RU2807509C1 - Fluidized bed regenerator, device for producing low-carbon olefins and their application - Google Patents

Abstract

FIELD: chemical technology.

SUBSTANCE: fluidized bed regenerator for activating a catalyst to produce low carbon olefins from an oxygen-containing compound. The regenerator includes the second activation zone, the first activation zone, and the gas-solid separation zone from bottom to top; wherein the second activation zone in the axial direction communicates with the gas-solid separation zone; the first activation zone is located at the periphery of the connection between the second activation zone and the gas-solid separation zone; the first activation zone is an annular cavity; n partitions are radially installed in the first activation zone, and n partitions divide the first activation zone into n subzones of the first activation zone; and a catalyst circulation port is formed in each of the n-1 partitions so that the catalyst entering the first activation zone flows in an annular direction. The invention also relates to a device and a method for producing low-carbon olefins from an oxygen-containing compound.

EFFECT: controlled activation of spent catalyst conversion into regenerated catalyst, wherein regenerated catalyst is characterized by high activity, high selectivity for low-carbon olefins, etc, and ensures a reduction in specific consumption of methanol and the degree of coking of methanol, as well as an increase in atomic efficiency of methanol to olefins (MTO) process.

10 cl, 2 dwg, 4 ex

Description

TECHNICAL FIELD

The present application relates to a fluidized bed regenerator, a device for producing low carbon olefins and their use and belongs to the field of chemical catalysis.

BACKGROUND OF THE ART

Methanol-to-olefin technology (MTO) mainly includes the DMTO (methanol to olefin) technology of the Dalian Institute of Chemical Physics of the Chinese Academy of Sciences and the MTO technology of UOP from the United States. In 2010, the Shenhua Baotou methanol to olefins plant using DMTO technology was completed and put into operation. This is the world's first industrial application of MTO technology. As of the end of 2019, 14 commercial DMTO plants were operational with a total production capacity of approximately 8 million tons of low-carbon olefins per year.

In recent years, DMTO technology has been further developed and new generation DMTO catalysts with improved performance have gradually been introduced into industry, providing greater benefits to DMTO plants. The new generation DMTO catalyst provides higher methanol throughput and low carbon olefin selectivity.

MTO technologies typically utilize a SAPO-34 molecular sieve catalyst, and high selectivity for low carbon olefins in the MTO process is achieved by combining molecular sieve acid catalysis with pore restriction in the molecular sieve framework. The methanol conversion process is also accompanied by the coking process of an acid catalyst based on a molecular sieve. Existing MTO plants are capable of providing methanol coking rates from 1.5% wt. up to 2.5% wt., i.e. 3.3% to 5.5% of the carbon atoms (C) in methanol are converted to coke on the catalyst and the coke is burned in the regenerator to form CO, CO ₂ , H ₂ O, etc., which are removed, with the degree of utilization of C only from 94.5% to 96.7%. With the advancement of technology, the selectivity for low-carbon olefins in the MTO process has been greatly improved, but the high coking rate of methanol and low carbon utilization have become bottlenecks hindering technology development. Therefore, new MTO technologies need to be developed to improve C utilization and atomic efficiency.

DISCLOSURE OF THE INVENTION

The MTO process is accompanied by a coking process of the molecular sieve acid catalyst so that coke particles are formed in the molecular sieve cells, initiating the MTO catalysis process. Coking of the catalyst causes the closure of some of the active sites of the molecular sieve, resulting in reduced catalyst activity, but the coke in the molecular sieve also restricts the pores in the molecular sieve framework, improving selectivity for low carbon olefins.

Low carbon olefins mentioned in this application refer to ethylene and propylene. Applicants have discovered through research that the main factors affecting DMTO catalyst activity and low carbon olefin selectivity are coke content, distribution of coke content and coke particles in the catalyst. Given the same average coke content in the catalysts, the narrower the distribution of coke content, the higher the selectivity and activity of low-carbon olefins. The coke particles in the catalyst may include polymethylaromatic hydrocarbons, polymethylcycloalkanes, and the like, and polymethylbenzene and polymethylnaphthalene may contribute to the formation of ethylene. Thus, controlling the coke content, distribution of coke content and coke particles in the catalyst is a key factor to control the operating window of the DMTO catalyst and improve selectivity to low carbon olefins.

The coke content of spent MTO catalyst is typically between 7% wt. up to 13 wt.%, and too high a coke content significantly reduces the activity of the catalyst. Currently, MTO plants typically use an air regeneration method to restore catalyst activity, thereby recycling the catalyst; and during this process the coke is burned in a regenerator to produce CO, CO ₂ , H ₂ O and other substances that are removed. Essentially, the coke in spent catalysts can be divided into two categories: coke with high molecular weight, high degree of graphitization and lack of catalytic activity, which can be called inactive coke; and polymethylaromatic hydrocarbons and polymethylcycloalkanes with low molecular weight and catalytic activity, which can be called active cokes. When air is used as the regeneration medium, due to the strong oxidation of air, inactive coke and active coke undergo deep oxidation reaction with oxygen, mainly producing substances such as CO, _CO2 and _H2O , and it is difficult to realize controlled coke conversion and coke content control , distribution of coke content and the formation of coke particles in the catalyst. Thus, when using air as a regeneration medium and when the coke content in the catalyst is <3% wt. sufficient catalytic activity of the catalyst can be restored when most of the coke is oxidized and removed. The regenerated catalyst produced by this regeneration scheme has low selectivity for low-carbon olefins, a high degree of methanol coking and a high specific methanol consumption. When water is used as the regeneration medium, active coke reacts with water, large molecular particles are converted into low molecular weight particles, and under suitable conditions, active coke can be converted into particles mainly consisting of polymethylbenzene and polymethylnaphthalene. When a combination of water and oxygen is used as a regeneration medium, under the influence of oxygen and water, inactive coke and active coke are converted into particles of oxygen-containing hydrocarbons and particles of oxygen-free hydrocarbons with low molecular weight, while the particles of oxygen-containing hydrocarbons do not have catalytic activity. Oxygen-containing hydrocarbon particles can be converted into oxygen-free hydrocarbon particles with catalytic activity by the action of substances such as water vapor, hydrogen, methane, ethane and propane.

Thus, this application proposes a controlled activation method for converting a spent catalyst into a regenerated catalyst, wherein the regenerated catalyst is characterized by high activity, high selectivity for low-carbon olefins, etc., and provides a reduction in the specific consumption of methanol and the degree of coking of methanol, as well as increasing the atomic efficiency of MTO technology.

According to a first aspect of the present application, a fluidized bed regenerator is provided for activating a catalyst for producing low carbon olefins from an oxygen-containing compound.

A fluidized bed regenerator is proposed for activating a catalyst for producing low-carbon olefins from an oxygen-containing compound, including a second activation zone, a first activation zone, and a bottom-up gas-solid separation zone;

wherein the second activation zone in the axial direction communicates with the gas-solid separation zone;

the first activation zone is located at the periphery of the connection between the second activation zone and the gas-solid separation zone;

the first activation zone is an annular cavity;

n partitions are radially installed in the first activation zone, and n partitions divide the first activation zone into n subzones of the first activation zone; And

each of the n-1 partitions is provided with a catalyst circulation hole such that the catalyst entering the first activation zone flows in an annular direction.

If necessary, the n partitions in the first activation zone may include the ^1st partition and from the ^2nd partition to the ^nth partition;

in the ^1st partition there is no hole for catalyst circulation;

in each partition, from ^{the 2nd} partition to the ^nth partition, a hole is formed for the circulation of the catalyst;

an inlet or inlet for the spent catalyst is formed in the ^1st subzone of the first activation zone formed by separation by the ^1st partition and the ^2nd partition;

in the ^nth subzone of the first activation zone, formed by separation using the ^1st partition and the ^nth partition, there is a pipe for supplying the catalyst to the first activation zone;

Below the subzones of the first activation zone there is a distributor of the first activation zone; And

in the upper parts of the subzones of the first activation zone there is a pipe for supplying gas to the first activation zone.

In particular, one or more openings for catalyst circulation may be formed in each of the partitions, which is not strictly limited in the present application. When a plurality of catalyst circulation holes are formed, their relative positions are not strictly limited in the present application. For example, a plurality of catalyst circulation holes may be arranged in parallel or may be arranged randomly.

Preferably, a first activation zone distributor may be provided below each of the subzones of the first activation zone. Thus, all of the raw material of the first activation zone can be uniformly supplied to the subzones of the first activation zone.

Preferably, the upper part of each of the subzones of the first activation zone may be provided with a pipe for supplying gas to the first activation zone.

In particular, the raw material of the first activation zone can be allowed to interact and react with the spent catalyst through the distributor of the first activation zone.

If necessary, a first unit for separating gas and solids of the regenerator may be located in the upper part of the first activation zone; And

the first gas-solid separation unit of the regenerator is configured to communicate with the first activation zone through the spent catalyst inlet.

In particular, the spent catalyst may enter the first activation zone through the first gas-solid separation unit.

Specifically, the first activation zone may be provided with a first activation zone catalyst supply pipe, an inlet of a first activation zone catalyst supply pipe may be connected to the ^nth subzone of the first activation zone, and an outlet of a first activation zone catalyst supply pipe may be formed at second activation zone.

Optionally, the first gas-solid separation unit of the regenerator may be a cyclone gas-solid separator.

If necessary, n can have the following range of values: 2 ≤ n ≤ 10.

If necessary, the cross-section of each of the subzones of the first activation zone can be sector-ring.

If necessary, m perforated plates can be horizontally located in the second activation zone,

where 1 ≤ m ≤ 10.

If necessary, said perforated plates can have a porosity of from 5% to 50%.

In the present application, perforated plates are located in the second activation zone to prevent back-mixing of the catalyst between layers and improve the uniformity of coke distribution in the catalyst.

If necessary, the distributor of the second activation zone can be located in the lower part of the second activation zone.

Optionally, the fluidized bed regenerator may include a regenerator gas collection chamber and a fluidized bed regenerator cooler;

a regenerator gas collection chamber may be located at the top of the fluidized bed regenerator;

an upper portion of the regenerator gas collection chamber may be provided with a pipe for supplying the regenerator product gas;

the gas-solid separation zone may be provided with a second gas-solid separation unit;

a gas collection chamber of the regenerator may be connected to an outlet of the second unit for separating gas and solid; And

a fluidized bed regenerator cooler may be located at the bottom of the second activation zone.

In particular, the inner diameter of the connection between the second activation zone and the gas-solid separation zone can gradually increase.

In particular, the inner diameter of the connection between the lower shell and the upper shell of the fluidized bed regenerator can be gradually increased.

If desired, the second gas-solid separation unit of the regenerator may have one or more sets of cyclone separators for gas-solid separation.

Preferably, each set of gas-solid separation cyclones may include a first stage gas-solid separation cyclone separator and a second stage gas-solid separation cyclone separator.

In a preferred embodiment, the fluidized bed regenerator may be divided from bottom to top into a second activation zone, a first activation zone, and a gas-solid separation zone;

The fluidized bed regenerator may include a regenerator shell, a first unit for separating gas and solids of the regenerator, a first activation zone distributor, a baffle, a first activation zone catalyst supply pipe, a first activation zone gas supply pipe, a second activation zone distributor, a perforated plate, a fluidized bed regenerator cooler, a second regenerator gas/solid separation unit, a regenerator gas collection chamber, a regenerator product gas supply pipe, a regenerated catalyst slant pipe, a regenerated catalyst sliding or spool valve, and a feed pipe regenerated catalyst;

the first activation zone may be located in an annular zone above the second activation zone, n partitions may be located in the first activation zone and these partitions may divide the first activation zone into n subzones of the first activation zone, where 2 ≤ n ≤ 10; the lower part of each of the subzones of the first activation zone can be independently provided with a distributor of the first activation zone; the cross-section of the first activation zone can be circular, and the cross-section of each of the subzones of the first activation zone can be sector-ring; from the ^1st to the ^nth subzones of the first activation zone can be located sequentially and concentrically; a catalyst circulation hole may be formed in the partitions, but there may be no catalyst circulation hole in the partition between the ^1st subzone of the first activation zone and the ^nth subzone of the first activation zone;

a first gas-solid separation unit of the regenerator may be located in a gas-solid separation zone of the fluidized bed regenerator; an inlet of the first gas-solid separation unit of the regenerator may be connected to an outlet of a spent catalyst supply pipe, a gas outlet of the first gas-solid separation unit of the regenerator may be formed in a gas-solid separation zone, and an outlet a catalyst hole from the first unit for separating gas and solids of the regenerator may be formed in the ^1st subzone of the first activation zone;

an inlet of the catalyst supply pipe of the first activation zone may be connected to the n ^th subzone of the first activation zone, and an outlet of the catalyst supply pipe of the first activation zone may be formed in the second activation zone; an upper portion of each of the sub-zones of the first activation zone may be independently provided with a gas supply pipe of the first activation zone, and an outlet of the gas supply pipe of the first activation zone may be formed in a gas-solid separation zone;

a second activation zone distributor may be located at the bottom of a second activation zone of the fluidized bed regenerator, and m perforated plates may be located in the second activation zone, where 1 ≤ m ≤ 10; a fluidized bed regenerator cooler may be located in the second activation zone;

a second regenerator gas-solid separation unit and a regenerator gas collection chamber may be located in a gas-solid separation zone of the fluidized bed regenerator; an inlet port of the second gas-solid separation unit of the regenerator may be formed in a gas-solid separation zone of the fluidized bed regenerator, a gas outlet from the second gas-solid separation unit of the regenerator may be connected to a gas collection chamber of the regenerator, and a catalyst outlet from the second gas-solid separation unit of the regenerator may be formed in the second activation zone; a regenerator product gas supply pipe may be connected to an upper portion of the regenerator gas collection chamber;

a slant pipe inlet for the regenerated catalyst may be connected to the bottom of the second activation zone; and the inlet of the regenerated catalyst slide valve may be connected to the outlet of the regenerated catalyst inclined pipe, the outlet of the regenerated catalyst slide valve may be connected by a pipeline to the inlet of the regenerated catalyst supply pipe, and the outlet of the regenerated catalyst supply pipe may be connected to the reaction zone of the fluidized bed reactor.

According to a second aspect of the present application, a device is provided for producing low-carbon olefins from an oxygen-containing compound. This device is a DMTO device including a fluidized bed reactor and a fluidized bed regenerator.

A device is proposed for producing low-carbon olefins from an oxygen-containing compound, including a fluidized bed reactor and a fluidized bed regenerator described above.

Optionally, the apparatus may include a spent catalyst slant pipe, a stripper or stripper, a fluidized bed reactor, a spent catalyst supply pipe, a regenerated catalyst slant pipe, and a regenerated catalyst supply pipe;

the spent catalyst zone, the spent catalyst inclined pipe, the stripper or stripper of the fluidized bed reactor, the spent catalyst supply pipe, and the first gas-solid separation unit of the regenerator are configured to communicate in series with each other; And

the second activation zone, the regenerated catalyst inclined pipe, the regenerated catalyst supply pipe, and the reaction zone of the fluidized bed reactor are configured to communicate with each other in series.

Specifically, the spent catalyst inclined pipe, the fluidized bed reactor stripper, and the spent catalyst supply pipe can be connected in series with each other;

the regenerated catalyst inclined pipe and the regenerated catalyst supply pipe can be connected in series with each other;

a slant pipe inlet for the regenerated catalyst may be connected to the bottom of the second activation zone;

the spent catalyst that has been reacted in the fluidized bed reactor can be supplied to the spent catalyst inclined pipe, and then supplied to the fluidized bed regenerator through the spent catalyst supply pipe; And

the regenerated catalyst obtained from the fluidized bed regenerator may be supplied to the regenerated catalyst slant pipe, and then supplied to the fluidized bed reactor through the regenerated catalyst supply pipe.

If necessary, the fluidized bed reactor stripper and the spent catalyst supply pipe can be connected to each other by means of a spent catalyst slide valve.

If necessary, the regenerated catalyst slant pipe and the regenerated catalyst supply pipe can be connected to each other by means of a regenerated catalyst slide valve.

Optionally, the fluidized bed reactor may include a lower shell, a feed pipe and an upper shell;

the lower shell may enclose the reaction zone;

the supply pipe may be located above the reaction zone and configured to communicate with the reaction zone;

the upper shell may be located at the periphery of the supply pipe;

the upper shell and the supply pipe may form a cavity; And

said cavity can be divided from bottom to top into a spent catalyst zone and a gas-solid separation zone;

In particular, the inner diameter of the connection between the reaction zone of the fluidized bed reactor and the feed pipe can be gradually reduced.

In particular, the inner diameter of the connection between the lower shell and the upper shell of the fluidized bed reactor can be gradually increased.

If necessary, the reaction zone can be a rapid fluidization zone.

If necessary, the spent catalyst zone may be a bubbling fluidization zone.

In the present application, the type of fluidization in the reaction zone is not strictly limited, and preferably the reaction zone may be a fast fluidization zone. In the reaction zone, the apparent linear gas velocity can reach 7.0 m/s, the methanol flow is strong, the methanol processing capacity per unit volume of the device is large, and the weight hourly space velocity (WHSV) of methanol can reach 20 h ^-1 . In the present application, the type of fluidization in the spent catalyst zone is not strictly limited, and preferably the spent catalyst zone may be a bubbling fluidization zone. The spent catalyst zone may be configured to reduce the temperature of the spent catalyst, supply low-temperature spent catalyst to the reaction zone, increase the density of the bed in the reaction zone, and control the temperature of the bed in the reaction zone. When the apparent linear gas velocity is from 0.5 m/s to 7.0 m/s, the corresponding layer density is from 500 kg/m ³ to 100 kg/m ³ .

If necessary, the gas-solid separation zone may be provided with a first gas-solid separation unit of the fluidized bed reactor; And

the upper portion of the supply pipe may be connected to the inlet of the first unit for separating the gas and solid of the fluidized bed reactor.

Optionally, the fluidized bed reactor may include a fluidized bed reactor distributor, a fluidized bed reactor cooler, a spent catalyst zone gas distributor, a fluidized bed reactor gas collection chamber, and a second fluidized bed reactor gas-solid separation unit;

a fluidized bed reactor distributor may be located at the bottom of the reaction zone;

a fluidized bed reactor cooler may be located at the bottom of the spent catalyst zone;

the spent catalyst zone gas distributor may be located in the lower part of the spent catalyst zone;

gas outlets from the second gas-solid separation unit of the fluidized bed reactor and the first gas-solid separation unit of the fluidized bed reactor may be connected to a gas collection chamber of the fluidized bed reactor;

the gas collection chamber of the fluidized bed reactor may be provided with a product gas supply pipe; And

catalyst outlets from the first gas-solid separation unit of the fluidized bed reactor and the second gas-solid separation unit of the fluidized bed reactor may be connected to a spent catalyst zone.

In particular, the oxygen-containing compound raw material can contact and react with the regenerated catalyst through the distributor of the fluidized bed reactor.

In particular, the spent catalyst zone fluidizing gas may contact the spent catalyst through a spent catalyst zone gas distributor.

If necessary, the reaction zone and the spent catalyst zone are configured to communicate with each other through a pipe for circulating the spent catalyst.

Specifically, the inlet of the spent catalyst circulation pipe may be connected to the spent catalyst area; And

the outlet of the spent catalyst circulation pipe may be connected to the bottom of the reaction zone.

If necessary, the spent catalyst circulation pipe may be provided with a spool valve for circulating the spent catalyst.

Optionally, the first gas-solid separation unit of the fluidized bed reactor may have one or more sets of cyclone separators for gas-solid separation.

Preferably, each set of gas-solid separation cyclones may include a first stage gas-solid separation cyclone separator and a second stage gas-solid separation cyclone separator.

If desired, the second gas-solid separation unit of the fluidized bed reactor may have one or more sets of cyclone separators for gas-solid separation.

Preferably, each set of gas-solid separation cyclones may include a first stage gas-solid separation cyclone separator and a second stage gas-solid separation cyclone separator.

In a preferred embodiment, the fluidized bed reactor may include a fluidized bed reactor shell, a fluidized bed reactor distributor, a supply pipe, a first fluidized bed reactor gas-solid separation unit, a fluidized bed reactor gas collection chamber, spent catalyst zone gas distributor, fluidized bed reactor cooler, second fluidized bed reactor gas-solid separation unit, product gas supply pipe, spent catalyst circulation pipe, spent catalyst circulation spool valve, spent catalyst inclined pipe, stripper a fluidized bed reactor device, a spent catalyst slide valve and a spent catalyst supply pipe;

the bottom portion of the fluidized bed reactor may be a reaction zone, the middle portion thereof may be a spent catalyst zone, and the top portion thereof may be a gas-solid separation zone;

a fluidized bed reactor distributor may be located at the bottom of the reaction zone of the fluidized bed reactor, a feed pipe may be located in the central zones of the middle and top portions of the fluidized bed reactor, and the lower end of the feed pipe may be connected to the upper end of the reaction zone ; the upper part of the supply pipe may be connected to the inlet of the first gas-solid separation unit of the fluidized bed reactor, and the first gas-solid separation unit of the fluidized bed reactor may be located in the gas-solid separation zone of the fluidized bed reactor layer; a gas outlet from the first gas-solid separation unit of the fluidized bed reactor may be connected to a gas collection chamber of the fluidized bed reactor, and a catalyst outlet from the first gas-solid separation unit of the fluidized bed reactor may be formed in the spent catalyst zone; a spent catalyst zone gas distributor may be located at the bottom of the spent catalyst zone, and a fluidized bed reactor cooler may be located in the spent catalyst zone; a second gas-solid separation unit of the fluidized bed reactor may be located in a gas-solid separation zone of the fluidized bed reactor, an inlet of the second gas-solid separation unit of the fluidized bed reactor may be formed in a gas-solid separation zone of the fluidized bed reactor. substances of the fluidized bed reactor, the gas outlet from the second unit for gas-solid separation of the fluidized bed reactor may be connected to the gas collection chamber of the fluidized bed reactor, and the catalyst outlet from the second unit for gas-solid separation a fluidized bed reactor may be formed in the spent catalyst zone; a gas collecting chamber of the fluidized bed reactor may be located in an upper part of the fluidized bed reactor, and a product gas supply pipe may be connected to an upper part of the gas collecting chamber of the fluidized bed reactor; an inlet of the spent catalyst circulation pipe may be connected to a spent catalyst zone, and an outlet of the spent catalyst circulation pipe may be connected to a lower part of a reaction zone of the fluidized bed reactor; The spent catalyst circulation slide valve may be located in the spent catalyst circulation pipe, the spent catalyst slant pipe inlet may be connected to the spent catalyst area, and the spent catalyst slant pipe outlet may be connected to the upper portion of the stripping unit of the fluidized reactor. layer; a stripping device of the fluidized bed reactor may be located outside the shell of the fluidized bed reactor; and the inlet of the spent catalyst slide valve may be connected by a pipeline to the bottom of the stripper of the fluidized bed reactor, the outlet of the spent catalyst slide valve may be connected by a pipeline to the inlet of the spent catalyst supply pipe, and the outlet of the spent catalyst supply pipe can be connected to a fluidized bed regenerator.

According to a third aspect of the present application, a method is provided for activating a catalyst to produce low carbon olefins from an oxygen-containing compound.

A method is proposed for activating a catalyst for the production of low-carbon olefins from an oxygen-containing compound, according to which the fluidized bed regenerator described above is used.

If necessary, the method may include:

supplying the raw material of the first activation zone and the spent catalyst to the first activation zone, in which the spent catalyst chemically reacts with the raw material of the first activation zone, flowing in an annular direction along the subzones of the first activation zone, to form a partially activated catalyst; And

supplying the partially activated catalyst and the raw material of the second activation zone to the second activation zone and conducting a chemical reaction to obtain a regenerated catalyst;

wherein the coke composition in the partially activated catalyst includes particles of oxygen-containing hydrocarbons and particles of oxygen-free hydrocarbons.

If necessary, the first activation zone feedstock may be supplied to the first activation zone through a first activation zone distributor to react with the coke in the catalyst.

If necessary, the second activation zone feedstock may be supplied to the second activation zone through a second activation zone distributor to react with the coke in the catalyst.

Specifically, while the spent catalyst flows in an annular direction along the catalyst circulation holes formed in the baffles, the raw material of the first activation zone enters the subzone of the first activation zone from the distributor of the first activation zone located below and contacts the spent catalyst so that the inactive coke and active coke in the spent catalyst are converted into particles of oxygen-containing hydrocarbons and particles of oxygen-free hydrocarbons with low molecular weight; and the gas phase (including the unreacted raw material of the first activation zone) is supplied to the gas-solid separation zone through a pipe for supplying gas to the first activation zone above the first activation zone.

Specifically, the catalyst enters the second activation zone through a pipe for supplying catalyst to the first activation zone, and the raw material of the second activation zone enters the second activation zone through a distributor of the second activation zone located below to interact with the catalyst, so that the catalytically inactive oxygen-containing hydrocarbon particles in the catalyst coke is converted into particles of catalytically active oxygen-free hydrocarbon; and the gas phase (including the unreacted raw material of the second activation zone) enters the gas-solid separation zone.

If necessary, the coke in the spent catalyst can react chemically with the feed material of the first activation zone to form a gaseous product of the first activation zone.

If necessary, the coke in the partially activated catalyst can react chemically with the feedstock of the second activation zone to form a gaseous product of the second activation zone.

If necessary, the gaseous product of the first activation zone and the gaseous product of the second activation zone can be mixed in the gas-solid separation zone to produce a gaseous product of the regenerator.

If necessary, the regenerator product gas containing the catalyst may be supplied to a second regenerator gas-solid separation unit to effect gas-solid separation to obtain a regenerator product gas and catalyst;

the regenerator product gas may be supplied to the regenerator gas collecting chamber; And

the catalyst may be returned to the second activation zone of the fluidized bed regenerator.

If desired, the regenerator product gas may include CO, H ₂ and CO ₂ ; And

the CO and H ₂ content may exceed 90 wt%.

If necessary, the raw material of the first activation zone may include oxygen, air and water vapor;

the mass fraction of oxygen can range from 0% wt. to 10% wt.;

the mass fraction of air can range from 0% wt. to 20% wt.;

the mass fraction of water vapor ranges from 80% wt. to 100% wt..

If desired, the raw material of the second activation zone may include water vapor.

If necessary, the coke content in the spent catalyst can be from 9% wt. up to 13% wt.

Preferably, the coke content in the spent catalyst can range from 10 wt%. up to 12% wt.

If necessary, the coke content in the regenerated catalyst can be from 5% wt. up to 11% wt.; And

the quartile deviation of the coke content distribution in the regenerated catalyst may be less than 1.0 wt%.

If desired, the coke particles in the regenerated catalyst may include polymethylbenzene and polymethylnaphthalene;

the total mass of polymethylbenzene and polymethylnaphthalene may be more than 60% by weight of the total mass of coke or may be equal to the specified amount;

the mass of coke particles with a molecular weight greater than 184 may be less than 30% by weight. from the total mass of coke or may be equal to the specified amount; A

total coke mass may refer to the total mass of coke particles.

In this application, the types and content of coke particles are very important; and the coke content and coke content distribution of the catalyst are controlled by controlling the average residence time and residence time distribution of the catalyst in the first activation zone and in the second activation zone to ensure a mass fraction of polymethylbenzene and polymethylnaphthalene in the total mass of coke that is greater than or equal to 60 wt%. , thereby increasing catalyst activity and selectivity for low-carbon olefins.

If desired, the spent catalyst may include a SAPO-34 molecular sieve.

In the present application, the catalyst active component may be a SAPO-34 molecular sieve.

If necessary, the operating conditions for the process in the first activation zone of the fluidized bed regenerator can be as follows: apparent linear gas velocity: from 0.1 m/s to 0.5 m/s; temperature: from 650°C to 750°C; pressure: from 100 kPa to 500 kPa; and layer density: from 400 kg/ ^m3 to 700 kg/ ^m3 .

If necessary, the operating conditions for the process in the second activation zone of the fluidized bed regenerator can be as follows: apparent linear gas velocity: from 0.1 m/s to 0.5 m/s; temperature: from 550°C to 700°C; pressure: from 100 kPa to 500 kPa; and layer density: from 400 kg/ ^m3 to 700 kg/ ^m3 .

The first activation zone of the fluidized bed regenerator in the present application includes n subzones of the first activation zone and the catalyst can only flow from the upstream subzone to the downstream subzone through catalyst circulation holes in the baffles in the first activation zone, which provides the following: Benefits: 1. The operating conditions of the process can be changed to control the average residence time of the catalyst in the first activation zone and thus control the coke content of the catalyst. 2. The structure of n subzones of the first activation zone is used to control the residence time distribution of the catalyst (residence time distribution is similar to the use of n series tank tank reactors with complete mixing) and thus a regenerated catalyst with a narrow coke content distribution can be obtained.

Since the catalyst in the present application is a powder, the coke content of the catalyst refers to the average coke content of the catalyst granules, but the actual coke content of different catalyst granules may be different. In the present application, the quartile deviation of the distribution of coke content in the regenerated catalyst can be controlled so that it is less than 1.0% by weight. to narrow the overall distribution of coke content in the catalyst and thus increase catalyst activity and selectivity for low carbon olefins.

In the fluidized bed regenerator according to the present application, the catalyst activation process includes two steps: S1. water vapor and oxygen are used as an activating gas to convert inactive coke and active coke in the spent catalyst into oxygen-containing hydrocarbon particles and low molecular weight oxygen-free hydrocarbon particles, wherein the oxygen-containing hydrocarbon particles do not exhibit catalytic activity and step S1 is carried out in the first activation zone; and S2. water vapor is used as an activating gas to convert particles of catalytically inactive oxygen-containing hydrocarbon in the coke into particles of catalytically active oxygen-free hydrocarbon and further reduce the molecular weight of the coke, i.e. the coke in the catalyst is converted into particles mainly consisting of polymethylbenzene and polymethylnaphthalene, with S2 carried out in the second activation zone. In step S1, the activating gas used can decompose inactive coke due to strong oxidizability, but this results in the formation of particles of some catalytically inactive oxygen-containing hydrocarbons; and in step S2, the non-oxidizable activating gas is used to further convert the catalytically inactive oxygen-containing hydrocarbon particles into catalytically active oxygen-free hydrocarbon particles. After two-step activation, the coke particles in the regenerated catalyst are mainly polymethylbenzene and polymethylnaphthalene with high ethylene selectivity.

In the fluidized bed regenerator of the present application, the catalyst regeneration process is a combination of an exothermic reaction and an endothermic reaction, wherein the raw material of the first activation zone and the coke in the catalyst react in the first activation zone to produce substances such as CO and H ₂ and generate heat leads to an increase in the temperature of the layer; and the raw material of the second activation zone and the coke in the catalyst react in the second activation zone to produce substances such as CO and H ₂ , and this reaction is an endothermic reaction, and the heat required for this reaction is provided by the exothermic reaction carried out in the first activation zone .

In a preferred embodiment, the first activation zone feedstock may be supplied to the first activation zone of the fluidized bed regenerator from a first activation zone distributor; the spent catalyst can be supplied to the first gas-solid separation unit of the regenerator from the spent catalyst supply pipe to perform gas-solid separation, the resulting gas can be discharged to the gas-solid separation zone of the fluidized bed regenerator through the gas outlet from a first gas-solid separation unit of the regenerator, and the resulting spent catalyst may be discharged to the first activation zone of the fluidized bed regenerator through a catalyst outlet from the first gas-solid separation unit of the regenerator; the raw material of the first activation zone can contact and react chemically with the spent catalyst in the first activation zone, so that the inactive coke and active coke in the spent catalyst are converted into oxygen-containing hydrocarbon particles and oxygen-free hydrocarbon particles of small molecular weight, and a gaseous product of the first zone is generated activation; the catalyst in the first activation zone may sequentially pass through subzones 1 ^{to n} of the first activation zone through the catalyst circulation holes in the partitions, and then enter the second activation zone of the fluidized bed regenerator through the catalyst supply pipe of the first activation zone; a gaseous product of the first activation zone may be supplied to a gas-solid separation zone of the fluidized bed regenerator through a gas supply pipe of the first activation zone; the feedstock of the second activation zone may be supplied to the second activation zone of the fluidized bed regenerator from the distributor of the second activation zone to react and react chemically with the catalyst from the first activation zone so that the catalytically inactive oxygen-containing hydrocarbon particles in the coke are converted into catalytically active oxygen-free hydrocarbon particles , the molecular weight of the coke is further reduced (i.e., the coke in the catalyst is converted into particles mainly consisting of polymethylbenzene and polymethylnaphthalene; and the catalyst removed from the second activation zone is called regenerated catalyst), and the feedstock of the second activation zone is converted into a gaseous product the second activation zone in the second activation zone, and then enters the gas-solid separation zone of the fluidized bed regenerator; the gaseous product of the first activation zone and the gaseous product of the second activation zone may be mixed in the gas-solid separation zone to obtain a gaseous product of the regenerator, and the gaseous product of the regenerator may contain a catalyst and enter the second gas-solid separation unit of the regenerator to effect gas separation and a solid to produce a gaseous product of regenerator and catalyst; the regenerator product gas may be supplied to a regenerator gas collection chamber and then supplied to a downstream system for recirculating the regenerator product gas through a regenerator product gas supply pipe, and the catalyst may be returned to a second activation zone of the fluidized bed regenerator; the regenerated catalyst in the second activation zone can be cooled and then enters the fluidized bed reactor through the regenerated catalyst slant pipe, through the regenerated catalyst slide valve and the regenerated catalyst supply pipe.

In this application, the main components of the gaseous product of the regenerator are CO, H ₂ and a small amount of CO ₂ , while the total content of CO and H ₂ is more than 90% by weight, and the content of CO ₂ is less than 10% by weight (dry basis, for minus unreacted H ₂ O); after simply separating the regenerator product gas, a mixture of CO and H ₂ gases can be obtained, and the mixture of CO and H ₂ gases can be recycled as a raw material to produce methanol; and thus, in the technical solution according to the present application, coke obtained from methanol is an intermediate product of this process, and the degree of utilization of C atoms in the entire process is greater than or equal to 99%.

According to a fourth aspect of the present application, a method for producing low-carbon olefins from an oxygen-containing compound is provided.

A method is proposed for producing low-carbon olefins from an oxygen-containing compound, according to which the device described above is used.

If necessary, the method may include:

supplying a raw material with an oxygen-containing compound and a regenerated catalyst to a reaction zone and reacting to produce a stream A with low carbon olefins and spent catalyst;

performing separation of stream A into gas and solid, and transferring spent catalyst to a spent catalyst zone; And

returning a portion of the spent catalyst from the spent catalyst zone to the fluidized bed reaction zone and causing the remainder of the spent catalyst to enter the fluidized bed regenerator.

Specifically, a portion of the spent catalyst from the spent catalyst zone is returned to the fluidized bed reaction zone through the spent catalyst circulation pipe, and the remaining spent catalyst enters the fluidized bed regenerator through the spent catalyst slant pipe, through the fluidized bed reactor stripper, and through a pipe for supplying spent catalyst.

If necessary, the regenerated catalyst regenerated from the spent catalyst by the fluidized bed regenerator can be supplied to the reaction zone of the fluidized bed reactor through a regenerated catalyst supply pipe.

Optionally, while the regenerated catalyst enters the reaction zone of the fluidized bed reactor, the oxygen-containing compound feedstock can be supplied to the reaction zone of the fluidized bed reactor through a distributor of the fluidized bed reactor to react to produce stream A with low carbon olefins and spent catalyst .

If necessary, Stream A with the low carbon olefins and spent catalyst may be supplied to the first gas-solid separation unit of the fluidized bed reactor through a supply pipe to perform gas-solid separation to produce a gas containing the low carbon olefin and spent catalyst.

If necessary, low carbon gas containing olefin can be supplied to the gas collection chamber of the fluidized bed reactor.

If necessary, the spent catalyst can be stripped and then fed into a fluidized bed regenerator.

Optionally, the fluidizing gas from the spent catalyst zone may be at least one of nitrogen and steam.

Optionally, the oxygen-containing compound raw material may be at least one of the group consisting of methanol and dimethyl ether (DME).

If necessary, the ratio of the mass flow rate of the regenerated catalyst to the supplied amount of oxygen-containing compound (ratio of catalyst to alcohol) can be from 0.3 to 1.0 t of catalyst per 1 t of methanol.

Preferably, the ratio of catalyst to alcohol may be from 0.5 to 1.0 tons of catalyst per 1 ton of methanol.

If necessary, the operating conditions for the process in the reaction zone of a fluidized bed reactor can be as follows: apparent linear gas velocity: from 0.5 m/s to 7.0 m/s; reaction temperature: from 350°C to 550°C; reaction pressure: from 100 kPa to 500 kPa; and layer density: from 100 kg/ ^m3 to 500 kg/ ^m3 .

If necessary, the operating conditions for the process in the spent catalyst zone of the fluidized bed reactor can be as follows: apparent linear gas velocity: from 0.1 m/s to 1.0 m/s; reaction temperature: from 350°C to 550°C; reaction pressure: from 100 kPa to 500 kPa; and layer density: from 200 kg/ ^m3 to 800 kg/ ^m3 .

If necessary, the oxygen-containing feedstock may be reacted with the regenerated catalyst in the reaction zone of the fluidized bed reactor to produce a stream A with low carbon olefins and spent catalyst, wherein stream A may be supplied to the first gas-solid separation unit of the fluidized bed reactor at a supply pipe for performing gas-solid separation to obtain a gas-phase stream B and a solid-phase stream C; solid phase stream C may enter the spent catalyst zone, and fluidizing gas from the spent catalyst zone and solid phase stream C may form stream D; and stream D may be supplied to a second gas-solid separation unit of the fluidized bed reactor to perform gas-solid separation to obtain gas-phase stream E and solid-phase stream F; the solid phase stream F can be returned to the spent catalyst zone, and the spent catalyst in the spent catalyst zone can be stripped and then fed to the fluidized bed regenerator; and the regenerated catalyst regenerated by the fluidized bed regenerator can be supplied to the reaction zone of the fluidized bed reactor through a regenerated catalyst supply pipe.

If necessary, a portion of the spent catalyst located in the spent catalyst zone can be returned to the lower portion of the reaction zone of the fluidized bed reactor through the spent catalyst circulation pipe.

Optionally, solid phase stream C and solid phase stream F may each include spent catalyst.

If necessary, gas-phase stream B and gas-phase stream E can be mixed in a gas collection chamber of the fluidized bed reactor to produce a gaseous product, and

gas phase stream B may include low carbon olefins.

In this application, the reaction zone is a rapid fluidization zone in which an apparent linear gas velocity of 7.0 m/s, a relatively intense methanol flow, a large methanol processing capacity per unit volume of the device and a weight hourly space velocity can be achieved. , WHSV) methanol 20 h ^-1 ; and the spent catalyst zone is a bubbling fluidization zone, which is configured to reduce the temperature of the spent catalyst, supply low-temperature spent catalyst to the reaction zone, increase the density of the bed in the reaction zone, and control the temperature of the bed in the reaction zone. When the apparent linear gas velocity is from 0.5 m/s to 7.0 m/s, the corresponding layer density is from 500 kg/m ³ to 100 kg/m ³ .

In the present application, the structure in which the first gas-solid separation unit of the fluidized bed reactor is directly connected to the feed pipe ensures rapid separation of the low carbon olefin containing gas and the spent catalyst in stream A and prevents the low carbon olefins from further reacting under the influence of the spent catalyst. catalyst to form high molecular weight hydrocarbon by-products.

In a preferred embodiment, the oxygenate feedstock may be supplied from the fluidized bed reactor distributor to the fluidized bed reactor reaction zone, where it is reacted with regenerated catalyst from the regenerated catalyst supply pipe to produce a stream A with low carbon olefins and spent catalyst; Stream A may be supplied to the first gas-solid separation unit of the fluidized bed reactor through a feed pipe to perform gas-solid separation to produce gas-phase stream B and solid-phase stream C, wherein gas-phase stream B is a low-carbon olefin gas and solid phase stream C represents spent catalyst; gas-phase stream B may be supplied to a gas collection chamber of the fluidized bed reactor, and solid-phase stream C may be supplied to a spent catalyst zone; the fluidizing gas from the spent catalyst zone can be supplied from the gas distributor of the spent catalyst zone to the spent catalyst zone where it interacts with the spent catalyst, and the fluidizing gas from the spent catalyst zone and the spent catalyst carried by it can form a stream D; Stream D may be supplied to a second gas-solid separation unit of the fluidized bed reactor to perform gas-solid separation to produce gas-phase stream E and solid-phase stream F, wherein gas-phase stream E is fluidizing gas from the spent catalyst zone and solid-phase stream stream F represents spent catalyst; the gas-phase stream E may be supplied to the gas collection chamber of the fluidized bed reactor, and the solid-phase stream F may be returned to the spent catalyst zone; gas-phase stream B and gas-phase stream E may be mixed in a gas collecting chamber of the fluidized bed reactor to obtain a gaseous product, and the gaseous product may be supplied to a downstream operating section through a gaseous product supply pipe; a portion of the spent catalyst located in the spent catalyst zone may be returned to the bottom of the reaction zone of the fluidized bed reactor through the spent catalyst circulation pipe and through the spent catalyst circulation spool valve, and the remainder of the spent catalyst may be supplied to the stripper of the fluidized bed reactor. layer through the spent catalyst slant pipe to perform its stripping, and then enters the fluidized bed regenerator through the spent catalyst spool valve and through the spent catalyst supply pipe; and the regenerated catalyst regenerated by the fluidized bed regenerator can be supplied to the fluidized bed reactor through the regenerated catalyst slant pipe, through the regenerated catalyst slide valve and the regenerated catalyst supply pipe.

As used herein, the term “catalyst to alcohol ratio” refers to the ratio of the mass flow rate of regenerated catalyst to the amount of oxygenate compound supplied. When the ratio of catalyst to alcohol is expressed herein, the mass of dimethyl ether in the oxygen-containing compound is equivalently converted to the mass of methanol according to the mass of element C.

According to the method in the present application, the gaseous product may consist of ethylene in an amount from 38 wt.% to 55 wt.%, propylene in an amount from 37 wt.%. up to 54% by weight, C ₄ -C ₆ hydrocarbon compounds in an amount of 6% by weight or less and other components in an amount of 3% by weight or less; in this case, other components can be methane, ethane, propane, hydrogen, CO, CO ₂ , etc., and the overall selectivity for ethylene and propylene in the gaseous product can be from 92% wt. up to 97% wt.

In this application, when expressing the specific production rate, the mass of dimethyl ether in the oxygen-containing compound is equivalently converted to the mass of methanol per mass of element C, and the unit of specific production rate is ton of methanol per ton of low carbon olefins.

In the method according to this application, the specific production consumption can be from 2.4 to 2.5 tons of methanol per 1 ton of low-carbon olefins.

Possible beneficial effects of this application:

(1) The coke particles in the regenerated catalyst are mainly polymethylbenzene and polymethylnaphthalene with high ethylene selectivity.

(2) The coke content and coke content distribution of the catalyst are controlled by controlling the average residence time and residence time distribution of the catalyst in the first activation zone and the second activation zone.

(3) Perforated plates are used to prevent back-mixing of the catalyst between layers and improve the uniformity of coke distribution in the catalyst.

(4) The coke in the spent catalyst is converted to CO and H ₂ , and the spent catalyst is activated; CO and _H2 can be recycled as raw material to produce methanol, in other words, coke produced from methanol is an intermediate product of this process; and the degree of utilization of C atoms in the entire process is greater than or equal to 99%.

BRIEF DESCRIPTION OF THE DRAWINGS

FIG. 1 is a schematic illustration of a DMTO apparatus for producing low carbon olefins from an oxygen-containing compound according to an embodiment of the present application.

FIG. 2 is a schematic cross-sectional view of the first activation zone of FIG. 1.

Reference symbols in Fig.1 and Fig.2:

1 is a fluidized bed reactor; 1-1 is a fluidized bed reactor shell; 1-2 is a fluidized bed reactor distributor; 1-3 represents a supply pipe; 1-4 represents a first gas-solid separation unit of a fluidized bed reactor; 1-5 is a gas collection chamber of a fluidized bed reactor; 1-6 represents a spent catalyst zone gas distributor; 1-7 is a fluidized bed reactor cooler; 1-8 represents a second gas-solid separation unit of the fluidized bed reactor; 1-9 represents a pipe for supplying a gaseous product; 1-10 represents a spent catalyst circulation pipe; 1-11 is a spool valve for circulating spent catalyst; 1-12 is an inclined pipe for spent catalyst; 1-13 is a stripping device of a fluidized bed reactor; 1-14 is a spool valve for spent catalyst; 1-15 is a spent catalyst supply pipe;

2 is a fluidized bed regenerator; 2-1 represents the regenerator shell; 2-2 represents a first gas-solid separation unit of the regenerator; 2-3 represents a first activation zone distributor; 2-4 represents the septum; 2-5 represents a catalyst supply pipe for the first activation zone; 2-6 represents a gas supply pipe for the first activation zone; 2-7 represents a second activation zone distributor; 2-8 is a perforated plate; 2-9 is a fluidized bed regenerator cooler; 2-10 represents a second gas-solid separation unit of the regenerator; 2-11 represents a chamber for collecting regenerator gas; 2-12 represents a pipe for supplying a gaseous product of the regenerator; 2-13 is an inclined pipe for regenerated catalyst; 2-14 is a spool valve for regenerated catalyst; and 2-15 is a regenerated catalyst supply pipe.

IMPLEMENTATION OF THE INVENTION

The present invention will be described in detail below with reference to examples, but the present invention is not limited to these examples.

Unless otherwise indicated, all raw materials and catalysts in the examples of this application were purchased from commercial sources.

As an embodiment of the present application, FIG. 1 and FIG. 2 show a schematic diagram of a DMTO device that includes a fluidized bed reactor (1) and a fluidized bed regenerator (2). In particular:

As shown in Fig. 1, the fluidized bed reactor (1) includes a fluidized bed reactor shell (1-1), a fluidized bed reactor distributor (1-2), a supply pipe (1-3), a first unit (1-4) for gas-solid separation of the fluidized bed reactor, chamber (1-5) for collecting gas of the fluidized bed reactor, gas distributor (1-6) of the spent catalyst zone, cooler (1-7) of the fluidized bed reactor , second block (1-8) for gas-solid separation of the fluidized bed reactor, pipe (1-9) for supplying gaseous product, pipe (1-10) for circulation of spent catalyst, spool valve (1-11) for circulation a spent catalyst, a spent catalyst slant pipe (1-12), a fluidized bed reactor stripper (1-13), a spent catalyst slide valve (1-14), and a spent catalyst supply pipe (1-15); wherein the lower part of the fluidized bed reactor (1) represents a reaction zone, its middle part represents a spent catalyst zone, and its upper part represents a gas-solid separation zone; the distributor (1-2) of the fluidized bed reactor is located in the lower part of the reaction zone of the fluidized bed reactor (1), the supply pipe (1-3) is located in the central zones of the middle and upper parts of the fluidized bed reactor (1), and the lower the end of the supply pipe (1-3) is connected to the upper end of the reaction zone; the upper part of the supply pipe (1-3) is connected to the inlet of the first unit (1-4) for separating gas and solid of the fluidized bed reactor, and the first unit (1-4) for separating gas and solid of the fluidized bed reactor located in the gas-solid separation zone of the fluidized bed reactor (1); a gas outlet from the first block (1-4) for separating gas and solids of the fluidized bed reactor is connected to a gas collection chamber (1-5) of the fluidized bed reactor, and a catalyst outlet from the first block (1-4 ) for gas-solid separation of a fluidized bed reactor is formed in the spent catalyst zone; a spent catalyst zone gas distributor (1-6) is located in the lower part of the spent catalyst zone and a fluidized bed reactor cooler (1-7) is located in the spent catalyst zone; the second gas-solid separation unit (1-8) of the fluidized bed reactor is located in the gas-solid separation zone of the fluidized bed reactor (1), the inlet of the second unit (1-8) for gas-solid separation of the fluidized bed reactor fluidized bed is formed in the gas-solid separation zone of the fluidized bed reactor (1), the gas outlet from the second gas-solid separation unit (1-8) of the fluidized bed reactor is connected to the collection chamber (1-5) gas of the fluidized bed reactor, and a catalyst outlet from the second unit (1-8) for separating gas and solid of the fluidized bed reactor is formed in the spent catalyst zone; a fluidized bed reactor gas collection chamber (1-5) is located at the top of the fluidized bed reactor (1), and a product gas supply pipe (1-9) is connected to the top of the fluidized bed reactor gas collection chamber (1-5). fluidized bed; the inlet of the spent catalyst circulation pipe (1-10) is connected to the spent catalyst zone, and the outlet of the spent catalyst circulation pipe (1-10) is connected to the bottom of the reaction zone of the fluidized bed reactor (1); The slide valve (1-11) for circulating the spent catalyst is located in the pipe (1-10) for circulating the spent catalyst, the inlet of the inclined pipe (1-12) for the spent catalyst is connected to the spent catalyst area, and the outlet of the inclined pipe (1- 12) for spent catalyst is connected to the upper part of the stripping device (1-13) of the fluidized bed reactor; a stripping device (1-13) of the fluidized bed reactor is located outside the shell (1-1) of the fluidized bed reactor; the inlet of the spent catalyst spool valve (1-14) is connected by a pipeline to the bottom of the stripper (1-13) of the fluidized bed reactor, and the outlet of the spent catalyst spool valve (1-14) is connected by a pipeline to the inlet of the pipe (1 -15) for supplying spent catalyst; and the outlet of the spent catalyst supply pipe (1-15) is connected to the fluidized bed regenerator (2). The first gas-solid separation unit (1-4) of the fluidized bed reactor may have a plurality of sets of cyclone separators for separating gas and solid, and each of the plurality of sets of cyclone separators for separating gas and solid may include a cyclone separator for a first-stage gas-solid separation unit and a second-stage gas-solid separation cyclone separator; and the second gas-solid separation unit (1-8) of the fluidized bed reactor may have a plurality of sets of cyclone separators for separating gas and solid, and each of the plurality of sets of cyclone separators for separating gas and solid may include a cyclone separator for gas-solid separation of the first stage and a cyclone separator for gas-solid separation of the second stage.

As shown in FIG. 1, the fluidized bed regenerator (2) includes a regenerator shell (2-1), a first unit (2-2) for separating gas and solids of the regenerator, a first activation zone distributor (2-3), partition (2-4), pipe (2-5) for supplying catalyst to the first activation zone, pipe (2-6) for supplying gas to the first activation zone, distributor (2-7) for the second activation zone, perforated plate (2-8) , fluidized bed regenerator cooler (2-9), second unit (2-10) for separating regenerator gas and solids, chamber (2-11) for collecting regenerator gas, pipe (2-12) for supplying regenerator gaseous product, an inclined pipe (2-13) for the regenerated catalyst, a spool valve (2-14) for the regenerated catalyst, and a pipe (2-15) for supplying the regenerated catalyst; wherein the fluidized bed regenerator (2) is divided from bottom to top into a second activation zone, a first activation zone and a gas-solid separation zone; the first activation zone is located in the annular zone above the second activation zone, n partitions (2-4) are located in the first activation zone and partitions (2-4) can divide the first activation zone into n subzones of the first activation zone; the lower part of each of the subzones of the first activation zone is independently equipped with a distributor (2-3) of the first activation zone; the cross section of the first activation zone is circular, and the cross section of each of the subzones of the first activation zone is sector-ring; from the ^1st to the ^nth subzones of the first activation zone are located sequentially and concentrically; a hole for catalyst circulation is formed in the partitions (2-4) and there is no hole for catalyst circulation in the partition between the ^1st subzone of the first activation zone and the ^nth subzone of the first activation zone; a first gas-solid separation unit (2-2) of the regenerator is located in the gas-solid separation zone of the fluidized bed regenerator (2); the inlet inlet of the first block (2-2) for separating the gas and solid of the regenerator is connected to the outlet of the pipe (1-15) for supplying the spent catalyst, the gas outlet of the first block (2-2) for separating the gas and solid the regenerator is formed in the gas-solid separation zone, and the outlet for the catalyst from the first block (2-2) for separating the gas and solid substance of the regenerator is formed in the ^1st subzone of the first activation zone; the inlet of the pipe (2-5) for supplying the catalyst of the first activation zone is connected to the ^nth subzone of the first activation zone, and the outlet of the pipe (2-5) for supplying the catalyst of the first activation zone is formed in the second activation zone; the upper part of each of the subzones of the first activation zone is independently provided with a pipe (2-6) for supplying gas to the first activation zone, and the outlet of the pipe (2-6) for supplying gas to the first activation zone is formed in the gas-solid separation zone; the distributor (2-7) of the second activation zone is located in the lower part of the second activation zone of the fluidized bed regenerator (2) and m perforated plates (2-8) are located in the second activation zone, the cooler (2-9) of the fluidized bed regenerator is located in second activation zone; a second block (2-10) for separating gas and solids of the regenerator and a chamber (2-11) for collecting gas of the regenerator are located in the gas-solid separation zone of the fluidized bed regenerator (2); an inlet port of the second gas-solid separation unit (2-10) of the regenerator is formed in the gas-solid separation zone of the fluidized bed regenerator (2), a gas outlet from the second unit (2-10) for gas-solid separation the regenerator is connected to a chamber (2-11) for collecting regenerator gas, and a catalyst outlet from the second unit (2-10) for separating gas and solids of the regenerator is formed in the second activation zone; a pipe (2-12) for supplying a gaseous product of the regenerator is connected to the upper part of the chamber (2-11) for collecting the regenerator gas; the slant pipe inlet (2-13) for the regenerated catalyst is connected to the bottom of the second activation zone, the spool valve inlet (2-14) for the regenerated catalyst is connected to the slant pipe outlet (2-13) for the regenerated catalyst, and the spool valve outlet the valve (2-14) for the regenerated catalyst is connected by a pipeline to the inlet of the pipe (2-15) for supplying the regenerated catalyst; the outlet of the pipe (2-15) for supplying the regenerated catalyst is connected to the reaction zone of the fluidized bed reactor (1); the second gas-solid separation unit (2-10) of the regenerator has a plurality of sets of cyclone separators for gas-solid separation; and each of the plurality of sets of gas-solid separation cyclones includes a first stage gas-solid separation cyclone separator and a second stage gas-solid separation cyclone separator.

As a specific embodiment of the present application, the method for producing low carbon olefins from an oxygen-containing compound in the present application includes the following steps:

the raw material with the oxygen-containing compound is supplied from the distributor (1-2) of the fluidized bed reactor to the reaction zone of the fluidized bed reactor (1), where it interacts with the regenerated catalyst from the pipe (2-15) to supply the regenerated catalyst to obtain a stream A with low carbon olefins and spent catalyst; stream A enters the first gas-solid separation unit (1-4) of the fluidized bed reactor through a supply pipe (1-3) to perform gas-solid separation to produce gas-phase stream B and solid-phase stream C, wherein the gas-phase stream B is a low carbon olefin gas and solid stream C is spent catalyst; gas-phase stream B enters the gas collection chamber (1-5) of the fluidized bed reactor, and solid-phase stream C enters the spent catalyst zone; the fluidizing gas from the spent catalyst zone is supplied from the gas distributor (1-6) of the spent catalyst zone to the spent catalyst zone, where it interacts with the spent catalyst, and the fluidizing gas from the spent catalyst zone and the spent catalyst carried thereby form a stream D; stream D enters the second gas-solid separation unit (1-8) of the fluidized bed reactor to perform gas-solid separation to produce gas-phase stream E and solid-phase stream F, wherein gas-phase stream E is fluidizing gas from the exhaust zone catalyst, and the solid stream F is spent catalyst; the gas-phase stream E enters the gas collection chamber (1-5) of the fluidized bed reactor, and the solid-phase stream F is returned to the spent catalyst zone; gas-phase stream B and gas-phase stream E are mixed in the gas-collecting chamber (1-5) of the fluidized-bed reactor to produce a gaseous product, and the gaseous product is supplied to the downstream operating section through a gaseous-product supply pipe (1-9); part of the spent catalyst located in the spent catalyst zone is returned to the lower part of the reaction zone of the fluidized bed reactor (1) through a pipe (1-10) for circulating the spent catalyst and through a spool valve (1-11) for circulating the spent catalyst, and the remaining part of the spent catalyst enters the stripper (1-13) of the fluidized bed reactor through the inclined pipe (1-12) for the spent catalyst to perform its stripping, and then enters the fluidized bed regenerator (2) through the spool valve (1- 14) for spent catalyst and through a pipe (1-15) for supplying spent catalyst;

the raw material of the first activation zone is supplied to the first activation zone of the fluidized bed regenerator (2) from the distributor (2-3) of the first activation zone; the spent catalyst is supplied to the first block (2-2) for separating the gas and solid matter of the regenerator from the pipe (1-15) for supplying the spent catalyst to perform gas-solid separation, the resulting gas is discharged to the gas-solid separation zone of the regenerator (2 ) with a fluidized bed through the gas outlet of the first block (2-2) to separate the gas and solids of the regenerator, and the resulting spent catalyst is discharged into the first activation zone of the fluidized bed regenerator (2) through the catalyst outlet of the first block ( 2-2) for separation of gas and solid matter of the regenerator; the raw material of the first activation zone reacts and reacts chemically with the spent catalyst in the first activation zone, so that the inactive coke and active coke in the spent catalyst are converted into oxygen-containing hydrocarbon particles and oxygen-free hydrocarbon particles of small molecular weight, and a gaseous product of the first activation zone is generated ; the catalyst in the first activation zone sequentially passes through subzones from the ^1st to ^{the nth} of the first activation zone through the holes for catalyst circulation in the partitions (2-4), and then enters the second activation zone of the regenerator (2) with a fluidized bed through a pipe (2- 5) to supply catalyst to the first activation zone; the gaseous product of the first activation zone enters the gas-solid separation zone of the fluidized bed regenerator (2) through a pipe (2-6) for supplying gas to the first activation zone; the raw material of the second activation zone is supplied to the second activation zone of the fluidized bed regenerator (2) from the distributor (2-7) of the second activation zone to interact and enter into a chemical reaction with the catalyst from the first activation zone, so that the particles of catalytically inactive oxygen-containing hydrocarbon in the coke are converted into particles of catalytically active oxygen-free hydrocarbon, the molecular weight of the coke is further reduced (i.e., the coke in the catalyst is converted into particles mainly consisting of polymethylbenzene and polymethylnaphthalene; and the catalyst removed from the second activation zone is called regenerated catalyst), and the raw material the second activation zone is converted into a gaseous product of the second activation zone in the second activation zone, and then enters the gas-solid separation zone of the fluidized bed regenerator (2); the gaseous product of the first activation zone and the gaseous product of the second activation zone are mixed in the gas-solid separation zone to obtain a gaseous product of the regenerator, and the gaseous product of the regenerator containing the catalyst enters the second unit (2-10) for separating the gas and solid of the regenerator for performing gas-solid separation to produce a gaseous product of a regenerator and a catalyst; the regenerator product gas enters the regenerator gas collection chamber (2-11), and then enters the downstream regenerator product gas recirculation system through the regenerator product gas supply pipe (2-12), and the catalyst is returned to the second activation zone regenerator (2) with a fluidized bed; the regenerated catalyst in the second activation zone is cooled and then fed into the fluidized bed reactor (1) through the inclined pipe (2-13) for the regenerated catalyst, through the spool valve (2-14) for the regenerated catalyst and through the pipe (2-15) for supplying regenerated catalyst.

To better illustrate this application and to facilitate understanding of the technical solutions presented in this application, the following are typical, but not limiting, examples of this application:

Example 1

In this example, the device shown in Fig. 1 and Fig. 2 is used, in which the first unit (2-2) for separating gas and solids of the regenerator is a cyclone separator for separating gas and solids; 2 partitions (2-4) are located in the first activation zone of the fluidized bed regenerator (2), i.e. n=2; partitions (2-4) divide the first activation zone into 2 subzones of the first activation zone; and 10 perforated plates (2-8) are located in the second activation zone of the fluidized bed regenerator (2), i.e. m=10; and perforated plates (2-8) have a porosity of 50%.

In this example, the oxygen-containing compound is methanol; the fluidizing gas of the spent catalyst zone is nitrogen; the raw material of the first activation zone includes 10% wt. oxygen and 90% wt. water vapor; the raw material of the second activation zone is water vapor; the active component of the catalyst is a SAPO-34 molecular sieve; The coke content of the regenerated catalyst is approximately 5 wt.%, and the coke particles include polymethylbenzene and polymethylnaphthalene, the mass of polymethylbenzene and polymethylnaphthalene is approximately 72 wt.%. of the total mass of coke, the mass of coke particles with a molecular weight of more than 184 is approximately 19% wt. of the total mass of coke, and the quartile deviation of the distribution of coke content in the regenerated catalyst is approximately 0.9% by weight; The coke content of the spent catalyst is approximately 9% by weight; the reaction zone of the fluidized bed reactor (1) is a rapid fluidization zone, and the process operating conditions in the reaction zone of the fluidized bed reactor (1) are as follows: apparent linear gas velocity: approximately 7.0 m/s, reaction temperature: approximately 550°C, reaction pressure: approximately 100 kPa and layer density: approximately 100 kg/m ³ ; The process operating conditions of the spent catalyst zone of the fluidized bed reactor (1) are as follows: apparent linear gas velocity: approximately 1.0 m/s, reaction temperature: approximately 550°C, reaction pressure: approximately 100 kPa and bed density: approximately 200 kg/m ³ ; the operating conditions for the process of the first activation zone of the fluidized bed regenerator (2) are as follows: apparent linear gas velocity: 0.5 m/s; temperature: 750°C; pressure: 100 kPa; and layer density: 400 kg/m ³ ; and the operating conditions for the process in the second activation zone of the fluidized bed regenerator (2) are as follows: apparent linear gas velocity: 0.5 m/s; temperature: 700°C; pressure: 100 kPa; and layer density: 400 kg/ ^m3 .

In this example, the ratio of catalyst to alcohol is approximately 0.3 tons of catalyst per 1 ton of methanol; the gaseous product consists of ethylene in an amount of 55 wt.%, propylene in an amount of 37 wt.%, C ₄ -C ₆ hydrocarbon compounds in an amount of 5 wt.%. and other components in an amount of 3% by weight, wherein other components include methane, ethane, propane, hydrogen, CO, CO ₂ and the like; and the specific production consumption is 2.50 tons of methanol per 1 ton of low-carbon olefins. The utilization rate of C atoms in the entire process is 99.0%.

Example 2

In this example, the device shown in Fig. 1 and Fig. 2 is used, in which the first unit (2-2) for separating gas and solids of the regenerator is a cyclone separator for separating gas and solids; 10 partitions (2-4) are located in the first activation zone of the fluidized bed regenerator (2), i.e. n=10; partitions (2-4) divide the first activation zone into 10 subzones of the first activation zone; and 1 perforated plate (2-8) is located in the second activation zone of the fluidized bed regenerator (2), i.e. m=1; and the perforated plate (2-8) has a porosity of 5%.

In this example, the oxygen-containing compound includes 82 wt%. methanol and 18% wt. dimethyl ether; the fluidizing gas of the spent catalyst zone is water vapor; the raw material of the first activation zone includes 20% wt. air and 80% wt. water vapor; the raw material of the second activation zone is water vapor; the active component of the catalyst is a SAPO-34 molecular sieve; The coke content of the regenerated catalyst is approximately 7% by weight, and the coke particles include polymethylbenzene and polymethylnaphthalene, the mass of polymethylbenzene and polymethylnaphthalene is approximately 66% by weight. of the total mass of coke, the mass of coke particles with a molecular weight of more than 184 is approximately 26% wt. of the total mass of coke, and the quartile deviation of the distribution of coke content in the regenerated catalyst is approximately 0.6% by weight; the coke content of the spent catalyst is approximately 11% by weight; The process operating conditions in the reaction zone of the fluidized bed reactor (1) are as follows: apparent linear gas velocity: approximately 0.5 m/s, reaction temperature: approximately 350° C., reaction pressure: approximately 500 kPa and bed density: approximately 500 kg/m ³ ; the spent catalyst zone of the fluidized bed reactor (1) is a bubbling fluidization zone; and the process operating conditions of the spent catalyst zone of the fluidized bed reactor (1) are as follows: apparent linear gas velocity: approximately 0.1 m/s, reaction temperature: approximately 350°C, reaction pressure: approximately 500 kPa, and bed density: approximately 800 kg/ ^m3 ; the operating conditions for the process of the first activation zone of the fluidized bed regenerator (2) are as follows: apparent linear gas velocity: 0.3 m/s; temperature: 700°C; pressure: 500 kPa; and layer density: 510 kg/m ³ ; and the operating conditions for the process in the second activation zone of the fluidized bed regenerator (2) are as follows: apparent linear gas velocity: 0.3 m/s; temperature: 550°C; pressure: 500 kPa; and layer density: 510 kg/ ^m3 .

In this example, the ratio of catalyst to alcohol is approximately 0.5 tons of catalyst per 1 ton of methanol; the gaseous product consists of ethylene in the amount of 38% wt., propylene in the amount of 54% wt., hydrocarbon compounds C ₄ -C ₆ in the amount of 6% wt. and other components in an amount of 2% by weight, wherein other components include methane, ethane, propane, hydrogen, CO, CO ₂ and the like; and the specific production consumption is 2.50 tons of methanol per 1 ton of low-carbon olefins. The utilization rate of C atoms in the entire process is 99.3%.

Example 3

In this example, the device shown in Fig. 1 and Fig. 2 is used, in which the first unit (2-2) for separating gas and solids of the regenerator is a cyclone separator for separating gas and solids; 4 partitions (2-4) are located in the first activation zone of the fluidized bed regenerator (2), i.e. n=4; partitions (2-4) divide the first activation zone into 4 subzones of the first activation zone; and 6 perforated plates (2-8) are located in the second activation zone of the fluidized bed regenerator (2), i.e. m=6; and perforated plates (2-8) have a porosity of 30%.

In this example, the oxygen-containing compound is dimethyl ether; the fluidizing gas of the spent catalyst zone includes 5% wt. nitrogen and 95% wt. water vapor; the raw material of the first activation zone includes 1% wt. oxygen and 99% wt. water vapor; the raw material of the second activation zone is water vapor; the active component of the catalyst is a SAPO-34 molecular sieve; The coke content of the regenerated catalyst is approximately 9% by weight, and the coke particles include polymethylbenzene and polymethylnaphthalene, the mass of polymethylbenzene and polymethylnaphthalene is approximately 79% by weight. of the total mass of coke, the mass of coke particles with a molecular weight of more than 184 is approximately 13% wt. of the total mass of coke, and the quartile deviation of the distribution of coke content in the regenerated catalyst is approximately 0.2% by weight; the coke content of the spent catalyst is approximately 12% by weight; The process operating conditions in the reaction zone of the fluidized bed reactor (1) are as follows: apparent linear gas velocity: approximately 3.0 m/s, reaction temperature: approximately 450° C., reaction pressure: approximately 300 kPa and bed density: approximately 230 kg/m ³ ; The process operating conditions of the spent catalyst zone of the fluidized bed reactor (1) are as follows: apparent linear gas velocity: approximately 0.2 m/s, reaction temperature: approximately 450°C, reaction pressure: approximately 300 kPa and bed density: approximately 600 kg/m ³ ; the operating conditions for the process of the first activation zone of the fluidized bed regenerator (2) are as follows: apparent linear gas velocity: 0.2 m/s; temperature: 680°C; pressure: 300 kPa; and layer density: 580 kg/m ³ ; and the operating conditions for the process in the second activation zone of the fluidized bed regenerator (2) are as follows: apparent linear gas velocity: 0.2 m/s; temperature: 630°C; pressure: 300 kPa; and layer density: 580 kg/ ^m3 .

In this example, the ratio of catalyst to alcohol is approximately 0.8 tons of catalyst per 1 ton of methanol; the gaseous product consists of ethylene in the amount of 45% wt., propylene in the amount of 51% wt., hydrocarbon compounds C ₄ -C ₆ in the amount of 3% wt. and other components in an amount of 1% by weight, wherein other components include methane, ethane, propane, hydrogen, CO, CO ₂ and the like; and the specific production consumption is 2.42 tons of methanol per 1 ton of low-carbon olefins. The degree of utilization of C atoms in the entire process is 99.5%.

Example 4

In this example, the device shown in Fig. 1 and Fig. 2 is used, in which the first unit (2-2) for separating gas and solids of the regenerator is a cyclone separator for separating gas and solids; 8 partitions (2-4) are located in the first activation zone of the fluidized bed regenerator (2), i.e. n=8; partitions (2-4) divide the first activation zone into 8 subzones of the first activation zone; and 4 perforated plates (2-8) are located in the second activation zone of the fluidized bed regenerator (2), i.e. m=4; and perforated plates (2-8) have a porosity of 20%.

In this example, the oxygen-containing compound is methanol; the fluidizing gas of the spent catalyst zone is water vapor; the raw material of the first activation zone includes 5% wt. air and 95% wt. water vapor; the raw material of the second activation zone is water vapor; the active component of the catalyst is a SAPO-34 molecular sieve; The coke content of the regenerated catalyst is approximately 11 wt.%, and the coke particles include polymethylbenzene and polymethylnaphthalene, the mass of polymethylbenzene and polymethylnaphthalene is approximately 88 wt.%. of the total mass of coke, the mass of coke particles with a molecular weight of more than 184 is approximately 7% wt. of the total mass of coke, and the quartile deviation of the distribution of coke content in the regenerated catalyst is approximately 0.1% by weight; the coke content of the spent catalyst is approximately 13% by weight; The process operating conditions in the reaction zone of the fluidized bed reactor (1) are as follows: apparent linear gas velocity: approximately 4.0 m/s, reaction temperature: approximately 500° C., reaction pressure: approximately 200 kPa and bed density: approximately 160 kg/m ³ ; The process operating conditions of the spent catalyst zone of the fluidized bed reactor (1) are as follows: apparent linear gas velocity: approximately 0.5 m/s, reaction temperature: approximately 500°C, reaction pressure: approximately 200 kPa and bed density: approximately 300 kg/m ³ ; the operating conditions for the process of the first activation zone of the fluidized bed regenerator (2) are as follows: apparent linear gas velocity: 0.1 m/s; temperature: 650°C; pressure: 200 kPa; and layer density: 700 kg/m ³ ; and the operating conditions for the process in the second activation zone of the fluidized bed regenerator (2) are as follows: apparent linear gas velocity: 0.1 m/s; temperature: 600°C; pressure: 200 kPa; and layer density: 700 kg/ ^m3 .

In this example, the ratio of catalyst to alcohol is approximately 1.0 tons of catalyst per 1 ton of methanol; the gaseous product consists of ethylene in the amount of 51% wt., propylene in the amount of 46% wt., hydrocarbon compounds C ₄ -C ₆ in the amount of 2% wt. and other components in an amount of 1% by weight, wherein other components include methane, ethane, propane, hydrogen, CO, CO ₂ and the like; and the specific production consumption is 2.40 tons of methanol per 1 ton of low-carbon olefins. The utilization rate of C atoms in the entire process is 99.6%.

The above examples are just a few examples of the present application and are not intended to limit it in any way. Although the present application has been described above with preferred examples, the present application is not limited to them. Certain changes or modifications, which may be suggested by those skilled in the art using the technical content disclosed above without departing from the scope of the technical solutions of the present invention, are equivalent to equivalent implementation cases and are included in the specified scope of technical solutions.

Claims (80)

1. A fluidized bed regenerator for activating a catalyst to produce low-carbon olefins from an oxygen-containing compound, comprising a second activation zone, a first activation zone, and a gas-solid separation zone from bottom to top; wherein the second activation zone in the axial direction communicates with the gas-solid separation zone; the first activation zone is located at the periphery of the connection between the second activation zone and the gas-solid separation zone; the first activation zone is an annular cavity; n partitions are radially installed in the first activation zone, and n partitions divide the first activation zone into n subzones of the first activation zone; And each of the n-1 partitions is provided with a catalyst circulation hole such that the catalyst entering the first activation zone flows in an annular direction. 2. The fluidized bed regenerator according to claim 1, wherein the n partitions in the first activation zone comprise the 1st partition and from the 2nd partition to the nth partition; there is no hole for catalyst circulation in the 1st partition; in each partition from the 2nd partition to the nth partition a hole is formed for circulation of the catalyst; in the 1st subzone of the first activation zone, formed by separation using the 1st partition and the 2nd partition, an inlet for spent catalyst is formed; in the n-th subzone of the first activation zone, formed by separation using the 1st partition and the n-th partition, there is a pipe for supplying the catalyst to the first activation zone; Below the subzones of the first activation zone there is a distributor of the first activation zone; in the upper parts of the subzones of the first activation zone there is a pipe for supplying gas to the first activation zone, preferably n has the following range of values: 2 ≤ n ≤ 10; preferably, the cross-section of each of the subzones of the first activation zone is sector-ring; preferably, m perforated plates are located horizontally in the second activation zone, where 1 ≤ m ≤ 10; preferably the perforated plates have a porosity of 5 to 50%; preferably, a distributor of the second activation zone is located in the lower part of the second activation zone. 3. The fluidized bed regenerator according to claim 1, wherein the first unit for separating gas and solids of the regenerator is located at the top of the first activation zone; And a first gas-solid separation unit of the regenerator communicates with the first activation zone through a spent catalyst inlet; preferably, the fluidized bed regenerator includes a regenerator gas collection chamber and a fluidized bed regenerator cooler; a regenerator gas collection chamber is located at the top of the fluidized bed regenerator; the upper part of the regenerator gas collection chamber is provided with a pipe for supplying the regenerator gas product; the gas-solid separation zone is provided with a second gas-solid separation unit; a gas collection chamber of the regenerator is connected to an outlet of the second gas-solid separation unit; And The fluidized bed regenerator cooler is located at the bottom of the second activation zone. 4. An apparatus for producing low carbon olefins from an oxygen-containing compound, comprising a fluidized bed reactor and a fluidized bed regenerator, wherein the fluidized bed regenerator comprises the fluidized bed regenerator according to claim 1. 5. The apparatus of claim 4, comprising a spent catalyst slant pipe, a fluidized bed reactor stripper, a spent catalyst supply pipe, a regenerated catalyst slant pipe, and a regenerated catalyst supply pipe; wherein the spent catalyst zone, the spent catalyst inclined pipe, the fluidized bed reactor stripper, the spent catalyst supply pipe, and the first gas-solid separation unit of the regenerator are in sequential communication with each other; And the second activation zone, the regenerated catalyst inclined pipe, the regenerated catalyst supply pipe and the reaction zone of the fluidized bed reactor are sequentially communicated with each other; preferably the fluidized bed reactor comprises a lower shell, a feed pipe and an upper shell; the lower shell encloses the reaction zone; the supply pipe is located above the reaction zone and communicates with the reaction zone; the upper shell is located on the periphery of the supply pipe; the upper shell and the supply pipe form a cavity; And said cavity is divided from bottom to top into a spent catalyst zone and a gas-solid separation zone; preferably the reaction zone is a rapid fluidization zone; preferably the spent catalyst zone is a bubble fluidization zone; preferably, the gas-solid separation zone is provided with a first gas-solid separation unit of the fluidized bed reactor; And an upper portion of the supply pipe is connected to an inlet of the first gas-solid separation unit of the fluidized bed reactor; preferably, the fluidized bed reactor includes a fluidized bed reactor distributor, a fluidized bed reactor cooler, a spent catalyst zone gas distributor, a fluidized bed reactor gas collection chamber, and a second fluidized bed reactor gas-solid separation unit; a fluidized bed reactor distributor is located at the bottom of the reaction zone; a fluidized bed reactor cooler is located at the bottom of the spent catalyst zone; the gas distributor of the spent catalyst zone is located in the lower part of the spent catalyst zone; gas outlets from the second gas-solid separation unit of the fluidized bed reactor and the first gas-solid separation unit of the fluidized bed reactor are connected to a gas collection chamber of the fluidized bed reactor; a gas collection chamber of the fluidized bed reactor is provided with a pipe for supplying a gaseous product; And catalyst outlets from the first gas-solid separation unit of the fluidized bed reactor and the second gas-solid separation unit of the fluidized bed reactor are connected to a spent catalyst zone; preferably, the reaction zone and the spent catalyst zone communicate with each other through a spent catalyst circulation pipe. 6. A method for producing low-carbon olefins from an oxygen-containing compound using a device according to claim 4, wherein the method for producing low-carbon olefins from an oxygen-containing compound comprises a method for activating a catalyst for producing low-carbon olefins from an oxygen-containing compound, and the method for activating a catalyst for producing low-carbon olefins from an oxygen-containing compound uses a fluidized bed regenerator according to claim 1; wherein a method of activating a catalyst for producing low-carbon olefins from an oxygen-containing compound includes: supplying the raw material of the first activation zone and the spent catalyst to the first activation zone, in which the spent catalyst chemically reacts with the raw material of the first activation zone, flowing in an annular direction along the subzones of the first activation zone, to form a partially activated catalyst; And supplying the partially activated catalyst and the raw material of the second activation zone to the second activation zone and conducting a chemical reaction to obtain a regenerated catalyst; wherein the coke composition in the partially activated catalyst contains particles of oxygen-containing hydrocarbons and particles of oxygen-free hydrocarbons; wherein the method for producing low-carbon olefins from an oxygen-containing compound includes: supplying a raw material with an oxygen-containing compound and a regenerated catalyst to a reaction zone and reacting to produce a stream A with low carbon olefins and spent catalyst; performing separation of stream A into gas and solid and transferring spent catalyst to a spent catalyst zone; And returning a portion of the spent catalyst from the spent catalyst zone to the fluidized bed reaction zone and causing the remainder of the spent catalyst to enter the fluidized bed regenerator. 7. The method according to claim 6, according to which the raw material of the first activation zone contains oxygen, air and water vapor; the mass fraction of oxygen ranges from 0 to 10% by weight; the mass fraction of air ranges from 0 to 20% wt.; And the mass fraction of water vapor ranges from 80 to 100% wt.; Preferably, the operating conditions for the process in the first activation zone of the fluidized bed regenerator are as follows: apparent linear gas velocity: 0.1 to 0.5 m/s; temperature: from 650 to 750°C; pressure: from 100 to 500 kPa; and layer density: from 400 to 700 kg/m ³ ; preferably, the raw material of the second activation zone is water vapor; Preferably, the operating conditions for the process in the second activation zone of the fluidized bed regenerator are as follows: apparent linear gas velocity: 0.1 to 0.5 m/s; temperature: from 550 to 700°C; pressure: from 100 to 500 kPa; and layer density: from 400 to 700 kg/ ^m3 . 8. The method according to claim 6, according to which the coke content in the spent catalyst is from 9 to 13% by weight; preferably the coke content of the spent catalyst is from 10 to 12% by weight; preferably the spent catalyst contains a SAPO-34 molecular sieve; preferably the coke content of the regenerated catalyst is from 5 to 11% by weight; And the quartile deviation of the distribution of coke content in the regenerated catalyst is less than 1.0% by weight; preferably, the coke particles in the regenerated catalyst contain polymethylbenzene and polymethylnaphthalene; the total mass of polymethylbenzene and polymethylnaphthalene is more than 60% wt. from the total mass of coke or may be equal to the specified amount; the mass of coke particles with a molecular weight of more than 184 is less than 30% wt. from the total mass of coke or may be equal to the specified amount; A total coke mass refers to the total mass of coke particles. 9. The method according to claim 6, according to which the operating conditions for the process in the spent catalyst zone of the fluidized bed reactor are as follows: apparent linear gas velocity: from 0.1 to 1.0 m/s; reaction temperature: from 350 to 550°C; reaction pressure: from 100 to 500 kPa; and layer density: from 200 to 800 kg/ ^m3 . 10. The method according to claim 6, wherein the raw material with the oxygen-containing compound is at least one of the group consisting of methanol and dimethyl ether (DME); preferably, the ratio of the mass flow of the regenerated catalyst to the supplied amount of oxygen-containing compound is from 0.3 to 1.0 tons of catalyst per 1 ton of methanol; preferably, the ratio of the mass flow of the regenerated catalyst to the supplied amount of oxygen-containing compound is from 0.5 to 1.0 t of catalyst per 1 t of methanol; Preferably, the operating conditions of the process in the reaction zone of the fluidized bed reactor are as follows: apparent linear gas velocity: from 0.5 to 7.0 m/s; reaction temperature: from 350 to 550°C; reaction pressure: from 100 to 500 kPa; and layer density: from 100 to 500 kg/ ^m3 .