WO2017189839A1 - New cyclic metal deactivation unit design for fcc catalyst deactivation - Google Patents
New cyclic metal deactivation unit design for fcc catalyst deactivation Download PDFInfo
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- WO2017189839A1 WO2017189839A1 PCT/US2017/029825 US2017029825W WO2017189839A1 WO 2017189839 A1 WO2017189839 A1 WO 2017189839A1 US 2017029825 W US2017029825 W US 2017029825W WO 2017189839 A1 WO2017189839 A1 WO 2017189839A1
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- vessel
- gas
- cracker
- regenerator
- catalyst
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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
- C10G25/00—Refining of hydrocarbon oils in the absence of hydrogen, with solid sorbents
- C10G25/06—Refining of hydrocarbon oils in the absence of hydrogen, with solid sorbents with moving sorbents or sorbents dispersed in the oil
- C10G25/09—Refining of hydrocarbon oils in the absence of hydrogen, with solid sorbents with moving sorbents or sorbents dispersed in the oil according to the "fluidised bed" technique
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- 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
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- 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
- B01J38/00—Regeneration or reactivation of catalysts, in general
- B01J38/04—Gas or vapour treating; Treating by using liquids vaporisable upon contacting spent catalyst
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- 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
- B01J8/0015—Feeding of the particles in the reactor; Evacuation of the particles out of the reactor
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- 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
- B01J8/1818—Feeding of the fluidising gas
- B01J8/1827—Feeding of the fluidising gas the fluidising gas being a reactant
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- 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
- B01J8/1836—Heating and cooling the reactor
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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
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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
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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
- C10G11/182—Regeneration
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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
- C10G25/00—Refining of hydrocarbon oils in the absence of hydrogen, with solid sorbents
- C10G25/12—Recovery of used adsorbent
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- 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
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00743—Feeding or discharging of solids
- B01J2208/00752—Feeding
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- 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
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00743—Feeding or discharging of solids
- B01J2208/00761—Discharging
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- 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
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00743—Feeding or discharging of solids
- B01J2208/00769—Details of feeding or discharging
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- 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
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00796—Details of the reactor or of the particulate material
- B01J2208/00893—Feeding means for the reactants
- B01J2208/0092—Perforated plates
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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
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/70—Catalyst aspects
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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
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/70—Catalyst aspects
- C10G2300/706—Catalytic metal recovery
Definitions
- the present invention relates generally to the field of fluid catalytic cracking
- FCC units e.g., reactor and regenerator devices
- the present invention relates to a cyclic metals deactivation unit system for an FCC catalyst deactivation device. More specifically still, the present invention relates to a cyclic metals deactivation unit system for an FCC catalyst deactivation device that uses separate vessels (e.g., cracker and regenerator) to crack and regenerate a catalyst within the system.
- vessels e.g., cracker and regenerator
- FCC units may be used in industrial applications for producing gasoline, middle distillate (e.g., light cycle oil (LCO)), and light petroleum gas (LPG), and additionally, for reducing the amount of residue in crude oil, converting the residue into lighter, more valuable products, such as light hydrocarbons, through the process of cracking.
- FCC catalyst deactivation devices may be used in experimental applications to reproduce the environment to which a catalyst is exposed in a commercial FCC unit.
- experiments involving catalyst deactivation aim to mimic what may occur to a catalyst in an FCC unit over a relatively long period of time (e.g., over a period of many weeks) in an accelerated amount of experimental time (e.g., over a period of many hours).
- experiments may involve FCC catalyst deactivation devices that can be used to produce a simulated equilibrium catalyst (Ecat) from fresh catalyst to match the commercial Ecat used in FCC units.
- Ecat simulated equilibrium catalyst
- Some FCC catalyst deactivation devices use a single vessel, in which a catalyst is metallated and deactivated in the one vessel where cracking and regeneration/hydrothermal deactivation conditions of an FCC process are simulated in an alternative fashion, repeatedly.
- One embodiment of the invention relates to a cyclic metals deactivation system unit for the production of equilibrium catalyst materials.
- the cyclic metals deactivation system unit includes a cracker vessel configured for cracking and stripping a catalyst material and a regenerator vessel in fluid communication with the cracker vessel, the regenerator vessel configured for regeneration and steam deactivation of the catalyst material.
- Another embodiment of the invention relates to a method of catalyst deactivation.
- the method includes cracking, by a cracker vessel, a catalyst; regenerating, by a regenerator vessel, the catalyst; distributing, by an age distribution vessel, the catalyst based at least in part on the age of the catalyst; and transporting, by one or more dip tubes, the catalyst between the cracker vessel, regenerator vessel, and age distribution vessel to deactivate the catalyst.
- FIG. 1 is a schematic diagram of a cyclic metal deactivation unit, according to an exemplary embodiment.
- FIG. 1 A is a schematic diagram of a cyclic metal deactivation unit, according to an exemplary embodiment.
- FIG. IB is a graphical representation of the operational runtime of a cyclic metal deactivation unit, according to an exemplary embodiment.
- FIG. 1C is a comparative graphical representation of the operational runtime of two cyclic metal deactivation systems, according to an exemplary embodiment.
- FIG. 2 is a cross-sectional view of a vessel in a fluidization process of FIG. 1, according to an exemplary embodiment.
- FIG. 3 is a cross-sectional view of a vessel in a gas preheating process of FIG.
- fresh catalyst denotes a catalyst that has never been exposed to reactants at reaction conditions, such as new catalyst received from a vendor.
- catalyst denotes any catalyst that has less activity at the same reaction conditions (e.g., temperature, pressure, inlet flows) than the catalyst had when it was originally exposed to the process. This can be due to a number of reasons, several non- limiting examples of causes of catalyst deactivation are coking or carbonaceous material sorption or accumulation, metals (and ash) sorption or accumulation, attrition, morphological changes including changes in pore sizes, cation or anion substitution, and/or chemical or compositional changes.
- regenerated catalyst denotes a catalyst that had become spent, as defined above, and was then subjected to a process that increased its activity, as defined above, to a level greater than it had as a spent catalyst. This may involve, for example, reversing transformations or removing contaminants outlined above as possible causes of reduced activity.
- the regenerated catalyst typically has an activity that is equal or less than the fresh catalyst activity.
- the cyclic metal deactivation system may be used to produce E-cat material in an industrial or experimental setting.
- the cyclic metal deactivation system includes a cracker vessel, a regenerator vessel, and an age distribution vessel.
- using two or more vessels for cyclic metal deactivation provides a number of advantages over conventional deactivation systems.
- using two or more vessels for cyclic metal deactivation may significantly reduce the thermal stress to each of the vessels relative to deactivation systems that use a single vessel for all steps of the deactivation process.
- the change in temperature between steps in the deactivation process requires the vessel of a conventional deactivation system to heat up and cool down between process steps.
- the repetitive change in temperature additionally results in poor sample efficiency due to long non-productive periods while the vessel is heating up and cooling down.
- the cyclic metal deactivation system of the present disclosure includes an improved fluidization homogeneity through use of a porous plate located in each of the cracker and regenerator vessels. Due to redirection of incoming gas flow the porous plate acts to improve fluidization homogeneity relative to a conventional deactivation system.
- the cyclic metal deactivation system 10 is shown as a three vessel system, having a cracker vessel 12, a regenerator vessel 14, and an age distribution vessel 16.
- the cyclic metal deactivation system 10 may include only the cracker vessel 12 and the regenerator vessel 14.
- the age distribution vessel 16 may additionally be included.
- the system 10 includes more than one regenerator vessel 14.
- the cracker vessel 12 is shown as a cylindrical vessel having a bottom 18, a fluidization chamber 22, a gas distribution chamber 24, and a porous plate 20 intermediately positioned between the fluidization chamber 22 and the gas distribution chamber 24, separating the two chambers.
- the fluidization chamber 22 may include an oil feed 30, where preheated feedstock that may consist of long-chain hydrocarbon molecules, combined with recycled slurry oil, enters the cracker vessel 12 as shown in FIG. 1.
- the oil feed 30 may feed oil into the cracker vessel 12 using a single oil injection nozzle, positioned horizontally relative to the vessel 12.
- the feedstock is shown to enter the fluidization chamber 22 near or into a material bed 26.
- the fluidization chamber 22 may be configured to vaporize and crack the feedstock into smaller molecules of vapor by contacting and mixing with a hot, powdered catalyst.
- the hydrocarbon vapors fluidize the powdered catalyst, which acts to fluidize the material bed 26.
- the gas distribution chamber 24 may include a gas feed 28, a gas redirector
- Gas may enter the gas distribution chamber 24 through the gas feed 28 and may be redirected toward the bottom 18 by the gas redirector 32.
- the gas redirector 32 may be structured to redirect incoming gas from the gas feed 28 to the bottom 18 of the gas distribution chamber 24, where the incoming gas may be distributed across the cross-sectional area of the bottom 18.
- the gas redirector 32 may be positioned at or near a vertical axis 50 of the cracker vessel 12, such that the gas may be distributed across the bottom 18 evenly.
- the porous plate 20 may be configured as a sieve plate with a plurality of apertures in the plate 20.
- the size of the apertures may be customized.
- the size of the apertures are configured to allow the particles of feedstock to pass through the apertures, while preventing the particles of catalyst from passing through the apertures.
- the porous plate 20 may separate catalyst and feedstock.
- the porous plate 20 may be structured to provide contact between any down-flowing catalyst in the fluidization chamber 22 and up-flowing gas (e.g., steam) in the gas distribution chamber 24.
- up-flowing gas e.g., steam
- the porous plate 20 may act as a stripper of the catalyst to rid the catalyst of any hydrocarbon vapors before returning the catalyst to any other components in the cyclic metal deactivation system 10 (e.g., to the regenerator vessel 14).
- the porous plate 20 may be removable and replaceable as described further herein with regard to FIG. 3.
- the cyclic metal deactivation system 10 is shown as having a dip tube 34 for each vessel.
- the one or more dip tubes 34 may be structured to pneumatically transport catalyst material between each of the vessels. Transportation of catalyst material occurs due to pressure differences and volume flow between each of the vessels. Accordingly, the vessel that is sending the catalyst material may have a higher pressure, thus having higher volume flow, than a vessel that is receiving the catalyst material. As an example, if catalyst is being transported from the cracker vessel 12 to the regenerator vessel 14, the cracker vessel 12 will be at a higher pressure at that point in the process relative to the regenerator vessel 14, causing the catalyst to flow to the regenerator vessel 14.
- the catalyst material including spent catalyst, may be sent to a regenerator vessel 14 (e.g., a regeneration unit) where the spent catalyst is regenerated by combusting any residual (e.g., remaining, left-over, etc.) carbonaceous material to produce mainly regenerated catalyst and ash residue of the combusted carbonaceous material.
- a portion of the spent catalyst may be sent back to the cracker vessel 12 without being regenerated, or may be discarded.
- An oxygen-carrying gas such as air, may be introduced into the regenerator vessel 14 to regenerate the spent catalyst and combust the remaining carbonaceous material in the regenerator vessel 14.
- the regenerator vessel 14 may be structured to burn off any deposited coke on the catalyst, supply the heat requirements of the process, and restore the catalyst's activity.
- the regenerator vessel 14 may be similar in configuration to the cracker vessel 12. Accordingly, the regenerator vessel 14 is shown as a cylindrical vessel having a bottom 18 and a porous plate 20. As shown in FIG. 1, the regenerator vessel also includes two chambers, a gas redistribution chamber 24 and a catalyst regeneration chamber 36.
- the gas redistribution chamber 24, enclosed by the bottom 18 and the porous plate 20, may be similarly configured as the gas redistribution chamber 24 in the cracker vessel 12. Accordingly, the gas redistribution chamber 24 includes a gas feed 28, a gas redirector 32, and a bottom 18. Gas may enter the gas distribution chamber 24 through the gas feed 28 and may be redirected toward the bottom 18 by the gas redirector 32.
- the catalyst regeneration chamber 36 may be structured to receive spent catalyst from other components of the cyclic metals deactivation unit 10 (e.g., from the cracker vessel 12), via the pneumatic transport system and one or more dip tubes 34, and regenerate that catalyst by burning off any deposited coke that may be deposited on the catalyst. The regenerated catalyst can then be recycled through the cyclic metals deactivation system 10 by reentering the cracker vessel 12.
- each of the cracker vessel 12 and the regenerator vessel 14 may be maintained at constant temperatures.
- the process conditions of each of the vessels may be maintained as follows.
- the cracker vessel 12 may be maintained at a maximum operating pressure of approximately 10 psi (0.7 bar) and at a maximum operating temperature of approximately 1000 F (538 C).
- the regenerator vessel 14 may be maintained at a maximum operating pressure of approximately 10 psi (0.7 bar) and at a maximum operating temperature of approximately 1650 F (899 C).
- the vessels may be maintained at different constant or variable temperatures sufficient for the processes within the cyclic metals deactivation system 10.
- the age distribution vessel 16 is shown as having a gas feed 38, a material feed 40, and a material removal 42.
- the age distribution vessel 16 additionally utilizes one or more dip tubes 34 for transport of catalyst similar to the regenerator vessel 14 and the cracker vessel 12.
- the age distribution vessel 16 may introduce catalyst to the cyclic metals deactivation system 10 through the material feed 40.
- the age distribution vessel 16 may additionally remove catalyst from the system 10 through the material removal 42.
- the age distribution vessel 16 is shown as having a top portion 44 and a bottom portion 46, wherein the catalyst existing within the system 10 is distributed within the age distribution vessel 16.
- the top portion 44 may be cylindrical in shape and the bottom portion may be conical in shape to facilitate removal of catalyst material.
- older spent catalyst may settle to the bottom portion 46 of the vessel 16, whereas fresher catalyst may be near the top portion 44 of the vessel 16.
- the bottom portion 46 may include one or more outlets, such as the material removal 42.
- the top portion 44 may include one or more inlets, such as the material feed 40.
- the catalyst may be removed through the material removal 42 and newer catalyst (e.g., fresh catalyst, regenerated catalyst, a combination thereof) replaces the older catalyst through the material feed 40 at or near the top portion 44 of the vessel 16.
- newer catalyst e.g., fresh catalyst, regenerated catalyst, a combination thereof
- the cyclic metal deactivation system 11 is shown as a five vessel system, having a cracker vessel 12, three regenerator vessels 13, 14, 15, and an age distribution vessel 16.
- the cyclic metal deactivation system 11 includes more or less than three regenerator vessels.
- the cyclic metal deactivation system 11 may include only the cracker vessel 12 and one regenerator vessel 14.
- the age distribution vessel 16 may additionally be included.
- regenerator vessels 13, 15 shown in FIG. 1A are structured similarly to the regenerator vessel 14 described with regard to FIG. 1.
- the regenerator vessels 13, 15 are structured to burn off any deposited coke on the catalyst, supply the heat requirements of the process, and restore the catalyst's activity.
- the regenerator vessels 13, 15 may be similar in configuration to the cracker vessel 12. Accordingly, the regenerator vessels 13, 15 are shown as cylindrical vessels having a bottom 18 and a porous plate 20.
- the regenerator vessels 13, 15 also include two chambers, a gas redistribution chamber 24, and a catalyst regeneration chamber 36.
- the transport of catalyst occurs similarly with two or more regenerator vessels as in the system with one regenerator vessel.
- the cyclic metal deactivation system 11 uses a dip tube 34 to pneumatically transport catalyst material between each of the vessels.
- the catalyst material including spent catalyst, is sent to the regenerator vessel 13, 14, 15 where the spent catalyst is regenerated by combusting any residual carbonaceous material to produce mainly regenerated catalyst and ash residue of the combusted carbonaceous material.
- each of the regenerator vessels 13, 14, 15 are configured to transport material (e.g., catalyst) directly to and from the cracker vessel 12, each having a separate material transport connection as shown in FIG. 1A.
- An oxygen-carrying gas such as air, may be introduced into the regenerator vessel 13, 14, 15 to regenerate the spent catalyst and combust the remaining carbonaceous material in the regenerator vessel 13, 14, 15.
- the processes e.g., regeneration, deactivation
- the processes that take place in the regenerator vessels for each cycle of the system 1 1 require significant more time to complete than the processes (e.g., cracking, stripping) that take place in the cracker vessel.
- the cracker vessel 12 may remain idle for a period of time while the catalyst is being processed by the regenerator vessel 14 in each cycle of the system 10.
- the overall operating time may additionally be decreased with use of more than one regenerator vessel. Comparing the graph for a system with one regenerator vessel (shown as "1R x 1C") to the graph for a system with three regenerator vessels (shown as "3R x 1C"), the system with three regenerator vessels takes a total of approximately four hours less in overall operating time for a 12 cycles run than the system with only one regenerator vessel. It should be understood that FIG. 1C is illustrative only and various other arrangements and/or outcomes may result from the system.
- a fluidization system 100 is shown, according to an exemplary embodiment.
- the fluidization system 100 is shown as occurring in the cracker vessel 12.
- fluidization occurs in the cracker vessel 12.
- fluidization may be performed in the regenerator vessel 14, as well as the cracker vessel 12.
- Incoming gas 102 may enter the gas redistribution chamber 24 of the cracker vessel 12 at a relatively high velocity.
- the incoming gas 102 may be redirected through the gas redirector 32 toward the bottom 18 of the chamber 24.
- the incoming gas 102 is distributed over the cross-sectional area of the cracker vessel 12 and then moves upward to contact the porous plate 20.
- the redirection of the incoming gas 102 provides a reduction in velocity of the gas 102 and results in a homogeneous distributed gas flow 104 contacting the porous plate 20.
- the gas flow 104 may then pass through the porous plate 20 and enter the fluidization chamber 22.
- a gas preheating system 200 is shown, according to an exemplary embodiment.
- the gas preheating system 200 is shown as occurring in the cracker vessel 12. Gas preheating may be performed in the cracker vessel 12 and in the regenerator vessel 14.
- the gas preheating system 200 may include a piping coil 220 positioned inside the gas distribution chamber 24.
- the gas feed 28 may be preheated inside the piping coil 220 prior to entering the gas redirector 32 for redirection and distribution of the gas.
- each of the cracker vessel 12 and the regenerator vessel 14 may include a top portion 202 and a bottom portion 204.
- the top portion 202 may include top chamber (e.g., fluidization chamber 22, catalyst regeneration chamber 36), enclosed by top chamber walls 206.
- the bottom portion 204 may include a gas distribution chamber 24 enclosed by gas distribution chamber walls 208.
- the top chamber walls 206 may be coupled to the gas distribution chamber walls 208 by one or more porous plate mounts 210 and a sealing device 212 separating the top chamber walls 206 from the porous plate mounts 210.
- the sealing device 212 is configured to seal the top portion 202 of the vessel from the bottom portion 204 of the vessel.
- the porous plate mounts 210 couple the porous plate 20 to the gas distribution chamber walls 208 and to the top chamber walls 206.
- the gas distribution chamber walls 208 may be spring mounted to the vessel bottom flange 216 by springs 214 contacting the vessel bottom flange 216.
- the gas distribution chamber walls 208 may be otherwise mounted to the vessel bottom flange 216 by any other means suitable.
- Each of the springs 214 may provide sufficient force to press the one or more porous plate mounts 210 and the sealing device 212 against the top chamber walls 206, thereby sealing the top portion 202 of the vessel from the bottom portion 204 of the vessel.
- the sealing device 212 is additionally configured to hold back material in the top chamber (e.g., fluidization chamber 22, catalyst regeneration chamber 36) of the vessel. Additional sealing is provided by the sealing of the vessel bottom flange 216. Unlike the sealing device 212, this additional sealing may provide gas sealing of the vessel bottom flange 216, containing gasses with the gas distribution chamber 24.
- the elements and assemblies may be constructed from any of a wide variety of materials that provide sufficient strength or durability, in any of a wide variety of colors, textures, and combinations. Further, elements shown as integrally formed may be constructed of multiple parts or elements.
- the word "exemplary” is used to mean serving as an example, instance or illustration. Any implementation or design described herein as "exemplary” is not necessarily to be construed as preferred or advantageous over other implementations or designs. Rather, use of the word exemplary is intended to present concepts in a concrete manner. Accordingly, all such modifications are intended to be included within the scope of the present disclosure. Other substitutions, modifications, changes, and omissions may be made in the design, operating conditions, and arrangement of the preferred and other exemplary implementations without departing from the scope of the appended claims.
- the term "coupled” means the joining of two members directly or indirectly to one another. Such joining may be stationary in nature or moveable in nature and/or such joining may allow for the flow of fluids, electricity, electrical signals, or other types of signals or communication between the two members. Such joining may be achieved with the two members or the two members and any additional intermediate members being integrally formed as a single unitary body with one another or with the two members or the two members and any additional intermediate members being attached to one another. Such joining may be permanent in nature or alternatively may be removable or releasable in nature.
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- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- General Chemical & Material Sciences (AREA)
- Combustion & Propulsion (AREA)
- Materials Engineering (AREA)
- Dispersion Chemistry (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
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Abstract
Description
Claims
Priority Applications (11)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
KR1020187034145A KR20180132931A (en) | 2016-04-29 | 2017-04-27 | Design of new circulating metal deactivation unit for FCC catalyst deactivation |
RU2018141870A RU2018141870A (en) | 2016-04-29 | 2017-04-27 | NEW DESIGN FOR THE INSTALLATION OF CYCLIC METAL DEACTIVATION FOR THE DEACTIVATION OF THE CATALYST USING A FLUIDIZED Pseudo-LIQUID CATALYST (KFK) |
JP2018556903A JP6921119B2 (en) | 2016-04-29 | 2017-04-27 | Design of a novel cyclic metal inactivating unit for FCC catalyst inactivation |
US16/096,895 US10828614B2 (en) | 2016-04-29 | 2017-04-27 | Cyclic metal deactivation unit design for FCC catalyst deactivation |
PL17790424.0T PL3448960T3 (en) | 2016-04-29 | 2017-04-27 | New cyclic metal deactivation unit design for fcc catalyst deactivation |
ES17790424T ES2939602T3 (en) | 2016-04-29 | 2017-04-27 | New Design of Cyclic Metal Deactivation Unit for FCC Catalyst Deactivation |
CN201780026173.2A CN109153922A (en) | 2016-04-29 | 2017-04-27 | New Cycle metal inactivation unit design for FCC catalyst inactivation |
BR112018072147-6A BR112018072147A2 (en) | 2016-04-29 | 2017-04-27 | new cyclic metal deactivation unit design for fcc catalyst deactivation |
EP17790424.0A EP3448960B1 (en) | 2016-04-29 | 2017-04-27 | New cyclic metal deactivation unit design for fcc catalyst deactivation |
US17/000,955 US11446624B2 (en) | 2016-04-29 | 2020-08-24 | Cyclic metal deactivation unit design for FCC catalyst deactivation |
US17/873,610 US11691116B2 (en) | 2016-04-29 | 2022-07-26 | Cyclic metal deactivation unit design for FCC catalyst deactivation |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
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US201662329374P | 2016-04-29 | 2016-04-29 | |
US62/329,374 | 2016-04-29 |
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US16/096,895 A-371-Of-International US10828614B2 (en) | 2016-04-29 | 2017-04-27 | Cyclic metal deactivation unit design for FCC catalyst deactivation |
US17/000,955 Division US11446624B2 (en) | 2016-04-29 | 2020-08-24 | Cyclic metal deactivation unit design for FCC catalyst deactivation |
Publications (1)
Publication Number | Publication Date |
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WO2017189839A1 true WO2017189839A1 (en) | 2017-11-02 |
Family
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Family Applications (1)
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PCT/US2017/029825 WO2017189839A1 (en) | 2016-04-29 | 2017-04-27 | New cyclic metal deactivation unit design for fcc catalyst deactivation |
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US (3) | US10828614B2 (en) |
EP (1) | EP3448960B1 (en) |
JP (1) | JP6921119B2 (en) |
KR (1) | KR20180132931A (en) |
CN (1) | CN109153922A (en) |
BR (1) | BR112018072147A2 (en) |
ES (1) | ES2939602T3 (en) |
PL (1) | PL3448960T3 (en) |
RU (1) | RU2018141870A (en) |
WO (1) | WO2017189839A1 (en) |
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- 2017-04-27 US US16/096,895 patent/US10828614B2/en active Active
- 2017-04-27 PL PL17790424.0T patent/PL3448960T3/en unknown
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- 2017-04-27 CN CN201780026173.2A patent/CN109153922A/en active Pending
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Also Published As
Publication number | Publication date |
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PL3448960T3 (en) | 2023-03-27 |
EP3448960A1 (en) | 2019-03-06 |
ES2939602T3 (en) | 2023-04-25 |
EP3448960B1 (en) | 2023-02-08 |
US11691116B2 (en) | 2023-07-04 |
CN109153922A (en) | 2019-01-04 |
US20190134589A1 (en) | 2019-05-09 |
BR112018072147A2 (en) | 2019-02-12 |
US20220355261A1 (en) | 2022-11-10 |
US11446624B2 (en) | 2022-09-20 |
KR20180132931A (en) | 2018-12-12 |
US20200384432A1 (en) | 2020-12-10 |
JP2019520194A (en) | 2019-07-18 |
RU2018141870A3 (en) | 2020-05-29 |
RU2018141870A (en) | 2020-05-29 |
US10828614B2 (en) | 2020-11-10 |
EP3448960A4 (en) | 2020-01-22 |
JP6921119B2 (en) | 2021-08-18 |
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