WO2022268151A1 - 流化床反应器和制备低碳烯烃的装置以及制备低碳烯烃的方法 - Google Patents

流化床反应器和制备低碳烯烃的装置以及制备低碳烯烃的方法 Download PDF

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WO2022268151A1
WO2022268151A1 PCT/CN2022/100672 CN2022100672W WO2022268151A1 WO 2022268151 A1 WO2022268151 A1 WO 2022268151A1 CN 2022100672 W CN2022100672 W CN 2022100672W WO 2022268151 A1 WO2022268151 A1 WO 2022268151A1
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distributor
catalyst
raw material
fluidized bed
bed reactor
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PCT/CN2022/100672
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English (en)
French (fr)
Inventor
宗弘元
齐国祯
高攀
李晓红
曹静
俞志楠
王艳学
彭飞
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China Petroleum and Chemical Corp
Sinopec Shanghai Research Institute of Petrochemical Technology
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China Petroleum and Chemical Corp
Sinopec Shanghai Research Institute of Petrochemical Technology
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Priority to BR112023026372A priority Critical patent/BR112023026372A2/pt
Priority to AU2022297494A priority patent/AU2022297494A1/en
Priority to US18/566,128 priority patent/US20240246052A1/en
Publication of WO2022268151A1 publication Critical patent/WO2022268151A1/zh
Priority to ZA2023/11707A priority patent/ZA202311707B/en
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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
    • 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
    • B01J29/00—Catalysts comprising molecular sieves
    • B01J29/82—Phosphates
    • B01J29/84—Aluminophosphates containing other elements, e.g. metals, boron
    • B01J29/85—Silicoaluminophosphates [SAPO compounds]
    • 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
    • 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
    • B01J38/02—Heat treatment
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • 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
    • B01J38/14—Treating with free oxygen-containing gas with control of oxygen content in oxidation gas
    • 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
    • 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
    • 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
    • B01J8/1872—Details of the fluidised bed reactor
    • 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
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C1/00—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon
    • C07C1/20—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon starting from organic compounds containing only oxygen atoms as heteroatoms
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C1/00—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon
    • C07C1/20—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon starting from organic compounds containing only oxygen atoms as heteroatoms
    • C07C1/24—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon starting from organic compounds containing only oxygen atoms as heteroatoms by elimination of water
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00743—Feeding or discharging of solids
    • B01J2208/00752—Feeding
    • 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
    • B01J2208/00823—Mixing elements
    • B01J2208/00831—Stationary elements
    • B01J2208/00849—Stationary elements outside the bed, e.g. baffles
    • 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
    • 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
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2529/00—Catalysts comprising molecular sieves
    • C07C2529/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites, pillared clays
    • C07C2529/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
    • C07C2529/40—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2529/00—Catalysts comprising molecular sieves
    • C07C2529/82—Phosphates
    • C07C2529/84—Aluminophosphates containing other elements, e.g. metals, boron
    • C07C2529/85—Silicoaluminophosphates (SAPO compounds)
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P30/00—Technologies relating to oil refining and petrochemical industry
    • Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P30/00—Technologies relating to oil refining and petrochemical industry
    • Y02P30/40—Ethylene production

Definitions

  • the invention relates to the field of olefin preparation, in particular to a fluidized bed reactor, a device for preparing low-carbon olefins, and a method for preparing low-carbon olefins.
  • Low-carbon olefins namely ethylene and propylene
  • ethylene and propylene are two important basic chemical raw materials, and their demand is increasing.
  • ethylene and propylene are produced through petroleum routes, but due to the limited supply and high price of petroleum resources, the cost of producing ethylene and propylene from petroleum resources continues to increase.
  • people have begun to vigorously develop the technology of converting alternative raw materials into ethylene and propylene.
  • oxygenated compounds such as alcohols (methanol, ethanol), ethers (dimethyl ether, methyl ethyl ether), esters (dimethyl carbonate, methyl formate Esters), etc.
  • these oxygenated compounds can be converted from coal, natural gas, biomass and other energy sources.
  • Some oxygenated compounds can already be produced on a large scale, such as methanol, which can be produced from coal or natural gas, and the process is very mature, which can achieve a production scale of millions of tons.
  • the current oxygenate-to-olefins unit is similar to the catalytic cracking unit, both of which are continuous reaction-regeneration methods.
  • a turbulent fluidized bed reactor, device and method for preparing propylene and C4 hydrocarbons from oxygenates are disclosed.
  • the technical scheme sets n reactions in the reaction zone of the turbulent fluidized bed reactor feed distributor, the oxygen-containing compound concentration is relatively uniform, which weakens the inhibition of the MTO reaction on the olefin alkylation reaction, and the regenerated catalyst directly enters the bottom of the reaction zone, which is beneficial to the alkylation reaction of ethylene, propylene and methanol.
  • the Chinese patent application with the publication number CN107235821A describes a methanol-to-olefins device.
  • the first external circulation catalyst distributor and the first catalyst redistributor are arranged in the reaction zone of the fluidized bed reactor, and the regeneration zone is set.
  • the second external circulation catalyst distributor, the low-activity catalyst distributor, the cooled catalyst distributor and the second catalyst redistributor can not only ensure the uniform distribution of the temperature and activity of the reactants and the catalyst, but also ensure the contact between the reaction gas and the catalyst Effect.
  • the regeneration process mainly uses air as the regeneration gas, By adjusting the amount of auxiliary gas in the regeneration feed gas, the "flying temperature" phenomenon in the regeneration process can be prevented.
  • this method will generate a large amount of greenhouse gas CO 2 , which is not conducive to environmental protection. If the catalyst is partially burned by air charcoal Regeneration, its carbon burning rate is faster, which is not conducive to the control of the amount of residual carbon in the catalyst, and increases the difficulty in the operation process.
  • the purpose of the present invention is to overcome the problems of uneven catalyst distribution, insufficient utilization of regeneration heat and low yield of low-carbon olefins existing in the existing device for preparing low-carbon olefins, and provide a fluidized bed reactor and a device for preparing low-carbon olefins.
  • a first aspect of the present invention provides a fluidized bed reactor, which includes:
  • the first raw material distributor, the second raw material second distributor and the catalyst distributor are arranged in sequence, which are used to distribute the gas raw material, wherein the The first raw material distributor is below the second raw material distributor; wherein the first raw material distributor and the second raw material distributor have the same or different opening ratios, each independently being 0.05-5%;
  • the first raw material inlet at the bottom of the fluidized bed reactor enables at least a portion of the raw material to be distributed twice sequentially through the first raw material distributor and the second raw material distributor;
  • the catalyst distributor includes a catalyst distributor main flow pipe, which is distributed coaxially with the raw material first distributor and the raw material second distributor, wherein the catalyst distributor main flow pipe passes through the raw material second distributor from bottom to top.
  • One distributor and feedstock second distributor catalyst second catalyst first.
  • the second aspect of the present invention provides a device for preparing low-carbon olefins, which device includes the fluidized bed reactor, the settler and the regenerator described in the present invention, and the side wall of the reactor is provided with at least one device for dissolving the catalyst One is fed to the catalyst first feed port between the first raw material distributor and the second raw material distributor, and the bottom of the reactor is provided with a feed for the second catalyst feed to the distributor
  • the catalyst second feed port of the main draft pipe of the device wherein: the settler is communicated with the above of the reaction zone of the fluidized bed reactor, and the lower part of the settler is respectively connected with the first feed port of the catalyst and the first feed port of the catalyst.
  • the regenerator is communicated, and the outlet of the regenerated catalyst of the regenerator is communicated with the second feed port of the catalyst.
  • the third aspect of the present invention provides a method for preparing low-carbon olefins, which uses the device for preparing low-carbon olefins described in the present invention, the method comprising:
  • the settler separates the product from the entrained catalyst, and a part of the separated catalyst is directly fed into the feedstock first distributor (8) and In the dense-phase area formed between the second distributors (11) of raw materials, another part is regenerated by the regenerator and fed into the catalyst distribution area from the second catalyst feed port.
  • the unregenerated circulating catalyst supplied from the first feed port of the catalyst can directly enter the dense-phase zone for contact reaction with the reaction raw materials, and the regenerated catalyst supplied from the second feed port of the catalyst enters the After the fluidized bed reactor, it is pre-distributed in the catalyst distribution area through the action of the catalyst distributor, so as to realize energy transfer and reaction under the action of the flow field, so as to make the distribution of the regenerated catalyst more uniform and realize the particle mixing of the regenerated catalyst. Control and improve the reaction efficiency in the fluidized bed reactor;
  • the reaction raw materials enter the reaction area through the first raw material distributor and the second raw material distributor in layers, so as to realize the fluidized bed reactor
  • the segmented flow field control can effectively realize the full contact between the catalyst and the reaction raw materials, effectively eliminate the defects of poor fluidization state and low selectivity of low-carbon olefins, further improve the reaction efficiency, and help increase the yield of low-carbon olefins .
  • a fluidized bed reactor comprising:
  • the raw material first distributor (8), the raw material second distributor (11) and the catalyst distributor (16) in the reaction zone of the fluidized bed reactor are used to distribute the gaseous raw material, wherein the raw material The first distributor (8) is below the second distributor of raw materials (11); wherein the first distributor of raw materials (8) and the second distributor of raw materials (11) have the same or different opening ratios, each independently 0.05-5%;
  • the raw material first inlet (1) at the bottom of the fluidized bed reactor which allows at least a part of the raw material to be distributed twice sequentially through the raw material first distributor (8) and the raw material second distributor (11);
  • the catalyst distributor (16) comprises a catalyst distributor main flow pipe (47), which is coaxially distributed with the raw material first distributor (8) and the raw material second distributor (11), wherein the catalyst distributor
  • the main draft pipe (47) passes through the first raw material distributor (8) and the second raw material distributor (11) from bottom to top.
  • the arrangement of the Y feeding port makes the ratio of the feeding amount of the raw material feeding port Y to the feeding amount of the raw material feeding port (Y-1) be 1:1-10.
  • the raw material first distributor (8) includes a first distributor central area (40) and a first distributor outer annular area (42) located on the outer periphery of the first distributor central area (40).
  • a first distributor enhanced area (38) corresponding to the radial position of the catalyst first feed port (24) is provided on the outer annular area (42) of the distributor, and the first distributor enhanced area (38) has a reduced pore size relative to other regions of the feedstock first distributor (8) such that the catalyst has a diameter between said feedstock first distributor (8) and said feedstock second distributor (11) substantially evenly distributed upwards.
  • the area of the enhanced area (38) is set to be 1/10 ⁇ 1/2 in ratio to the area of the outer area (42) of the first distributor.
  • the opening rate is 1.5-10%, preferably 2-5%, and the aperture is 2-30mm, preferably the aperture difference between each hole is no more than ⁇ 10%; the opening rate of the first distributor reinforcement area (38) 0.01-1.5%, and the pore diameter is 0.1-20mm, preferably, the difference between the pore diameters of each hole is not more than ⁇ 10%.
  • the first distributor reinforcing nozzle (39) comprises a reinforcing nozzle inlet (39-1), a reinforcing nozzle progressively connected in sequence Shrink tube (39-2), enhanced nozzle throat (39-3), enhanced nozzle expansion section (39-4) and enhanced nozzle outlet (39-5), said enhanced nozzle inlet (39-1) and said enhanced nozzle
  • the main body of the raw material first distributor (8) is connected; wherein
  • the angle interval formed by the reducer pipe (39-2) of the enhanced nozzle and the horizontal direction is 30°-70°
  • the angle interval formed by the enlarged section of the enhanced nozzle (39-4) and the horizontal direction is 30°-70°.
  • the ratio of the diameter of the enhanced nozzle throat (39-3) to the diameter of the enhanced nozzle inlet (39-1) is 1:5-20, and the length of the enhanced nozzle throat (39-3) is the same as that of the enhanced nozzle inlet (39-1).
  • the ratio between the diameters of the throat (39-3) is 5-10:1.
  • the fluidized bed reactor according to any one of the first series of exemplified embodiments 1 to 7, characterized in that the fluidized bed reactor is from the feedstock first distributor (8) up to a diameter of The section before reduction has a height h, and the second raw material distributor (11) is arranged at an axial distance of 1/4 ⁇ 1/2 h from the first raw material distributor (8).
  • the fluidized bed reactor according to any one of the first series of exemplary embodiments 1 to 7, characterized in that the catalyst distributor main flow pipe (47) passes through the raw material first Distributor (8) and raw material second distributor (11), described fluidized bed reactor has height h from described raw material first distributor (8) up to the section before diameter reduction, and described catalyst distributor The upward height of the main draft pipe (47) from the first raw material distributor (8) is h1, then 1/4h ⁇ h1 ⁇ 3/4h.
  • a fluidized bed reactor according to embodiment 13 of the first series of exemplary embodiments characterized in that
  • the flow pipe (47) is connected, and the catalyst first distribution conduit (49) and the catalyst second distribution conduit (50) are respectively provided with a plurality of catalyst outlets (51);
  • the number of catalyst distribution conduits in each layer of catalyst distribution member (48) is X (X ⁇ 2), and the circumferential angular spacing of multiple catalyst distribution conduits is distributed at 180°/X; the catalyst outlet (51) has a shape selected from square, circular and polymorphic shapes. .
  • the included angle ( ⁇ ) formed by the baffle groove (37) and the horizontal direction is 30°-75°.
  • a device for preparing light olefins characterized in that the device comprises a fluidized bed reactor (7), a settler (9) and A regenerator (10), at least one first catalyst feeder (8) and second catalyst distributor (11) for feeding the catalyst to the second distributor (11) of the raw material is provided on the side wall of the reactor.
  • a feed inlet (24), the bottom of the reactor is provided with a catalyst second feed inlet (27) for feeding the catalyst second feed to the distributor main flow pipe (47);
  • the settler (9) communicates with the top of the reaction zone of the fluidized bed reactor (7), and the lower part of the settler (9) is respectively connected to the catalyst first feed port (24) and the The regenerator (10) is in communication, and the regenerated catalyst outlet of the regenerator (10) is in communication with the second catalyst feed port (27).
  • the device characterized in that the settler (9) is provided with a lower settler section (17) and an upper settler section above the lower settler section (17) (18) and the settler cyclone separator (19) that is positioned at described settler upper section (18), the gas outlet of described settler cyclone separator (19) and the product gas outlet (5) of described settler (9) ) is communicated, the bottom of the lower section of the settler (17) is provided with a settler distribution plate (12), and the bottom of the settler distribution plate (12) is connected with the catalyst first feed port through a circulation pipe (22) (24) is connected, and is connected with the regenerator (10) through a stripper (21).
  • the size ratio of the first distribution plate hole (35) of the settler to the second distribution plate hole (36) of the settler is 1-3:4.
  • the top of the fluidized bed reactor (7) is provided with a Lifting the separation pipe (15)
  • the settler (9) is provided with a riser baffle plate (14) located above the outlet of the lifting separation pipe (15).
  • the settler separates the product from the entrained catalyst, and a part of the separated catalyst is directly fed into the feedstock first distributor (8) and In the dense-phase area formed between the second distributors (11) of raw materials, another part is regenerated by the regenerator and fed into the catalyst distribution area from the second catalyst feed port.
  • Fig. 1 is the schematic diagram of the device of a kind of embodiment of preparing light olefin according to the present invention
  • Fig. 2 is a structural schematic diagram of a specific embodiment of the first distributor of raw materials in the device for preparing light olefins according to the present invention
  • Fig. 3 is the structure schematic diagram of another embodiment of the first distributor of raw materials in the device for preparing light olefins according to the present invention
  • Fig. 4 is a schematic structural view of a specific embodiment of the first sparger in the device for preparing light olefins according to the present invention
  • Fig. 5 is a structural schematic diagram of a specific embodiment of the second distributor of raw materials in the device for preparing light olefins according to the present invention
  • Fig. 6 is a schematic structural view of a specific embodiment of the catalyst distributor in the device for preparing light olefins according to the present invention.
  • Fig. 7 is a structural schematic diagram of another specific embodiment of the catalyst distributor in the device for preparing light olefins according to the present invention.
  • Fig. 8 is the distribution diagram in the fluidized bed reactor when the circulating distribution baffle is set to two in the device for preparing low-carbon olefins according to the present invention
  • Fig. 9 is the distribution diagram in the fluidized bed reactor when the circulating distribution baffle is set to four in the device for preparing light olefins according to the present invention.
  • Fig. 10 is a structural schematic diagram of a specific embodiment of the circulating cloth baffle in the device for preparing low-carbon olefins according to the present invention.
  • Fig. 11 is a schematic structural diagram of an example of a catalyst distributor according to the present invention.
  • Fig. 12 is a structural representation of a specific embodiment of the settler distribution plate in the device for preparing light olefins according to the present invention.
  • Fig. 13 is a schematic diagram of the unevenness of the distribution of the regenerated catalyst in Example 1 of the present invention as a function of height;
  • Fig. 14 is a comparison chart of the unevenness of the regenerated catalyst distribution with height in Example 1 and Comparative Example 3 of the present invention.
  • the first inlet for raw materials 2.
  • Fluidized bed reactor 8. Raw material first distributor
  • orientation words used such as "upper and lower” generally refer to the upper and lower parts shown in the accompanying drawings; The inside and outside of the silhouette.
  • the "gas raw material” has a well-known meaning in the art.
  • the gas feedstock for the fluidized bed reactor of the present invention may optionally contain a certain amount of liquid, especially in the form of dispersed droplets, as long as the presence of the liquid does not substantially hinder the The fluidized state of the fluidized bed is sufficient.
  • the reaction zone of the fluidized bed reactor 7 described in the first aspect of the present invention is provided with the first distributor 8 of raw material, the second distributor 11 of raw material and the catalyst distributor 16 successively from bottom to top, and the catalyst distribution
  • the device 16 is communicated with the second feed port 27 of the catalyst, and a dense-phase zone 28 is formed between the first raw material distributor 8 and the second raw material distributor 11, and the area where the catalyst distributor 16 is located is formed to communicate with the dense-phase zone 28.
  • the catalyst distribution area 29 is provided with at least one catalyst first feed port 24 on the reactor side wall of the dense phase area 28 .
  • the catalyst distributor 16 functions to perform pre-distribution in the catalyst distribution area 29, so as to realize energy transfer and reaction under the action of the flow field, thereby making the catalyst distribution more uniform, realizing the particle mixing control of the catalyst, and improving the performance of the fluidized bed reactor. 7.
  • the full contact of the raw materials further improves the reaction efficiency and is beneficial to increase the yield of low-carbon olefins.
  • the catalyst first feed port 24 and the second catalyst feed port 27 of the fluidized bed reactor 7 can be used to feed the same catalyst or different catalysts;
  • the first catalyst feed port 24 can be used to feed unregenerated recycled catalyst, and the second catalyst feed port 27 is used to feed regenerated catalyst.
  • the first distributor outer annular area 42 on the outer periphery of the distributor central area 40 is provided with a first distributor reinforcement area 38 corresponding to the radial position of the first catalyst feed port 24 .
  • the first distributor enhanced area 38 has a reduced pore size relative to the other areas of the raw material first distributor 8, so that the catalyst is distributed between the raw material first distributor 8 and the raw material There is a substantially uniform distribution in the radial direction among the second distributors 11 .
  • the first distributor enhanced area 38 is provided in one-to-one correspondence with the first catalyst feed port 24, so that the first distributor enhanced area 38 can supply the reaction raw materials it receives with the first catalyst feed port 24. catalyst for rapid mixing.
  • the catalyst first feed port 24 is located above the center of the outer edge of its corresponding first distributor enhanced area 38, so as to further enhance the first distributor enhanced area 38's interaction between the reaction raw material and the first catalyst feed port. 24 The effect of uniform mixing of the catalyst supplied. More preferably, the ratio of the area of the first distributor reinforcement area 38 to the area of the first distributor outer annular area 42 is 1/10 ⁇ 1/2.
  • the first distributor central region 40 is a circle with radius r
  • the area of the first distributor enhanced area 38 is 1/N of the area of the first distributor outer area 42, and N is 2 , The natural number of 3.
  • the opening rate of the raw material first distributor 8 is 1.5-10%, preferably 2-5%, and the pore diameter is 2- 30mm, preferably the aperture difference between the holes is no more than ⁇ 10%; the opening ratio of the first distributor reinforcement area 38 is 0.05-1.5%, and the aperture is 0.1-20mm, preferably the aperture difference between the holes is the same More than ⁇ 10%.
  • the tuyere 41 in the central area of the first distributor on the central area 40 of the first distributor can be circular, triangular, square, hexagonal, etc., with an effective diameter of 0.1-10mm and an opening ratio of 0.05-5%. .
  • the first distributor enhanced area 38 is provided with a plurality of columnar first distributor enhanced nozzles 39, and the angle formed between the centerline of the first distributor enhanced nozzles 39 and the horizontal direction is 45°-75°,
  • the first distributor enhances the nozzle 39 to form a stronger mixing force between the distributed reaction raw material and the catalyst supplied by the first catalyst feed port 24 .
  • the effective diameter of the first distributor enhanced nozzle 39 can be set to 0.1-10mm, and the opening ratio is 0.05-5%;
  • the distribution hole set as the area of the reinforcement area 38 of the first distributor has the same size and opening ratio as the tuyere 41 in the central area of the first distributor.
  • first distributor enhanced nozzle 39 in the present invention referring to FIG. Nozzle throat 39-3, reinforced nozzle expansion section 39-4, reinforced nozzle outlet 39-5, reinforced nozzle inlet 39-1 are connected with the main body of the first raw material distributor 8.
  • Raw materials are fed into the first distributor 8.
  • the raw materials enter through the enhanced nozzle inlet 39-1, and are sequentially transmitted through the enhanced nozzle reducer 39-2, the enhanced nozzle throat 39-3, and the enhanced nozzle expansion section 39-4. Exit 39-5 ejects.
  • the angle interval formed between the constriction pipe 39-2 of the enhanced nozzle and the horizontal direction is 30°-70°
  • the angle interval formed between the enlarged section 39-4 of the enhanced nozzle and the horizontal direction is 30°-70°
  • the enhanced nozzle The ratio of the diameter of the pipe throat 39-3 to the diameter of the reinforced nozzle inlet 39-1 is 1:5-20, and the ratio between the length of the reinforced nozzle throat 39-3 and the diameter of the reinforced nozzle throat 39-3 is 5 -10:1.
  • the horizontal direction specifically refers to the direction in which the horizontal plane extends when the fluidized bed reactor 7 is placed on the horizontal plane.
  • the fluidized bed reactor has a height h from the first raw material distributor 8 up to the section before diameter reduction, and the second raw material distributor 11 is set at a distance from the first raw material distributor 8 Distributors 8 are axially separated by 1/4 to 1/2h.
  • the opening ratio of the second raw material distributor 11 is 0.05-5%, preferably 3-5%, and the aperture It is 1-30mm, preferably the difference between the diameters of the holes is not more than ⁇ 10%.
  • the second raw material distributor 11 is provided with a second distributor gas main duct 43 extending radially along the second raw material distributor 11, and a plurality of gas flow pipes sequentially arranged along the radial direction of the second raw material distributor 11.
  • the gas annulus guide pipe 44 is arranged to form a circular distribution around the central area of the second raw material distributor 11, and the second distributor solid guide groove 46 is located between two adjacent second distributor gas annulus guide pipes 44 Between; wherein the fluidized bed reactor has a second raw material feed port 2, which is in fluid communication with the second distributor gas main flow pipe 43.
  • the opening level of the second distributor tuyere 45 can be circular, triangular, square, hexagonal, etc., with an effective diameter of 0.1-10 mm and an opening rate of 0.05-5%.
  • the ratio between the width of the gas annulus guide pipe 44 of the second distributor and the width of the solid guide groove 46 of the second distributor is 1:2-6.
  • the catalyst distributor 16 includes a catalyst distributor main flow pipe 47 .
  • the catalyst distributor 16 can have different structures, as long as the catalyst conveyed axially along the main flow pipe 47 of the catalyst distributor can be distributed radially inside the fluidized bed reactor.
  • the main flow pipe 47 of the catalyst distributor passes through the first raw material distributor 8 and the second raw material distributor from bottom to top. device 11, the fluidized bed reactor has a height h from the first raw material distributor 8 up to the section before the diameter is reduced, and the main flow pipe 47 of the catalyst distributor starts from the first raw material distributor 8
  • the upward height is h1, then 1/4h ⁇ h1 ⁇ 3/4h.
  • the catalyst distributor 16 is a dendritic arrangement, which includes a catalyst distributor main flow pipe 47 and a multi-layer distribution along the up and down direction of the catalyst distributor main flow pipe 47.
  • Catalyst distribution member 48, the main flow pipe 47 of the catalyst distributor is vertically arranged in the reaction area and communicated with the second catalyst feed port 27, the catalyst distribution member 48 extends in the radial direction, so that the main flow pipe 47 along the catalyst distributor Axially conveyed catalyst can be distributed radially within the fluidized bed reactor.
  • the catalyst distribution member (48 includes a plurality of catalyst first distribution conduits 49 and a plurality of catalyst second distribution conduits 50 respectively extending radially outward from the distributor main flow conduit 47, the catalyst first distribution conduits 50
  • the conduit 49 and the second distribution conduit 50 of the catalyst are alternately distributed along the main flow pipe 47 of the catalyst distributor and communicate with the main flow pipe 47 of the catalyst distributor.
  • the first distribution conduit 49 of the catalyst and the second distribution conduit 50 of the catalyst are respectively provided with multiple Catalyst outlet 51. Catalyst enters each catalyst distribution member 48 from the main flow pipe 47 of the catalyst distributor, is transported through the first catalyst distribution pipe 49 and the second catalyst distribution pipe 50 and enters the reactor through the catalyst outlet 51.
  • the number of catalyst distribution conduits in each layer of catalyst distribution member 48 is X (X ⁇ 2 and ⁇ 15), and the circumferential angular spacing of multiple catalyst distribution conduits is distributed at 360°/X; the catalyst outlet 51 has an optional From square, round and multi-morph shapes.
  • the number of the catalyst distribution members 48 is preferably M layers (M ⁇ 3 and ⁇ 10), and the catalyst distribution members 48 are the first layer, the second layer, ... the Mth layer from top to bottom. layer; wherein the length of the catalyst distribution conduit in the catalyst distribution member 48 of the nth layer is (0.7-0.9) n *D/2, D is the inner diameter of the reactor, and n is the corresponding number of layers, for example, the diameter of the distribution conduit is 0.75 n * D/2.
  • the lengths of the catalyst first distribution conduit 49 and the catalyst second distribution conduit 50 corresponding to the catalyst distribution member 48 decrease sequentially from top to bottom, and the catalyst outlets on the catalyst first distribution conduit 49 and the catalyst second distribution conduit 50 51 equidistant distribution.
  • the first catalyst distribution conduit 49 and the second catalyst distribution conduit 50 can be collectively referred to as the catalyst distribution conduit
  • the number of catalyst distribution members 48 is preferably M layers (M ⁇ 3 and ⁇ 10), and the inner diameter of the reactor is D meters
  • the catalyst distribution member 48 is successively the first layer, the second layer, the third layer...the Mth layer from top to bottom, and the diameter of the catalyst distribution conduit in each catalyst distribution member 48 is 0.75n*D meters ( n is the corresponding number of layers);
  • the number of catalyst distribution conduits in each layer of catalyst distribution member 48 is X (X ⁇ 2 and ⁇ 15), and the circumferential angular spacing of multiple catalyst distribution conduits is distributed at 360°/X;
  • catalyst outlet 51 It can be square, circular and multi-deformed, etc.
  • the diameter of the effective channel is 20-100mm, and the ratio of the center-to-center distance between two adjacent catalyst outlets 51 and the width of the catalyst outlet 51 along its distribution direction is 1.5- 5:1.
  • the catalyst distributor 16 is a main flow pipe arrangement comprising or consisting only of the main catalyst distributor flow pipe 47 .
  • the main flow pipe 47 of the catalyst distributor is generally tubular, with an open top, and the catalyst is transported from bottom to top along it, and enters the fluidized bed reactor through the open top opening.
  • the catalyst distributor main flow pipe 47 has openings on the pipe wall, for example, the opening ratio is 5-30%, so that the catalyst can be evenly distributed in the radial direction through the openings. .
  • the catalyst distributor 16 is an inner baffle arrangement, which includes a catalyst distributor main flow pipe 47 and a catalyst main flow pipe inner baffle 47 - 2 .
  • the shape of the inner baffle 47-2 is not specifically limited, for example, it can be substantially circular, elliptical (for example, when it is in the installation position, the projection on the horizontal plane is circular), and its projected area on the horizontal plane is the catalyst distribution area. 1/10 ⁇ 1/4 of the internal cross-section of the main flow pipe 47 of the device.
  • the inner baffle 47-2 extends obliquely downward from the contact point with the pipe wall of the main flow pipe 47 of the catalyst distributor, and the vertical angle with the pipe wall is 10-75°, for example, 30-45°.
  • the catalyst distributor 16 is a secondary distribution arrangement, which includes a catalyst distributor main flow pipe 47 and two or more dispersed secondary distribution flow pipes connected to its top. 47-3, such as 2-12 pieces, such as 3-6 pieces.
  • the outer wall of each secondary distribution draft pipe 47-3 is connected with the outer wall of the main draft pipe 47 of the catalyst distributor in an arc shape of about 1/4 circle, and the radius of the circle is the distance from the center of the horizontal ring of the outlet of the secondary distribution draft pipe to the catalyst.
  • the part of each secondary distribution draft pipe 47-3 except the arc connection part is a straight round pipe communicating with the arc.
  • a plurality of secondary distribution ducts 47-3 are evenly spaced on the circumference.
  • multiple secondary distribution ducts 47-3 have consistent shapes and sizes.
  • the length of the secondary distribution duct 47-3 can be specifically determined according to the actual situation, for example, the length extending in the radial direction is (0.1-0.9)*D/2, where D is the inner diameter of the reactor.
  • the catalyst distributor 16 is a spiral draft tube arrangement, which includes a catalyst distributor main draft tube 47 and a layer or layers distributed along the axial direction of the catalyst distributor main draft tube 47 Multi-layer spiral guide pipe 47-4.
  • Each layer contains 2 or more dispersed spiral draft tubes 47-4, such as 2-15, such as 3 or 4.
  • a plurality of spiral draft tubes 47-4 in each layer are arranged at even intervals on the circumference.
  • the catalyst distributor 16 comprises 2-10 layers of spiral draft tubes 47-4.
  • the length of the secondary distribution duct 47-4 of each layer can be specifically determined according to the actual situation, for example, the length extending in the radial direction is (0.5-0.9) n *D/2, D is the inner diameter of the reactor, n is the corresponding number of layers.
  • the catalyst distributor 16 is an annular draft tube arrangement, which includes a main catalyst distributor duct 47 and a layer of catalyst distributor main duct 47 distributed along the axial direction. Or multi-layer annular draft tube 47-5.
  • the annular guide pipe includes a guide ring 47-6 and a connecting pipe 47-7 connecting it with the main guide pipe 47 of the catalyst distributor.
  • the connecting pipe 47-7 is preferably a spiral structure.
  • Each layer of annular draft tubes includes 2 or more dispersed connecting tubes 47-7, such as 2-10, such as 2-6, such as 3 or 4.
  • the connecting pipes 47-7, 47-4 of each layer are evenly spaced on the circumference.
  • the catalyst distributor 16 comprises 2-10 layers, for example, 2-6 layers of annular draft tubes 47-5.
  • the diameter of each layer of annular draft tube 47-5 is (0.5-0.9) n *D/2, where D is the inner diameter of the reactor, and n is the corresponding number of layers.
  • n representing the number of layers counts the corresponding members from top to bottom.
  • the fluidized bed reactor has one or more Y-th raw material inlets arranged above the first raw material inlet 1 and arranged from bottom to top, wherein Y is a positive integer ⁇ 2, provided that when there is When the one or more raw material Y feed inlets are used, the arrangement of the raw material first inlet and the raw material Y feed inlet is such that the feed amount of the raw material Y feed inlet is equal to that of the raw material (Y-1)
  • the feed ratio of the feed port is 1:1-10.
  • the fluidized bed reactor 7 is provided with a corresponding feed port, so as to be able to supply the reaction raw material to the first raw material distributor 8 and the second raw material distributor 11 .
  • the fluidized bed reactor 7 is provided with a first feed port 1 for raw materials and a second feed port 2 for raw materials, the first feed port 1 for raw materials and the first feed port for raw materials
  • the bottom of the distributor 8 is connected, and the second raw material feed port 2 is located at the confluence area of the dense phase area 28 and the catalyst distribution area 29 .
  • the feed ports in the present invention are not limited to the first raw material feed port 1 and the raw material second feed port 2, and other feed ports can be provided according to the input requirements of the reaction raw materials.
  • a circulation distribution baffle connected to the inner wall of the fluidized bed reactor 7 is arranged above the first feed port 24 of the catalyst 34.
  • the circulating cloth baffles 34 are provided in one-to-one correspondence with the first catalyst feed ports 24 , and are located directly above the corresponding catalyst first feed ports 24 .
  • the ratio of the distance between the circulating cloth baffle plate 34 and the first catalyst feed port 24 to the diameter of the first catalyst feed port 24 is 1-10:1.
  • the circulating cloth baffle 34 is specifically a structure in which the center of the circle is located on the inner wall of the fluidized bed reactor 7, and the circle whose radius is R intersects the inner wall of the fluidized bed reactor 7, wherein the size of R is equal to the radius of the reactor.
  • the ratio is 1:4-10.
  • the circulating cloth baffle 34 is provided with a plurality of circulating cloth baffle slots 37, and the angle ⁇ formed between the circulating cloth baffle slots 37 and the horizontal direction is 30°-75°, so that the circulating cloth baffle slots 37 Towards the center of the fluidized bed reactor 7.
  • the circulation distribution baffle 34 can distribute the catalyst supplied by the first catalyst feed port 24 to the center of the fluidized bed reactor 7, and the flow direction of the catalyst is strengthened through the circulation distribution baffle groove 37, so that the catalyst distribution uniformity is further improved.
  • the width of circulating cloth baffle groove 37 is H1, and its ratio with the size of the radius R of circulating cloth baffle 34 is 0.01-0.1: 1; The size ratio of the radius R is 0.001-0.05:1.
  • the second aspect of the present invention provides a device for preparing low-carbon olefins, referring to Fig. 1, the device includes a fluidized bed reactor 7, a settler 9 and a regenerator 10 provided by any of the above-mentioned technical solutions, and on the side wall of the reactor There is at least one first catalyst feed port 24 for feeding the first catalyst between the first distributor 8 of the raw material and the second distributor 11 of the raw material, and the bottom of the reactor is provided with a The feed of the second catalyst feed is fed to the second catalyst feed pipe 27 of the main flow pipe 47 of the distributor; wherein the settler 9 communicates with the upper part of the reaction zone of the fluidized bed reactor 7, and the lower part of the settler 9 is respectively It communicates with the first catalyst feed port 24 and the regenerator 10 , and the regenerated catalyst outlet of the regenerator 10 communicates with the second catalyst feed port 27 .
  • the number of catalyst first feed ports 24 is k, k ⁇ 2, and preferably k ⁇ 12; each catalyst first feed port (24) center The line angle is 360°/k.
  • the lower part of the settler 9 is connected with the first feed port 24 of the catalyst through a circulation pipe 22 .
  • the number of circulation pipes 22 is the same as the quantity of the first feed port 24 of the catalyst, and the circulation pipe control valve 23 is arranged on the circulation pipe 22, so as to be able to control the amount of gas supplied to the dense phase zone 28 from the first feed port 24 of the catalyst. Supply amount.
  • the settler 9 can adopt a settling device with a conventional structure to separate the product output from the fluidized bed reactor 7 from the entrained catalyst.
  • the settler 9 is provided with a settler lower section 17, a settler upper section 18 above the settler lower section 17 and a settler cyclone separator 19 positioned at the settler upper section 18, and the gas outlet of the settler cyclone separator 19 is connected to the
  • the product gas outlet 5 of the settler 9 is connected, and the lower part of the lower section 17 of the settler is provided with a settler distribution plate 12 , and the upper part of the settler distribution plate 12 is connected to the circulation pipe 22 and connected to the regenerator 10 through the stripper 21 .
  • the top of the upper section 18 of the settler is hemispherical, referring to Fig. 12, the first distribution plate hole 35 of the settler and the second distribution plate hole 36 of the settler are set on the distribution plate 12 of the settler, the first distribution plate hole of the settler 35 and the second distribution plate hole 36 of the settler are arranged to be distributed in a ring around the central area of the settler distribution plate 12 respectively, and the size ratio of the first distribution plate hole 35 of the settler to the second distribution plate hole 36 of the settler is 1-3 : 4.
  • the first distribution plate holes 35 of the settler and the second distribution plate holes 36 of the settler are preferably distributed alternately in a circular shape on the distribution plate 12 of the settler, and the opening ratio of the two is 0.05-5%.
  • the upper section 18 of the settler adopts a hemispherical design. Compared with the structure of the traditional settler, under the same volume, the size of the settler 9 can be reduced by 10-21%.
  • the dome design of the upper section 18 of the settler can make the The gas flow field is more stable.
  • the settler cyclone separator 19 can adopt a conventional cyclone separation device to effectively separate the product from the entrained catalyst.
  • the settler cyclone separator 19 is set as a two-stage or multi-stage cyclone separator structure in series, the inlet of the first-stage cyclone separator communicates with the upper section 18 of the settler, and the gas of the first-stage cyclone separator The outlet is communicated with the inlet of the adjacent cyclone separator, and the product gas is obtained from the gas outlet of the cyclone separator of the last stage, and the solid outlets of all cyclone separators are connected with the settler 9 area; the gas outlet of the last stage cyclone separator It communicates with the product gas outlet 5 of the settler 9, so that the product gas obtained by the final cyclone separator is discharged from the product gas outlet 5.
  • the bottom of settler 9 is connected with regenerator 10 by stripper 21, and concrete connection mode can be: the bottom of settler 9 is connected with stripper 21 by stripper feeding pipe 30, and stripper 21 is provided with a stripping medium inlet, to introduce the stripping medium 3 in the stripper 21, the outlet of the stripper 21 communicates with the regenerator feed pipe 33 of the regenerator 10 through the stripper discharge pipe 31 ,
  • the stripper outlet pipe 31 is provided with a stripper control valve 32 to control the amount of feed entering the regenerator 10 from the regenerator feed pipe 33 .
  • the regenerator 10 is provided with a regenerator gas distributor 13 and a regenerator cyclone separator 20 above the regenerator gas distributor 13, the gas outlet of the regenerator cyclone separator 20 and the flue gas outlet of the regenerator 10 6 communication, the lower part of the regenerator 10 is provided with a regenerator gas inlet communicating with the regenerator gas distributor 13, so as to introduce the regenerator gas 4 into the regenerator 10 and distribute it through the regenerator gas distributor 13 to improve the regenerator 10% work efficiency.
  • the bottom of the regenerator 10 is provided with a regenerated catalyst outlet, and the regenerated catalyst outlet is communicated with the second feed port 27 of the catalyst through the regenerator circulation discharge pipe 26, and the regenerator circulation discharge pipe control valve is arranged on the regenerator circulation discharge pipe 26 25.
  • the structure design and parameters of the regenerator gas distributor 13 and the raw material second distributor 11 are the same.
  • the regenerator gas distributor 13 is provided with a regenerator gas main duct extending along the radial direction of the regenerator gas distributor 13, and a plurality of regenerator gas distributors sequentially arranged along the radial direction of the regenerator gas distributor 13.
  • Annulus guide pipe, regenerator tuyeres and regenerator solid guide grooves arranged on regenerator gas annulus guide pipe, each regenerator gas annulus guide pipe is set to surround the center of regenerator gas distributor 13 The area is distributed in a ring shape, and the regenerator solid diversion groove is located between two adjacent regenerator gas annular gap diversion pipes.
  • the regenerator cyclone separator 20 of the regenerator 10 is the same as the settler cyclone separator 19, and is configured as a two-stage or multi-stage series cyclone separator structure; the last stage cyclone separator of the regenerator cyclone separator 20
  • the gas outlet of the regenerator communicates with the flue gas outlet 6 of the regenerator 10, so that the flue gas obtained by the final cyclone separator is discharged from the flue gas outlet 6.
  • the top of the fluidized bed reactor 7 is provided with a lifting separation pipe extending into the settler 9 15.
  • a riser baffle 14 located above the outlet of the lift separation pipe 15 is arranged in the settler 9 .
  • the shape of the riser baffle 14 is herringbone, circular or rectangular, so as to reduce the catalyst particles brought from the fluidized bed reactor 7 into the settler 9 .
  • a method for preparing low-carbon olefins provided by the third aspect of the present invention uses the device provided by any one of the above-mentioned technical solutions, and the method includes:
  • the resulting product and entrained catalyst are fed into the settler 9 via above the reaction zone;
  • the settler 9 separates the product from the entrained catalyst, and a part of the separated catalyst is directly fed into the dense-phase zone 28 from the catalyst first feed port 24, and the other part is regenerated by the regenerator 10 from the second part of the catalyst.
  • Feed port 27 feeds into catalyst distribution zone 29 .
  • the gaseous raw material can be selected from at least one of methanol, ethanol, propanol, butanol, acetaldehyde, propionaldehyde, butyraldehyde, acetone, butanone, formic acid, acetic acid and propionic acid.
  • a part of the separated catalyst is fed into the regenerator 10 through a stripper 21 whose stripping medium 3 is steam.
  • the pressure in the fluidized bed reactor 7 is 0-0.5MPa in gauge pressure, the average temperature is 350-560°C, and the temperature difference is ⁇ 5°C, the catalyst is SAPO-34, and the The linear velocity of the material in the dense phase zone 28 is 1-10m/s.
  • the mass ratio of the part fed into the dense phase zone 28 to the part fed into the regenerator 10 is 1:0.2-1.
  • the coke content of the regenerated catalyst obtained from the regenerator 10 is 5-15% by weight.
  • the regeneration medium of the regenerator 10 is a mixture of CO and air, and the volume ratio of CO and air in the mixture is 0.005-0.5:1, so as to perform partial regeneration reaction A regenerated catalyst is obtained; the regeneration temperature of the regenerator 10 is 600-750°C.
  • Introducing CO2 into the regeneration medium can effectively and selectively eliminate carbon deposition, stably control the carbon deposition of the regenerated catalyst and the temperature of the regenerated catalyst, and at the same time realize the efficient use of reaction heat to convert greenhouse gas CO2 .
  • the coke content of the partially regenerated catalyst is between 1-3% by weight, and the average temperature of the regenerated catalyst is controlled within the range of 400-500°C.
  • the pressure drop generated when the gaseous raw material passes through the dense-phase region 28 is related to the distribution of the gaseous raw material through the catalyst.
  • Zone 29 produces a pressure drop ratio of 1.5-4:1.
  • the gaseous raw material passes through the first raw material distributor 8 to redistribute the gas direction, and the angle formed by the annulus space velocity and the horizontal direction is 45°-75°,
  • the ratio of inner and outer porosity fluctuations is 0.9-0.95:1.
  • the method of the invention can realize the uniform distribution of the regenerated catalyst and its full contact with the raw material, effectively suppress the uneven temperature distribution and low diene selection, and can be used in the industrial production of low-carbon olefins.
  • the catalyst distribution in a fluidized bed reactor is measured, and the mean square error ⁇ 2 is used to characterize the heterogeneity of the catalyst. Its expression is shown in formula (1). The larger the value, the more uneven the catalyst distribution in this area. The minimum value of 0 means that the concentration at each position is equal to the average concentration under ideal conditions.
  • ⁇ 1 2 represents the concentration distribution of the regenerated catalyst relative to the three phases (gas phase, circulating catalyst, regenerated catalyst);
  • c again refers to the particle concentration of the regenerated catalyst at each grid area required for the calculation; is the particle concentration of all catalysts in each grid area; m represents the number of cross-sections of the reactor area measured, generally 5 ⁇ m ⁇ 50 in different measurements; , i represents the type of catalyst fed to the reactor.
  • the fluidized bed reactor 7 preferably comprises a catalyst first feed port 24 and a catalyst second feed port 27, so as to feed different catalysts respectively, for example feed a recycled catalyst and a regenerated catalyst respectively;
  • the device for preparing light olefins includes a fluidized bed reactor 7, a settler 9 and a regenerator 10;
  • the reaction area of the fluidized bed reactor 7 is sequentially provided with a first raw material distributor 8, a second raw material distributor 11 and a catalyst distributor 16 from bottom to top. It is the dense-phase area 28 of catalyst, and the area where catalyst distributor 16 is located is formed as the catalyst distribution area 29 communicating with dense-phase area 28, and the reactor side wall of dense-phase area 28 is provided with a plurality of catalyst first feed ports twenty four;
  • the raw material first distributor 8 includes a first distributor central area 40 and a first distributor outer annular area 42 positioned at the outer periphery of the first distributor central area 40.
  • the first distributor outer annular area 42 is provided with a The first distributor enhancement area 38 corresponding to the feed port 24, the catalyst first feed inlet 24 is located above the center of the outer edge of its corresponding first distributor enhancement area 38, and the first distributor enhancement area 38 is provided with a plurality of A columnar first distributor enhanced nozzle 39, the angle formed between the centerline of the first distributor enhanced nozzle 39 and the horizontal direction is 45°-75°, the first distributor enhanced nozzle 39 includes sequentially connected enhanced nozzle inlets 39 -1. Reinforced nozzle reducer 39-2, reinforced nozzle throat 39-3, reinforced nozzle expansion section 39-4, reinforced nozzle outlet 39-5, reinforced nozzle inlet 39-1 and the main body of the first raw material distributor 8 connect;
  • the second raw material distributor 11 is provided with a second distributor gas main duct 43 extending in the radial direction of the second raw material distributor 11 and a plurality of second distributors arranged in sequence along the radial direction of the second raw material distributor 11
  • the gas annulus guide pipe 44, the second distributor tuyere 45 and the second distributor solid guide groove 46 arranged on the second distributor gas annulus guide pipe 44, each second distributor gas annulus guide
  • the flow pipe 44 is arranged to be annularly distributed around the central area of the second raw material distributor 11, and the second distributor solid guide groove 46 is located between two adjacent second distributor gas annulus guide pipes 44, and the second
  • the ratio between the width of the distributor gas annulus guide pipe 44 and the width of the second distributor solid guide groove 46 is 1:2-6;
  • Catalyst distributor 16 includes catalyst distributor main flow pipe 47 and multi-layer catalyst distribution member 48 distributed along the up and down direction of said catalyst distributor main flow pipe 47, catalyst distributor main flow pipe 47 is vertically arranged in the reaction area and is connected with The catalyst second feed port 27 communicates, and the catalyst distribution member 48 includes a plurality of catalyst first distribution conduits 49 and a plurality of catalyst second distribution conduits 50, and the catalyst first distribution conduits 49 and the catalyst second distribution conduits 50 lead along the catalyst distributor.
  • the flow pipes 47 are arranged staggered in the circumferential direction and communicate with the main flow pipe 47 of the catalyst distributor.
  • the first catalyst distribution conduit 49 and the second catalyst distribution conduit 50 are respectively provided with a plurality of catalyst outlets 51.
  • the corresponding catalyst distribution pipes of the catalyst distribution member 48 The length of the catalyst decreases successively from top to bottom, and a plurality of catalyst outlets 51 are equidistantly distributed on the catalyst first distribution conduit 49 and the catalyst second distribution conduit 50;
  • the fluidized bed reactor 7 is provided with a raw material first feed port 1 and a raw material second feed port 2, the raw material first feed port 1 communicates with the bottom of the raw material first distributor 8, and the raw material second feed port 2 Located in the confluence area of the dense phase zone 28 and the catalyst distribution zone 29, the feed ratio of the first raw material feed port 1 to the raw material second feed port 2 is 1-10:1;
  • the top of the catalyst first feeding port 24 is provided with a circulation distribution baffle 34 connected with the inner wall of the fluidized bed reactor, and the circulation distribution baffle 34 is provided with a plurality of circulation distribution baffle grooves 37, and the circulation distribution baffle groove 37
  • the angle ⁇ formed with the horizontal direction is 30°-75°;
  • the settler 9 comprises the settler lower section 17 below, the settler upper section 18 above and the settler cyclone separator 19 positioned at the settler upper section 18, the gas outlet of the settler cyclone separator 19 and the product gas outlet of the settler 9 5 connected, the lower part of the lower section 17 of the settler is provided with a settler distribution plate 12, and the top of the settler distribution plate 12 is connected to the corresponding catalyst first feed port 24 through a circulation pipe 22, and the circulation pipe 22 is provided with a circulation pipe control valve 23.
  • the top of the settler distribution plate 12 is connected to the stripper 21 through the stripper feed pipe 30, the upper section 18 of the settler is hemispherical, and the first distribution plate hole 35 of the settler and the settler distribution plate 12 are set on the settler distribution plate
  • the second distribution plate hole 36, the first distribution plate hole 35 of the settler and the second distribution plate hole 36 of the settler are respectively arranged to be annularly distributed around the central area of the settler distribution plate 12;
  • stripper 21 The outlet of stripper 21 is communicated with the regenerator feed pipe 33 of regenerator 10 by stripper discharge pipe 31, is provided with stripper control valve 32 on the stripper discharge pipe 31;
  • the regenerator 10 is provided with a regenerator gas distributor 13 and a regenerator cyclone separator 20 above the regenerator gas distributor 13.
  • the gas outlet of the regenerator cyclone separator 20 communicates with the flue gas outlet 6 of the regenerator 10, and the regeneration
  • the structural design and parameters of the gas distributor 13 of the regenerator are the same as that of the second distributor 11 of the raw material.
  • the lower part of the regenerator 10 is provided with a regenerated catalyst outlet, and the regenerated catalyst outlet communicates with the second catalyst inlet 27 through the regenerator circulation outlet pipe 26. ;
  • the top of the fluidized bed reactor 7 is provided with a lift separation pipe 15 extending into the settler 9 , and the settler 9 is provided with a riser baffle plate 14 above the outlet of the lift separation pipe 15 .
  • the specific steps of the method for preparing low-carbon olefins are:
  • step S2 the product obtained by the reaction described in step S1 and the entrained catalyst enter the settler 9 from the lifting separation pipe 15, and the product and the entrained catalyst are separated through the action of the settler cyclone separator 19, and the product gas obtained is Output from the product gas outlet 5, a part of the catalyst obtained by separation is transported to the catalyst first feed port 24 from the circulation pipe 22, so as to be directly supplied into the dense phase zone 28, and the other part enters the stripper from the stripper feed pipe 30 21, after being stripped by the stripper 21, it is transported to the regenerator 10 from the stripper discharge pipe 31 and the regenerator feed pipe 33, and the flue gas and the regenerated catalyst are obtained after being separated and regenerated by the regenerator cyclone separator 20, and the flue gas
  • the gas is discharged from the flue gas outlet 6, and the regenerated catalyst is fed into the second catalyst feed port 27 from the regenerator circulation discharge pipe 26 to be fed into the catalyst distribution area 29 and react with the gaseous raw material in the dense phase area 28.
  • a fluidized bed reactor characterized in that, the reaction zone of the fluidized bed reactor is sequentially provided with a first raw material distributor (8), a second raw material distributor (11) and a catalyst distributor (16), the catalyst distributor (16) is communicated with the second catalyst feed pipe (27), and the first raw material distributor (8) and the second raw material distributor (11) are formed as dense Phase zone (28), the area where the catalyst distributor (16) is located is formed as a catalyst distribution zone (29) communicated with the dense phase zone (28), at the reactor side of the dense phase zone (28) At least one first catalyst feed port (24) is provided on the wall.
  • the first distributor reinforcing nozzle (39) includes a reinforcing nozzle inlet (39-1), a reinforcing nozzle progressively connected in sequence Shrink tube (39-2), enhanced nozzle throat (39-3), enhanced nozzle expansion section (39-4) and enhanced nozzle outlet (39-5), said enhanced nozzle inlet (39-1) and said enhanced nozzle
  • the main body of the first material distributor (8) is connected.
  • the fluidized bed reactor according to the second series of exemplary embodiment 5 characterized in that the ratio of the diameter of the enhanced nozzle throat (39-3) to the diameter of the enhanced nozzle inlet (39-1) is 1:5-20, and the ratio between the length of the enhanced nozzle throat (39-3) and the diameter of the enhanced nozzle throat (39-3) is 5-10:1.
  • the second raw material distributor (11) is provided with (11) the radially extending second distributor gas main guide pipe (43), a plurality of second distributor gas annulus guide pipes ( 44), the second distributor tuyere (45) and the second distributor solid guide groove (46) arranged on the second distributor gas annulus guide pipe (44), each of the second distributor
  • the gas annulus guide pipe (44) of the device is arranged to be annularly distributed around the central area of the second raw material distributor (11), and the solid guide groove (46) of the second distributor is located at two adjacent between the second distributor gas annulus guide tubes (44).
  • the catalyst distributor (16) comprises a catalyst distributor main flow pipe (47) and a multi-layer A catalyst distribution system (48) distributed along the up and down direction of the main flow pipe (47) of the catalyst distributor, the main flow pipe (47) of the catalyst distributor is vertically arranged in the reaction area and connected to the second catalyst
  • the feed pipe (27) communicates, and the catalyst distribution system (48) includes a plurality of first catalyst distribution conduits (49) and a plurality of second catalyst distribution conduits (50), and the first catalyst distribution conduit (49) is connected to
  • the second catalyst distribution conduits (50) are circumferentially staggered along the catalyst distributor main flow pipe (47) and are all communicated with the catalyst distributor main flow conduits (47), and the first catalyst distribution conduits ( 49) and the second catalyst distribution conduit (50) are respectively provided with a plurality of catalyst outlets (51).
  • the fluidized bed reactor according to any one of the second series of exemplary embodiments 1 to 6, characterized in that, above the first catalyst feed port (24) there is a The circulating cloth baffle (34) connected to the inner wall of the reactor.
  • the fluidized bed reactor according to Embodiment 13 of the second series of examples characterized in that, the circulating material baffle (34) is provided with a plurality of circulating material baffle grooves (37), and the circulating material
  • the included angle ( ⁇ ) formed by the baffle groove (37) and the horizontal direction is 30°-75°.
  • a device for preparing light olefins characterized in that the device comprises a fluidized bed reactor (7) according to any one of the second series of exemplary embodiments 1 to 15, a settler (9) and A regenerator (10), the settler (9) communicates with the top of the reaction zone of the fluidized bed reactor (7), and the lower part of the settler (9) is respectively connected to the first catalyst inlet (24) communicates with the regenerator (10), and the regenerated catalyst outlet of the regenerator (10) communicates with the second catalyst feed pipe (27).
  • the central axis of the fluidized bed reactor (7) is arranged symmetrically, and the lower part of the settler (9) is connected with the first catalyst feed port (24) through a circulation pipe (22).
  • the bottom of the lower section of the settler (17) is provided with a settler distribution plate (12), the top of the settler distribution plate (12) is connected with the circulation pipe (22), and is connected with the The regenerator (10) is connected.
  • the central area of the plate (12) is distributed in a ring shape, and the size ratio of the distribution plate holes (35) of the first settler and the distribution plate holes (36) of the second settler is 1-3:4.
  • regenerator gas distributor (13) is arranged inside the regenerator (10) and a regenerator gas
  • the regenerator gas distributor (13) is provided with a regenerator gas main flow pipe extending radially along the regenerator gas distributor (13), a plurality of pipes along the regenerator gas distributor (13)
  • the regenerator gas annular gap guide tube arranged in radial order, the regenerator tuyere and the regenerator solid guide groove arranged on the regenerator gas annular gap guide tube, each of the regenerator gas annular gap guide
  • the pipes are arranged to be annularly distributed around the central area of the regenerator gas distributor (13), and the regenerator solid guide groove is located between two adjacent regenerator gas annular gap guide pipes.
  • the settler separates the product from the entrained catalyst, and feeds a part of the separated catalyst directly into the dense phase zone from the first catalyst feed port, and another part through the After the regenerator is regenerated, it is fed into the catalyst distribution area from the second catalyst feed pipe.
  • the preparation of low-carbon olefins is carried out by using the relatively preferred specific embodiments of the above-mentioned device for preparing low-carbon olefins and the specific steps of the method for preparing low-carbon olefins;
  • FIG. 1 there are four catalyst first feed ports 24 in the device for preparing light olefins, and the structure of the first raw material distributor 8 is shown in FIG. 3 and FIG. 4 , and the porosity is 1%.
  • the angle interval formed between the reducer pipe 39-2 of the enhanced nozzle and the horizontal direction is 45°
  • the angle interval between the enlarged section 39-4 of the enhanced nozzle and the horizontal direction is 70°
  • the diameter ratio of 39-1 is 1:10
  • the ratio between the length of the reinforced nozzle throat 39-3 and the diameter of the reinforced nozzle throat 39-3 is 8:1.
  • the porosity of the first distributor reinforcement area 38 is 0.2%, and the hole diameter is 2 mm.
  • the opening ratio of the outer area 42 of the first distributor and the central area 40 of the first distributor are both 2%, and the apertures are both 6mm.
  • the ratio between the width of the gas annulus guide pipe 44 of the second distributor and the width of the solid guide groove 46 of the second distributor is 1:4.
  • the opening ratio of the second raw material distributor 11 is 5%, and the axial distance from the first raw material distributor 8 is 1/2.
  • the catalyst distribution member 48 adopts a dendritic arrangement scheme, which is arranged in 3 layers, and each layer is provided with 3 catalyst distribution conduits (the catalyst first distribution conduit 49 and the catalyst second distribution conduit 50 are distributed alternately), and the diameter of the effective channel of the catalyst outlet 51
  • the ratio of the distance between the centers of two adjacent catalyst outlets 51 to the width of the catalyst outlets 51 along their distribution direction is 3:1.
  • the height of the main flow pipe 47 of the catalyst distributor from the first raw material distributor (8) is 3 /4h; the lengths of the multi - layer distribution pipes are 0.75D, 0.75 2D and 0.75 3D in sequence.
  • methanol with a purity of 99.5% is used as the raw material
  • SAPO-34 is used as the catalyst
  • the stripping medium 3 of the stripper 21 is water vapor.
  • the pressure in the fluidized bed reactor 7 is 0.3MPa, the average temperature is 450°C, the temperature difference is controlled to be ⁇ 5°C, and the linear velocity is 5m/s.
  • the mass ratio of the catalyst supplied to the regenerator 10 through the second catalyst feed port 27 is 1:0.5.
  • the coke content of the regenerated catalyst obtained by the regenerator 10 is 10% by weight
  • the regeneration medium of the regenerator 10 is a mixed gas of CO and air, and the volume ratio of CO and air in the mixed gas is 0.2:1.
  • the regeneration temperature of the regenerator 10 was 650°C.
  • the ratio of the pressure drop generated when the gaseous raw material passes through the dense-phase region 28 to the pressure drop generated when the gaseous raw material passes through the catalyst distribution region 29 is 3:1.
  • the angle formed by the annular space velocity and the horizontal direction is 45, and the ratio of inner and outer porosity fluctuations is 0.95:1.
  • the distribution unevenness of the regenerated catalyst varies with height as shown in Figure 13, and the average uniformity of the three phases of the regenerated catalyst is 0.29.
  • the conversion rate of methanol is 99.995%, and the total yield (mass) of ethylene and propylene is 84.8%.
  • the difference is:
  • the structure of the first distributor 8 for raw materials is shown in Figure 2.
  • 45° the angle interval between the enlarged section 39-4 of the enhanced nozzle and the horizontal direction is 70°
  • the ratio of the diameter of the throat 39-3 of the enhanced nozzle to the diameter of the inlet 39-1 of the enhanced nozzle is 1:5
  • the throat of the enhanced nozzle 39- The ratio between the length of 3 and the diameter of the enhanced nozzle throat 39-3 is 5:1.
  • the ratio between the width of the gas annulus guide tube 44 of the second distributor and the width of the solid guide groove 46 of the second distributor is 1:2.
  • Catalyst distribution member 48 is arranged as 3 layers, and every layer is provided with 2 catalyst distribution conduits (catalyst first distribution conduit 49 and catalyst second distribution conduit 50 are distributed alternately), the diameter size of the effective channel of catalyst outlet 51 is 80mm, adjacent The ratio of the distance between the centers of two catalyst outlets 51 to the width of the catalyst outlets 51 along their distribution direction is 1.5:1.
  • the feed rate ratio of the first raw material feed port 1 to the second raw material feed port 2 is 2:1, and the distance between the circulating cloth baffle plate 34 and the catalyst first feed port 24 is the same as that of the catalyst first feed port 24.
  • the ratio of the aperture is 2: 1, the angle ⁇ formed by the circulating cloth baffle groove 37 and the horizontal direction is 30°, and the size ratio of the first distribution plate hole 35 of the settler and the second distribution plate hole 36 of the settler is 1: 4.
  • the settler cyclone separator 19 and the regenerator cyclone separator 20 are respectively arranged as a two-stage cyclone separator structure in series.
  • the raw material is methanol with a purity of 99.5%
  • the catalyst is SAPO-34
  • the pressure in the fluidized bed reactor 7 is 0.1MPa
  • the average temperature is 350°C
  • the temperature difference is ⁇ 5°C
  • the linear velocity The mass ratio of the catalyst fed into the dense phase zone 28 through the first catalyst feed port 24 to the catalyst fed into the regenerator 10 through the second catalyst feed port 27 is 1:0.2.
  • the stripping medium 3 of the stripper 21 is water vapor.
  • the coke content of the regenerated catalyst obtained by the regenerator 10 is 5% by weight
  • the regeneration medium of the regenerator 10 is a mixed gas of CO and air, and the volume ratio of CO and air in the mixed gas is 0.01:1.
  • the regeneration temperature of the regenerator 10 was 600°C.
  • the ratio of the pressure drop generated when the gaseous raw material passes through the dense-phase region 28 to the pressure drop generated when the gaseous raw material passes through the catalyst distribution region 29 is 1.5:1.
  • the angle formed by the annular space velocity and the horizontal direction is 45°-75°, and the ratio of inner and outer porosity fluctuations is 0.9-0.95:1.
  • the three-phase average homogeneity of the regenerated catalyst was 0.89.
  • the conversion rate of methanol is 99.985%, and the total yield (mass) of ethylene and propylene is 83.58%.
  • the difference is that the first catalyst feed port 24 is set to two in the device for preparing low-carbon olefins, and the structure of the first distributor 8 of raw materials is as shown in Figure 2, and the nozzle is enhanced
  • the angle interval formed by the reducer 39-2 and the horizontal direction is 45°
  • the angle interval between the enlarged section 39-4 of the enhanced nozzle and the horizontal direction is 70°
  • the diameter of the throat 39-3 of the enhanced nozzle is the same as that of the inlet 39-
  • the diameter ratio of 1 is 1:20
  • the ratio between the length of the reinforced nozzle throat 39-3 and the diameter of the reinforced nozzle throat 39-3 is 10:1.
  • the ratio between the width of the gas annulus guide pipe 44 of the second distributor and the width of the solid guide groove 46 of the second distributor is 1:6.
  • Catalyst distribution member 48 is set to 3 layers, and every layer is provided with 2 catalyst distribution conduits (catalyst first distribution conduit 49 and catalyst second distribution conduit 50 are distributed alternately), the diameter size of the effective channel of catalyst outlet 51 is 100mm, adjacent
  • the ratio of the distance between the centers of two catalyst outlets 51 to the width of the catalyst outlets 51 along their distribution direction is 5:1.
  • the feed rate ratio of the first raw material feed port 1 to the raw material second feed port 2 is 10:1, and the distance between the circulating cloth baffle plate 34 and the catalyst first feed port 24 is the same as that of the catalyst first feed port 24.
  • the ratio of the aperture is 10:1
  • the angle ⁇ formed between the circulating cloth baffle groove 37 and the horizontal direction is 75°
  • the size ratio of the first distribution plate hole 35 of the settler to the second distribution plate hole 36 of the settler is 3: 4.
  • the settler cyclone separator 19 and the regenerator cyclone separator 20 are respectively arranged as a two-stage cyclone separator structure in series.
  • the raw material is methanol with a purity of 99.5%
  • the catalyst is SAPO-34
  • the pressure in the fluidized bed reactor 7 is 0.5MPa
  • the average temperature is 560°C
  • the temperature difference is ⁇ 5°C
  • the linear velocity The mass ratio of the catalyst fed into the dense phase zone 28 through the first catalyst feed port 24 to the catalyst fed into the regenerator 10 through the second catalyst feed port 27 is 1:1.
  • the stripping medium 3 of the stripper 21 is water vapor.
  • the coke content of the regenerated catalyst obtained by the regenerator 10 is 15% by weight
  • the regeneration medium of the regenerator 10 is a mixed gas of CO and air, and the volume ratio of CO and air in the mixed gas is 0.5:1.
  • the regeneration temperature of the regenerator 10 was 750°C.
  • the ratio of the pressure drop generated when the gaseous raw material passes through the dense-phase region 28 to the pressure drop generated when the gaseous raw material passes through the catalyst distribution region 29 is 4:1.
  • the angle formed by the annular space velocity and the horizontal direction is 45°-75°, and the ratio of inner and outer porosity fluctuations is 0.9-0.95:1.
  • the conversion rate of methanol is 99.981%, and the total yield (mass) of ethylene and propylene is 83.14%.
  • the difference is that the first distributor 8 of the raw material is only provided with the tuyere 41 in the central area of the first distributor, and the first distributor corresponding to the first feed port 24 of the catalyst is not provided.
  • the enhanced area 38 and the first distributor enhance the spray head 39 .
  • the conversion rate of methanol is 99.98%, and the total yield (mass) of ethylene and propylene is 82.65%.
  • the difference is that the angle formed between the reducing pipe 39-2 of the reinforcing nozzle and the horizontal direction on the raw material first distributor 8 is 90°, and the enlarged section 39-4 of the reinforcing nozzle is connected to the horizontal direction.
  • the angle formed by the directions is 90°.
  • the conversion rate of methanol is 99.96%, and the total yield (mass) of ethylene and propylene is 80.61%.
  • the difference is that only a plurality of openings are provided on the second raw material distributor 11 .
  • the conversion rate of methanol is 99.959%, and the total yield (mass) of ethylene and propylene is 80.68%.
  • the difference is that the ratio between the width of the gas annulus guide pipe 44 of the second distributor and the width of the solid guide groove 46 of the second distributor is 2:1.
  • the conversion rate of methanol is 99.978%, and the total yield (mass) of ethylene and propylene is 80.61%.
  • the catalyst distributor 16 comprises a main flow pipe 47 of the catalyst distributor, and the main flow pipe 47 of the catalyst distributor is vertically arranged in the reaction area and is connected to the second feed port 27 of the catalyst.
  • the main flow pipe 47 of the catalyst distributor is provided with a plurality of vertically arranged openings.
  • the conversion rate of methanol is 99.977%, and the total yield (mass) of ethylene and propylene is 82.45%.
  • the difference is that the first raw material feed port 1 and the second raw material feed port 2 are both communicated with the bottom of the first raw material distributor 8 .
  • the conversion rate of methanol is 99.95%, and the total yield (mass) of ethylene and propylene is 81.7%.
  • the difference is that the feed ratio of the first raw material feed port 1 to the raw material second feed port 2 is 1:5.
  • the conversion rate of methanol is 99.975%, and the total yield (mass) of ethylene and propylene is 82.75%.
  • the difference is that no circulation distribution baffle 34 is provided above the first catalyst feed port 24 .
  • the conversion rate of methanol is 99.945%, and the total yield (mass) of ethylene and propylene is 81.71%.
  • the difference is that the circulating cloth baffle groove 37 is not provided on the circulating cloth baffle 34 .
  • the conversion rate of methanol is 99.94%, and the total yield (mass) of ethylene and propylene is 81.63%.
  • the difference is that only a plurality of settler first distribution plate holes 35 are provided on the settler distribution plate 12 .
  • the conversion rate of methanol is 99.965%, and the total yield (mass) of ethylene and propylene is 82.5%.
  • the difference is that the regeneration medium of the regenerator 10 is air.
  • the conversion rate of methanol is 99.974%, and the total yield (mass) of ethylene and propylene is 81.55%.
  • the difference is that the regeneration medium of the regenerator 10 is a mixture of CO 2 and air, and the volume ratio of CO 2 and air in the mixture is 0.7:1.
  • the conversion rate of methanol is 99.975%, and the total yield (mass) of ethylene and propylene is 82.53%.
  • the difference is that the first raw material distributor 8 , the second raw material distributor 11 and the catalyst distributor 16 are not set in the fluidized bed reactor 7 . Only the first catalyst feed port 24 and the second catalyst feed port 27 are respectively communicated with the reaction area of the fluidized bed reactor 7 .
  • the conversion rate of methanol is 99.91%, and the total yield (mass) of ethylene and propylene is 80.05%.
  • the difference is that only the first raw material distributor 8 is installed in the fluidized bed reactor 7, and the second raw material distributor 11 and the catalyst distributor 16 are not installed. Connect the first catalyst feed port 24 and the second catalyst feed port 27 to the top of the first raw material distributor 8 respectively.
  • the fluidized bed reactor 7 is provided with a first raw material feed port 1 communicating with the bottom of the first raw material distributor 8 .
  • the conversion rate of methanol is 99.93%, and the total yield (mass) of ethylene and propylene is 81.01%.
  • the difference is that the first distributor 8 of raw material and the second distributor 11 of raw material are arranged in the fluidized bed reactor 7; but the catalyst distributor 16 is not provided, but the regenerated catalyst Side feed as usual. Connect the first catalyst feed port 24 and the second catalyst feed port 27 to the top of the first raw material distributor 8 respectively.
  • the fluidized bed reactor 7 is provided with a first raw material feed port 1 communicating with the bottom of the first raw material distributor 8 .
  • the conversion rate of methanol was 99.84%, and the total yield (mass) of ethylene and propylene was 78.5%.

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Abstract

一种流化床反应器和制备低碳烯烃的装置以及制备低碳烯烃的方法。流化床反应器的反应区域从下至上依次设置有原料第一分布器(8)、原料第二分布器(11)和催化剂分布器(16)，催化剂分布器(16)与催化剂第二进料口(27)连通，原料第一分布器(8)与原料第二分布器(11)之间形成为密相区(28)，催化剂分布器(16)所在的区域形成为与密相区(28)连通的催化剂分布区(29)，在密相区(28)的反应器侧壁上设置有至少一个催化剂第一进料口(24)。

Description

流化床反应器和制备低碳烯烃的装置以及制备低碳烯烃的方法 技术领域
本发明涉及烯烃制备领域，具体地，涉及一种流化床反应器，制备低碳烯烃的装置，以及制备低碳烯烃的方法。
背景技术
低碳烯烃，即乙烯和丙烯，是两种重要的基础化工原料，其需求量在不断增加。一般地，乙烯、丙烯通过石油路线来生产，但由于石油资源有限的供应量及较高的价格，由石油资源生产乙烯、丙烯的成本不断增加。近年来，人们开始大力发展替代原料转化制乙烯、丙烯的技术。其中，一类重要的用于低碳烯烃生产的替代原料是含氧化合物，例如醇类(甲醇、乙醇)、醚类(二甲醚、甲乙醚)、酯类(碳酸二甲酯、甲酸甲酯)等，这些含氧化合物可以通过煤、天然气、生物质等能源转化而来。某些含氧化合物已经可以达到较大规模的生产，如甲醇，可以由煤或天然气制得，工艺十分成熟，可以实现上百万吨级的生产规模。由于含氧化合物来源的广泛性，以及转化生成低碳烯烃工艺的经济性，所以由含氧化合物转化制烯烃(OTO)的工艺，特别是由甲醇转化制烯烃(MTO)的工艺受到越来越多的重视。
目前含氧物制烯烃的装置与催化裂化装置相似，均为连续反应-再生方式。在PCT申请WO2018072139A1中公布了一种由含氧化合物制备丙烯和C4烃类的湍动流化床反应器、装置及方法，该技术方案在湍动流化床反应器的反应区设置n个反应器进料分布器，含氧化合物浓度较为均匀，削弱MTO反应对烯烃烷基化反应的抑制，再生催化剂直接进入反应区底部，有利于乙烯、丙烯和甲醇的烷基化反应。
公开号为CN108794294A和CN108786669A的中国专利申请分别记载了一种流化床分布器及包括该流化床分布器的流化床反应器，该流化床分布器包括第一分布器和第二分布器，所述第一分布器位于流化床底部，所述第二分布器位于第一分布器的气体流向下游的至少一个区域，通过不同原料物流在不同区域分布进料，实现传质控制，进而协调优化共进料体系。
公开号为CN107235821A的中国专利申请记载了一种甲醇制烯烃 的装置，在流化床反应器的反应区内设置第一外循环催化剂分布器和催化剂第一再分配器，以及在再生区内设置第二外循环催化剂分布器、低活性催化剂分布器、冷后催化剂分布器和催化剂第二再分配器，不仅能保证反应物和催化剂的温度及活性均匀分布，且能保证反应气体与催化剂的接触效果。
在现有技术中，流化床反应器内仍存在再生催化剂分布不均匀的现象，导致床层温度波动较大，对双烯的选择影响较大；此外，再生过程主要采用空气为再生气体，通过调节再生进料气中辅助气体的量，防止再生过程出现“飞温”现象，但是，这种方法会产生大量的温室气体CO 2，不利于环境保护，若利用空气烧炭对催化剂进行部分再生，其烧炭速率较快，不利于催化剂残炭量的控制，增加操作过程中的难度。
发明内容
本发明的目的是克服现有的制备低碳烯烃的装置中存在中催化剂分布不均匀、再生热量利用不充分和低碳烯烃收率低的问题，提供一种流化床反应器和制备低碳烯烃的装置以及制备低碳烯烃的方法。
本发明第一方面提供了一种流化床反应器，其包括：
在该流化床反应器的反应区域从下至上依次设置有第一中的原料第一分布器、第二原料第二分布器和催化剂分布器，其用于对气体原料进行分布，其中所述原料第一分布器在原料第二分布器下方；其中所述原料第一分布器和原料第二分布器具有相同或不同的开孔率，各自独立地为0.05-5％；
在该流化床反应器底部的原料第一进口，其使得原料的至少一部分经由所述原料第一分布器和原料第二分布器依次进行两次分布；
所述催化剂分布器包括催化剂分布器主导流管，其与所述原料第一分布器和原料第二分布器同轴分布，其中所述催化剂分布器主导流管从下往上穿越所述原料第一分布器和原料第二分布器催化剂第二催化剂第一。
本发明第二方面提供了一种制备低碳烯烃的装置，该装置包括本发明所述的流化床反应器、沉降器和再生器，反应器侧壁上设置有至少一个用于将催化剂第一进料至所述原料第一分布器与所述原料第二分布器之间的催化剂第一进料口，所述反应器底部设置有用于将催化 剂第二进料的进料至所述分布器主导流管的催化剂第二进料口；其中：所述沉降器与所述流化床反应器的反应区域的上方连通，所述沉降器的下部分别与所述催化剂第一进料口和所述再生器连通，所述再生器的再生催化剂出口与所述催化剂第二进料口连通。
本发明第三方面提供了一种制备低碳烯烃的方法，其使用了本发明所述的制备低碳烯烃的装置，该方法包括：
将气态原料和催化剂在流化床反应器的反应区域内进行反应；
将得到的产物和被夹带的催化剂经所述反应区域的上方送入沉降器；
所述沉降器将所述产物和所述被夹带的催化剂分离开，并且将分离得到的催化剂的一部分从所述催化剂第一进料口直接供入在所述原料第一分布器(8)与所述原料第二分布器(11)之间形成的密相区内，另一部分经所述再生器再生后从所述催化剂第二进料口供入所述催化剂分布区内。
根据本发明提供的所述流化床反应器和所述制备低碳烯烃的装置，通过在流化床反应器的反应区域内设置原料第一分布器、原料第二分布器和催化剂分布器，以形成密相区和催化剂分布区，使得从催化剂第一进料口供入的未再生的循环催化剂能够直接进入密相区，与反应原料进行接触反应，催化剂第二进料口供入的再生催化剂进入流化床反应器后则经催化剂分布器作用，在催化剂分布区进行预分配，以能够在流场的作用下实现能量传递和反应，进而使得再生催化剂分布更加均匀，实现对再生催化剂的颗粒混合控制，提高流化床反应器内的反应效率；
根据本发明提供的所述流化床反应器和所述制备低碳烯烃的装置，反应原料通过原料第一分布器与原料第二分布器进行分层进入反应区域，实现对流化床反应器的分段流场控制，能够有效实现催化剂与反应原料的充分接触，有效消除流化状态不佳、低碳烯烃选择性不高的缺陷，进一步提高反应效率，有利于提高低碳烯烃的收率。
本发明的其它特征和优点将在随后的具体实施方式部分予以详细说明。
本发明由此提供了以下的第一系列的例示实施方案：
1、一种流化床反应器，包括：
在该流化床反应器的反应区域中的原料第一分布器(8)、原料第二分布器(11)和催化剂分布器(16)，其用于对气体原料进行分布，其中所述原料第一分布器(8)在原料第二分布器(11)下方；其中所述原料第一分布器(8)和原料第二分布器(11)具有相同或不同的开孔率，各自独立地为0.05-5％；
在该流化床反应器底部的原料第一进口(1)，其使得原料的至少一部分经由所述原料第一分布器(8)和原料第二分布器(11)依次进行两次分布；
所述催化剂分布器(16)包括催化剂分布器主导流管(47)，其与所述原料第一分布器(8)和原料第二分布器(11)同轴分布，其中所述催化剂分布器主导流管(47)从下往上穿越所述原料第一分布器(8)和原料第二分布器(11)。
2、根据第一系列例示实施方案1所述的流化床反应器，其特征在于，所述流化床反应器具有在所述原料第一进口(1)上方、且从下往上依次布置的一个或多个原料第Y进料口，其中Y是≥2的正整数，条件是当存在所述一个或多个原料第Y进料口时，所述原料第一进口和所述原料第Y进料口的布置使得原料第Y进料口的进料量与原料第(Y-1)进料口进料量比为1∶1-10。
3、根据第一系列例示实施方案1所述的流化床反应器，其特征在于，在所述原料第一分布器(8)与所述原料第二分布器(11)之间的反应器侧壁上设置有至少一个催化剂第一进料口(24)；以及
所述原料第一分布器(8)包括第一分布器中心区域(40)和位于所述第一分布器中心区域(40)外周的第一分布器外部环形区域(42)，所述第一分布器外部环形区域(42)上设置有与所述催化剂第一进料口(24)的径向位置相对应的第一分布器增强区域(38)，该第一分布器增强区域(38)具有相对于原料第一分布器(8)的其它区域来说减小的孔径，以使得催化剂在所述原料第一分布器(8)和所述原料第二分布器(11)之间具有径向上基本均匀的分布。
4、根据第一系列例示实施方案3所述的流化床反应器，其特征在于，所述第一分布器中心区域(40)是半径为r的圆形，第一分布器外部区域(42)是外径和内径之差为d的圆环，其中r/d＝1/2～3/5，r+d＝D，该D为所述流化床反应器的内径；第一分布器增强区域(38)面积设 置为与第一分布器外部区域(42)面积之比为1/10～1/2。
5、根据第一系列例示实施方案3所述的流化床反应器，其特征在于，所述原料第一分布器(8)除所述第一分布器增强区域(38)之外的区域的开孔率为1.5-10％，优选2-5％，孔径为2-30mm，优选各孔之间的孔径相差不超过±10％；所述第一分布器增强区域(38)的开孔率为0.01～1.5％，孔径为0.1～20mm，优选各孔之间的孔径相差不超过±10％。
6、根据第一系列例示实施方案3所述的流化床反应器，其特征在于，所述第一分布器增强区域(38)上设置有多个呈柱状的第一分布器增强喷头(39)，所述第一分布器增强喷头(39)的中心线与水平方向形成的夹角为45°-75°。
7、根据第一系列例示实施方案6所述的流化床反应器，其特征在于，所述第一分布器增强喷头(39)包括依次连接的增强喷头进口(39-1)、增强喷头渐缩管(39-2)、增强喷头管喉(39-3)、增强喷头扩大段(39-4)和增强喷头出口(39-5)，所述增强喷头进口(39-1)与所述原料第一分布器(8)的主体连接；其中
增强喷头渐缩管(39-2)与水平方向形成的夹角区间为30°-70°，增强喷头扩大段(39-4)与水平方向形成的夹角区间为30°-70°，所述增强喷头管喉(39-3)的直径与所述增强喷头进口(39-1)的直径比例为1∶5-20，所述增强喷头管喉(39-3)的长度与该增强喷头管喉(39-3)的直径之间的比例为5-10∶1。
8、根据第一系列例示实施方案1至7中任一项所述的流化床反应器，其特征在于，所述流化床反应器从所述原料第一分布器(8)向上至直径缩减前的区段具有高度h，所述原料第二分布器(11)设置在距离所述原料第一分布器(8)轴向相距1/4～1/2h处。
9、根据第一系列例示实施方案8所述的流化床反应器，其特征在于，所述原料第二分布器(11)的开孔率为0.05-5％，优选3-5％，孔径为1-30mm，优选各孔之间的孔径相差不超过±10％。
10、根据第一系列例示实施方案8所述的流化床反应器，其特征在于，所述原料第二分布器(11)上设置有沿所述原料第二分布器(11)的径向延伸的第二分布器气体主导流管(43)、多个沿所述原料第二分布器(11)的径向依次设置的第二分布器气体环隙导流管(44)、设置在所述第二分布器气体环隙导流管(44)上的第二分布器风口(45) 和第二分布器固体导流槽(46)，每个所述第二分布器气体环隙导流管(44)设置为绕所述原料第二分布器(11)的中心区域呈环形分布，所述第二分布器固体导流槽(46)位于相邻的两个所述第二分布器气体环隙导流管(44)之间；其中流化床反应器具有原料第二进料口(2)，其与所述第二分布器气体主导流管(43)流体连通。
11、根据第一系列例示实施方案10所述的流化床反应器，其特征在于，所述第二分布器气体环隙导流管(44)的宽度与所述第二分布器固体导流槽(46)的宽度之间的比例为1∶2-6。
12、根据第一系列例示实施方案1至7中任一项所述的流化床反应器，其特征在于，所述催化剂分布器主导流管(47)从下往上穿越所述原料第一分布器(8)和原料第二分布器(11)，所述流化床反应器从所述原料第一分布器(8)向上至直径缩减前的区段具有高度h，所述催化剂分布器主导流管(47)从所述原料第一分布器(8)起向上的高度为h1，则1/4h＜h1≤3/4h。
13、根据第一系列例示实施方案12所述的流化床反应器，其特征在于，所述催化剂分布器(16)包括沿所述催化剂分布器主导流管(47)的上下方向分布的多层催化剂分布构件(48)，所述催化剂分布构件(48)在径向延伸，以使得沿所述催化剂分布器主导流管(47)轴向输送的催化剂能够在流化床反应器内部沿径向分配。
14、根据第一系列例示实施方案13所述的流化床反应器，其特征在于，
15、根据第一系列例示实施方案13所述的流化床反应器，其特征在于，所述催化剂分布构件(48)包括多个催化剂第一分布导管(49)和多个催化剂第二分布导管(50)，所述催化剂第一分布导管(49)与所述催化剂第二分布导管(50)沿所述催化剂分布器主导流管(47)环向交错分布且均与所述催化剂分布器主导流管(47)连通，所述催化剂第一分布导管(49)与所述催化剂第二分布导管(50)分别设置有多个催化剂出口(51)；其中
每层催化剂分布构件(48)中催化剂分布导管的数量为X个(X≥2)，多个催化剂分布导管圆周角度间距为180°/X分布；催化剂出口(51)具有选自正方形、圆形和多变形的形状。。
16、根据第一系列例示实施方案14所述的流化床反应器，其特征 在于，所述催化剂分布构件(48)的数量优选为M层(M≥3)，催化剂分布构件(48)由上至下依次为第1层、第2层、......第M层；其中第n层催化剂分布构件(48)中催化剂分布导管的长度为(0.7-0.9) n*D/2，D为反应器内径，n为对应的层数。
17、根据第一系列例示实施方案14所述的流化床反应器，其特征在于，所述催化剂第一分布导管(49)和所述催化剂第二分布导管(50)上的所述催化剂出口(51)等距分布。
18、根据第一系列例示实施方案3至7中任意一项所述的流化床反应器，其特征在于，所述催化剂第一进料口(24)的上方设置有与所述流化床反应器的内壁连接的循环布料挡板(34)。
19、根据第一系列例示实施方案18所述的流化床反应器，其特征在于，所述循环布料挡板(34)和所述催化剂第一进料口(24)之间的距离与所述催化剂第一进料口(24)的孔径的比例为1-10∶1。
20、根据第一系列例示实施方案18所述的流化床反应器，其特征在于，所述循环布料挡板(34)上设置有多个循环布料挡板槽(37)，所述循环布料挡板槽(37)与水平方向形成的夹角(α)为30°-75°。
21、一种制备低碳烯烃的装置，其特征在于，该装置包括根据第一系列例示实施方案1至19中任意一项所述的流化床反应器(7)、沉降器(9)和再生器(10)，反应器侧壁上设置有至少一个用于将催化剂第一进料至所述原料第一分布器(8)与所述原料第二分布器(11)之间的催化剂第一进料口(24)，所述反应器底部设置有用于将催化剂第二进料的进料至所述分布器主导流管(47)的催化剂第二进料口(27)；其中：
所述沉降器(9)与所述流化床反应器(7)的反应区域的上方连通，所述沉降器(9)的下部分别与所述催化剂第一进料口(24)和所述再生器(10)连通，所述再生器(10)的再生催化剂出口与所述催化剂第二进料口(27)连通。
22、根据第一系列例示实施方案21所述的装置，其特征在于，所述催化剂第一进料口(24)的数量为k个，k≥2，且优选k≤12；各所述催化剂第一进料口(24)中心线夹角为360°/k。
23、根据第一系列例示实施方案22所述的装置，其特征在于，所述沉降器(9)内设置有沉降器下段(17)、处于所述沉降器下段(17) 上方的沉降器上段(18)和位于所述沉降器上段(18)的沉降器旋风分离器(19)，所述沉降器旋风分离器(19)的气体出口与所述沉降器(9)的产品气出口(5)连通，所述沉降器下段(17)的下部设置有沉降器分布板(12)，并所述沉降器分布板(12)的下方通过循环管(22)与所述催化剂第一进料口(24)连接，且通过汽提器(21)与所述再生器(10)连接。
24、根据第一系列例示实施方案23所述的装置，其特征在于，所述沉降器分布板(12)上设置沉降器第一分布板孔(35)和沉降器第二分布板孔(36)，所述沉降器第一分布板孔(35)与所述沉降器第二分布板孔(36)分别设置为绕所述沉降器分布板(12)的中心区域呈环形分布，所述沉降器第一分布板孔(35)与所述沉降器第二分布板孔(36)的尺寸比为1-3∶4。
25、根据第一系列例示实施方案21至24中任意一项所述的装置，其特征在于，所述流化床反应器(7)的顶部设置有伸入所述沉降器(9)内的提升分离管(15)，所述沉降器(9)内设置有位于所述提升分离管(15)的出口上方的提升管挡板(14)。
26、在第一系列例示实施方案21-24任一项所述的装置中制备低碳烯烃的方法，包括：
将气态原料和催化剂在流化床反应器的反应区域内进行反应；
将得到的产物和被夹带的催化剂经所述反应区域的上方送入沉降器；
所述沉降器将所述产物和所述被夹带的催化剂分离开，并且将分离得到的催化剂的一部分从所述催化剂第一进料口直接供入在所述原料第一分布器(8)与所述原料第二分布器(11)之间形成的密相区内，另一部分经所述再生器再生后从所述催化剂第二进料口供入所述催化剂分布区内。
27、根据第一系列例示实施方案26所述的方法，其特征在于，所述密相区中的物料线速为1-10m/s。
28、根据第一系列例示实施方案26所述的方法，其特征在于，所述分离得到的催化剂中，供入所述密相区内的部分与供入所述再生器的部分质量比为1∶0.2-1。
29、根据第一系列例示实施方案26所述的方法，其特征在于，所 述气态原料在经过所述密相区时产生的压降与所述气态原料经过所述催化剂分布区时产生的压降之比1.5-4∶1。
30、根据第一系列例示实施方案26所述的方法，其特征在于，所述气态原料经过所述原料第一分布器后，环隙空间速度与水平方向形成的夹角为45°-75°，内外孔隙率波动之比为0.9-0.95∶1。
附图说明
附图是用来提供对本发明的进一步理解，并且构成说明书的一部分，与下面的具体实施方式一起用于解释本发明，但并不构成对本发明的限制。在附图中：
图1是本发明所述的制备低碳烯烃的一种具体实施方式的装置的示意图；
图2是本发明所述的制备低碳烯烃的装置中原料第一分布器的一种具体实施方式的结构示意图；
图3是本发明所述的制备低碳烯烃的装置中原料第一分布器的另一种具体实施方式的结构示意图；
图4是本发明所述的制备低碳烯烃的装置中第一分布器增强喷头的一种具体实施方式的结构示意图；
图5是本发明所述的制备低碳烯烃的装置中原料第二分布器的一种具体实施方式的结构示意图；
图6是本发明所述的制备低碳烯烃的装置中催化剂分布器的一种具体实施方式的结构示意图；
图7是本发明所述的制备低碳烯烃的装置中催化剂分布器的另一种具体实施方式的结构示意图；
图8是本发明所述的制备低碳烯烃的装置中循环布料挡板设置为两个时在流化床反应器内的分布图；
图9是本发明所述的制备低碳烯烃的装置中循环布料挡板设置为四个时在流化床反应器内的分布图；
图10是本发明所述的制备低碳烯烃的装置中循环布料挡板的一种具体实施方式的结构示意图；
图11是本发明所述的催化剂分布器的例示结构示意图；
图12是本发明所述的制备低碳烯烃的装置中沉降器分布板的一种 具体实施方式的结构示意图；
图13是本发明所实施例1再生催化剂分布的不均匀度随高度的变化示意图；
图14是本发明所实施例1和对比例3中再生催化剂分布的不均匀度随高度的变化对比图。
部分附图标记说明
1、原料第一进料口             2、原料第二进料口
3、汽提介质                   4、再生器气体
5、产品气出口                 6、烟气出口
7、流化床反应器               8、原料第一分布器
9、沉降器                     10、再生器
11、原料第二分布器            12、沉降器分布板
13、再生器气体分布器          14、提升管挡板
15、提升分离管                16、催化剂分布器
17、沉降器下段                18、沉降器上段
19、沉降器旋风分离器          20、再生器旋风分离器
21、汽提器                    22、循环管
23、循环管控制阀              24、催化剂第一进料口
25、再生器循环出料管控制阀    26、再生器循环出料管
27、催化剂第二进料口          28、密相区
29、催化剂分布区              30、汽提器进料管
31、汽提器出料管              32、汽提器控制阀
33、再生器进料管              34、循环布料挡板
35、沉降器第一分布板孔        36、沉降器第二分布板孔
37、循环布料挡板槽            38、第一分布器增强区域
39、第一分布器增强喷头        39-1、增强喷头进口
39-2、增强喷头渐缩管          39-3、增强喷头管喉
39-4、增强喷头扩大段          39-5、增强喷头出口
40、第一分布器中心区域        41、第一分布器中心区域风口
42、第一分布器外部环形区域    43、第二分布器气体主导流管
44、第二分布器气体环隙导流管  45、第二分布器风口
46、第二分布器固体导流槽        47、催化剂分布器主导流管
48、催化剂分布构件              49、催化剂第一分布导管
50、催化剂第二分布导管          51、催化剂出口
α、循环布料挡板槽与水平方向形  R、循环布料挡板的半径。
成的夹角
具体实施方式
以下对本发明的具体实施方式进行详细说明。应当理解的是，此处所描述的具体实施方式仅用于说明和解释本发明，并不用于限制本发明。
在本文中，除非有其他说明，本文关于各个方面、各个系列和/或各个实施方案所提到的所有技术特征以及优选特征可以相互组合形成新的技术方案。
在本文中，除非有其他说明，实施例中记载的具体步骤、具体数值以及具体物质可与说明书其它部分的其他特征结合。例如，说明书发明内容或具体实施方式部分提到反应的温度为10-100℃，而实施例记载的具体反应温度为20℃，那么可以认为本文已经具体公开了10-20℃的范围，或者20-100℃的范围，且该范围可以与说明书其它部分的其他特征结合起来形成新的技术方案。
在本文中所披露的范围的端点和任何值都不限于该精确的范围或值，这些范围或值应当理解为包含接近这些范围或值的值。对于数值范围来说，各个范围的端点值之间、各个范围的端点值和单独的点值之间，以及单独的点值之间可以彼此组合而得到一个或多个新的数值范围，这些数值范围应被视为在本文中具体公开。
在本发明中，在未作相反说明的情况下，使用的方位词如“上、下”通常是指参考附图所示的上、下；“内、外”是指相对于各部件本身的轮廓的内、外。
在本文中，除非有其他说明，术语“包括”、“包含”、“含有”、“具有”和类似措词表示开放式，但是也应当理解为同时明确公开了封闭式的情形。例如，“包括”表示还可以包含没有列出的其他要素，但是也同时明确公开了仅包括所列出的要素的情形。
在本文中，所述“气体原料”具有本领域公知的含义。特别地，本发 明所述用于流化床反应器的气体原料中可以视情况含有一定量的液体，尤其是例如以分散的液滴状态存在，只要该液体的存在不会实质阻碍所述所述流化床的流化状态即可。
如图1所示，本发明第一方面所述的流化床反应器7的反应区域从下至上依次设置有原料第一分布器8、原料第二分布器11和催化剂分布器16，催化剂分布器16与催化剂第二进料口27连通，原料第一分布器8与原料第二分布器11之间形成为密相区28，催化剂分布器16所在的区域形成为与密相区28连通的催化剂分布区29，在密相区28的反应器侧壁上设置有至少一个催化剂第一进料口24。
根据本发明，通过在流化床反应器7的反应区域内设置原料第一分布器8、原料第二分布器11和催化剂分布器16，以在反应区域形成密相区28和催化剂分布区29，使得从催化剂第一进料口24供入的催化剂能够直接进入密相区28，与反应原料进行接触反应，催化剂第二进料口27供入的催化剂进入流化床反应器7后则经催化剂分布器16作用，在催化剂分布区29进行预分配，以能够在流场的作用下实现能量传递和反应，进而使得催化剂分布更加均匀，实现对催化剂的颗粒混合控制，提高流化床反应器7内的反应效率；反应原料通过原料第一分布器8与原料第二分布器11进行分层进入反应区域，实现对流化床反应器7的分段流场控制，能够有效实现催化剂与反应原料的充分接触，进一步提高反应效率，有利于提高低碳烯烃的收率。
本发明中，流化床反应器7的催化剂第一进料口24与催化剂第二进料口27可以用于供入相同的催化剂或者不同的催化剂；在流化床反应器7应用于制备低碳烯烃的装置时，催化剂第一进料口24可以用于供入未再生的循环催化剂，催化剂第二进料口27用于供入再生催化剂。
作为本发明所述的流化床反应器中原料第一分布器8的一种具体实施方式，参见图2至图4，原料第一分布器8包括第一分布器中心区域40和位于第一分布器中心区域40外周的第一分布器外部环形区域42，第一分布器外部环形区域42上设置有与催化剂第一进料口24的径向位置相对应的第一分布器增强区域38。
参见图2和图3，该第一分布器增强区域38具有相对于原料第一分布器8的其它区域来说减小的孔径，以使得催化剂在所述原料第一分布器8和所述原料第二分布器11之间具有径向上基本均匀的分布。 优选地，第一分布器增强区域38与催化剂第一进料口24一一对应设置，以使得第一分布器增强区域38能够将其接收到的反应原料与催化剂第一进料口24供入的催化剂进行快速混合作用。
在优选情况下，催化剂第一进料口24位于其对应的第一分布器增强区域38的外边缘中心的上方，以进一步提升第一分布器增强区域38对反应原料与催化剂第一进料口24供入的催化剂进行均匀混合的效果。更优选地，第一分布器增强区域38的面积可以设置为与第一分布器外部环形区域42的面积之比为1/10～1/2。
在一个实施方案中，所述第一分布器中心区域40是半径为r的圆形，第一分布器外部区域42是外径和内径之差为d的圆环，其中r/d＝1/2～3/5，r+d＝D，该D为所述流化床反应器的内径；第一分布器增强区域38面积为第一分布器外部区域42面积的1/N，N为2、3......的自然数。
在一个实施方案中，所述原料第一分布器8除所述第一分布器增强区域(38)之外的区域的开孔率为1.5-10％，优选2-5％，孔径为2-30mm，优选各孔之间的孔径相差不超过±10％；所述第一分布器增强区域38的开孔率为0.05～1.5％，孔径为0.1～20mm，优选各孔之间的孔径相差不超过±10％。
根据本发明，第一分布器中心区域40上的第一分布器中心区域风口41可以是圆形、三角形、正方形以及六边形等，有效直径为0.1-10mm，开孔率为0.05-5％。
进一步优选地，第一分布器增强区域38设置有多个呈柱状的第一分布器增强喷头39，第一分布器增强喷头39的中心线与水平方向形成的夹角为45°-75°，第一分布器增强喷头39能够将其分布的反应原料与催化剂第一进料口24供入的催化剂形成更强的混合作用力。第一分布器增强喷头39的有效直径可以设置为0.1-10mm，开孔率为0.05-5％；第一分布器外部环形区域42上未与催化剂第一进料口24对应的区域(即未设置为第一分布器增强区域38的区域)的分布孔，与第一分布器中心区域风口41的尺寸及开孔率相同。
作为本发明中第一分布器增强喷头39的一种优选实施方式，参见图4，第一分布器增强喷头39包括依次连接的增强喷头进口39-1、增强喷头渐缩管39-2、增强喷头管喉39-3、增强喷头扩大段39-4和增强 喷头出口39-5，增强喷头进口39-1与原料第一分布器8的主体连接。通入原料第一分布器8原料经增强喷头进口39-1进入，依次经增强喷头渐缩管39-2、增强喷头管喉39-3、增强喷头扩大段39-4传输后，经增强喷头出口39-5喷出。
具体地，增强喷头渐缩管39-2与水平方向形成的夹角区间在30°-70°，增强喷头扩大段39-4与水平方向形成的夹角区间在30°-70°，增强喷头管喉39-3的直径与增强喷头进口39-1的直径比例为1∶5-20，增强喷头管喉39-3的长度与该增强喷头管喉39-3的直径之间的比例为5-10∶1。本发明中水平方向具体指的是流化床反应器7放置在水平面时水平面延伸的方向。
在一个实施方案中，所述流化床反应器从所述原料第一分布器8向上至直径缩减前的区段具有高度h，所述原料第二分布器11设置在距离所述原料第一分布器8轴向相距1/4～1/2h处。
作为本发明所述的流化床反应器中原料第二分布器11的一种具体实施方式，所述原料第二分布器11的开孔率为0.05-5％，优选3-5％，孔径为1-30mm，优选各孔之间的孔径相差不超过±10％。参见图5，原料第二分布器11上设置有沿原料第二分布器11的径向延伸的第二分布器气体主导流管43、多个沿原料第二分布器11的径向依次设置的第二分布器气体环隙导流管44、设置在第二分布器气体环隙导流管44上的第二分布器风口45和第二分布器固体导流槽46，每个第二分布器气体环隙导流管44设置为绕原料第二分布器11的中心区域呈环形分布，第二分布器固体导流槽46位于相邻的两个第二分布器气体环隙导流管44之间；其中流化床反应器具有原料第二进料口2，其与所述第二分布器气体主导流管43流体连通。第二分布器风口45的开孔水平，可以是圆形、三角形、正方形以及六边形等，有效直径为0.1-10mm，开孔率为0.05-5％。
优选情况下，第二分布器气体环隙导流管44的宽度与第二分布器固体导流槽46的宽度之间的比例为1∶2-6。
在本发明中，催化剂分布器16包含催化剂分布器主导流管47。催化剂分布器16可以有不同结构，只要能够使得沿所述催化剂分布器主导流管47轴向输送的催化剂能够在流化床反应器内部沿径向分配。
作为本发明所述的流化床反应器中催化剂分布器16的一种具体实 施方式，所述催化剂分布器主导流管47从下往上穿越所述原料第一分布器8和原料第二分布器11，所述流化床反应器从所述原料第一分布器8向上至直径缩减前的区段具有高度h，所述催化剂分布器主导流管47从所述原料第一分布器8起向上的高度为h1，则1/4h＜h1≤3/4h。
在一个实施方案中，参见图6和图7，催化剂分布器16为树枝状布置方案，其包括催化剂分布器主导流管47和多层沿所述催化剂分布器主导流管47的上下方向分布的催化剂分布构件48，催化剂分布器主导流管47竖向设置于反应区域且与催化剂第二进料口27连通，催化剂分布构件48在径向延伸，以使得沿所述催化剂分布器主导流管47轴向输送的催化剂能够在流化床反应器内部沿径向分配。
在一个实施方案中，所述催化剂分布构件(48包括多个从分布器主导流管47分别径向向外延伸的催化剂第一分布导管49和多个催化剂第二分布导管50，催化剂第一分布导管49与催化剂第二分布导管50沿催化剂分布器主导流管47环向交错分布且均与催化剂分布器主导流管47连通，催化剂第一分布导管49与催化剂第二分布导管50分别设置有多个催化剂出口51。催化剂由催化剂分布器主导流管47进入各个催化剂分布构件48，通过催化剂第一分布导管49和催化剂第二分布导管50传输并经催化剂出口51进入反应器内。
在一个实施方案中，每层催化剂分布构件48中催化剂分布导管的数量为X个(X≥2且≤15)，多个催化剂分布导管圆周角度间距为360°/X分布；催化剂出口51具有选自正方形、圆形和多变形的形状。
优选地，所述催化剂分布构件48的数量优选为M层(M≥3且≤10)，催化剂分布构件48由上至下依次为第1层、第2层、......第M层；其中第n层催化剂分布构件48中催化剂分布导管的长度为(0.7-0.9) n*D/2，D为反应器内径，n为对应的层数，例如分布导管的直径为0.75 n*D/2。
优选情况下，催化剂分布构件48对应的催化剂第一分布导管49和催化剂第二分布导管50的长度由上至下依次减小，催化剂第一分布导管49和催化剂第二分布导管50上的催化剂出口51等距分布。
示例性地，催化剂第一分布导管49和催化剂第二分布导管50可统称催化剂分布导管，催化剂分布构件48的数量优选为M层(M≥3且≤10)，反应器内径尺寸为D米，催化剂分布构件48由上至下依次为第1层、第2层、第3层......第M层，每层催化剂分布构件48中催 化剂分布导管的直径为0.75n*D米(n为对应的层数)；每层催化剂分布构件48中催化剂分布导管的数量为X个(X≥2且≤15)，多个催化剂分布导管圆周角度间距为360°/X分布；催化剂出口51可以是正方形、圆形和多变形等，有效通道的直径尺寸为20-100mm，相邻的两个催化剂出口51的中心间距的尺寸与催化剂出口51沿其分布方向的宽度尺寸之比为1.5-5∶1。
在一个实施方案中，参见图11A，催化剂分布器16为主导流管布置方案，其包含催化剂分布器主导流管47或仅由所述催化剂分布器主导流管47构成。在此情况下，催化剂分布器主导流管47一般为管状，上部顶端敞开，催化剂延其从下往上输送，并从顶端敞开的开口进入流化床反应器。在一个例示的实施方案中，任选地，所述催化剂分布器主导流管47的管壁上具有开孔，例如开孔率为5-30％，以使催化剂通过开孔沿径向均匀分布。
在一个实施方案中，参见图11B，催化剂分布器16为内挡板布置方案，其包含催化剂分布器主导流管47和催化剂主导流管内挡板47-2。该内挡板47-2的形状没有具体限制，例如可以为基本圆形、椭圆(例如使其处于安装位置时，在水平面的投影为圆形)等形状，其在水平面的投影面积为催化剂分布器主导流管47的管内横截面的1/10～1/4。该内挡板47-2从与催化剂分布器主导流管47的管壁的接触处斜向下延伸，与管壁所在的垂直方向角度为10-75°，例如30-45°。
在一个实施方案中，参见图11C，催化剂分布器16为二次分布布置方案，其包含催化剂分布器主导流管47及其顶部连接的2个或更多个分散开的二次分布导流管47-3，例如2-12个，例如3-6个。各二次分布导流管47-3的外壁与催化剂分布器主导流管47的外壁以大约1/4圆的弧形连接，圆的半径为二次分布导流管出口水平圆环中心距离催化剂分布器主导流管中心线的距离。各二次分布导流管47-3除所述弧线连接部分之外的部分为直圆管与圆弧连通。多个二次分布导流管47-3在圆周上均匀间隔地布置。优选，多个二次分布导流管47-3具有一致的形状和尺寸。优选，二次分布导流管47-3的长度可根据实际情况具体确定，例如使其在径向延伸的长度为(0.1-0.9)*D/2，D为反应器内径。
在一个实施方案中，参见图11D，催化剂分布器16为螺旋导流管 布置方案，其包含催化剂分布器主导流管47和沿所述催化剂分布器主导流管47的轴向分布的一层或多层螺旋导流管47-4。每层包含2个或更多个分散开的螺旋导流管47-4，例如2-15个，例如3或4个。每层的多个螺旋导流管47-4在圆周上均匀间隔地布置。优选地，催化剂分布器16包含2-10层螺旋导流管47-4。优选，每层二次分布导流管47-4的长度可根据实际情况具体确定，例如使其在径向延伸的长度为(0.5-0.9) n*D/2，D为反应器内径，n为对应的层数。
在一个实施方案中，参见图11E，催化剂分布器16为环状导流管布置方案，其包含催化剂分布器主导流管47，沿所述催化剂分布器主导流管47的轴向分布的一层或多层环状导流管47-5。所述环状导流管包括导流环47-6以及将其与所述催化剂分布器主导流管47连接的连接管47-7。所述连接管47-7优选为螺旋结构。每层环状导流管包含2个或更多个分散开的连接管47-7，例如2-10个，如2-6个，例如3或4个。每层的连接管47-7、47-4在圆周上均匀间隔地布置。优选地，催化剂分布器16包含2-10层，例如2-6层环状导流管47-5。优选，每层环状导流管47-5的直径为(0.5-0.9) n*D/2，D为反应器内径，n为对应的层数。
在以上催化剂分布器16的各个布置方案中，参见所述树枝状布置方案中的例示，表示层数的“n”由上至下对相应构件计数。
所述流化床反应器具有在所述原料第一进口1上方、且从下往上依次布置的一个或多个原料第Y进料口，其中Y是≥2的正整数，条件是当存在所述一个或多个原料第Y进料口时，所述原料第一进口和所述原料第Y进料口的布置使得原料第Y进料口的进料量与原料第(Y-1)进料口进料量比为1∶1-10。优选地，Y≤10，优选≤5，例如所述流化床反应器具有总共2个或3个原料进料口。
根据本发明，流化床反应器7上设置有相应的进料口，以能够向原料第一分布器8与原料第二分布器11提供反应原料。作为本发明中进料口的一种优选实施方式，流化床反应器7上设置有原料第一进料口1和原料第二进料口2，原料第一进料口1与原料第一分布器8的底部连通，原料第二进料口2位于密相区28与催化剂分布区29的交汇区域。本发明中的进料口并不局限于仅设置原料第一进料口1和原料第二进料口2，可以根据反应原料的输入需求，设置其它的进料口。
作为本发明中流化床反应器7的一种优选实施方式，参见图8至图10，催化剂第一进料口24的上方设置有与流化床反应器7的内壁连接的循环布料挡板34。循环布料挡板34与催化剂第一进料口24一一对应设置，且位于相应的催化剂第一进料口24的正上方。
优选情况下，循环布料挡板34和催化剂第一进料口24之间的距离与催化剂第一进料口24的孔径的比例为1-10∶1。循环布料挡板34具体是以圆心位于流化床反应器7的内壁上、半径为R的圆与流化床反应器7的内壁相交形成的结构，其中R的尺寸与反应器的半径尺寸之比为1∶4-10。
参见图10，循环布料挡板34上设置有多个循环布料挡板槽37，循环布料挡板槽37与水平方向形成的夹角α为30°-75°，以使得循环布料挡板槽37朝向流化床反应器7的中心。循环布料挡板34能够将催化剂第一进料口24供入的催化剂向流化床反应器7的中心分布，通过循环布料挡板槽37强化催化剂的流向，使催化剂分布均匀度得到进一步提高。循环布料挡板槽37的宽度为H1，其与循环布料挡板34的半径R的尺寸之比为0.01-0.1∶1；循环布料挡板34的高度为H2，其与循环布料挡板34的半径R的尺寸之比在0.001-0.05∶1。
本发明第二方面提供一种制备低碳烯烃的装置，参见图1，该装置包括上述任意一种技术方案提供的流化床反应器7、沉降器9和再生器10，反应器侧壁上设置有至少一个用于将第一催化剂进料至所述原料第一分布器8与所述原料第二分布器11之间的第一催化剂进料口24，所述反应器底部设置有用于将第二催化剂进料的进料至所述分布器主导流管47的第二催化剂进料管27；其中沉降器9与流化床反应器7的反应区域的上方连通，沉降器9的下部分别与催化剂第一进料口24和再生器10连通，再生器10的再生催化剂出口与催化剂第二进料口27连通。
在本发明所述的制备低碳烯烃的装置中，催化剂第一进料口24的数量为k个，k≥2，且优选k≤12；各所述催化剂第一进料口(24)中心线夹角为360°/k。沉降器9的下部与催化剂第一进料口24通过循环管22连接。相应地，循环管22的数量与催化剂第一进料口24的数量相同，循环管22上设置有循环管控制阀23，以能够控制从催化剂第一进料口24供入密相区28的供入量。
在本发明所述的制备低碳烯烃的装置中，沉降器9可以采用常规结构的沉降装置，以将流化床反应器7输出的产物和被夹带的催化剂分离开。优选情况下，沉降器9内设置有沉降器下段17、处于沉降器下段17上方的沉降器上段18和位于沉降器上段18的沉降器旋风分离器19，沉降器旋风分离器19的气体出口与沉降器9的产品气出口5连通，沉降器下段17的下部设置有沉降器分布板12，沉降器分布板12的上方与循环管22连接，且通过汽提器21与再生器10连接。
优选情况下，沉降器上段18的顶部呈半球形，参见图12，沉降器分布板12上设置沉降器第一分布板孔35和沉降器第二分布板孔36，沉降器第一分布板孔35与沉降器第二分布板孔36分别设置为绕沉降器分布板12的中心区域呈环形分布，沉降器第一分布板孔35与沉降器第二分布板孔36的尺寸比为1-3∶4。沉降器第一分布板孔35和沉降器第二分布板孔36优选为在沉降器分布板12上交替呈环状分布，两者的开孔率为0.05-5％。沉降器上段18采用半球形设计，与传统沉降器的结构相比，相同体积下，沉降器9的尺寸可以降低10-21％，沉降器上段18的圆顶形设计可以使沉降器9内的气体流场更加稳定。
根据本发明，沉降器旋风分离器19可以采用常规的旋风分离器分离装置，以将产物与被夹带的催化剂进行有效的分离。示例性地，沉降器旋风分离器19设置为两级或多级串联的旋风分离器构造，第一级的旋风分离器的入口与沉降器上段18区域连通，第一级的旋风分离器的气体出口与相邻的旋风分离器的入口连通，从后一级的旋风分离器气体出口得到产物气，所有旋风分离器的固体出口与沉降器9区域相连通；最后一级旋风分离器的气体出口与沉降器9的产品气出口5连通，以使得最后一级旋风分离器得到的产物气从产品气出口5排出。
参见图1，沉降器9的下部通过汽提器21与再生器10连接，具体的连接方式可以为：沉降器9的下部通过汽提器进料管30与汽提器21连接，汽提器21上设置有汽提介质入口，以将汽提介质3引入汽提器21内，汽提器21的出料口通过汽提器出料管31与再生器10的再生器进料管33连通，汽提器出料管31上设置有汽提器控制阀32，以控制从再生器进料管33进入再生器10的进料量。
根据本发明，再生器10内设置有再生器气体分布器13和位于再生器气体分布器13上方的再生器旋风分离器20，再生器旋风分离器 20的气体出口与再生器10的烟气出口6连通，再生器10的下部设置有与再生器气体分布器13连通的再生器气体入口，以将再生器气体4引入再生器10内，并经再生器气体分布器13进行分布，提高再生器10的工作效率。再生器10的下部设置有再生催化剂出口，再生催化剂出口通过再生器循环出料管26与催化剂第二进料口27连通，再生器循环出料管26上设置有再生器循环出料管控制阀25。
优选情况下，再生器气体分布器13与原料第二分布器11的结构设计及参数相同。具体可以为，再生器气体分布器13上设置有沿再生器气体分布器13的径向延伸的再生器气体主导流管、多个沿再生器气体分布器13的径向依次设置的再生器气体环隙导流管、设置在再生器气体环隙导流管上的再生器风口和再生器固体导流槽，每个再生器气体环隙导流管设置为绕再生器气体分布器13的中心区域呈环形分布，再生器固体导流槽位于相邻的两个再生器气体环隙导流管之间。
根据本发明，再生器10的再生器旋风分离器20与沉降器旋风分离器19相同，设置为两级或多级串联的旋风分离器构造；再生器旋风分离器20的最后一级旋风分离器的气体出口与再生器10的烟气出口6连通，以使得最后一级旋风分离器得到的烟气从烟气出口6排出。
为了使得流化床反应器7与沉降器9更好地配合，作为本发明提供的装置的一种具体实施方式，流化床反应器7的顶部设置有伸入沉降器9内的提升分离管15，沉降器9内设置有位于提升分离管15的出口上方的提升管挡板14。其中，提升管挡板14的形状为人字型、圆形或矩形，以能够较少从流化床反应器7带入沉降器9的催化剂颗粒。
本发明第三方面提供的一种制备低碳烯烃的方法，其使用了上述任意一项技术方案提供的装置，该方法包括：
将气态原料和催化剂在流化床反应器7的反应区域内进行反应；
将得到的产物和被夹带的催化剂经反应区域的上方送入沉降器9；
沉降器9将产物和被夹带的催化剂分离开，并且将分离得到的催化剂的一部分从催化剂第一进料口24直接供入密相区28内，另一部分经再生器10再生后从催化剂第二进料口27供入催化剂分布区29内。
根据本发明，气态原料可以选自甲醇、乙醇、丙醇、丁醇、乙醛、丙醛、丁醛、丙酮、丁酮、甲酸、乙酸和丙酸中的至少一种。
在本发明所述的方法中，分离得到的催化剂的一部分通过汽提器 21供入再生器10内，汽提器21的汽提介质3为水蒸气。
在本发明所述的方法中，流化床反应器7内的压力以表压计为0-0.5MPa、平均温度为350-560℃、温差＜5℃，所述催化剂为SAPO-34，所述密相区28中的物料线速为1-10m/s。
在本发明所述的方法中，所述分离得到的催化剂中，供入所述密相区28内的部分与供入所述再生器10的部分质量比为1∶0.2-1。
在本发明所述的方法中，所述再生器10得到的再生催化剂的焦炭含量为5-15重量％。
在本发明所述的方法中，所述再生器10的再生介质为CO 2与空气的混合气，所述混合气中CO 2与空气的体积比为0.005-0.5∶1，以进行部分再生反应得到再生催化剂；所述再生器10的再生温度为600-750℃。将CO 2引入再生介质中，可以有效选择性消除积碳、稳定控制再生催化剂的积碳和再生催化剂的温度，同时实现高效利用反应热将温室气体CO 2转化。再生器10得到的再生催化剂中，部分再生催化剂的焦炭含量在1-3重量％之间，并控制再生催化剂的平均温度在400-500℃范围内。
在本发明所述的方法中，再生催化剂经催化剂分布器16的催化剂分布构件调控后，所述气态原料在经过所述密相区28时产生的压降与所述气态原料经过所述催化剂分布区29时产生的压降之比1.5-4∶1。
在本发明所述的方法中，所述气态原料经过所述原料第一分布器8，以对气体方向进行二次分布，环隙空间速度与水平方向形成的夹角为45°-75°，内外孔隙率波动之比为0.9-0.95∶1。
在本发明所述的方法能够实现再生催化剂分布的均匀分布及其与原料的充分接触，有效抑制温度分布不均匀和双烯选择低，可用于低碳烯烃的工业生产中。
在一个实施方案中，对流化床反应器中的催化剂分布进行测量，采用均方差σ 2来表征催化剂的不均匀度。其表达式如公式(1)所示，数值越大表明该区域的催化剂分布越不均匀，最小值0为理想状态下各位置处浓度均等于平均浓度值。其中σ 1 2代表再生催化剂相对于三相(气相、循环催化剂、再生催化剂)的浓度分布；
Figure PCTCN2022100672-appb-000001
c 1＝c 再               (II)
其中，c 再指的是再生催化剂在计算所需的每个网格区域的颗粒浓度；
Figure PCTCN2022100672-appb-000002
是所有催化剂在每个网格区域的颗粒浓度；m代表测量的反应器区域截面数，在不同测量中一般5≤m≤50；，i代表进料至反应器的催化剂的种类。
例如，在本发明中，流化床反应器7优选地包含催化剂第一进料口24和催化剂第二进料口27，以分别进料不同催化剂，例如分别进料循环催化剂和再生催化剂；相应地，在此情况下，i＝2，c 1＝c 再，其中c 再指的是再生催化剂在计算所需的每个网格区域的颗粒浓度，而c 2＝c 循 环，其中c 循环指的是循环催化剂在计算所需的每个网格区域的颗粒浓度。
本领域技术人员已知的是，根据CFD计算可以获取每个截面每个网格点的数据，然后提取出来进行数据处理，从而获得均方差数据。
下面根据图1所示的制备低碳烯烃的装置，来描述本发明中所述的制备低碳烯烃的装置及方法的一种相对优选的具体实施例：
制备低碳烯烃的装置包括流化床反应器7、沉降器9和再生器10；
流化床反应器7的反应区域从下至上依次设置有原料第一分布器8、原料第二分布器11和催化剂分布器16，原料第一分布器8与原料第二分布器11之间形成为催化剂的密相区28，催化剂分布器16所在的区域形成为与密相区28连通的催化剂分布区29，在密相区28的反应器侧壁上设置有多个催化剂第一进料口24；
原料第一分布器8包括第一分布器中心区域40和位于第一分布器中心区域40外周的第一分布器外部环形区域42，第一分布器外部环形区域42上设置有与催化剂第一进料口24相对应的第一分布器增强区域38，催化剂第一进料口24位于其对应的第一分布器增强区域38的外边缘中心的上方，第一分布器增强区域38设置有多个呈柱状的第一分布器增强喷头39，第一分布器增强喷头39的中心线与水平方向形成的夹角为45°-75°，第一分布器增强喷头39包括依次连接的增强喷头进口39-1、增强喷头渐缩管39-2、增强喷头管喉39-3、增强喷头扩大段39-4和增强喷头出口39-5，增强喷头进口39-1与原料第一分布器8的主体连接；
原料第二分布器11上设置有沿原料第二分布器11的径向延伸的第二分布器气体主导流管43、多个沿原料第二分布器11的径向依次设置的第二分布器气体环隙导流管44、设置在第二分布器气体环隙导流 管44上的第二分布器风口45和第二分布器固体导流槽46，每个第二分布器气体环隙导流管44设置为绕原料第二分布器11的中心区域呈环形分布，第二分布器固体导流槽46位于相邻的两个第二分布器气体环隙导流管44之间，第二分布器气体环隙导流管44的宽度与第二分布器固体导流槽46的宽度之间的比例为1∶2-6；
催化剂分布器16包括催化剂分布器主导流管47和多层沿所述催化剂分布器主导流管47的上下方向分布的催化剂分布构件48，催化剂分布器主导流管47竖向设置于反应区域且与催化剂第二进料口27连通，催化剂分布构件48包括多个催化剂第一分布导管49和多个催化剂第二分布导管50，催化剂第一分布导管49与催化剂第二分布导管50沿催化剂分布器主导流管47环向交错分布且均与催化剂分布器主导流管47连通，催化剂第一分布导管49与催化剂第二分布导管50分别设置有多个催化剂出口51，催化剂分布构件48对应的催化剂分布管的长度由上至下依次减小，多个催化剂出口51在催化剂第一分布导管49和催化剂第二分布导管50上等距分布；
流化床反应器7上设置有原料第一进料口1和原料第二进料口2，原料第一进料口1与原料第一分布器8的底部连通，原料第二进料口2位于密相区28与催化剂分布区29的交汇区域，原料第一进料口1与原料第二进料口2的进料量比为1-10∶1；
催化剂第一进料口24的上方设置有与流化床反应器的内壁连接的循环布料挡板34，循环布料挡板34上设置有多个循环布料挡板槽37，循环布料挡板槽37与水平方向形成的夹角α为30°-75°；
沉降器9包括处于下方的沉降器下段17、处于上方的沉降器上段18和位于沉降器上段18的沉降器旋风分离器19，沉降器旋风分离器19的气体出口与沉降器9的产品气出口5连通，沉降器下段17的下部设置有沉降器分布板12，沉降器分布板12的上方通过循环管22与对应的催化剂第一进料口24连接，循环管22上设置有循环管控制阀23，沉降器分布板12的上方通过汽提器进料管30与汽提器21连接，沉降器上段18呈半球形，沉降器分布板12上设置沉降器第一分布板孔35和沉降器第二分布板孔36，沉降器第一分布板孔35与沉降器第二分布板孔36分别设置为绕沉降器分布板12的中心区域呈环形分布；
汽提器21的出料口通过汽提器出料管31与再生器10的再生器进 料管33连通，汽提器出料管31上设置有汽提器控制阀32；
再生器10内设置有再生器气体分布器13和位于再生器气体分布器13上方的再生器旋风分离器20，再生器旋风分离器20的气体出口与再生器10的烟气出口6连通，再生器气体分布器13与原料第二分布器11的结构设计及参数相同，再生器10的下部设置有再生催化剂出口，再生催化剂出口通过再生器循环出料管26与催化剂第二进料口27连通；
流化床反应器7的顶部设置有伸入沉降器9内的提升分离管15，沉降器9内设置有位于提升分离管15的出口上方的提升管挡板14。
使用上述制备低碳烯烃的装置的相对优选的具体实施例，制备低碳烯烃的方法具体步骤为：
S1、将气态原料和催化剂从原料第一进料口1和原料第二进料口2输送至原料第一分布器8和原料第二分布器11，一部分经第一分布器增强喷头39和第一分布器中心区域风口41分布至密相区28，另一部分经原料第二分布器11分布至催化剂分布区29，以使得气态原料和催化剂在流化床反应器7的反应区域内进行反应；
S2、步骤S1中所述反应得到的产物和被夹带的催化剂从提升分离管15进入沉降器9内，经沉降器旋风分离器19的作用将产物和被夹带的催化剂分离开，得到的产品气从产品气出口5输出，分离得到的催化剂的一部分从循环管22输送至催化剂第一进料口24，以直接供入密相区28内，另一部分从汽提器进料管30进入汽提器21，经汽提器21汽提后从汽提器出料管31和再生器进料管33输送至再生器10，经再生器旋风分离器20分离再生后得到烟气和再生催化剂，烟气从烟气出口6排出，再生催化剂从再生器循环出料管26输入催化剂第二进料口27，以供入催化剂分布区29内，与密相区28内的气态原料接触反应。
本发明由此提供了以下的第二系列的例示实施方案：
1、一种流化床反应器，其特征在于，该流化床反应器的反应区域从下至上依次设置有第一原料分布器(8)、第二原料分布器(11)和催化剂分布器(16)，所述催化剂分布器(16)与第二催化剂进料管(27)连通，所述第一原料分布器(8)与所述第二原料分布器(11)之间形成为密相区(28)，所述催化剂分布器(16)所在的区域形成 为与所述密相区(28)连通的催化剂分布区(29)，在所述密相区(28)的反应器侧壁上设置有至少一个第一催化剂进料口(24)。
2、根据第二系列例示实施方案1所述的流化床反应器，其特征在于，所述第一原料分布器(8)包括第一分布器中心区域(40)和位于所述第一分布器中心区域(40)外周的第一分布器外部区域(42)，所述第一分布器外部区域(42)上设置有与所述第一催化剂进料口(24)相对应的第一分布器增强区域(38)。
3、根据第二系列例示实施方案2所述的流化床反应器，其特征在于，所述第一催化剂进料口(24)位于其对应的所述第一分布器增强区域(38)的外边缘中心的上方。
4、根据第二系列例示实施方案2所述的流化床反应器，其特征在于，所述第一分布器增强区域(38)上设置有多个呈柱状的第一分布器增强喷头(39)，所述第一分布器增强喷头(39)的中心线与水平方向形成的夹角为45°-75°。
5、根据第二系列例示实施方案4所述的流化床反应器，其特征在于，所述第一分布器增强喷头(39)包括依次连接的增强喷头进口(39-1)、增强喷头渐缩管(39-2)、增强喷头管喉(39-3)、增强喷头扩大段(39-4)和增强喷头出口(39-5)，所述增强喷头进口(39-1)与所述第一原料分布器(8)的主体连接。
6、根据第二系列例示实施方案5所述的流化床反应器，其特征在于，所述增强喷头管喉(39-3)的直径与所述增强喷头进口(39-1)的直径比例为1∶5-20，所述增强喷头管喉(39-3)的长度与该增强喷头管喉(39-3)的直径之间的比例为5-10∶1。
7、根据第二系列例示实施方案1至6中任意一项所述的流化床反应器，其特征在于，所述第二原料分布器(11)上设置有沿所述第二原料分布器(11)的径向延伸的第二分布器气体主导流管(43)、多个沿所述第二原料分布器(11)的径向依次设置的第二分布器气体环隙导流管(44)、设置在所述第二分布器气体环隙导流管(44)上的第二分布器风口(45)和第二分布器固体导流槽(46)，每个所述第二分布器气体环隙导流管(44)设置为绕所述第二原料分布器(11)的中心区域呈环形分布，所述第二分布器固体导流槽(46)位于相邻的两个所述第二分布器气体环隙导流管(44)之间。
8、根据第二系列例示实施方案7所述的流化床反应器，其特征在于，所述第二分布器气体环隙导流管(44)的宽度与所述第二分布器固体导流槽(46)的宽度之间的比例为1∶2-6。
9、根据第二系列例示实施方案1至6中任意一项所述的流化床反应器，其特征在于，所述催化剂分布器(16)包括催化剂分布器主导流管(47)和多层沿所述催化剂分布器主导流管(47)的上下方向分布的催化剂分布系统(48)，所述催化剂分布器主导流管(47)竖向设置于所述反应区域且与所述第二催化剂进料管(27)连通，所述催化剂分布系统(48)包括多个第一催化剂分布导管(49)和多个第二催化剂分布导管(50)，所述第一催化剂分布导管(49)与所述第二催化剂分布导管(50)沿所述催化剂分布器主导流管(47)环向交错分布且均与所述催化剂分布器主导流管(47)连通，所述第一催化剂分布导管(49)与所述第二催化剂分布导管(50)分别设置有多个催化剂出口(51)。
10、根据第二系列例示实施方案9所述的流化床反应器，其特征在于，所述催化剂分布系统(48)对应的所述第一催化剂分布导管(49)和所述第二催化剂分布导管(50)的长度由上至下依次减小，所述第一催化剂分布导管(49)和所述第二催化剂分布导管(50)上的所述催化剂出口(51)等距分布。
11、根据第二系列例示实施方案1至6中任意一项所述的流化床反应器，其特征在于，该流化床反应器上设置有第一进料口(1)和第二进料口(2)，所述第一进料口(1)与所述第一原料分布器(8)的底部连通，所述第二进料口(2)位于所述密相区(28)与所述催化剂分布区(29)的交汇区域。
12、根据第二系列例示实施方案11所述的流化床反应器，其特征在于，所述第一进料口(1)与所述第二进料口(2)的进料量比为1-10∶1。
13、根据第二系列例示实施方案1至6中任意一项所述的流化床反应器，其特征在于，所述第一催化剂进料口(24)的上方设置有与所述流化床反应器的内壁连接的循环布料挡板(34)。
14、根据第二系列例示实施方案13所述的流化床反应器，其特征在于，所述循环布料挡板(34)和所述第一催化剂进料口(24)之间 的距离与所述第一催化剂进料口(24)的孔径的比例为1-10∶1。
15、根据第二系列例示实施方案13所述的流化床反应器，其特征在于，所述循环布料挡板(34)上设置有多个循环布料挡板槽(37)，所述循环布料挡板槽(37)与水平方向形成的夹角(α)为30°-75°。
16、一种制备低碳烯烃的装置，其特征在于，该装置包括根据第二系列例示实施方案1至15中任意一项所述的流化床反应器(7)、沉降器(9)和再生器(10)，所述沉降器(9)与所述流化床反应器(7)的反应区域的上方连通，所述沉降器(9)的下部分别与所述第一催化剂进料口(24)和所述再生器(10)连通，所述再生器(10)的再生催化剂出口与所述第二催化剂进料管(27)连通。
17、根据第二系列例示实施方案16所述的装置，其特征在于，所述第一催化剂进料口(24)的数量为双数，所述第一催化剂进料口(24)沿所述流化床反应器(7)的中心轴对称设置，所述沉降器(9)的下部通过循环管(22)与所述第一催化剂进料口(24)连接。
18、根据第二系列例示实施方案17所述的装置，其特征在于，所述沉降器(9)内设置有沉降器下段(17)、处于所述沉降器下段(17)上方的沉降器上段(18)和位于所述沉降器上段(18)的沉降器旋风(19)，所述沉降器旋风(19)的气体出口与所述沉降器(9)的产品气出口(5)连通，所述沉降器下段(17)的下部设置有沉降器分布板(12)，所述沉降器分布板(12)的上方与所述循环管(22)连接，且通过汽提器(21)与所述再生器(10)连接。
19、根据第二系列例示实施方案18所述的装置，其特征在于，所述沉降器上段(18)的顶部呈半球形，所述沉降器分布板(12)上设置第一沉降器分布板孔(35)和第二沉降器分布板孔(36)，所述第一沉降器分布板孔(35)与所述第二沉降器分布板孔(36)分别设置为绕所述沉降器分布板(12)的中心区域呈环形分布，所述第一沉降器分布板孔(35)与所述第二沉降器分布板孔(36)的尺寸比为1-3∶4。
20、根据第二系列例示实施方案16至19中任意一项所述的装置，其特征在于，所述再生器(10)内设置有再生器气体分布器(13)和位于所述再生器气体分布器(13)上方的再生器旋风(20)，所述再生器旋风(20)的气体出口与所述再生器(10)的烟气出口(6)连通；
所述再生器气体分布器(13)上设置有沿所述再生器气体分布器(13)的径向延伸的再生器气体主导流管、多个沿所述再生器气体分布器(13)的径向依次设置的再生器气体环隙导流管、设置在所述再生器气体环隙导流管上的再生器风口和再生器固体导流槽，每个所述再生器气体环隙导流管设置为绕所述再生器气体分布器(13)的中心区域呈环形分布，所述再生器固体导流槽位于相邻的两个所述再生器气体环隙导流管之间。
21、根据第二系列例示实施方案16至19中任意一项所述的装置，其特征在于，所述流化床反应器(7)的顶部设置有伸入所述沉降器(9)内的提升分离管(15)，所述沉降器(9)内设置有位于所述提升分离管(15)的出口上方的挡板(14)。
22、一种制备低碳烯烃的方法，其使用了根据第二系列例示实施方案16所述的装置，该方法包括：
将气态原料和催化剂在流化床反应器的反应区域内进行反应；
将得到的产物和被夹带的催化剂经所述反应区域的上方送入沉降器；
所述沉降器将所述产物和所述被夹带的催化剂分离开，并且将分离得到的催化剂的一部分从所述第一催化剂进料口直接供入所述密相区内，另一部分经所述再生器再生后从所述第二催化剂进料管供入所述催化剂分布区内。
23、根据第二系列例示实施方案22所述的方法，其特征在于，所述分离得到的催化剂的一部分通过汽提器供入所述再生器内，所述汽提器的汽提介质为水蒸气。
24、根据第二系列例示实施方案22所述的方法，其特征在于，所述流化床反应器内的压力以表压计为0-0.5MPa、平均温度为350-560℃、温差＜5℃，所述催化剂为SAPO-34，所述密相区中的物料线速为1-10m/s。
25、根据第二系列例示实施方案22所述的方法，其特征在于，所述分离得到的催化剂中，供入所述密相区内的部分与供入所述再生器的部分质量比为1∶0.2-1。
26、根据第二系列例示实施方案22所述的方法，其特征在于，所述再生器得到的再生催化剂的焦炭含量为5-15重量％。
27、根据第二系列例示实施方案22所述的方法，其特征在于，所述再生器的再生介质为CO 2与空气的混合气，所述混合气中CO 2与空气的体积比为0.005-0.5∶1；所述再生器的再生温度为600-750℃。
28、根据第二系列例示实施方案22所述的方法，其特征在于，所述气态原料在经过所述密相区时产生的压降与所述气态原料经过所述催化剂分布区时产生的压降之比1.5-4∶1。
29、根据第二系列例示实施方案22所述的方法，其特征在于，所述气态原料经过所述第一原料分布器后，环隙空间速度与水平方向形成的夹角为45°-75°，内外孔隙率波动之比为0.9-0.95∶1。
以下通过实施例对本发明作进一步的阐述，但本发明的保护范围并不仅限于此。
以下实施例中，所使用的实验方法如无特殊说明，均为常规方法；所使用的材料、试剂等，如无特殊说明，均可从商业途径得到。
实施例1
采用上述制备低碳烯烃的装置的相对优选的具体实施例以及制备低碳烯烃的方法具体步骤进行低碳烯烃的制备；
参见图1，其中，制备低碳烯烃的装置中催化剂第一进料口24设置为4个，原料第一分布器8的结构如图3和图4所示，开孔率为1％。增强喷头渐缩管39-2与水平方向形成的夹角区间在45°，增强喷头扩大段39-4与水平方向夹角区间为70°，增强喷头管喉39-3的直径与增强喷头进口39-1的直径比例为1∶10，增强喷头管喉39-3的长度与该增强喷头管喉39-3的直径之间的比例为8∶1。第一分布器增强区域38的开孔率为0.2％，孔径为2mm。第一分布器外部区域42和第一分布器中心区域40的开孔率均为2％，孔径均为6mm。第一分布器中心区域40是半径为r的圆形，第一分布器外部区域42是外径和内径之差为d的圆环，r/d＝1/2，其面积之比1/2，反应器内径D为8米。
对于原料第二分布器11，第二分布器气体环隙导流管44的宽度与第二分布器固体导流槽46的宽度之间的比例为1∶4。第二原料分布器11的开孔率为5％，距离原料第一分布器8轴向相距1/2。
催化剂分布构件48采用树枝状布置方案，设置为3层，每层设置3个催化剂分布导管(催化剂第一分布导管49和催化剂第二分布导管50交错分布)，催化剂出口51的有效通道的直径尺寸为60mm，相邻 的两个催化剂出口51的中心间距的尺寸与催化剂出口51沿其分布方向的宽度尺寸之比为3∶1。催化剂分布器主导流管47从原料第一分布器(8)起向上的高度为3/4h；多层分布导管的长度依次是0.75D，0.75 2D以及0.75 3D。
使用两个原料进料口，其中原料第一进料口1与原料第二进料口2的进料量比为6∶1，循环布料挡板34和催化剂第一进料口24之间的距离与催化剂第一进料口24的孔径的比例为6∶1，循环布料挡板槽37与水平方向形成的夹角α为55°，沉降器第一分布板孔35与沉降器第二分布板孔36的尺寸比为2∶4，沉降器旋风分离器19和再生器旋风分离器20分别设置为两级串联的旋风分离器构造。
在制备低碳烯烃的过程中，原料采用纯度为99.5％的甲醇，催化剂采用SAPO-34，汽提器21的汽提介质3为水蒸气。流化床反应器7内的压力为0.3MPa、平均温度为450℃，控制温差＜5℃，线速为5m/s，经催化剂第一进料口24内供入密相区28内的催化剂与经催化剂第二进料口27供入再生器10的催化剂的质量比为1∶0.5。再生器10得到的再生催化剂的焦炭含量为10重量％，再生器10的再生介质为CO 2与空气的混合气，混合气中CO 2与空气的体积比为0.2∶1。再生器10的再生温度为650℃。气态原料在经过密相区28时产生的压降与气态原料经过催化剂分布区29时产生的压降之比3∶1。气态原料经过原料第一分布器8后，环隙空间速度与水平方向形成的夹角为45，内外孔隙率波动之比为0.95∶1。
再生剂催化剂分布不均匀度随高度的变化如图13所示，再生催化剂的三相平均均匀度为0.29。甲醇转化率99.995％，乙烯和丙烯总收率(质量)为84.8％。
实施例2
按照实施例1的装置和方法步骤，所不同的是：
制备低碳烯烃的装置中催化剂第一进料口24设置为2个，原料第一分布器8的结构如图2所示，增强喷头渐缩管39-2与水平方向形成的夹角区间在45°，增强喷头扩大段39-4与水平方向夹角区间在70°，增强喷头管喉39-3的直径与增强喷头进口39-1的直径比例为1∶5，增强喷头管喉39-3的长度与该增强喷头管喉39-3的直径之间的比例为5∶1。第二分布器气体环隙导流管44的宽度与第二分布器固体导流槽 46的宽度之间的比例为1∶2。催化剂分布构件48设置为3层，每层设置2个催化剂分布导管(催化剂第一分布导管49和催化剂第二分布导管50交错分布)，催化剂出口51的有效通道的直径尺寸为80mm，相邻的两个催化剂出口51的中心间距的尺寸与催化剂出口51沿其分布方向的宽度尺寸之比为1.5∶1。原料第一进料口1与原料第二进料口2的进料量比为2∶1，循环布料挡板34和催化剂第一进料口24之间的距离与催化剂第一进料口24的孔径的比例为2∶1，循环布料挡板槽37与水平方向形成的夹角α为30°，沉降器第一分布板孔35与沉降器第二分布板孔36的尺寸比为1∶4，沉降器旋风分离器19和再生器旋风分离器20分别设置为两级串联的旋风分离器构造。
在制备低碳烯烃的过程中，原料采用纯度为99.5％的甲醇，催化剂采用SAPO-34，流化床反应器7内的压力为0.1MPa、平均温度为350℃，温差＜5℃，线速为1m/s，经催化剂第一进料口24内供入密相区28内的催化剂与经催化剂第二进料口27供入再生器10的催化剂的质量比为1∶0.2。汽提器21的汽提介质3为水蒸气。再生器10得到的再生催化剂的焦炭含量为5重量％，再生器10的再生介质为CO 2与空气的混合气，混合气中CO 2与空气的体积比为0.01∶1。再生器10的再生温度为600℃。气态原料在经过密相区28时产生的压降与气态原料经过催化剂分布区29时产生的压降之比1.5∶1。气态原料经过原料第一分布器8后，环隙空间速度与水平方向形成的夹角为45°-75°，内外孔隙率波动之比为0.9-0.95∶1。
再生催化剂的三相平均均匀度为0.89。甲醇转化率99.985％，乙烯和丙烯总收率(质量)为83.58％。
实施例3
按照实施例1的装置和方法步骤，所不同的是，制备低碳烯烃的装置中催化剂第一进料口24设置为2个，原料第一分布器8的结构如图2所示，增强喷头渐缩管39-2与水平方向形成的夹角区间在45°，增强喷头扩大段39-4与水平方向夹角区间在70°，增强喷头管喉39-3的直径与增强喷头进口39-1的直径比例为1∶20，增强喷头管喉39-3的长度与该增强喷头管喉39-3的直径之间的比例为10∶1。第二分布器气体环隙导流管44的宽度与第二分布器固体导流槽46的宽度之间的比例为1∶6。催化剂分布构件48设置为3层，每层设置2个催化剂 分布导管(催化剂第一分布导管49和催化剂第二分布导管50交错分布)，催化剂出口51的有效通道的直径尺寸为100mm，相邻的两个催化剂出口51的中心间距的尺寸与催化剂出口51沿其分布方向的宽度尺寸之比为5∶1。原料第一进料口1与原料第二进料口2的进料量比为10∶1，循环布料挡板34和催化剂第一进料口24之间的距离与催化剂第一进料口24的孔径的比例为10∶1，循环布料挡板槽37与水平方向形成的夹角α为75°，沉降器第一分布板孔35与沉降器第二分布板孔36的尺寸比为3∶4，沉降器旋风分离器19和再生器旋风分离器20分别设置为两级串联的旋风分离器构造。
在制备低碳烯烃的过程中，原料采用纯度为99.5％的甲醇，催化剂采用SAPO-34，流化床反应器7内的压力为0.5MPa、平均温度为560℃，温差＜5℃，线速为10m/s，经催化剂第一进料口24内供入密相区28内的催化剂与经催化剂第二进料口27供入再生器10的催化剂的质量比为1∶1。汽提器21的汽提介质3为水蒸气。再生器10得到的再生催化剂的焦炭含量为15重量％，再生器10的再生介质为CO 2与空气的混合气，混合气中CO 2与空气的体积比为0.5∶1。再生器10的再生温度为750℃。气态原料在经过密相区28时产生的压降与气态原料经过催化剂分布区29时产生的压降之比4∶1。气态原料经过原料第一分布器8后，环隙空间速度与水平方向形成的夹角为45°-75°，内外孔隙率波动之比为0.9-0.95∶1。
甲醇转化率99.981％，乙烯和丙烯总收率(质量)为83.14％。
实施例4
按照实施例1的装置和方法步骤，所不同的是，原料第一分布器8上仅设置有第一分布器中心区域风口41，不设置与催化剂第一进料口24对应的第一分布器增强区域38和第一分布器增强喷头39。
甲醇转化率99.98％，乙烯和丙烯总收率(质量)为82.65％。
实施例5
按照实施例1的装置和方法步骤，所不同的是，原料第一分布器8上增强喷头渐缩管39-2与水平方向形成的夹角为90°，增强喷头扩大段39-4与水平方向形成的夹角为90°。
甲醇转化率99.96％，乙烯和丙烯总收率(质量)为80.61％。
实施例6
按照实施例1的装置和方法步骤，所不同的是，原料第二分布器11上仅设置有多个开孔。
甲醇转化率99.959％，乙烯和丙烯总收率(质量)为80.68％。
实施例7
按照实施例1的装置和方法步骤，所不同的是，第二分布器气体环隙导流管44的宽度与第二分布器固体导流槽46的宽度之间的比例为2∶1。
甲醇转化率99.978％，乙烯和丙烯总收率(质量)为80.61％。
实施例8
按照实施例1的装置和方法步骤，所不同的是，催化剂分布器16包括催化剂分布器主导流管47，催化剂分布器主导流管47竖向设置于反应区域且与催化剂第二进料口27连通，催化剂分布器主导流管47上设置有多个竖向排列的开孔。
甲醇转化率99.977％，乙烯和丙烯总收率(质量)为82.45％。
实施例9
按照实施例1的装置和方法步骤，所不同的是，原料第一进料口1和原料第二进料口2均与原料第一分布器8的底部连通。
甲醇转化率99.95％，乙烯和丙烯总收率(质量)为81.7％。
实施例10
按照实施例1的装置和方法步骤，所不同的是，原料第一进料口1与原料第二进料口2的进料量比为1∶5。
甲醇转化率99.975％，乙烯和丙烯总收率(质量)为82.75％。
实施例11
按照实施例1的装置和方法步骤，所不同的是，催化剂第一进料口24的上方未设置循环布料挡板34。
甲醇转化率99.945％，乙烯和丙烯总收率(质量)为81.71％。
实施例12
按照实施例1的装置和方法步骤，所不同的是，循环布料挡板34上未设置循环布料挡板槽37。
甲醇转化率99.94％，乙烯和丙烯总收率(质量)为81.63％。
实施例13
按照实施例1的装置和方法步骤，所不同的是，沉降器分布板12 上仅设置有多个沉降器第一分布板孔35。
甲醇转化率99.965％，乙烯和丙烯总收率(质量)为82.5％。
实施例14
按照实施例1的装置和方法步骤，所不同的是，再生器10的再生介质为空气。
甲醇转化率99.974％，乙烯和丙烯总收率(质量)为81.55％。
实施例15
按照实施例1的装置和方法步骤，所不同的是，再生器10的再生介质为CO 2与空气的混合气，所述混合气中CO 2与空气的体积比为0.7∶1。
甲醇转化率99.975％，乙烯和丙烯总收率(质量)为82.53％。
对比例1
按照实施例1的装置和方法步骤，所不同的是，流化床反应器7内不设置原料第一分布器8、原料第二分布器11和催化剂分布器16。仅将催化剂第一进料口24、催化剂第二进料口27分别与流化床反应器7的反应区域连通。
甲醇转化率99.91％，乙烯和丙烯总收率(质量)为80.05％。
对比例2
按照实施例1的装置和方法步骤，所不同的是，流化床反应器7内仅设置原料第一分布器8，不设置原料第二分布器11和催化剂分布器16。将催化剂第一进料口24、催化剂第二进料口27分别与原料第一分布器8的上方连通。流化床反应器7上设置有与原料第一分布器8的底部连通的原料第一进料口1。
甲醇转化率99.93％，乙烯和丙烯总收率(质量)为81.01％。
对比例3
按照实施例1的装置和方法步骤，所不同的是，流化床反应器7内设置原料第一分布器8和原料第二分布器11；但不设置催化剂分布器16，而是将再生催化剂如常规那样从侧面进料。将催化剂第一进料口24、催化剂第二进料口27分别与原料第一分布器8的上方连通。流化床反应器7上设置有与原料第一分布器8的底部连通的原料第一进料口1。
甲醇转化率99.84％，乙烯和丙烯总收率(质量)为78.5％。
对比例3与实施例1中再生催化剂分布的不均匀度随高度的变化对比如图14所示。清楚的是，再生催化剂侧面进料的对比例3的均匀度分布变化范围为2.57～62.15；相比之下，使用底部的再生催化剂分布器16的实施例1的均匀度变化范围为0.16～1.56，均匀性得到明显改善。
以上详细描述了本发明的优选实施方式，但是，本发明并不限于此。在本发明的技术构思范围内，可以对本发明的技术方案进行多种简单变型，包括各个技术特征以任何其它的合适方式进行组合，这些简单变型和组合同样应当视为本发明所公开的内容，均属于本发明的保护范围。

Claims (30)

  1. 一种流化床反应器，包括：
    在该流化床反应器的反应区域中的原料第一分布器(8)、原料第二分布器(11)和催化剂分布器(16)，其用于对气体原料进行分布，其中所述原料第一分布器(8)在原料第二分布器(11)下方；其中所述原料第一分布器(8)和原料第二分布器(11)具有相同或不同的开孔率，各自独立地为0.05-5％；
    在该流化床反应器底部的原料第一进口(1)，其使得原料的至少一部分经由所述原料第一分布器(8)和原料第二分布器(11)依次进行两次分布；
    所述催化剂分布器(16)包括催化剂分布器主导流管(47)，其与所述原料第一分布器(8)和原料第二分布器(11)同轴分布，其中所述催化剂分布器主导流管(47)从下往上穿越所述原料第一分布器(8)和原料第二分布器(11)。
  2. 根据权利要求1所述的流化床反应器，其特征在于，所述流化床反应器具有在所述原料第一进口(1)上方、且从下往上依次布置的一个或多个原料第Y进料口，其中Y是≥2的正整数，条件是当存在所述一个或多个原料第Y进料口时，所述原料第一进口和所述原料第Y进料口的布置使得原料第Y进料口的进料量与原料第(Y-1)进料口进料量比为1∶1-10。
  3. 根据权利要求1所述的流化床反应器，其特征在于，在所述原料第一分布器(8)与所述原料第二分布器(11)之间的反应器侧壁上设置有至少一个催化剂第一进料口(24)；以及
    所述原料第一分布器(8)包括第一分布器中心区域(40)和位于所述第一分布器中心区域(40)外周的第一分布器外部环形区域(42)，所述第一分布器外部环形区域(42)上设置有与所述催化剂第一进料口(24)的径向位置相对应的第一分布器增强区域(38)，该第一分布器增强区域(38)具有相对于原料第一分布器(8)的其它区域来说减小的孔径，以使得催化剂在所述原料第一分布器(8)和所述原料第二分布器(11)之间具有径向上基本均匀的分布。
  4. 根据权利要求3所述的流化床反应器，其特征在于，所述第一 分布器中心区域(40)是半径为r的圆形，第一分布器外部区域(42)是外径和内径之差为d的圆环，其中r/d＝1/2～3/5，r+d＝D，该D为所述流化床反应器的内径；第一分布器增强区域(38)面积设置为与第一分布器外部区域(42)面积之比为1/10～1/2。
  5. 根据权利要求3所述的流化床反应器，其特征在于，所述原料第一分布器(8)除所述第一分布器增强区域(38)之外的区域的开孔率为1.5-10％，优选2-5％，孔径为2-30mm，优选各孔之间的孔径相差不超过±10％；所述第一分布器增强区域(38)的开孔率为0.01～1.5％，孔径为0.1～20mm，优选各孔之间的孔径相差不超过±10％。
  6. 根据权利要求3所述的流化床反应器，其特征在于，所述第一分布器增强区域(38)上设置有多个呈柱状的第一分布器增强喷头(39)，所述第一分布器增强喷头(39)的中心线与水平方向形成的夹角为45°-75°。
  7. 根据权利要求6所述的流化床反应器，其特征在于，所述第一分布器增强喷头(39)包括依次连接的增强喷头进口(39-1)、增强喷头渐缩管(39-2)、增强喷头管喉(39-3)、增强喷头扩大段(39-4)和增强喷头出口(39-5)，所述增强喷头进口(39-1)与所述原料第一分布器(8)的主体连接；其中
    增强喷头渐缩管(39-2)与水平方向形成的夹角区间为30°-70°，增强喷头扩大段(39-4)与水平方向形成的夹角区间为30°-70°，所述增强喷头管喉(39-3)的直径与所述增强喷头进口(39-1)的直径比例为1∶5-20，所述增强喷头管喉(39-3)的长度与该增强喷头管喉(39-3)的直径之间的比例为5-10∶1。
  8. 根据权利要求1至7中任一项所述的流化床反应器，其特征在于，所述流化床反应器从所述原料第一分布器(8)向上至直径缩减前的区段具有高度h，所述原料第二分布器(11)设置在距离所述原料第一分布器(8)轴向相距1/4～1/2h处。
  9. 根据权利要求8所述的流化床反应器，其特征在于，所述原料第二分布器(11)的开孔率为0.05-5％，优选3-5％，孔径为1-30mm，优选各孔之间的孔径相差不超过±10％。
  10. 根据权利要求8所述的流化床反应器，其特征在于，所述原料第二分布器(11)上设置有沿所述原料第二分布器(11)的径向延伸 的第二分布器气体主导流管(43)、多个沿所述原料第二分布器(11)的径向依次设置的第二分布器气体环隙导流管(44)、设置在所述第二分布器气体环隙导流管(44)上的第二分布器风口(45)和第二分布器固体导流槽(46)，每个所述第二分布器气体环隙导流管(44)设置为绕所述原料第二分布器(11)的中心区域呈环形分布，所述第二分布器固体导流槽(46)位于相邻的两个所述第二分布器气体环隙导流管(44)之间；其中流化床反应器具有原料第二进料口(2)，其与所述第二分布器气体主导流管(43)流体连通。
  11. 根据权利要求10所述的流化床反应器，其特征在于，所述第二分布器气体环隙导流管(44)的宽度与所述第二分布器固体导流槽(46)的宽度之间的比例为1∶2-6。
  12. 根据权利要求1至7中任一项所述的流化床反应器，其特征在于，所述催化剂分布器主导流管(47)从下往上穿越所述原料第一分布器(8)和原料第二分布器(11)，所述流化床反应器从所述原料第一分布器(8)向上至直径缩减前的区段具有高度h，所述催化剂分布器主导流管(47)从所述原料第一分布器(8)起向上的高度为h1，则1/4h＜h1≤3/4h。
  13. 根据权利要求12所述的流化床反应器，其特征在于，所述催化剂分布器(16)为树枝状布置方案，包括沿所述催化剂分布器主导流管(47)的上下方向分布的多层催化剂分布构件(48)，所述催化剂分布构件(48)在径向延伸，以使得沿所述催化剂分布器主导流管(47)轴向输送的催化剂能够在流化床反应器内部沿径向分配。
  14. 根据权利要求13所述的流化床反应器，其特征在于，所述催化剂分布构件(48)包括多个催化剂第一分布导管(49)和多个催化剂第二分布导管(50)，所述催化剂第一分布导管(49)与所述催化剂第二分布导管(50)沿所述催化剂分布器主导流管(47)环向交错分布且均与所述催化剂分布器主导流管(47)连通，所述催化剂第一分布导管(49)与所述催化剂第二分布导管(50)分别设置有多个催化剂出口(51)；其中
    每层催化剂分布构件(48)中催化剂分布导管的数量为X个(X≥2)，多个催化剂分布导管圆周角度间距为180°/X分布；催化剂出口(51)具有选自正方形、圆形和多变形的形状。
  15. 根据权利要求13所述的流化床反应器，其特征在于，所述催化剂分布构件(48)的数量优选为M层(M≥3)，催化剂分布构件(48)由上至下依次为第1层、第2层、......第M层；其中第n层催化剂分布构件(48)中催化剂分布导管的长度为(0.7-0.9) n*D/2，D为反应器内径，n为对应的层数。
  16. 根据权利要求13所述的流化床反应器，其特征在于，所述催化剂第一分布导管(49)和所述催化剂第二分布导管(50)上的所述催化剂出口(51)等距分布。
  17. 根据权利要求12所述的流化床反应器，其特征在于，所述催化剂分布器(16为主导流管布置方案，其包含催化剂分布器主导流管(47)或仅由所述催化剂分布器主导流管(47)构成，其中催化剂分布器主导流管(47)为管状，上部顶端敞开；或
    所述催化剂分布器(16)为内挡板布置方案，其包含催化剂分布器主导流管(47)和催化剂主导流管内挡板(47-2)，优选其在水平面的投影面积为催化剂分布器主导流管47)的管内横截面的1/10～1/4；或
    所述催化剂分布器(16)为二次分布布置方案，其包含催化剂分布器主导流管(47)及其顶部连接的2个或更多个分散开的二次分布导流管(47-3)，优选其在径向延伸的长度为(0.1-0.9)*D/2，D为反应器内径；或
    所述催化剂分布器16为螺旋导流管布置方案，其包含催化剂分布器主导流管(47)和沿所述催化剂分布器主导流管(47)的轴向分布的一层或多层螺旋导流管(47-4)，优选其在径向延伸的长度为(0.5-0.9) n*D/2，D为反应器内径，n为对应的层数；或
    所述催化剂分布器(16)为环状导流管布置方案，其包含催化剂分布器主导流管(47，沿所述催化剂分布器主导流管(47)的轴向分布的一层或多层环状导流管(47-5)，优选每层环状导流管47-5的直径为(0.5-0.9) n*D/2，D为反应器内径，n为对应的层数。
  18. 根据权利要求3至7中任意一项所述的流化床反应器，其特征在于，所述催化剂第一进料口(24)的上方设置有与所述流化床反应器的内壁连接的循环布料挡板(34)。
  19. 根据权利要求18所述的流化床反应器，其特征在于，所述循 环布料挡板(34)和所述催化剂第一进料口(24)之间的距离与所述催化剂第一进料口(24)的孔径的比例为1-10∶1。
  20. 根据权利要求18所述的流化床反应器，其特征在于，所述循环布料挡板(34)上设置有多个循环布料挡板槽(37)，所述循环布料挡板槽(37)与水平方向形成的夹角(α)为30°-75°。
  21. 一种制备低碳烯烃的装置，其特征在于，该装置包括根据权利要求1至19中任意一项所述的流化床反应器(7)、沉降器(9)和再生器(10)，反应器侧壁上设置有至少一个用于将催化剂第一进料至所述原料第一分布器(8)与所述原料第二分布器(11)之间的催化剂第一进料口(24)，所述反应器底部设置有用于将催化剂第二进料的进料至所述分布器主导流管(47)的催化剂第二进料口(27)；其中：
    所述沉降器(9)与所述流化床反应器(7)的反应区域的上方连通，所述沉降器(9)的下部分别与所述催化剂第一进料口(24)和所述再生器(10)连通，所述再生器(10)的再生催化剂出口与所述催化剂第二进料口(27)连通。
  22. 根据权利要求21所述的装置，其特征在于，所述催化剂第一进料口(24)的数量为k个，k≥2，各所述催化剂第一进料口(24)中心线夹角为360°/k；且优选k≤12。
  23. 根据权利要求22所述的装置，其特征在于，所述沉降器(9)内设置有沉降器下段(17)、处于所述沉降器下段(17)上方的沉降器上段(18)和位于所述沉降器上段(18)的沉降器旋风分离器(19)，所述沉降器旋风分离器(19)的气体出口与所述沉降器(9)的产品气出口(5)连通，所述沉降器下段(17)的下部设置有沉降器分布板(12)，并所述沉降器分布板(12)的下方通过循环管(22)与所述催化剂第一进料口(24)连接，且通过汽提器(21)与所述再生器(10)连接。
  24. 根据权利要求23所述的装置，其特征在于，所述沉降器分布板(12)上设置沉降器第一分布板孔(35)和沉降器第二分布板孔(36)，所述沉降器第一分布板孔(35)与所述沉降器第二分布板孔(36)分别设置为绕所述沉降器分布板(12)的中心区域呈环形分布，所述沉降器第一分布板孔(35)与所述沉降器第二分布板孔(36)的尺寸比为1-3∶4。
  25. 根据权利要求21至24中任意一项所述的装置，其特征在于， 所述流化床反应器(7)的顶部设置有伸入所述沉降器(9)内的提升分离管(15)，所述沉降器(9)内设置有位于所述提升分离管(15)的出口上方的提升管挡板(14)。
  26. 在权利要求21-24任一项所述的装置中制备低碳烯烃的方法，包括：
    将气态原料和催化剂在流化床反应器的反应区域内进行反应；
    将得到的产物和被夹带的催化剂经所述反应区域的上方送入沉降器；
    所述沉降器将所述产物和所述被夹带的催化剂分离开，并且将分离得到的催化剂的一部分从所述催化剂第一进料口直接供入在所述原料第一分布器(8)与所述原料第二分布器(11)之间形成的密相区内，另一部分经所述再生器再生后从所述催化剂第二进料口供入所述催化剂分布区内。
  27. 根据权利要求26所述的方法，其特征在于，所述密相区中的物料线速为1-10m/s。
  28. 根据权利要求26所述的方法，其特征在于，所述分离得到的催化剂中，供入所述密相区内的部分与供入所述再生器的部分质量比为1∶0.2-1。
  29. 根据权利要求26所述的方法，其特征在于，所述气态原料在经过所述密相区时产生的压降与所述气态原料经过所述催化剂分布区时产生的压降之比1.5-4∶1。
  30. 根据权利要求26所述的方法，其特征在于，所述气态原料经过所述原料第一分布器后，环隙空间速度与水平方向形成的夹角为45°-75°，内外孔隙率波动之比为0.9-0.95∶1。
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