CN108212029B

CN108212029B - Catalytic conversion reaction method and reactor

Info

Publication number: CN108212029B
Application number: CN201710063754.5A
Authority: CN
Inventors: 石宝珍
Original assignee: Qingdao Jingrun Petrochemical Design & Research Institute Co ltd
Current assignee: Qingdao Jingrun Petrochemical Design & Research Institute Co ltd
Priority date: 2017-02-03
Filing date: 2017-02-03
Publication date: 2020-09-11
Anticipated expiration: 2037-02-03
Also published as: CN108212029A; WO2018141243A1

Abstract

The invention relates to the technical field of catalytic conversion processing of a methanol fluidized bed, in particular to a catalytic conversion reaction method and a reactor. The catalytic conversion reaction method is characterized in that the catalytic conversion reaction process of reaction raw materials is finished in a lower layer reactor (1) and an upper layer reactor (2) of a catalytic conversion reactor in parallel, and the reacted product gas of the lower layer reactor and the reacted product gas of the upper layer reactor respectively use independent cyclone separators arranged in a gas-solid separation zone (3) to separate catalysts and then flow out of the catalytic conversion reactor, or the catalysts are separated in a shared cyclone separator and then flow out of the catalytic conversion reactor. The invention adopts a mode of overlapping an upper layer and a lower layer in parallel, and can greatly improve the processing amount of the device on the premise of not increasing the diameter of the catalytic conversion reactor; when the gas-solid separation of the lower reactor and the upper reactor is independently arranged, the functions of two sets of catalytic conversion reactors can be completed, and the investment is saved.

Description

Catalytic conversion reaction method and reactor

Technical Field

The invention relates to the technical field of catalytic conversion processing of a methanol fluidized bed, in particular to a catalytic conversion reaction method and a reactor, which are particularly suitable for preparing olefin and aromatic hydrocarbon from methanol in a fluidized bed.

Background

The preparation of olefin or aromatic hydrocarbon by catalytic conversion of methanol is an important process technology in coal chemical industry and is highly regarded by various countries. Many of the reactions for preparing olefin or aromatic hydrocarbon from methanol adopt a gas-solid fluidized bed or circulating fluidized bed reaction method.

In the current technology for preparing hydrocarbon products by using fluidized bed methanol, such as DMTO, SMTO, FMTP and FMTA, the used catalyst is microspheric and has an average diameter of about 50-70 microns. The existing technical reaction process for preparing olefin or aromatic hydrocarbon from methanol uses two types of fluidized bed and circulating fluidized bed. The circulating fluidized bed uses the coke burning tank regeneration technology of FCC technology for reference. Because the methanol reaction produces coke far below FCC, the catalyst circulation between the reactor and the regenerator is very low, and the catalyst-to-alcohol ratio is only one twentieth to one thirtieth of the corresponding FCC catalyst-to-oil ratio. When the circulating fluidized bed is used, in order to ensure that the density, the inventory or the space velocity of the catalyst required by the reaction in the reactor is achieved, the catalyst can only be repeatedly circulated in the reactor, and the circulating amount is far greater than the original circulating amount between the reactor and the regenerator, so that the crushing of the catalyst and the energy consumption for operation are inevitably increased.

The existing fluidized bed reaction methanol catalytic conversion technology has the advantages that the flowing speed of gas and catalyst is low; the catalyst in the reaction process is only in a fluidized bed state, and the circulation of the catalyst does not occur in the reactor except a small amount of catalyst carried by dilute gas. The catalyst is broken down much less during the fluidized bed reaction than in the circulating fluidized bed. The reaction in the fluidized bed form is a preferable reaction state.

The methanol conversion reaction temperature is about 500 ℃, the reaction pressure is lower, and the diameter of the fluidized bed is larger along with the increase of the methanol processing amount. Such as 180 million tons/year methanol feed DMTO fluidized bed reactors up to 12 meters in diameter. Because the methanol conversion reaction only needs about 2 seconds of reaction time, the height of an ideal fluidized bed catalyst bed layer is only about 2 meters, and the height-diameter ratio of a catalyst fluidized bed area in the reactor is already low. In order to keep good catalyst fluidization and uniform reaction, the distribution requirements on methanol feeding and circulating catalyst are higher. The design of the reactor for methanol processing is difficult to further improve when a fluidized bed reactor is adopted due to the limitation of fluidization and reaction uniformity requirements. In practical application, the capacity of a single set of device is designed according to 180 ten thousand tons per year, and when a larger scale is needed, a plurality of sets of construction are adopted.

On the premise of not increasing the diameter of a reactor basically, not influencing the fluidization state of a catalyst and not changing reaction conditions, the technology for improving the methanol processing capacity is developed, so that the investment and the operation energy consumption of corresponding unit raw materials can be reduced obviously, and the method is significant.

Disclosure of Invention

The invention aims to provide a catalytic conversion reaction method capable of obviously improving the methanol treatment capacity, which adopts a mode of parallel upper and lower double-layer overlapping arrangement and can greatly improve the processing capacity of a device on the premise of not increasing the diameter of a catalytic conversion reactor; when the gas-solid separation of the lower reactor and the upper reactor is independently arranged, the functions of two sets of catalytic conversion reactors can be completed, and the investment is saved. The invention also provides a catalytic conversion reactor.

The invention adopts the following technical scheme:

a catalytic conversion reaction method, is used for the hydrocarbon products of catalytic conversion preparation of methanol, the reaction raw materials catalytic conversion reaction process is finished in lower reactor and upper reactor of the catalytic conversion reactor in parallel, the reaction raw materials enter the reaction zone of the bottom of lower reactor and upper reactor through the raw material distributor respectively, namely enter the lower reaction zone through the lower raw material distributor, enter the upper reaction zone through the upper raw material distributor, lower reactor reaction product gas and upper reactor reaction product gas after finishing the reaction enter the gas-solid separation zone above the catalytic conversion reactor, flow out the catalytic conversion reactor after separating out the catalyst;

corresponding reactor dilute phase spaces are arranged above the lower-layer reaction zone and the upper-layer reaction zone, and reaction product gas leaves the lower-layer reaction zone and the upper-layer reaction zone, enters the corresponding reactor dilute phase spaces and then enters the gas-solid separation zone; the gas-solid separation zone is provided with a gravity dilute phase settling zone and a cyclone separation zone;

the reaction product gas of the lower layer reactor is led out from a reaction material flow leading-out pipe isolated from the upper layer reactor, enters a gas-solid separation zone, and flows out from a product gas outlet of the reactor after the catalyst separation is finished in the gas-solid separation zone; the product gas of the upper layer reactor enters a gravity dilute phase settling zone of a gas-solid separation zone, the catalyst content or carrying capacity is reduced, and then the product gas enters a cyclone separation zone for catalyst separation, and then flows out from a product gas outlet of the reactor;

the reaction product gas of the lower layer reactor and the reaction product gas of the upper layer reactor are respectively separated by cyclone separators which are respectively independent in a gas-solid separation zone to separate the catalyst and then flow out of the catalytic conversion reactor; or the reaction product gas of the lower layer reactor and the reaction product gas of the upper layer reactor are firstly mixed in a gravity dilute phase settling zone of a gas-solid separation zone, and then enter a shared cyclone separator to separate the catalyst, and then flow out of the catalytic conversion reactor.

In the above catalytic conversion reaction method, the reaction raw material may be methanol, or may be a component of a non-target product in a catalytic conversion reaction product of other raw materials such as methanol, in the present invention, the target product of the catalytic conversion reaction of methanol is propylene and ethylene, and the component of the non-target product, i.e. a by-product of non-propylene and ethylene, such as C4, C5; in the method, other reaction raw materials, particularly components of non-target products in the methanol reaction product and the methanol raw materials can enter a lower layer reaction zone and an upper layer reaction zone together or independently for catalytic conversion again, so that the target products are increased; in particular, the methanol feedstock typically contains 5% water; the byproducts other than propylene and ethylene can be returned to the catalytic conversion reactor for secondary reaction;

in the catalytic conversion reaction process, the average apparent flow velocity of the gas in the catalytic conversion reaction of the methanol is lower than 1.2m/s (i.e. m/s), and preferably 0.6-1.1 m/s. In the present invention, the reaction zone is a reaction condition of a gas-solid fluidized state in which the gas flow rate is lower than the transition point of the turbulent fluidized bed to the circulating fluidized bed and the gas still exists in the form of bubbles; for the catalyst for the catalytic conversion reaction of methanol in the fluidized bed, the apparent flow velocity of gas in the reaction zone is lower than 1.2 m/s; the optimized average apparent flow velocity calculated according to the cross section of the fluidized bed is 0.6-1.1 m/s.

In the catalytic conversion reaction method, further, the regenerated catalyst from the regenerator enters the lower layer reaction zone and/or the upper layer reaction zone, the spent catalyst is led out from the lower layer reaction zone and/or the upper layer reaction zone and returns to the regenerator, and the catalyst inventory of the lower layer reactor and the upper layer reactor is controlled by the catalyst return pipe; the catalyst separated from the reaction product gas of the lower layer reactor and the reaction product gas of the upper layer reactor in the gas-solid separation zone is settled to the upper layer reaction zone by gravity, and the catalyst which is more than the catalyst required by the reaction flows back to the lower layer reaction zone.

In the catalytic conversion reaction method, reaction raw materials of the lower-layer reactor enter the lower-layer reaction zone from the lower-layer raw material distributor, product gas of the lower-layer reactor after reaction leaves a fluidized bed catalyst bed layer and upwards enters the dilute-phase space of the lower-layer reactor, and partial catalyst is settled in the lower-layer reaction zone due to gravity, so that the catalyst carried by the product gas of the lower-layer reactor is reduced; then the product gas of the lower layer reactor enters into the gravity dilute phase settling zone of the gas-solid separation zone from the reactant flow eduction tube to be mixed with the product gas of the upper layer reactor, or enters into the cyclone separator arranged at the outlet of the reactant flow eduction tube, and enters into the gravity dilute phase settling zone of the upper gas-solid separation zone from the gas outlet of the cyclone separator shell to be mixed with the product gas of the upper layer reactor; the product gas of the lower layer reactor further separates the catalyst in a gas-solid separation zone through a first-stage cyclone separator or a second-stage cyclone separator, and then flows out from a product gas outlet of the reactor; the catalyst separated by the cyclone separator settles to the upper reaction zone.

In the catalytic conversion reaction method, further, the product gas of the lower-layer reactor directly enters an independent first-stage cyclone separator or a two-stage cyclone separator after leaving the cyclone separator to complete gas-solid separation, and then flows out of the catalytic conversion reactor.

In the catalytic conversion reaction method, reaction raw materials of the upper-layer reactor directly enter the upper-layer reaction zone from the upper-layer raw material distributor, after the reaction is finished, product gas of the upper-layer reactor leaves a fluidized bed catalyst bed layer and upwards enters the dilute-phase space of the upper-layer reactor, part of the catalyst is settled in the upper-layer reaction zone due to gravity, the product gas of the upper-layer reactor enters the two-stage cyclone separator of the cyclone separation zone of the gas-solid separation zone above the upper-layer reactor, and the catalyst is further separated and flows out of the catalytic conversion reactor.

In the catalytic conversion reaction method, further, the reaction product gas of the lower layer reactor is led out by more than two reaction material flow leading-out pipes, or the outlets of the reaction material flow leading-out pipes are all provided with cyclone separators, and the reaction product gas of the lower layer reactor flowing out of the cyclone separators completes gas-solid separation in an independent first-stage cyclone separator or a two-stage cyclone separator; or the outlet part of the reactant flow outlet pipe is provided with a cyclone separator, the lower layer reactor reaction product gas flowing out of the cyclone separator completes gas-solid separation in an independent first-stage cyclone separator or a two-stage cyclone separator, and the rest of the lower layer reactor reaction product gas is mixed with the upper layer reactor reaction product gas in a gas-solid separation zone and then completes gas-solid separation in the two-stage cyclone separator.

When the method of the invention is implemented, a heat extraction pipe or a heat extractor can be arranged in the lower layer reactor and/or the lower layer reactor to control the reaction temperature.

The invention also provides a catalytic conversion reactor:

consists of a lower layer reactor, an upper layer reactor and a gas-solid separation zone;

the top of the lower layer reactor is provided with a reactant flow partition plate and a reactant flow eduction tube to separate the lower layer reactor from the upper layer reactor; the reactant flow partition plate is a flat plate or a conical plate; the reactant flow eduction tube is vertically arranged in the upper layer reactor; the bottom areas of the lower layer reactor and the upper layer reactor are respectively provided with a methanol raw material inlet;

the lower layer reactor comprises a lower layer reaction zone and a lower layer reactor dilute phase space above the lower layer reaction zone, the upper layer reactor comprises an upper layer reaction zone and an upper layer reactor dilute phase space above the upper layer reaction zone, and the gas-solid separation zone comprises a gravity dilute phase settling zone and a cyclone separation zone; the lower layer reactor and the upper layer reactor are respectively provided with an independent cyclone separator in a gas-solid separation zone or share a cyclone separator; the gas-solid separation zone shell is provided with a reactor product gas outlet; the reactor is characterized in that a tubular or plate-type lower-layer raw material distributor is arranged in the lower-layer reactor, and a tubular or plate-type upper-layer raw material distributor is arranged in the upper-layer reactor.

In the catalytic conversion reactor, the number of the reactant flow outlet pipes is one, and the reactant flow outlet pipes are arranged in the central area of the catalytic conversion reactor; or more than two reactant flow leading-out pipes are dispersedly arranged along the cross section of the catalytic conversion reactor.

In the above catalytic conversion reactor, further, the cross-sectional area of the reactant stream outlet pipe is constant or gradually decreases upward.

In the catalytic conversion reactor, part or all of the outlet of the reactant flow outlet pipe is provided with cyclone separators which rotate in the circumferential direction, and each cyclone separator consists of more than two cyclone pipes which are uniformly distributed in the circumferential direction and a cyclone separator shell; a cyclone separator shell is arranged outside the cyclone tube, and a cyclone separator shell gas outlet is arranged at the top of the cyclone separator shell; a catalyst outflow port is reserved between the lower edge of the cyclone separator shell and the upper layer reactor; an upper reaction zone is formed between the cyclone separator and the upper reactor shell.

In the catalytic conversion reactor, the gas-solid separation zone is provided with a first-stage cyclone separator or a second-stage cyclone separator which is directly connected with a gas outlet of the shell of the cyclone separator through a conveying pipe, so that the gas-solid separation of the product gas of the lower-layer reactor is completed.

In the catalytic conversion reactor, the lower reactor is provided with an independent first-stage cyclone separator or an independent second-stage cyclone separator, and the upper reactor is provided with an independent second-stage cyclone separator; the cyclone separators of the lower reactor and the cyclone separators of the upper reactor are arranged up and down in a staggered way or in parallel; when the lower-layer reactor and the upper-layer reactor are both provided with two stages of cyclone separators, the secondary cyclone separators and the primary cyclone separators of the two stages of cyclone separators are arranged in a vertically staggered manner; when the lower reactor is provided with a primary cyclone, the primary cyclone is arranged below.

In the above catalytic conversion reactor, further, more than two catalyst return pipes are arranged between the upper layer reaction zone and the lower layer reaction zone, and the catalyst in the upper layer reaction zone returns to the lower layer reaction zone through the catalyst return pipes, so as to maintain the catalyst inventory in the lower layer fluidized bed reaction and the upper layer fluidized bed reaction to be stable; when the catalyst return pipe adopts an overflow form, the inlet of the catalyst return pipe is arranged at the position of the upper edge of a catalyst bed layer required by the upper-layer reactor, and the catalyst higher than the position enters the inlet of the catalyst return pipe and flows back (also called overflow) into the lower-layer reactor, so that the height of the catalyst layer in the upper-layer reaction zone is naturally adjusted; or the inlet of the catalyst return pipe is arranged at the lower part of the position of the upper edge of the catalyst bed layer required by the upper-layer reactor, and the catalyst return pipe is provided with a valve which is used for controlling the catalyst return quantity.

In the above catalytic conversion reactor, further, the catalyst return pipe is disposed outside the catalytic conversion reactor housing or inside the catalytic conversion reactor housing.

In the catalytic conversion reactor, the gas-solid separation zone is provided with more than two groups of two-stage cyclone separators which are connected in parallel, and the lower-layer reactor and the upper-layer reactor share the two-stage cyclone separators; the outlet of the cyclone separator is connected with a common gas collection chamber and a reactor product gas outlet.

In the catalytic conversion reactor, when the lower-layer reactor and the upper-layer reactor are respectively provided with the independent cyclone separators in the gas-solid separation zone, the shell of the gas-solid separation zone is respectively provided with the reactor product gas outlets communicated with the independent cyclone separators, so that the reaction product gas of the lower-layer reactor and the reaction product gas of the upper-layer reactor are discharged from the outlets of the respective cyclone separators through the respective reactor product outlets.

In the above catalytic conversion reactor, a heat extraction pipe is disposed in the lower reactor and the upper reactor or a heat extractor outside the reactors is disposed to control the reaction temperature.

In the invention, the equipment such as the cyclone tube, the lower layer raw material distributor, the upper layer raw material distributor raw material, the cyclone separator and the like can be designed by related professional technicians. In the invention, the primary cyclone separator is equipment which is only provided with a primary inlet cyclone separator and a primary outlet cyclone separator to realize primary/secondary gas-solid separation, and is provided with an inlet and an outlet; the two-stage cyclone separator is equipment provided with a primary cyclone separator and a secondary cyclone separator and capable of realizing two-stage/two-stage series gas-solid separation, wherein the primary cyclone separator and the secondary cyclone separator are respectively provided with an inlet and an outlet, and the outlet of the primary cyclone separator is connected with the inlet of the secondary cyclone separator to form two-stage series gas-solid separation equipment.

Effects of the invention

The invention adopts a mode of overlapping an upper layer and a lower layer in parallel, and can greatly improve the processing amount of the device on the premise of not increasing the diameter of the catalytic conversion reactor; when the lower reactor and the upper reactor are independently arranged for gas-solid separation, the invention completes the functions of two sets of catalytic conversion reactors and saves the investment.

Drawings

FIG. 1: the catalytic conversion reactor device of one embodiment of the invention is schematically structured.

FIG. 2: a schematic view of a catalytic conversion reactor apparatus according to another embodiment of the present invention; FIG. 3: another embodiment of the present invention is a schematic structural view of a catalytic conversion reactor apparatus.

FIG. 4: another embodiment of the present invention is a schematic structural view of a catalytic conversion reactor apparatus.

FIG. 5: another embodiment of the present invention is a schematic structural view of a catalytic conversion reactor apparatus.

FIG. 6: another embodiment of the present invention is a schematic structural view of a catalytic conversion reactor apparatus.

FIG. 7: another embodiment of the present invention is a schematic structural view of a catalytic conversion reactor apparatus.

The numbering in the figures illustrates:

1A lower-layer reactor, 2 an upper-layer reactor, 3 a gas-solid separation zone, 110 a lower-layer reactor shell, 111A lower-layer raw material distributor, 112 a lower-layer reaction zone, 113 a lower-layer reactor dilute-phase space, 114A catalyst return pipe, 114B second catalyst return pipe, 115 reactant flow partition plate, 116 heat taking pipe, 120 cyclone separator, 121A second reactant flow outlet pipe and 121B reactant flow outlet pipe; 122 cyclone tube, 123 cyclone housing, 124 catalyst return tube inlet, 125 cyclone housing gas outlet, 126 transfer tube, 127 transfer tube and lower reactor primary cyclone inlet connecting tube, 131 lower reactor primary cyclone, 132 lower reactor primary cyclone inlet, 133 lower reactor primary cyclone outlet, 134 lower reactor primary cyclone catalyst outlet, 135 lower reactor primary cyclone outlet and secondary cyclone inlet connecting tube, 136 lower reactor product gas transfer tube, 141 lower reactor secondary cyclone, 142 lower reactor secondary cyclone inlet, 143 lower reactor secondary cyclone outlet, 144 lower reactor secondary cyclone catalyst outlet, 145 lower reactor secondary cyclone outlet and lower reactor product gas transfer tube connecting tube, 151 lower layer reactor first-level cyclone separator, 152 lower layer reactor first-level cyclone separator inlet, 153 lower layer reactor first-level cyclone separator outlet, 155 lower layer reactor first-level cyclone separator outlet and lower layer reactor product gas conveying pipe connecting pipe; the 157 conveying pipe is connected with an inlet connecting pipe of a first-stage cyclone separator of the lower-layer reactor;

210 upper reactor shell, 211 upper raw material distributor, 212 upper reaction zone and 213 upper reactor dilute phase space;

221 an upper reactor primary cyclone separator, 222 an upper reactor primary cyclone separator inlet, 223 an upper reactor primary cyclone separator outlet, 224 an upper reactor primary cyclone separator catalyst outflow pipe, 225 an upper reactor primary cyclone separator outlet and secondary cyclone separator inlet connecting pipe;

231 upper reactor secondary cyclone separator, 232 upper reactor secondary cyclone separator inlet, 233 upper reactor secondary cyclone separator outlet, 234 upper reactor secondary cyclone separator catalyst outflow pipe, 235 upper reactor secondary cyclone separator outlet and gas collecting chamber connecting pipe; 236 a second reactor product gas outlet;

310 gas-solid separation zone shell, 311 shares a primary cyclone separator, 312 shares a primary cyclone separator inlet, 313 shares a primary cyclone separator outlet, 314 shares a primary cyclone separator catalyst outflow pipe, 315 shares a primary cyclone separator outlet and secondary cyclone separator inlet connecting pipe, 315A first shares a primary cyclone separator outlet and secondary cyclone separator inlet connecting pipe, 315B second shares a primary cyclone separator outlet and secondary cyclone separator inlet connecting pipe; 316 gravity dilute phase settling zone, 321 shared secondary cyclone, 322 shared secondary cyclone inlet, 323 shared secondary cyclone outlet, 324 shared secondary cyclone catalyst outflow tube, 325 plenum chamber, 326 reactor product gas outlet;

h1 lower reaction zone height, H2 upper reaction zone height, H3 lower reactor dilute phase space height, H4 upper reactor dilute phase space height, D1 lower reactor diameter, D2 upper reactor diameter, D3 gas-solid separation zone diameter, D4 second reactant flow outlet pipe lower diameter, D5 second reactant flow outlet pipe upper diameter, D6 cyclone separator shell diameter, D7 cyclone separator shell gas outlet diameter, Y1 reaction feedstock, Y2 second reaction feedstock, P reaction product gas, GC regeneration catalyst, GC1 second regeneration catalyst, SC spent catalyst, SC1 second spent catalyst.

Detailed Description

The present invention will be further described with reference to the accompanying drawings and the detailed description.

The first embodiment is as follows:

fig. 1 is a schematic structural diagram of a catalytic conversion reactor according to an embodiment of the present invention, and the following description is made with reference to fig. 1, and illustrates an implementation process of the present invention by taking a methanol-to-olefin reaction as an example:

the catalytic conversion reactor of the present invention, as shown in fig. 1, is composed of a lower reactor 1, an upper reactor 2 and a gas-solid separation zone 3, and has a lower reactor diameter D1, an upper reactor diameter D2 and a gas-solid separation zone diameter D3, respectively;

a reactant flow partition plate 115 and a reactant flow eduction tube 121B are arranged at the top of the lower layer reactor 1 to separate the lower layer reactor 1 from the upper layer reactor 2; in particular embodiments, the reactant flow baffle 115 may be a flat plate or a tapered plate, in this embodiment, the reactant flow baffle 115 is a flat plate, i.e., horizontally disposed; the reactant flow eduction tubes are vertically arranged in the upper layer reactor 2, during specific implementation, one reactant flow eduction tube can be arranged in the central area of the catalytic conversion reactor, or more than two reactant flow eduction tubes can be arranged along the cross section of the catalytic conversion reactor in a dispersing way, the cross section area of the reactant flow eduction tubes is unchanged or gradually reduced upwards, in the embodiment, the reactant flow eduction tubes 121B are arranged in parallel, the cross section area is unchanged, namely, the diameter of the reactant flow eduction tubes is a pipeline with the diameter being unchanged from top to bottom, and the diameter D5 of the upper part is equal to the diameter D4 of; the bottom areas of the lower layer reactor 1 and the upper layer reactor 2 are respectively provided with a reaction raw material inlet, in the embodiment, a reaction raw material Y1 is introduced from the reaction raw material inlet at the bottom of the lower layer reactor 1, and a second reaction raw material Y2 is introduced from the reaction raw material inlet at the bottom of the upper layer reactor 2;

the lower layer reactor 1 comprises a lower layer reaction zone 112 and a lower layer reactor dilute phase space 113 above the lower layer reaction zone, the upper layer reactor 2 comprises an upper layer reaction zone 212 and an upper layer reactor dilute phase space 213 above the upper layer reaction zone, and the gas-solid separation zone 3 comprises a gravity dilute phase settling zone 316 and a cyclone separation zone;

the lower layer reactor 1 and the upper layer reactor 2 of the invention can be respectively provided with an independent cyclone separator in the gas-solid separation zone 3 or the lower layer reactor 1 and the upper layer reactor 2 share the cyclone separator which is arranged in the cyclone separation zone; the gas-solid separation zone shell 310 is provided with a reactor product gas outlet 326; in the embodiment, the gas-solid separation zone 3 is provided with more than two groups of two-stage cyclone separators which are connected in parallel, the lower-layer reactor 1 and the upper-layer reactor 2 share the two-stage cyclone separators, and the outlets of the cyclone separators are connected with a shared gas collection chamber 325 and a reactor product gas outlet 326; in practice, each set of two-stage cyclones includes a common primary cyclone 311 and a common secondary cyclone 321, the common primary cyclone 311 is provided with a common primary cyclone inlet 312, a common primary cyclone outlet 313 and a common primary cyclone catalyst outflow pipe 314, the common secondary cyclone 321 is provided with a common secondary cyclone inlet 322, a common secondary cyclone outlet 323 and a common secondary cyclone catalyst outflow pipe 324, and the common secondary cyclone 321 is connected to the primary cyclone 311 through a common primary cyclone outlet and secondary cyclone inlet connection pipe 315A, a second common primary cyclone outlet and secondary cyclone inlet connection pipe 315B, respectively; in this mode, the shared two-stage cyclone separator apparatus main body is installed in a vertically staggered manner, and the shared primary cyclone separator 311 is located below;

a tubular or plate-type lower layer raw material distributor 111 is arranged in the lower layer reactor 1, and a tubular or plate-type upper layer raw material distributor 211 is arranged in the upper layer reactor 2, in the embodiment, the lower layer raw material distributor 111 is arranged in a tubular manner, and the upper layer raw material distributor 211 is arranged in a plate manner;

two catalyst return pipes, namely a catalyst return pipe 114A and a second catalyst return pipe 114B, are arranged between the upper layer reaction zone 212 and the lower layer reaction zone 112, the catalyst return pipe 114A is arranged outside the shell of the catalytic conversion reactor, the second catalyst return pipe 114B is arranged in the shell of the catalytic conversion reactor and is provided with a catalyst return pipe inlet 124, and the catalyst in the upper layer reaction zone 212 returns to the lower layer reaction zone 112 to maintain the stable catalyst inventory in the lower layer fluidized bed reaction and the upper layer fluidized bed reaction; in the invention, the two catalyst return pipes have the same function, and the catalyst can only flow from top to bottom, part of the catalyst in the lower reactor is carried into the upper reactor by the product gas, and the carried amount is generally larger than the entering regeneration amount (because the methanol catalytic conversion coke formation is less, the catalyst circulation amount between the reactor and the regenerator is less, the catalyst return pipe is needed to return part of the catalyst, and the catalyst amount in the lower reactor is maintained); in specific implementation, the catalyst return pipe can be provided with a valve or not; when the valve is not arranged, the backflow is also called overflow, the backflow amount during the overflow depends on the position of the inlet of the backflow pipe, and the catalyst in the upper layer reactor higher than the inlet of the backflow pipe can return to the lower layer reactor, so that the amount of the catalyst in the upper layer reactor is naturally stable; when the valve is arranged, the position of the inlet of the catalyst return pipe can be lower, and the return amount is adjusted through the valve. The number of catalyst return lines is not essential and one is not problematic, simply because the reactor diameter is large and the catalyst is more uniform in the multiple return line reactor. In this embodiment, the catalyst return pipe 114A and the second catalyst return pipe 114B both adopt an overflow form, and the catalyst flow rate thereof is naturally adjusted by the height of the catalyst layer of the upper reaction zone 212 without using a valve for control;

in the present invention, heat extraction pipes may be disposed in the lower reactor and the upper reactor or a heat extractor outside the lower reactor, and in this embodiment, the heat extraction pipes 116 are disposed in the lower reactor to control the reaction temperature of the lower reaction zone 112.

The catalytic conversion reaction process shown in fig. 1 is as follows:

the reaction raw material catalytic conversion reaction process is completed in a lower layer reactor 1 and an upper layer reactor 2 of the catalytic conversion reactor in parallel, the reaction raw material respectively enters reaction zones at the bottom of the lower layer reactor 1 and the upper layer reactor 2 through a raw material distributor, namely enters a lower layer reaction zone 112 through a lower layer raw material distributor 111, enters an upper layer reaction zone 212 through an upper layer raw material distributor 211, the reaction product gas of the lower layer reactor and the reaction product gas of the upper layer reactor after the reaction are completed enter a gas-solid separation zone 3 above the catalytic conversion reactor, and the catalyst is separated out and flows out of the catalytic conversion reactor;

the regenerated catalyst GC from the regenerator meeting the requirement enters the lower reaction zone 112, the spent catalyst SC is led out from the upper reaction zone 212 and returns to the regenerator, and the catalyst amount of the lower reactor 1 and the upper reactor 2 is determined according to the space velocity required by the reaction or the height of the reaction catalyst layer or the retention time of gas in the catalyst layer under the corresponding normal operation condition;

the reaction raw material Y1 (such as methanol raw material) after heat exchange enters the lower layer reaction zone 112 from the lower layer raw material distributor 111, the second reaction raw material Y2 (such as methanol raw material) after heat exchange directly enters the upper layer reaction zone 212 from the upper layer raw material distributor 211, catalytic conversion reaction is carried out in the environment of catalyst, and the gas apparent flow velocity of the lower layer reaction zone 112 and the upper layer reaction zone 211 is lower than the conversion flow velocity of the turbulent fluidized bed to the fast fluidized bed or the circulating fluidized bed;

after the methanol raw material is reacted, the reaction product gas leaves the lower layer reaction zone 112 and the upper layer reaction zone 212, enters the dilute phase space of the corresponding reactor and then enters the gas-solid separation zone 3; the product gas of the lower reactor leaves the catalyst bed of the fluidized bed, and enters the dilute phase space 113 of the lower reactor upwards, and part of the catalyst is settled in the lower reaction zone 112 due to gravity, so that the catalyst carried by the product gas of the lower reactor is reduced; the reaction product gas of the lower layer reactor is led out from two reactant flow leading-out pipes 121B which are isolated from the upper layer reactor 2 and enters a gravity dilute phase settling zone 316 of the gas-solid separation zone 3; the product gas of the upper reactor after the reaction leaves the catalyst bed layer of the fluidized bed, and enters the dilute phase space 213 of the upper reactor upwards, and part of the catalyst is settled in the upper reaction zone 212 due to gravity; the reaction product gas of the lower layer reactor and the reaction product gas of the upper layer reactor are firstly mixed in a gravity dilute phase settling zone 316 of the gas-solid separation zone 3, then enter two-stage cyclone separators shared by the cyclone separation zones, further separate out the catalyst, flow out of the catalytic conversion reactor from a product gas outlet 326 of the reactor, the separated catalyst is settled in the upper layer reaction zone 212, and the catalyst which is more than the reaction requirement overflows to the lower layer reaction zone 112 from a catalyst return pipe;

during specific operation, firstly, a regenerated catalyst GC is loaded into the lower-layer reactor 1, so that the height of the catalyst reaches the height H1 of the lower-layer reaction zone, the height of the dilute-phase space reaches the height H3 of the dilute-phase space of the lower-layer reactor, and a methanol raw material after heat exchange, namely a reaction raw material Y1 uniformly enters the lower-layer reaction zone 112 from a reaction raw material inlet through the lower-layer raw material distributor 111, so that the catalyst in the lower-layer reaction zone is fluidized and reacts; the lower reaction zone 112 is operated under conventional turbulent fluidized bed conditions with gas flow rate controlled at a gas superficial velocity of less than 1.1 m/s; after the reaction is finished, the product gas of the lower layer reactor carries partial catalyst to enter two reactant flow eduction tubes 121B, and then directly enters a gravity dilute phase settling zone 316 of the gas-solid separation zone 3; the separated catalyst is settled to the upper reaction zone 212, when the accumulated catalyst reaches the requirement of the upper reaction zone 212, namely the height of the catalyst reaches the height H2 of the upper reaction zone, the methanol raw material, namely the reaction raw material Y2 enters the upper reactor 2 through the lower raw material distributor 111, the reaction is realized in the catalyst environment, and the product gas of the upper reactor upwards enters the gas-solid separation zone 3; in the reaction process, the lower fluidized bed, i.e., the lower reaction zone 112, continuously carries the catalyst to the upper fluidized bed, i.e., the upper reaction zone 212, the upper fluidized bed realizes the stability of the catalyst layer height or the catalyst inventory through catalyst overflow, and the redundant catalyst overflows into the catalyst return pipe 114A and the second catalyst return pipe 114B and returns to the lower fluidized bed; the upper reactor product gas leaves the upper fluidized bed and enters the gravity dilute phase settling zone 316 of the gas-solid separation zone 3 to reduce the catalyst content, then enters the two-stage cyclone separator to separate the catalyst continuously, the catalyst enters the upper reaction zone 212 from the catalyst outflow pipe 314 of the common primary cyclone separator and the catalyst outflow pipe 324 of the common secondary cyclone separator downwards, and the reaction product gas P enters the plenum chamber 325 from the outlet 323 of the common secondary cyclone separator and flows out from the outlet 326 of the reactor product gas. In specific implementation, the reaction raw material Y1 and the second reaction raw material Y2 can be the same or different, and proper water or water vapor can be added into the methanol raw material before the methanol raw material enters the catalytic conversion reactor; other reaction raw materials, especially the components of the methanol reaction product which are not the target products, can be mixed with the methanol or enter the upper reaction zone 212 or the lower reaction zone 112 separately for catalytic conversion again to increase the target products.

The second embodiment is as follows:

FIG. 2 is a schematic diagram of a catalytic conversion reactor apparatus according to another embodiment of the present invention;

the catalytic conversion reactor shown in FIG. 2 consists of a lower reactor, an upper reactor and a gas-solid separation zone; reactant flow baffle 115 is a tapered plate; a second reactant flow outlet 121A, which is disposed in the central region of the catalytic conversion reactor and whose cross-sectional area is gradually reduced, specifically, whose lower portion has a diameter smaller than that of the upper portion;

the gas-solid separation zone shell 310 is provided with a reactor product gas outlet 326; the gas-solid separation zone is provided with more than two groups of two-stage cyclone separators which are connected in parallel, the lower-layer reactor and the upper-layer reactor share the two-stage cyclone separators, and the outlets of the cyclone separators are connected with a shared gas collection chamber 325 and a reactor product gas outlet 326; in implementation, each group of two-stage cyclone separators comprises a shared primary cyclone separator 311 and a shared secondary cyclone separator 321, the shared two-stage cyclone separators are arranged in a vertically staggered manner, and the shared primary cyclone separator 311 is arranged below;

two catalyst return pipes, namely a catalyst return pipe 114A and a second catalyst return pipe 114B, are arranged between the upper reaction zone 212 and the lower reaction zone 112, and the two catalyst return pipes are designed in an overflow mode; a heat taking pipe 116 is arranged in the lower reactor; a cyclone separator 120 which rotates in the circumferential direction is arranged at the outlet of the second reactant flow leading-out pipe 121A, and the cyclone separator 120 consists of more than two cyclone pipes 122 which are uniformly distributed in the circumferential direction and a cyclone separator shell 123; a cyclone separator shell 123 is arranged outside the cyclone tube 122, and a cyclone separator shell gas outlet 125 is arranged at the top of the cyclone separator shell 123; a catalyst outflow port is reserved between the lower edge of the cyclone separator shell 123 and the upper layer reactor; an upper reaction zone 212 is formed between the cyclone separator 120 and the upper reactor shell 210;

in this embodiment, the product gas of the lower reactor enters the second reactant flow outlet pipe 121A, then enters the cyclone separator 120, enters the gravity dilute phase settling zone 316 of the upper gas-solid separation zone from the gas outlet 125 of the cyclone separator housing to mix with the product gas of the upper reactor, is further separated from the catalyst by the two-stage cyclone separator, and then flows out from the product gas outlet 326 of the reactor; the catalyst separated by the cyclone 120 settles into the upper reaction zone 212.

Other parts of the device structure of this embodiment are the same as those of the first embodiment.

The catalytic conversion reaction process shown in fig. 2 is as follows:

the reaction raw material catalytic conversion reaction process is completed in a lower layer reactor and an upper layer reactor of the catalytic conversion reactor in parallel, the reaction raw material respectively enters reaction zones at the bottoms of the lower layer reactor and the upper layer reactor through a raw material distributor, namely enters a lower layer reaction zone 112 through a lower layer raw material distributor 111 and enters an upper layer reaction zone 212 through an upper layer raw material distributor 211, the reacted reaction product gas of the lower layer reactor and the reaction product gas of the upper layer reactor enter a gas-solid separation zone above the catalytic conversion reactor, and the catalyst is separated and flows out of the catalytic conversion reactor;

the second regenerated catalyst GC1 which meets the requirements from the regenerator enters the upper reaction zone 212, and the spent catalyst SC is led out from the upper reaction zone 212 and returns to the regenerator; the catalyst amount of the lower layer reactor and the upper layer reactor is determined according to the space velocity required by the reaction or the height of the reaction catalyst layer or the residence time of the gas in the catalyst layer under the corresponding normal operating condition;

the reaction raw material Y1 after heat exchange enters the lower reaction zone 112 from the lower raw material distributor 111, the second reaction raw material Y2 after heat exchange directly enters the upper reaction zone 212 from the upper raw material distributor 211, catalytic conversion reaction is carried out in the environment of catalyst, and the gas apparent flow velocity of the lower reaction zone 112 and the upper reaction zone 211 is lower than the conversion flow velocity of the fast fluidized bed or the circulating fluidized bed;

after the reaction raw materials are reacted, the reaction product gas leaves the lower layer reaction zone 112 and the upper layer reaction zone 212, enters the dilute phase space of the corresponding reactor and then enters the gas-solid separation zone; the product gas of the lower reactor leaves the catalyst bed of the fluidized bed, and enters the dilute phase space 113 of the lower reactor upwards, and part of the catalyst is settled in the lower reaction zone 112 due to gravity, so that the catalyst carried by the product gas of the lower reactor is reduced; the reaction product gas of the lower layer reactor is led out from a second reactant flow outlet pipe 121A isolated from the upper layer reactor, enters a cyclone pipe 122, is changed into circumferential rotary flow from upward flow in the cyclone pipe 122, the gas and the catalyst continuously flow in the cyclone separator shell 123 in a circumferential rotary manner after flowing out of the cyclone pipe 122, the catalyst is concentrated towards the cyclone separator shell 123 under the action of centrifugal force and is descended into the upper layer reaction zone 212 under the action of gravity, and the gas enters a gravity dilute phase settling zone 316 of a gas-solid separation zone upwards at a gas outlet 125 of the cyclone separator shell; the product gas of the upper reactor after the reaction leaves the catalyst bed layer of the fluidized bed, and enters the dilute phase space 213 of the upper reactor upwards, and part of the catalyst is settled in the upper reaction zone 212 due to gravity; the reaction product gas of the lower layer reactor and the reaction product gas of the upper layer reactor are firstly mixed in a gravity dilute phase settling zone 316 of a gas-solid separation zone, then enter a two-stage cyclone separator shared by the cyclone separation zones, after the catalyst is further separated, the reaction product gas flows out of the catalytic conversion reactor from a product gas outlet 326 of the reactor, the separated catalyst is settled in the upper layer reaction zone 212, and the catalyst which is more than the reaction requirement overflows to the lower layer reaction zone 112 from a catalyst return pipe.

In operation, a second regenerated catalyst GC1 is first provided to the upper reactor to reach the upper reaction zone height H2, and when the catalyst layer height continues to rise, the catalyst overflows from the catalyst return pipe inlet 124 into the second catalyst return pipe 114B or into the catalyst return pipe 114A and down into the lower reaction zone 112; after the catalyst in the lower reaction zone 112 reaches the required amount, namely the height H1 of the lower reaction zone, the heat-exchanged reaction raw material Y1 uniformly enters the lower reaction zone 112 from the reaction raw material inlet through the lower raw material distributor 111, and the heat-exchanged reaction raw material Y2 uniformly enters the upper reaction zone 212 from the reaction raw material inlet through the upper raw material distributor 211, so that the catalyst in the lower reaction zone 112 and the catalyst in the upper reaction zone 212 are fluidized and react; after the reaction is finished, the product gas of the lower layer reactor carries partial catalyst to enter a second reactant flow eduction tube 121A, then enters a cyclone separator 120 to separate partial catalyst, and then enters a gravity dilute phase settling zone 316 of a gas-solid separation zone; the separated catalyst settles to the upper reaction zone 212; the product gas of the upper reactor upwards enters a gas-solid separation zone; in the reaction process, the lower reaction zone 112 continuously carries the catalyst to the upper reaction zone 212, and the redundant catalyst overflows into the catalyst return pipe 114A and the second catalyst return pipe 114B and returns to the lower fluidized bed; the upper reactor product gas leaves the upper fluidized bed and enters the gravity dilute phase settling zone 316 of the gas-solid separation zone to reduce the catalyst content, then enters the two-stage cyclone separator to separate the catalyst continuously, the catalyst enters the upper reaction zone 212 from the catalyst outflow pipe 314 of the common primary cyclone separator and the catalyst outflow pipe 324 of the common secondary cyclone separator downwards, and the reaction product gas P enters the plenum chamber 325 from the outlet 323 of the common secondary cyclone separator and flows out from the product gas outlet 326 of the reactor.

The third concrete implementation mode:

FIG. 3 is a schematic diagram of a catalytic conversion reactor apparatus according to another embodiment of the present invention;

the catalytic conversion reactor shown in FIG. 3, which consists of a lower reactor, an upper reactor and a gas-solid separation zone; reactant flow baffle 115 is a tapered plate; a second reactant flow outlet pipe 121A is arranged in the central area of the catalytic conversion reactor, and the cross-sectional area thereof is gradually reduced;

the lower layer reactor and the upper layer reactor are respectively provided with an independent cyclone separator in the gas-solid separation zone, and the shell 310 of the gas-solid separation zone is provided with a reactor product gas outlet 326; the cyclone separation zone is respectively provided with an independent first-stage cyclone separator 151 of the lower-layer reactor and an independent two-stage cyclone separator of the upper-layer reactor;

wherein the first-stage cyclone separator 151 of the lower-layer reactor is provided with a first-stage cyclone separator inlet 152 of the lower-layer reactor and a first-stage cyclone separator outlet 153 of the lower-layer reactor, the first-stage cyclone separator outlet 153 of the lower-layer reactor is communicated with a product gas conveying pipe connecting pipe 155 of the lower-layer reactor, a product gas conveying pipe 136 of the lower-layer reactor is communicated with a gas collection chamber 325 through the outlet of the first-stage cyclone separator of the lower-layer reactor, and the gas collection chamber 325 is communicated with a product gas outlet 326 of the;

the upper reactor two-stage cyclone separator is provided with an upper reactor primary cyclone separator 221 and an upper reactor secondary cyclone separator 231, wherein the upper reactor primary cyclone separator 221 is provided with an upper reactor primary cyclone separator inlet 222, an upper reactor primary cyclone separator outlet 223 and an upper reactor primary cyclone separator catalyst outflow pipe 224, and the upper reactor secondary cyclone separator 231 is provided with an upper reactor secondary cyclone separator inlet 232, an upper reactor secondary cyclone separator outlet 233 and an upper reactor secondary cyclone separator catalyst outflow pipe 234; the upper reactor secondary cyclone 231 is connected to the upper reactor primary cyclone 221 through an upper reactor primary cyclone outlet and secondary cyclone inlet connection pipe 225; the upper reactor secondary cyclone 231 is communicated with the gas collection chamber 325 through an outlet of the upper reactor secondary cyclone and a gas collection chamber connecting pipe 235; when the device is specifically installed, the primary cyclone separator 151 of the lower reactor is installed at the lowest part, and the device main body and the primary cyclone separator 221 of the upper reactor are installed in a vertically staggered manner;

a cyclone separator 120 which rotates in the circumferential direction is arranged at the outlet of the second reactant flow leading-out pipe 121A, and the cyclone separator 120 consists of more than two cyclone pipes 122 which are uniformly distributed in the circumferential direction and a cyclone separator shell 123; a cyclone separator shell 123 is arranged outside the cyclone tube 122, and a cyclone separator shell gas outlet 125 is arranged at the top of the cyclone separator shell 123; a catalyst outflow port is reserved between the lower edge of the cyclone separator shell 123 and the upper layer reactor; an upper reaction zone 212 is formed between the cyclone separator 120 and the upper reactor shell 210; the gas outlet 125 of the cyclone separator shell is respectively connected with the inlet 152 of the first-stage cyclone separator of the lower-layer reactor through a conveying pipe 126, a conveying pipe and a connecting pipe 157 of the inlet of the first-stage cyclone separator of the lower-layer reactor;

two catalyst return pipes, i.e., a catalyst return pipe 114A and a second catalyst return pipe 114B, are provided between the upper reaction zone 212 and the lower reaction zone 112;

in this mode, the lower reactor and the upper reactor are provided with external heat collectors, which can be conveniently mastered by engineering technicians and are not shown in the figure;

in this embodiment, the second regenerated catalyst GC1 which comes from the regenerator and meets the requirement enters the upper reaction zone 212, the regenerated catalyst GC which comes from the regenerator and meets the requirement enters the lower reaction zone 112, the spent catalyst SC is led out from the upper reaction zone 212 and returns to the regenerator, the second spent catalyst SC1 is led out from the lower reaction zone 112 and returns to the regenerator, and when the height of the catalyst layer is higher than the inlet of the second catalyst return pipe 114B or the catalyst return pipe 114A, the catalyst enters the second catalyst return pipe 114B or the catalyst return pipe 114A and downwardly enters the lower reaction zone 112; the catalyst height of the upper layer reactor reaches the upper layer reaction zone height H2, and the catalyst height of the lower layer reactor reaches the upper layer reaction zone height H1; the reaction raw material Y1 after heat exchange enters the lower reaction zone 112 from the lower raw material distributor 111, and the second reaction raw material Y2 after heat exchange directly enters the upper reaction zone 212 from the upper raw material distributor 211 to perform catalytic conversion reaction in the catalyst environment; after the reaction is finished, the product gas of the lower layer reactor firstly enters the cyclone separator 120 arranged at the outlet of the second reactant flow outlet pipe 121A, enters the first-stage cyclone separator 151 of the lower layer reactor from the gas outlet 125 and the conveying pipe 126 of the cyclone separator shell to further separate the catalyst, and directly flows out of the catalytic conversion reactor along the product gas conveying pipe 136 of the lower layer reactor or enters the gas collection chamber 325 to be mixed with the product gas of the upper layer reactor; the upper reactor product gas firstly enters a gravity dilute phase settling zone 316 of a gas-solid separation zone, the catalyst content is reduced, and then the product gas respectively flows through an upper reactor primary cyclone separator 221 and an upper reactor secondary cyclone separator 231, and enters a gas collection chamber 325 after the catalyst is separated; the final reactor product gas P exits the catalytic conversion reactor via reactor product gas outlet 326.

The fourth concrete implementation mode:

FIG. 4 is a schematic diagram of a catalytic conversion reactor apparatus according to another embodiment of the present invention;

the catalytic conversion reactor shown in FIG. 4, which consists of a lower reactor, an upper reactor and a gas-solid separation zone; a reactant flow baffle 115 and a second reactant flow outlet tube 121A are arranged;

the lower layer reactor and the upper layer reactor are respectively provided with an independent cyclone separator in the gas-solid separation zone, and the shell 310 of the gas-solid separation zone is provided with a reactor product gas outlet 326 and a second reactor product gas outlet 236; the cyclone separation zone is respectively provided with two independent cyclone separators of the lower layer reactor and two independent cyclone separators of the upper layer reactor;

the two-stage cyclone separator of the lower layer reactor is provided with a lower layer reactor primary cyclone separator 131 and a lower layer reactor secondary cyclone separator 141 which are connected with a secondary cyclone separator inlet connecting pipe 135 through an outlet of the lower layer reactor primary cyclone separator, the lower layer reactor secondary cyclone separator 141 is communicated with a gas collection chamber 325 through a lower layer reactor secondary cyclone separator outlet and a lower layer reactor product gas conveying pipe connecting pipe 145, a lower layer reactor product gas conveying pipe 146 and the gas collection chamber 325 are communicated, and the gas collection chamber 325 is communicated with a reactor product gas outlet 326;

the upper reactor two-stage cyclone separator is provided with an upper reactor primary cyclone separator 221 and an upper reactor secondary cyclone separator 231 which are connected through an upper reactor primary cyclone separator outlet and a secondary cyclone separator inlet connecting pipe 225, and an upper reactor secondary cyclone separator outlet 233 is directly connected with a second reactor product gas outlet 236;

when the device is installed, the two-stage cyclone separators of the lower layer reactor are installed below, and the device main body and the two-stage cyclone separators of the upper layer reactor are installed in a vertically staggered mode;

a cyclone separator 120 rotating in the circumferential direction is arranged at the outlet of the second reactant flow outlet pipe 121A, and a gas outlet 125 of a shell of the cyclone separator is connected with an inlet 132 of a primary cyclone separator of a lower layer reactor through a conveying pipe 126, the conveying pipe and a connecting pipe 127 of the inlet of the primary cyclone separator of the lower layer reactor respectively;

in this embodiment, the second regenerated catalyst GC1 which comes from the regenerator and meets the requirements enters the upper reaction zone 212, the second spent catalyst SC1 is led out from the lower reaction zone 112 and returns to the regenerator, the reaction raw material Y1 after heat exchange enters the lower reaction zone 112 from the lower raw material distributor 111, and the second reaction raw material Y2 after heat exchange directly enters the upper reaction zone 212 from the upper raw material distributor 211, and undergoes catalytic conversion reaction in the presence of a catalyst; after the reaction is finished, the product gas of the lower layer reactor firstly enters the cyclone separator 120 arranged at the outlet of the second reactant flow outlet pipe 121A, enters the primary cyclone separator 131 of the lower layer reactor and the secondary cyclone separator 141 of the lower layer reactor from the gas outlet 125 and the conveying pipe 126 of the cyclone separator shell to further separate the catalyst, then enters the gas collection chamber 325 along the product gas conveying pipe 136 of the lower layer reactor, and flows out of the catalytic conversion reactor along the product gas outlet 326 of the reactor; the upper reactor product gas firstly enters the gravity dilute phase settling zone 316 of the gas-solid separation zone, the catalyst content is reduced, and then the catalyst flows through the upper reactor primary cyclone 221 and the upper reactor secondary cyclone 231 respectively, after the catalyst is separated, the catalyst flows out of the catalytic conversion reactor through the second reactor product gas outlet 236.

The other parts of the device structure of this embodiment are the same as those of the third embodiment.

The fifth concrete implementation mode:

FIG. 5 is a schematic diagram of a catalytic conversion reactor apparatus according to another embodiment of the present invention;

the catalytic conversion reactor shown in fig. 5, which consists of a lower reactor 1, an upper reactor 2 and a gas-solid separation zone 3, has a lower reactor diameter D1, an upper reactor diameter D2 and a gas-solid separation zone diameter D3, respectively; a reactant flow divider 115 and a second reactant flow outlet 121A, the second reactant flow outlet 121A having a progressively decreasing cross-sectional area, i.e., an upper diameter D5 less than a lower diameter D4;

the gas-solid separation zone shell 310 is provided with a reactor product gas outlet 326; the gas-solid separation zone 3 is provided with more than two groups of two-stage cyclone separators which are connected in parallel, the lower layer reactor 1 and the upper layer reactor 2 share the two-stage cyclone separators, and the outlets of the cyclone separators are connected with a shared gas collection chamber 325 and a reactor product gas outlet 326; in implementation, each group of two-stage cyclone separators comprises a shared primary cyclone separator 311 and a shared secondary cyclone separator 321, the shared two-stage cyclone separators are arranged in a vertically staggered manner, and the shared primary cyclone separator 311 is arranged below;

two catalyst return pipes, i.e., a catalyst return pipe 114A and a second catalyst return pipe 114B, are provided between the upper reaction zone 212 and the lower reaction zone 112; a heat taking pipe 116 is arranged in the lower reactor;

a cyclone separator 120 rotating in the circumferential direction is arranged at the outlet of the second reactant flow outlet pipe 121A, the cyclone separator shell 123 of the cyclone separator 120 is provided with a cyclone separator shell diameter D6 and a cyclone separator shell gas outlet diameter D7, the size of D7 is smaller than D6, and the top of the cyclone separator shell 123 is provided with a cyclone separator shell gas outlet 125; a catalyst outlet is reserved between the lower edge of the cyclone separator shell 123 and the upper reactor 2; an upper reaction zone 212 is formed between the cyclone separator 120 and the upper reactor shell 210;

in this embodiment, the regenerated catalyst GC from the regenerator meeting the requirements enters the lower reaction zone 112, and the spent catalyst SC is led out from the upper reaction zone 212 and returned to the regenerator; the reaction raw material Y1 after heat exchange enters the lower reaction zone 112 from the lower raw material distributor 111, and the second reaction raw material Y2 after heat exchange directly enters the upper reaction zone 212 from the upper raw material distributor 211 to perform catalytic conversion reaction in the catalyst environment; after the reaction is completed, the product gas of the lower layer reactor firstly enters the cyclone separator 120 arranged at the outlet of the second reactant flow outlet pipe 121A, enters the gravity dilute phase settling zone 316 of the upper gas-solid separation zone 3 from the gas outlet 125 of the cyclone separator shell to be mixed with the product gas of the upper layer reactor, and after the catalyst is further separated by the two-stage cyclone separator, the product gas P of the reactor flows out of the catalytic conversion reactor from the product gas outlet 326 of the reactor.

Other parts of the device structure of this embodiment are the same as those of the second embodiment.

The sixth specific implementation mode:

FIG. 6 is a schematic diagram of a catalytic conversion reactor apparatus according to another embodiment of the present invention;

as shown in fig. 6, the catalytic conversion reactor is composed of a lower reactor 1, an upper reactor 2 and a gas-solid separation zone 3, and has a lower reactor diameter D1, an upper reactor diameter D2 and a gas-solid separation zone diameter D3, respectively;

the reactant flow withdrawal tubes 121B are two in parallel, have a constant cross-sectional area with an upper diameter D5, and have a lower diameter of the same size as the upper diameter D5;

the lower layer reactor 1 and the upper layer reactor 2 share a cyclone separator in the gas-solid separation zone 3, and the gas-solid separation zone shell 310 is provided with a gas collection chamber 325 and a reactor product gas outlet 326; the gas-solid separation zone 3 is provided with more than two groups of two-stage cyclone separators which are connected in parallel, each group of two-stage cyclone separators comprises a shared primary cyclone separator 311 and a shared secondary cyclone separator 321, and the shared secondary cyclone separator 321 is respectively connected with the primary cyclone separator 311 through a shared primary cyclone separator outlet and secondary cyclone separator inlet connecting pipe 315A and a second shared primary cyclone separator outlet and secondary cyclone separator inlet connecting pipe 315B; the common secondary cyclone outlet 323 is in communication with the plenum 325; in this mode, the shared two-stage cyclone separator apparatus main body is installed in a vertically staggered manner, and the shared primary cyclone separator 311 is located below;

a cyclone separator 120 rotating circumferentially is arranged at the outlet of each reactant flow outlet pipe 121B, a cyclone separator shell 123 of the cyclone separator 120 is provided with a cyclone separator shell diameter D6, and a cyclone separator shell gas outlet 125 is arranged at the top of the cyclone separator shell 123; a catalyst outlet is reserved between the lower edge of the cyclone separator shell 123 and the upper reactor 2;

in this embodiment, the regenerated catalyst GC from the regenerator meeting the requirements enters the lower reaction zone 112, and the spent catalyst SC is led out from the upper reaction zone 212 and returned to the regenerator; the reaction raw material Y1 after heat exchange enters the lower reaction zone 112 from the lower raw material distributor 111, and the second reaction raw material Y2 after heat exchange directly enters the upper reaction zone 212 from the upper raw material distributor 211 to perform catalytic conversion reaction in the catalyst environment; after the reaction is finished, the product gas of the lower layer reactor enters the cyclone separators 120 arranged at the outlets of the reactant flow leading-out pipes 121B respectively, is collected from the gas outlets 125 of the cyclone separator shells and enters the gravity dilute phase settling zone 316 of the upper gas-solid separation zone 3 to be mixed with the product gas of the upper layer reactor, and after the catalyst is further separated by the two stages of cyclone separators, the product gas P of the reactor flows out of the catalytic conversion reactor from the product gas outlet 326 of the reactor.

The seventh embodiment:

FIG. 7 is a schematic diagram of a catalytic conversion reactor apparatus according to another embodiment of the present invention;

the catalytic conversion reactor shown in fig. 7, which is composed of a lower reactor 1, an upper reactor 2 and a gas-solid separation zone 3, has a lower reactor diameter D1, an upper reactor diameter D2 and a gas-solid separation zone diameter D3, respectively; the reactant flow withdrawal tubes 121B are two in parallel, have a constant cross-sectional area with an upper diameter D5, and have a lower diameter of the same size as the upper diameter D5;

the outlets of the two reactant flow leading-out pipes 121B are respectively provided with a cyclone separator 120 which rotates in the circumferential direction, and each cyclone separator 120 consists of more than two cyclone pipes 122 which are uniformly distributed in the circumferential direction and a cyclone separator shell 123; a cyclone shell 123 is arranged outside the cyclone tube 122 and has the diameter D6 of the cyclone shell, and a cyclone shell gas outlet 125 is arranged at the top of the cyclone shell 123; a catalyst outlet is reserved between the lower edge of the cyclone separator shell 123 and the upper reactor 2;

the gas-solid separation zone 3 is provided with a common gas collecting chamber 325, and the gas-solid separation zone shell 310 is provided with a reactor product gas outlet 326; the lower layer reactor 1 is provided with an independent lower layer reactor primary cyclone separator 151 communicated with one cyclone separator 120 in the gas-solid separation zone 3, the lower layer reactor primary cyclone separator 151 is communicated with a gas outlet 125 of a cyclone separator shell through a conveying pipe and a lower layer reactor primary cyclone separator inlet connecting pipe 157 and a conveying pipe 126, the lower layer reactor primary cyclone separator 151 is communicated with a gas collection chamber 325 through a lower layer reactor product gas conveying pipe 136, and the gas collection chamber 325 is communicated with a reactor product gas outlet 326;

a shared two-stage cyclone separator is arranged in the gas-solid separation zone 3, the other cyclone separator 120 and the upper reactor 2 share the shared two-stage cyclone separator, the two-stage cyclone separator comprises a shared primary cyclone separator 311 and a shared secondary cyclone separator 321, the shared secondary cyclone separator 321 is connected with the primary cyclone separator 311 through a shared primary cyclone separator outlet and a secondary cyclone separator inlet connecting pipe 315, and a shared secondary cyclone separator outlet 323 is communicated with a gas collection chamber 325; in the mode, the primary cyclone separator 151 of the lower-layer reactor and the shared two-stage cyclone separator device main body are arranged in a vertically staggered manner, and the primary cyclone separator 151 of the lower-layer reactor is arranged below the lower-layer reactor;

in this embodiment, the regenerated catalyst GC from the regenerator meeting the requirements enters the lower reaction zone 112, and the spent catalyst SC is led out from the upper reaction zone 212 and returned to the regenerator; the reaction raw material Y1 after heat exchange enters the lower reaction zone 112 from the lower raw material distributor 111, and the second reaction raw material Y2 after heat exchange directly enters the upper reaction zone 212 from the upper raw material distributor 211 to perform catalytic conversion reaction in the catalyst environment; after the reaction is finished, the product gas of the lower layer reactor firstly enters a cyclone separator 120 arranged at the outlet of a reactant flow outlet pipe 121B, after a part of catalyst is separated, a part of the catalyst enters a first-stage cyclone separator 151 of the lower layer reactor from a gas outlet 125 and a conveying pipe 126 of a cyclone separator shell to be further separated, the catalyst directly flows out of the catalytic conversion reactor or enters a gas collection chamber 325 along a conveying pipe 136 of the product gas of the lower layer reactor, and a part of the catalyst directly enters a gravity dilute phase settling zone 316 of a gas-solid separation zone 3 from the gas outlet 125 of the cyclone separator shell to be mixed with the product gas of the upper layer reactor; the product gas of the upper reactor firstly enters a gravity dilute phase settling zone 316, the catalyst content is reduced, and then the product gas respectively passes through a flow sharing primary cyclone separator 311 and a sharing secondary cyclone separator 321, and enters a gas collection chamber 325 after the catalyst is separated; the final reactor product gas P exits the catalytic conversion reactor via reactor product gas outlet 326.

Example (b):

the method of the invention is adopted to prepare olefin by taking methanol as a raw material. The methanol feed was 300 million tons/year, the desired products were ethylene and propylene, the ethylene and propylene ratio was 1: 1.

Reaction condition parameters are as follows:

the methanol feed temperature was 250 ℃ and the water content was 5% by weight; the reaction time of the upper reactor and the lower reactor is 2.0 seconds, the reaction temperature is 495 ℃, the space velocity (WHSV) is 5(1/H), the catalyst-alcohol ratio of the circulating regeneration catalyst of the upper reactor and the lower reactor is 1/5, and the average diameter of catalyst particles is 60 microns; the feeding amount of methanol in the upper reactor is 120 ten thousand tons/year, the reaction pressure is 0.13MPaG, the apparent flow velocity of gas in the upper reaction zone is 0.8 m/s, the height H2 of the upper reaction zone, namely the height of a catalyst layer, is 1.6 m, the height H4 of dilute phase space of the upper reactor is 2m, and the diameter D2 of the upper reactor is 12 m; the methanol feeding amount of the lower reactor is 180 ten thousand tons per year, the reaction pressure is 0.14MPa (MPa), the gas apparent flow velocity of the lower reaction zone is 1.0 m/s, the height of the catalyst layer above the lower raw material distributor, namely the height H1 of the lower reaction zone is 2m, the height H3 of dilute phase space of the lower reactor is 4m, and the diameter D1 of the lower reactor is 12 m; a reactant flow eduction tube is arranged at the center of the upper layer reactor, a conical partition plate is arranged between the inlet of the reactant flow eduction tube and the shell of the lower layer reactor, the residence time of the product gas of the lower layer reactor in the conical space under the conical partition plate and the reactant flow eduction tube is 2.0 seconds, and an equal-diameter reactant flow eduction tube with the upper diameter D5 of 3.5 meters (inner diameter) is adopted; the regenerated catalyst enters the catalytic conversion reactor from the upper reaction zone, the spent catalyst flows out from the upper reaction zone, and the input amount of the regenerated catalyst is 130 tons/hour; 4 catalyst return pipes are uniformly arranged outside the upper layer reactor shell and the lower layer reactor shell in the circumferential direction; the material flow velocity of the reactant flow eduction tube is 12 m/s, 8 cyclone tubes are arranged at the outlet of the reactant flow eduction tube, and the apparent gas flow velocity at the outlet of the cyclone tubes is 10 m/s; the diameter D6 of the shell of the cyclone separator is designed according to the gas apparent flow velocity of the cross section area of 5 m/s, and the lower edge of the shell of the cyclone separator is 600 mm away from the upper layer raw material distributor; the gas outlet of the shell of the cyclone separator is provided with 18 parallel primary cyclone separators, and the gas flow speed at the inlet of each primary cyclone separator is 12 m/s; the product gas of the lower layer reactor directly enters a shared gas collecting chamber at the top of the gas-solid separation zone from the outlet of the first-stage cyclone separator through a product gas conveying pipe of the lower layer reactor and flows out from the product gas outlet of the reactor, and the product gas conveying pipe of the lower layer reactor is vertically arranged at the center of the gas-solid separation zone; the diameter D3 of the gas-solid separation zone is 16 meters, and the tangent height of the straight section is 14 meters; the height of a transition cone between the upper layer reactor shell and the gas-solid separation zone shell is 8 m; the total tangential height of the upper layer reactor shell and the lower layer reactor shell is 10.6 meters; the lower layer raw material distributor adopts a tubular distributor, the upper layer raw material distributor adopts a plate-type distribution plate, and the opening rate is 10%; the inner diameter of the shell of the lower layer reactor is 11.5 meters, and the inner diameter of the upper layer reactor is 12 meters; a methanol raw material heat taking pipe is arranged in the upper layer reactor, and the temperature of a reaction area is controlled; the lower reactor is provided with an external heat collector for gasifying water and controlling the temperature of the reaction zone.

The implementation result shows that: for the same reaction conditions, the prior art uses a single-bed fluidized-bed reactor reaction zone with a reactor diameter of 16 meters. The diameter is only 12 meters when the invention is used.

Claims

1. A catalytic conversion reaction method, the reaction raw materials catalytic conversion reaction process is finished in the lower reactor (1) and upper reactor (2) of the catalytic conversion reactor in parallel, the reaction raw materials enter the reaction zone of the bottom of the lower reactor (1) and upper reactor (2) through the raw material distributor respectively, namely enter the lower reaction zone (112) through the lower raw material distributor (111), enter the upper reaction zone (212) through the upper raw material distributor (211), the lower reactor reaction product gas and upper reactor reaction product gas after finishing the reaction enter the gas-solid separation zone (3) above the catalytic conversion reactor, flow out the catalytic conversion reactor after separating out the catalyst;

corresponding reactor dilute phase spaces are arranged above the lower-layer reaction zone (112) and the upper-layer reaction zone (212), and reaction product gas firstly enters the corresponding reactor dilute phase spaces and then enters the gas-solid separation zone (3) after leaving the lower-layer reaction zone (112) and the upper-layer reaction zone (212); the gas-solid separation zone (3) is provided with a gravity dilute phase settling zone and a cyclone separation zone;

the reaction product gas of the lower layer reactor is led out from a reaction material flow leading-out pipe isolated from the upper layer reactor (2), enters a gas-solid separation zone (3), and flows out from a product gas outlet of the reactor after the gas-solid separation zone (3) finishes the separation of the catalyst; the product gas of the upper layer reactor enters a gravity dilute phase settling zone of a gas-solid separation zone (3), the catalyst content or carrying capacity is reduced, then the product gas enters a cyclone separation zone for catalyst separation, and then the product gas flows out from a product gas outlet of the reactor;

the reaction product gas of the lower layer reactor and the reaction product gas of the upper layer reactor are respectively separated out of the catalyst by a cyclone separator which is arranged in a gas-solid separation zone (3) and is independent from each other and then flow out of the catalytic conversion reactor; or the reaction product gas of the lower layer reactor and the reaction product gas of the lower layer reactor are firstly mixed in a gravity dilute phase settling zone of the gas-solid separation zone (3), then enter a shared cyclone separator to separate the catalyst, and then flow out of the catalytic conversion reactor.

2. The catalytic conversion reaction process according to claim 1, wherein the regenerated catalyst from the regenerator is introduced into the lower reaction zone (112) and/or the upper reaction zone (212), the spent catalyst is led out from the lower reaction zone (112) and/or the upper reaction zone (212) and returned to the regenerator, and the catalyst inventory of the lower reactor (1) and the upper reactor (2) is controlled by a catalyst return pipe; the catalyst separated from the reaction product gas of the lower layer reactor and the reaction product gas of the upper layer reactor in the gas-solid separation zone (3) is settled to the upper layer reaction zone (212) by gravity, and the catalyst which is more than the catalyst required by the reaction flows back to the lower layer reaction zone (112).

3. The catalytic conversion reaction method according to claim 1, wherein the reaction raw material of the lower reactor (1) enters the lower reaction zone (112) from the lower raw material distributor (111), the product gas of the lower reactor after the reaction leaves the fluidized bed catalyst bed layer and enters the dilute phase space (113) of the lower reactor upwards, and part of the catalyst is settled into the lower reaction zone (112) due to gravity, so that the catalyst carried by the product gas of the lower reactor is reduced; then the product gas of the lower layer reactor firstly enters a gravity dilute phase settling zone of the gas-solid separation zone (3) from the reactant flow eduction tube to be mixed with the product gas of the upper layer reactor, or firstly enters a cyclone separator (120) arranged at the outlet of the reactant flow eduction tube to enter the gravity dilute phase settling zone of the upper gas-solid separation zone (3) from a gas outlet (125) of a shell of the cyclone separator to be mixed with the product gas of the upper layer reactor; the product gas of the lower layer reactor flows out from the product gas outlet of the reactor after the catalyst is further separated in the gas-solid separation zone (3) by a first-stage cyclone separator or a second-stage cyclone separator; the catalyst separated by the cyclone separator (120) settles to the upper reaction zone (212).

4. The catalytic conversion reaction process according to claim 3, wherein the product gas in the lower reactor directly enters the single-stage cyclone separator or the two-stage cyclone separator after leaving the cyclone separator (120) to complete the gas-solid separation, and then flows out of the catalytic conversion reactor.

5. The catalytic conversion reaction process according to claim 1, wherein the reaction raw material of the upper reactor (2) directly enters the upper reaction zone (212) from the upper raw material distributor (211), the product gas of the upper reactor after the reaction leaves the fluidized bed catalyst bed layer and upwards enters the dilute phase space (213) of the upper reactor, part of the catalyst settles into the upper reaction zone (212) due to gravity, the product gas of the upper reactor enters the two-stage cyclone separator of the cyclone separation zone of the upper gas-solid separation zone (3), and the catalyst is further separated and flows out of the catalytic conversion reactor.

6. The catalytic conversion reaction method according to claim 1, wherein the reaction product gas of the lower reactor is led out by more than two reactant flow outlet pipes, or the outlets of the reactant flow outlet pipes are all provided with cyclone separators (120), and the reaction product gas of the lower reactor flowing out of the cyclone separators (120) is subjected to gas-solid separation in an independent first-stage cyclone separator or a two-stage cyclone separator; or the outlet part of the reactant flow outlet pipe is provided with a cyclone separator (120), the reaction product gas of the lower layer reactor flowing out of the cyclone separator (120) is subjected to gas-solid separation in an independent first-stage cyclone separator or a two-stage cyclone separator, and the reaction product gas of the rest lower layer reactor is mixed with the reaction product gas of the upper layer reactor in a gas-solid separation zone (3) and then is subjected to gas-solid separation in the two-stage cyclone separator.

7. A catalytic conversion reactor, characterized by:

consists of a lower layer reactor (1), an upper layer reactor (2) and a gas-solid separation zone (3);

the top of the lower layer reactor (1) is provided with a reactant flow partition plate (115) and a reactant flow eduction tube to separate the lower layer reactor (1) from the upper layer reactor (2); the reactant flow separator (115) is a flat or tapered plate; the reactant flow eduction tube is vertically arranged in the upper layer reactor (2); the bottom areas of the lower layer reactor (1) and the upper layer reactor (2) are respectively provided with a reaction raw material inlet;

the lower-layer reactor (1) comprises a lower-layer reaction zone (112) and a lower-layer reactor dilute-phase space (113) above the lower-layer reaction zone, the upper-layer reactor (2) comprises an upper-layer reaction zone (212) and an upper-layer reactor dilute-phase space (213) above the upper-layer reaction zone, and the gas-solid separation zone (3) comprises a gravity dilute-phase settling zone and a cyclone separation zone;

the lower layer reactor (1) and the upper layer reactor (2) are respectively provided with an independent cyclone separator in the gas-solid separation zone (3) or the lower layer reactor (1) and the upper layer reactor (2) share a cyclone separator; the gas-solid separation zone shell (310) is provided with a reactor product gas outlet; the reactor is characterized in that a tubular or plate-type lower-layer raw material distributor (111) is arranged in the lower-layer reactor (1), and a tubular or plate-type upper-layer raw material distributor (211) is arranged in the upper-layer reactor (2).

8. The catalytic conversion reactor of claim 7, wherein the reactant flow outlet is one and is disposed in a central region of the catalytic conversion reactor; or more than two reactant flow leading-out pipes are dispersedly arranged along the cross section of the catalytic conversion reactor.

9. The catalytic conversion reactor according to claim 7, wherein the outlet of the reactant stream outlet is partially or completely provided with a cyclone separator (120) rotating in the circumferential direction, each cyclone separator (120) being composed of more than two cyclone tubes (122) uniformly distributed in the circumferential direction and a cyclone separator housing (123); a cyclone separator shell (123) is arranged outside the cyclone tube (122), and a cyclone separator shell gas outlet (125) is arranged at the top of the cyclone separator shell (123); a catalyst outflow port is reserved between the lower edge of the cyclone separator shell (123) and the upper layer reactor (2); an upper reaction zone (212) is formed between the cyclone separator (120) and the upper reactor shell (210).

10. The catalytic conversion reactor according to claim 9, characterized in that the gas-solid separation zone (3) is provided with a first cyclone or a second cyclone directly connected to the gas outlet (125) of the cyclone housing via a duct (126).

11. The catalytic conversion reactor of claim 10, wherein: the lower layer reactor (1) is provided with an independent first-stage cyclone separator or a two-stage cyclone separator, and the upper layer reactor (2) is provided with an independent two-stage cyclone separator; the cyclone separators of the lower reactor (1) and the cyclone separators of the upper reactor (2) are arranged up and down in a staggered way or in parallel; when the lower-layer reactor (1) and the upper-layer reactor (2) are both provided with two stages of cyclone separators, the secondary cyclone separators and the primary cyclone separators of the two stages of cyclone separators are arranged in a vertically staggered manner; when the lower reactor (1) is provided with a primary cyclone, the primary cyclone is arranged below.

12. The catalytic conversion reactor of claim 7, wherein more than two catalyst return conduits are disposed between the upper reaction zone (212) and the lower reaction zone (112), the catalyst return conduits being disposed within or outside the catalytic conversion reactor housing.

13. The catalytic conversion reactor according to claim 7, wherein the gas-solid separation zone (3) is provided with more than two sets of two-stage cyclone separators connected in parallel, and the two-stage cyclone separators are shared by the lower reactor (1) and the upper reactor (2); the outlet of the cyclone separator is connected with a common gas collection chamber and a reactor product gas outlet.

14. The catalytic conversion reactor according to claim 7, wherein when the lower reactor (1) and the upper reactor (2) are provided with separate cyclones in the gas-solid separation zone (3), the gas-solid separation zone housing (310) is provided with a reactor product gas outlet communicated with each separate cyclone.