes mixing a carrier gas 52 and the pyrolysis oil stream 16 prior to mixing the pyrolysis oil stream 16 and the hydrocarbon stream 20.
  • the optional embodiment may further include mixing another carrier gas 54 and the hydrocarbon stream 20 concurrent with mixing the pyrolysis oil stream 16 and the hydrocarbon stream 20, and may further include mixing the particulate cracking catalyst 30 with a catalyst carrier gas 56 prior to catalytic cracking.
  • the carrier gases 52, 54, 56 may be FCC product gas, steam, and/or an inert gas such as nitrogen, and the carrier gases 52, 54, 56 may be the same or different.
  • the carrier gas 52 that is mixed with the pyrolysis oil stream 16 prior to mixing the pyrolysis oil stream 16 and the hydrocarbon stream 20 can also assist with maintaining the temperature of the pyrolysis oil stream 16 low to further inhibit deposit formation from the pyrolysis oil stream 16 prior to mixing with the hydrocarbon stream 20.
  • the reaction chamber 24 of the FCC unit 14 is further defined as a vertical conduit or riser 24.
  • the particulate cracking catalyst 30 is introduced into the riser 24 at a catalyst inlet 58 and the mixture 46 of pyrolysis oil stream 16 and hydrocarbon stream 20 is introduced from the spray head 44 of the feed distributor 26 that is downstream of the catalyst inlet 58.
  • the residence time of the particulate cracking catalyst 30 and the mixture 46 of the pyrolysis oil stream 16 and the hydrocarbon stream 20 in the riser 24 is generally only a few seconds.
  • General operating conditions for the reaction zone 28 in FCC units are known in the art.
  • Catalytic cracking of the mixture 46 of the pyrolysis oil stream 16 and the hydrocarbon stream 20 produces an effluent 59 that includes spent particulate cracking catalyst 76 and a gaseous component 60.
  • the gaseous component 60 includes products from the reaction in the reaction chamber 24 such as cracked hydrocarbons.
  • the spent particulate cracking catalyst 76 and the gaseous component 60 are separated.
  • the FCC unit 14 further includes a separator vessel 62 that is in fluid communication with the reaction zone 28. The separator vessel 62 separates the spent particulate cracking catalyst 76 from the effluent 59.
  • the separator vessel 62 may include a solids-vapor separation device 64, which is normally located within and at the top of the separator vessel 62.
  • the gaseous component 60 of the effluent 59 is separated from the spent particulate cracking catalyst 76 by the separator vessel 62, and the gaseous component 60 may be vented from the separator vessel 62 via a product line 66.
  • the gaseous component 60 may be compressed to obtain the upgraded fuel products, and FCC product gas that is not condensed may be recycled for use as the carrier gas 52, 54, 56 in
  • the spent particulate cracking catalyst 76 falls downward to a stripper 68 that is located in a lower part of the separator vessel 62.
  • the stripper 68 assists with removing deposited compounds from the spent particulate cracking catalyst 76 prior to further catalyst regeneration.
  • the FCC unit 14 further includes a catalyst regenerator 70 that is in fluid communication with the separator vessel 62 and that is also in fluid communication with the reaction chamber 24.
  • the spent particulate cracking catalyst 76 that is separated from the gaseous component 60 is introduced into the catalyst regenerator 70 from the stripper 68, and deposited compounds are removed from the spent particulate cracking catalyst 76 in the catalyst regenerator 70 by contacting the spent particulate cracking catalyst 76 with oxygen-containing regeneration gas.
  • the spent particulate cracking catalyst 76 is transferred to the catalyst regenerator 70 by way of a first transfer line 72 connected between the catalyst regenerator 70 and the stripper 68.
  • the catalyst regenerator 70 being in fluid communication with the reaction zone 28, passes regenerated particulate catalyst 30 to the reaction zone 28.
  • the particulate cracking catalyst 30 is continuously circulated from the reaction zone 28 to the catalyst regenerator 70 and then again to the reaction zone 28, such as through a second transfer line 74.

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

Abstract

L'invention concerne des procédés et des appareils de traitement de combustible pour améliorer un courant d'huile de pyrolyse et un courant d'hydrocarbures. Dans un mode de réalisation, un procédé d'amélioration d'un courant d'huile de pyrolyse et d'un courant d'hydrocarbures comprend : l'utilisation d'un courant d'huile de pyrolyse et l'utilisation d'un courant d'hydrocarbures séparé du courant d'huile de pyrolyse. Le courant d'huile de pyrolyse et le courant d'hydrocarbures sont mélangés dans une zone de mélange et en l'absence d'un catalyseur de craquage particulaire. Le courant d'huile de pyrolyse et le courant d'hydrocarbures sont introduits dans une direction sensiblement commune dans la zone de mélange pour former un mélange du courant d'huile de pyrolyse et du courant d'hydrocarbures. Le mélange du courant d'huile de pyrolyse et du courant d'hydrocarbures est craqué de façon catalytique en présence du catalyseur de craquage particulaire.
PCT/US2014/014806 2014-02-05 2014-02-05 Procédés et appareils de traitement de combustible pour améliorer un courant d'huile de pyrolyse et un courant d'hydrocarbures WO2015119598A1 (fr)

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Citations (3)

* Cited by examiner, † Cited by third party
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