WO2011079355A1 - Combustor de alta eficiência e processo de craqueamento catalítico fluidizado orientado para a produção de olefinas leves - Google Patents
Combustor de alta eficiência e processo de craqueamento catalítico fluidizado orientado para a produção de olefinas leves Download PDFInfo
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- WO2011079355A1 WO2011079355A1 PCT/BR2010/000297 BR2010000297W WO2011079355A1 WO 2011079355 A1 WO2011079355 A1 WO 2011079355A1 BR 2010000297 W BR2010000297 W BR 2010000297W WO 2011079355 A1 WO2011079355 A1 WO 2011079355A1
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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
- B01J29/00—Catalysts comprising molecular sieves
- B01J29/90—Regeneration or reactivation
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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
- B01J29/00—Catalysts comprising molecular sieves
- B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
- B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
- B01J29/08—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the faujasite type, e.g. type X or Y
- B01J29/084—Y-type faujasite
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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
- B01J29/00—Catalysts comprising molecular sieves
- B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
- B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
- B01J29/80—Mixtures of different zeolites
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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
- B01J38/12—Treating with free oxygen-containing gas
- B01J38/30—Treating with free oxygen-containing gas in gaseous suspension, e.g. fluidised bed
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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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- 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
- B01J8/1845—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with particles moving upwards while fluidised
- B01J8/1863—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with particles moving upwards while fluidised followed by a downward movement outside the reactor and subsequently re-entering it
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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
- B01J8/1872—Details of the fluidised bed 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
- 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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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN A CARRIER GAS OR AIR
- F23C10/00—Fluidised bed combustion apparatus
- F23C10/01—Fluidised bed combustion apparatus in a fluidised bed of catalytic particles
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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
- B01J2208/00902—Nozzle-type feeding elements
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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
- B01J2208/00938—Flow distribution elements
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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
- B01J2208/00991—Disengagement zone in fluidised-bed reactors
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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
- B01J29/00—Catalysts comprising molecular sieves
- B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
- B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
- B01J29/08—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the faujasite type, e.g. type X or Y
- B01J29/085—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the faujasite type, e.g. type X or Y containing rare earth elements, titanium, zirconium, hafnium, zinc, cadmium, mercury, gallium, indium, thallium, tin or lead
- B01J29/088—Y-type faujasite
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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
- B01J29/00—Catalysts comprising molecular sieves
- B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
- B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
- B01J29/40—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11, as exemplified by patent documents US3702886, GB1334243 and US3709979, respectively
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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
- B01J29/00—Catalysts comprising molecular sieves
- B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
- B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
- B01J29/40—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11, as exemplified by patent documents US3702886, GB1334243 and US3709979, respectively
- B01J29/405—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11, as exemplified by patent documents US3702886, GB1334243 and US3709979, respectively containing rare earth elements, titanium, zirconium, hafnium, zinc, cadmium, mercury, gallium, indium, thallium, tin or lead
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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
- C10G2300/20—Characteristics of the feedstock or the products
- C10G2300/201—Impurities
- C10G2300/202—Heteroatoms content, i.e. S, N, O, P
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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
- C10G2300/20—Characteristics of the feedstock or the products
- C10G2300/201—Impurities
- C10G2300/205—Metal content
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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
- C10G2300/708—Coking aspect, coke content and composition of deposits
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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
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/20—C2-C4 olefins
Definitions
- the present invention is in the field of processes for producing light olefins in fluidized bed catalytic cracking units and is applicable to processes in which the thermal energy produced during catalyst reactivation by coke combustion is insufficient to meet the energy demand of the coke. converter. More specifically, the present invention describes a high efficiency combustor capable of providing heat to the fluid catalytic cracking process for the production of light olefins.
- Petrochemical FCC is a fluidized bed catalytic cracking process oriented to the production of light olefins (ethylene and propylene), which has as characteristics: the use of cargo comprising low boiling hydrocarbons (diesel range), catalyst inventory highly selective, with high proportion of Pentasil family zeolite mixed with type Y zeolite, elevated reaction temperature in a riser reactor; and a quenching section 1 ⁇ 4 above the reactor load feed section.
- the coke burned in the regenerator to recover catalyst activity and generate process energy, only reaches between 5% and 20% of the total energy required, requiring continuous heat addition to the process to maintain the energy balance. of the converter.
- the process for the supply of energy is via combustion of a oil in the fluidized catalyst bed of the combustor (regenerator).
- the object of the present invention is a process in which catalyst regeneration is performed within a high efficiency combustor, the main energy source for the process, in order to avoid problems such as hot spots in the fluidized catalytic bed of the catalyst. combustion or afterburning in the diluted bed phase, which can cause irreversible catalyst deactivation and damage to internal combustion equipment.
- the cargo comprises hydrocarbons in the diesel range, whether or not added with heavy hydrocarbon residues, in addition to the generation of products such as fuel gas, LPG, cracked naphtha, light and heavy oils, with the formation of a carbonaceous deposit or coke on the catalyst surface.
- the reaction is conducted on a catalyst consisting mostly of type Y zeolite in a riser tubular reactor.
- the catalyst When significant amounts of coke are deposited on the catalyst, the catalyst loses activity and selectivity, leading to a lower yield of desired products such as LPG and cracked naphtha. Thus, at the end of cracking reactions inside the riser, the catalyst has its catalytic surface blocked by coke deposition, requiring reactivation. On the other hand, the reaction section needs energy to vaporize the liquid charge and to supply the catalytic cracking endothermic reactions.
- EP 1285042 teaches a method for introducing torch-oil and sufficient air for torch-oil combustion into an upstream transfer line, wherein the line diameter is increased to accommodate the feed rate increase. combustion air, trying to minimize the damaging results of the use of "torch-oil" directly in the regenerator.
- US Patent 7,153,479 discloses a method for removing catalyst from the effluent stream of an FCC process for the production of light olefins. Catalyst removal is preferably by the addition and recirculation of fuel oil in a cooling tower, and the flushing of the catalyst fines from the effluent gases, contemplating the recovery of the catalyst in fuel oil through the formation of a sludge (" slurry oil ").
- this slurry oil allows to supply the thermal balance of FCC units for the production of light olefins, where coke production is insufficient to maintain the thermal balance.
- the present invention relates a process for performing the complete burning of oil within a fluidized bed, in order to maintain the spent catalyst regeneration conditions and to meet the thermal demand of the conversion section of an FCC aimed at the production of light olefins. in a riser with or without a quenching section, avoiding the problems of hot spots or hot spots in the bed and afterburning in the dilute phase of the combustor and the undesirable consequences thereof.
- the present invention relates to a high efficiency combustor and a fluidized bed catalytic cracking process for the production of light olefins.
- the thermal energy produced during catalyst regeneration by coke combustion is insufficient to meet the energy demand of the converter, with spent catalyst heating and regeneration being carried out within a high efficiency combustor. , in which oil combustion is the main source of energy for the process.
- Figure 1 illustrates a process scheme for fluidized catalytic cracking or Petrochemical FCC for producing light olefins indicating the bottom and top that make up the high efficiency combustor that is part of said process.
- Figure 2 illustrates a scheme of the high efficiency combustor that makes up the Petrochemical FCC.
- Figure 3 illustrates a top view of a cross section of the lower section of the combustor containing length lances. different things.
- Figure 4 illustrates a bottom plan view of the combustor comprising several lances placed on the radial bottom of the combustor at three different height levels of the high efficiency combustor bottom.
- the present invention relates to a high efficiency combustor comprising a plurality of lances, into which a heating oil (OAQ) is injected, the combustion of which is capable of complementing the energy demand of an FCC unit.
- OAQ heating oil
- combustion of such oil is performed in such a way as to prevent the formation of hot spots concentrated within the fluidized bed of the combustor and in the afterburning phase, minimizing catalyst deactivation. and the risk of damage to internal combustion equipment.
- Another aspect of the invention is a fluid catalytic cracking process directed towards the production of light olefins, or Petrochemical FCC, wherein the reactions proceed in a larger upstream Pentasil zeolite-containing catalyst containing riser or reactor. , in admixture with type Y zeolite, whether or not exchanged with rare earths, as solid particles.
- a high efficiency combustor is employed for maintaining the thermal balance as well as promoting catalyst regeneration.
- a catalyst consisting mostly of a Pentasil family zeolite in admixture with a smaller part of type Y zeolite, having low carbon or coke content from the combustor (1), and heated to a temperature above 700 ° C, feeds the bottom of the base of a riser or riser tubular reactor (2). Above this a water vapor stream (3) is introduced to promote turbulent fluidization and dragging of the A heated stream of light hydrocarbons in the diesel range or a heavier hydrocarbon charge (4) is fed through a radial atomizer assembly using water vapor as the atomizing fluid.
- the finely dispersed filler (4) vaporizes upon contact with the catalyst initiating cracking reactions and product generation.
- a quenching or quenching fluid (5) is fed to 1 ⁇ 4 of the riser (2) above the load injection point (4).
- the product mixture and deactivated catalyst passes through a cyclone system (6) to separate the gaseous products (7) from the catalyst.
- Effluent gaseous product (7) rich in light olefins, is fed to the product recovery section and the deactivated catalyst passes through a fluidized bed (8) within a rectifier (9) below a vessel. separator (10).
- the deactivated catalyst is in countercurrent flow after water vapor injection (11) for the removal of adsorbed hydrocarbons.
- the resulting catalyst containing a reduced coke deposit slightly larger than the catalyst fed to the riser base (2) is transferred in dense phase through a spent catalyst pipe or standpipe (12a) containing a sliding control valve. circulation (13a) for the combustor (1). As shown in Figure 1 the regenerated catalyst is transferred via a regenerated catalyst standpipe (12b). This standpipe is angled outside the combustion vessel (1), and contains a sliding control valve. circulation (13b).
- the speed of the riser vapors (2) must be sufficient to ensure stable flow of the catalyst, being carried out below the load injection point (4).
- An auxiliary steam injection called carrier steam, is used to suspend the catalyst to the load inlet nozzles (4).
- carrier steam is used to suspend the catalyst to the load inlet nozzles (4).
- a quenching or rapid cooling fluid (5) is injected at a ratio of 15% to 30% of the charge mass flow (4). ), in at least one point, to create a second reaction section, aiming to favor the production of light olefins by increasing catalyst circulation and at the same time by cooling, inhibiting undesirable reactions while contributing to the flow stability. of the catalyst.
- the catalyst is reactivated by the combustion reaction of the coke with air within a turbulent flow fluidized catalytic bed (14), as shown in Figure 2.
- the heat released only by burning the coke is insufficient to maintain the combustion and heating reactions of the catalyst and to meet the thermal need of the reaction, ie the sum of the energy of the processes comprised in the heating and vaporization of the charge, the heating of the products to the reaction temperature and the endothermic heat.
- a heating oil (OAQ) is combusted within a combustor. (1).
- the combustion of the heating oil is carried out smoothly and uniformly with high efficiency, avoiding hot spots inside the fluidized bed (14) and in the afterburning phase. by minimizing catalyst deactivation and the risk of damage to internal combustion equipment (1) such as cyclones (15) and internal ducts or dip-legs (16) as shown in Figure 2.
- internal combustion equipment (1) such as cyclones (15) and internal ducts or dip-legs (16) as shown in Figure 2.
- the combustor (1) comprises a vessel with two distinct sections, a lower section (17) and another upper section (18).
- the lower section (17) comprises a turbulent fluidized catalytic bed (14), promoted by the passage of air and combustion products.
- the air supply (19) performed in the lower section (17) of the fluidized catalytic bed (14) is provided by one or more pipe-grid air distributors (21). Before being fed to the pipe-grid distributors, the air is heated by passing through an oven (20).
- the mode of operation of this bed (14) is that of turbulent fluidization regime, thus the design of the lower section (17) of the combustor (1) contemplates gas surface velocity in the range between 0.5 m / s and 1.50 m / s, preferably between 0.7 m / s and 1.30 m / s.
- the lower section (17) of the fluidized bed (14) of the combustor (1) has catalyst inventory for maintaining the residence time of the combustion gases between 4 and 10 seconds and preferably between 5 and 8 seconds.
- the upper section (18) above the fluidized bed (14) of the combustor (1) has a larger diameter (23) than that of the lower section (17), so as to reduce the solids load drawn into the cyclones (15), the upper section being designed to operate in a surface velocity range between 0,6 m / s and 1,10 m / s.
- (1) passes through a heat exchanger (25) in order to reduce the viscosity to a range of 10 Cst to 15 Cst sufficiently to achieve efficient atomization of the atomizing nozzles.
- the OAQ (24) after passing through the heat exchanger (25) is distributed through a plurality of lances (26), installed horizontally to from the periphery in the lower section (17) of the combustor vessel (1), as further illustrated in Figure 2.
- booms (26) In order to prevent the occurrence of high temperature or hot spots, a feature of the booms (26) is that they have high efficiency dispersing nozzles that operate with low spray fluid consumption (27).
- the (spray fluid) / (heating oil) ratio is calculated for a range of 15% to 30% by weight of OAQ (24).
- the spray fluid 27 used is water vapor, however, it may be replaced by another fluid, for example compressed air, without prejudice to good spray.
- the spent catalyst from the rectifier (9) is fed into the fluidized bed (14) of the combustor (1) through a catalyst distributor (28), positioned higher than the feeder booms (26). heating oil.
- the catalyst distributor (28) is designed to provide rapid dispersion of the spent coldest catalyst in the hot bed, avoiding the formation of dense and cold regions within the fluidized bed (14) of the combustor.
- Figure 3 and Figure 4 show, respectively, a section of the combustor and a plan view of the various combustor lances (26).
- the OAQ (24) is fed through a plurality of spears (26), of short (29), medium (30) and large (31) lengths.
- the process has an annular section purge fluid (32) formed between the boom (26) and a guide tube (33) (physical boom protection).
- Figure 4 illustrates a three-dimensional half-section longitudinal view of the lower section of the fluidized bed of the combustor (1), comprising lances (26) of small (29), medium (30) and large (31) lengths placed at the bottom radial portion. of the combustor (1) at two different levels (34) of high height of the high efficiency combustor (1).
- a series of cyclones (6) separates the catalyst from reaction products or gaseous products (7).
- the catalyst While promoting cracking reactions throughout the reactor, the catalyst is being deactivated by the coke deposited on it as a byproduct of the reactions.
- the deactivated catalyst is first rectified by steam injection separating volatile hydrocarbons - products that have been entrained by the catalyst.
- the coke deposited on the catalyst surface is burned, and then the regenerated catalyst is obtained, which returns to an elevated temperature to the reactor base, initiating a new process reaction cycle by contact with a new load introduced into the reactor (2).
- the present invention relates to a combustor capable of completely combustion of a heating oil within the turbulent fluidized bed (14) of a combustor (1) so as to minimize hot spot formation. -spots in (14) and afterburning reactions in the dilute phase of the upper section (18) of the combustor (1).
- heating oil feed by means of lances located on the combustor (1) of the present invention has the advantage of high simplicity in that the operation of the gas system at the reactor outlet (1) is performed independently and the operation bottom of the separating vessel (10) or rectifier (9).
- the Petrochemical FCC converter arrangement shown in Figure 1 is of the "side-by-side” type ie the separator vessel (10) with rectifier (9) and the combustor (1) are side-by-side. side by side at different elevations.
- the spent catalyst (12a) and regenerated catalyst (12b) standpipes are inclined and external to the combustion vessel (1).
- Circulation control valves which are of the slide type, or
- Slide valves (13a and 13b) are also external to the combustor (1). This type of arrangement offers the advantage of eliminating various equipment inside the combustor (1) and interfering with oil and catalyst dispersion processes.
- the flow pattern for the turbulent fluidized bed (14) in large vessels has the following characteristics: the bubble set generated by the pipegrid air distributor (21) rises at high speed. resulting in the dragging of the dense emulsion in its surroundings forming a more central region of the vessel of high ascension velocity and low density.
- dispersibility is, the ability to spread the dispersed phase in unit area per unit time from an arbitrary point of the catalyst bed.
- the dispersion is proportional to the degree of fluidization, that is, higher in regions with higher surface velocity of gases and conversely, lower in dense regions with low surface velocity.
- the OAQ (24) to be burned inside the combustor (1) is fed through a plurality of lances (26) installed in horizontal position from the periphery of the vessel, located in the lower section (17) of the fluidized catalyst bed (14). More specifically, the lances (26) are installed at elevation above the equilibrium point between coalescence and bubble breaking in the fluidized bed (14), which in the case of industrial scale unit vessels occurs at an elevation greater than 0.50 m pipe grid (21), as shown in Figure 1 and Figure 4.
- each boom (26) At the end of each boom (26) a high efficiency spray nozzle is installed and the booms (26) have different lengths to provide full distribution of the OAQ (24) sprayed along the cross section of the combustor (1) as illustrated. in Figure 3 and Figure 4.
- the lances (26) are comprised of a set of at least two concentric tubes, the inner for OAQ segregated feed (24) and the outer for OAQ sprinkler fluid (27), which in turn feed distinct sections of the boom spray nozzle (26).
- Table 1 presents an example of boom arrangements considering three different regions or distribution for a plurality of OAQ booms / nozzles (24) in a combustor (1).
- the total boom / nozzle depends on the cross-sectional area of the combustor (1), the characteristics of the fed OAQ (24) and the type of oil sprayer.
- the feed of OAQ (24) into the turbulent fluidized bed (14) occurs in the form of a small droplet haze at an elevation above the pipegrid air distributor (21), where The turbulent fluidization process is fully established.
- the spray nozzle is capable of spraying the OAQ (24) into droplets 30 to 100 micrometres in size and the spray of spray fluid and droplets exiting the spray nozzle are in the range of 30 m / s to 60 m. / s considering the bubble cross section at the end of the nozzle in contact with the fluidized bed.
- OAQ combustion (24) occurs in series reaction steps, where the first step is the fastest, and hydrocarbons are converted through a series of elemental oxidation reactions in water and carbon monoxide (CO) and thereafter, the reduction of the hydrocarbon concentration occurs at the slowest step comprising oxidation of CO to C0 2.
- the combustor (1) operates in the temperature range 700 ° C to 750 ° C and has sufficient catalyst inventory to effect total oxidation of hydrocarbons and coke to water and C0 2 within the fluidized bed (14), ensuring that the residence time of the gases within the bed (14) is longer than 5 seconds.
- the OAQ (24) to be burned in the combustor (1) is heated by passing through a heat exchanger (25) before being fed by a plurality of lances (26), maintaining the viscosity of the OAQ (24). within the spears between 5 and 30 Centistokes, preferably between 10 and 15 Centistokes, to ensure high spray efficiency.
- the lances (26) are inserted into a physical protection guide tube (33) and fed with a purge fluid (32) or cleaning in the annular region formed between the outer boom body (26) and the guide tube ( 33).
- the boom spray nozzle (26) can operate with various fluids such as water vapor or air.
- the vapor / OAQ ratio is between 0.02 and 0.50 mass / mass and preferably between 0.05 and 0.30 mass / mass.
- the combustion air of the OAQ (24) and the coke is heated by a direct combustion gas combustion furnace, which heats the air from the blower outlet temperature to between 400 ° C and 700 ° C and preferably between 550 ° C and 650 ° C before feeding the combustion air distributor (1).
- the air fed to the combustion for the combustion reactions is higher than necessary to meet the total combustion stoichiometry, ie all hydrocarbon material fed to the combustor (coke and oil) is transformed into water and carbon dioxide. carbon within the fluidized bed.
- One way of specifying the above-stoichiometric air supply for the combustion process is through the parameter "excess oxygen in the combustion gases".
- the combustion gases (22) leaving the upper section (18) of the combustor (1) to the energy recovery system therefore have an excess oxygen content of between 1% to 5.0 mole% quantified on a dry basis.
- means are provided for removing the booms while the unit is in operation, allowing replacement of the spray nozzle in the event of a failure or a drop in performance.
- the OAQ (24) to be used in the combustor (1) has low contaminants such as nitrogen and sulfur (less than 10 ppm) as well as metals (sodium, nickel, vanadium, iron), less than 1 ppm, minimizing the emission. pollutant gases and the contamination of the catalyst inventory with metals leading to loss of activity and catalytic selectivity.
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Chemistry (AREA)
- Combustion & Propulsion (AREA)
- Materials Engineering (AREA)
- Crystallography & Structural Chemistry (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- General Chemical & Material Sciences (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
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Priority Applications (4)
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JP2012545027A JP6147503B2 (ja) | 2009-12-28 | 2010-09-14 | 軽質オレフィンを製造する高性能燃焼装置及び流動接触分解方法 |
CN201080053849.5A CN102639936B (zh) | 2009-12-28 | 2010-09-14 | 高性能燃烧设备和用于生产轻石蜡的流体催化裂化工艺 |
EP10840231.4A EP2520856B1 (en) | 2009-12-28 | 2010-09-14 | High-efficiency combustion device and fluidized catalytic cracking process for the production of light olefins |
US13/511,316 US9089839B2 (en) | 2009-12-28 | 2010-09-14 | High-performance combustion device and fluid catalytic cracking process for the production of light olefins |
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BRPI0905256-9 | 2009-12-28 | ||
BRPI0905256 | 2009-12-28 |
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WO2011079355A1 true WO2011079355A1 (pt) | 2011-07-07 |
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PCT/BR2010/000297 WO2011079355A1 (pt) | 2009-12-28 | 2010-09-14 | Combustor de alta eficiência e processo de craqueamento catalítico fluidizado orientado para a produção de olefinas leves |
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US (1) | US9089839B2 (pt) |
EP (1) | EP2520856B1 (pt) |
JP (1) | JP6147503B2 (pt) |
CN (1) | CN102639936B (pt) |
WO (1) | WO2011079355A1 (pt) |
Cited By (1)
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CN116212974A (zh) * | 2021-12-03 | 2023-06-06 | 中国石油化工股份有限公司 | 一种流化催化裂化再生器以及再生方法 |
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CN105916851A (zh) | 2013-07-11 | 2016-08-31 | 艾森生物科学公司 | 嘧啶衍生物作为激酶抑制剂 |
CN104832915B (zh) * | 2015-01-30 | 2017-05-03 | 武汉凯迪工程技术研究总院有限公司 | 生物质循环流化床锅炉掺烧燃煤飞灰方法及其设备 |
US9889418B2 (en) | 2015-09-29 | 2018-02-13 | Dow Global Technologies Llc | Fluidized fuel gas combustor system for a catalytic dehydrogenation process |
CN108543501A (zh) * | 2018-05-14 | 2018-09-18 | 中国石油大学(北京) | 气固流化床反应装置 |
US11577237B2 (en) * | 2019-12-13 | 2023-02-14 | Uop Llc | Process and apparatus for regenerating catalyst with supplemental fuel |
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- 2010-09-14 US US13/511,316 patent/US9089839B2/en active Active
- 2010-09-14 JP JP2012545027A patent/JP6147503B2/ja active Active
- 2010-09-14 WO PCT/BR2010/000297 patent/WO2011079355A1/pt active Application Filing
- 2010-09-14 CN CN201080053849.5A patent/CN102639936B/zh active Active
- 2010-09-14 EP EP10840231.4A patent/EP2520856B1/en active Active
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CN116212974A (zh) * | 2021-12-03 | 2023-06-06 | 中国石油化工股份有限公司 | 一种流化催化裂化再生器以及再生方法 |
Also Published As
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JP2013515788A (ja) | 2013-05-09 |
EP2520856A1 (en) | 2012-11-07 |
US9089839B2 (en) | 2015-07-28 |
EP2520856A4 (en) | 2016-12-28 |
EP2520856B1 (en) | 2019-11-06 |
JP6147503B2 (ja) | 2017-06-14 |
US20120234727A1 (en) | 2012-09-20 |
CN102639936A (zh) | 2012-08-15 |
CN102639936B (zh) | 2016-05-04 |
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