CN112536001B - Catalytic conversion reactor and system - Google Patents

Catalytic conversion reactor and system Download PDF

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Publication number
CN112536001B
CN112536001B CN201910891587.2A CN201910891587A CN112536001B CN 112536001 B CN112536001 B CN 112536001B CN 201910891587 A CN201910891587 A CN 201910891587A CN 112536001 B CN112536001 B CN 112536001B
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reactor
height
section
reaction zone
diameter
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CN112536001A (en
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龚剑洪
张执刚
魏晓丽
常学良
张久顺
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Sinopec Research Institute of Petroleum Processing
China Petroleum and Chemical Corp
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Sinopec Research Institute of Petroleum Processing
China Petroleum and Chemical Corp
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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
    • B01J8/08—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with moving 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
    • B01J8/24—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
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C4/00—Preparation of hydrocarbons from hydrocarbons containing a larger number of carbon atoms
    • C07C4/02—Preparation of hydrocarbons from hydrocarbons containing a larger number of carbon atoms by cracking a single hydrocarbon or a mixture of individually defined hydrocarbons or a normally gaseous hydrocarbon fraction
    • C07C4/06—Catalytic processes
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G11/14—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G11/14—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts
    • C10G11/18—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts according to the "fluidised-bed" technique
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G55/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process
    • C10G55/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process plural serial stages only
    • C10G55/06—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process plural serial stages only including at least one catalytic cracking step
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/1037—Hydrocarbon fractions
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
    • C10G2400/20—C2-C4 olefins
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
    • C10G2400/30—Aromatics
    • 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
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts

Abstract

The invention relates to a catalytic conversion reactor and a catalytic conversion system, wherein the reactor sequentially comprises an optional pre-lifting section, a full-concentration phase reaction zone, a transition section and an outlet zone from bottom to top, the full-concentration phase reaction zone is in a hollow cylinder form comprising one or more expanding sections with diameters continuously or discontinuously increasing from bottom to top, at least one catalyst inlet is arranged on the optional pre-lifting section and/or the bottom of the full-concentration phase reaction zone, and one or more supplementary catalyst inlets are arranged on the side wall of the full-concentration phase reaction zone. When the reactor and the system are used for catalytic conversion reaction, the contact efficiency of the raw materials and the catalyst is high, so that the yield of dry gas and coke can be effectively reduced, the catalytic reaction selectivity is improved, and the yield of high value-added products such as ethylene and propylene is improved.

Description

Catalytic conversion reactor and system
Technical Field
The application relates to the technical field of catalytic conversion, in particular to a catalytic conversion reactor and a catalytic conversion system.
Background
The low-carbon olefin represented by ethylene and propylene is the most basic raw material in chemical industry, and natural gas or light petroleum fraction is mostly used as a raw material at home and abroad, and the low-carbon olefin is produced by adopting a steam cracking process in an ethylene combined device. Benzene, toluene and xylene (BTX) are important basic chemical raw materials, wherein the Paraxylene (PX) accounts for about 45 percent of the total consumption amount of the BTX. With the development of polyester and other industries in China, the demand of BTX is expected to continue to increase at a high speed. About 90% of ethylene, about 70% of propylene, 90% of butadiene, and 30% of aromatics are all from steam cracking by-products. Although the steam cracking technology is developed for decades and the technology is continuously improved, the steam cracking technology still has the advantages of high energy consumption, high production cost and CO 2 The discharge amount is large, the product structure is not easy to adjust, and other technical limitations are imposed, if the petrochemical industry adopts the traditional route of preparing ethylene and propylene by steam cracking, the petrochemical industry faces a plurality of restrictive factors such as shortage of light raw oil, insufficient production capacity, high cost and the like, and in addition, along with the lightening of the steam cracking raw material, the reduction of the yield of propylene and light aromatic hydrocarbon is more an aggravated supply-demand contradiction. The catalytic cracking technology can be used as a beneficial supplement to the production process for producing the low-carbon olefin and the light aromatic hydrocarbon, and has obvious social and economic benefits for oil refining and chemical engineering integrated enterprises by adopting a catalytic technical route to produce chemical raw materials.
Chinese patent application publication CN1234426A discloses a method for simultaneously preparing low-carbon olefin and high-aromatic gasoline from heavy oil, which comprises subjecting heavy petroleum hydrocarbon and steam to catalytic cracking reaction in a composite reactor composed of a lift pipe and a dense-phase fluidized bed, so as to increase the yield of low-carbon olefin, especially propylene, and increase the aromatic content in gasoline to about 80 wt%.
Chinese patent application publication CN1393510A discloses a method for increasing the yield of ethylene and propylene by catalytic conversion of heavy petroleum hydrocarbon, which comprises contacting and reacting a hydrocarbon oil raw material with a catalyst containing pentasil zeolite in a riser or fluidized bed reactor.
Chinese patent application publication CN1721510A discloses a method for producing low-carbon olefins and aromatics by catalytic cracking in two reaction zones, which uses different weight hourly space velocities in the two reaction zones to achieve the purpose of producing low-carbon olefins such as propylene and ethylene from heavy raw oil to the maximum extent, wherein the yield of propylene exceeds 20 wt%, and simultaneously co-producing aromatics such as toluene and xylene.
U.S. patent application publications US2002003103A and US2002189973A disclose FCC units employing dual risers for propylene stimulation, wherein gasoline (60-300 ° f/15-150 ℃) produced by the cracking reaction is fed to a second riser for further reaction, and the catalyst is a mixture of USY molecular sieve and ZSM-5 molecular sieve catalyst.
The processes disclosed in U.S. patent application publication No. US2002195373A and International patent application publication No. WO2017223310A utilize a downflow reactor operating at high temperatures (1020-. The procatalyst (Y-type faujasite) has low hydrogen transfer activity and is formulated to maximize light olefin yield in conjunction with operating conditions. The high efficiency separator separates the product from the catalyst within 0.1 seconds, minimizing secondary reactions and coke formation. In addition, LCO is used to quench the separated gaseous product to about 930 ° f/500 ℃ and prevent further cracking.
The processes disclosed in US6538169A and US patent application publication US2003121825A are also reaction-regeneration systems employing two reaction zones and a common regenerator. In the first reaction zone, the heavy feedstock is cracked to light olefins or intermediates that can be converted to light olefins using high temperature and high catalyst to oil ratios. The second reaction zone consists of a second riser where the operating conditions are more severe and more light components are produced from the gasoline product. The conversion of gasoline to light olefins is aided by the use of shape selective molecular sieves such as ZSM-5, suitable feedstocks include VGO, HVGO and hydrogenated gas oil.
Chinese patent application publication CN1403540A discloses a catalytic conversion method for preparing ethylene and propylene, in which a riser and a dense-phase fluidized bed reactor are connected in series, a light raw material is injected into the riser to react at a higher severity, and the reaction product and a carbon deposit catalyst enter the fluidized bed to continue reacting under a relatively mild condition.
Chinese patent application publication CN102051213A discloses a catalytic cracking method, which comprises the steps of contacting a heavy raw material with a catalyst in a first riser reactor comprising at least two reaction zones to perform a cracking reaction, and contacting a light raw material and cracked heavy oil with the catalyst in a second riser reactor and a fluidized bed reactor to perform a cracking reaction. The method is used for heavy oil catalytic cracking, the heavy oil conversion rate and the propylene yield are high, and the dry gas and coke yield is low.
The structural contradiction of the oil refining chemical industry in China is increasingly serious, on one hand, the traditional petrochemical products have excessive capacity, and the contradiction between the supply and the demand of the finished oil is remarkable, on the other hand, the resource products and high-end petrochemical products have remarkable shortage, and the transformation of oil refining to the chemical industry is in great tendency. Catalytic cracking devices used as bridges for oil refining and chemical engineering face unprecedented pressure and challenge. At present, the proportion of blending atmospheric residue oil in a catalytic cracking device is getting larger and larger, and even the requirement of blending vacuum residue oil is raised, the most advanced catalytic cracking technology of the existing catalytic cracking technology which generally takes vacuum wax oil or paraffin-based atmospheric residue oil as a raw material adopts equipment with double lifting pipes or lifting pipes connected in series with a dense phase bed layer, and the aim of producing more low-carbon olefin and/or light hydrocarbon is achieved under the reaction condition with higher severity, and the equipment inevitably has the problems of high dry gas and coke yield and poor yield and selectivity of the target product when processing the residue-blended heavy oil. The decrease of coke yield can be achieved by adopting a descending device, but the yield of the target product is relatively low due to short retention time, limited oil agent contact efficiency and relatively low reaction conversion rate. Along with the heavy conversion of raw materials, the requirements of blending residual oil in a catalytic cracking device are more and more, and in order to efficiently utilize inferior heavy oil resources and meet the increasing demands of chemical raw materials such as low-carbon olefins and heavy aromatics, it is necessary to develop a catalytic cracking device for converting inferior heavy oil raw materials into high value-added products.
Disclosure of Invention
The present invention has an object to provide a catalytic conversion reactor and system which can greatly improve the contact efficiency of a reaction raw material, such as a hydrocarbon oil, particularly inferior heavy oil, with a catalyst, thereby effectively reducing the yield of dry gas and coke, improving the catalytic reaction selectivity, and improving the yield of high value-added products, such as ethylene, propylene, light aromatic hydrocarbons, and the like.
In order to achieve the above objects, in one aspect, the present invention provides a catalytic conversion reactor, which comprises, from bottom to top, an optional pre-lift section, a fully dense phase reaction zone, a transition section and an outlet zone, wherein the fully dense phase reaction zone is in the form of a hollow cylinder with a substantially circular cross section, an open bottom end and an open top end, and comprises one or more diameter-increasing sections with diameters increasing continuously or discontinuously from bottom to top, the optional pre-lift section is communicated with the bottom end of the fully dense phase reaction zone, the top end of the fully dense phase reaction zone is communicated with the outlet zone through the transition section, at least one catalyst inlet is arranged on the optional pre-lift section and/or the bottom of the fully dense phase reaction zone, and at least one raw material inlet is arranged on the optional pre-lift section and/or the bottom of the fully dense phase reaction zone,
wherein the cross-sectional diameter of the bottom end of the fully dense phase reaction zone is greater than or equal to the diameter of the optional pre-lift section and the cross-sectional diameter of the top end is greater than the diameter of the optional pre-lift section and the diameter of the outlet zone, and the side wall of the fully dense phase reaction zone is provided with one or more supplemental catalyst inlets each independently located at a height of greater than 0% to 90% of the total height of the fully dense phase reaction zone, preferably at a height of 20% to 80%, more preferably at a height of 30% to 75%.
In another aspect, the present invention provides a catalytic conversion reaction system comprising a catalytic conversion reactor, an oil agent separating device, an optional reaction product separating device, and a regenerator,
the catalytic conversion reactor is provided with a catalyst inlet at the bottom, a raw material feed inlet at the lower part and an oil agent outlet at the top, the oil agent separation equipment is provided with an oil agent inlet, a catalyst outlet and a reaction product outlet, the optional reaction product separation equipment is provided with a reaction product inlet, a dry gas outlet, a liquefied gas outlet, a pyrolysis naphtha outlet, a pyrolysis light oil outlet and a pyrolysis heavy oil outlet, the regenerator is provided with a catalyst inlet and a catalyst outlet,
a catalyst inlet of the catalytic conversion reactor is in fluid communication with a catalyst outlet of the regenerator, a finish oil outlet of the catalytic conversion reactor is in fluid communication with a finish oil inlet of the finish oil separation device, a reaction product outlet of the finish oil separation device is in fluid communication with a reaction product inlet of the optional reaction product separation device, a catalyst outlet of the finish oil separation device is in fluid communication with a catalyst inlet of the regenerator,
wherein the catalytic conversion reactor comprises one or more reactors according to the invention.
In yet another aspect, the present invention provides a catalytic conversion method comprising the step of contact-reacting a reaction raw material with a catalyst in a catalytic conversion reactor according to the present invention or a catalytic conversion reaction system according to the present invention.
In the catalytic conversion reactor and the system, the arranged full-dense phase reaction zone can effectively improve the density of the catalyst in the reactor, thereby greatly improving the ratio of the instantaneous catalyst to the reaction raw materials in the reactor, controlling relatively long reaction time, leading the catalyst to be capable of fully reacting with the raw materials, improving the reaction conversion rate, improving the yield of low-carbon olefin and light aromatic hydrocarbon, simultaneously reducing the reaction temperature, effectively reducing the generation of dry gas and coke, and improving the product distribution and the product quality.
When the reactor and the system are used for catalytic cracking of inferior heavy oil, chemical raw materials with high added values can be produced from the cheap inferior heavy oil to the maximum extent by petrochemical enterprises, the refining and chemical integration process of oil refining enterprises in China is facilitated to be promoted, the problem of petrochemical raw material shortage is solved, and the economic benefit and the social benefit of the petrochemical industry are improved.
Additional features and advantages of the invention will be set forth in the detailed description which follows.
Drawings
The accompanying drawings, which are included to provide a further understanding of the invention and are incorporated in and constitute a part of this specification, illustrate embodiments of the invention and together with the description serve to explain the principles of the invention and not to limit the invention. In the drawings:
FIG. 1 is a schematic view of a preferred embodiment of the present invention;
fig. 2 is a schematic view of another preferred embodiment of the present invention.
Description of the reference numerals
1 pre-lifting section 2 full dense phase reaction zone 3 transition section
4 outlet area 5 regenerative inclined tube 6 complement pipeline
7 complement pipeline 8 pre-lift medium line 9 feed line
Detailed Description
The present application will now be described in further detail with reference to specific embodiments thereof, it being understood that the specific embodiments described herein are merely illustrative and explanatory of the present application and are not restrictive thereof in any way.
Any specific value disclosed herein (including endpoints of ranges of values) is not to be limited to the precise value of that value, but rather should be construed to also encompass values close to the precise value, for example, all possible values within 5% of the precise value. Also, for the disclosed ranges of values, any combination between the endpoints of the ranges, between the endpoints and specific points within the ranges, and between specific points within the ranges can result in one or more new ranges of values, which should also be considered as specifically disclosed herein.
In this application, the term "fast fluidized bed" or "fast fluidized reaction zone/reactor" refers to a fluidized bed reaction zone/reactor in which the catalyst is in a fast fluidized state, where fast fluidization is a gas-solid contact fluidization without bubbles, the important feature being that the solid particles tend to move in clusters. The axial solids fraction epsilon of the catalyst in the reaction zone/reactor is typically in the range of 0.05 to 0.4 when the catalyst is in a fast fluidized state. However, in a conventional fast fluidized bed, the catalyst is typically distributed in a lean-down rich manner, e.g., the upper catalyst axial solids fraction ε may be in the range of 0.05 to 0.1, while the lower catalyst axial solids fraction ε may be in the range of 0.3 to 0.4.
According to the present application, in a fast fluidized reaction zone, when the axial solids fraction ε of the catalyst is maintained in the range of 0.1 to 0.2 from the bottom to the top (i.e., the axial solids fraction ε of the catalyst as measured in the upper, middle and lower axially equally divided portions of the reaction zone is 0.1 or more and 0.2 or less in each of these three portions), the catalyst is distributed in a quasi-uniform, fully concentrated phase throughout the fast fluidized reaction zone, which is referred to as a "fully concentrated phase reaction zone".
In this application, the term "water to oil weight ratio" refers to the ratio of the total steam weight injected into the reactor to the weight of the feedstock.
In this application, the terms "upstream" and "downstream" are used with reference to the direction of flow of the reactant materials. For example, when the reactant stream flows from bottom to top, "upstream" refers to a position located below, and "downstream" refers to a position located above.
Unless otherwise defined, terms used herein have the same meaning as commonly understood by one of ordinary skill in the art, and if a term is defined herein and its definition is different from that commonly understood in the art, the definition herein controls.
In the present application, anything or things that are not mentioned are directly applicable to those known in the art without any change except what is explicitly stated. Moreover, any embodiment described herein may be freely combined with one or more other embodiments described herein, and the technical solutions or ideas thus formed are considered part of the original disclosure or original description of the present invention, and should not be considered as new matters not disclosed or contemplated herein, unless a person skilled in the art would consider such combination to be clearly unreasonable.
All patent and non-patent documents referred to herein, including but not limited to textbooks and journal articles and the like, are incorporated by reference in their entirety.
As described above, in one aspect, the present invention provides a catalytic conversion reactor, which comprises, in order from bottom to top, an optional pre-lift section, a fully dense phase reaction zone, a transition section and an outlet section, wherein the fully dense phase reaction zone is in the form of a hollow cylinder with a substantially circular cross section, an open bottom end and an open top end, and comprises one or more expanding sections with diameters continuously or discontinuously increasing from bottom to top, the optional pre-lift section is communicated with the bottom end of the fully dense phase reaction zone, the top end of the fully dense phase reaction zone is communicated with the outlet section through the transition section, at least one catalyst inlet is arranged on the optional pre-lift section and/or on the bottom of the fully dense phase reaction zone, and at least one raw material inlet is arranged on the optional pre-lift section and/or on the bottom of the fully dense phase reaction zone,
wherein the bottom end of the fully dense phase reaction zone, preferably the bottom end of each expanded diameter section, has a cross-sectional diameter greater than or equal to the diameter of the optional pre-lift section, and the top end of the fully dense phase reaction zone, preferably the top end of each expanded diameter section, has a cross-sectional diameter greater than the diameter of the optional pre-lift section and the diameter of the outlet zone, and the side walls of the fully dense phase reaction zone are provided with one or more supplemental catalyst inlets, each independently located at a height greater than 0% to 90% of the total height of the fully dense phase reaction zone, preferably at a height from 20% to 80%, more preferably from 30% to 75% of the total height of the fully dense phase reaction zone.
In a preferred embodiment, the cross-sectional diameter of the top end of the fully dense phase reaction zone is greater than or equal to the cross-sectional diameter of the bottom end thereof, more preferably greater than the cross-sectional diameter of the bottom end thereof.
According to the application, the axial solid fraction epsilon of the catalyst in the fully dense phase reaction zone always satisfies from bottom to top: epsilon is more than or equal to 0.1 and less than or equal to 0.2, and at the moment, the catalyst is distributed in a fully concentrated phase in the fully concentrated phase reaction zone, so that the actual catalyst-oil ratio above and below the fully concentrated phase reaction zone is kept consistent, the dry gas coke yield is reduced, and the target product yield is improved.
According to the present application, the pre-lift section is not essential, for example when the reactor of the invention is used in series with other reactors, such as riser reactors, the fully dense phase reaction zone can be in direct communication with the outlet of the reactor located upstream without the need to employ the pre-lift section.
According to the present application, the phrase "substantially circular in cross-section" refers to a shape having a circular or nearly circular cross-section, such as an ellipse, an oval, a regular polygon, etc., as long as the ratio of the diameter of the circumscribed circle to the diameter of the inscribed circle of the cross-section is in the range of 1:0.9 to 1: 1. When the cross section is approximately circular, the diameter of the cross section (or simply diameter) refers to the average value of the diameter of the circumscribed circle and the diameter of the inscribed circle of the cross section.
According to the present application, by "diameter increases continuously" is meant that the diameter increases continuously in a linear or non-linear manner. As an example of the "diameter-enlarged section having a diameter continuously increasing from bottom to top", an inverted hollow truncated cone can be given.
According to the present application, by "discontinuously increasing in diameter" is meant that the diameter is continuously increasing in a discontinuous manner, such as stepwise or in a jump. As an example of the "diameter-enlarged section discontinuously increasing in diameter from bottom to top", a column composed of two or more hollow cylinders increasing in diameter is cited.
By way of example, the fully dense phase reaction zone may be of a cylindrical type comprising one or more inverted hollow frustoconical sections, or a cylindrical type comprising two or more hollow cylindrical sections.
In a preferred embodiment, the fully dense phase reaction zone is of the cylindrical type consisting of one or more inverted hollow-frustum sections with optional connecting sections for connecting adjacent hollow-frustum sections, or of two or more hollow-frustum sections with optional connecting sections for connecting adjacent hollow-frustum sections.
Where, according to the present application, the fully dense phase reaction zone comprises two or more expanded diameter sections, the expanded diameter sections may have the same or different heights, and the invention is not limited in this respect.
In certain preferred embodiments, the bottom of the fully dense phase reaction zone is provided with a catalyst distribution plate.
In a preferred embodiment, each expanded diameter section of the fully dense phase reaction zone is independently provided with one or more supplemental catalyst inlets; preferably, the location of each of said supplementary catalyst inlets is each independently located at a height of more than 0% to 90% of the height of the respective expanded diameter section, preferably 20% to 80% of the height, more preferably 30% to 75% of the height.
In a preferred embodiment, the diameter of the pre-lift section is from 0.2 to 5 meters, preferably from 0.4 to 4 meters, more preferably from 0.6 to 3 meters; the ratio of its height to the total height of the reactor was 0.01: 1 to 0.2: 1, preferably 0.03: 1 to 0.18: 1, more preferably 0.05: 1 to 0.15: 1.
in a preferred embodiment, the ratio of the diameter of the maximum cross-section of the fully dense phase reaction zone to the total reactor height is 0.005: 1 to 1:1, preferably 0.01: 1 to 0.8: 1, more preferably 0.05: 1 to 0.5: 1; the ratio of the total height of the fully dense phase reaction zone to the total height of the reactor was 0.1: 1 to 0.9: 1, preferably 0.15: 1 to 0.8: 1, more preferably 0.2: 1 to 0.75: 1.
in a preferred embodiment, the total height of the fully dense phase reaction zone is from about 2 to 50 meters, preferably from about 5 to 40 meters, and more preferably from about 8 to 20 meters.
In certain preferred embodiments, the fully dense phase reaction zone comprises one or more expanded diameter sections, each of which is independently in the form of an inverted hollow frustum, in which case the fully dense phase reaction zone is in the form of a cylinder comprising one or more inverted hollow frustum sections. The longitudinal section of the hollow truncated cone is an isosceles trapezoid, and the diameter of the cross section at the bottom end of the hollow truncated cone is 0.2-10 meters, preferably 0.5-8 meters, and more preferably 1-5 meters; a ratio of the top end cross-sectional diameter to the bottom end cross-sectional diameter is greater than 1 to 50, preferably 1.2 to 10, more preferably 1.5 to 5; the ratio of the diameter of the maximum cross section to the total height of the reactor is 0.005: 1 to 1:1, preferably 0.01: 1 to 0.8: 1, more preferably 0.05: 1 to 0.5: 1. the ratio of the height of the one or more expanded diameter sections to the total reactor height is each independently 0.1: 1 to 0.9: 1, preferably 0.15: 1 to 0.8: 1, more preferably 0.2: 1 to 0.75: 1 and the ratio of the total height of the fully dense phase reaction zone to the total reactor height is from 0.1: 1 to 0.9: 1, preferably 0.15: 1 to 0.8: 1, more preferably 0.2: 1 to 0.75: 1.
in certain further preferred embodiments, said fully dense phase reaction zone comprises an expanded diameter section in the form of an inverted hollow truncated cone, i.e. said fully dense phase reaction zone is in the form of an inverted hollow truncated cone with a longitudinal section in the form of an isosceles trapezoid, the cross-section at the bottom end of which has a diameter of 0.2 to 10 meters, preferably 0.5 to 8 meters, more preferably 1 to 5 meters; a ratio of the top end cross-sectional diameter to the bottom end cross-sectional diameter is greater than 1 to 50, preferably 1.2 to 10, more preferably 1.5 to 5; the ratio of the diameter of the maximum cross section to the total height of the reactor is 0.005: 1 to 1:1, preferably 0.01: 1 to 0.8: 1, more preferably 0.05: 1 to 0.5: 1; the ratio of the height of the fully dense phase reaction zone to the total reactor height is 0.1: 1 to 0.9: 1, preferably 0.15: 1 to 0.8: 1, more preferably 0.2: 1 to 0.75: 1.
in yet further preferred embodiments, the fully dense phase reaction zone comprises two or more expanded diameter sections, each of which is independently in the form of an inverted hollow truncated cone having a longitudinal section in the form of an isosceles trapezoid with a cross-sectional diameter at its bottom end in the range of 0.2 to 10 meters, preferably 0.5 to 8 meters, more preferably 1 to 5 meters; a ratio of the top end cross-sectional diameter to the bottom end cross-sectional diameter is greater than 1 to 50, preferably 1.2 to 10, more preferably 1.5 to 5; the ratio of the diameter of the maximum cross section to the total height of the reactor is 0.005: 1 to 1:1, preferably 0.01: 1 to 0.8: 1, more preferably 0.05: 1 to 0.5: 1; the ratio of the height of the two or more expanding sections to the total reactor height is each independently 0.1: 1 to 0.9: 1, preferably 0.15: 1 to 0.8: 1, more preferably 0.2: 1 to 0.75: 1 and the ratio of the total height of the fully dense phase reaction zone to the total reactor height is from 0.1: 1 to 0.9: 1, preferably 0.15: 1 to 0.8: 1, more preferably 0.2: 1 to 0.75: 1. still further preferably, each of the two or more expanding sections is independently provided with one or more make-up catalyst inlets each independently located at a height of more than 0% to 90%, preferably 20% to 80%, more preferably 30% to 75% of the height of the respective expanding section.
In other preferred embodiments, the fully dense phase reaction zone comprises one or more expanded diameter sections each independently comprising two or more hollow cylinders of increasing diameter, in which case the fully dense phase reaction zone is of the cylindrical type comprising two or more hollow cylinder sections. The two or more hollow cylinder sections each independently have a cross-sectional diameter of from 0.2 to 10 m, preferably from 1 to 5 m, the ratio of this diameter to the total reactor height being from 0.005: 1 to 1:1, preferably 0.01: 1 to 0.8: 1, more preferably 0.05: 1 to 0.5: 1, the ratio of the height of the two or more hollow cylinder sections to the total reactor height is each independently 0.1: 1 to 0.9: 1, preferably 0.15: 1 to 0.8: 1, more preferably 0.2: 1 to 0.75: 1 and the ratio of the height of the fully dense phase reaction zone to the total reactor height is from 0.1: 1 to 0.9: 1, preferably 0.15: 1 to 0.8: 1, more preferably 0.2: 1 to 0.75: 1. still further preferably, each of the two or more hollow cylinder sections is independently provided with one or more supplemental catalyst inlets at a location which is independently located at a height greater than 0% to 90% of the height of the respective hollow cylinder section, preferably 20% to 80% of the height, more preferably 30% to 75% of the height.
According to the present application, the catalyst distribution plate may be provided at the location where the catalyst enters the bottom of the fully dense phase reaction zone, for example at the outlet end of the pre-lift section.
The catalyst distribution plate may be any of various types of distribution plates commonly used in the industry, such as one or more of flat plate, arched, dished, annular, and umbrella-shaped, according to the application. The adoption of the catalyst distribution plate is helpful for enabling the catalyst to uniformly contact with the raw material in the axial direction of the full-dense phase reaction zone in concentration to carry out catalytic conversion reaction, thereby reducing the generation of agent-oil specific coke and thermal reaction coke caused by overhigh or overlow concentration of the catalyst.
In a preferred embodiment, the ratio of the height of the transition section to the total reactor height is 0.01: 1 to 0.1: 1, preferably 0.02: 1 to 0.05: 1. further preferably, the transition section is in the form of a hollow truncated cone, the longitudinal section of which is an isosceles trapezoid, the internal inclination angle alpha of the side of the isosceles trapezoid being 5-85 o Preferably 15 to 75 o 。
In a preferred embodiment, the outlet zone has a diameter of 0.2 to 5 meters, preferably 0.4 to 4 meters, more preferably 0.6 to 3 meters, and a ratio of its height to the total reactor height of 0.05: 1 to 0.2: 1, preferably 0.08: 1 to 0.18: 1, more preferably 0.1: 1 to 0.15: 1, the outlet end of the outlet area can be open or can be directly connected with the inlet of the cyclone separator.
In certain embodiments, the reactor of the present application may further comprise one or more other forms of reaction zones, such as dilute phase transport beds, dense phase fluidized beds, fast fluidized beds, etc., upstream of the fully dense phase reaction zone (e.g., between the optional pre-lift section and the fully dense phase reaction zone), and/or downstream of the fully dense phase reaction zone (e.g., between the transition section and the outlet zone).
In other embodiments, the reactor of the present application does not include additional reaction zones upstream and downstream of the fully dense phase reaction zone.
According to the present application, the reactor may be provided with one or more, e.g., one, two or more, feed inlets, which may each be independently provided at the outlet end of the pre-lift section, at a distance from its outlet end that is less than or equal to about 1/3 of the height of the pre-lift section, or at the bottom of the fully dense phase reaction zone.
Optionally, when a raw material feed port is provided at the bottom of the fully dense phase reaction zone, a gas distributor may be provided at the raw material feed port.
According to the present application, the carbon content of the make-up catalyst may be in the range of from 0 to 1% by weight, and may for example be selected from one or more of regenerated catalyst, spent catalyst and semi-regenerated catalyst. The supplemental catalyst inlets can be 1, 2, or more and are each independently located at a height greater than 0% to 90% of the total height of the fully dense phase reaction zone, preferably at a height from 20% to 80% of the height of the fully dense phase reaction zone, more preferably at a height from 30% to 75%, for example at a height of 2/3% of the fully dense phase reaction zone. The temperature of the supplementary catalyst can be adjusted according to the reaction temperature, for example, cold and/or hot regenerated catalyst can be introduced, and cold and/or hot spent catalyst can also be introduced. The catalyst can be supplemented in the full-dense phase reaction zone to adjust the oil ratio of the catalyst in a larger range, more active centers are provided for the cracking reaction, meanwhile, the flexibility of adjusting the reaction temperature is enhanced, and the gradient of the temperature in equipment of the full-dense phase reaction zone and the activity of the catalyst can be effectively adjusted. In addition, the supplementary catalyst is introduced into the full-dense phase reaction zone, so that the density uniformity of the catalyst in the equipment can be maintained as much as possible, the density distribution of the catalyst is effectively adjusted, the cracking reaction is ensured to be fully and effectively carried out, and the selectivity of a target product is improved.
In a second aspect, the present application provides a catalytic conversion reaction system comprising a catalytic conversion reactor, an oil separation device, an optional reaction product separation device, and a regenerator,
the catalytic conversion reactor is provided with a catalyst inlet at the bottom, a raw material feed inlet at the lower part and an oil agent outlet at the top, the oil agent separation equipment is provided with an oil agent inlet, a catalyst outlet and a reaction product outlet, the optional reaction product separation equipment is provided with a reaction product inlet, a dry gas outlet, a liquefied gas outlet, a pyrolysis naphtha outlet, a pyrolysis light oil outlet and a pyrolysis heavy oil outlet, the regenerator is provided with a catalyst inlet and a catalyst outlet,
the catalyst inlet of the catalytic conversion reactor is in fluid communication with the catalyst outlet of the regenerator, the finish oil outlet of the catalytic conversion reactor is in fluid communication with the finish oil inlet of the finish oil separation device, the reaction product outlet of the finish oil separation device is in fluid communication with the reaction product inlet of the optional reaction product separation device, and the catalyst outlet of the finish oil separation device is in fluid communication with the catalyst inlet of the regenerator.
In a preferred embodiment, the catalytic conversion reactor comprises one or more reactors according to the present application.
In certain further preferred embodiments, the catalytic conversion reactor further comprises one or more other forms of reactor, such as dilute phase transport beds, dense phase fluidized beds, fast fluidized beds, etc., in series and/or in parallel with the reactor of the present application.
In yet other further preferred embodiments, the catalytic conversion reactor consists of the reactor of the present application.
According to the present application, the oil separation device and the reaction product separation device may be any devices known to those skilled in the art. For example, the oil separation device may include a cyclone, a settler, a stripper, and the like, and the reaction product separation device may be a fractionation column, and the like.
In certain embodiments, the oil separation device comprises a settler arranged coaxially or in high-low juxtaposition with the catalytic conversion reactor.
The catalytic conversion reactor and the catalytic conversion system are suitable for catalytic conversion reaction of various raw materials, such as the reaction for producing low-carbon olefin by catalytic cracking of petroleum hydrocarbon, particularly the reaction for producing low-carbon olefin by catalytic cracking of heavy oil.
In certain embodiments, the properties of heavy oils suitable for processing using the reactors and systems of the present invention can meet one, two, three, or four of the following criteria: the density at 20 ℃ is 850- 3 Preferably 890- 3 Carbon residue of 0 to 10 wt.%, preferably 2 to 8 wt.%, nickel and vanadium content of 2 to 30ppm, preferably 5 to 20ppm, and a characteristic factor K of less than 12.1, preferably less than 12.0.
For example, the heavy oil can be a heavy petroleum hydrocarbon and/or other mineral oil; the heavy petroleum hydrocarbon may be selected from one or more of Vacuum Residue (VR), low quality Atmospheric Residue (AR), low quality hydrogenated residue, coker gas oil, deasphalted oil, vacuum wax oil, high acid number crude oil, and high metal crude oil, and the other mineral oil may be selected from one or more of coal liquefied oil, oil sand oil, and shale oil. The carbon residue in the heavy oil can be measured by adopting an ASTMD-189 Conradson carbon residue experimental method.
In a third aspect, the present invention provides a catalytic conversion process comprising the step of contact reacting a reaction feedstock with a catalyst in a catalytic conversion reactor according to the present invention or in a catalytic conversion reaction system according to the present invention.
In a preferred embodiment, the reaction starting materialsIs heavy raw oil, and the properties of the heavy raw oil meet at least one of the following indexes: the density at 20 ℃ is 850- 3 Preferably 890- 3 Carbon residue of 0 to 10 wt.%, preferably 2 to 8 wt.%, nickel and vanadium content of 2 to 30ppm, preferably 5 to 20ppm, and a characteristic factor K of less than 12.1, preferably less than 12.0.
In a preferred embodiment, the reaction conditions within the fully dense phase reaction zone include: the reaction temperature is 510-700 ℃, the reaction time is 1-20 seconds, and the weight ratio of the catalyst to the oil is 3: 1 to 50: 1, the weight ratio of water to oil is 0.03: 1 to 0.8: 1, catalyst density of 120- 3 The gas linear speed is 0.8-2.5 m/s, the reaction pressure is 130-450 kPa, and the mass flow rate of the catalyst is 15-150 kg/(m) 2 Seconds).
In a further preferred embodiment, the reaction conditions within the fully dense phase reaction zone include: the reaction temperature is 550-650 ℃, the reaction time is 3-15 seconds, and the weight ratio of the catalyst to the oil is 10: 1 to 30: 1, the weight ratio of water to oil is 0.05: 1 to 0.5: 1, catalyst density of 150- 3 The gas linear velocity is 1-1.8 m/s, the reaction pressure is 130-450 kPa, and the mass flow rate of the catalyst is 20-130 kg/(m) 2 Seconds).
In a preferred embodiment, the catalyst comprises from 1 to 50 wt%, preferably from 5 to 45 wt%, more preferably from 10 to 40 wt% zeolite on a dry basis and based on the weight of the catalyst on a dry basis; 5-99 wt%, preferably 10-80 wt%, more preferably 20-70 wt% of an inorganic oxide, and 0-70 wt%, preferably 5-60 wt%, more preferably 10-50 wt% of a clay.
In a further preferred embodiment, the zeolite comprises an intermediate pore zeolite selected from the group consisting of ZSM series zeolites, ZRP zeolites, and any combination thereof, and optionally a large pore zeolite; the large pore zeolite is selected from the group consisting of rare earth Y-type zeolite, rare earth hydrogen Y-type zeolite, ultrastable Y-type zeolite, and high silicon Y-type zeolite, and any combination thereof.
In a still further preferred embodiment, the medium pore zeolite comprises from 0 to 50 wt%, preferably from 0 to 20 wt%, of the total weight of the zeolite on a dry basis.
In this application, the medium and large pore zeolites are as conventionally defined in the art, i.e., the medium pore size of the medium pore zeolite is from about 0.5 to 0.6 nm and the large pore zeolite is from about 0.7 to 1.0 nm.
By way of example, the large-pore zeolite may be selected from one or more of rare earth Y (rey) type zeolites, rare earth hydrogen Y (rehy) type zeolites, ultrastable Y-type zeolites obtained by different processes, and high-silica Y-type zeolites. The medium pore zeolite may be selected from zeolites having the MFI structure, such as ZSM series zeolites and/or ZRP zeolites. Optionally, the mesoporous zeolite may be modified with a nonmetallic element such as phosphorus and/or a transition metal element such as iron, cobalt, nickel. A more detailed description of ZRP zeolites can be found in U.S. Pat. No. US5,232,675A. The ZSM-series zeolite is preferably one or a mixture of more selected from ZSM-5, ZSM-11, ZSM-12, ZSM-23, ZSM-35, ZSM-38, ZSM-48 and other zeolites of similar structure. For a more detailed description of ZSM-5, see U.S. Pat. No. US3,702,886A.
According to the application, the inorganic oxide is preferably silicon dioxide (SiO) as a binder 2 ) And/or alumina (Al) 2 O 3 ). The clay acts as a matrix (i.e., carrier), preferably kaolin and/or halloysite.
In a preferred embodiment, the process comprises introducing one or more make-up catalysts into the fully dense phase reaction zone, the total amount of which can range from 0 to 50 wt%, preferably from 5 to 45 wt%, more preferably from 10 to 40 wt%, of the reactor catalyst recycle.
Preferably, the one or more supplemental catalysts each independently have a carbon content of about 0 to 1.0 weight percent, e.g., the one or more supplemental catalysts may each independently be selected from regenerated catalysts, spent catalysts, and semi-regenerated catalysts, e.g., regenerated, spent, and semi-regenerated catalytic cracking catalysts.
The present application will be further described with reference to preferred embodiments shown in the drawings, but the application is not limited thereto.
FIG. 1 shows the catalytic conversion reaction of the present applicationA preferred embodiment of the reactor, wherein the reactor comprises, from bottom to top, a pre-lift section 1, a fully dense phase reaction zone 2, a transition section 3 and an outlet section 4. The fully dense phase reaction zone 2 is in an inverted hollow truncated cone shape, and the longitudinal section of the fully dense phase reaction zone is in an isosceles trapezoid shape. The transition section 3 is in the form of a hollow truncated cone, the longitudinal section of which is in the form of an isosceles trapezoid, the internal inclination angle alpha of the side of which is about 5-85 o Preferably about 15 to 75 o . The lower part of the pre-lifting section 1 is provided with a catalyst inlet, and the upper part of the pre-lifting section 1 and/or the bottom of the full-dense phase reaction zone 2 is provided with a raw material inlet. The cross-sectional diameter of the bottom end of the fully dense phase reaction zone is greater than the diameter of the pre-lift section, and the cross-sectional diameter of the top end is greater than the diameter of the pre-lift section and the diameter of the outlet zone. The side wall of the fully dense phase reaction zone is provided with one or more, e.g., one, two or more make-up catalyst inlets, such as make-up catalyst inlets for make-up line 6 or make-up line 7. The one or more supplemental catalyst inlets are each independently positioned at a height that is between greater than 0% and about 90% of the total height of the fully concentrated phase reaction zone, preferably at a height of about 20% to about 80%, more preferably at a height of about 30% to about 75%.
The pre-lift medium enters the catalytic conversion reactor from the bottom of the pre-lift section 1 through a pre-lift medium line 8, and the pre-lift medium can be dry gas, water vapor or a mixture thereof. The hot regenerated catalyst, with or without cooling, from the regeneration chute 5 enters the lower part of the pre-lift section 1 and moves upwards under the lifting action of the pre-lift medium. Reaction raw materials such as preheated heavy raw oil and atomized steam are injected into the upper part of the pre-lifting section 1 and/or the bottom of the full-dense phase reaction zone 2 through a feed pipeline 9, are mixed and contacted with the existing material flow in the catalytic conversion reactor, and carry out catalytic conversion reaction in the process of passing through the reactor from bottom to top. One or more make-up catalysts are introduced in the fully concentrated phase reaction zone 2 via make-up line 6 and/or make-up line 7 and are contacted with the feed in the fully concentrated phase reaction zone to effect the catalytic conversion reaction. The reaction effluent of the fully dense phase reaction zone 2 enters an outlet zone 4 through a transition section 3, and then enters subsequent oil agent separation equipment and product separation equipment through the outlet zone 4.
Fig. 2 shows another preferred embodiment of the catalytic conversion reactor of the present application, wherein the reactor comprises, from bottom to top, a pre-lift section 1, a fully dense phase reaction zone 2, a transition section 3 and an outlet zone 4. The fully dense phase reaction zone 2 is of a cylindrical type comprising two inverted hollow truncated cone sections, and the longitudinal section of each hollow truncated cone section is of an isosceles trapezoid shape. The transition section 3 is in the form of a hollow truncated cone, the longitudinal section of which is in the form of an isosceles trapezoid, the internal inclination angle alpha of the side of which is about 5-85 o Preferably about 15 to 75 o . The lower part of the pre-lifting section 1 is provided with a catalyst inlet, and the upper part of the pre-lifting section 1 and/or the bottom of the full-dense phase reaction zone 2 is provided with a raw material inlet. The cross-sectional diameter of the bottom end of each of the hollow frustocone segments is greater than the diameter of the pre-lift segment and the cross-sectional diameter of the top end is greater than the diameter of the pre-lift segment and the diameter of the exit region. The side wall of each of said hollow frustocone sections is provided with one or more, e.g. one, two or more, make-up catalyst inlets, e.g. for make-up line 6 or make-up line 7. The one or more supplemental catalyst inlets are each independently located at a height between greater than 0% to about 90% of the height of the respective hollow frustum section, preferably at a height of about 20% to about 80%, more preferably at a height of about 30% to about 75%.
The pre-lift medium, which may be dry gas, steam or a mixture thereof, enters the catalytic conversion reactor from the bottom of the pre-lift section 1 via a pre-lift medium line 8. The hot regenerated catalyst, with or without cooling, from the regeneration chute 5 enters the lower part of the pre-lift section 1 and moves upwards under the lifting action of the pre-lift medium. Reaction raw materials such as preheated heavy raw oil and atomized steam are injected into the upper part of the pre-lifting section 1 and/or the bottom of the full-dense phase reaction zone 2 through a feed pipeline 9, are mixed and contacted with the existing material flow in the catalytic conversion reactor, and carry out catalytic conversion reaction in the process of passing through the reactor from bottom to top. One or more make-up catalysts are introduced in the fully dense phase reaction zone 2 via make-up line 6 and/or make-up line 7 to contact the feed in the fully dense phase reaction zone for catalytic conversion reactions. The reaction effluent of the fully dense phase reaction zone 2 enters an outlet zone 4 through a transition section 3, and then enters subsequent oil agent separation equipment and product separation equipment through the outlet zone 4.
The definition and calculation of each parameter in the application are as follows:
(1) the axial solids fraction of the catalyst, ε = the pressure difference between two points in the reaction zone in the axial direction measured by a pressure difference meter divided by the distance between the two points in the axial direction divided by the catalyst particle density;
wherein the unit of the pressure difference is kilogram/meter 2 The distance between two axial points is expressed in meters, and the density of the catalyst particles is expressed in kilograms per meter 3 。
Catalyst particle density = framework density/(catalyst pore volume x framework density + 1), where the unit of framework density is kg/m 3 The unit of pore volume of the catalyst is meter 3 The skeletal density and the pore volume of the catalyst were measured by the pycnometer method and the water titration method, respectively.
(2) Reaction time = volume of reaction zone/oil gas log mean volume flow;
wherein the volume of the reaction zone is measured in meters 3 The unit of the logarithmic mean volume flow of oil and gas is meter 3 A/second;
oil gas log mean volume flow = (V) out -V in ）/ln（V out /V in ），V out And V in The volume flow of oil gas at the outlet and the inlet of the reaction zone respectively;
volume flow V of oil gas at outlet of reaction zone out =m/ρ 3 ；
Volume flow V of oil gas at inlet of reaction zone in =m/ρ 4 ；
Wherein m is the feeding amount of raw oil and atomized steam in unit time, and the unit is kilogram/second; ρ is a unit of a gradient 3 The density of oil gas at the outlet of the reaction zone is in kilograms/meter 3 ；ρ 4 The density of oil gas at the inlet of the reaction zone is expressed in kg/m 3 。
(3) The catalyst density of the reaction zone (or upper, middle and lower parts thereof) is = the pressure difference between two points in the axial direction in the reaction zone (or upper, middle and lower parts thereof) measured by a pressure difference meter divided by the distance between the two points in the axial direction;
wherein the unit of the pressure difference is kilogram/meter 2 The reaction zone is axially divided into an upper part, a middle part and a lower part, and the unit of the distance between the two axial points is meter.
(4) Gas linear velocity = oil gas logarithmic mean volume flow ÷ reaction zone cross-sectional area;
when the reaction zone is of a non-cylindrical type, the gas linear velocity is the logarithmic average of the gas linear velocity at the bottom of the reaction zone and the gas linear velocity at the top of the reaction zone.
(5) Catalyst mass flow rate G s = reactor catalyst circulation ÷ reaction zone cross-sectional area;
when the reaction zone is of a non-cylindrical type, the catalyst mass flow rate G s Taking the bottom G of the reaction zone s G from the top of the reaction zone s A logarithmic average of;
wherein the unit of the catalyst circulating amount is kilogram/second;
reactor catalyst circulation = coke formation speed ÷ (spent catalyst carbon content-regenerated catalyst carbon content);
wherein, the unit of coke generation speed is kilogram/second, and the carbon content of the spent catalyst and the carbon content of the regenerated catalyst are both weight content;
coke formation rate = flue gas amount × (CO) 2 %+CO%）÷Vm×M；
Wherein Vm is the molar volume of gas and is 22.4 multiplied by 10 -3 Rice made of glutinous rice 3 M is the molar mass of carbon and takes the value of 12 multiplied by 10 -3 Kilogram/mole;
flue gas amount = (regeneration air amount × 79 vol%)/(1-CO 2 %-CO%-O 2 %）；
Wherein the regeneration air quantity is in meters 3 Second, the unit of smoke is meter 3 Second, CO 2 %、CO%、O 2 % of respectively CO in the flue gas 2 CO and O 2 Volume percent of (a).
Examples
The following examples further illustrate the invention but are not intended to limit the invention thereto.
The feed oils used in the following examples and comparative examples were hydrogenated residual oils, properties of which are shown in Table 1, and the catalysts used were commercial catalytic cracking catalysts available from catalyst division of petrochemical Co., Ltd., China, under the trade designation DMMC-2.
TABLE 1 Properties of the stock oils used
Density (20 deg.C)/g.cm -3 0.9237
Refractive index/70 deg.C 1.4914
Basic nitrogen/microgram g -1 506
Carbon residue/wt.% 3.11
Value of characteristic factor K 11.8
Distillation range/. degree C
5% by volume 357
10% by volume 387
30% by volume 443
50% by volume 490
70% by volume 550
Metal content/microgram g -1
Fe 34.4
Ni 4.4
Ca 7.8
V 4.3
Na 2.0
Example 1
The experiments were carried out on a medium-sized apparatus using the base oil and DMMC-2 catalyst shown in Table 1, the reactor being in the form of the reactor shown in FIG. 1, in which the pre-lift section had a diameter of 0.2 m and a height of 1 m; the diameter of the lower section of the fully-concentrated phase reaction zone is 0.4 meter, the diameter of the upper section of the fully-concentrated phase reaction zone is 0.5 meter, and the height of the fully-concentrated phase reaction zone is 4 meters; the height of the transition section is 0.5 m, and the inner inclination angle alpha of the isosceles trapezoid side edge of the longitudinal section is 40 o (ii) a Straight in the outlet zoneThe diameter is 0.2 m and the height is 1 m.
The preheated raw oil enters the upper part of the pre-lifting section to contact with a catalytic cracking catalyst and enters a full-dense phase reaction zone from bottom to top to perform catalytic cracking reaction, the catalyst in the full-dense phase reaction zone is distributed in a full-dense phase, and the axial solid fraction epsilon is distributed in the range of 0.1-0.2 from bottom to top. And the reacted material flow enters a transition section and then enters subsequent oil agent separation equipment and product separation equipment through an outlet area. Wherein a stream of hot regenerated catalyst (temperature 695 ℃, carbon content 0.05 wt%) was replenished to the fully dense phase reaction zone at a level 50% of the total height of the fully dense phase reaction zone, and a stream of spent catalyst (carbon content 0.8 wt%) was replenished at a level 60% of the total height of the fully dense phase reaction zone, wherein the amounts of the replenished regenerated catalyst and spent catalyst were 10 wt% and 5 wt%, respectively, of the reactor catalyst circulation, and the operating conditions and product distribution are listed in table 2.
As can be seen from table 2, the ethylene yield of this example reached 5.3 wt%, the propylene yield reached 20.8 wt%, the light aromatic hydrocarbons (BTX) yield reached 11.7 wt%, and the dry gas and coke yields were 10.4 wt% and 8.2 wt%, respectively.
Example 2
The experiments were carried out on a medium-sized apparatus using the feed oil and DMMC-2 catalyst shown in Table 1, the reactor being in the form of the reactor shown in FIG. 1, wherein the pre-lift section had a diameter of 0.6 m and a height of 1.5 m; the diameter of the lower section of the fully-concentrated phase reaction zone is 0.8 meter, the diameter of the upper section of the fully-concentrated phase reaction zone is 1.6 meters, and the height of the fully-concentrated phase reaction zone is 6 meters; the height of the transition section is 1 meter, and the inclination angle alpha of the isosceles trapezoid side edge of the longitudinal section is 27 o (ii) a The exit zone was 0.6 meters in diameter and 1.5 meters in height.
The preheated raw oil enters the upper part of the pre-lifting section to contact with a catalytic cracking catalyst and enters a full-dense phase reaction zone from bottom to top to perform catalytic cracking reaction, the catalyst in the full-dense phase reaction zone is distributed in a full-dense phase, and the axial solid fraction epsilon is distributed in the range of 0.1-0.2 from bottom to top. And the reacted material flow enters a transition section and then enters subsequent oil agent separation equipment and product separation equipment through an outlet area. Wherein, a strand of cooled regenerated catalyst (temperature 630 ℃, carbon content 0.05 wt%) is supplemented to the fully dense phase reaction zone at a position 55% of the total height of the fully dense phase reaction zone, and a strand of spent catalyst (carbon content 0.8 wt%) is supplemented at a position 65% of the total height of the fully dense phase reaction zone, wherein the amounts of the supplemented regenerated catalyst and spent catalyst respectively account for 10 wt% and 5 wt% of the catalyst circulation volume of the reactor; the operating conditions and product distribution are listed in table 2.
As can be seen from table 2, the ethylene yield of this example reached 5.5 wt%, the propylene yield reached 21.6 wt%, the light aromatic hydrocarbons (BTX) yield reached 11.5 wt%, and the dry gas and coke yields were 10.3 wt% and 8.5 wt%, respectively.
Example 3
The experiments were carried out on a medium-sized apparatus using the feedstock oil and DMMC-2 catalyst shown in Table 1, the reactor being of the form shown in FIG. 2, in which the fully dense phase reaction zone comprises two inverted hollow frusto-conical sections in series, with a pre-lift section of 0.6 m diameter and a height of 1.5 m; the diameters of the lower sections of the two inverted hollow truncated cone sections are both 0.8 meter, the diameters of the upper sections of the two inverted hollow truncated cone sections are both 1.6 meters, and the heights of the two inverted hollow truncated cone sections are both 3 meters; the height of the transition section is 0.5 m, and the inclination angle alpha of the isosceles trapezoid side edge of the longitudinal section is 26.5 o (ii) a The exit zone was 0.6 meters in diameter and 1.5 meters in height.
The preheated raw oil enters the upper part of the pre-lifting section to contact with a catalytic cracking catalyst and enters a full-dense phase reaction zone from bottom to top to perform catalytic cracking reaction, the catalyst in the full-dense phase reaction zone is distributed in a full-dense phase, and the axial solid fraction epsilon is distributed in the range of 0.1-0.2 from bottom to top. And the reacted material flow enters a transition section and then enters subsequent oil agent separation equipment and product separation equipment through an outlet area. Wherein, a hot regenerated catalyst (temperature 695 ℃, carbon content 0.05 wt%) is supplemented to the fully dense phase reaction zone at a position at 60% of the height of the lower hollow truncated cone section, and a spent catalyst (carbon content 0.8 wt%) is supplemented at a position at 60% of the height of the upper hollow truncated cone section, wherein the amounts of the supplemented regenerated catalyst and spent catalyst respectively account for 10 wt% and 5 wt% of the catalyst circulation amount of the reactor; the operating conditions and the product distribution are listed in table 2.
As can be seen from table 2, the ethylene yield of this example reached 5.6 wt%, the propylene yield reached 22.0 wt%, the light aromatic hydrocarbons (BTX) yield reached 10.5 wt%, and the dry gas and coke yields were 10.5 wt% and 8.7 wt%, respectively.
Comparative example 1
The test was carried out on a medium-sized apparatus using the raw oil and DMMC-2 catalyst shown in Table 1, the reactor being a combined reactor in which a riser having a diameter of 0.2 m and a height of 5 m was connected in series with a dense-phase fluidized bed having a diameter of 0.4 m and a height of 1.5 m. The preheated raw oil enters the lower part of a riser reaction zone to contact with a catalytic cracking catalyst for catalytic cracking reaction, the reaction oil, the water vapor and the spent catalyst enter a dense-phase fluidized bed reaction zone from an outlet of the riser for continuous reaction, and the material flow after the reaction enters subsequent oil agent separation equipment and product separation equipment; the operating conditions and the product distribution are listed in table 2.
As can be seen from the results of table 2, the comparative example had an ethylene yield of only 3.7 wt%, a propylene yield of only 12.8 wt%, a light aromatic hydrocarbon (BTX) yield of only 5.5 wt%, and dry gas and coke yields of 12.9 wt% and 13.3 wt%, respectively.
Comparative example 2
The tests were carried out on a medium-sized apparatus using the raw oil and DMMC-2 catalyst shown in Table 1, and the reactor was a conventional fast fluidized bed reactor having a diameter of 1.2 m and a height of 6 m. The preheated raw oil enters the lower part of a fast fluidized bed reactor to contact with a catalytic cracking catalyst for catalytic cracking reaction, and the reacted material flow enters subsequent oil agent separation equipment and product separation equipment, wherein the axial solid fraction epsilon of the catalyst in the fast fluidized bed reactor is gradually increased from top to bottom by 0.1 → 0.2 → 0.3; the operating conditions and the product distribution are listed in table 2.
As can be seen from the results of table 2, the comparative example had an ethylene yield of only 4.2 wt%, a propylene yield of only 16.2 wt%, a light aromatic hydrocarbon (BTX) yield of only 8.6 wt%, and dry gas and coke yields of 11.3 wt% and 10.4 wt%, respectively.
TABLE 2 comparison of reaction results of examples 1-3 and comparative examples 1-2
Example 1 Example 2 Example 3 Comparative example 1 Comparative example 2
Riser/fast bed/full dense phase reaction zone conditions
Outlet temperature of reaction zone,. deg.C 585 585 585 585 585
Reaction time in seconds 4 4 4 2 4
Water to oil weight ratio 0.25 0.25 0.25 0.25 0.25
Weight ratio of solvent to oil 22 23 23 10 20
Lower catalyst density, kg/m 3 220 224 218 60 190
Upper catalyst density, kg/m 3 215 220 214 110
Gas lineSpeed, m/s 2 2 2 12 2
Reaction pressure, kPa 210 210 210 210 210
Gs, kg/(meter) 2 Second) 74 75 75 300 74
Dense phase fluidized bed conditions
Outlet temperature of reaction zone,. deg.C / / / 565 /
Weight hourly space velocity, hours -1 / / / 4 /
Catalyst density in kg/m 3 / / / 480 /
Linear velocity of gas, m/s / / / 0.6 /
Product distribution, weight%
Dry gas 10.4 10.3 10.5 12.9 11.3
Wherein ethylene 5.3 5.5 5.6 3.7 4.2
Liquefied gas 38.6 40.1 42.3 26.1 33.2
Wherein propylene is 20.8 21.6 22.0 12.8 16.2
Gasoline (R) and its preparation method 27.1 25.9 23.7 22.9 24.8
Wherein BTX 11.7 11.5 10.5 5.5 8.6
Diesel oil 11.5 11.1 10.9 16.4 14.2
Heavy oil 4.2 4.1 3.9 8.4 6.1
Coke 8.2 8.5 8.7 13.3 10.4
Is totaled 100 100 100 100 100
From the results of the above examples and comparative examples, it can be seen that the yield of ethylene, propylene and light aromatic hydrocarbons is significantly increased while the yield of dry gas and coke is decreased by performing the catalytic cracking of heavy oil using the reactor of the present invention.
The preferred embodiments of the present application have been described above in detail, however, the present application is not limited to the details of the above embodiments, and various simple modifications may be made to the technical solution of the present application within the technical idea of the present application, and these simple modifications all belong to the protection scope of the present application.
It should be noted that, in the foregoing embodiments, various features described in the above embodiments may be combined in any suitable manner, and in order to avoid unnecessary repetition, various possible combinations are not described in the present application.
In addition, any combination of the various embodiments of the present application is also possible, and the same should be considered as the content of the invention of the present application as long as it does not depart from the idea of the present application.

Claims (32)

1. A catalytic conversion reactor comprises an optional pre-lifting section, a fully dense phase reaction zone, a transition section and an outlet zone from bottom to top in sequence, wherein the fully dense phase reaction zone is in the form of a hollow cylinder which is approximately circular in cross section, open at the bottom end and the top end and comprises one or more expanding sections with diameters continuously or discontinuously increasing from bottom to top, the optional pre-lifting section is communicated with the bottom end of the fully dense phase reaction zone, the top end of the fully dense phase reaction zone is communicated with the outlet zone through the transition section, at least one catalyst inlet is arranged on the optional pre-lifting section and/or the bottom of the fully dense phase reaction zone, and at least one raw material feeding hole is arranged on the optional pre-lifting section and/or the bottom of the fully dense phase reaction zone,
wherein the axial solids fraction epsilon of the catalyst in the fully dense phase reaction zone is maintained in the range of from 0.1 to 0.2 throughout from bottom to top, the cross-sectional diameter of the bottom end of the fully dense phase reaction zone is greater than or equal to the diameter of the optional pre-lift section and the cross-sectional diameter of the top end is greater than the diameter of the optional pre-lift section and the diameter of the outlet zone, and the side wall of the fully dense phase reaction zone is provided with one or more supplemental catalyst inlets each independently located at a height of from greater than 0% to 90% of the total height of the fully dense phase reaction zone.
2. The reactor of claim 1, wherein the one or more supplemental catalyst inlets are each independently located at 20% to 80% of the height of the fully dense phase reaction zone.
3. The reactor of claim 1, wherein the one or more supplemental catalyst inlets are each independently located at 30% to 75% of the height of the fully dense phase reaction zone.
4. The reactor of any one of claims 1-3, wherein the one or more expanded diameter sections are each independently an inverted hollow frustoconical pattern, or a cylindrical pattern comprised of two or more sections of hollow cylinders of increasing diameter.
5. The reactor of claim 4, wherein each expanded diameter section of the fully dense phase reaction zone is independently provided with one or more supplemental catalyst inlets.
6. The reactor of claim 5, wherein the location of each of the supplemental catalyst inlets of each expanded diameter section is each independently located at a height greater than 0% to 90% of the height of the respective expanded diameter section.
7. The reactor of claim 5 wherein the location of each of the supplemental catalyst inlets of each expanded diameter section is each independently located at a height of 20% to 80% of the height of the respective expanded diameter section.
8. The reactor of claim 5 wherein the location of each of the supplemental catalyst inlets of each expanded diameter section is each independently located at a height of 30% to 75% of the height of the respective expanded diameter section.
9. The reactor of claim 5, wherein the bottom of the fully dense phase reaction zone is provided with a catalyst distribution plate.
10. The reactor according to any one of claims 1-3, wherein the pre-lift section has a diameter of 0.2-5 meters; the ratio of its height to the total height of the reactor was 0.01: 1 to 0.2: 1.
11. the reactor according to any one of claims 1-3, wherein the pre-lift section has a diameter of 0.4-4 meters; the ratio of its height to the total height of the reactor was 0.03: 1 to 0.18: 1.
12. the reactor according to any one of claims 1-3, wherein the pre-lift section has a diameter of 0.6-3 meters; the ratio of its height to the total reactor height is 0.05: 1 to 0.15: 1.
13. the reactor of any one of claims 1-3, wherein the ratio of the diameter of the maximum cross-section of the fully dense phase reaction zone to the total reactor height is 0.005: 1 to 1: 1; the ratio of the total height of the fully dense phase reaction zone to the total height of the reactor was 0.1: 1 to 0.9: 1.
14. the reactor of any one of claims 1-3, wherein the ratio of the diameter of the maximum cross-section of the fully dense phase reaction zone to the total reactor height is from 0.01: 1 to 0.8: 1; the ratio of the total height of the fully dense phase reaction zone to the total reactor height was 0.15: 1 to 0.8: 1.
15. the reactor of any one of claims 1-3, wherein the ratio of the diameter of the maximum cross-section of the fully dense phase reaction zone to the total reactor height is 0.05: 1 to 0.5: 1; the ratio of the total height of the fully dense phase reaction zone to the total reactor height was 0.2: 1 to 0.75: 1.
16. the reactor according to any one of claims 1 to 3, wherein each of said one or more expanding sections is independently in the form of an inverted hollow truncated cone, with a longitudinal section in the form of an isosceles trapezoid, having a diameter of 0.2-10 m in cross section at its bottom end; the ratio of the diameter of the top end cross section to the diameter of the bottom end cross section is greater than 1 to 50; the ratio of the diameter of the largest cross-section to the total height of the reactor is 0.005: 1 to 1: 1; the ratio of the height of the one or more expanded diameter sections to the total reactor height is each independently 0.1: 1 to 0.9: 1 and the ratio of the total height of the fully dense phase reaction zone to the total reactor height is from 0.1: 1 to 0.9: 1.
17. the reactor of claim 16, wherein the diameter of the bottom end cross section of the one or more expanded diameter sections is 0.5-8 meters; the ratio of the diameter of the top end cross section to the diameter of the bottom end cross section is 1.2 to 10; the ratio of the diameter of the maximum cross section to the total height of the reactor was 0.01: 1 to 0.8: 1; the ratio of the height of the one or more expanding sections to the total reactor height is each independently 0.15: 1 to 0.8: 1 and the ratio of the total height of the fully dense phase reaction zone to the total height of the reactor is 0.15: 1 to 0.8: 1.
18. the reactor of claim 16, wherein the diameter of the bottom end cross section of the one or more expanded diameter sections is 1-5 meters; the ratio of the diameter of the top end cross section to the diameter of the bottom end cross section is 1.5 to 5; the ratio of the diameter of the maximum cross section to the total height of the reactor was 0.05: 1 to 0.5: 1; the ratio of the height of the one or more expanding sections to the total reactor height is each independently 0.2: 1 to 0.75: 1 and the ratio of the total height of the fully dense phase reaction zone to the total reactor height is 0.2: 1 to 0.75: 1.
19. the reactor of any of claims 1-3, wherein the ratio of the height of the transition section to the total reactor height is 0.01: 1 to 0.1: 1; the transition section is in the form of a hollow truncated cone, the longitudinal section of the transition section is in the form of an isosceles trapezoid, and the inner inclination angle alpha of the side edge of the isosceles trapezoid is 5-85 o 。
20. The reactor of claim 19, wherein the ratio of the height of the transition section to the total reactor height is 0.02: 1 to 0.05: 1; the inner inclination angle alpha of the isosceles trapezoid side edge of the transition section is 15-75 o 。
21. A reactor according to any one of claims 1 to 3, wherein the outlet zone has a diameter of 0.2 to 5 meters and a height to total reactor height ratio of 0.05: 1 to 0.2: 1, the outlet end of the outlet area can be opened or can be directly connected with the inlet of the cyclone separator.
22. The reactor of claim 21 wherein the outlet zone has a diameter of 0.4 to 4 meters and a ratio of height to total reactor height of 0.08: 1 to 0.18: 1.
23. the reactor of claim 21 wherein the outlet zone has a diameter of 0.6 to 3 meters and a height to total reactor height ratio of 0.1: 1 to 0.15: 1.
24. the reactor according to any one of claims 1-3, wherein each of the at least one feedstock feeds is independently provided at a location 1/3 on the pre-lift section at a distance from its outlet end that is less than or equal to the height of the pre-lift section, at the outlet end of the pre-lift section, or at the bottom of the fully dense phase reaction zone.
25. The reactor of claim 24, wherein a feed inlet is provided at the bottom of the fully dense phase reaction zone and a gas distributor is provided at the feed inlet.
26. The reactor of any one of claims 1-3, wherein the reactor further comprises one or more additional reaction zones selected from dilute phase transport beds, dense phase fluidized beds, and fast fluidized beds upstream and/or downstream of the fully dense phase reaction zone.
27. The reactor of any one of claims 1-3, wherein the reactor does not include additional reaction zones upstream and downstream of the fully dense phase reaction zone.
28. A catalytic conversion reaction system comprises a catalytic conversion reactor, an oil agent separation device, an optional reaction product separation device and a regenerator,
the catalytic conversion reactor is provided with a catalyst inlet at the bottom, a raw material feed inlet at the lower part and an oil agent outlet at the top, the oil agent separation equipment is provided with an oil agent inlet, a catalyst outlet and a reaction product outlet, the optional reaction product separation equipment is provided with a reaction product inlet, a dry gas outlet, a liquefied gas outlet, a pyrolysis naphtha outlet, a pyrolysis light oil outlet and a pyrolysis heavy oil outlet, the regenerator is provided with a catalyst inlet and a catalyst outlet,
a catalyst inlet of the catalytic conversion reactor is in fluid communication with a catalyst outlet of the regenerator, a finish oil outlet of the catalytic conversion reactor is in fluid communication with a finish oil inlet of the finish oil separation device, a reaction product outlet of the finish oil separation device is in fluid communication with a reaction product inlet of the optional reaction product separation device, a catalyst outlet of the finish oil separation device is in fluid communication with a catalyst inlet of the regenerator,
wherein the catalytic conversion reactor comprises one or more reactors according to any one of claims 1-27.
29. The reaction system of claim 28, wherein the catalytic conversion reactor further comprises one or more reactors selected from the group consisting of dilute phase transport beds, dense phase fluidized beds, and fast fluidized beds in series and/or parallel with the reactor of any of claims 1-27.
30. The reaction system of claim 28, wherein the catalytic conversion reactor is comprised of one or more reactors of any one of claims 1-27.
31. The reaction system of any one of claims 28-30, wherein the oil separation device comprises a settler arranged coaxially or in high-low juxtaposition with the catalytic conversion reactor.
32. A catalytic conversion process comprising the step of contact reacting a reactant feedstock with a catalyst in a catalytic conversion reactor according to any one of claims 1-27 or in a catalytic conversion reaction system according to any one of claims 28-31.
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