Gas-solid combined fluidized bed reactor and its applications

Abstract

A gas-solid combined fluidized bed reactor is disclosed, which comprises an upflow-bed reaction zone and an upflow-bed reaction zone connected in series from bottom to top, the upper part of the upflow-bed reaction zone being connected to the lower part of the upflow-bed reaction zone; the lower part of the upflow-bed reaction zone being provided with a first feed inlet, a first catalyst outlet, and an optional first pumping medium inlet, the upper part of the upflow-bed reaction zone being provided with a first catalyst inlet and a first catalyst distributor connected to the first catalyst inlet; the upper outlet of the upflow-bed reaction zone and / or the lower inlet of the upflow-bed reaction zone are optionally provided with a first catalyst separator, the lower part of the upflow-bed reaction zone being provided with a second catalyst inlet, an optional second feed inlet, and an optional second pumping medium inlet; and the upper part of the upflow-bed reaction zone being provided with a material outlet. The catalyst separation reactor can conveniently realize different catalytic reactions to be carried out in sequence, and can realize independent and flexible adjustment of the reaction conditions in the two reaction zones, thereby improving the conversion rate of the reaction raw materials and the yield of the target product.

Description

Detailed Description of the Invention

[0001] [Technical Field] The present disclosure relates to the technical field of fluidized bed reactors, and in particular to gas-solid composite fluidized bed reactors and their applications.

[0002] [Background technology] Petrochemical manufacturing processes often use single or multiple feedstocks to produce desired products through multiple reactions, such as dehydrogenation and cracking of alkanes, hydrogenation and cracking of inferior feedstocks, isomerization and hydrogen transfer reactions to convert linear olefins in gasoline to multi-branched alkanes to improve gasoline properties, and primary cracking reactions to convert heavy feedstocks or crude oils to lower olefin precursors and then secondary cracking reactions to convert them to lower olefins.

[0003] For example, CN104560149A discloses a catalytic conversion method for producing butenes, which includes a total of four reactors. In addition to the reactor configuration of two risers and a fluidized bed, a fluidized bed reactor for cracking the gasoline fraction is installed outside the settler, and the reaction product enters the riser reactor to continue the cracking reaction. After the reaction, the catalyst is carbonized and regenerated, and then returned to the reactor for recycling. This method uses a mixture containing Y zeolite and β zeolite as a catalyst, and can achieve high yields of propylene and butenes.

[0004] However, there remains a need for a fluidized bed reactor that can efficiently perform two or more different catalytic reactions.

[0005] Summary of the Invention The objective of the present disclosure is to provide a gas-solid combined fluidized-bed reactor and its application, wherein the fluidized-bed reactor can efficiently carry out at least two different catalytic reactions on a reaction feedstock in succession (e.g., dehydrogenation of an alkane and cracking of the dehydrogenated product), thereby improving the conversion ratio of the reaction feedstock and the yield of the target product.

[0006] To achieve the above-mentioned object, in one aspect, the present disclosure provides a gas-solid combined fluidized bed reactor, the gas-solid combined fluidized bed reactor comprising: a reverse-flow bed reaction zone and an up-flow bed reaction zone connected in series from bottom to top, with the upper part of the reverse-flow bed reaction zone connected to the lower part of the up-flow bed reaction zone; a first feed inlet, a first catalyst outlet, and an optional first lifting medium inlet located at a lower portion of the upflow bed reaction zone; a first catalyst inlet disposed at an upper portion of the upflow bed reaction zone and a first catalyst distributor connected to the first catalyst inlet; a first catalyst separator optionally located at the upper outlet of the upflow-bed reaction zone and / or the lower inlet of the upflow-bed reaction zone; a second catalyst inlet, an optional second feed inlet, and an optional second pumping medium inlet located in the lower portion of the upflow bed reaction zone; and a material outlet located at the top of said upflow bed reaction zone;

[0007] In another aspect, a fluidized catalytic conversion system is provided, the fluidized catalytic conversion system comprising the gas-solid hybrid fluidized bed reactor of the present disclosure, a first catalyst stripper, a first catalyst regenerator, a second catalyst separator, a second catalyst stripper, and a second catalyst regenerator, or the first catalyst regenerator and the second catalyst regenerator are combined into a hybrid catalyst regenerator having a first catalyst regeneration zone and a second catalyst regeneration zone; The first catalyst outlet of the upflow bed reaction zone in the gas-solid combined fluidized bed reactor is connected to the spent catalyst inlet of the first catalyst regenerator or the first catalyst regeneration zone via the first catalyst stripper, and the regenerated catalyst outlet of the first catalyst regenerator or the first catalyst regeneration zone is connected to the first catalyst inlet of the upflow bed reaction zone; and The material outlet at the top of the upflow-bed reaction zone in the gas-solid combined fluidized-bed reactor is connected to the inlet of the second catalyst separator, the catalyst outlet of the second catalyst separator is connected to the spent catalyst inlet of the second catalyst regenerator or the second catalyst regeneration zone via the second catalyst stripper, and the regenerated catalyst outlet of the second catalyst regenerator or the second catalyst regeneration zone is connected to the second catalyst inlet of the upflow-bed reaction zone.

[0008] In the gas-solid combined fluidized bed reactor of the present disclosure, the upflow bed reaction zone and the upflow bed reaction zone are connected in series, and different catalytic reactions can be carried out in the upflow bed reaction zone and the upflow bed reaction zone. The catalysts in the two reaction zones move in opposite directions, which makes it possible to carry out different catalytic reactions in sequence and to independently and flexibly adjust the reaction conditions in the two reaction zones, thereby improving the conversion rate of the reaction raw materials and the yield of the target product.

[0009] In yet another aspect, there is provided a method for producing ethylene and propylene from C4 to C12 alkanes using the gas-solid combined fluidized bed reactor of the present disclosure, the method comprising the steps of: 1) introducing a first feedstock containing C4 to C12 lower alkanes into a lower part of the countercurrent bed reaction zone of the gas-solid combined fluidized bed reactor, and bringing the first feedstock into countercurrent contact with a dehydrogenation catalyst introduced from an upper part of the reaction zone to carry out a dehydrogenation reaction of the alkanes, and optionally separating the entrained catalyst from the resulting reaction stream through a first catalyst separator to obtain a first oil-gas product containing olefins; 2) The first oil-gas product, optionally together with the second feedstock containing C4 to C12 lower olefins introduced from the lower part of the upflow-bed reaction zone, is directly introduced into the lower part of the upflow-bed reaction zone of the gas-solid combined fluidized-bed reactor, and brought into co-current contact with a catalytic cracking catalyst introduced from the lower part of the reaction zone to carry out an olefin cracking reaction, thereby obtaining a reaction product stream containing ethylene and propylene.

[0010] The method of the present disclosure uses a composite fluidized-bed reactor equipped with a reverse-flow bed reaction zone and an upflow bed reaction zone connected in series. The alkane dehydrogenation reaction is primarily carried out in the reverse-flow bed reaction zone, while the olefin cracking reaction is primarily carried out in the upflow bed reaction zone. By using the reverse-flow bed reaction zone to carry out the alkane dehydrogenation reaction, the reaction between the alkane and the dehydrogenation catalyst can be strengthened and the alkane conversion can be improved. The reverse-flow bed reaction zone and the upflow bed reaction zone are connected to each other, allowing the alkane dehydrogenation reaction and the olefin cracking reaction to be carried out sequentially. The active species produced in the first stage of the dehydrogenation reaction can be sufficiently retained in the feed for the olefin cracking reaction, thereby facilitating the olefin cracking reaction and suppressing the occurrence of side reactions. At the same time, the reaction conditions for the alkane dehydrogenation reaction and the olefin cracking reaction can be independently and flexibly adjusted, thereby improving the conversion of the alkane feedstock and the yields of the target products, ethylene and propylene.

[0011] Other features and advantages of the present disclosure are detailed in the specific embodiments section below.

[0012] BRIEF DESCRIPTION OF THE DRAWINGS The accompanying drawings are included to provide a further understanding of the present disclosure and constitute a part of this specification. The accompanying drawings, together with the following specific embodiments, are used to explain the present disclosure but are not intended to limit the configuration of the present disclosure. In the accompanying drawings: FIG. 1 is a schematic structural diagram of a preferred embodiment of the present disclosure; FIG. 2 is a schematic structural diagram of another preferred embodiment of the present disclosure; FIG. 3 is a schematic structural diagram of yet another preferred embodiment of the present disclosure; FIG. 4 is a schematic structural diagram of yet another preferred embodiment of the present disclosure; FIG. 5 is a schematic structural diagram of a preferred embodiment of the first catalyst distributor of the present disclosure.

[0013] [Explanation of Reference Numbers] 1-Upflow bed reaction zone 2-1st catalyst stripper 3-Upflow bed reaction zone 4-Settler 5-Stripping section (second catalyst stripper) 6-1st catalyst regeneration zone 7-Second catalyst regeneration zone 11-First raw material 12,15 - First spent catalyst supply pipe 13,21-Stripping Gas 14,22-Stripping baffle 16-First stripping product 17-1st catalyst distributor 18-1st catalyst separator 19-Second raw material 20-Product supply pipe 23-Second spent catalyst supply pipe 24-Cyclone separator (second catalyst separator) 25-Gas collection chamber 26-Second Oil and Gas Products 27-Main Air 28-Fuel Gas 29-First regenerated catalyst supply pipe 30-Second regenerated catalyst supply pipe 31-Regenerator partition plate 32,33-Cyclone separator 34-Gas collection chamber 35-Regenerated exhaust gas Detailed Description Specific embodiments of the present disclosure are described in detail below. It should be understood that the specific embodiments described herein are used only to illustrate and explain the present disclosure, and are not intended to limit the scope of the present disclosure.

[0014] Any specific numerical value disclosed herein (including the endpoints of a numerical range) is not limited to the exact value of the numerical value, but should be understood to encompass values ​​close to the exact value (such as all possible values ​​within ±5% of the exact value). Furthermore, for any disclosed numerical range, the endpoints of the range, the endpoints and the specific points within the range, and the specific points can be combined in any way to create one or more new numerical ranges, and these new numerical ranges should also be considered to be specifically disclosed herein.

[0015] Unless otherwise specified, terms used herein have the same meaning as commonly understood by those skilled in the art. If a term is defined herein and that definition differs from the meaning commonly understood by those skilled in the art, the definition herein shall prevail.

[0016] In this disclosure, the term "counter-flow bed reaction zone" refers to a fluidized bed reaction zone in which the reactants move from bottom to top and the catalyst moves from top to bottom, with the two contacting in a counter-current manner.

[0017] In this disclosure, the term "upflow-bed reaction zone" refers to a fluidized-bed reaction zone in which both the reactants and the catalyst move from bottom to top, contacting the two in a co-current manner.

[0018] In this disclosure, except for the explicitly stated contents, any unmentioned matters or items are directly applied to those known in the art without any changes. Furthermore, any embodiment described herein can be freely combined with one or more other embodiments described herein, and the technical solutions or technical ideas formed thereby shall be considered to be part of the original disclosure or original record of this disclosure, and shall not be considered to be new contents not disclosed or anticipated in this specification, unless a person skilled in the art considers the combination to be obviously unreasonable.

[0019] All patent and non-patent literature (including, but not limited to, textbooks and journal articles, and the like) referred to herein is hereby incorporated by reference in its entirety.

[0020] As mentioned above, in a first aspect, the present disclosure provides a gas-solid combined fluidized bed reactor, the gas-solid combined fluidized bed reactor comprising: an upflow-bed reaction zone and an upflow-bed reaction zone connected in series from bottom to top, the upper part of the upflow-bed reaction zone being connected to the lower part of the upflow-bed reaction zone; a first feed inlet, a first catalyst outlet, and an optional first pumping medium inlet located at a lower portion of the upflow bed reaction zone; a first catalyst inlet disposed at an upper portion of the upflow bed reaction zone and a first catalyst distributor connected to the first catalyst inlet; a first catalyst separator, optionally and preferably provided at the upper outlet of the upflow-bed reaction zone and / or the lower inlet of the upflow-bed reaction zone; a second catalyst inlet, an optional second feed inlet, and an optional second pumping medium inlet located in the lower portion of the upflow bed reaction zone; and a material outlet located at the top of said upflow bed reaction zone;

[0021] According to the present disclosure, in the gas-solid combined fluidized-bed reactor, the reaction feedstock is first countercurrently contacted with the first catalyst in the upflow-bed reaction zone to carry out a first catalytic conversion reaction. The resulting reaction stream is then fed upward into the upflow-bed reaction zone and contacted with the second catalyst in a cocurrent manner to carry out a second catalytic conversion reaction to obtain a target product. This allows the first and second catalytic conversion reactions to be carried out sequentially. Preferably, a first catalyst separator is disposed at the upper outlet of the upflow-bed reaction zone and / or the lower inlet of the upflow-bed reaction zone to separate the entrained catalyst from the reaction stream ascending from the upflow-bed reaction zone, so that the reaction stream flowing into the upflow-bed reaction zone is substantially free of the first catalyst. This prevents adverse effects on the second catalytic conversion reaction in the upflow-bed reaction zone.

[0022] In the gas-solid combined fluidized-bed reactor of the present disclosure, since the lower reaction zone is in the form of an upflow bed and the first catalyst moves from top to bottom within the upflow-bed reaction zone, the reaction flow rising from the upflow-bed reaction zone usually entrains only a small amount of the first catalyst. The first catalyst can be conveniently separated and returned to the upflow-bed reaction zone by a first separator disposed at the upper outlet of the upflow-bed reaction zone and / or the lower inlet of the upflow-bed reaction zone without easily causing clogging of the separator. According to the present disclosure, various separation devices suitable for separating solid particles from a mixed fluid containing solid particles can be used as the first catalyst separator. In a preferred embodiment, the first catalyst separator is in the form of one or more combinations selected from a filter, a filter plate, a porous partition plate, and a quick separator, wherein the porous partition plate includes various plates or perforated plates having a filtering function made of a porous material, and the quick separator includes, but is not limited to, separators of different structures (e.g., a cyclone-type quick separator, a three-leaf-type quick separator, a catapult-type quick separator, a U-tube-type separator, a wall-cutting-type quick separator, and the like), and preferably, the first catalyst separator is a filter plate. More preferably, the pore size of the filter plate is 5 to 40 μm, preferably 10 to 30 μm.

[0023] In a preferred embodiment, the upflow-bed reaction zone and the countercurrent-bed reaction zone are arranged coaxially one above the other, and the upper part of the countercurrent-bed reaction zone is directly connected to the lower part of the upflow-bed reaction zone. In such a preferred embodiment, the reaction stream in the countercurrent-bed reaction zone is optionally and preferably separated from entrained catalyst by the first catalyst separator and then directly introduced into the lower part of the upflow-bed reaction zone for the second catalytic conversion reaction, thereby more fully retaining the active species in the reaction stream from the countercurrent-bed reaction zone and facilitating the second catalytic conversion reaction.

[0024] According to the present disclosure, the first catalyst distributor is used to introduce the first catalyst into the counterflow bed reaction zone, and preferably has the structure of an open-hole disc, and the aperture ratio of the open-hole disc is 50% to 90%, preferably 60% to 80%.

[0025] In a preferred embodiment, the upflow bed reaction zone is in the form of a constant diameter reaction zone or a variable diameter reaction zone, and the ratio of the diameter to the height of the upflow bed reaction zone is 1:1 to 5, preferably 1:1.5 to 3, wherein when the upflow bed reaction zone is in the form of a variable diameter reaction zone, the term "diameter" refers to the arithmetic mean value of the maximum and minimum diameters of the variable diameter reaction zone.

[0026] In a preferred embodiment, the upflow bed reaction zone is in the form of a combination of one or more selected from a bubbling bed, a turbulent bed, a quick bed and a conveying bed, and is preferably in the form of a riser reactor.

[0027] In a preferred embodiment, the first feed inlet and the first pumping medium inlet are provided in the lower part of the upflow bed reaction zone, and the second feed inlet and the second pumping medium inlet are provided in the lower part of the upflow bed reaction zone.

[0028] In a second aspect, there is provided a fluid catalytic conversion system of the present disclosure, the fluid catalytic conversion system comprising the gas-solid hybrid fluidized bed reactor of the present disclosure, a first catalyst stripper, a first catalyst regenerator, a second catalyst separator, a second catalyst stripper, and a second catalyst regenerator, or the first catalyst regenerator and the second catalyst regenerator are combined into a hybrid catalyst regenerator having a first catalyst regeneration zone and a second catalyst regeneration zone; The first catalyst outlet of the upflow bed reaction zone in the gas-solid combined fluidized bed reactor is connected to the spent catalyst inlet of the first catalyst regenerator or the first catalyst regeneration zone via the first catalyst stripper, and the regenerated catalyst outlet of the first catalyst regenerator or the first catalyst regeneration zone is connected to the first catalyst inlet of the upflow bed reaction zone; and The fluidized catalytic conversion system is such that the material outlet at the top of the upflow-bed reaction zone in the gas-solid combined fluidized bed reactor is connected to the inlet of the second catalyst separator, the catalyst outlet of the second catalyst separator is connected to the spent catalyst inlet of the second catalyst regenerator or the second catalyst regeneration zone via the second catalyst stripper, and the regenerated catalyst outlet of the second catalyst regenerator or the second catalyst regeneration zone is connected to the second catalyst inlet of the upflow-bed reaction zone.

[0029] In a preferred embodiment, the second catalyst separator is in the form of a combination of one or more selected from a cyclone type rapid separator, a three-lobe type rapid separator, a projection type rapid separator, a U-tube type separator and a wall-cutting type rapid separator, and is preferably a cyclone type rapid separator.

[0030] In certain preferred embodiments, the fluidized catalytic conversion system includes a settler, wherein the second catalyst separator is a cyclone separator located above the settler, and the second catalyst stripper is a stripping section located below the settler.

[0031] In a preferred embodiment, in order to effectively utilize the heat produced during the regeneration of the first and second catalysts, the first catalyst regenerator and the second catalyst regenerator are combined into a composite catalyst regenerator having a first catalyst regeneration zone and a second catalyst regeneration zone.

[0032] In certain further preferred embodiments, the first catalyst regeneration zone and the second catalyst regeneration zone are arranged horizontally side by side to facilitate heat transfer between them, and each of the first catalyst regeneration zone and the second catalyst regeneration zone has a main air inlet. In certain further preferred embodiments, the first catalyst regeneration zone and the second catalyst regeneration zone are separated by a vertically arranged regenerator partition plate, and the upper portions of the first catalyst regeneration zone and the second catalyst regeneration zone are connected. Gas-solid separators (e.g., cyclone separators) are also arranged therein, and the upper ends of the regenerator partition plates are higher than the solid outlets of the gas-solid separators.

[0033] In some further preferred embodiments, to facilitate transport of regeneration exhaust gas between the first catalyst regeneration zone and the second catalyst regeneration zone, the first catalyst regeneration zone and the second catalyst regeneration zone are arranged vertically in series, the first catalyst regeneration zone has a main air inlet, and the first regeneration exhaust gas outlet of the first catalyst regeneration zone is connected to the bottom of the second catalyst regeneration zone. In some further preferred embodiments, the first catalyst regeneration zone and the second catalyst regeneration zone are separated by a horizontally arranged regenerator partition plate, the first regeneration exhaust gas outlet is disposed on the regenerator partition plate, and a gas-solid separator (e.g., a cyclone separator) is disposed in the second catalyst regeneration zone.

[0034] In a preferred embodiment, the second catalyst regeneration zone is further provided with a fuel inlet for injecting a supplemental fuel to increase the regeneration temperature in the second catalyst regeneration zone. If necessary, the first catalyst regeneration zone may also be provided with a fuel inlet.

[0035] 1-4 are schematic structural diagrams of certain preferred embodiments of the gas-solid combined fluidized bed reactor and fluidized catalytic conversion system of the present disclosure: In the gas-solid composite fluidized bed reactor and the fluidized catalytic conversion system shown in FIG. 1, the upflow bed reaction zone is in the form of a constant diameter reaction zone and the upflow bed reaction zone is in the form of a conveying bed (e.g., a riser reactor), and the first catalyst regeneration zone and the second catalyst regeneration zone of the composite catalyst regenerator are arranged horizontally side-by-side; The gas-solid combined fluidized bed reactor and the fluidized catalytic conversion system shown in FIG. 2 are essentially the same as those shown in FIG. 1, except that the first catalyst separator is not provided at the upper outlet of the upflow bed reaction zone and the lower inlet of the upflow bed reaction zone; In the gas-solid composite fluidized bed reactor and the fluidized catalytic conversion system shown in FIG. 3, the upflow bed reaction zone is in the form of a constant diameter reaction zone and the upflow bed reaction zone is in the form of a high velocity bed, and the first catalyst regeneration zone and the second catalyst regeneration zone of the composite catalyst regenerator are arranged vertically in series; In the gas-solid hybrid fluidized bed reactor and the fluidized catalytic conversion system shown in FIG. 4, the upflow bed reaction zone is in the form of a variable diameter reaction zone and the upflow bed reaction zone is in the form of a conveying bed (e.g., a riser reactor), and the first catalyst regeneration zone and the second catalyst regeneration zone of the hybrid catalyst regenerator are arranged horizontally side-by-side.

[0036] 1 to 4, in a preferred embodiment of the present disclosure, the first feedstock 11 enters the lower part of the upflow-bed reaction zone 1 through a first feed pipeline, contacts with the first catalyst from the first catalyst regeneration zone 6, and is introduced into the upper part of the upflow-bed reaction zone 1 through the first catalyst distributor 17 to carry out the first catalytic conversion reaction. The resulting reaction stream enters the lower part of the upflow-bed reaction zone 3 through the upper outlet of the upflow-bed reaction zone 1; or, if a first catalyst separator 18 is provided, the resulting reaction stream is separated from the entrained catalyst by the separator and enters the lower part of the upflow-bed reaction zone 3. After the reaction, the first catalyst is withdrawn from the lower part of the upflow-bed reaction zone 1 and introduced into the first catalyst stripper 2 through the first spent catalyst supply pipe 12 for stripping. A small amount of reactants formed on the catalyst is removed to obtain the first spent catalyst. The first spent catalyst is introduced into the first catalyst regeneration zone 6 through the first spent catalyst supply pipe 15 for regeneration, and the resulting first regenerated catalyst is returned to the upflow-bed reaction zone 1 through the first regenerated catalyst supply pipe 29 for recycling. After the reaction stream from the upflow-bed reaction zone 1 enters the upflow-bed reaction zone 3, the reaction stream contacts the second catalyst from the second catalyst regeneration zone 7 to carry out the second catalytic conversion reaction. Optionally, the second feedstock 19 can be introduced into the upflow-bed reaction zone 3 through the second supply pipe, and the second feedstock 19 can then carry out the second catalytic conversion reaction in the upflow-bed reaction zone 3 together with the reaction stream from the upflow-bed reaction zone 1. The reaction stream obtained in the upflow bed reaction zone 3 is introduced into the cyclone separator (i.e., the second catalyst separator) 24 in the settler 4 through the product supply pipe 20, and the separated catalyst is introduced into the stripping section (i.e., the second catalyst stripper) 5 for stripping, and a small amount of reactants formed on the catalyst is removed to obtain the second spent catalyst.This second spent catalyst is introduced into the second catalyst regeneration zone 7 through the second spent catalyst supply pipe 23 for regeneration, and the resulting second regenerated catalyst is returned to the counterflow bed reaction zone 3 through the first regenerated catalyst supply pipe 30 for recycling. The reaction products separated by the cyclone separator 24 are led out of the apparatus.

[0037] FIG. 5 shows a preferred embodiment of the first catalyst distributor of the present disclosure, which has a perforated disc structure with an opening ratio of 50% to 90%, preferably 60% to 80%.

[0038] In a third aspect, there is provided a method for producing ethylene and propylene from C4 to C12 alkanes using the gas-solid combined fluidized bed reactor of the present disclosure, the method comprising the steps of: 1) introducing a first feedstock containing C4 to C12 lower alkanes into a lower part of the countercurrent bed reaction zone of the gas-solid combined fluidized bed reactor, and countercurrently contacting the first feedstock with a dehydrogenation catalyst introduced from an upper part of the reaction zone to carry out a dehydrogenation reaction of the alkanes, and optionally and preferably separating the entrained catalyst from the resulting reaction stream by a first catalyst separator to obtain a first oil-gas product containing olefins; 2) The first oil-gas product, optionally together with the second feedstock containing C4 to C12 lower olefins introduced into the reaction zone from the bottom, is directly introduced into the lower part of the upflow bed reaction zone of the gas-solid combined fluidized bed reactor, and brought into co-current contact with a catalytic cracking catalyst introduced into the lower part of the reaction zone to carry out an olefin cracking reaction, thereby obtaining a reaction product stream containing ethylene and propylene.

[0039] In a preferred embodiment, the lower alkane is a C4 to C8 alkane; and the content of the lower alkane in the first feedstock is 90 to 100 wt %.

[0040] In a preferred embodiment, the lower olefin is a C4 to C8 olefin; and the content of the lower olefin in the second feedstock is 90 to 100% by weight.

[0041] In a preferred embodiment, the second feedstock is partially or entirely derived from the reaction product stream obtained in step 2. For example, the second feedstock may be a lower olefin component separated from the reaction product stream.

[0042] In a preferred embodiment, the dehydrogenation catalyst comprises a support and an active component, wherein the support is selected from alumina, silicon oxide, titanium oxide, or a combination thereof, and the active component is selected from K, Ce, Pt, Cr, Ga, Fe, Ni, V, W, Zn, Zr, Co, Mo, and oxides of these metals, or a combination thereof. Preferably, the content of the support is 20 to 98%, preferably 30 to 97%, and the content of the active component or its oxide is 2 to 80%, preferably 3 to 70%, based on the total weight of the dehydrogenation catalyst.

[0043] In a preferred embodiment, the catalytic cracking catalyst comprises an active component, clay, and a binder, wherein the active component is selected from an MFI molecular sieve or a modified MFI molecular sieve, the clay is selected from kaolin, montmorillonite, bentonite, or a combination thereof, and the binder is selected from silica sol, alumina sol, pseudoboehmite, or a combination thereof. Preferably, based on the total weight of the catalytic cracking catalyst, the content of the active component is 10 to 60%, preferably 20 to 50%, the content of the clay is 10 to 80%, preferably 20 to 70%, and the content of the binder is 10 to 30%, preferably 10 to 20%.

[0044] In a further preferred embodiment, the MFI-structured molecular sieve is a ZSM-5 molecular sieve or a modified ZSM-5 molecular sieve, such as one or more selected from ZRP zeolites, phosphorus-containing ZRP zeolites, rare earth-containing ZRP zeolites, phosphorus- and rare earth-containing ZRP zeolites, phosphorus- and alkaline earth metal-containing ZRP zeolites, and phosphorus- and transition metal-containing ZRP zeolites, preferably phosphorus- and rare earth-containing ZRP zeolites.

[0045] In a preferred embodiment, the reaction conditions in the upflow bed reaction zone include the following: a reaction temperature of 520 to 720°C, preferably 560 to 660°C, and a reaction time of 5 to 30 hours. -1 , preferably 10 to 20 hours -1 Weight hourly space velocity: 100-500 kg / m 3 , preferably 150 to 300 kg / m 3 and a reaction pressure of 0 to 0.4 MPa, preferably 0.05 to 0.3 MPa. In such a preferred embodiment, the reaction stream ascending from the upflow bed reaction zone typically entrains only a small amount of dehydrogenation catalyst, and does not have a significant adverse effect on the olefin cracking reaction in the upflow bed reaction zone. More preferably, the reaction stream ascending from the upflow bed reaction zone is separated from the entrained catalyst by the first catalyst separator before entering the upflow bed reaction zone, thereby substantially eliminating the effect of the entrained catalyst on the olefin cracking reaction.

[0046] In a preferred embodiment, the reaction conditions in the upflow bed reaction zone include: a reaction temperature of 520-700°C, preferably 560-620°C; a catalyst to oil ratio of 2-30, preferably 5-20; a reaction time of 1-15 seconds, preferably 2-10 seconds; and a reaction pressure of 0-0.4 MPa, preferably 0-0.2 MPa.

[0047] In a preferred embodiment, the method further comprises the steps of: removing the spent dehydrogenation catalyst from the lower part of the upflow bed reaction zone; and returning the spent dehydrogenation catalyst to the upper part of the upflow bed reaction zone after stripping and regenerating the spent dehydrogenation catalyst. Preferably, the regeneration conditions for the spent dehydrogenation catalyst comprise the following: a regeneration temperature of 640-700°C, preferably 660-680°C; a feed rate of 50-400 kg / m 3 , preferably 100 to 300 kg / m 3 and a main air residence time of 0.5 to 20 seconds, preferably 2 to 10 seconds.

[0048] In a preferred embodiment, the method further comprises the steps of: separating the spent catalytic cracking catalyst from the reaction product stream of step 2), and returning the spent catalytic cracking catalyst to the lower part of the upflow-bed reaction zone after stripping and regenerating the spent catalytic cracking catalyst. Preferably, the regeneration conditions for the spent catalytic cracking catalyst comprise the following: a regeneration temperature of 670-730°C, preferably 690-710°C, a feed rate of 30-350 kg / m 3 , preferably 80 to 250 kg / m 3 and a main air residence time of 0.5 to 15 seconds, preferably 2 to 10 seconds.

[0049] In a preferred embodiment, the method further comprises the step of introducing an auxiliary fuel into the process of regenerating the spent dehydrogenation catalyst and / or the spent catalytic cracking catalyst. The addition of the auxiliary fuel can be used to supplement heat when coke is insufficient, and the fuel can be selected from a mixture of one or more of refined methane, ethane, and propane, and the fuel can be obtained from an external system or from the catalytic conversion process of the present disclosure that produces ethylene and propylene from lower alkanes.

[0050] 1 to 4, in a preferred embodiment of the method of the present disclosure, the preheated first feedstock 11 containing C4 to C12 lower alkanes is sprayed through the first feed pipe via a nozzle into the lower part of the upflow-bed reaction zone 1, and then countercurrently contacted with the dehydrogenation catalyst from the first catalyst regeneration zone 6. The preheated first feedstock 11 is then introduced into the upper part of the upflow-bed reaction zone 1 through the first catalyst distributor 17 to carry out alkane dehydrogenation. The resulting reaction stream (also referred to as a first oil-catalyst mixture) is optionally and preferably separated from the entrained catalyst by the first catalyst separator 18 at the upper outlet of the upflow-bed reaction zone 1 to obtain a first oil-gas product containing olefins. The spent dehydrogenation catalyst is withdrawn from the lower part of the upflow-bed reaction zone 1 and introduced into the first catalyst stripper 2 through the first spent catalyst feed pipe 12 for stripping, and a small amount of reaction oil gas generated on the catalyst is removed. The spent dehydrogenation catalyst after stripping is introduced into the first catalyst regeneration zone 6 through the first spent catalyst supply pipe 15 for regeneration, and the obtained regenerated dehydrogenation catalyst is returned to the upflow-bed reaction zone 1 through the first regenerated catalyst supply pipe 29 for recycling. A first oil-gas product containing olefins enters the lower part of the upflow-bed reaction zone 3 and contacts with the catalytic cracking catalyst from the second catalyst regeneration zone 7 to carry out the olefin cracking reaction. Optionally, the second feedstock 19 containing C4 to C12 lower olefins can be introduced into the upflow-bed reaction zone 3 through the second supply pipe. In this case, the second feedstock 19 can carry out the olefin cracking reaction in the upflow-bed reaction zone 3 together with the first oil-gas product from the upflow-bed reaction zone 1. The reaction stream (also called the second oil-catalyst mixture) obtained in the upflow bed reaction zone 3 is introduced into the cyclone separator 24 in the settler 4 through the product supply pipe 20, and the separated spent catalytic cracking catalyst is introduced into the stripping section 5 for stripping, to remove a small amount of reaction oil gas produced on the catalyst.The spent catalytic cracking catalyst after stripping is introduced into the second catalyst regeneration zone 7 through the second spent catalyst supply pipe 23 for regeneration, and the obtained regenerated catalytic cracking catalyst is returned to the upflow-bed reaction zone 3 through the second catalyst supply pipe 30 for recycling. The reaction oil gas separated by the cyclone separator 24 is led out of the apparatus.

[0051] In certain preferred embodiments, the present disclosure provides the following technical solutions: 1. A combined upflow bed and upflow bed catalytic conversion system, the catalytic conversion system comprises a combined upflow bed reactor unit and an upflow bed reactor unit; the upflow bed reaction unit comprises an upflow bed reaction zone, a first catalyst distributor, a first reaction catalyst-oil separator, a first catalyst stripper, and a first regeneration zone; the first catalyst separator is located above the upflow bed reaction zone and has a first reacted oil-gas outlet; the first catalyst distributor is located below the first catalyst separator; a delivery connection for the first catalyst to be stripped between the upflow bed reaction zone and the first catalyst stripper; a feed line connection for the first catalyst to be regenerated between the first catalyst stripper and the first regeneration zone; a feed line connection for said first stripping product between said first catalytic stripper and said upflow bed reaction zone; a feed line connection for the first regenerated catalyst between the first regeneration zone and the counterflow bed reaction zone; the upflow-bed reaction unit comprises an upflow-bed reaction zone, a settler, a second catalyst separator, a second catalyst stripper, and a second regeneration zone; a lower portion of the upflow-bed reaction zone connected to the first reaction oil-gas outlet; an upper end of the upflow-bed reaction zone is connected to the material inlet of the second catalyst separator disposed within the settler; a lower end of the settler connected to the second catalyst stripper; a supply line connection for the second catalyst to be regenerated between the second catalyst stripper and the second regeneration zone; and a feed line connection for the second regenerated catalyst is provided between the second regeneration zone and the upflow bed reaction zone; A catalytic conversion system comprising:

[0052] 2. The catalytic conversion system of claim 1, wherein, under said operating conditions, a first catalyst is fluidized in said upflow bed reaction zone and a second catalyst is fluidized in said upflow bed reaction zone.

[0053] 3. The catalytic conversion system according to item 1 or 2, wherein the upflow bed reaction zone is in the form of a combination of one or more selected from a constant diameter upflow bed reaction zone and a variable diameter upflow bed reaction zone, and the ratio of the diameter to the height of the upflow bed reaction zone is 1:1 to 5, preferably 1:1.5 to 3.

[0054] 4. The catalytic conversion system according to item 1, wherein the first catalyst separator is in the form of a combination of one or more selected from a filter, a filter plate, a porous partition plate, and a rapid separation device, and is preferably a filter plate; the pore size of the filter plate is 5 to 40 μm, preferably 10 to 30 μm.

[0055] 5. The catalytic conversion system according to item 1 or 4, wherein the first catalyst distributor has a perforated disc structure, and the aperture ratio of the perforated disc is 50% to 90%, preferably 60% to 80%.

[0056] 6. The catalytic conversion system according to item 1, wherein the upflow reaction zone is in the form of a combination of one or more selected from a bubbling bed, a turbulent bed, a high velocity bed and a conveying bed; and the second catalyst separator is in the form of a combination of one or more selected from a cyclone type rapid separator, a three-lobe type rapid separator, a projection type rapid separator, a U-tube type separator and a wall cutting type rapid separator, preferably a cyclone type rapid separator.

[0057] 7. A first feed oil inlet and a first pumping medium inlet are provided at the bottom of the countercurrent bed reaction zone; A second feed oil inlet and a second pumping medium inlet are provided at the bottom of the upflow-bed reaction zone. Item 1. The catalytic conversion system of item 1.

[0058] 8. The catalytic conversion system according to item 1, wherein the first catalyst regeneration zone and the second catalyst regeneration zone are arranged side-by-side in a horizontal direction.

[0059] 9. The catalytic conversion system described in item 1, wherein the first catalyst regeneration zone and the second catalyst regeneration zone are arranged in series vertically, and the first regeneration exhaust gas outlet of the first catalyst regeneration zone is connected to the bottom of the second catalyst regeneration zone.

[0060] 10. The catalytic conversion system according to item 1, wherein the second catalyst regeneration zone is also provided with a fuel inlet.

[0061] 11. A process for preparing ethylene and propylene from lower alkanes, characterized in that the process comprises the following steps: 1) in a counter-flow reaction zone, a first feedstock and a first catalyst are counter-flow contacted to carry out a first catalytic conversion reaction, and after the first catalytic conversion reaction, the material is separated by a first catalyst separator to obtain a first spent catalyst and a first oil-gas product; the first spent catalyst is led out of the counter-flow reaction zone; and the lower alkane is a C4-C12 alkane; 2) the first oil-gas product and the optional second feed enter a riser reaction zone and contact a second catalyst in the riser reaction zone to undergo a second catalytic conversion reaction to produce a second oil-gas product and a second spent catalyst; and the lower olefins are C4 to C12 olefins.

[0062] 12. The lower alkane is a C4 to C8 alkane; and the content of the lower alkane in the first raw material is 90 to 100 wt %; the lower olefin is a C4 to C8 olefin; and the content of the lower olefin in the second feedstock is 90 to 100 wt %; Preferably, some or all of the second feedstock is derived from the second oil-gas product; Item 12. The method according to item 11.

[0063] 13. The first catalyst comprises a first support and a first active component, wherein the first support is selected from one or more of alumina, silicon oxide, and titanium oxide, and the first active component is selected from one or more of K, Ce, Pt, Cr, Ga, Fe, Ni, V, W, Zn, Zr, Co, Mo, and oxides of these metals; The second catalyst comprises a second active component, a clay, and a binder, wherein the second active component is a molecular sieve with an MFI structure or a modified molecular sieve with an MFI structure, the clay is selected from one or more of kaolin, montmorillonite, and bentonite, and the binder is selected from one or more of silica sol, alumina sol, and pseudoboehmite. Item 12. The method according to item 11.

[0064] 14. The method according to item 11, wherein the conditions for the first catalytic conversion reaction include the following: a reaction temperature of 520 to 720°C, preferably 560 to 660°C, for 5 to 30 hours -1 , preferably 10 to 20 hours -1 Weight hourly space velocity: 100-500 kg / m 3 , preferably 150 to 300 kg / m 3and a reaction pressure of 0 to 0.4 MPa, preferably 0.05 to 0.3 MPa.

[0065] 15. The method according to item 11 or 14, wherein the conditions of the second catalytic conversion reaction include the following: a reaction temperature of 520 to 700°C, preferably 560 to 620°C; a catalyst to oil ratio of 2 to 30, preferably 5 to 20; a reaction time of 1 to 15 seconds, preferably 2 to 10 seconds; and a reaction pressure of 0 to 0.4 MPa, preferably 0 to 0.2 MPa.

[0066] 16. subjecting the first spent catalyst to a first stripping and a first regeneration to obtain a first regenerated catalyst, and returning the first regenerated catalyst to step 1) to participate in the first catalytic conversion reaction; subjecting the second spent catalyst to a second stripping and a second regeneration to obtain a second regenerated catalyst, and returning the second regenerated catalyst to step 2) to participate in the second catalytic conversion reaction; Item 12. The method of item 11, further comprising:

[0067] 17. The conditions of the first regeneration include the following: a regeneration temperature of 640 to 700°C, preferably 660 to 680°C; 3 , preferably 100 to 300 kg / m 3 Catalyst distribution density of 0.5 to 20 seconds, preferably 2 to 10 seconds, and the main air residence time of 0.5 to 20 seconds, preferably 2 to 10 seconds; The conditions for the second regeneration include the following: a regeneration temperature of 670 to 730°C, preferably 690 to 710°C; 3 , preferably 80 to 250 kg / m 3 Catalyst distribution density of 0.5 to 15 seconds, preferably 2 to 10 seconds, and the main air residence time of 0.5 to 15 seconds, preferably 2 to 10 seconds; Item 17. The method according to item 16.

[0068] 18. The method of claim 16 or 17, further comprising introducing a supplemental fuel into the first regeneration and / or the second regeneration.

[0069] 19. The first catalyst separator is disposed in the upper part of the countercurrent reaction zone, and a first catalyst distributor is disposed in the lower part of the first catalyst separator, the first reaction oil-gas is guided out of the countercurrent reaction zone through the first catalyst separator, and the first catalyst enters the countercurrent reaction zone through the first catalyst distributor; the first catalyst separator is in the form of a combination of one or more selected from a filter, a filter plate, a porous partition plate, and a rapid separation device, preferably a filter plate; The pore size of the filter plate is 5 to 40 μm, preferably 10 to 30 μm. Item 12. The method according to item 11.

[0070] 20. A catalytic conversion system for producing ethylene and propylene from lower alkanes, comprising: the catalytic conversion system comprising a combined countercurrent reaction unit and a riser reaction unit; the countercurrent reaction unit comprising a countercurrent reaction zone, a first catalyst distributor, an optional first catalyst separator, a first catalyst stripper, and a first regeneration zone; the first catalyst separator is positioned above the countercurrent reaction zone; the first catalyst distributor is disposed below the first catalyst separator; a feed line connection for the first catalyst to be stripped between the countercurrent reaction zone and the first catalyst stripper; a feed line connection for the first catalyst to be regenerated between the first catalyst stripper and the first regeneration zone; a feed line connection for the first stripping product between the first catalytic stripper and the countercurrent reaction zone; a feed line connection for the first regenerated catalyst between the first regeneration zone and the countercurrent reaction zone; the riser reaction unit comprising a riser reaction zone, a settler, a cyclone separator, a second catalyst stripper, and a second regeneration zone; a lower portion of the riser reaction zone connected to the reaction oil-gas outlet of the countercurrent reaction zone; an upper end of the riser reaction zone connected to the material inlet of the cyclone separator disposed within the settler; a lower end of the settler connected to the second catalyst stripper; a supply line connection for the second catalyst to be regenerated between the second catalyst stripper and the second regeneration zone; and a supply line connection for the second regenerated catalyst is provided between the second regeneration zone and the riser reaction zone; A catalytic conversion system comprising:

[0071] [Example] The present disclosure will be described in detail below with reference to examples, but the scope of the present disclosure is not limited thereby.

[0072] Unless otherwise specified, all reagents used in the following examples and comparative examples are commercially available products of chemical purity.

[0073] The lower alkane feedstocks used in the following examples and comparative examples were mixed butane and a mixture of C5 to C8 alkanes, and their respective compositions are shown in Tables 1 and 2. The lower olefin feedstocks were a mixture of n-butene and n-hexene, and a mixture of C5 to C8 olefins, and their compositions are shown in Table 3.

[0074] [Table 1]

[0075] [Table 2]

[0076] [Table 3]

[0077] The dehydrogenation catalyst used in the following examples and comparative examples is DH-1, and the catalytic cracking catalyst is RAG-6, both of which are manufactured by Sinopec Catalyst Co., Ltd. The chemical compositions and properties of the two catalysts are shown in Table 4.

[0078] [Table 4]

[0079] In the following examples and comparative examples: Ethylene yield (%) = ethylene flow rate in product / feedstock flow rate × 100%; Propylene yield (%) = propylene flow rate in product / feedstock flow rate × 100%; Here, when the second raw material is used, if the second raw material originates from this device, the calculation method is the same as above; if the second raw material originates from another device, the raw material flow rate is calculated according to the total amount of the second raw material and the first raw material.

[0080] Example 1 The test was conducted using the system shown in Figure 1. The diameter of the upflow-bed reaction zone was 300 mm and the height was 600 mm. The diameter of the upflow-bed reaction zone was 20 mm and the height was 1000 mm. The first catalyst used in the upflow-bed reaction zone was DH-1 catalyst, and the second catalyst used in the upflow-bed reaction zone was RAG-6 catalyst. The mixed butane was preheated to 150°C and introduced into the lower part of the upflow-bed reaction zone. There, the mixed butane countercurrently contacted and reacted with the first catalyst. The resulting first oil-catalyst mixture was separated by the first catalyst separator. After reaction, the first catalyst was withdrawn from the lower part of the upflow-bed reaction zone and introduced into the first catalyst stripper for stripping, and then into the first catalyst regeneration zone for regeneration. The regenerated first catalyst was returned to the upflow-bed reaction zone for recycling. The first reaction gas obtained after the catalyst was separated by the first catalyst separator entered the upflow reaction zone. There, the first reaction gas contacted the second catalyst and continued to react. The resulting second oil-catalyst mixture was introduced into the cyclone separator in the settler for separation. The resulting reaction gas was led out of the system from the top of the settler, and the resulting catalyst to be regenerated was introduced into the stripping section of the settler for stripping, and then into the second catalyst regeneration zone for regeneration. The regenerated second catalyst returned to the upflow reaction zone for recycling. The reaction conditions and results are shown in Table 5.

[0081] Example 2A The test was conducted according to the method of Example 1, except that n-butene from an external source was simultaneously introduced as a second feed into the upflow bed reaction zone and reacted therein. The mass ratio of n-butene to mixed butanes was 0.05:1. The reaction conditions and results are shown in Table 5.

[0082] Example 2B Testing was performed according to the method of Example 2A (see Figure 2), except that the first catalyst separator was not installed at the top outlet of the upflow-bed reaction zone and the bottom inlet of the upflow-bed reaction zone. The reaction conditions and results are shown in Table 5.

[0083] Comparative Example 1 The test was conducted in a single upflow reactor (riser reactor) with a diameter of 20 mm and a height of 1000 mm. The catalyst used was RAG-6 catalyst. The mixed butane was preheated to 150°C and introduced into the lower part of the upflow reactor. The mixed butane contacted the RAG-6 catalyst introduced from the lower part of the reactor, moved upward, and reacted. The resulting oil-catalyst mixture was introduced into the cyclone separator in the settler for separation. The resulting reacted oil-gas was led out of the system from the top of the settler. The resulting catalyst to be regenerated was introduced into the stripping section of the settler for stripping, and then entered the catalyst regenerator for regeneration. The regenerated catalyst was returned to the upflow reactor for recycling. The reaction conditions and results are shown in Table 5.

[0084] Comparative Example 2 The test was carried out in the same manner as in Example 1, except that the first catalyst used in the upflow bed reaction zone and the second catalyst used in the upflow bed reaction zone were both mixed catalysts obtained by mixing DH-1 catalyst and RAG-6 catalyst in a mass ratio of 1:1. The reaction conditions and results are shown in Table 5.

[0085] Comparative Example 3 The test was conducted in two independent upflow reactors (riser reactors), both with a diameter of 20 mm and a height of 1000 mm. The catalyst used in the first upflow reactor was DH-1 catalyst, and the catalyst used in the second upflow reactor was RAG-6 catalyst. The mixed butane was preheated to 150°C and introduced into the lower part of the first upflow reactor. There, the mixed butane contacted the DH-1 catalyst and moved upward to react. The resulting oil-catalyst mixture was introduced into the cyclone separator in the first settler for separation, and the resulting catalyst to be regenerated was introduced into the stripping section of the first settler for stripping and then into the first catalyst regenerator for regeneration. The regenerated DH-1 catalyst was returned to the first upflow reactor for recycling. The reaction oil-gas obtained from the top of the first settler was introduced into the second upflow reactor, where it contacted the RAG-6 catalyst and moved upward to react. The resulting oil-catalyst mixture was introduced into the cyclone separator in the second settler for separation, and the resulting catalyst to be regenerated was introduced into the stripping section of the second settler for stripping, and then into the second catalyst regenerator for regeneration. The regenerated RAG-6 catalyst was returned to the second upflow reactor for recycling. The reaction oil-gas obtained from the top of the second settler was led out of the system. The reaction conditions and results are shown in Table 5.

[0086] [Table 5]

[0087] Example 3 The test was conducted using the system shown in Figure 3. The diameter of the upflow-bed reaction zone was 300 mm and the height was 600 mm. The diameter of the upflow-bed reaction zone was 50 mm and the height was 1000 mm. The first catalyst used in the upflow-bed reaction zone was DH-1 catalyst, and the second catalyst used in the upflow-bed reaction zone was RAG-6 catalyst. C5-C8 alkanes were preheated to 150°C and introduced into the lower part of the upflow-bed reaction zone. There, the C5-C8 alkanes were countercurrently contacted with the first catalyst and reacted. The resulting first oil-catalyst mixture was separated by the first catalyst separator. After reaction, the first catalyst was withdrawn from the lower part of the upflow-bed reaction zone and introduced into the first catalyst stripper for stripping, and then into the first catalyst regeneration zone for regeneration. The regenerated first catalyst was returned to the upflow-bed reaction zone for recycling. The first reaction gas obtained after the catalyst was separated by the first catalyst separator entered the upflow reaction zone. There, the first reaction gas contacted the second catalyst and continued to react. The resulting second oil-catalyst mixture was introduced into the cyclone separator in the settler for separation. The resulting reaction gas was led out of the system from the top of the settler, and the resulting catalyst to be regenerated was introduced into the stripping section of the settler for stripping, and then into the second catalyst regeneration zone for regeneration. The regenerated second catalyst returned to the upflow reaction zone for recycling. The regeneration exhaust gas produced in the first catalyst regeneration zone was introduced into the second catalyst regeneration zone to provide heat for the second catalyst regeneration process. The reaction conditions and results are shown in Table 6.

[0088] Example 4 The test was conducted according to the method of Example 3, except that n-hexene from an external source was introduced as a second feedstock into the upflow bed reaction zone and reacted. The mass ratio of n-hexene to C5-C8 alkanes was 0.1:1. The reaction conditions and results are shown in Table 6.

[0089] Comparative Example 4 The test was carried out in a single upflow bed reactor with a diameter of 300 mm and a height of 600 mm. The catalyst used was RAG-6 catalyst. C5-C8 alkanes were preheated to 150°C and introduced into the bottom of the upflow bed reactor. The C5-C8 alkanes were countercurrently contacted with the RAG-6 catalyst introduced from the top of the reactor and reacted. The resulting oil-catalyst mixture was separated in a catalyst separator. The catalyst to be regenerated was withdrawn from the bottom of the reactor and introduced into a catalyst stripper for stripping, and then into a catalyst regenerator for regeneration. The regenerated catalyst was returned to the upflow bed reactor for recycling. After the catalyst was separated by the catalyst separator, the reacted oil-gas was led out of the system. The reaction conditions and results are shown in Table 6.

[0090] Comparative Example 5 The test was carried out in the same manner as in Example 3, except that the first catalyst used in the upflow bed reaction zone and the second catalyst used in the upflow bed reaction zone were both mixed catalysts obtained by mixing DH-1 catalyst and RAG-6 catalyst in a mass ratio of 1:1. The reaction conditions and results are shown in Table 6.

[0091] [Table 6]

[0092] Example 5 The test was conducted using the system shown in Figure 4, where the upflow bed reaction zone had an upper diameter of 500 mm, a lower diameter of 200 mm, and a height of 600 mm, and the upflow bed reaction zone had a diameter of 20 mm and a length of 1000 mm. The first catalyst used in the upflow bed reaction zone was DH-1 catalyst, and the second catalyst used in the upflow bed reaction zone was RAG-6 catalyst. C5-C8 alkanes were preheated to 150°C and introduced into the lower part of the upflow bed reaction zone. There, the C5-C8 alkanes were countercurrently contacted with the first catalyst and reacted. The resulting first oil-catalyst mixture was separated by the first catalyst separator. After the reaction, the first catalyst was withdrawn from the lower part of the upflow bed reaction zone and introduced into the first spent catalyst stripper for stripping, and then into the first catalyst regeneration zone for regeneration. The regenerated first catalyst was returned to the upflow bed reaction zone for recycling. The first reaction oil-gas obtained after the catalyst was separated by the first catalyst separator was introduced into the upflow bed reaction zone, where it contacted the second catalyst and continued to react. The resulting second oil-catalyst mixture was introduced into the cyclone separator in the settler for separation. The resulting reaction oil-gas was led out of the system from the top of the settler, and the resulting catalyst to be regenerated was introduced into the stripping section of the settler for stripping, and then into the second catalyst regeneration zone for regeneration. The regenerated second catalyst was returned to the upflow bed reaction zone for recycling. The reaction conditions and results are shown in Table 7.

[0093] Example 6 The test was carried out according to the method of Example 5, except that the preheated C5-C8 olefins from an external source were introduced as a second feedstock into the upward reaction zone and reacted. The mass ratio of C5-C8 olefins to C5-C8 alkanes was 0.1:1. The reaction conditions and results are shown in Table 7.

[0094] Comparative Example 6 The test was carried out according to the method of Example 5, except that the first catalyst used in the upflow bed reaction zone and the second catalyst used in the upflow bed reaction zone were both mixed catalysts obtained by mixing DH-1 catalyst and RAG-6 catalyst in a mass ratio of 1:1. The reaction conditions and results are shown in Table 7.

[0095] Comparative Example 7 Testing was carried out according to the method of Example 5, except that the first catalyst used in the upflow bed reaction zone and the second catalyst used in the upflow bed reaction zone were both RAG-6 catalysts. The reaction conditions and results are shown in Table 7.

[0096] [Table 7]

[0097] Tables 5, 6, and 7 show that by using the reactor, system, and method of the present disclosure to produce ethylene and propylene from C4 to C12 alkanes, the conversion of reactants and the yield of desired products can be significantly improved.

[0098] Although the preferred embodiments of the present disclosure have been described in detail above, the present disclosure is not limited to the specific contents in the above embodiments. Within the technical concept of the present disclosure, various simple modifications can be made to the technical solutions of the present disclosure, and all of these simple modifications fall within the protection scope of the present disclosure.

[0099] It should also be noted that the various specific technical features described in the above specific embodiments can be combined in any suitable manner without contradiction, and in order to avoid unnecessary repetition, the present disclosure will not further describe the various possible combinations.

[0100] It should be noted that the various embodiments of the present disclosure can be combined in any manner, and as long as they do not contradict the concept of the present disclosure, they should also be considered as being disclosed in the present disclosure. [Brief explanation of the drawings]

[0101] [Figure 1] FIG. 1 is a schematic structural diagram of a preferred embodiment of the present disclosure. [Figure 2] FIG. 2 is a schematic structural diagram of another preferred embodiment of the present disclosure. [Figure 3] FIG. 3 is a schematic structural diagram of yet another preferred embodiment of the present disclosure. [Figure 4] FIG. 4 is a schematic structural diagram of yet another preferred embodiment of the present disclosure. [Figure 5] FIG. 5 is a schematic structural diagram of a preferred embodiment of the first catalyst distributor of the present disclosure.

Claims

1. an upflow-bed reaction zone and an upflow-bed reaction zone connected in series from bottom to top, the upper part of the upflow-bed reaction zone being connected to the lower part of the upflow-bed reaction zone; a first feed inlet, a first catalyst outlet, and an optional first pumping medium inlet, all located at a lower portion of the upflow bed reaction zone; and a first catalyst inlet and a first catalyst distributor connected to the first catalyst inlet, all located at an upper portion of the upflow bed reaction zone; a first catalyst separator optionally located at an upper outlet of the upflow-bed reaction zone and / or a lower inlet of the upflow-bed reaction zone; a second catalyst inlet, an optional second feedstock inlet, and an optional second pumping medium inlet located in a lower portion of the upflow-bed reaction zone; a material outlet located at an upper portion of the upflow bed reaction zone; A gas-solid combined fluidized bed reactor comprising:

2. 2. The gas-solid combined fluidized bed reactor of claim 1, wherein the upflow-bed reaction zone and the countercurrent-bed reaction zone are vertically coaxially arranged, and the upper part of the countercurrent-bed reaction zone is directly connected to the lower part of the upflow-bed reaction zone.

3. The first catalyst separator is in the form of a combination of one or more selected from a filter, a filter plate, a porous partition plate, and a rapid separator, preferably a filter plate; More preferably, the filter plate has a pore size of 5 to 40 μm, preferably 10 to 30 μm.

4. The gas-solid combined fluidized bed reactor according to any one of claims 1 to 3, wherein the first catalyst distributor has a perforated disc structure, and the perforated disc has an opening ratio of 50 to 90%, preferably 60 to 80%.

5. 5. The gas-solid combined fluidized bed reactor according to claim 1, wherein the countercurrent bed reaction zone is in the form of a constant diameter reaction zone or a variable diameter reaction zone, and the ratio of the diameter to the height of the countercurrent bed reaction zone is 1:1-5, preferably 1:1.5-3.

6. The gas-solid combined fluidized bed reactor according to any one of claims 1 to 5, wherein the upflow bed reaction zone is in the form of a combination of one or more selected from a bubbling bed, a turbulent bed, a high velocity bed and a conveying bed, and is preferably a riser reactor.

7. A fluidized catalytic conversion system comprising the gas-solid combined fluidized bed reactor of any one of claims 1 to 6, a first catalyst stripper, a first catalyst regenerator, a second catalyst separator, a second catalyst stripper and a second catalyst regenerator, or the first catalyst regenerator and the second catalyst regenerator are combined into a combined catalyst regenerator having a first catalyst regeneration zone and a second catalyst regeneration zone; The first catalyst outlet of the upflow bed reaction zone in the gas-solid combined fluidized bed reactor is connected to the spent catalyst inlet of the first catalyst regenerator or the first catalyst regeneration zone via the first catalyst stripper, and the regenerated catalyst outlet of the first catalyst regenerator or the first catalyst regeneration zone is connected to the first catalyst inlet of the upflow bed reaction zone; and the material outlet at the top of the upflow-bed reaction zone in the gas-solid combined fluidized-bed reactor is connected to the inlet of the second catalyst separator, the catalyst outlet of the second catalyst separator is connected to the spent catalyst inlet of the second catalyst regenerator or the second catalyst regeneration zone via the second catalyst stripper, and the regenerated catalyst outlet of the second catalyst regenerator or the second catalyst regeneration zone is connected to the second catalyst inlet of the upflow-bed reaction zone; Fluidized catalytic conversion system.

8. 8. The fluidized catalytic conversion system according to claim 7, wherein the second catalyst separator is in the form of one or more combinations selected from a cyclone type rapid separator, a three-lobe type rapid separator, a projection type rapid separator, a U-tube type separator and a wall-cutting type rapid separator, and is preferably a cyclone type rapid separator.

9. The first catalyst regeneration zone and the second catalyst regeneration zone of the composite catalyst regenerator are arranged horizontally side by side, and the first catalyst regeneration zone and the second catalyst regeneration zone are each provided with a main air inlet; or The first catalyst regeneration zone and the second catalyst regeneration zone of the composite catalyst regenerator are arranged vertically in series, the first catalyst regeneration zone is provided with a main air inlet, the first regeneration exhaust gas outlet of the first catalyst regeneration zone is connected to the bottom of the second catalyst regeneration zone, and optionally, the second catalyst regeneration zone is also provided with a main air inlet; 9. A fluid catalytic conversion system according to claim 7 or 8, optionally provided with a fuel inlet in the first catalyst regeneration zone and / or the second catalyst regeneration zone.

10. A method for producing ethylene and propylene from C4 to C12 alkanes using the gas-solid combined fluidized bed reactor according to any one of claims 1 to 6, comprising the steps of: 1) introducing a first feedstock containing C4 to C12 lower alkanes into a lower part of the countercurrent bed reaction zone of the gas-solid combined fluidized bed reactor, and causing countercurrent contact with a dehydrogenation catalyst introduced from an upper part of the reaction zone to carry out a dehydrogenation reaction of the alkanes, and optionally separating the entrained catalyst from the resulting reaction stream through a first catalyst separator to obtain a first oil-gas product containing olefins; 2) directly introducing the first oil-gas product, optionally together with a second feedstock containing C4 to C12 lower olefins introduced into the reaction zone from the bottom, into the lower part of the upflow-bed reaction zone of the gas-solid combined fluidized-bed reactor, and bringing them into co-current contact with a catalytic cracking catalyst introduced into the lower part of the reaction zone to carry out an olefin cracking reaction, thereby obtaining a reaction product stream containing ethylene and propylene; A method comprising:

11. the lower alkane is a C4 to C8 alkane, and the content of the lower alkane in the first feedstock is 90 to 100 wt. %; and / or the lower olefins are C4 to C8 olefins, and the content of the lower olefins in the second feedstock is 90 to 100 wt%; Preferably, the second feedstock is derived in part or entirely from the reaction product stream obtained in step 2). The method of claim 10.

12. the dehydrogenation catalyst comprises a support selected from alumina, silicon oxide, titanium oxide, or a combination thereof, and an active component selected from K, Ce, Pt, Cr, Ga, Fe, Ni, V, W, Zn, Zr, Co, Mo, and oxides of these metals, or a combination thereof, and preferably, the content of the support is 20 to 98%, preferably 30 to 97%, and the content of the active component or its oxide is 2 to 80%, preferably 3 to 70%, based on the total weight of the dehydrogenation catalyst; and The catalytic cracking catalyst comprises an active component selected from MFI molecular sieves and modified MFI molecular sieves, a clay selected from kaolin, montmorillonite, bentonite or a combination thereof, and a binder selected from silica sol, alumina sol, pseudoboehmite or a combination thereof, and preferably, based on the total weight of the catalytic cracking catalyst, the content of the active component is 10 to 60%, preferably 20 to 50%, the content of the clay is 10 to 80%, preferably 20 to 70%, and the content of the binder is 10 to 30%, preferably 10 to 20%.

12. The method according to claim 10 or 11.

13. The reaction conditions in the upflow bed reaction zone include: a reaction temperature of 520 to 720°C, preferably 560 to 660°C, and a reaction time of 5 to 30 hours. －１ , preferably 10 to 20 hours －１ Weight hourly space velocity, 100 to 500 kg / m ３ , preferably 150 to 300 kg / m ３ a catalyst bed density of 0 to 0.4 MPa, preferably 0.05 to 0.3 MPa, and a reaction pressure of 0 to 0.4 MPa, preferably 0.05 to 0.3 MPa; and / or The reaction conditions in the upflow bed reaction zone include: a reaction temperature of 520-700°C, preferably 560-620°C; a catalyst to oil ratio of 2-30, preferably 5-20; a reaction time of 1-15 seconds, preferably 2-10 seconds; a reaction pressure of 0-0.4 MPa, preferably 0-0.2 MPa; The method according to any one of claims 10 to 12.

14. removing the spent dehydrogenation catalyst from a lower portion of the upflow bed reaction zone and returning the spent dehydrogenation catalyst to an upper portion of the upflow bed reaction zone after stripping and regenerating the spent dehydrogenation catalyst; Preferably, the regeneration conditions for the spent dehydrogenation catalyst include the following: a regeneration temperature of 640 to 700°C, preferably 660 to 680°C; a regeneration pressure of 50 to 400 kg / m ３ , preferably 100 to 300 kg / m ３ and a main air residence time of 0.5 to 20 seconds, preferably 2 to 10 seconds; and / or separating the spent catalytic cracking catalyst from the reaction product stream of step 2) and returning the spent catalytic cracking catalyst to the lower part of the upflow-bed reaction zone after stripping and regenerating the spent catalytic cracking catalyst; Preferably, the regeneration conditions of the spent catalytic cracking catalyst include the following: a regeneration temperature of 670 to 730°C, preferably 690 to 710°C; a regeneration rate of 30 to 350 kg / m ３ , preferably 80 to 250 kg / m ３ a catalyst distribution density of 0.5 to 15 seconds, preferably 2 to 10 seconds, main air residence time; The method of any one of claims 10 to 13, further comprising:

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