Patent Description:
Methanol-to-olefin technology (MTO) mainly includes DMTO (methanol-to-olefin) technology of Dalian Institute of Chemical Physics, Chinese Academy of Sciences and MTO technology of UOP Company of the United States. In <NUM>, the Shenhua Baotou methanol-to-olefin 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 <NUM>, <NUM> DMTO industrial plants have been put into production, with a total production capacity of about <NUM> million tons of light olefins per year.

In recent years, DMTO technology has been further developed, and a new generation of DMTO catalyst with better performance have gradually begun industrial applications, creating higher benefits for DMTO plants. The new generation of DMTO catalyst has higher methanol processing capacity and light olefin selectivity. It is difficult for the existing DMTO industrial devices to take full advantage of the advantages of the new generation of DMTO catalyst. Therefore, it is necessary to develop a DMTO device and production method that can meet the needs of a new generation of DMTO catalyst with high methanol processing capacity and high selectivity of light olefins. <CIT> discloses a method for producing oxygen-containing "low carbon" olefins from light olefins, with the use of a reactor with a riser reactor and fluidised bed reactor zones surrounding said riser reactor, and a regenerator with a delivery tube, wherein the upper, lower and middle parts are separated by walls.

According to a first aspect of the present application, a coke control reactor is provided, which can control the conversion and generation of coke species in a catalyst. On the one hand, inactive large-molecule coke species remaining in a regenerated catalyst are converted into small-molecule coke species; and on the other hand, a riser reactor raw material and a bed reactor raw material can also enter the catalyst to generate highly-active small-molecule coke species, and the small-molecule coke species are mainly polymethylbenzene and polymethylnaphthalene, which can improve the selectivity for ethylene.

The coke control reactor includes a riser reactor and a bed reactor; the bed reactor includes a bed reactor shell, and the bed reactor shell encloses a reaction zone I, a transition zone, and a gas-solid separation zone I from bottom to top, the transition zone has a diameter gradually increasing from bottom to top such that a bottom of the transition zone is connected to a top of the reaction zone I and a top of the transition zone is connected to a bottom of the gas-solid separation zone I; a bed reactor distributor is arranged in an inner lower part of the reaction zone I; a coke controlled catalyst delivery pipe is arranged outside the reaction zone I and configured to deliver a coke controlled catalyst to a next-level reactor; an upper section of the riser reactor penetrates through a bottom of the bed reactor and is axially inserted in the bed reactor; and an outlet end of the riser reactor is located in the transition zone; at least one perforated plate is arranged in the reaction zone I; the plurality of perforated plates is axially arranged on a periphery of the riser reactor in sequence; the outlet end of the riser reactor is located above the perforated plate; the bed reactor distributor is located below the perforated plate; preferably, the perforated plate has a porosity of <NUM>% to <NUM>%.

Specifically, the next-level reactor can be a methanol conversion reactor.

According to a second aspect of the present application, a device for preparing light olefins from an oxygen-containing compound is also provided, including a methanol conversion reactor and the coke control reactor described above.

The light olefins mentioned in the present application refer to ethylene and propylene.

The methanol conversion reactor includes a methanol conversion reactor shell and a delivery pipe; the methanol conversion reactor shell includes a lower shell and an upper shell; the lower shell encloses a reaction zone II, and a methanol conversion reactor distributor is arranged in an inner lower part of the reaction zone II; the delivery pipe is axially located above the reaction zone II; the delivery pipe has one end closed and the other end communicating with the reaction zone II; the upper shell is arranged on a periphery of the delivery pipe; the upper shell and a pipe wall of the delivery pipe encloses to a cavity; the cavity is divided into a spent catalyst zone and a gas-solid separation zone II from bottom to top; and the spent catalyst zone is provided with a spent catalyst zone gas distributor.

Specifically, the upper shell may be arranged on a periphery of the delivery pipe in a wrapping form. The methanol conversion reactor distributor may be configured to feed a raw material with an oxygen-containing compound; and the spent catalyst zone gas distributor may be configured to feed a spent catalyst zone fluidizing gas.

Optionally, the gas-solid separation zone II may be provided with a first gas-solid separation unit of the methanol conversion reactor; an upper part of the delivery pipe may be connected to an inlet of the first gas-solid separation unit of the methanol conversion reactor; a catalyst outlet of the first gas-solid separation unit of the methanol conversion reactor may be formed in the spent catalyst zone; a gas outlet of the first gas-solid separation unit of the methanol conversion reactor may communicate with a methanol conversion reactor gas collection chamber; and the methanol conversion reactor gas collection chamber may be connected to a product gas delivery pipe.

Optionally, the gas-solid separation zone II may be further provided with a second gas-solid separation unit of the methanol conversion reactor; a gas inlet of the second gas-solid separation unit of the methanol conversion reactor may be formed in the gas-solid separation zone II; a catalyst outlet of the second gas-solid separation unit of the methanol conversion reactor may be formed in the spent catalyst zone; and a gas outlet of the second gas-solid separation unit of the methanol conversion reactor may communicate with the methanol conversion reactor gas collection chamber.

Optionally, the spent catalyst zone gas distributor may be located below the first gas-solid separation unit of the methanol conversion reactor and the second gas-solid separation unit of the methanol conversion reactor; and a methanol conversion reactor cooler may be further provided in the spent catalyst zone.

Optionally, a spent catalyst circulation pipe and a spent catalyst inclined pipe may be further arranged outside the spent catalyst zone; the spent catalyst circulation pipe may be configured to connect the spent catalyst zone and the reaction zone II; and the spent catalyst inclined pipe may be configured to output a spent catalyst.

Specifically, the spent catalyst circulation pipe may be configured to deliver a part of the spent catalyst in the spent catalyst zone to the reaction zone II. The spent catalyst circulation pipe may be provided with a spent catalyst circulation slide valve.

Optionally, the gas-solid separation zone II may communicate with the bed reactor gas collection chamber through a coke control product gas delivery pipe; and the reaction zone II may communicate with the reaction zone I through a coke controlled catalyst delivery pipe.

Specifically, a coke controlled catalyst slide valve may be further provided on the coke controlled catalyst delivery pipe.

The device further includes a regenerator; the regenerator is connected to the spent catalyst inclined pipe, and a spent catalyst is delivered to the regenerator; the regenerator is connected to a riser reactor, and a regenerated catalyst is delivered to the coke control reactor; and an inner bottom of the regenerator is provided with a regenerator distributor.

Specifically, the regenerator distributor may be configured to feed a regeneration gas.

Optionally, a bottom of the regenerator may be further provided with a regenerator stripper; an upper section of the regenerator stripper may be arranged inside the regenerator, and an inlet of the upper section of the regenerator stripper may be located above the regenerator distributor; a lower section of the regenerator stripper may be arranged outside the regenerator, and an outlet of the lower section of the regenerator stripper may be connected to the riser reactor; and the regenerator stripper may be further provided with a regenerator cooler.

Optionally, the regenerator may be connected to the spent catalyst inclined pipe through a spent catalyst delivery pipe and a methanol conversion reactor stripper; and the regenerator may be connected to an inlet of the riser reactor through the regenerator stripper and a regenerated catalyst inclined pipe.

Specifically, a spent catalyst slide valve may be arranged between the spent catalyst delivery pipe and the methanol conversion reactor stripper; and an inlet of the spent catalyst slide valve may be connected to a bottom of the methanol conversion reactor stripper through a pipeline, and an outlet of the spent catalyst slide valve may be connected to an inlet of the spent catalyst delivery pipe through a pipeline.

A regenerated catalyst slide valve may be arranged between the regenerator stripper and the regenerated catalyst inclined pipe; and an inlet of the regenerated catalyst slide valve is connected to a bottom of the regenerator stripper through a pipeline, and an outlet of the regenerated catalyst slide valve is connected to an inlet of the regenerated catalyst inclined pipe through a pipeline.

Optionally, the regenerator may be further provided with a regenerator gas-solid separation unit and a regenerator gas collection chamber; a catalyst outlet of the regenerator gas-solid separation unit may be formed above the regenerator distributor; a gas outlet of the regenerator gas-solid separation unit may be connected to the regenerator gas collection chamber; and the regenerator gas collection chamber may be connected to a flue gas delivery pipe located outside the regenerator.

According to a third aspect of the present application, a method for on-line modification of a DMTO catalyst using the coke control reactor described above is also provided, including feeding a riser reactor raw material and a catalyst into a transition zone from a riser reactor, and feeding a bed reactor raw material into a reaction zone I; and allowing the catalyst to contact and react with the riser reactor raw material and the bed reactor raw material to generate a coke controlled catalyst and a coke control product gas, where the catalyst is a DMTO catalyst; and the coke controlled catalyst is a modified DMTO catalyst.

Optionally, an active component of the catalyst may be an SAPO-<NUM> molecular sieve.

In the present application, the catalyst entering the riser reactor may be a fresh catalyst or a regenerated catalyst and preferably a regenerated catalyst, such that both coke control and catalyst regeneration can be realized on-line.

Optionally, the catalyst may be a regenerated catalyst; and a coke content in the regenerated catalyst may be less than or equal to <NUM> wt%.

Optionally, a coke content in the coke controlled catalyst may be <NUM> wt% to <NUM> wt%.

Optionally, a quartile deviation of a coke content distribution in the coke controlled catalyst may be less than <NUM> wt%. Specifically, in the present application, the coke content in the coke controlled catalyst is controlled at <NUM> wt% to <NUM> wt% through the arrangement of the coke control reactor and the selection of the coke control process. Since the catalyst is granular, the coke content in the catalyst refers to an average coke content in catalyst granules, but coke contents in different catalyst granules may actually be different. In the present application, the quartile deviation of the coke content distribution in the coke controlled catalyst can be controlled to be less than <NUM> wt%, such that the overall coke content distribution of the catalyst is narrow, thereby improving the activity of the catalyst and the selectivity for light olefins.

Optionally, coke species in the coke controlled catalyst may include polymethylbenzene and polymethylnaphthalene; a total mass of the polymethylbenzene and the polymethylnaphthalene may account for greater than or equal to <NUM> wt% of a total mass of coke; a mass of coke species with a molecular weight greater than <NUM> may account for less than or equal to <NUM> wt% of the total mass of coke; and the total mass of coke may refer to a total mass of coke species.

In the present application, types and contents of coke species are also very important, which is also one of the objectives of control in the present application. In the present application, a total mass of the polymethylbenzene and the polymethylnaphthalene is controlled to be greater than or equal to <NUM> wt% of the total mass of coke through the arrangement of coke control and the selection of coke control process parameters to improve the activity of the catalyst and the selectivity for light olefins.

Optionally, process operating conditions of the riser reactor may be as follows: apparent gas linear velocity: <NUM>/s to <NUM>/s; reaction temperature: <NUM> to <NUM>; reaction pressure: <NUM> kPa to <NUM> kPa; and bed density: <NUM>/m<NUM> to <NUM>/m<NUM>.

Optionally, process operating conditions of the reaction zone I of a bed reactor may be as follows: apparent gas linear velocity: <NUM>/s to <NUM>/s; reaction temperature: <NUM> to <NUM>; reaction pressure: <NUM> kPa to <NUM> kPa; and bed density: <NUM>/m<NUM> to <NUM>/m<NUM>.

According to a fourth aspect of the present application, a method for preparing light olefins from an oxygen-containing compound is also provided, including the method for on-line modification of a DMTO catalyst described above.

Optionally, the method may further include: feeding a coke control product gas into a gas-solid separation zone of a methanol conversion reactor; and feeding a coke controlled catalyst into a reaction zone II of the methanol conversion reactor.

Optionally, in the reaction zone II, a raw material with an oxygen-containing compound may contact and react with the coke controlled catalyst to generate a stream A with light olefins and a spent catalyst.

Optionally, the stream A may be separated into a gas-phase stream B and a solid-phase stream C after being subjected to gas-solid separation in a gas-solid separation zone II of the methanol conversion reactor; the gas-phase stream B may enter a methanol conversion reactor gas collection chamber; the solid-phase stream C may enter a spent catalyst zone; and the gas-phase stream B may include the light olefins, and the solid-phase stream C may include the spent catalyst.

Optionally, a spent catalyst zone fluidizing gas may be fed into the spent catalyst zone; the spent catalyst zone fluidizing gas and a coke control product gas may be mixed and carry a part of the spent catalyst to produce a stream D; the stream D may be separated into a gas-phase stream E and a solid-phase stream F after being subjected to gas-solid separation; the gas-phase stream E may enter the methanol conversion reactor gas collection chamber; the solid-phase stream F may enter the spent catalyst zone; the gas-phase stream E may be a mixed gas of the spent catalyst zone fluidizing gas and the coke control product gas; and the solid-phase stream F may be the spent catalyst.

Optionally, the gas-phase stream B and the gas-phase stream E may be mixed in the methanol conversion reactor gas collection chamber to produce a product gas, and the product gas may enter a downstream working section through a product gas delivery pipe.

Optionally, a part of the spent catalyst in the spent catalyst zone may be returned to a bottom of the reaction zone II through a spent catalyst circulation pipe; and the remaining part of the spent catalyst may be discharged through a spent catalyst inclined pipe.

Optionally, the spent catalyst discharged through the spent catalyst inclined pipe may be fed into a regenerator; and a regeneration gas may be fed into the regenerator to contact and react with the spent catalyst to obtain a stream G with a flue gas and a regenerated catalyst.

Optionally, the stream G may be subjected to gas-solid separation; a separated flue gas may enter a regenerator gas collection chamber, and then enter a downstream flue gas treatment system through a flue gas delivery pipe; and a separated regenerated catalyst may be stripped and cooled, and then enter a coke control reactor.

Specifically, the separated regenerated catalyst may enter the riser reactor for stripping and cooling, and then may be fed into the bed reactor from the riser reactor.

Optionally, the oxygen-containing compound may include methanol and/or dimethyl ether (DME).

Optionally, a coke content in the spent catalyst may be <NUM> wt% to <NUM> wt%.

Optionally, the spent catalyst zone fluidizing gas may include nitrogen and/or water vapor.

Optionally, the regeneration gas may include <NUM> wt% to <NUM> wt% of air, <NUM> wt% to <NUM> wt% of oxygen, <NUM> wt% to <NUM> wt% of nitrogen, and <NUM> wt% to <NUM> wt% of water vapor; and contents of the air, the oxygen, the nitrogen, and the water vapor may not be simultaneously zero.

Optionally, process operating conditions of the reaction zone II of the methanol conversion reactor may be as follows: apparent gas linear velocity: <NUM>/s to <NUM>/s; reaction temperature: <NUM> to <NUM>; reaction pressure: <NUM> kPa to <NUM> kPa; and bed density: <NUM>/m<NUM> to <NUM>/m<NUM>.

Optionally, process operating conditions of the spent catalyst zone of the methanol conversion reactor may be as follows: apparent gas linear velocity: <NUM>/s to <NUM>/s; reaction temperature: <NUM> to <NUM>; reaction pressure: <NUM> kPa to <NUM> kPa; and bed density: <NUM>/m<NUM> to <NUM>/m<NUM>.

Optionally, process operating conditions of the regenerator may be as follows: apparent gas linear velocity: <NUM>/s to <NUM>/s; regeneration temperature: <NUM> to <NUM>; regeneration pressure: <NUM> kPa to <NUM> kPa; and bed density: <NUM>/m<NUM> to <NUM>/m<NUM>.

In the present application, the "coke content" refers to a mass ratio of the coke species to the coke controlled catalyst.

Subscripts in C<NUM>-C<NUM> each represent the number of carbon atoms in a corresponding group, for example, C<NUM>-C<NUM> hydrocarbon compounds represent hydrocarbon compounds with <NUM> to <NUM> carbon atoms.

In the present application, when the unit consumption of production is expressed, a mass of DME in the oxygen-containing compound is equivalently converted into a mass of methanol based on a mass of the element C, and a unit of the unit consumption of production is ton of methanol/ton of light olefins.

In the method of the present application, the unit consumption of production may be <NUM> to <NUM> tons of methanol/ton of light olefins.

The riser reactor is similar to a plug flow reactor (PFR). Therefore, when the riser reactor is used for a coke control treatment of a catalyst, a narrow coke content distribution can be obtained. A residence time of a catalyst in the riser reactor is short, generally <NUM> second to <NUM> seconds. Therefore, it is difficult to greatly increase a coke content in a regenerated catalyst by treating the catalyst only with the riser reactor. The coke control reactor in the present application includes a riser reactor and a bed reactor. On the one hand, a catalyst with a narrow coke content distribution can be obtained through the advantages of the riser reactor; and on the other hand, the bed reactor is used to further increase a coke content in the catalyst and improve the selectivity for light olefins. A main feature of the bed reactor in the present application is that a perforated plate is arranged to inhibit the back-mixing of a catalyst among beds and improve the uniformity of coke distribution in the catalyst. The catalyst first enters an upper layer of the bed reactor from the riser reactor, gradually flows downward to a lower layer, and then enters the reaction zone II of the methanol conversion reactor from the lower layer.

Possible beneficial effects of the present application:.

<FIG> is a schematic structural diagram of a DMTO device for preparing light olefins from an oxygen-containing compound according to an embodiment of the present application.

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

A major characteristic of a DMTO catalyst is that the light olefin selectivity in a methanol conversion process increases with the increase of a coke content in the catalyst. The light olefins mentioned in the present application refer to ethylene and propylene.

The applicants have found through research that main factors affecting the activity of a DMTO catalyst and the selectivity of light olefins include coke content, coke content distribution, and coke species in the catalyst. Under the same average coke content in catalysts, the narrower the coke content distribution, the higher the selectivity and activity of light olefins. Coke species in a catalyst may include polymethyl aromatic hydrocarbons, polymethyl cycloalkanes, and the like, where polymethylbenzene and polymethylnaphthalene can promote the formation of ethylene. Therefore, the control of the coke content, coke content distribution, and coke species in a catalyst is the key to control the activity of the DMTO catalyst and improve the selectivity of light olefins.

In order to improve the performance of a DMTO catalyst, the present application provides a method for on-line modification of a DMTO catalyst through a coke control reaction, including the following steps:.

The regenerated catalyst may be a DMTO catalyst with a coke content of less than or equal to <NUM> wt%, and an active component of the DMTO catalyst may be an SAPO-<NUM> molecular sieve.

The coke control raw material may be composed of <NUM> wt% to <NUM> wt% of hydrogen, <NUM> wt% to <NUM> wt% of methane, <NUM> wt% to <NUM> wt% of ethane, <NUM> wt% to <NUM> wt% of ethylene, <NUM> wt% to <NUM> wt% of propane, <NUM> wt% to <NUM> wt% of propylene, <NUM> wt% to <NUM> wt% of butane, <NUM> wt% to <NUM> wt% of butene, <NUM> wt% to <NUM> wt% of pentane, <NUM> wt% to <NUM> wt% of pentene, <NUM> wt% to <NUM> wt% of hexane, <NUM> wt% to <NUM> wt% of hexene, <NUM> wt% to <NUM> wt% of methanol, <NUM> wt% to <NUM> wt% of ethanol, and <NUM> wt% to <NUM> wt% of water, and a total content of methanol, ethanol, and water may be greater than or equal to <NUM> wt%.

A reaction temperature of the coke control reaction may be <NUM> to <NUM>.

In the present application, both the bed reactor raw material and the riser reactor raw material are coke control raw materials.

According to an aspect of the present application, a method for preparing light olefins from an oxygen-containing compound that includes the method for on-line modification of a DMTO catalyst through a coke control reaction described above, and a device used thereby are provided. The device includes a coke control reactor (<NUM>), a methanol conversion reactor (<NUM>), and a regenerator (<NUM>).

A coke control reactor (<NUM>) for on-line modification of a DMTO catalyst is provided, where the coke control reactor (<NUM>) includes a riser reactor (<NUM>-<NUM>) and a bed reactor (<NUM>-<NUM>); the bed reactor (<NUM>-<NUM>) includes a bed reactor shell (<NUM>-<NUM>), a bed reactor distributor (<NUM>-<NUM>), a perforated plate (<NUM>-<NUM>), a bed reactor gas-solid cyclone separator (<NUM>-<NUM>), a bed reactor gas collection chamber (<NUM>-<NUM>), a coke control product gas delivery pipe (<NUM>-<NUM>), a coke controlled catalyst delivery pipe (<NUM>-<NUM>), and a coke controlled catalyst slide valve (<NUM>-<NUM>);.

In a preferred embodiment, the perforated plate may have a porosity of <NUM>% to <NUM>%.

A methanol conversion reactor (<NUM>) for preparing light olefins through methanol conversion, where the methanol conversion reactor (<NUM>) includes a methanol conversion reactor shell (<NUM>-<NUM>), a methanol conversion reactor distributor (<NUM>-<NUM>), a delivery pipe (<NUM>-<NUM>), a first gas-solid separation unit (<NUM>-<NUM>) of the methanol conversion reactor, a methanol conversion reactor gas collection chamber (<NUM>-<NUM>), a spent catalyst zone gas distributor (<NUM>-<NUM>), a methanol conversion reactor cooler (<NUM>-<NUM>), a second gas-solid separation unit (<NUM>-<NUM>) of the methanol conversion reactor, a product gas delivery pipe (<NUM>-<NUM>), a spent catalyst circulation pipe (<NUM>-<NUM>), a spent catalyst circulation slide valve (<NUM>-<NUM>), a spent catalyst inclined pipe (<NUM>-<NUM>), a methanol conversion reactor stripper (<NUM>-<NUM>), a spent catalyst slide valve (<NUM>-<NUM>), and a spent catalyst delivery pipe (<NUM>-<NUM>);.

In a preferred embodiment, the first gas-solid separation unit (<NUM>-<NUM>) of the methanol conversion reactor may adopt one or more sets of gas-solid cyclone separators, and each set of gas-solid cyclone separators may include a first-stage gas-solid cyclone separator and a second-stage gas-solid cyclone separator.

In a preferred embodiment, the second gas-solid separation unit (<NUM>-<NUM>) of the methanol conversion reactor may adopt one or more sets of gas-solid cyclone separators, and each set of gas-solid cyclone separators may include a first-stage gas-solid cyclone separator and a second-stage gas-solid cyclone separator.

The methanol conversion reactor (<NUM>) may be a fluidized bed reactor.

A regenerator (<NUM>) for regenerating a catalyst is provided, where the regenerator (<NUM>) includes a regenerator shell (<NUM>-<NUM>), a regenerator distributor (<NUM>-<NUM>), a regenerator gas-solid separation unit (<NUM>-<NUM>), a regenerator gas collection chamber (<NUM>-<NUM>), a flue gas delivery pipe (<NUM>-<NUM>), a regenerator stripper (<NUM>-<NUM>), a regenerator cooler (<NUM>-<NUM>), a regenerated catalyst slide valve (<NUM>-<NUM>), and a regenerated catalyst inclined pipe (<NUM>-<NUM>);.

In a preferred embodiment, the regenerator gas-solid separation unit (<NUM>-<NUM>) may adopt one or more sets of gas-solid cyclone separators, and each set of gas-solid cyclone separators may include a first-stage gas-solid cyclone separator and a second-stage gas-solid cyclone separator.

The regenerator (<NUM>) may be a fluidized bed reactor.

In the present application, an inner diameter of the transition zone of the coke control reactor gradually increases from bottom to top; in the methanol conversion reactor, an inner diameter of a junction between the reaction zone II and the delivery pipe gradually decreases from bottom to top; and an inner diameter of a junction between the reaction zone II and the spent catalyst zone gradually increases from bottom to top.

Optionally, an inlet of the coke controlled catalyst delivery pipe may be formed above the bed reactor distributor; an outlet of the coke controlled catalyst delivery pipe may be formed above the methanol conversion reactor distributor; an inlet of the spent catalyst circulation pipe may be formed above the spent catalyst zone gas distributor, and an outlet of the spent catalyst circulation pipe may be formed above the methanol conversion reactor distributor; and the spent catalyst inclined pipe may be located above the spent catalyst zone gas distributor.

According to another aspect of the present application, an MTO method including the method for on-line modification of a DMTO catalyst through a coke control reaction is also provided, including the following steps:.

In a preferred embodiment, the method of the present application may be implemented using the above-mentioned device including a coke control reactor (<NUM>), a methanol conversion reactor (<NUM>), and a regenerator (<NUM>).

In a preferred embodiment, a riser reactor raw material in the method may be composed of <NUM> wt% to <NUM> wt% of hydrogen, <NUM> wt% to <NUM> wt% of methane, <NUM> wt% to <NUM> wt% of ethane, <NUM> wt% to <NUM> wt% of ethylene, <NUM> wt% to <NUM> wt% of propane, <NUM> wt% to <NUM> wt% of propylene, <NUM> wt% to <NUM> wt% of butane, <NUM> wt% to <NUM> wt% of butene, <NUM> wt% to <NUM> wt% of pentane, <NUM> wt% to <NUM> wt% of pentene, <NUM> wt% to <NUM> wt% of hexane, <NUM> wt% to <NUM> wt% of hexene, <NUM> wt% to <NUM> wt% of methanol, <NUM> wt% to <NUM> wt% of ethanol, and <NUM> wt% to <NUM> wt% of water, and a total content of methanol, ethanol, and water may be greater than or equal to <NUM> wt%.

In a preferred embodiment, a bed reactor raw material in the method may be composed of <NUM> wt% to <NUM> wt% of hydrogen, <NUM> wt% to <NUM> wt% of methane, <NUM> wt% to <NUM> wt% of ethane, <NUM> wt% to <NUM> wt% of ethylene, <NUM> wt% to <NUM> wt% of propane, <NUM> wt% to <NUM> wt% of propylene, <NUM> wt% to <NUM> wt% of butane, <NUM> wt% to <NUM> wt% of butene, <NUM> wt% to <NUM> wt% of pentane, <NUM> wt% to <NUM> wt% of pentene, <NUM> wt% to <NUM> wt% of hexane, <NUM> wt% to <NUM> wt% of hexene, <NUM> wt% to <NUM> wt% of methanol, <NUM> wt% to <NUM> wt% of ethanol, and <NUM> wt% to <NUM> wt% of water, and a total content of methanol, ethanol, and water may be greater than or equal to <NUM> wt%.

In a preferred embodiment, the oxygen-containing compound in the method may be one from the group consisting of methanol, DME, and a mixture of methanol and DME.

In a preferred embodiment, the spent catalyst zone fluidizing gas in the method may be one from the group consisting of nitrogen, water vapor, and a mixture of nitrogen and water vapor.

In a preferred embodiment, the regeneration gas in the method may be <NUM> wt% to <NUM> wt% air, <NUM> wt% to <NUM> wt% oxygen, <NUM> wt% to <NUM> wt% nitrogen, and <NUM> wt% to <NUM> wt% water vapor.

In a preferred embodiment, an active component of the catalyst may be an SAPO-<NUM> molecular sieve.

In a preferred embodiment, a coke content in the regenerated catalyst may be less than or equal to <NUM> wt%.

In a preferred embodiment, a coke content in the coke controlled catalyst may be <NUM> wt% to <NUM> wt%, and a quartile deviation of coke content distribution may be less than <NUM> wt%; coke species may include polymethylbenzene and polymethylnaphthalene, and a total mass of the polymethylbenzene and the polymethylnaphthalene may account for greater than or equal to <NUM> wt% of a total mass of coke; and a mass of coke species with a molecular weight greater than <NUM> may account for less than or equal to <NUM> wt% of the total mass of coke.

In a preferred embodiment, a coke content in the spent catalyst may be <NUM> wt% to <NUM> wt%, and further preferably, the coke content in the spent catalyst may be <NUM> wt% to <NUM> wt%.

In a preferred embodiment, process operating conditions of the riser reactor (<NUM>-<NUM>) may be as follows: apparent gas linear velocity: <NUM>/s to <NUM>/s; reaction temperature: <NUM> to <NUM>; reaction pressure: <NUM> kPa to <NUM> kPa; and bed density: <NUM>/m<NUM> to <NUM>/m<NUM>.

In a preferred embodiment, process operating conditions of the reaction zone of the bed reactor (<NUM>-<NUM>) may be as follows: apparent gas linear velocity: <NUM>/s to <NUM>/s; reaction temperature: <NUM> to <NUM>; reaction pressure: <NUM> kPa to <NUM> kPa; and bed density: <NUM>/m<NUM> to <NUM>/m<NUM>.

In a preferred embodiment, process operating conditions of the reaction zone of the methanol conversion reactor (<NUM>) may be as follows: apparent gas linear velocity: <NUM>/s to <NUM>/s; reaction temperature: <NUM> to <NUM>; reaction pressure: <NUM> kPa to <NUM> kPa; and bed density: <NUM>/m<NUM> to <NUM>/m<NUM>.

In a preferred embodiment, process operating conditions of the spent catalyst zone of the methanol conversion reactor (<NUM>) may be as follows: apparent gas linear velocity: <NUM>/s to <NUM>/s; reaction temperature: <NUM> to <NUM>; reaction pressure: <NUM> kPa to <NUM> kPa; and bed density: <NUM>/m<NUM> to <NUM>/m<NUM>.

In a preferred embodiment, process operating conditions of the regenerator (<NUM>) may be as follows: apparent gas linear velocity: <NUM>/s to <NUM>/s; regeneration temperature: <NUM> to <NUM>; regeneration pressure: <NUM> kPa to <NUM> kPa; and bed density: <NUM>/m<NUM> to <NUM>/m<NUM>.

In the method of the present application, the product gas may be composed of <NUM> wt% to <NUM> wt% of ethylene, <NUM> wt% to <NUM> wt% of propylene, less than or equal to 4wt% of C<NUM>-C<NUM> hydrocarbon compounds, and less than or equal to <NUM> wt% of other components; and the other components may be methane, ethane, propane, hydrogen, CO, CO<NUM>, and the like, and the total selectivity of ethylene and propylene in the product gas may be <NUM> wt% to <NUM> wt%.

In this example, the device shown in <FIG> is adopted, where there is no perforated plate in the bed reactor.

In this example, the riser reactor raw material is a mixture of <NUM> wt% of butane, <NUM> wt% of butene, <NUM> wt% of methanol, and <NUM> wt% of water; the bed reactor raw material is a mixture of <NUM> wt% of butane, <NUM> wt% of butene, <NUM> wt% of methanol, and <NUM> wt% of water; the oxygen-containing compound is methanol; the spent catalyst zone fluidizing gas is nitrogen; the regeneration gas is air; an active component in the catalyst is an SAPO-<NUM> molecular sieve; a coke content in the regenerated catalyst is about <NUM> wt%; a coke content in the coke controlled catalyst is about <NUM> wt%, where a total mass of polymethylbenzene and polymethylnaphthalene accounts for about <NUM> wt% of a total mass of coke, a mass of coke species with a molecular weight greater than <NUM> accounts for about <NUM> wt% of a total mass of coke, and a quartile deviation of coke content distribution in the coke controlled catalyst is about <NUM> wt%; a coke content in the spent catalyst is about <NUM> wt%; process operating conditions of the riser reactor (<NUM>-<NUM>) are as follows: apparent gas linear velocity: <NUM>/s, reaction temperature: <NUM>, reaction pressure: <NUM> kPa, and bed density: <NUM>/m<NUM>; process operating conditions of the reaction zone of the bed reactor (<NUM>-<NUM>) are as follows: apparent gas linear velocity: about <NUM>/s, reaction temperature: about <NUM>, reaction pressure: about <NUM> kPa, and bed density: about <NUM>/m<NUM>; process operating conditions of the reaction zone of the methanol conversion reactor (<NUM>) are as follows: apparent gas linear velocity: about <NUM>/s, reaction temperature: about <NUM>, reaction pressure: about <NUM> kPa, and bed density: about <NUM>/m<NUM>; process operating conditions of the spent catalyst zone of the methanol conversion reactor (<NUM>) are as follows: apparent gas linear velocity: about <NUM>/s, reaction temperature: about <NUM>, reaction pressure: about <NUM> kPa, and bed density: about <NUM>/m<NUM>; and process operating conditions of the regenerator (<NUM>) are as follows: apparent gas linear velocity: about <NUM>/s, regeneration temperature: about <NUM>, regeneration pressure: about <NUM> kPa, and bed density: about <NUM>/m<NUM>.

In this example, a WHSV of the oxygen-containing compound in the methanol conversion reactor is about <NUM>-<NUM>; the product gas is composed of <NUM> wt% of ethylene, <NUM> wt% of propylene, <NUM> wt% of C<NUM>-C<NUM> hydrocarbon compounds, and <NUM> wt% of other components, where the other components include methane, ethane, propane, hydrogen, CO, CO<NUM>, and the like; and the unit consumption of production is <NUM> tons of methanol/ton of light olefins.

In this example, the device shown in <FIG> is adopted, where there are <NUM> perforated plates in the bed reactor, and the perforated plates have a porosity of <NUM>%.

In this example, the riser reactor raw material is a mixture of <NUM> wt% of methane, <NUM> wt% of ethane, <NUM> wt% of ethylene, <NUM> wt% of propane, <NUM> wt% of propylene, <NUM> wt% of hydrogen, and <NUM> wt% of water; the bed reactor raw material is a mixture of <NUM> wt% of methane, <NUM> wt% of ethane, <NUM> wt% of ethylene, <NUM> wt% of propane, <NUM> wt% of propylene, <NUM> wt% of hydrogen, and <NUM> wt% of water; the oxygen-containing compound is a mixture of <NUM> wt% of methanol and <NUM> wt% of DME; the spent catalyst zone fluidizing gas is water vapor; the regeneration gas is a mixture of <NUM> wt% of air and <NUM> wt% of water vapor; an active component in the catalyst is an SAPO-<NUM> molecular sieve; a coke content in the regenerated catalyst is about <NUM> wt%; a coke content in the coke controlled catalyst is about <NUM> wt%, where a total mass of polymethylbenzene and polymethylnaphthalene accounts for about <NUM> wt% of a total mass of coke, a mass of coke species with a molecular weight greater than <NUM> accounts for about <NUM> wt% of a total mass of coke, and a quartile deviation of coke content distribution in the coke controlled catalyst is about <NUM> wt%; a coke content in the spent catalyst is about <NUM> wt%; process operating conditions of the riser reactor (<NUM>-<NUM>) are as follows: apparent gas linear velocity: <NUM>/s, reaction temperature: <NUM>, reaction pressure: <NUM> kPa, and bed density: <NUM>/m<NUM>; process operating conditions of the reaction zone of the bed reactor (<NUM>-<NUM>) are as follows: apparent gas linear velocity: about <NUM>/s, reaction temperature: about <NUM>, reaction pressure: about <NUM> kPa, and bed density: about <NUM>/m<NUM>; process operating conditions of the reaction zone of the methanol conversion reactor (<NUM>) are as follows: apparent gas linear velocity: about <NUM>/s, reaction temperature: about <NUM>, reaction pressure: about <NUM> kPa, and bed density: about <NUM>/m<NUM>; process operating conditions of the spent catalyst zone of the methanol conversion reactor (<NUM>) are as follows: apparent gas linear velocity: about <NUM>/s, reaction temperature: about <NUM>, reaction pressure: about <NUM> kPa, and bed density: about <NUM>/m<NUM>; and process operating conditions of the regenerator (<NUM>) are as follows: apparent gas linear velocity: about <NUM>/s, regeneration temperature: about <NUM>, regeneration pressure: about <NUM> kPa, and bed density: about <NUM>/m<NUM>.

In this example, the riser reactor raw material is a mixture of <NUM> wt% of propane, <NUM> wt% of propylene, <NUM> wt% of butane, <NUM> wt% of butene, <NUM> wt% of pentane, <NUM> wt% of pentene, <NUM> wt% of hexane, <NUM> wt% of hexene, <NUM> wt% of methanol, and <NUM> wt% of water; the bed reactor raw material is a mixture of <NUM> wt% of propane, <NUM> wt% of propylene, <NUM> wt% of butane, <NUM> wt% of butene, <NUM> wt% of pentane, <NUM> wt% of pentene, <NUM> wt% of hexane, <NUM> wt% of hexene, <NUM> wt% of methanol, and <NUM> wt% of water; the oxygen-containing compound is DME; the spent catalyst zone fluidizing gas is a mixture of <NUM> wt% of nitrogen and <NUM> wt% of water vapor; the regeneration gas is a mixture of <NUM> wt% of air and <NUM> wt% of oxygen; an active component in the catalyst is an SAPO-<NUM> molecular sieve; a coke content in the regenerated catalyst is about <NUM> wt%; a coke content in the coke controlled catalyst is about <NUM> wt%, where a total mass of polymethylbenzene and polymethylnaphthalene accounts for about <NUM> wt% of a total mass of coke, a mass of coke species with a molecular weight greater than <NUM> accounts for about <NUM> wt% of a total mass of coke, and a quartile deviation of coke content distribution in the coke controlled catalyst is about <NUM> wt%; a coke content in the spent catalyst is about <NUM> wt%; process operating conditions of the riser reactor (<NUM>-<NUM>) are as follows: apparent gas linear velocity: <NUM>/s, reaction temperature: <NUM>, reaction pressure: <NUM> kPa, and bed density: <NUM>/m<NUM>; process operating conditions of the reaction zone of the bed reactor (<NUM>-<NUM>) are as follows: apparent gas linear velocity: about <NUM>/s, reaction temperature: about <NUM>, reaction pressure: about <NUM> kPa, and bed density: about <NUM>/m<NUM>; process operating conditions of the reaction zone of the methanol conversion reactor (<NUM>) are as follows: apparent gas linear velocity: about <NUM>/s, reaction temperature: about <NUM>, reaction pressure: about <NUM> kPa, and bed density: about <NUM>/m<NUM>; process operating conditions of the spent catalyst zone of the methanol conversion reactor (<NUM>) are as follows: apparent gas linear velocity: about <NUM>/s, reaction temperature: about <NUM>, reaction pressure: about <NUM> kPa, and bed density: about <NUM>/m<NUM>; and process operating conditions of the regenerator (<NUM>) are as follows: apparent gas linear velocity: about <NUM>/s, regeneration temperature: about <NUM>, regeneration pressure: about <NUM> kPa, and bed density: about <NUM>/m<NUM>.

In this example, the riser reactor raw material is a mixture of <NUM> wt% of butane, <NUM> wt% of butene, <NUM> wt% of methanol, and <NUM> wt% of water; the bed reactor raw material is a mixture of <NUM> wt% of butane, <NUM> wt% of butene, <NUM> wt% of methanol, and <NUM> wt% of water; the oxygen-containing compound is methanol; the spent catalyst zone fluidizing gas is a mixture of <NUM> wt% of nitrogen and <NUM> wt% of water vapor; the regeneration gas is a mixture of <NUM> wt% of air and <NUM> wt% of nitrogen; an active component in the catalyst is an SAPO-<NUM> molecular sieve; a coke content in the regenerated catalyst is about <NUM> wt%; a coke content in the coke controlled catalyst is about <NUM> wt%, where a total mass of polymethylbenzene and polymethylnaphthalene accounts for about <NUM> wt% of a total mass of coke, a mass of coke species with a molecular weight greater than <NUM> accounts for about <NUM> wt% of a total mass of coke, and a quartile deviation of coke content distribution in the coke controlled catalyst is about <NUM> wt%; a coke content in the spent catalyst is about <NUM> wt%; process operating conditions of the riser reactor (<NUM>-<NUM>) are as follows: apparent gas linear velocity: <NUM>/s, reaction temperature: <NUM>, reaction pressure: <NUM> kPa, and bed density: <NUM>/m<NUM>; process operating conditions of the reaction zone of the bed reactor (<NUM>-<NUM>) are as follows: apparent gas linear velocity: about <NUM>/s, reaction temperature: about <NUM>, reaction pressure: about <NUM> kPa, and bed density: about <NUM>/m<NUM>; process operating conditions of the reaction zone of the methanol conversion reactor (<NUM>) are as follows: apparent gas linear velocity: about <NUM>/s, reaction temperature: about <NUM>, reaction pressure: about <NUM> kPa, and bed density: about <NUM>/m<NUM>; process operating conditions of the spent catalyst zone of the methanol conversion reactor (<NUM>) are as follows: apparent gas linear velocity: about <NUM>/s, reaction temperature: about <NUM>, reaction pressure: about <NUM> kPa, and bed density: about <NUM>/m<NUM>; and process operating conditions of the regenerator (<NUM>) are as follows: apparent gas linear velocity: about <NUM>/s, regeneration temperature: about <NUM>, regeneration pressure: about <NUM> kPa, and bed density: about <NUM>/m<NUM>.

This example is a comparative example and is different from Example <NUM> in that, the coke control reaction is not used for on-line modification of the DMTO catalyst; and the raw material fed into the riser reactor and the bed reactor is nitrogen, which is an inert gas and does not change the properties of the regenerated catalyst in the riser reactor and the bed reactor, that is, a catalyst entering the reaction zone II of the methanol conversion reactor is the regenerated catalyst.

In this example, the product gas is composed of <NUM> wt% of ethylene, <NUM> wt% of propylene, <NUM> wt% of C<NUM>-C<NUM> hydrocarbon compounds, and <NUM> wt% of other components, where the other components include methane, ethane, propane, hydrogen, CO, CO<NUM>, and the like; and the unit consumption of production is <NUM> tons of methanol/ton of light olefins.

This comparative example shows that the on-line modification of a DMTO catalyst through a coke control reaction can greatly improve the performance of the catalyst and reduce the unit consumption of production.

Claim 1:
A coke control reactor (<NUM>), wherein the coke control reactor comprises a riser reactor (<NUM>-<NUM>) and a bed reactor (<NUM>-<NUM>), an upper section of the riser reactor penetrates through a bottom of the bed reactor and is axially inserted in the bed reactor;
the bed reactor comprises a bed reactor shell (<NUM>-<NUM>), and characterized in that the bed reactor shell encloses a reaction zone I, a transition zone, and a gas-solid separation zone I from bottom to top, the transition zone has a diameter gradually increasing from bottom to top such that a bottom of the transition zone is connected to a top of the reaction zone I and a top of the transition zone is connected to a bottom of the gas-solid separation zone I;
a bed reactor distributor (<NUM>-<NUM>) is arranged in an inner lower part of the reaction zone I;
a coke controlled catalyst delivery pipe (<NUM>-<NUM>) is arranged outside the reaction zone I and configured to deliver a coke controlled catalyst to a next-level reactor; and
an outlet end of the riser reactor is located in the transition zone;
wherein at least one perforated plate (<NUM>-<NUM>) is arranged in the reaction zone I; the plurality of perforated plates is axially arranged on a periphery of the riser reactor in sequence;
the outlet end of the riser reactor is located above the perforated plate;
the bed reactor distributor is located below the perforated plate;
preferably, the perforated plate has a porosity of <NUM>% to <NUM>%.