CN110818521A - Device and method for preparing aromatic hydrocarbon and low-carbon olefin by using oxygen-containing compound - Google Patents
Device and method for preparing aromatic hydrocarbon and low-carbon olefin by using oxygen-containing compound Download PDFInfo
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- CN110818521A CN110818521A CN201810888053.XA CN201810888053A CN110818521A CN 110818521 A CN110818521 A CN 110818521A CN 201810888053 A CN201810888053 A CN 201810888053A CN 110818521 A CN110818521 A CN 110818521A
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C1/00—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon
- C07C1/20—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon starting from organic compounds containing only oxygen atoms as heteroatoms
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2/00—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms
- C07C2/54—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by addition of unsaturated hydrocarbons to saturated hydrocarbons or to hydrocarbons containing a six-membered aromatic ring with no unsaturation outside the aromatic ring
- C07C2/64—Addition to a carbon atom of a six-membered aromatic ring
- C07C2/66—Catalytic processes
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
- Y02P30/40—Ethylene production
Abstract
The invention discloses a device for preparing aromatic hydrocarbon and olefin by using oxygen-containing compounds in the field of petrochemical industry, which comprises a reactor, a regenerator, an external heat remover, a spent stripper and a regenerated stripper, and is characterized in that: the reactor comprises a first reactor and a second reactor, and a spent catalyst circulating pipe is arranged between the first reactor and the second reactor; the first reactor and the second reactor are coaxially arranged and are arranged in parallel with the regenerator, and the second reactor is higher than the regenerator; and feeding distributors are arranged at the bottoms of the first reactor and the second reactor, and raw materials are introduced into the feeding distributors for distribution. The device provided by the invention can improve the selectivity of target products to the maximum extent, such as the selectivity and yield of gasoline or aromatic hydrocarbon products; the problems of high bed layer and difficult fluidization of the catalyst in the reactor and the regenerator are solved, and the fluidization state is maintained; can meet the requirements of reaction regeneration conditions of the MTA process.
Description
Technical Field
The invention relates to the technical field of hydrocarbon preparation from one or more non-hydrocarbon compounds, in particular to a device and a method for preparing aromatic hydrocarbon and low-carbon olefin from oxygen-containing compounds.
Background
Ethylene, propylene and aromatic hydrocarbons (especially benzene, toluene and xylene, BTX) are important basic organic chemicals. At present, paraxylene is mainly obtained by an aromatic hydrocarbon combination device, naphtha is firstly reformed to prepare reformed oil containing aromatic hydrocarbon, and then the paraxylene product is obtained to the maximum extent by units such as aromatic hydrocarbon extraction, aromatic hydrocarbon fractionation, disproportionation, transalkylation, xylene isomerization, adsorption separation and the like. Because the content of the p-xylene in the three isomers is controlled by thermodynamics, the p-xylene only accounts for about 23 percent in the C8 mixed aromatic hydrocarbon, the material circulating treatment capacity in the whole p-xylene production process is large, the equipment is huge, and the operation cost is high. In particular, the difference in boiling points of the three isomers of xylene is small, and high purity para-xylene cannot be obtained by a conventional distillation technique, but an expensive adsorption separation process must be used. In order to avoid the trouble and technical obstacles of xylene separation, there is a need to develop catalysts and process technologies with para-xylene selectivity approaching 100%, which is a new way to radically improve the para-xylene production process.
Toluene shape selective disproportionation and toluene methanol alkylation are new technologies for producing p-xylene with high selectivity by shape selection of a catalyst, wherein the reaction condition for producing p-xylene by toluene methanol alkylation is mild, and methanol which is a non-petroleum product can be used as a raw material, so that organic combination of petrochemical industry and coal chemical industry is realized, the technology is an important new route, and has already attracted the interest of many researchers at home and abroad, but no large-scale production device is published in the world at present. This process is attractive because it doubles the yield of the toluene disproportionation process and has many advantages: (1) the amount of toluene required per ton of p-xylene can be reduced from about 2 tons to 1 ton of toluene shape selective disproportionation method; (2) the methanol is easy to obtain and is relatively cheap; (3) the production of benzene is very small. Therefore, the alkylation of toluene with methanol to produce p-xylene will be the most economically feasible technical route for producing p-xylene in the future and is a new process with the greatest development prospect.
The selective alkylation of toluene and methanol utilizes the toluene resource which is surplus in the market and the cheap methanol resource which is produced by a non-petroleum route to produce the p-xylene with high selectivity, the breakthrough of the technology and the industrial application can not only relieve the huge supply and demand contradiction of the market, but also avoid the adsorption separation technology with huge investment in the production of the high-selectivity p-xylene, and the high-purity p-xylene product can be obtained through crystallization separation, which will bring about great change in the production industry of the p-xylene. For decades, many research institutes and large companies at home and abroad invest a lot of manpower and material resources to carry out a lot of research work on the catalyst and the process of the technology, but unfortunately, the industrial application of the technology still faces a lot of technical difficulties. Therefore, under the push of huge market demand and technology development, accelerating the development of high-level catalysts of the technology and process technology research will still have important significance.
In recent years, the methods for producing aromatic hydrocarbons and light olefins from oxygenates have become the focus and focus of research by those skilled in the art. People have conducted extensive research and exploration in the aspects of process flows, equipment structures and the like.
The invention discloses a fluidized bed reaction regeneration device, which belongs to the technical field of petrochemical and coal chemical equipment and is used for producing low-carbon olefin, gasoline and aromatic hydrocarbon by using methanol as a raw material. The device includes reactor, regenerator, catalyst strip conveyer pipe and regenerator outer heat collector, and this utility model adopts the air lift to wait to give birth to the catalyst conveyer pipe, and it is connected with the reactor to wait to give birth to strip section upper portion, simultaneously through hot regenerant pipe and regenerant strip section sub-unit connection. The spent catalyst is conveyed without nitrogen or steam, so that the energy consumption can be reduced; the high-temperature regenerated catalyst is doped in the spent catalyst, so that the temperature can be increased, and the stripping efficiency can be improved. Is applied to the comprehensive utilization of methanol. The invention has the problems that a small amount of oil gas is possibly carried in the high-temperature spent catalyst from the reactor due to poor stripping effect, if air is adopted to lift the spent catalyst conveying pipe, the spent catalyst generates tail combustion, and the spent catalyst conveying pipe is in partial overheating risk.
CN104177210A discloses a method for co-producing olefin and aromatic hydrocarbon with alcohol ether compounds, the invention relates to the field of basic chemical industry, in particular to a method for co-producing olefin and aromatic hydrocarbon with alcohol ether compounds, which comprises the following steps: (1) taking alcohol or/and ether compounds as raw materials, and carrying out chemical reaction for generating olefin in a first fluidized bed reactor; (2) separating a target olefin product from mixed gas at an outlet of the first fluidized bed reactor; part of the by-products enter a second reactor to carry out chemical reaction for generating mixed aromatic hydrocarbon; (3) and separating out mixed aromatic hydrocarbon and a target olefin product from the mixed gas at the outlet of the second reactor, and circulating part of by-products to the second reactor to continue the chemical reaction for generating the mixed aromatic hydrocarbon. The invention comprises two reactors, wherein the two reactors respectively carry out alcohol ether-to-olefin reaction and low-carbon hydrocarbon aromatization reaction under the action of two catalysts, and alcohol ether raw materials are converted into olefin and aromatic hydrocarbon products with high selectivity through specific selection of the catalysts, the reactor forms and the operation conditions. The problem with this invention is that two different types of catalysts are used and the regeneration of the catalyst is carried out in two regenerators independently or in different zones of one regenerator.
Chinese patent CN104557365A discloses a coaxial fluidized bed reaction system and a reaction method thereof for preparing ethylene, propylene and aromatic hydrocarbon by converting methanol and/or dimethyl ether, and relates to a coaxial fluidized bed reaction system and a method thereof for preparing ethylene, propylene and aromatic hydrocarbon by converting methanol and/or dimethyl ether, which mainly solve the problem of low yield of ethylene, propylene and aromatic hydrocarbon in the prior art. The invention adopts the technical scheme that a system comprises a reactor (1), a regenerator (2) and a stripper (3), raw materials (15) enter the reactor (1) from the lower part of a reactor reaction section (24) to be in contact reaction with a catalyst, the reacted carbon-deposited catalyst descends into a to-be-regenerated inclined pipe (7) connected with the bottom of the reactor (1), then is lifted to the stripper (3) through a stripping vertical pipe (8), the stripped catalyst enters the regenerator (2) to be regenerated, and the regenerated catalyst descends to the reactor reaction section (24) through degassing of a degassing tank (4). The invention has the problems that the reactor is a single reactor, and the catalyst bed layer is high, and the fluidization is difficult.
Chinese patent CN106794437A discloses an apparatus and process for producing gasoline, olefin and aromatic compounds from oxygenates, which invention provides an apparatus and process for converting oxygenate feedstocks such as methanol and dimethyl ether to hydrocarbons such as gasoline boiling components, olefin and aromatic compounds in a fluidized bed containing a catalyst. The invention has the problems that the reactor is a single reactor, and the catalyst bed layer is high, and the fluidization is difficult.
In summary, in the prior art, the product selectivity is improved to a certain extent by optimizing the internal structure of the reactor, optimizing the process flow and optimizing the operating conditions, but the device type in the prior art has the problems of high catalyst bed layer, difficult catalyst fluidization, difficult heat extraction and large selectivity in the reactor and the regenerator, and the invention specifically solves the problems.
Disclosure of Invention
The invention provides a device and a method for preparing aromatic hydrocarbon and low-carbon olefin by using an oxygen-containing compound, which are suitable for the characteristics of high temperature, pressurization, strong heat release, high conversion rate requirement, product selectivity requirement and the like of a process for preparing aromatic hydrocarbon and low-carbon olefin by using the oxygen-containing compound, and are used for solving the problems of high catalyst bed height, difficult fluidization, different gas circulation requirement conditions and the like in the prior art, exerting the advantages of respective reaction to the greatest extent and improving the selectivity of target products.
In order to solve the technical problems, the technical scheme adopted by the invention is as follows:
a device for preparing aromatic hydrocarbon and low-carbon olefin by using oxygen-containing compounds comprises a reactor, a regenerator, an external heat collector, a spent stripper and a regenerated stripper, and is characterized in that: the reactor comprises a first reactor and a second reactor, the regenerator is connected with the first reactor through a regeneration stripper, a regeneration slide valve and a regenerated catalyst conveying pipe, and the regenerated catalyst conveying pipe extends into the first reactor; the first reactor is communicated with the second reactor; the stripper to be regenerated is respectively communicated with the bottoms of the second reactor and the regenerator; the regeneration stripper is communicated with the first reactor through a regeneration slide valve and a regeneration catalyst conveying pipe; an external heat collector is arranged in the second reactor and communicated with the second reactor; a spent catalyst circulating pipe is arranged between the first reactor and the second reactor; the first reactor and the second reactor are coaxially arranged and are arranged in parallel with the regenerator, and the second reactor is higher than the first reactor; and feeding distributors are arranged at the bottoms of the first reactor and the second reactor, and raw materials are introduced into the feeding distributors for distribution.
The invention relates to a device for preparing aromatic hydrocarbon and low-carbon olefin by using oxygen-containing compounds, which is further characterized in that: the regenerated catalyst transfer line may be used as a riser reactor. When light hydrocarbon is recycled, gas (C) is returned4~C8Gas), the regenerated catalyst conveying pipe is used as a riser reactor, and the riser reactor is fed with preferably light hydrocarbon return gas (C)4~C8Gas), the light hydrocarbon return gas may beOne or more streams are injected into the upper, middle or lower portion of the riser reactor. When the light hydrocarbon is not recycled, the gas (C) is returned4~C8Gas), the regenerated catalyst transport pipe is used only to transport the regenerated catalyst, and the transport medium is preferably steam.
The invention relates to a device for preparing aromatic hydrocarbon and low-carbon olefin by using oxygen-containing compounds, which is further characterized in that: the external heat collector is connected with the second reactor through an external heat outlet inlet pipe, and the catalyst enters the external heat collector through the external heat outlet inlet pipe to be heated and returns to the reactor.
The invention relates to a device for preparing aromatic hydrocarbon and low-carbon olefin by using oxygen-containing compounds, which is further characterized in that: the spent catalyst circulating pipe is an external circulating pipe, the inlet of the external circulating pipe is connected with the middle part and the lower part of the second reactor, and the outlet of the external circulating pipe is connected with the lower part of the first reactor. A slide valve is arranged on the spent catalyst circulating pipe. The spent catalyst circulating pipe is an internal circulating pipe which is arranged in the middle of the first reactor and is coaxially arranged with the first reactor, an inlet is connected with the bottom of the second reactor, and an outlet is connected with the bottom of the first reactor. A plug valve is arranged on the spent catalyst circulating pipe and is positioned at the bottom of the first reactor.
The invention relates to a device for preparing aromatic hydrocarbon and low-carbon olefin by using oxygen-containing compounds, which is further characterized in that: the first reactor and the second reactor are both fluidized bed reactors, the second reactor is preferably a turbulent bed reactor, and the first reactor can be a fast bed reactor or a turbulent bed reactor. Raw materials are respectively fed into each reactor according to the reaction requirements, and the raw materials fed into the first reactor can be mixed feed of oxygen-containing compounds and aromatic hydrocarbons, or mixed feed of light hydrocarbon return gas, oxygen-containing compounds and aromatic hydrocarbons, preferably mixed feed of oxygen-containing compounds and aromatic hydrocarbons; the oxygen-containing compound such as light hydrocarbon gas, methanol, dimethyl ether and the like or the mixture of the two can also enter the second reactor, and the oxygen-containing compound is preferred.
The invention relates to a device for preparing aromatic hydrocarbon and low-carbon olefin by using oxygen-containing compounds, which is further characterized in that: the first reactor and the second reactor are connected through a gas-solid distributor or a pipeline.
The invention relates to a device for preparing aromatic hydrocarbon and low-carbon olefin by using oxygen-containing compounds, which is further characterized in that: one end of the spent stripper is communicated with the bottom of the second reactor through a spent agent inlet pipe, and the other end of the spent stripper is communicated with the regenerator through a spent agent conveying pipe. A slide valve is arranged on the spent agent conveying pipe. One end of the regeneration stripper is communicated with the bottom of the regenerator, the other end of the regeneration stripper is communicated with the first reactor through a regenerated catalyst conveying pipe, and a slide valve is arranged on the regenerated catalyst conveying pipe.
The invention relates to a device for preparing aromatic hydrocarbon and low-carbon olefin by using oxygen-containing compounds, which is further characterized in that: the spent stripper is internally provided with a stripping grating or a stripping baffle and a stripping medium distributor. The regeneration stripper is internally provided with a stripping grid or a stripping baffle and a stripping medium distributor.
The invention relates to a device for preparing aromatic hydrocarbon and low-carbon olefin by using oxygen-containing compounds, which is further characterized in that: the feed distributor is positioned at the bottom of the reactor and is a distribution pipe or a distribution plate, preferably a distribution pipe.
The invention relates to a device for preparing aromatic hydrocarbon and low-carbon olefin by using oxygen-containing compounds, which is further characterized in that: the interior of the second reactor is divided into a reactor dilute phase section, a reactor transition section and a reactor dense phase section from top to bottom.
The invention relates to a device for preparing aromatic hydrocarbon and low-carbon olefin by using oxygen-containing compounds, which is further characterized in that: and a gas-solid separation facility is arranged in the second reactor, an oil-gas collection chamber is arranged at the top of the second reactor, and the gas-solid separation facility is introduced into the oil-gas collection chamber.
The invention relates to a device for preparing aromatic hydrocarbon and low-carbon olefin by using oxygen-containing compounds, which is further characterized in that: the gas-solid separation device is a primary cyclone separator and a secondary cyclone separator, and the secondary cyclone separator is introduced into the oil gas collection chamber.
The invention relates to a device for preparing aromatic hydrocarbon and low-carbon olefin by using oxygen-containing compounds, which is further characterized in that: a third cyclone, preferably external, is provided outside or inside the second reactor. Is coaxial with the reactor when being arranged in the second reactor; the reactor three-stage cyclone separator can be vertical or horizontal.
The invention relates to a device for preparing aromatic hydrocarbon and low-carbon olefin by using oxygen-containing compounds, which is further characterized in that: and a reactor fourth-stage cyclone separator is arranged outside the second reactor, one end of the reactor fourth-stage cyclone separator is communicated with the reactor third-stage cyclone separator, and the other end of the reactor fourth-stage cyclone separator is communicated with a reactor third-stage recovery catalyst storage tank.
The invention relates to a device for preparing aromatic hydrocarbon and low-carbon olefin by using oxygen-containing compounds, which is further characterized in that: the regenerator is a fluidized bed regenerator. The regenerator is internally divided into a regenerator dilute phase section, a regenerator transition section and a regenerator coking section. The regenerator char section may be a turbulent bed or a fast bed or a combination of both.
The invention relates to a device for preparing aromatic hydrocarbon and low-carbon olefin by using oxygen-containing compounds, which is further characterized in that: the dilute phase section of the regenerator is provided with a gas-solid separation device, the top of the dilute phase section is provided with a flue gas outlet, the regeneration and burning section is provided with a main air distributor, and the bottom of the regenerator is provided with a main air inlet. The main wind distributor can be a distribution pipe or/and a distribution plate, preferably a distribution pipe. Not only the main wind is evenly distributed and is wear-resistant, but also the service life is long.
The invention relates to a device for preparing aromatic hydrocarbon and low-carbon olefin by using oxygen-containing compounds, which is further characterized in that: the regenerator is a fluidized bed regenerator, preferably a turbulent fluidized bed regenerator.
The invention relates to a device for preparing aromatic hydrocarbon and low-carbon olefin by using oxygen-containing compounds, which is further characterized in that: the gas-solid separation device in the regenerator is preferably a cyclone separator, and the cyclone separator is 1-3 grade.
The catalyst in the regenerator of the present invention can be regenerated completely or incompletely, preferably completely.
The invention relates to a device for preparing aromatic hydrocarbon and low-carbon olefin by using oxygen-containing compounds, which is further characterized in that: and heat taking facilities are arranged in the regenerator, the first reactor and the second reactor.
The invention relates to a device for preparing aromatic hydrocarbon and low-carbon olefin by using oxygen-containing compounds, which is further characterized in that: arranging internal and/or heat-taking facilities in the first reactor and the second reactor, wherein the internal heat-taking and heat-taking medium can be one or more of an oxygen-containing compound raw material, water, an inert medium and heat conducting oil, preferably, the oxygen-containing compound raw material is used as the heat-taking medium, the oxygen-containing compound raw material is preferably a liquid-phase raw material, and the temperature can be within the range of 25-200 ℃, preferably, within the range of 25-150 ℃; the internal heat extraction facility is arranged at the middle lower part of the reaction section of each reactor and above the feeding distributor of the reactor. The external heat-removal means may be provided in consideration of the fact that the lower catalyst is returned to any of the upper, middle and lower portions of the first reactor, preferably the middle portion. And an external heat taking facility is arranged in the second reactor, and the heat taking medium is preferably deoxygenated water so as to generate steam with different grades.
The invention relates to a device for preparing aromatic hydrocarbon and low-carbon olefin by using oxygen-containing compounds, which is further characterized in that: and an external heat taking facility is arranged in the regenerator, and the heat taking medium is preferably deoxygenated water which is used for generating medium-pressure steam.
The invention relates to a device for preparing aromatic hydrocarbon and low-carbon olefin by using oxygen-containing compounds, which is further characterized in that: the first reactor, the second reactor and the regenerator are all high beds, and the ratio of the height of the catalyst bed in the dense-phase section of the reactor to the diameter of the dense-phase section of the reactor is within the range of 0.5-20.0, preferably within the range of 1-10. The ratio of the height of the catalyst bed in the dense phase section of the regenerator to the diameter of the dense phase section of the regenerator is in the range of 0.5 to 30.0, preferably in the range of 1 to 20.
The reactor of the device for preparing the aromatic hydrocarbon and the low-carbon olefin by using the oxygen-containing compound is a multistage series reactor and comprises a first reactor and a second reactor, wherein the reactors can be fast bed reactors or turbulent beds, and the first reactor and the second reactor can be connected by a gas-solid distributor. Raw materials are respectively fed into each reactor according to reaction requirements, and the raw materials can be mixed feed of oxygen-containing compounds, methylbenzene and/or benzene or mixed feed of light hydrocarbon return gas, oxygen-containing compounds, methylbenzene and/or benzene, preferably the mixed feed of the oxygen-containing compounds and the methylbenzene and/or benzene, which is fed into the first reactor; the oxygen-containing compounds such as light hydrocarbon gas, methanol, dimethyl ether and the like or the mixture of the light hydrocarbon gas, the methanol, the dimethyl ether and the like can also enter the second reactor. Oxygen-containing compounds are preferred.
The invention also provides a method for preparing aromatic hydrocarbon and low-carbon olefin by using the oxygen-containing compound, which is carried out by using the device for preparing aromatic hydrocarbon and low-carbon olefin by using the oxygen-containing compound, and the method specifically comprises the following steps:
a method for preparing aromatic hydrocarbon and low-carbon olefin by using oxygen-containing compounds is characterized by comprising the following steps:
1) preheating raw materials of a first reactor, then feeding the preheated raw materials into the first reactor, directly contacting the reaction raw materials in the first reactor with a high-temperature catalyst from a regeneration conveying pipe, quickly reacting under the action of the catalyst, and feeding reaction products into a second reactor through the top of the first reactor;
2) preheating raw materials of a second reactor, then feeding the preheated raw materials into the second reactor for reaction, removing most of carried catalyst from reaction products fed into the second reactor in the step 1) through a gas-solid separation facility of the second reactor, removing the carried catalyst through a three-stage cyclone separator of the reactor and a four-stage cyclone separator of the reactor, and then leading out;
3) the spent catalyst in the second reactor enters an external heat collector through an external heat collecting inlet and outlet pipe to be heated; a spent catalyst circulating pipe is arranged between the first reactor and the second reactor, and a slide valve or a plug valve is arranged on the spent catalyst circulating pipe to control the circulating amount of the spent catalyst;
4) the spent catalyst which loses activity after reaction enters a spent stripper for stripping reaction gas carried by the spent catalyst, and the spent catalyst after stripping enters a regenerator through a spent conveying pipe;
5) and after the spent catalyst in the regenerator is in countercurrent contact with main air and is burnt, the regenerated catalyst enters a regeneration stripper for stripping flue gas carried by the regenerated catalyst, and the regenerated catalyst after stripping enters the first reactor and the second reactor through a regenerated catalyst conveying pipe.
The invention relates to a device for preparing aromatic hydrocarbon and low-carbon olefin by using oxygen-containing compounds, which is further characterized in that: the first reactor and the second reactor are both fluidized bed reactors.
The invention relates to a method for preparing aromatic hydrocarbon and low-carbon olefin by using oxygen-containing compounds, which is further characterized in that: the raw material of the first reactor is mixed feed of an oxygen-containing compound and aromatic hydrocarbon or mixed feed of an oxygen-containing compound, aromatic hydrocarbon and light hydrocarbon return gas, and preferably mixed feed of the oxygen-containing compound and the aromatic hydrocarbon; the weight ratio of the oxygen-containing compound to the aromatic hydrocarbon is in the range of 0.1: 10-10: 0.1, preferably in the range 0.5: 1-10: 1.
the invention relates to a method for preparing aromatic hydrocarbon and low-carbon olefin by using oxygen-containing compounds, which is further characterized in that: the second reactor feed is an oxygenate or a mixture of an oxygenate and a light hydrocarbon return gas, preferably an oxygenate.
The invention relates to a method for preparing aromatic hydrocarbon and low-carbon olefin by using oxygen-containing compounds, which is further characterized in that: when light hydrocarbon is recycled, gas (C) is returned4~C8Gas), the regenerated catalyst transport pipe serves as a riser reactor. The riser reactor is fed with preferably light hydrocarbon return gas (C)4~C8Gas), light hydrocarbon return gas can be injected into the upper part, the middle part or the lower part of the riser reactor by one or more (2-5) strands. When the light hydrocarbon is not recycled, the gas (C) is returned4~C8Gas), the regenerated catalyst transport pipe is used only to transport the regenerated catalyst, and the transport medium is preferably steam.
The invention relates to a method for preparing aromatic hydrocarbon and low-carbon olefin by using oxygen-containing compounds, which is further characterized in that: the oxygen-containing compound is an oxygen-containing compound mainly comprising methanol or dimethyl ether, the aromatic hydrocarbon is more than one of toluene, benzene and C8-C10 aromatic hydrocarbon, and the light hydrocarbon return gas is C4~C8A gas.
The invention relates to a method for preparing aromatic hydrocarbon and low-carbon olefin by using oxygen-containing compounds, which is further characterized in that: light hydrocarbon return gas injection ports are arranged on the raw material feeding pipelines of the first reactor and the second reactor, and light hydrocarbon return gas enters the reactors through the raw material feeding pipelines.
The invention relates to a method for preparing aromatic hydrocarbon and low-carbon olefin by using oxygen-containing compounds, which is further characterized in that: and 2) removing the entrained catalyst from the reaction product in the step 2) through a reactor three-stage cyclone separator and a reactor four-stage cyclone separator, leading out, and sending to a rear quenching and water washing system after heat exchange. The catalyst recovered from the reactor three-stage cyclone separator and the reactor four-stage cyclone separator enters a waste catalyst storage tank, and the waste catalyst is sent to a waste catalyst tank through a catalyst unloading pipeline.
The invention relates to a method for preparing aromatic hydrocarbon and low-carbon olefin by using oxygen-containing compounds, which is further characterized in that: the reaction product in the step 2) enters a second reactor through a gas-solid distributor at the top of the first reactor to continue to react,
the invention relates to a method for preparing aromatic hydrocarbon and low-carbon olefin by using oxygen-containing compounds, which is further characterized in that: and 5) removing most of carried catalyst from the flue gas generated after the catalyst and main air are contacted and burned in a countercurrent mode through a two-stage cyclone separator, discharging the flue gas, sending the flue gas to a waste heat boiler through a pressure reducing valve (if needed), a double-acting slide valve and a pressure reducing pore plate to recover heat, and exhausting the flue gas to atmosphere through a chimney.
The invention relates to a method for preparing aromatic hydrocarbon and low-carbon olefin by using oxygen-containing compounds, which is further characterized in that: the spent stripper is internally provided with a stripping grating or a stripping baffle and a stripping medium distribution ring. The regeneration stripper is internally provided with a stripping grid or a stripping baffle and a stripping medium distribution ring.
The invention relates to a device for preparing aromatic hydrocarbon and low-carbon olefin by using oxygen-containing compounds, which is further characterized in that: a spent catalyst circulating pipe is arranged between the first reactor and the second reactor. When the spent catalyst circulating pipe is an external circulating pipe, the inlet of the external circulating pipe is connected with the middle lower part of the second reactor, and the outlet of the external circulating pipe is connected with the lower part of the first reactor. A slide valve is arranged on the spent catalyst circulating pipe.
The invention relates to a device for preparing aromatic hydrocarbon and low-carbon olefin by using oxygen-containing compounds, which is further characterized in that: when the spent catalyst circulating pipe is an internal circulating pipe, the internal circulating pipe is arranged in the middle of the first reactor and is coaxially arranged with the first reactor, the inlet is connected with the lower part of the second reactor, and the outlet is connected with the bottom of the first reactor. A plug valve is arranged on the spent catalyst circulating pipe and is positioned at the bottom of the first reactor.
The invention relates to a method for preparing aromatic hydrocarbon and low-carbon olefin by using oxygen-containing compounds, which is further characterized in that: and internal and/or external heat-taking facilities are arranged in the first reactor and the second reactor, and an external heat-taking device is arranged in the regenerator.
The invention relates to a device for preparing aromatic hydrocarbon and low-carbon olefin by using oxygen-containing compounds, which is further characterized in that: the regenerator is a fluidized bed regenerator, preferably a turbulent fluidized bed regenerator.
The invention relates to a device for preparing aromatic hydrocarbon and low-carbon olefin by using oxygen-containing compounds, which is further characterized in that: the catalyst in the regenerator can be regenerated completely or incompletely, preferably completely.
The method for preparing the aromatic hydrocarbon and the low-carbon olefin by using the oxygen-containing compound can be used in the industrial production of liquid products by converting the oxygen-containing compound, such as an MTA process.
The invention relates to a method for preparing aromatic hydrocarbon and low-carbon olefin by using oxygen-containing compounds, which is further characterized by comprising the following steps: a light hydrocarbon return gas injection port is arranged on the raw material feeding pipe line, and light hydrocarbon return gas enters the reactor through the raw material feeding pipe; the regenerated catalyst conveying pipe can also be used as a riser reactor, light hydrocarbon return gas is injected into the riser reactor, and the light hydrocarbon return gas can be injected into the upper part, the middle part or the lower part of the riser reactor in one or more strands.
The reaction temperature of the device is in the range of 300-650 ℃, preferably 400-600 ℃; the regeneration temperature is in the range of 350-750 ℃, preferably 450-700 ℃; the reaction pressure is in the range of 0.1 to 1.0MPaG, preferably in the range of 0.1 to 0.5 MPaG. The regeneration pressure is in the range of 0.1 to 1.0MPaG, preferably in the range of 0.1 to 0.5 MPaG.
The temperature of the three-stage reaction gas cyclone separator is in the range of 300-650 ℃, preferably 400-600 ℃; the pressure is in the range of 0.1 to 1.0MPaG, preferably in the range of 0.1 to 0.5 MPaG.
The device for preparing the aromatic hydrocarbon and the low-carbon olefin by the oxygen-containing compound better solves the problems of high catalyst bed layer, difficult fluidization of the catalyst, difficult heat extraction and poor selectivity in the prior art, and can be used in the industrial production of preparing liquid products by converting the oxygen-containing compound, such as: MTA process (methanol to aromatics process), MTG process (methanol to gasoline process), and the like. In addition, the equipment has the advantages of simple structure, easy realization, wide application range, low equipment investment and the like, and can be widely applied to devices for preparing liquid products by converting oxygen-containing compounds.
Compared with the prior art, the invention has the advantages that:
(1) by adopting the device provided by the invention, the selectivity of the target product, such as the selectivity and yield of aromatic hydrocarbon and low-carbon olefin products, can be improved to the greatest extent;
(2) by adopting the device provided by the invention, the problems of high bed layer and difficult fluidization of the catalyst in the reactor and the regenerator are solved, and the fluidization state is maintained;
(3) the device provided by the invention can meet the requirements of MTA process reaction regeneration conditions. Namely, the reaction gas has long retention time, the catalyst has long retention time and the catalyst has low circulation volume. The reaction condition and the regeneration condition can be effectively controlled, the problem of reaction heat extraction caused by high pressure and strong heat release is solved, and the heat balance of the device can be realized. Simple operation and low equipment investment.
(4) The device provided by the invention can meet the requirements of MTA process reaction regeneration conditions. Namely, the requirements on different airspeeds of methanol and toluene, longer catalyst retention time and reduced catalyst abrasion. Simple operation and low equipment investment.
The invention is further described with reference to the following figures and detailed description. But not to limit the scope of the invention.
Drawings
FIG. 1 is a diagram of an apparatus for producing aromatic hydrocarbons and light olefins from an oxygen-containing compound according to the present invention.
The reference symbols shown in the figures are: 1-regenerated catalyst conveying pipe, 2-light hydrocarbon return gas, 3-raw material feeding pipe, 4-external heat collector, 5-external heat-collecting inlet pipe, 6-second reactor internal heat-collecting facility, 7-reactor dense-phase section, 8-reactor transition section, 9-reactor dilute-phase section, 10-reactor gas-solid separation facility, 11-waste catalyst, 12-reactor triple-rotation recovered catalyst storage tank, 13-reactor four-stage cyclone separator, 14-reactor four-stage cyclone separator outlet gas, 15-reactor three-stage cyclone separator, 17-oil gas, 18-oil gas collection chamber, 19-spent agent inlet pipe, 20-flue gas, 21-regenerator separation facility, 22-regenerator, 23-regenerator dilute-phase section, 24-a regenerator transition section, 25-a regenerator burning section, 26-a regenerator external heat taking inlet and outlet, 27-a regenerator external heat taking device, 28-main air, 29-conveying gas or raw materials, 30-a regeneration slide valve, 31-a spent slide valve, 32-a spent agent conveying pipe, 33-a spent stripper, 34-a feeding distributor I, 35-a main air distributor, 36-a feeding distributor II, 37-a spent slide valve II/plug valve, 38-a spent catalyst circulating pipe, 39-a first reactor, 40-a second reactor, 41-a gas-solid distributor, 42-a first reactor internal heat taking facility and 43-a regeneration stripping section.
Detailed Description
As shown in fig. 1, the apparatus for preparing aromatic hydrocarbons and light olefins from oxygen-containing compounds comprises a first reactor 39, a second reactor 40, a regenerator 22, a reactor third-stage cyclone 15, a reactor fourth-stage cyclone 13, a reactor third-stage recovered catalyst storage tank 12, a spent stripper 33, a regenerative stripper 43, an external heat remover 4 and an external regenerator 27. The first reactor 39 is communicated with the second reactor 40 through a gas-solid distributor 43, and the first reactor 39 is communicated with the spent catalyst circulating pipe 38 and the regenerated catalyst conveying pipe 1; the second reactor 40 is communicated with the spent stripper 33, the external heat collector 4 and the reactor tertiary cyclone separator 15; the regenerator 22 is in communication with a regenerator stripper 43, an external regenerator 27, and a spent agent transfer line 32.
The first reactor 39 and the second reactor 40 are arranged coaxially and in parallel with the regenerator 22, the second reactor 40 being higher than the first reactor 39; the bottom of the first reactor 39 is provided with a raw material feeding pipe 3 and a first feeding distributor 34, the bottom of the second reactor 40 is provided with a raw material feeding pipe 3 and a second feeding distributor 36, and the raw material feeding pipe 3 is introduced into the feeding distributors for distribution.
One end of the spent stripper 33 is communicated with the bottom of the second reactor 40 through a spent agent inlet pipe 19, and the other end is communicated with the regenerator 22 through a spent conveying pipe 32. The second reactor 40 is internally provided with a reactor gas-solid separation facility 10. The regenerator 22 is internally provided with a regenerator gas-solid separation facility 21. The regenerator 22 is provided with an external regenerator 27 which is connected with the regenerator 22 through an external regenerator heat taking inlet 26; the first reactor 39 is provided with an internal heat-taking device and an external heat-taking device, preferably an internal heat-taking device 44 of the first reactor; the second reactor 40 is provided with internal and external heat-taking means, preferably the internal heat-taking means 6 of the second reactor. The second reactor 40 is provided with an external heat collector 4, and is connected with the second reactor 40 through an external heat outlet inlet pipe 5.
A spent catalyst circulation pipe 38 is provided between the first reactor 39 and the second reactor 40. When the spent catalyst circulating pipe 38 is an external circulating pipe, the inlet of the external circulating pipe is connected with the bottom of the second reactor 40, the outlet of the external circulating pipe is connected with the bottom of the first reactor 39, and a spent slide valve II 37 is arranged on the spent catalyst circulating pipe 38. When the spent catalyst circulation pipe 38 is an internal circulation pipe, the internal circulation pipe is arranged at the middle part of the first reactor 39 and is coaxially arranged with the first reactor, the inlet is connected with the bottom of the second reactor 40, and the outlet is connected with the bottom of the first reactor 39. A plug valve 37 is arranged on the spent catalyst circulating pipe 38 and is positioned at the bottom of the first reactor 39. The interior of the second reactor 40 is divided into a reactor dilute phase section 9, a reactor transition section 8 and a reactor dense phase section 7 from top to bottom. The top of the second reactor 40 is provided with an oil gas collection chamber 18, and the reaction oil gas 17 is introduced into the oil gas collection chamber 18 through the reactor gas-solid separation facility 10.
The regenerator 22 is internally divided into a regenerator dilute phase section 23, a regenerator transition section 24 and a regenerator char section 25. The regenerator char section 25 may be a turbulent bed or a fast bed or a combination of both. The regenerator dilute phase section 23 is provided with a regenerator gas-solid separation facility 21, the top of the regenerator dilute phase section is provided with a flue gas 20 outlet, the regeneration and burning section 25 is provided with a main air distributor 35, and the bottom of the regenerator is provided with a main air 28 inlet. One end of the regeneration stripper 43 is communicated with the bottom of the regenerator 22, the other end is communicated with the first reactor 39 through a regenerated catalyst conveying pipe 1, and a regenerated slide valve 30 is arranged on the regenerated catalyst conveying pipe 1; the regenerated catalyst transfer line 1 is also a riser reactor.
Preheating oxygen-containing compounds mainly containing methanol or dimethyl ether and toluene and/or benzene, then entering a first feeding distributor 34 in a first reactor 39 from a raw material feeding pipe 3, directly contacting the oxygen compounds in the first reactor 39 with a high-temperature regenerated catalyst from a regenerated catalyst conveying pipe 1, and rapidly reacting under the action of the catalyst; the reaction product enters the second reactor 40 through the gas-solid distributor 43 at the top of the first reactor 39 to continue the reaction; and a part of preheated oxygen-containing compounds mainly containing methanol or dimethyl ether also enter the second reactor 40 for reaction, most of carried catalyst is removed from reaction products through a reactor gas-solid separation facility 10, the carried catalyst is removed through a reactor three-stage cyclone separator 15 and a reactor four-stage cyclone separator 13, the reaction products are led out, and the reaction products are sent to a rear quenching and water washing system after heat exchange. The reactor gas-solid separation facility 10 is a two-stage cyclone separator.
The catalyst recovered by the reactor three-stage cyclone separator 15 and the reactor four-stage cyclone separator 13 enters a reactor three-cycle recovered catalyst storage tank 12, and the waste catalyst 11 enters a waste catalyst tank through a discharging pipeline.
The spent catalyst enters a spent stripper 33 for stripping, and a stripping grid or a stripping baffle plate and a stripping medium distributor are arranged in the spent stripper 33. The device is used for stripping reaction gas carried by spent catalyst, and the stripped spent catalyst enters a spent agent conveying pipe 32 after passing through a spent slide valve 31 and then enters the regenerator 22. After the regenerated catalyst is in countercurrent contact with main air 28 in the regenerator 22 and is burnt, the regenerated catalyst enters a regeneration stripper 43 for stripping flue gas carried by the regenerated catalyst, and the regenerated catalyst enters a regenerated catalyst conveying pipe through a regeneration slide valve after being stripped and then enters a first reactor 39 and a second reactor 40 for reaction. The regenerated flue gas 20 is passed through a regenerator gas-solid separation facility 21 to remove most of the carried catalyst, then passed through a pressure reducing valve (if necessary), a double-acting slide valve and a pressure reducing orifice plate, and then sent to a waste heat boiler to recover heat, and then discharged to atmosphere through a chimney.
The raw materials are respectively fed into each reactor according to the reaction requirement, the feed of the reactor is one or two of oxygen-containing compounds, toluene and/or benzene, and the feed can be singly fed or mixed. The feed to the first reactor 39 is preferably a mixed feed of an oxygenate based on methanol or dimethyl ether, toluene and/or benzene. The feed to the second reactor 40 preferably recommends an oxygenate based on methanol or dimethyl ether. The regenerated catalyst conveying pipe 1 can also be used as a riser reactor, and light hydrocarbon return gas 2 (C) can enter the riser reactor4~C8Gas), light hydrocarbon return gas 2 (C)4~C8Gas) may be provided on the oxygenate feed line and mixed to be fed together into the first reactor 39 or the second reactor 40; or can be arranged at the upper part, the middle part or/and the lower part of the riser reactor, and can be divided into one or more light hydrocarbon return gases. When light hydrocarbon returns to gas 2 (C)4~C8Gas) is not recycled into the regenerated catalyst transfer pipe 1, the regenerated catalyst transfer pipe is used for transferring the regenerated catalyst, and the transfer gas 29 is preferably steam. The feeding material of the first reactor is a mixed feeding material of an oxygen-containing compound mainly comprising methanol or dimethyl ether and toluene and/or benzene, and the weight ratio of the oxygen-containing compound to the toluene and/or benzene is in the range of 0.1: 10-10: 0.1, preferably in the range 0.5: 1-10: 1.
Claims (34)
1. a device for preparing aromatic hydrocarbon and low-carbon olefin by using oxygen-containing compounds comprises a reactor, a regenerator, an external heat collector, a spent stripper and a regenerated stripper, and is characterized in that: the reactor comprises a first reactor and a second reactor, the regenerator is connected with the first reactor through a regeneration stripper, a regeneration slide valve and a regenerated catalyst conveying pipe, and the regenerated catalyst conveying pipe extends into the first reactor; the first reactor is communicated with the second reactor; the stripper to be regenerated is respectively communicated with the bottoms of the second reactor and the regenerator; the regeneration stripper is communicated with the first reactor through a regeneration slide valve and a regeneration catalyst conveying pipe; an external heat collector is arranged in the second reactor and communicated with the second reactor; a spent catalyst circulating pipe is arranged between the first reactor and the second reactor; the first reactor and the second reactor are coaxially arranged and are arranged in parallel with the regenerator, and the second reactor is higher than the first reactor; and feeding distributors are arranged at the bottoms of the first reactor and the second reactor, and raw materials are introduced into the feeding distributors for distribution.
2. The apparatus for preparing aromatic hydrocarbons and light olefins from oxygenates according to claim 1, characterized in that: the external heat collector is connected with the second reactor through an external heat outlet inlet pipe.
3. The apparatus for preparing aromatic hydrocarbons and light olefins from oxygenates according to claim 1, characterized in that: the regenerated catalyst transfer line is also a riser reactor.
4. The apparatus for preparing aromatic hydrocarbons and light olefins from oxygenates according to claim 1, characterized in that: the first reactor and the second reactor are both fluidized bed reactors.
5. The apparatus for preparing aromatic hydrocarbons and light olefins from oxygenates according to claim 1, characterized in that: the first reactor and the second reactor are connected through a gas-solid distributor or a pipeline.
6. The apparatus for preparing aromatic hydrocarbons and light olefins from oxygenates according to claim 1, characterized in that: the spent catalyst circulating pipe is an external circulating pipe, the inlet of the external circulating pipe is connected with the middle lower part of the second reactor, and the outlet of the external circulating pipe is connected with the lower part of the first reactor; a slide valve is arranged on the spent catalyst circulating pipe.
7. The apparatus for preparing aromatic hydrocarbons and light olefins from oxygenates according to claim 1, characterized in that: the spent catalyst circulating pipe is an internal circulating pipe which is arranged in the middle of the first reactor and is coaxially arranged with the first reactor, an inlet is connected with the bottom of the second reactor, and an outlet is connected with the bottom of the first reactor; a plug valve is arranged on the spent catalyst circulating pipe and is positioned at the bottom of the first reactor.
8. The apparatus for preparing aromatic hydrocarbons and light olefins from oxygenates according to claim 1, characterized in that: one end of the spent stripper is communicated with the bottom of the second reactor through a spent agent inlet pipe, the other end of the spent stripper is communicated with the regenerator through a spent agent conveying pipe, and a slide valve is arranged on the spent agent conveying pipe.
9. The apparatus for preparing aromatic hydrocarbons and light olefins from oxygenates according to claim 1, characterized in that: one end of the regeneration stripper is communicated with the bottom of the regenerator, the other end of the regeneration stripper is communicated with the first reactor through a regenerated catalyst conveying pipe, and a slide valve is arranged on the regenerated catalyst conveying pipe.
10. The apparatus for preparing aromatic hydrocarbons and light olefins from oxygenates according to claim 1, characterized in that: a stripping grating or a stripping baffle is arranged in the to-be-regenerated stripper, and a stripping medium distributor is also arranged in the to-be-regenerated stripper; a stripping grating or a stripping baffle plate is arranged in the regeneration stripper, and a stripping medium distributor is also arranged in the regeneration stripper.
11. The apparatus for preparing aromatic hydrocarbons and light olefins from oxygenates according to claim 1, characterized in that: the feeding distributor is a distribution pipe or a distribution plate.
12. The apparatus for preparing aromatic hydrocarbons and light olefins from oxygenates according to claim 1, characterized in that: the interior of the second reactor is divided into a reactor dilute phase section, a reactor transition section and a reactor dense phase section from top to bottom.
13. The apparatus for preparing aromatic hydrocarbons and light olefins from oxygenates according to claim 1, characterized in that: and a gas-solid separation facility is arranged in the second reactor, an oil-gas collection chamber is arranged at the top of the second reactor, and the gas-solid separation facility is introduced into the oil-gas collection chamber.
14. The apparatus for producing aromatics and lower olefins from oxygenates according to claim 13, characterized in that: the gas-solid separation facility is a primary cyclone separator and a secondary cyclone separator, and the secondary cyclone separator is introduced into the oil gas collection chamber.
15. The apparatus for preparing aromatic hydrocarbons and light olefins from oxygenates according to claim 1, characterized in that: and a third-stage cyclone separator is arranged outside or inside the second reactor, and the reaction gas third-stage cyclone separator is vertical or horizontal.
16. The apparatus for producing aromatics and lower olefins from oxygenates according to claim 15, characterized in that: and a reactor fourth-stage cyclone separator is arranged outside the second reactor, one end of the reactor fourth-stage cyclone separator is communicated with the reactor third-stage cyclone separator, and the other end of the reactor fourth-stage cyclone separator is communicated with a reactor third-stage recovery catalyst storage tank.
17. The apparatus for preparing aromatic hydrocarbons and light olefins from oxygenates according to claim 1, characterized in that: the regenerator is a fluidized bed regenerator, and the regenerator is internally divided into a regenerator dilute phase section, a regenerator transition section and a regenerator coking section.
18. The apparatus for producing aromatics and lower olefins from oxygenates according to claim 17, characterized in that: the dilute phase section of the regenerator is provided with a gas-solid separation device, the top of the dilute phase section is provided with a flue gas outlet, the regeneration and burning section is provided with a main air distributor, and the bottom of the regenerator is provided with a main air inlet.
19. The apparatus for producing aromatics and lower olefins from oxygenates according to claim 18, characterized in that: the main wind distributor is a distribution pipe and/or a distribution plate.
20. The apparatus for preparing aromatic hydrocarbons and light olefins from oxygenates according to claim 1, characterized in that: arranging a heat taking facility and/or a heat taking facility in the first reactor and the second reactor, wherein the heat taking facility is arranged at the middle lower part of the first reactor and the second reactor and above the feeding distributor of the reactors; and an external heat taking facility is arranged in the regenerator.
21. The apparatus for preparing aromatic hydrocarbons and light olefins from oxygenates according to claim 1, characterized in that: the first reactor, the second reactor and the regenerator are all high beds, and the ratio of the height of the catalyst bed in the dense-phase section of the reactor to the height of the dense-phase section of the reactor is 0.5-20.0; the ratio of the height of the catalyst bed in the dense phase section of the regenerator to the height of the dense phase section of the regenerator is in the range of 0.5 to 30.0.
22. A method for preparing aromatic hydrocarbon and low-carbon olefin by using oxygen-containing compounds is characterized by comprising the following steps:
1) preheating raw materials of a first reactor, then feeding the preheated raw materials into the first reactor, directly contacting the reaction raw materials in the first reactor with a high-temperature catalyst from a regeneration conveying pipe, quickly reacting under the action of the catalyst, and feeding reaction products into a second reactor through the top of the first reactor;
2) preheating raw materials of a second reactor, then feeding the preheated raw materials into the second reactor for reaction, removing most of carried catalyst from reaction products fed into the second reactor in the step 1) through a gas-solid separation facility of the second reactor, removing the carried catalyst through a three-stage cyclone separator of the reactor and a four-stage cyclone separator of the reactor, and then leading out;
3) the spent catalyst in the second reactor enters an external heat collector through an external heat collecting inlet and outlet pipe to be heated; a spent catalyst circulating pipe is arranged between the first reactor and the second reactor, and a slide valve or a plug valve is arranged on the spent catalyst circulating pipe to control the circulating amount of the spent catalyst;
4) the spent catalyst which loses activity after reaction enters a spent stripper for stripping reaction gas carried by the spent catalyst, and the spent catalyst after stripping enters a regenerator through a spent conveying pipe;
5) and after the spent catalyst in the regenerator is in countercurrent contact with main air and is burnt, the regenerated catalyst enters a regeneration stripper for stripping flue gas carried by the regenerated catalyst, and the regenerated catalyst after stripping enters the first reactor and the second reactor through a regenerated catalyst conveying pipe.
23. The method for preparing aromatic hydrocarbons and lower olefins from oxygen-containing compounds according to claim 22, wherein: the regenerated catalyst conveying pipe is used as a riser reactor, the feeding of the riser reactor is light hydrocarbon return gas, and the light hydrocarbon return gas is injected into the upper part, the middle part or the lower part of the riser reactor in one or more strands.
24. The method for preparing aromatic hydrocarbons and lower olefins from oxygen-containing compounds according to claim 22, wherein: the raw material of the first reactor is a mixed feed of an oxygen-containing compound and aromatic hydrocarbon or a mixed feed of light hydrocarbon return gas, the oxygen-containing compound and the aromatic hydrocarbon; the weight ratio of the oxygen-containing compound to the aromatic hydrocarbon is in the range of 0.1: 10-10: 0.1.
25. the method for preparing aromatic hydrocarbons and lower olefins from oxygen-containing compounds according to claim 22, wherein: the second reactor raw material is an oxygen-containing compound or a mixture of the oxygen-containing compound and light hydrocarbon return gas.
26. The method for preparing aromatic hydrocarbons and lower olefins from oxygen-containing compounds according to claim 22, wherein: the raw material of the first reactor is a mixed feed of an oxygen-containing compound and aromatic hydrocarbon, and the weight ratio of the oxygen-containing compound to the aromatic hydrocarbon is in the range of 0.5: 1-10: 1; the second reactor feed is an oxygenate.
27. The method for preparing aromatic hydrocarbons and lower olefins from oxygen-containing compounds according to claim 22, wherein: the oxygen-containing compound is an oxygen-containing compound mainly comprising methanol or dimethyl ether, and the aromatic hydrocarbon is toluene,More than one of benzene and C8-C10 aromatic hydrocarbon, wherein the light hydrocarbon return gas is C4～C8A gas.
28. The method for preparing aromatic hydrocarbons and lower olefins from oxygen-containing compounds according to claim 22, wherein: and 2) removing the entrained catalyst from the reaction product in the step 2) through a reactor three-stage cyclone separator and a reactor four-stage cyclone separator, leading out, and sending to a rear quenching and water washing system after heat exchange. The catalyst recovered by the reactor three-stage cyclone separator and the reactor four-stage cyclone separator enters a reactor three-cyclone recovery catalyst storage tank, and the waste catalyst is sent to a waste catalyst tank through a discharging agent pipeline.
29. The method for preparing aromatic hydrocarbons and lower olefins from oxygen-containing compounds according to claim 22, wherein: and 2) allowing the reaction product to enter a second reactor through a gas-solid distributor at the top of the first reactor for continuous reaction.
30. The method for preparing aromatic hydrocarbons and lower olefins from oxygen-containing compounds according to claim 22, wherein: and 5) removing most of carried catalyst from the regenerated flue gas by a two-stage cyclone separator, discharging, sending to a waste heat boiler through a pressure reducing valve, a double-acting slide valve and a pressure reducing pore plate, recovering heat, and discharging the air through a chimney.
31. The method for preparing aromatic hydrocarbons and lower olefins from oxygen-containing compounds according to claim 22, wherein: the first reactor and the second reactor are fluidized bed reactors; the regenerator is a fluidized bed regenerator.
32. The method for preparing aromatic hydrocarbons and lower olefins from oxygen-containing compounds according to claim 22, wherein: the reaction temperature of the first reactor and the second reactor is within the range of 300-650 ℃; the reaction pressure is in the range of 0.1-1.0 MPaG; the regeneration temperature is in the range of 350-750 ℃; the regeneration pressure is in the range of 0.1-1.0 MPaG.
33. The method for preparing aromatic hydrocarbons and lower olefins from oxygen-containing compounds according to claim 32, wherein: the reaction temperature of the first reactor and the second reactor is within the range of 400-600 ℃; the reaction pressure is in the range of 0.1-0.5 MPaG; the regeneration temperature is in the range of 450-700 ℃; the regeneration pressure is in the range of 0.1-0.5 MPaG.
34. The method for preparing aromatic hydrocarbons and lower olefins from oxygen-containing compounds according to claim 22, wherein: the temperature of the three-stage cyclone separator of the reactor is within the range of 400-600 ℃; the pressure is in the range of 0.1 to 0.5 MPaG.
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