WO2020063449A1 - 石脑油催化裂解催化剂、催化裂解方法以及反应装置 - Google Patents

石脑油催化裂解催化剂、催化裂解方法以及反应装置 Download PDF

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WO2020063449A1
WO2020063449A1 PCT/CN2019/106752 CN2019106752W WO2020063449A1 WO 2020063449 A1 WO2020063449 A1 WO 2020063449A1 CN 2019106752 W CN2019106752 W CN 2019106752W WO 2020063449 A1 WO2020063449 A1 WO 2020063449A1
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Prior art keywords
section
diverter
cross
outlet
catalyst
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PCT/CN2019/106752
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English (en)
French (fr)
Inventor
李春义
张凌云
张笑毓
张颖
毛凯田
李慧
庞春天
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Hanyi Shenfei New Materials Co Ltd
Jiangsu Bosong Chemical Technology Co Ltd
Shanghai Supezet Engineering Technology Co Ltd
China University of Petroleum East China
Original Assignee
Hanyi Shenfei New Materials Co Ltd
Jiangsu Bosong Chemical Technology Co Ltd
Shanghai Supezet Engineering Technology Co Ltd
China University of Petroleum East China
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Priority claimed from CN201811135535.4A external-priority patent/CN109232153B/zh
Priority claimed from CN201910201901.XA external-priority patent/CN111715154B/zh
Priority claimed from CN201910265854.5A external-priority patent/CN111774015B/zh
Application filed by Hanyi Shenfei New Materials Co Ltd, Jiangsu Bosong Chemical Technology Co Ltd, Shanghai Supezet Engineering Technology Co Ltd, China University of Petroleum East China filed Critical Hanyi Shenfei New Materials Co Ltd
Priority to ES19867980T priority Critical patent/ES2974266T3/es
Priority to EP19867980.5A priority patent/EP3854772B1/en
Priority to US17/279,856 priority patent/US11473019B2/en
Priority to EA202100169A priority patent/EA202100169A1/ru
Publication of WO2020063449A1 publication Critical patent/WO2020063449A1/zh
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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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
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G11/14—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts
    • C10G11/18—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts according to the "fluidised-bed" technique
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J21/00—Catalysts comprising the elements, oxides, or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium, or hafnium
    • B01J21/02—Boron or aluminium; Oxides or hydroxides thereof
    • 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
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
    • B01J23/74—Iron group metals
    • B01J23/755—Nickel
    • 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
    • B01J8/005—Separating solid material from the gas/liquid stream
    • B01J8/0065—Separating solid material from the gas/liquid stream by impingement against stationary members
    • 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
    • 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
    • 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
    • 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
    • B01J8/38—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 fluidised bed containing a rotatable device or being subject to rotation or to a circulatory movement, i.e. leaving a vessel and subsequently re-entering it
    • B01J8/384—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 fluidised bed containing a rotatable device or being subject to rotation or to a circulatory movement, i.e. leaving a vessel and subsequently re-entering it being subject to a circulatory movement only
    • B01J8/388—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 fluidised bed containing a rotatable device or being subject to rotation or to a circulatory movement, i.e. leaving a vessel and subsequently re-entering it being subject to a circulatory movement only externally, i.e. the particles leaving the vessel and subsequently re-entering it
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C4/00—Preparation of hydrocarbons from hydrocarbons containing a larger number of carbon atoms
    • C07C4/02—Preparation of hydrocarbons from hydrocarbons containing a larger number of carbon atoms by cracking a single hydrocarbon or a mixture of individually defined hydrocarbons or a normally gaseous hydrocarbon fraction
    • C07C4/06—Catalytic processes
    • 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
    • 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
    • C10G2300/10—Feedstock materials
    • C10G2300/1037—Hydrocarbon fractions
    • C10G2300/1044—Heavy gasoline or naphtha having a boiling range of about 100 - 180 °C
    • 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
    • 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 application relates to the field of petrochemical industry, and in particular, to a method and a device for catalytic cracking of alkanes.
  • Hydrocarbon steam cracking has been the mainstream production technology of low-carbon olefins such as ethylene and propylene.
  • the raw materials for steam cracking are mainly light hydrocarbons such as ethane, propane, butane, and straight run naphtha.
  • heavy hydrocarbons in addition to aromatic hydrocarbons, can also be used as raw materials for steam cracking, but heavy hydrocarbons
  • coking in the cracking furnace will be more serious.
  • the content of olefins in the steam cracking feedstock must also be strictly limited. High olefin content will also accelerate the coking of cracking furnace tubes.
  • the amount of steam cracked steam is relatively large, and the mass ratio of steam to hydrocarbon is generally about 0.5.
  • the reaction temperature of steam cracking is relatively high, generally above 800 ° C. The high temperature and large amount of water vapor lead to very high energy consumption in the reaction part.
  • the present application aims to broaden the catalytic cracking reaction method of alkanes.
  • a first object of the present application is to provide a catalyst for catalytic cracking of naphtha, which has high catalytic efficiency.
  • a catalyst for catalytic cracking of naphtha including aluminosilicate, alkali metal oxide, alkaline earth metal oxide, TiO 2 , iron oxide, vanadium oxide and nickel oxide.
  • the catalyst is used for catalytic cracking of alkanes, especially for the catalytic cracking reaction of naphtha, and its catalytic effect.
  • a second object of the present application is to provide a method for catalytic cracking of naphtha.
  • the reaction temperature of catalytic cracking is significantly lower than that of the conventional steam cracking method.
  • a method for catalytic cracking of naphtha includes the following steps:
  • Naphtha undergoes a catalytic cracking reaction under the action of the aforementioned catalyst.
  • the temperature of the naphtha catalytic cracking under the above conditions can be reduced by about 100 ° C compared with the conventional cracking method.
  • a third object of the present application is to provide a method for catalytic cracking of naphtha, which can reduce or avoid coking in the reaction section.
  • a method for catalytic cracking of naphtha includes the following steps:
  • the catalyst enters the pre-riser through the regeneration inclined pipe, flows upward into the dense phase section of the reactor under the action of the pre-lifting medium, and the raw materials are sprayed into the reactor through the nozzle at the bottom of the dense phase section of the reactor in a tangential upward manner;
  • the reactor nozzle sprays tangentially along the circular cross section and at an angle of 10-90 ° to the vertical direction;
  • the catalyst enters the settler section of the regenerator. After falling into the stripping section of the settler section of the regenerator, it enters the degassing tank. After further stripping in the degassing tank, the catalyst returns to the reactor through the regeneration inclined pipe.
  • the catalyst can be rotated to reduce the stagnation zone in the dense phase section, thereby reducing or avoiding coking in the reactor.
  • a fourth object of the present application is to provide a catalyst regeneration device.
  • the gas-solid separation effect in the settler of the regeneration device is high, and the catalyst wear is reduced.
  • a catalyst regeneration device of the present application includes a regenerator reaction section and a regenerator sedimentation section.
  • the regenerator sedimentation section is located above the regenerator reaction section.
  • the exit of the regenerator reaction section is located inside the regenerator sedimentation section.
  • the area of the opening at the lower end of the cover is larger than the area of the reactor exit; the outer periphery of the bottom surface of the round table is connected to the outer circumference of the initial spin riser, or the outer periphery of the bottom surface of the round table is above the entrance of the initial spin separator Peripheral connections.
  • a catalyst regeneration device of the present application includes a regenerator reaction section and a regenerator sedimentation section.
  • the regenerator sedimentation section is connected to the regenerator reaction section.
  • the exit of the regenerator reaction section is located inside the regenerator sedimentation section for regeneration.
  • a first diverter and a second diverter are provided in the settling section of the reactor, and the first diverter and the second diverter are both located above the outlet of the reactor; the first diverter is for reducing the air velocity of the airflow discharged from the outlet of the reactor in the upward direction.
  • the assembly and the second shunt include a second shroud whose cross-sectional area gradually decreases from bottom to top. The upper and lower ends of the second shroud are both open. The first shunt is located in the second shunt.
  • the conveying separation height is greatly reduced without changing the gas volume and the diameter of the settling section of the regenerator.
  • the separation efficiency of the flue gas and the catalyst is improved.
  • FIG. 1 Schematic diagram of the naphtha catalytic cracking reaction-regeneration device of the present application
  • FIG. 2 Schematic diagram of a naphtha catalytic cracking reaction device of the present application
  • FIG. 3 Schematic diagram of the structure of the shroud and the primary splitter in the settlement section of the regenerator in Fig. 2
  • 4A-4C are cross-sectional views of the quick separation device in the regenerator settling section of the present application
  • FIG. 5 is a cross-sectional view of another rapid separation device of the regenerator settling section of the present application
  • FIG. 7 Schematic diagram of flue gas flow direction in the regenerator settling section of the present application
  • Dense phase section This section has a larger bed diameter, lower gas velocity and higher catalyst fluidization density, which is conducive to gas-solid two-phase contact and reaction.
  • Lifting section The diameter of the bed in this section is small, the gas velocity is high, and the catalyst fluidization density is low. Purpose: To increase the line speed, to make oil or gas or gas quickly leave the reactor, reduce secondary reactions of olefins; low catalyst density is also beneficial to reduce secondary reactions, especially the formation of coke; the need for catalyst transportation.
  • the "peripheral wall" of the reactor of the present application refers to the wall of the reactor parallel to the central axis of the reactor.
  • Cracking also known as cracking, refers to the process by which organic compounds are thermally decomposed and condensed to produce products with different molecular weights.
  • mass space-time refers to the ratio of the mass of the catalyst to the mass of the feed per hour.
  • apparent gas velocity is the velocity of the fluid after it has escaped from the bed material after the bed has been fluidized. It is an important operating parameter of a circulating fluidized bed.
  • the term "repose angle”, also known as the angle of repose, is the minimum angle that the inclined surface makes when the object placed on it is in a critical state sliding along the inclined surface (that is, as the inclined angle increases, the The easier it is to slide down; when the object reaches a state where it begins to slide down, the angle of this critical state is called the angle of repose).
  • oil and gas in this application is the sum of all reactants and products within the reaction device.
  • a naphtha-catalyzed cracking catalyst of the present application includes an aluminosilicate, an alkali metal oxide, an alkaline earth metal oxide, TiO 2 , iron oxide, vanadium oxide, and nickel oxide.
  • Aluminosilicates include SiO 2 and Al 2 O 3 .
  • the aluminosilicate is selected from one or more of molecular sieves, kaolin, and mullite.
  • the aluminosilicate is composed of SiO 2 or a precursor thereof, silica sol and / or a precursor of sodium silicate and Al 2 O 3 .
  • the mass percentage content of each component in the catalyst is:
  • the mass percentage of SiO 2 is 30 to 80 wt%, and the mass percentage of Al 2 O 3 is 10 to 70 wt%.
  • the mass percentage content of each component in the catalyst is respectively: the mass percentage of SiO 2 is 40-60% by weight; the mass percentage of Al 2 O 3 is 25-60% by weight.
  • the mass percentage of the alkali metal oxide is not more than 5 wt%; preferably, not more than 3 wt%.
  • the alkali metal oxide includes one or two of Na 2 O and K 2 O.
  • the mass percentage of the alkaline earth metal oxide is not more than 5 wt%; preferably, not more than 3 wt%.
  • the alkaline earth metal oxide includes one or two of CaO and MgO.
  • the mass percentage content of TiO 2 , iron oxide, vanadium oxide and nickel oxide is not more than 2 wt%, preferably, not more than 1 wt%.
  • the oxide of the sub-group metal element in the catalyst may be one or a mixture of two or more of TiO 2 , iron oxide, vanadium oxide, and nickel oxide, and all of the sub-group metal elements
  • the mass percentage content of the oxide is not more than 2 wt%, preferably, not more than 1 wt%.
  • the catalytic cracking catalyst of the present application has good thermal and hydrothermal stability, and has suitable acidity.
  • the specific surface area of the catalyst of the present application is not greater than 150m 2 / g, preferably not greater than 80m 2 / g, and having a high mechanical strength.
  • the catalytic cracking catalyst of the present application can be prepared by methods existing in the art, such as a precipitation method, an impregnation method, and a mixing method.
  • the catalyst enters the pre-riser through the regeneration inclined pipe, flows upward into the dense phase section of the reactor under the action of the pre-lifting medium, and the raw materials are sprayed into the reactor through the nozzle at the bottom of the dense phase section of the reactor through a tangential upward manner;
  • the reactor nozzle sprays tangentially along the circular cross section and at an angle of 10-90 ° to the vertical direction;
  • the catalyst in the naphtha catalytic cracking reaction adopts the catalytic cracking catalyst provided in the present application.
  • the pre-lifting medium is selected from one or more of water vapor, ethane, propane, butane, and naphtha.
  • the high-temperature catalyst first enters the pre-riser tube and contacts the pre-lifting medium in the pre-riser tube to react, and then the catalyst enters the dense phase section.
  • the temperature of the catalyst will gradually decrease.
  • the catalyst reacts with the naphtha.
  • the temperature when the catalyst enters the dense phase is lower than the temperature when it enters the pre-riser. It contacts and reacts with different hydrocarbons at different stages, so that it can meet the requirements of the reaction temperature of different raw materials.
  • the final product has low selectivity to low-carbon olefins, which can effectively reduce the production of low-value-added products such as methane.
  • the catalytic cracking method of the present application has a relatively low reaction temperature and relatively small amount of steam, so energy consumption is reduced.
  • the pre-lifting medium is water vapor and ethane.
  • the mass ratio of water vapor to ethane is between 1/20 and 1/1, preferably between 1/10 and 1/2.
  • a high-temperature catalyst for example, a temperature of about 800 ° C
  • ethane in a pre-riser reacts with ethane in a pre-riser and then enters a dense phase section, and the temperature of the catalyst can be reduced (for example, about 700 ° C), which is just satisfied with naphtha The temperature of the reaction.
  • a method for catalytic cracking of naphtha of the present application can be adjusted by changing the reaction temperature and reaction components.
  • the feedstock includes naphtha and water vapor.
  • the mass ratio of water vapor to naphtha is between 1/20 and 1/1, preferably between 1/10 and 1/2.
  • the pre-lifting medium is selected from one or more of ethane, propane, butane, and naphtha.
  • the raw materials include naphtha and water vapor, and the water vapor and hydrocarbons as the pre-lifting medium.
  • the mass ratio of the sum of matter and petroleum brain is between 1/20 and 1/1, preferably between 1/10 and 1/2.
  • the pre-lifting medium includes water vapor and hydrocarbons
  • the hydrocarbons include one or more of ethane, propane, butane, and naphtha.
  • Raw materials include naphtha.
  • the mass ratio of water vapor to the sum of the hydrocarbon substances and petroleum brain as the pre-lifting medium is between 1/20 and 1/1, and preferably between 1/10 and 1/2.
  • the average gas velocity in the dense phase section is greater than 0.25 m / s, preferably, greater than 1 m / s.
  • the average residence time of oil and gas in the dense phase is no more than 4s, preferably no more than 2s.
  • the average air velocity in the riser is greater than 3 m / s, preferably, greater than 7 m / s.
  • the average residence time in the riser is not more than 5s, preferably not more than 3s.
  • the linear velocity of the feedstock at the exit of the nozzle is greater than 5 m / s, preferably, greater than 10 m / s.
  • the catalyst can be rotated in the dense phase section to enhance the relationship between oil and gas and the catalyst. Mass transfer, heat transfer, and reaction, and thereby reduce the stagnation zone in the dense phase section, thereby reducing or avoiding coking in the reactor.
  • the device can run safely and stably for a long period of time.
  • a naphtha catalytic cracking reaction device includes:
  • the dense phase section of the reactor, the first end of the dense phase section is in communication with the pre-riser,
  • the regeneration inclined pipe communicates with the inside of the pre-rise pipe
  • the riser is in communication with the second end of the dense phase section of the reactor,
  • the settler section of the settler is in communication with the riser
  • the settler stripping section is in communication with the settler settling section
  • the inclined pipe to be born is connected with the stripper of the settler
  • the degassing tank is connected with the waiting inclined pipe and the regenerator.
  • a catalyst regeneration device includes a regenerator reaction section and a regenerator settling section.
  • the reaction section adopts any structure disclosed in the prior art. A part of the reaction section extends into the sedimentation section.
  • the settler section of the regenerator is located above the reaction section of the regenerator, and the outlet of the reaction section is located in the settling section.
  • the primary spin separator, primary spin air pipe and cover are set in the settling section.
  • the part is in the shape of a circular table.
  • the lower bottom surface of the circular table is the lower part of the cover.
  • the lower part of the cover is a cylindrical structure.
  • the area of the opening at the lower end of the cover is larger than the area of the reactor outlet.
  • the outer perimeter of the primary spiral riser is connected, or the outer periphery of the bottom surface on the circular table is connected to the outer periphery above the entrance of the primary circulator.
  • the cross section of the cylindrical structure of the lower part of the cover body perpendicular to the axial direction may be equal or different. That is, the lower part of the cover body may be a cylinder that gradually reduces its diameter from top to bottom, or a cylinder that gradually expands its diameter from top to bottom.
  • the lower portion of the cover is a cylindrical structure.
  • the primary splitter is any structure disclosed in the prior art, and generally includes a primary splitter body and a feeding leg, and the feeding leg is located below the body.
  • the outlet of the lower leg of the primary separator is lower than the outlet of the reactor.
  • the included angle ⁇ between the circular table bus of the circular table-shaped portion of the cover and the lower bottom surface is larger than the repose angle of the catalyst particles. This is to ensure that the catalyst particles falling on the cone surface can slide freely.
  • the area of the lowermost opening of the cover is greater than or equal to the area of the exit of the lifting section.
  • the area of the lowermost opening of the cover is 1.5 to 5 times, and more preferably 2 to 3 times the area of the exit of the reaction section.
  • a separator is provided outside the cover body. More than two resolvers can be set. Alternatively, two or more first-stage resolvers and two or more second-stage resolvers are provided. The cyclone provided outside the cover communicates with the gas collection chamber in the regenerator settling section through a riser pipe.
  • the outlet of the primary spiral riser is not connected to the inlet of the primary cyclone.
  • the outlet of the primary swirler and the inlet of the primary splitter are plug-in connected, and there is a gap between the tube wall of the primary swirler and the inlet of the primary splitter, which can be used for the settlement section.
  • the oil and gas inside enters the cyclone.
  • the distance between the top end of the casing in the settling section of the regenerator and the exit of the reaction section is relatively long.
  • the top of the hood is about a distance away from the height of the spinner at the exit of the reaction section.
  • the lowermost end of the hood is lower than the outlet of the reaction section. That is, the plane where the lowermost end of the cover is located is lower than the plane where the exit of the reaction section is located. It is convenient for the oil and gas discharged from the outlet of the reaction section to enter the casing, or directly into the settlement section outside the casing.
  • the regenerator settling section includes a dense phase section and a dilute phase section, and the lowermost end of the cover is higher than the interface between the thin phase section and the dense phase section, that is, the lower end of the cover is located in the settling section.
  • the lowermost end of the cover body is higher than the interface between the dilute phase section and the dense phase section by 0.5 m or more, more preferably, 1 m or more.
  • the inlet of the primary spin separator is not connected to the reactor outlet.
  • the riser outlet of the primary spin separator is at the same level as the inlet of the primary separator, or the outlet of the riser of the primary separator is higher than the inlet of the primary separator.
  • the regenerator reaction section of the present application may include a dense phase section and a lifting section. Both the lifting section and the dense phase section are of equal diameter cylindrical structure, and the diameter of the lifting section is smaller than the diameter of the dense phase section. It is also possible to separate the dense phase section and the lifting section, the reaction section is a straight pipe, and the reaction section is an equal tank.
  • the body of the primary spin separator is disposed coaxially with the reaction section.
  • the centerline of the primary spin separator body coincides with the centerline of the cover.
  • another catalyst regeneration device of the present application includes a regenerator reaction section and a regenerator settling section.
  • the settling section is connected to the reaction section.
  • the outlet of the reaction section is located inside the settling section, and a first shunt is provided in the settling section.
  • the second diverter, the first diverter and the second diverter are located above the outlet of the reaction section;
  • the first diverter is a component that reduces the air velocity in the upward direction of the air flow discharged from the outlet of the reaction section, and the second diverter includes the upper and lower two
  • the second cover body is open at both ends, and the cross-sectional diameter of the lower end opening is larger than the cross-sectional diameter of the upper end opening.
  • the first diverter is located in the second diverter.
  • At least two layers of splitter are provided in the settling section of the regenerator. Under the action of the first splitter closest to the exit of the reaction section, most of the flue gas and catalyst discharged from the exit of the reaction section directly settle into the settling section. Dense phase bed.
  • the gas is divided into two parts. One part of the gas carries part of the catalyst and flows upward along the gap between the first and the second part, and the other part flows obliquely upward from the second part.
  • the ratio of the two parts of the gas can be adjusted flexibly by adjusting the area ratio, spacing, and the size of the top outlet of the second splitter and the second splitter.
  • the first shunt is a first cover body, and the cross-sectional area of the first cover body gradually decreases from bottom to top.
  • the lowermost end of the cover body is an opening from the lower end of the cover body to the cover body.
  • the top is a continuous face.
  • the first diverter has an inverted conical structure or a spherical cap structure.
  • the area of the cross-section of the lowermost end (ie, the end closest to the reactor outlet) of the first splitter is greater than or equal to the cross-sectional area of the outlet of the reaction section.
  • the area of the cross section of the lowermost end of the first diverter is larger than the cross-sectional area of the outlet of the reaction section and is less than twice the cross-sectional area of the outlet of the reaction section.
  • the lowermost end of the first diverter is lower than the outlet of the reaction section.
  • the cross-sectional area of the annular gap formed between the outlet of the reaction section and the first diverter is less than or equal to the cross-sectional area of the outlet of the reaction section.
  • the lowermost end of the first splitter is higher than the outlet of the reaction section.
  • the cross-sectional area of the annular gap formed by the outlet of the reaction section and the lower edge of the first flow dividing member is less than or equal to the cross-sectional area of the outlet of the reaction section.
  • the first diverter is preferably an inverted conical structure, and the angle ⁇ between the cone bus bar and the bottom surface is greater than the angle of repose of the catalyst particles. This is to ensure that the catalyst particles falling on the cone surface can slide freely.
  • the first diverter includes a first cover body with a tapered structure that gradually becomes larger in cross section from bottom to top, and two cross-sections passing through the apex in the longitudinal direction of the first cover body passing through the tapered apex. Curves, the curvature of each curve increases from the top of the cone to the bottom of the cone, and then decreases.
  • the first diverter includes a first cover with a tapered structure that gradually becomes larger in cross section from bottom to top, and the tapered surface of the tapered structure gradually moves away from the cone from the apex of the cone to the bottom of the cone.
  • the shape of the centerline is curved.
  • the first diverter also includes a cavity having a tapered structure that gradually becomes larger in cross section from top to bottom.
  • the end of the cavity adjacent to the outlet of the reaction section is a bottom surface, and the end of the first cover away from the outlet of the reaction section is a bottom surface.
  • the bottom edge of the first cover body of the shape structure is connected to the bottom edge of the cavity.
  • the cross-sectional area of the lowermost end of the cavity of the first shunt member with a conical structure is larger than the cross-sectional area of the outlet of the reaction section. More preferably, the cross-sectional area of the lowermost end of the cavity with the conical structure of the first diverter is greater than the cross-sectional area of the exit of the reaction section and less than twice the cross-sectional area of the exit of the reaction section.
  • the gas is divided into two parts. One part of the gas carries part of the catalyst and flows upward along the space guided between the first part and the second part by the first part, and the other part flows obliquely upward from the outside of the second part.
  • the second flow dividing member further includes an equal-diameter guide tube, and one end of the guide tube is connected to the upper end of the cover body.
  • the diversion tube is a straight tube of equal diameter, or it may be a variable diameter tube.
  • the second shunting member is a circular truncated hood, and the end (upper bottom surface) of the circular trellis having the smallest cross section is connected to the guide tube.
  • the second diverter is a round-shaped cover, and the angle between the bus bar and the bottom surface is greater than the rest angle of the catalyst particles.
  • the second diverter is a spherical crown structure, and an outlet is provided on the spherical crown structure.
  • an outlet is provided at the uppermost end of the spherical crown structure (that is, away from the reactor outlet).
  • the outlet area of the second diverter should be designed so that the outlet air speed is less than or equal to the outlet air speed of the lifting section. That is, the cross-sectional area of the outlet of the second diverter is larger than the cross-sectional area of the outlet of the reaction section.
  • the cross-sectional area of the lowermost end of the second diverter is greater than 1.5 times the maximum cross-sectional area of the first diverter.
  • the minimum distance between the first diverter and the second diverter should be greater than the cross-sectional diameter of the outlet of the reaction section.
  • the ratio of the fluid that directly enters the sedimentation section and the fluid that continues to flow upward through the gap between the first and second diverter can be adjusted.
  • the ratio of the two shunts is preferably between 3/1 and 1/1.
  • the position of the lowermost end of the second splitter is higher than the dense phase interface of the catalyst in the sedimentation section. More preferably, the position of the lowermost end of the second splitter is at least 1 m higher than the dense phase interface of the catalyst in the sedimentation section.
  • a third diverter is also provided in the settlement section, the third diverter is located above the second diverter, and the third diverter is also a third shroud.
  • the third shroud is from bottom to top. The cross-sectional area gradually becomes smaller, and the lowermost end of the cover is an opening, and the continuous surface is from the lower end of the cover to the top of the cover.
  • the third diverter has an inverted conical structure or a spherical cap structure.
  • part of the catalyst entrained by the gas flowing upward from the outlet of the second diverter or the outlet of the diversion tube directly sinks and falls, and the other part continues to be entrained by the gas. It flows horizontally or obliquely downward to the inlet of the separator (as shown in FIG. 5). There is no upward force to balance the gravity of the catalyst, so this part of the catalyst will also naturally settle. It can be seen that the multi-layer splitter combination setting further reduces the entrainment of the catalyst by changing the flow field distribution, and promotes the sedimentation of the catalyst.
  • the cross-section of the lowermost end of the third diverter is greater than or equal to the cross-sectional area of the outlet of the second diverter.
  • the cross section of the lowermost end of the third flow dividing member is larger than or equal to the cross-sectional area of the outlet of the flow guiding tube in the second flow dividing member.
  • the lowermost end of the third diverter is lower than the exit position of the second diverter guide tube.
  • the cross-sectional area of the annular gap formed between the outlet of the diversion tube and the third diverter is greater than or equal to the cross-sectional area of the outlet of the diversion tube.
  • the cross-sectional area of the annular gap formed between the outlet of the deflector and the third diverter is larger than the cross-sectional area of the reactor outlet.
  • the lowermost end of the third diverter is higher than the exit position of the second diverter guide tube.
  • the cross-sectional area of the annular gap formed by the outlet of the diversion tube and the lower edge of the third diverter is greater than or equal to the cross-sectional area of the outlet of the diversion tube.
  • the cross-sectional area of the annular gap formed by the outlet of the deflector and the lower edge of the third diverter is larger than the cross-sectional area of the outlet of the reaction section.
  • the third diverter is preferably an inverted conical structure, and the angle ⁇ between the cone generatrix and the bottom surface is greater than the repose angle of the catalyst particles. This is to ensure that the catalyst particles falling on the cone surface can slide freely.
  • the first, second, and third shunts are respectively installed in the settlement section of the regenerator through connection methods commonly used in the art.
  • a cyclone is also provided outside the first, second, and third diverter pieces. More than two resolvers can be set. Alternatively, two or more first-stage resolvers and two or more second-stage resolvers are provided. The cyclone provided outside the cover communicates with the gas collection chamber in the settler through a riser pipe.
  • the outlet of the second splitter or the outlet of the deflector is higher than or equal to the height of the inlet of the splitter.
  • the inlets of two or more separators in the regenerator settling section are arranged close to the wall of the regenerator settling section.
  • the entrance directions of the resolvers are all oriented to a circumferential direction.
  • the entrances of the resolvers are arranged in a clockwise direction or both are arranged in a counterclockwise direction.
  • the gas in the settling section of the regenerator rotates in the same direction, which is beneficial for the catalyst suspended in the settling section to be "flipped" toward the wall of the settling section under the action of centrifugal force. And slide along the wall into the dense phase bed. The amount of catalyst entering the cyclone will be further reduced.
  • the flue gas of the present application flows into the cyclone from the upper and lower directions of the settling section. In this way, the apparent gas velocity is greatly reduced, thereby reducing the amount of catalyst carried by the upward flow of the flue gas and reducing the transport separation height (TDH).
  • TDH transport separation height
  • a 200 kg cracking catalyst was prepared by spray granulation.
  • the catalyst having good thermal and hydrothermal stability, suitable acidic, less surface area (specific surface area of not greater than 150m 2 / g, somewhat greater than 80m 2 / g), having a high mechanical strength.
  • a method for preparing light olefins from naphtha includes the following steps:
  • the catalyst enters the pre-riser through the regeneration inclined pipe, flows upward into the dense phase section of the reactor under the action of the pre-lifting medium, and the naphtha and water vapor are sprayed through the nozzle at the bottom of the dense phase section of the reactor through the tangent upward Into the reactor;
  • the reactor nozzle sprays tangentially along the circular cross section and at an angle of 10-90 ° to the vertical direction;
  • the catalyst enters the settling section of the regenerator. After falling into the regenerator stripping section, it enters the degassing tank. After further stripping in the degassing tank, the catalyst returns to the reactor through the regeneration inclined pipe.
  • the nozzle sprays at an angle of 30-60 ° to the vertical direction, and the linear velocity of the outlet is greater than 10m / s.
  • the nozzles are equidistantly arranged on the same cross section, and the number of nozzles is 2-6.
  • the catalyst includes aluminosilicate, alkali metal oxides, alkaline earth oxides, TiO 2, iron oxide, vanadium oxide and nickel oxide.
  • the mass percentage content of each component in the catalyst is:
  • the aluminosilicate includes SiO 2 and Al 2 O 3 , wherein the mass percentage of SiO 2 is 30 to 80 wt%, and the mass percentage of Al 2 O 3 is 10 to 70 wt%;
  • the alkali metal oxide includes one or two of Na 2 O and K 2 O, and the mass percentage of the alkali metal oxide is not more than 5 wt%;
  • the alkaline earth metal oxide includes one or two of CaO and MgO, and the mass percentage of the alkaline earth metal oxide is not more than 5% by weight.
  • the mass percentage content of TiO 2 , iron oxide, vanadium oxide and nickel oxide is not more than 2% by weight.
  • the pre-lifting medium is water vapor and ethane.
  • the mass ratio of water vapor to ethane is between 1/20 and 1/1.
  • the mass ratio of water vapor to naphtha is between 1/20 and 1/1.
  • the average gas velocity in the dense phase section is greater than 0.25 m / s.
  • the average residence time of oil and gas in the dense phase is no more than 4s.
  • the average air velocity in the riser should be greater than 3m / s.
  • An apparatus for implementing the method described in Embodiment 2 includes at least:
  • the dense phase section 4 of the reactor, the first end of the dense phase section is in communication with the pre-riser tube 2,
  • the regeneration inclined pipe 10 communicates with the inside of the pre-riser pipe 2,
  • the nozzle 3 is located at the bottom of the dense phase section 4 of the reactor;
  • the riser 5 is in communication with the second end of the dense phase section 4 of the reactor,
  • the settling section 7 of the settler is in communication with the riser 5,
  • the settler stripping section 8 communicates with the settler settling section 7,
  • the inclined pipe 9 is in communication with the settler stripping section 8,
  • the degassing tank 18 is connected to the waiting inclined pipe 9 and the regenerator 12.
  • the high-temperature regeneration catalyst enters the pre-riser 2 through the regeneration oblique tube 10, and flows upward into the dense phase section 4 of the reactor under the action of the pre-lifting medium 1.
  • the raw material naphtha and water vapor pass through the dense phase of the reactor.
  • Nozzle 3 at the bottom of section 4 sprays into the reactor.
  • FIG. 1 an enlarged view of a nozzle setting mode, the nozzle is tangentially cut along a circular cross section of the reactor, and is sprayed at an angle of 30-60 ° from the vertical direction.
  • the nozzle outlet linear speed should be greater than 5m / s, which promotes the rotation of the catalyst, strengthens the mass transfer, heat transfer and reaction between the oil and gas and the catalyst, and thereby reduces the stagnation zone in the dense phase section, thereby reducing or avoiding coking in the reactor. .
  • the average velocity in the dense phase section is greater than 0.25m / s; the average residence time of oil and gas in the dense phase section is not greater than 4s.
  • the oil and gas leaves the dense phase section and enters the riser 5.
  • the average gas velocity in the riser 5 is greater than 3m / s; the average residence time in the riser 5 is not greater than 5s.
  • the oil and gas 6 and catalyst leaving the riser 5 directly enter the separator in the sedimentation section 7 of the reactor.
  • the oil and gas leave the sedimentator to the separation system, and the catalyst flows out through the legs of the separator and falls.
  • the settler stripping section 8. A large amount of oil and gas is not allowed to enter the settler, the main purpose is to avoid high temperature oil and gas coking in the settler.
  • the catalyst After the catalyst is stripped by water vapor 15, it enters the regenerator 12 through the stand-by inclined pipe 9.
  • the regenerator 12 the injected air and fuel 11 are burned to heat the regenerant to a high temperature of 750-850 ° C, and at the same time, the coke on the catalyst surface is burned off.
  • the high-temperature catalyst enters the regenerator settler 13 under the impetus of the flue gas, and then falls into the regenerator stripping section. After the water vapor 17 is stripped, it enters the degassing tank 18. After further stripping with water vapor 16 in the degassing tank 18, the catalyst is returned to the reactor through the regeneration inclined pipe 10.
  • the components of naphtha (labeled No. 1) in this example are shown in Table 1.
  • the naphtha cracking reaction was performed on the fluidized bed apparatus of Example 3.
  • the catalyst regeneration temperature is 800 ° C
  • the pre-lifting medium is water vapor, which accounts for 5 wt% of the mass of naphtha.
  • the content of the oxide catalyst composition are: 51wt% SiO 2, 42wt% Al 2 O 3, 4wt% MgO, 0.5wt% Fe 2 O 3, 1.5wt% Na 2 O, 1.0wt% V 2 O 5.
  • the exit temperature of the riser reactor is controlled at 700 ° C, and the ratio of water vapor to naphtha feed quality is 1/4.
  • the average residence time of oil and gas in the dense phase of the reactor is 1.5s, and the average residence time in the riser is 1.5s. Results The yields of ethylene and propylene were 47% by weight.
  • the specific cracked product distribution is shown in Table 3.
  • Embodiment 4 The difference between this embodiment and Embodiment 4 is that the components of naphtha are different.
  • the components of naphtha (labeled No. 2) in this embodiment are shown in Table 2, and other conditions are the same as in Embodiment 4.
  • the yield of ethylene and propylene is 50.48% by weight. See Table 3 for specific cracked product distribution.
  • Example 4 The difference between this embodiment and Example 4 is that the components of naphtha are different.
  • the components of naphtha (labeled No. 2) in this embodiment are shown in Table 2.
  • the outlet temperature of the riser is increased to 750 ° C. .
  • Other conditions are the same as in Example 4.
  • the yield of ethylene and propylene is 55.20 wt%. See Table 3 for specific cracked product distribution.
  • Example 4 The difference between this embodiment and Example 4 is that the components of naphtha (labeled No. 2) in this embodiment are shown in Table 2, and the temperature at the outlet of the riser is increased to 750 ° C; Naphtha was fed with 3% by weight of ethane; ethane and water vapor were used together as a pre-lifting medium, wherein water vapor accounted for 1.5% by weight of the naphtha feed. Other conditions are the same as in Example 4. The yield of ethylene and propylene is 57.65 wt%. See Table 3 for specific cracked product distribution.
  • This embodiment is a partial structure of a catalyst regeneration device of a naphtha catalytic cracking reaction device. This is further described in detail with reference to FIGS. 2 and 3.
  • a catalyst regeneration device for catalytic cracking of naphtha includes a regeneration reactor 12 and a regeneration sedimenter 13.
  • the regeneration reactor 12 includes a dense phase section 122 and a lifting section 125.
  • the lifting section 125 extends into the regeneration sedimenter 13.
  • the regenerative settler 13 is provided with a swirling quick-splitting component, and the swirling quick-splitting component includes a primary swirler 20 and a cover body 19.
  • the primary spin splitter 20 includes a cylinder 201, an inverted cone 204, and a feeding leg 205 in order from top to bottom.
  • the inlet 202 of the primary spin splitter 20 is provided on the upper portion of the cylinder 201, and the airflow from the inlet 202 enters the primary splitter 20 in a tangential direction.
  • a gas riser 203 is provided on the top of the primary cyclone 20 and communicates with the primary cyclone 20, and the oil, gas or smoke entering the primary cyclone 20 is discharged through the gas riser 203.
  • the cover body 19 includes two parts, the upper part is a circular table shape, and the lower part is a cylindrical shape.
  • the cover body may be integrally formed.
  • the edge of the upper end of the cover body 19 (that is, the upper bottom surface of the circular table) is connected to the outer periphery of the air lift pipe 203, and the primary splitter 20 is placed in the cover body.
  • the lower end surface of the cover body 19 is lower than the exit of the lifting section 125, and the lower end surface of the cover body 19 is located in the lean phase section of the settler.
  • the included angle between the bus-shaped upper portion of the cover 19 and the lower bottom surface is larger than the rest angle of the catalyst particles. That is, the included angle of the circular table is related to the angle of repose of the catalyst particles used, which can ensure that the catalyst flows downward.
  • the cross-sectional area of the opening at the lower end of the cover 19 is larger than the cross-sectional area of the exit of the dilute phase conveying section 125.
  • the center lines of the cylindrical body 201, the inverted cone body 204, the cover body 19, and the regeneration reactor 12 of the primary spin splitter 20 coincide.
  • the exit of the feeding leg should be far away from the exit of the lifting section 125, that is, the exit of the feeding leg cannot be far from the exit of the lifting section 125, otherwise, the catalyst of the primary spinner 20 is not conducive to the upward air flow of the lifting section 125. Discharge from the unloading leg.
  • the inlet 202 of the primary splitter 20 and the outlet of the lifting section 125 are not connected.
  • a space other than the cover body 19 is further provided with a separator 21 and a plenum 22.
  • two sets of resolvers are provided.
  • Each set of resolvers includes a primary resolver 211 and a secondary resolver 212.
  • the secondary resolver 212 communicates with the gas collection chamber 22 through a riser pipe.
  • the inlet of the first-stage splitter 211 is at the same level as the inlet 202 of the primary splitter 20, or the inlet of the first-stage splitter 211 is slightly lower than the inlet 202 of the primary splitter 20.
  • This embodiment is another embodiment of a partial structure of a catalyst regeneration device for catalytic cracking of naphtha. This will be further described in detail with reference to Figures 4-7.
  • a catalyst regeneration device for catalytic cracking of naphtha includes a regeneration reactor 12 and a regeneration sedimenter 13.
  • the regeneration reactor 12 includes a dense phase section and a lifting section 125.
  • the lifting section 125 extends into the regeneration sedimenter 13.
  • the settler 13 includes a swirling quick-separating component 23.
  • the swirling-quick-swiping component 23 includes a first diverter 231, a second diverter 232, and further includes a third diverter 233.
  • the first, second and third splitter are located above the outlet of the regeneration reactor.
  • the swirling fast-separating component can also achieve the fast-separating effect of the flue gas and the catalyst of the present application when only the first partial flow 231 and the second partial flow element 232 are included.
  • the third diverter 233 is included, the separation effect achieved by the third diverter 233 is better.
  • the first diverter 231 may be a conical first cover as shown in FIG. 4A, or a spherical cap-shaped first cover as shown in FIG. 4B. It may also be a first cover with a structure as shown in FIG. 4C.
  • the first diverter 231 shown in FIG. 4C is composed of two parts, the upper part is a conical structure, and the lower part is a first cover body which gradually expands in diameter from bottom to top.
  • the longitudinal section of the first cover body passing through its center line is The two curves passing through the vertex that are bent away from the central direction, the curvature of the curve increases first and then decreases from bottom to top.
  • the bottom edge of the lowermost end of the conical structure of the upper part is connected to the periphery of the uppermost end of the lower part.
  • the upper and lower parts can also be integrally formed.
  • the second diverter 232 includes a circular truncated structure and a flow guide tube 621, and the flow guide tube 621 is connected to the circular truncated structure at least in cross section, or the flow guide tube 621 is integrated with the circular truncated structure Forming a second shunt member 232.
  • the first diverter 231 is located inside the second diverter 232.
  • the shape of the third diverter 233 is similar to that of the first diverter 231.
  • the shapes of the first and third diverter pieces may be the same or different.
  • the first diverter 231 has a spherical crown structure
  • the third diverter 233 may have a conical structure.
  • the angle between the conical generatrix of the first and third diverter pieces (231, 233) and the bottom surface is greater than the rest angle of the catalyst particles. That is, the angle of the cone shape is related to the angle of repose of the catalyst particles used, which can ensure that the catalyst flows downward.
  • the cross-sectional area of the lower end is greater than or equal to the outlet of the lifting section 125 of the regeneration reactor.
  • Cross-sectional area Preferably, the cross-sectional area of the lowermost end of the first diverter is larger than the cross-sectional area of the outlet of the lifting section 125 of the regeneration reactor, and is less than twice the cross-sectional area of the lifting section 125 of the reactor.
  • the cross-sectional area of the lowermost end of the upper part of the conical structure is larger than the cross-sectional area of the exit section of the lifting section 125 of the regeneration reactor, and smaller than the lifting section 125 of the regeneration reactor. 2 times the cross-sectional area.
  • the lowermost end of the first splitter 231 is higher than the exit of the lifting section 125 of the regeneration reactor.
  • the cross-sectional area of the annular gap formed by the exit of the lifting section 125 of the regeneration reactor and the lower 231 edge of the first splitter is smaller than or equal to the cross-sectional area of the exit of the lifting section 125 of the regeneration reactor.
  • the lower end of the first splitter 231 may be lower than the exit of the lifting section 125 of the regeneration reactor.
  • the cross-sectional area of the annular gap formed between the exit of the lifting section 125 of the regeneration reactor and the first splitter (The shaded part of FIG. 5) is smaller than or equal to the cross-sectional area of the outlet of the lifting section 125 of the regeneration reactor.
  • the maximum cross-sectional area of the circular truncated structure of the second diverter 232 is greater than 1.5 times the cross-sectional area of the lowermost end of the first diverter 231.
  • the minimum distance between the gaps between the first diverter 231 and the second diverter 232 should be larger than the cross-sectional diameter of the exit of the lifting section 125 of the regeneration reactor.
  • the cross-section of the lowermost end of the third diverter 233 is greater than or equal to the cross-sectional area of the outlet of the deflector 621 in the second diverter 232.
  • the lowermost end of the third diverter is higher than the exit position of the second diverter guide tube.
  • the cross-sectional area of the annular gap formed by the outlet of the diversion tube and the lower edge of the third diverter is greater than or equal to the cross-sectional area of the outlet of the diversion tube.
  • a cyclone 21 is provided inside the settler 13 and outside the cyclone fast-splitting assembly 23, and includes at least two first-stage cyclones 211 and at least two second-stage cyclones 212.
  • the splitter 222 communicates with the plenum 22 through a riser pipe.
  • the inlet of the primary splitter 211 is at the same level as the inlet of the second diverter 232 diversion tube 621, or the inlet of the primary splitter 211 is slightly lower than the inlet of the diversion tube 621. As shown in FIG.
  • a plurality of resolvers are evenly arranged along the circumferential direction of the settler 13, and the entrances of the first-stage resolvers 211 are arranged near the wall of the settler 13, and the entrances 24 of all the resolvers 211 are oriented on the circumference. Set counterclockwise.

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Abstract

一种石脑油催化裂解的方法，石脑油在催化剂作用下催化裂解，催化剂包括硅铝酸盐、碱金属氧化物、碱土金属氧化物、TiO 2、铁氧化物、钒氧化物和镍氧化物。另一方面，在催化裂解反应装置的沉降器内设有快分组件，在不改变气量、沉降器直径的情况下，大幅度的降低了输送分离高度。另外，油气和催化剂的分离效率提高。

Description

石脑油催化裂解催化剂、催化裂解方法以及反应装置 技术领域
本申请涉及石油化工领域，具体的，涉及烷烃催化裂解的方法以及装置。
背景技术
烃类蒸汽裂解，一直是乙烯、丙烯等低碳烯烃的主流生产技术。蒸汽裂解的原料主要有乙烷、丙烷、丁烷和直馏石脑油等轻质烃类，理论上来讲重质烃类，除了芳烃以外，也可以用作蒸汽裂解的原料，但重质烃类进行蒸汽裂解，裂解炉结焦会比较严重。此外，烯烃在蒸汽裂解原料中的含量也必须严格限制，烯烃含量高，也会加速裂解炉管的结焦。蒸汽裂解水蒸汽的用量都比较大，一般水蒸汽/烃的质量比在0.5左右。此外，蒸汽裂解的反应温度都比较高，一般在800℃以上。温度高、水蒸汽用量大，导致反应部分的能耗非常高。
蒸汽裂解是热反应，多年来，研究人员一直希望借助催化反应来降低反应温度和水蒸汽的用量。从文献的公开报道来看，无论是催化剂还是反应器，研究人员都提出了多种解决方案。譬如，蒸汽裂解与催化裂解相结合的方法，或者对催化裂解的方法进行改性。
本申请旨在拓宽烷烃的催化裂解反应方法。
概述
一方面，本申请的第一个目的，提供一种石脑油催化裂解的催化剂，该催化剂的催化效率高。
一种石脑油催化裂解的催化剂，包括硅铝酸盐、碱金属氧化物、碱土金属氧化物、TiO 2、铁氧化物、钒氧化物和镍氧化物。
该催化剂用于烷烃催化裂解，尤其用于石脑油催化裂解反应中，其催化效果。
另一方面，本申请的第二个目的，提供一种石脑油催化裂解的方法，在方法中，催化裂解的反应温度比传统的蒸汽裂解方法中反应温度显著降低。
一种石脑油催化裂解的方法，包括以下步骤：
石脑油在上述催化剂的作用下进行催化裂解反应。
在上述条件下进行的石脑油催化裂解的温度比传统的裂解方法可降低100℃左右。
本申请的第三个目的，提供一种石脑油催化裂解的方法，该方法可以减少或者避免了在反应段内结焦。
一种石脑油催化裂解的方法，包括以下步骤：
S1：催化剂经再生斜管进入预提升管，在预提升介质的作用下向上流动进入反应器密相段，原料经位于反应器密相段底部的喷嘴通过切线向上的方式喷入反应器；
反应器喷嘴沿着横截面圆环切向并与垂直方向呈10-90°角喷射；
S2：离开提升管的油气和催化剂进入反应装置的沉降器，油气离开沉降器去分离系统，催化剂经旋风分离器的料腿流出后落入沉降器的汽提段；
S3：催化剂汽提后经待生斜管进入再生器，在再生器内对催化剂进行加热；
S4：催化剂进入再生器沉降段，落入再生器沉降段的汽提段后进入到脱气罐，在脱气罐内进一步汽提后，催化剂经再生斜管返回反应器。
通过反应器内的进料喷嘴的设置方式，可以推动催化剂旋转，减少在密相段内的滞留区，从而减少或避免了在反应器内结焦。
本申请的第四个目的，提供一种催化剂再生装置。该再生装置的沉降器内的气固分离效果高，且催化剂磨损降低。
本申请的一种催化剂再生装置，包括再生器反应段和再生器沉降段，再生器沉降段位于再生器反应段上的上方，再生器反应段的出口位于再生器沉降段内部，再生器沉降段内设置初旋分器、初旋升气管以及罩体；罩体包括上下两部分，罩体的上部分呈圆台状，圆台的下底面为罩体的下部分，罩体的下部分呈圆筒状结构；罩体最下端的开口的面积大于反应器出口的面积；圆台上底面的外圆周边与初旋升气管的外周连接，或者圆台上底面的外圆周边与初旋分器的入口以上的外周连接。
另一方面，本申请的一种催化剂再生装置，包括再生器反应段和再生器沉降段，再生器沉降段与再生器反应段相连通，再生器反应段的出口位于再生器沉降段内部，再生器沉降段内设有第一分流件、第二分流件，第一分流件和第二分流件均位于反应器的出口上方；第一分流件为降低反应器出口排出的气流向上方向气速的组件，第二分流件包括横截面的面积从下到上逐渐变小的第二罩体，第二罩体的最上端、最下端均为开口，第一分流件位于第二分流件内。
在本申请的催化剂再生装置中，在不改变气量、再生器沉降段直径的情况下，大幅度的降低了输送分离高度。另外，烟气和催化剂的分离效率提高。
附图说明
图1本申请的石脑油催化裂解反应-再生装置示意图
图2本申请的石脑油催化裂解反应装置示意图
图3附图2中的再生器的沉降段内的罩体与初旋分器结构示意图
图4A-4C是本申请的再生器沉降段内的快速分离装置的剖面图
图5本申请的再生器沉降段的另一种快速分离装置的剖面图
图6本申请的再生器沉降段内的俯视图
图7本申请的再生器沉降段内的烟气流向示意图
具体实施方式
为了更好的理解本申请的发明内容，下面将结合本申请具体实施方式、实施例以及附图，对本申请的技术方案进行清楚、完整地描述，以下实施方式用于说明本申请，但不用来限制本申请的范围。
下列实施例中未注明具体条件的实验方法，通常按照常规条件或按照制造厂商所建议的条件。除非另外说明，否则所有的百分数、比率、比例、或份数按重量计。
密相段：该段床层直径较大，气速较低，催化剂流化密度较高，有利于气固两相的接触和反应。
提升段：该段床层直径较小，气速较高，催化剂流化密度较低。目的：线速度提高，使油气或者烟气快速离开反应器，减少烯烃的二次反应；催化剂密度低，也 有利于减少二次反应，尤其是焦炭的生成；催化剂输送的需要。
本申请的反应器的“周壁”是指与反应器中心轴平行的反应器的器壁。
裂解又称裂化系指有机化合物受热分解和缩合生成相对分子质量不同的产品的过程。
术语“质量空时”是指催化剂的质量与每小时的进料质量之比。
术语“表观气速”为当床层流态化后流体逸出床层物料后的速度。它是循环流化床一个重要的操作参数。
术语“安息角”，亦作休止角，是斜面使置于其上的物体处于沿斜面下滑的临界状态时，与水平表面所成的最小角度(即随着倾斜角增加，斜面上的物体将越容易下滑；当物体达到开始下滑的状态时，该临界状态的角度称为休止角)。
术语“油气”在本申请中反应装置内的所有反应物以及产物的总和。
除非另行定义，文中所使用的所有专业与科学用语与本领域熟练人员所熟悉的意义相同。此外，任何与所记载内容相似或均等的方法及材料皆可应用于本申请方法中。文中所述的较佳实施方法与材料仅作示范之用。
一方面，本申请的一种石脑油催化裂解的催化剂，包括硅铝酸盐、碱金属氧化物、碱土金属氧化物、TiO 2、铁氧化物、钒氧化物和镍氧化物。
硅铝酸盐包括SiO 2和Al 2O 3。硅铝酸盐选自分子筛、高岭土、莫来石中的一种或几种。或者硅铝酸盐是由SiO 2或其前身物硅溶胶和/或硅酸钠与Al 2O 3的前身物组成。
在一种实施方式中，催化剂中各组分的质量百分比含量分别为：
SiO 2的质量百分比为30～80wt％，Al 2O 3的质量百分比为10～70wt％。
在某些实施方式中，催化剂中各组分的在质量百分比含量分别为：SiO 2的质量百分比为40～60wt％；Al 2O 3的质量百分比为25～60wt％。
在某些实施方式中，碱金属氧化物的质量百分比不大于5wt％；优选，不大于3wt％。所述的碱金属氧化物包括Na 2O、K 2O中的一种或两种。
在某些实施方式中，碱土金属氧化物的质量百分比不大于5wt％；优选，不大于3wt％。所述的碱土金属氧化物包括CaO、MgO中的一种或两种。
在某些实施方式中，TiO 2、铁氧化物、钒氧化物和镍氧化物的质量百分比含量不大于2wt％，优选，不大于1wt％。
在本申请中，所述的催化剂中的副族金属元素的氧化物可以为TiO 2、铁氧化物、钒氧化物和镍氧化物中的一种或者两种以上的混合，所有副族金属元素的氧化物的质量百分比含量不大于2wt％，优选，不大于1wt％。
本申请的催化裂解的催化剂具有良好的热和水热稳定性，具有适宜的酸性。另一方面，本申请的催化剂的比表面积不大于150m 2/g，最好不大于80m 2/g，且具有较高的机械强度。
本申请的催化裂解的催化剂可以采用本领域现有的方法进行制备，譬如沉淀法、浸渍法、混合法。
另一方面，一种石脑油催化裂解的方法，
S1：催化剂经再生斜管进入预提升管，在预提升介质的作用下向上流动进入反 应器密相段，原料经位于反应器密相段底部的喷嘴通过切线向上的方式喷入反应器；
反应器喷嘴沿着横截面圆环切向并与垂直方向呈10-90°角喷射；
S2：离开提升管的油气和催化剂进入反应装置的沉降器，油气离开沉降器去分离系统，催化剂经旋风分离器的料腿流出后落入沉降器的汽提段；
S3：催化剂汽提后经待生斜管进入再生器，在再生器内对催化剂进行加热；
S4：催化剂进入再生器沉降段，落入再生器汽提段后进入到脱气罐，在脱气罐内进一步汽提后，催化剂经再生斜管返回反应器。
在石脑油催化裂解反应中的催化剂采用本申请提供的催化裂解催化剂。
在某些实施方式中，预提升介质选自水蒸汽、乙烷、丙烷、丁烷和石脑油中的一种或几种。
本申请的石脑油催化裂解的方法，高温催化剂先进入预提升管内、且与预提升管内的预提升介质接触反应，随后催化剂进入密相段。在催化剂预提升管向上运动进入密相段的过程中，催化剂温度会逐渐降低。在密相段内，在催化剂与石脑油接触反应。催化剂进入密相段时的温度低于进入预提升管时的温度，在不同阶段与不同的烃类物质接触反应，如此可以满足不同原料的反应温度的要求。最终产物低碳烯烃的选择性高，可以有效减少甲烷等低附加值产物的生成。
与蒸汽裂解相比，本申请的催化裂解方法反应温度相对较低，蒸汽用量相对较少，因此能耗降低。
在某些实施方式中，预提升介质是水蒸汽和乙烷。水蒸汽与乙烷的质量比在1/20～1/1之间，最好在1/10～1/2之间。
在该实施方式中，高温催化剂(譬如温度为约800℃)与乙烷在预提升管内反应，随后进入密相段内，催化剂的温度可减低(譬如约700℃)，恰好满足于石脑油反应的温度。
本申请的石脑油催化裂解的方法。乙烯/丙烯比可通过改变反应温度和反应组分来进行调整。
在某些实施方式中，原料包括石脑油和水蒸气。水蒸汽与石脑油的质量比在1/20～1/1之间，最好在1/10～1/2之间。
在某些实施方案中，预提升介质选自乙烷、丙烷、丁烷和石脑油的一种或者几种，原料包括石脑油和水蒸气，且水蒸气与作为预提升介质的烃类物质和石油脑之和的质量比在1/20～1/1之间，最好在1/10～1/2之间。
在某些实施方案中，预提升介质包括水蒸汽和烃类物质，烃类物质包括乙烷、丙烷、丁烷和石脑油中的一种或几种。原料包括石脑油。水蒸气与作为预提升介质的烃类物质和石油脑之和的质量比在1/20～1/1之间，最好在1/10～1/2之间。
在某些实施方式中，密相段内的平均气速大于0.25m/s，优选，大于1m/s。
油气在密相段内平均停留时间不大于4s，优选不超过2s。
在某些实施方式中，在步骤S2中，提升管内的平均气速要大于3m/s，优选，大于7m/s。在提升管内的平均停留时间不大于5s，优选不大于3s。
在某些实施方案中，原料在喷嘴的出口处的线速度大于5m/s，优选，大于10m/s。
在喷嘴沿密相段的横截面圆环切向、并与垂直方向呈10～90°，且出口线速度大 于5m/s时，在密相段内可以推动催化剂旋转，强化油气与催化剂间的传质、传热和反应，并由此减少在密相段内的滞流区，从而减少或避免反应器内结焦。装置可以长周期安全稳定运行。
第三方面，一种石脑油催化裂解的反应装置，包括：
预提升管，
反应器的密相段，密相段的第一端与所述预提升管相连通，
再生斜管，与所述预提升管内相连通，
喷嘴，位于所述反应器密相段的底部；
提升管，与所述反应器的密相段的第二端相连通，
沉降器沉降段，与所述提升管相连通，
沉降器器汽提段，与所述的沉降器器沉降段相连通，
待生斜管，与沉降器汽提段相连通，
脱气罐，与所述待生斜管和再生器相连接。
提升管截面直径小于反应器的密相段截面直径。第四方面，一种催化剂再生装置，包括再生器反应段以及再生器沉降段。反应段采用现有技术所公开的任一结构。反应段的一部分伸入到沉降段内。
再生器沉降段位于再生器反应段上的上方，反应段的出口位于沉降段内，沉降段内设置初旋分器、初旋升气管以及罩体；罩体包括上下两部分，罩体的上部分呈圆台状，圆台的下底面为罩体的下部分，罩体的下部分呈圆筒状结构；罩体最下端的开口的面积大于反应器出口的面积；圆台上底面的外圆周边与初旋升气管的外周连接，或者圆台上底面的外圆周边与初旋分器的入口以上的外周连接。
罩体的下部分圆筒状结构与轴向方向垂直的横截面可以是相等也可以不等。即罩体的下部分可以是从上到下逐渐缩径的圆筒，也可以是从上到下逐渐扩径的圆筒。优选，罩体的下部分为圆柱状结构。
初旋分器为现有技术公开的任一种结构，通常包括初旋分器本体以及下料腿，下料腿位于本体的下方。
在一实施方式中，初旋分器的下料腿的出口低于反应器的出口。优选的，
在一实施方式中，罩体的圆台状部分的圆台母线和下底面的夹角θ大于催化剂颗粒的安息角。如此，以确保落在锥面上的催化剂颗粒能自由滑落。
在某些实施方式中，罩体最下端开口的面积大于等于提升段出口的面积。优选的，罩体最下端开口的面积为反应段出口的面积的1.5～5倍，更优选2～3倍。
本申请的再生器沉降段内，在罩体之外，还设有旋分器。可以设置两个以上的旋分器。或者设置两个以上的一级旋分器，以及两个以上的二级旋分器。在罩体外设置的旋分器的通过升气管与再生器沉降段内的集气室连通。
在某些实施方式中，初旋升气管的出口不与一级旋分器的入口相连。
在某些实施方式，初旋升气管的出口与一级旋分器的入口承插式连接，初旋升气管与一级旋分器入口两者的管壁之间有空隙，可以供沉降段内的油气进入旋分器内。
在本申请中，再生器沉降段内的罩体的顶端距反应段出口的距离比较远。在某 些情况下，罩体的顶端距反应段出口的距离大约一个旋分器高度的距离。另外，在圆台状下方还有圆柱形的部分。从反应段出口排出的油气，一部分油气从罩体下端开口边缘流入沉降段；另一部分油气进入罩体内，通过初旋分离器的入口直接进入沉降段的上部。这样，与油气全部进入沉降段向上流动的情况相比，本申请的油气从沉降段上、下两个方向流入旋分器，如此，表观气速降低很多，从而减少了油气向上流动携带的催化剂量、并降低了输送分离高度(TDH)。
在某些实施方式中，在再生器沉降段内，罩体的最下端低于反应段出口。也就是，罩体最下端所在的平面低于反应段出口所在的平面。便于反应段出口排出的油气既可以进入罩体内，也可以直接进入罩体外的沉降段内。
在某些实施方式中，再生器沉降段包括密相段和稀相段，罩体的最下端高于稀相段和密相段之间的分界面，即，罩体的最下端位于沉降段的稀相段内。优选的，罩体的最下端高于稀相段和密相段之间的分界面0.5m以上，更优选，在1m以上。
在某些实施方式中，初旋分离器的入口不与反应器出口相连。
在某些实施方式中，初旋分离器的升气管出口与一级旋分器入口处于同一水平面上，或者初旋分离器的升气管出口高于一级旋分器入口。
本申请的再生器反应段可以包括密相段和提升段，提升段和密相段均为等径圆筒结构，且提升段的直径小于密相段的直径。也可以不分密相段和提升段，反应段为直管，反应段为等经的罐体。
在某些实施方式，初旋分离器的本体与反应段同轴设置。初旋分离器本体的中心线与罩体的中心线重合。
如果只依靠惯性分离，在再生器反应段的出口采用简单的快分结构，催化剂与烟气的分离效率不高。进入旋分器的烟气中的催化剂浓度偏高，会加剧催化剂的磨损。
此外，在旋分器分离效率不变的情况下，进入旋分器的气体中催化剂含量越低，催化剂损耗就越低。因此，烟气与催化剂的初分效率，直接影响着催化剂的损耗。
除了本申请公开技术特征，其他烷烃催化裂解反应装置所采用的结构或者部件可以采用现有技术所公开的内容和结构，以保证上述反应顺利的进行。
可替代的，本申请另一种的催化剂再生装置，包括再生器反应段和再生器沉降段，沉降段与反应段相连通，反应段的出口位于沉降段内部，沉降段内设有第一分流件和第二分流件，第一分流件和第二分流件均位于反应段的出口上方；第一分流件为降低反应段出口排出的气流向上方向气速的组件，第二分流件包括上下两端均开口的第二罩体，且下端开口的截面直径大于上端开口的截面直径，第一分流件位于第二分流件内。
在本申请中，再生器沉降段内至少设有两层分流件，在最靠近反应段出口的第一分流件作用下，从反应段出口排出的烟气和催化剂大部分直接沉降进入沉降段的密相床。气体被分为两部分，一部分气体携带部分催化剂沿第一分流件与第二分流件之间的空隙向上流动，另一部分则从第二分流件外斜向上流动。这两部分气体的比例可以通过调整第一分流件与第二分流件底部面积比、间距和第二分流件顶部出口的大小来灵活调整。
在某些实施方式中，第一分流件为第一罩体，第一罩体从下到上的横截面积逐渐变小，罩体的最下端为开口，从罩体的最下端到罩体顶部为连续的面。
优选，第一分流件为倒圆锥状结构、或者为球冠结构。
在某些实施方式中，第一分流件的最下端(即最靠近反应器出口的端部)横截面的面积大于或者等于反应段出口的截面积。优选，第一分流件最下端的横截面的面积大于反应段出口的截面积，且小于反应段出口的截面积的2倍。
在一实施方式中，第一分流件的最下端低于反应段出口。优选的，反应段出口与第一分流件之间构成的环隙的横截面积小于等于反应段出口的截面积。
在另一实施方式中，第一分流件的最下端高于反应段出口。优选的，反应段出口与第一分流件下缘构成的环隙截面积小于等于反应段出口的截面积。
在某些实施方式中，第一分流件优选为倒圆锥状结构，圆锥母线和底面的夹角θ大于催化剂颗粒的安息角。如此，以确保落在锥面上的催化剂颗粒能自由滑落。
在一实施方式中，第一分流件包括从下向上横截面逐渐变大的锥形结构的第一罩体，在第一罩体的经过锥形顶点纵向方向上截面上呈经过顶点的两条曲线，各曲线的曲率从锥形顶点到锥形底边先增大，然后曲率再减少。
在另一实施方式中，第一分流件包括从下向上横截面逐渐变大的锥形结构的第一罩体，锥形结构的锥形面从锥形顶点到锥形底边逐渐向远离锥形中心线的方向弯曲。
进一步，第一分流件还包括从上向下横截面逐渐变大的呈锥形结构的腔体，腔体临近反应段出口的一端为底面，第一罩体远离反应段出口一端为底面，锥形结构的第一罩体底边与腔体底边相连接。
优选的，第一分流件呈锥形结构的腔体的最下端的横截面积大于反应段出口的截面积。更有选，第一分流件呈锥形结构的腔体的最下端的横截面积大于反应段出口的截面积、且小于反应段出口的截面积的2倍。
反应段出口排出的烟气和催化剂经如图2C所示的第一分流件作用后，大部分催化剂被阻挡进入沉降段的密相床。气体被分为两部分，一部分气体携带部分催化剂沿经第一分流件引导进入第一分流件与第二分流件之间的空隙向上流动，另一部分则从第二分流件外斜向上流动。
在某些实施方式中，第二分流件还包括等径的导流管，导流管的一端与罩体的上端开口连接。优选，导流管为一段等径的直管，也可以为变径的导管。
在某些实施方式中，第二分流件为圆台状罩体，圆台的横截面最少的一端(上底面)与导流管连接。
第二分流件为圆台状罩体，母线和下底面的夹角大于催化剂颗粒的安息角。
在某些实施方式中，第二分流件为球冠状结构，在球冠状结构上设有出口。优选的，在球冠状结构的最上端(即远离反应器出口)处设有出口。
第二分流件的出口面积以出口气速应小于等于提升段出口气速设计。即，第二分流件出口截面积大于反应段出口的截面积。
在某些实施方式中，第二分流件的最下端的横截面积大于第一分流件最大横截面积的1.5倍。
在某些实施方式中，第一分流件和第二分流件之间的最小间距应大于反应段出口的横截面直径。
通过控制或者改变第一、第二分流件之间的间距，可以调整直接进入沉降段的流体和通过第一、二分流件两者间的间隙继续向上流动的流体的比例(分流比)。优选的，两种分流的比例最好在3/1～1/1之间。
另外，第二分流件的最下端的位置高于沉降段内催化剂稀密相界面。更优选，第二分流件的最下端的位置至少高于沉降段内催化剂稀密相界面1m。
在某些实施方式中，沉降段内还设有第三分流件，第三分流件位于第二分流件的上方，第三分流件也为第三罩体，第三罩体从下到上的横截面积逐渐变小，罩体的最下端为开口，从罩体的最下端到罩体顶部为连续的面。
优选，第三分流件为倒圆锥状结构、或者为球冠结构。
从第二分流件出口或者导流管出口向上流动的气体所夹带的催化剂，在第三分流件的作用下，一部分直接沉降下落，另一部分继续被气体夹带，然而从此处出来的气体，总体上是水平或斜向下向旋分器入口流动(如附图5所示)，没有向上的力来平衡催化剂所受的重力，因而这部分催化剂也会自然沉降。由此可见，多层分流件组合设置通过改变流场分布，进一步减少催化剂的夹带，促进催化剂的沉降。
在某些实施方式中，第三分流件最下端的横截面大于或者等于第二分流件出口的截面积。或者第三分流件最下端的横截面大于或者等于第二分流件中导流管出口的截面积。
在某些实施方式中，第三分流件的最下端低于第二分流件导流管出口位置。优选的，导流管出口与第三分流件之间构成的环隙的横截面积大于等于导流管出口的截面积。优选的，导流管出口与第三分流件之间构成的环隙的横截面积大于反应器出口的截面积。
在另一实施方式中，第三分流件的最下端高于第二分流件导流管出口位置。优选的，导流管出口与第三分流件下缘构成的环隙截面积大于等于导流管出口的截面积。优选的，导流管出口与第三分流件下缘构成的环隙截面积大于反应段出口的截面积。
在某些实施方式中，第三分流件优选为倒圆锥状结构，圆锥母线和底面的夹角θ大于催化剂颗粒的安息角。如此，以确保落在锥面上的催化剂颗粒能自由滑落。
本申请中第一、第二、第三分流件分别通过本领域常用的连接方式将其分别安装在再生器的沉降段内。
本申请的再生器沉降段内，在第一分流件、第二分流件以及第三分流件的外部，还设有旋分器。可以设置两个以上的旋分器。或者设置两个以上的一级旋分器，以及两个以上的二级旋分器。在罩体外设置的旋分器的通过升气管与沉降器内的集气室连通。
在某些实施方式中，第二分流件出口或者导流管的出口高于或者等于旋分器入口的高度。
在某些实施方式中，在再生器沉降段内的两个以上旋分器的入口均靠近再生器沉降段的器壁的方式设置。优选的，旋分器的入口方向均朝向一个圆周方向，譬如 旋分器的入口都是朝向顺时针方向或者均朝向逆时针方向设置。
通过本申请的这种设置旋分器的方式，整个再生器沉降段内的气体都向同一方向旋转，有利于悬浮于沉降段内的催化剂在离心力的作用下被“甩”向沉降段器壁，并沿器壁下滑进入密相床。进一步将减少了进入旋分器内的催化剂的量。
本申请的烟气从沉降段上、下两个方向流入旋分器，如此，表观气速降低很多，从而减少了烟气向上流动携带的催化剂量、并降低了输送分离高度(TDH)。
下面结合具体附图以及具体实例进一步说明：
实施例1
采用喷雾造粒法制备200kg裂解催化剂。
将去离子水143kg、拟薄水铝石(酌减35wt％)96kg加入到搅拌釜中，在不断搅拌的情况下加入68％浓硝酸8kg进行混合，呈凝胶状。再加入硅溶胶(固含量40wt％)310kg、碳酸钠1.5kg、碳酸钙3.5kg、硝酸镍0.5kg、硝酸铁1.1kg。继续搅拌1h后，喷雾造粒。得到的催化剂，经700℃焙烧后，得到成品备用。
上述催化剂具有良好的热和水热稳定性，适宜的酸性，表面积不大(比表面积不大于150m 2/g，有些不大于80m 2/g)，具有较高的机械强度。
实施例2
在本实施例中，一种石脑油制备低碳烯烃的方法，包括如下步骤：
S1：催化剂经再生斜管进入预提升管，在预提升介质的作用下向上流动进入反应器密相段，石脑油和水蒸气经位于反应器密相段底部的喷嘴通过切线向上的方式喷入反应器；
反应器喷嘴沿着横截面圆环切向并与垂直方向呈10-90°角喷射；
S2：离开提升管的油气和催化剂进入反应装置的沉降器，油气离开沉降器去分离系统，催化剂经旋风分离器的料腿流出后落入沉降器的汽提段；
S3：催化剂汽提后经待生斜管进入再生器，在再生器内对催化剂进行加热；
S4：催化剂进入再生器的沉降段，落入再生器汽提段后进入到脱气罐，在脱气罐内进一步汽提后，催化剂经再生斜管返回反应器。
在S1中，喷嘴与垂直方向呈30-60°角喷射，出口线速度大于10m/s。
喷嘴在同一截面等距布置，喷嘴个数为2-6个。
催化剂包括硅铝酸盐、碱金属氧化物、碱土金属氧化物、TiO 2、铁氧化物、钒氧化物和镍氧化物。
催化剂中各组分的质量百分比含量分别为：
硅铝酸盐包括SiO 2和Al 2O 3，其中，SiO 2的质量百分比为30～80wt％，Al 2O 3的质量百分比为10～70wt％；
所述的碱金属氧化物包括Na 2O、K 2O中的一种或两种，碱金属氧化物的质量百分比不大于5wt％；
所述的碱土金属氧化物包括CaO、MgO中的一种或两种，碱土金属氧化物的质量百分比不大于5wt％。
TiO 2、铁氧化物、钒氧化物和镍氧化物的质量百分比含量不大于2wt％。
S1中，预提升介质是水蒸汽和乙烷。水蒸汽与乙烷的质量比在1/20～1/1之间。
S1中，水蒸汽与石脑油的质量比在1/20～1/1之间。
S1中，密相段内的平均气速大于0.25m/s。
S1中，油气在密相段内平均停留时间不大于4s。
S2中，提升管内的平均气速要大于3m/s。
实施例3
一种实现实施例2所述方法的装置，至少包括：
预提升管2，
反应器的密相段4，密相段的第一端与所述预提升管2相连通，
再生斜管10，与所述预提升管2内相连通，
喷嘴3，位于所述反应器密相段4的底部；
提升管5，与所述反应器的密相段4的第二端相连通，
沉降器沉降段7，与所述提升管5相连通，
沉降器汽提段8，与所述的沉降器沉降段7相连通，
待生斜管9，与沉降器汽提段8相连通，
脱气罐18，与所述待生斜管9和再生器12相连接。
利用该装置生产低碳烯烃的具体步骤为：
如图1所示，高温再生催化剂经再生斜管10进入预提升管2，在预提升介质1的作用下向上流动进入反应器密相段4，原料石脑油和水蒸气经反应器密相段4底部的喷嘴3喷入反应器。参考附图1中，喷嘴设置方式的放大图，喷嘴沿反应器横截面圆环切向，并与垂直方向呈30-60°角喷射。喷嘴出口线速度要大于5m/s，由此推动催化剂旋转，强化油气与催化剂间的传质、传热和反应，并由此减少密相段内的滞留区，从而减少或避免反应器内结焦。密相段内的平均其速度大于0.25m/s；油气在密相段内的平均停留时间不大于4s。油气离开密相段，进入提升管5，提升管5内的平均气速要大于3m/s；在提升管5内的平均停留时间不大于5s。离开提升管5的油气6和催化剂，直接进入反应器沉降段7内的旋分器，经两到三级分离后，油气离开沉降器去分离系统，催化剂经旋分器的料腿流出，落入沉降器汽提段8。不允许大量油气进入沉降器，主要目的是避免高温油气在沉降器内结焦。催化剂经水蒸气15汽提后，经待生斜管9进入再生器12。在再生器12内，喷入的空气和燃料11燃烧将再生剂加热到750-850℃的高温，同时烧除催化剂表面焦炭。高温催化剂在烟气的推动下进入再生器沉降器13，再落入再生器汽提段，进水蒸汽17汽提后，进入到脱气罐18内。在脱气罐18内进一步用水蒸气16汽提后，催化剂经再生斜管10返回反应器。
实施例4
本实施例中的石脑油(标记为No.1)的组分如表1所示，利用实施例3的流化床装置上进行石脑油裂解反应。
其中该方法中，催化剂再生温度800℃，预提升介质为水蒸气，占石脑油质量的5wt％。催化剂中氧化物的组成含量分别为：51wt％SiO 2，42wt％Al 2O 3，4wt％MgO，0.5wt％Fe 2O 3，1.5wt％Na 2O，1.0wt％V 2O 5。提升管反应器出口温度控制在700℃，水蒸气与石脑油进料质量之比1/4。油气在反应器密相段的平均停留时间为1.5s，在提 升管内的平均停留时间为1.5s。结果乙烯和丙烯的收率为47wt％，具体的裂解产物分布如见表3所示。
采用现有技术蒸汽法裂解的方式裂解同样的石脑油，乙烯和丙烯的收率为43wt％左右。
表1.实施例4的石脑油No.1的组成，wt％
Figure PCTCN2019106752-appb-000001
实施例5
本实施例5与实施例4的不同之处在于，提升管出口温度提高到750℃，其他条件与实施例4相同。乙烯和丙烯的收率为52.32wt％，具体的裂解产物分布如见表3
实施例6
本实施例与实施例4的不同之处在于，石脑油的组分不同，本实施例的石脑油(标记为No.2)组分如见表2，其他条件如同实施例4。乙烯和丙烯的收率为50.48wt％，具体的裂解产物分布如见表3。
表2.实施例6的石脑油No.2组成，wt％
Figure PCTCN2019106752-appb-000002
实施例7
本实施例与实施例4的不同之处在于，石脑油的组分不同，本实施例的石脑油(标记为No.2)组分如见表2，提升管出口温度提高到750℃。其他条件如同实施例4。乙烯和丙烯的收率为55.20wt％，具体的裂解产物分布如见表3。
实施例8
本实施例与实施例4的不同之处在于，本实施例的石脑油(标记为No.2)组分如见表2，提升管出口温度提高到750℃；进料中混入质量为石脑油进料3wt％的乙烷；乙烷和水蒸气共同作为预提升介质，其中，水蒸气占石脑油进料的1.5wt％。其他条件如同实施例4。乙烯和丙烯的收率为57.65wt％，具体的裂解产物分布如见表3。
表3.石脑油催化裂解产物分布，wt％
Figure PCTCN2019106752-appb-000003
实施例9
本实施例为石脑油催化裂解反应装置的催化剂再生装置的部分结构。结合如附图2、图3进一步具体说明。
如图2所示，石脑油催化裂解的催化剂再生装置包括再生反应器12和再生沉降器13。再生反应器12包括密相段122和提升段125，提升段125伸入再生沉降器13内。
再生沉降器13内设有旋流快分组件，所述的旋流快分组件包括初旋分器20和罩体19。如图3所示，初旋分器20从上到下依次包括圆柱体201、倒椎体204以及下料腿205，初旋分器20的入口202设在圆柱体201的上部，气流从入口202沿着切向方向进入初旋分器20内。在初旋分器20的顶部设有升气管203，且与初旋分器20相通，将进入初旋分器20内的油气或烟气经升气管203排出。罩体19包括两部分，上部分为圆台状，下部分为圆柱体状，罩体可以是一体成型。罩体19的上端(即圆台的上底面)边缘与升气管203的外周连接，将初旋分器20至于罩体内。罩体19的下端面低于提升段125出口，且罩体19的下端面位于沉降器的稀相段内。
罩体19的圆台状上部的母线与下底面的夹角大于催化剂颗粒的安息角。也就是说，圆台的夹角大小根据使用的催化剂颗粒的安息角有关，可以保证催化剂向下流 动。
罩体19下端的开口横截面积大于稀相输送段125出口的横截面积。
在本实施例中，初旋分器20的圆柱体201、倒椎体204、罩体19以及再生反应器12的各中心线相重合。下料腿的出口要远离提升段125的出口，也就是说，下料腿的出口不能远离提升段125的出口，否则，初旋分器20的催化剂由于受到提升段125向上的气流，不利于从下料腿排出。
在本实施例中，初旋分器20入口202与提升段125的出口不连接。
在沉降器13内，罩体19之外的空间还设有旋分器21、以及集气室22。在本实施例中，设有两套旋分器，每套旋分器包括一级旋分器211、二级旋分器212，二级旋分器212通过升气管与集气室22连通。一级旋分器211的入口与初旋分器20的入口202在同一水平面，或者一级旋分器211的入口略低于初旋分器20的入口202。
实施例10
本实施例为石脑油催化裂解的催化剂再生装置的部分结构的另一种实施方式。结合如附图4-7进一步具体说明。
如图2所示石脑油催化裂解的催化剂再生装置包括再生反应器12和再生沉降器13。再生反应器12包括密相段和提升段125，提升段125伸入再生沉降器13内。
沉降器13内包括旋流快分组件23，所述的旋流快分组件23包括第一分流件231、第二分流件232，进一步还包括第三分流件233。第一、二、三分流件均位于再生反应器出口上方。
旋流快分组件在仅包括第一分流231和第二分流件232也可以达到本申请烟气与催化剂的快分的效果。在包括第三分流件233的情况下，其达到的分离效果更好。
第一分流件231可以为如图4A所示的圆锥形第一罩体，也可以为如图4B所示的球冠形的第一罩体。还可以为如图4C所示结构的第一罩体。在图4C所示的第一分流件231由两部分组成，上部分为圆锥形结构，下部分为从下向上逐渐扩径的第一罩体，第一罩体经过其中心线的纵截面为经过顶点的两条向远离中心性方向弯曲的曲线，曲线的曲率从下到上先增加后减小。上部分圆锥形结构的最下端底边与下部分的最上端的周边相连接。上下两部分也可以是一体成型的。
如图4A,4B,4C所示，第二分流件232包括圆台状结构和导流管621，导流管621与圆台状结构的最少横截面连接，或者导流管621与圆台状结构为一体成型形成第二分流件232。第一分流件231位于第二分流件232内部。
第三分流件233的形状与第一分流件231结构相类似。第一、三分流件的形状可以是相同，也可以是不同。譬如，第一分流件231为球冠状结构，第三分流件233可以取圆锥形结构。
第一、三分流件(231,233)的圆锥形的母线与下底面的夹角大于催化剂颗粒的安息角。也就是说，圆锥形的夹角大小根据使用的催化剂颗粒的安息角有关，可以保证催化剂向下流动。
第一分流件231如果为锥形形或者球冠形结构的第一罩体，其最下端(即最靠近反应器出口的端部)横截面的面积大于或者等于再生反应器的提升段125出口的截面积。优选，第一分流件最下端的横截面的面积大于再生反应器的提升段125出 口的截面积，且小于反应器提升段125的截面积的2倍。
当第一分流件231为如图4C所示的结构，其上部分圆锥形结构的最下端的横截面积大于再生反应器的提升段125出口的截面积，且小于再生反应器的提升段125的截面积的2倍。
在本实施例中，第一分流件231的最下端高于再生反应器的提升段125出口。再生反应器的提升段125出口与第一分流件下231缘构成的环隙截面积小于或者等于再生反应器的提升段125出口的截面积。
也可以第一分流件231的最下端低于再生反应器的提升段125出口，如图5所示，再生反应器的提升段125出口与第一分流件之间构成的环隙的横截面积(附图5的阴影部分)小于或者等于再生反应器的提升段125出口的截面积。
在本实施例中，第二分流件232的圆台状结构的最大横截面积大于第一分流件231最下端横截面积的1.5倍。第一分流件231和第二分流件232之间空隙的最小间距应大于再生反应器的提升段125出口的横截面直径。
在本实施例中，第三分流件233最下端的横截面大于或者等于第二分流件232中导流管621出口的截面积。第三分流件的最下端高于第二分流件导流管出口位置。优选的，导流管出口与第三分流件下缘构成的环隙截面积大于等于导流管出口的截面积。
在本实施例中，在沉降器13内、旋流快分组件23外部设有旋分器21，包括至少两个一级旋分器211和至少两个二级旋分器212，二级旋分器222通过升气管与集气室22连通。一级旋分器211的入口与第二分流件232导流管621的的入口在同一水平面，或者一级旋分器211的入口略低于导流管621的的入口。如图7所示，在第二分流件232导流管621向上流动的夹带催化剂的气体，在第三分流件233作用下，一部分直接沉降下落，另一部分催化剂随着气体从第三分流件下方流出，气体总体上呈水平或斜向下向旋分器入口流动，催化剂在没有向上的作用力存在的情况下自然沉降。
如图6所示，多个旋分器均匀沿着沉降器13圆周方向设置，且一级旋分器211的入口靠近沉降器13器壁设置，所有旋分器211的入口24在圆周上朝向逆时针方向设置。
本申请做了详尽的描述，其目的在于让熟悉本领域的技术人员能够了解本申请的内容并加以实施，并不能以此限制本申请的保护范围，凡根据本申请的精神实质所做的等效变化或修饰，都应涵盖在本申请的保护范围内。

Claims (21)

  1. 一种石脑油催化裂解的方法，
    S1：催化剂经再生斜管进入预提升管，在预提升介质的作用下向上流动进入反应器密相段，包含石脑油的原料经位于反应器密相段底部的喷嘴通过切线向上的方式喷入反应器；
    反应器喷嘴沿着横截面圆环切向并与垂直方向呈10-90°角喷射；优选的，呈30-60°角喷射；
    S2：离开提升管的油气和催化剂进入反应装置的沉降器，油气离开沉降器去分离系统，催化剂经旋风分离器的料腿流出后落入沉降器的汽提段；
    S3：催化剂汽提后经待生斜管进入再生器，在再生器内对催化剂进行加热；
    S4：催化剂进入再生器的沉降段，落入再生器沉降段的汽提段后进入到脱气罐，在脱气罐内进一步汽提后，催化剂经再生斜管返回反应器。
  2. 根据权利要求1所述的方法，其中，所述的催化剂包括硅铝酸盐、碱金属氧化物、碱土金属氧化物、TiO 2、铁氧化物、钒氧化物和镍氧化物。
  3. 根据权利要求1或2所述的方法，其中，在步骤S1，预提升介质选自水蒸汽、乙烷、丙烷、和丁烷中的一种或几种；
    优选的，预提升介质为水蒸汽和乙烷，水蒸汽与乙烷的质量比在1/20～1/1之间，更优选在1/10～1/2之间。
  4. 根据权利要求1-3任一项所述的方法，其中，在步骤S1中，原料包括石脑油和水蒸气，水蒸汽与石脑油的质量比在1/20～1/1之间，更优选在1/10～1/2之间。
  5. 根据权利要求2所述的方法，其中，催化剂中各组分的质量百分比含量分别为：碱金属氧化物的质量百分比不大于5wt％；优选，不大于3wt％；
    碱土金属氧化物的质量百分比不大于5wt％；优选，不大于3wt％。
  6. 根据权利要求2或5所述的方法，其中，TiO 2、铁氧化物、钒氧化物和镍氧化物的质量百分比含量不大于2wt％，优选，不大于1wt％。
  7. 根据权利要求1-6任一项所述的方法，其中，再生器包括：
    包括再生器反应段以及再生器沉降段，再生器反应段包括密相段和提升段，密相段的出口连接提升段的入口，再生器反应段的提升段的出口位于再生器沉降段内，
    沉降段内设置初旋分器、初旋升气管以及罩体；罩体包括上下两部分，罩体的上部分呈圆台状，圆台的下底面以下为罩体的下部分，罩体的下部分呈圆筒状结构；罩体最下端的开口的面积大于反应段出口的面积；圆台上底面的外圆周边与初旋升气管的外周连接，或者圆台上底面的外圆周边与初旋分器的入口以上的外周连接。
  8. 根据权利要求7所述的方法，其中，初旋分器包括初旋分器本体以及下料腿，下料腿位于本体的下方，罩体的圆台状部分的上底面的边缘与初旋分器的入口以上的外周连接；
    优选的，初旋分器本体的顶部设有初旋升气管，且与初旋分器本体连通，罩体的圆台状部分的上底面的边缘与初旋分器的升气管的外周连接。
  9. 根据权利要求7或8所述的方法，其中，罩体的圆台状部分的圆台母线和下 底面的夹角θ大于催化剂颗粒的安息角。
  10. 根据权利要求7-9任一项所述的方法，其中，罩体最下端开口的面积大于等于提升段的出口的面积；
    优选的，罩体最下端开口的面积为反应段出口的面积的1.5～5倍；
    更优选，罩体最下端开口的面积为反应段出口的面积的2～3倍。
  11. 根据权利要求7-10任一项所述的方法，其中，在再生器沉降段内，罩体的最下端低于反应段的提升管的出口；
    优选的，沉降段包括密相段和稀相段，罩体的最下端位于沉降段的稀相段内。
  12. 根据权利要求7-11任一项所述的方法，其中，初旋分器的下料腿的出口低于反应段的提升管的出口；其中，沉降段的轴向方向上，下料腿的出口与提升管的出口无重叠部分。
  13. 根据权利要求1-6任一项所述的方法，其中，所述的再生器包括再生器反应段和再生器沉降段，再生器沉降段与再生器反应段相连通，再生器反应段的出口位于再生器沉降段内部，再生器沉降段内设有第一分流件和第二分流件，第一分流件和第二分流件均位于反应段的出口上方；第一分流件为降低反应段出口排出的气流向上方向气速的组件，第二分流件包括上、下两端均开口的第二罩体，且下端开口的截面积大于上端开口的截面积，第一分流件位于第二分流件内；
    优选的，第二分流件为圆台状的第二罩体；或者第二分流件为球冠状结构的第二罩体，在球冠状结构上设有出口。
  14. 根据权利要求13所述的方法，其中，第一分流件为第一罩体，第一罩体从下到上的横截面积逐渐变小，第一罩体只有最下端为开口。
    优选，第一分流件为倒圆锥状结构、或者为球冠结构。
    更优选，第一分流件为倒圆锥状结构，圆锥母线和底面的夹角θ大于催化剂颗粒的安息角；
    最优选，第一分流件和第二分流件之间间隙的最小间距大于反应段出口的横截面直径。
  15. 根据权利要求13或14所述的方法，其中，第一分流件靠近反应段出口的端部的横截面积大于或者等于反应段出口的截面积；
    优选，第一分流件靠近再生器反应段出口的端部的横截面积大于反应段出口的截面积，且小于反应段出口的截面积的2倍。
  16. 根据权利要求13所述的方法，其中，第一分流件包括从下向上横截面逐渐变大的锥形结构的第一罩体，在第一罩体经过锥形顶点纵向方向上的截面上为经过顶点的两条曲线，各曲线的曲率从锥形顶点到锥形底边先增大，然后曲率再减少；
    优选的，第一分流件还包括从上向下横截面逐渐变大的呈锥形结构的腔体，腔体临近反应段出口的一端为底面，第一罩体远离反应段出口一端为底面，锥形结构的第一罩体底边与腔体底边相连接。
  17. 根据权利要求13-16任一项所述的方法，其中，第二分流件还包括导流管，导流管的一端与第二罩体的上端开口连接；
    优选，导流管为一段等径的直管，或者为为变径的导管；
    更有选的，第二分流件的最下端的横截面积大于第一分流件最大横截面积的1.5倍。
  18. 根据权利要求14-17任一项所述的方法，其中，在沉降器内还设有第三分流件，第三分流件位于第二分流件的上方，第三分流件为从下到上的横截面积逐渐变小的第三罩体，第三罩体只有最下端为开口；
    优选，第三分流件为倒圆锥状结构、或者为球冠结构；
    更有选，第三分流件为倒圆锥状结构，圆锥母线和底面的夹角θ大于催化剂颗粒的安息角。
  19. 根据权利要求18所述的反应装置，其中，第三分流件最下端的横截面大于或者等于第二分流件出口的截面积；
    优选的，第三分流件的最下端低于第二分流件导流管出口位置；更有选，导流管出口与第三分流件之间构成的环隙的横截面积大于等于导流管出口的截面积；最优选的，导流管出口与第三分流件之间构成的环隙的横截面积大于反应段出口的截面积；
    或者，优选，第三分流件的最下端高于第二分流件导流管出口位置；更优选的，导流管出口与第三分流件下缘构成的环隙截面积大于等于导流管出口的截面积；最优选的，导流管出口与第三分流件下缘构成的环隙截面积大于反应段出口的截面积。
  20. 一种石脑油催化裂解的方法，包括：
    包含石脑油的原料在催化剂的作用下，在反应器进行催化裂解反应，反应器的出口温度在700-750℃之间。
    其中，所述的催化剂包括硅铝酸盐、碱金属氧化物、碱土金属氧化物、TiO 2、铁氧化物、钒氧化物和镍氧化物。
  21. 根据权利要求21所述的方法，其中，TiO 2、铁氧化物、钒氧化物和镍氧化物的质量百分比含量不大于2wt％，优选，不大于1wt％。
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