Circulating fluidized bed reactor regeneration apparatus and method

Abstract

This application discloses a circulating fluidized-bed reactor and its application method. The reactor includes a fluidized-bed reactor (1), a fluidized-bed regenerator (2), and a lift-tube reactor (3). The fluidized-bed reactor (1) is used to supply naphtha feedstock and methanol feedstock. The naphtha feedstock contacts the catalyst from the lift-tube reactor (3) to produce a product gas stream containing BTX and spent catalyst. The methanol feedstock undergoes a methylation reaction with benzene and toluene in the product gas stream to produce paraxylene. The product gas stream is subjected to gas-solid separation, and the separated product gas is sent to a downstream process. Unconverted naphtha is returned to the fluidized-bed reactor as feedstock, a portion of the low-carbon alkanes are returned to the lift-tube reactor (3) as feedstock, and the spent catalyst is sent to the fluidized-bed regenerator (2). The inlet of the lift-tube reactor (3) is connected to the fluidized-bed regenerator (2), and the outlet is connected to the fluidized-bed reactor (1). The application method includes producing aromatic hydrocarbons using the circulating fluidized bed reactor regenerator and the metal zeolite bifunctional catalyst.

Description

[Technical Field]

[0001] The present application relates to a circulating fluidized bed reactor and a method for using the same, which belongs to the chemical industry technical field, and in particular to a circulating fluidized bed reactor and a method for using the same. [Background technology]

[0002] Aromatic compounds (benzene, toluene, and dimethylbenzene, collectively known as BTX) are important organic chemical raw materials, and among them, dimethylbenzene (PX) is the most notable aromatic compound. It is primarily used in the production of polyesters such as terephthalic acid (PTA), polyethylene terephthalate (PET), polybutylene terephthalate (PBT), and polypropylene terephthalate (PTT). In recent years, China's production and consumption of dimethylbenzene have been steadily increasing. In 2021, China's total PX imports were approximately 13.65 million tons, with an external dependency rate of approximately 38%.

[0003] Naphtha catalytic reforming is the primary route for producing aromatic compounds. Naphtha has a highly complex composition. It is not only the primary feedstock for catalytic reforming but also the primary feedstock for thermal cracking to produce ethylene. Its composition plays a crucial role in the economic efficiency of the plant. Generally, a high aromatic potential content and a suitable distillation range are favorable for catalytic reforming. Meanwhile, naphtha with a high content of linear and branched aliphatic hydrocarbons and a low content of cycloalkanes and aromatic compounds is suitable for ethylene production by thermal cracking. To effectively utilize naphtha resources and improve economic efficiency, it is usually necessary to first separate the linear and branched aliphatic hydrocarbons from the cycloalkanes and aromatic compounds in naphtha. The former is used as a feedstock for ethylene production, and the latter is used as a feedstock for the catalytic reforming plant.

[0004] Because naphtha fractions have a relatively broad distillation range, it is difficult to efficiently separate linear and branched aliphatic hydrocarbons from cycloalkanes and aromatic compounds using conventional separation methods. Furthermore, catalytic reforming technology also faces challenges in converting linear and branched aliphatic hydrocarbons to aromatic compounds. The naphtha feedstock used in catalytic reforming typically requires distillation to remove light fractions with boiling points below 60°C to increase the aromatic potential of the catalytic reforming feedstock. However, fractions with boiling points above 60°C still contain large amounts of linear and branched aliphatic hydrocarbons that are difficult to convert to aromatic compounds. Therefore, highly selective conversion of linear and branched aliphatic hydrocarbons to aromatic compounds remains a key focus and challenge in the development of technologies for producing aromatic compounds from naphtha.

[0005] Due to thermodynamic equilibrium limitations, the paraxylene content of the xylene mixture produced in naphtha catalytic reforming units is only about 24%. It is necessary to further increase the paraxylene production volume through the isomerization-separation process. Therefore, increasing the paraxylene content in the xylene mixture is an important means of reducing the energy consumption for paraxylene production. Summary of the Invention [Problem to be solved by the invention]

[0006] Naphtha molecules contain only a small amount of methyl groups (methyl groups / benzene rings = ~1.3 (molar ratio)), and due to its molecular structure, catalytic reforming / aromatics combined units inevitably produce large amounts of benzene as a by-product.

[0007] Methanol aromatization is an emerging process for producing aromatic compounds. However, due to the excess hydrogen atoms in the methanol molecule relative to the aromatic compounds, the process of producing aromatic compounds from methanol inevitably produces large amounts of paraffins and hydrogen as by-products. Based on the molecular structure and reaction mechanism, it is clear that methanol can provide methyl groups to aromatic compounds, thereby increasing the production of toluene and xylene. This provides a new technological approach to producing aromatic compounds by coupling naphtha and methanol. [Means for solving the problem]

[0008] This application provides a circulating fluidized bed reactor and its application method for producing aromatic hydrocarbons using naphtha and methanol as raw materials.

[0009] The components of naphtha in this application are C4-C 12 Includes straight-chain and branched aliphatic hydrocarbons, naphthenic and aromatic hydrocarbons.

[0010] In this application, aromatic hydrocarbons refer to benzene, toluene, and xylene, collectively referred to as BTX.

[0011] According to one aspect of the present application, there is provided a circulating fluidized bed reaction regeneration apparatus, comprising a fluidized bed reactor, a fluidized bed regenerator, and a lift tube reactor;

[0012] The fluidized bed reactor is used to pass a naphtha feedstock and a methanol feedstock, the naphtha feedstock contacting the catalyst from the lift tube reactor to produce a product gas stream containing BTX and spent catalyst, the methanol feedstock undergoing a methylation reaction with benzene and toluene in the product gas stream containing BTX to produce paraxylene, the product gas stream undergoing gas-solid separation, the separated product gas being transported to a downstream process, unreacted naphtha being returned to the fluidized bed reactor as a feedstock, a portion of the low-carbon paraffins being returned to the lift tube reactor as a feedstock, and the spent catalyst being passed through the fluidized bed regenerator. The inlet of the lift tube reactor is connected to a fluidized bed regenerator, and the outlet of the lift tube reactor is connected to a fluidized bed reactor.

[0013] Preferably, the fluidized bed reactor includes a reactor housing, and the area enclosed by the reactor housing is divided into a first gas-solid separation zone and a reaction zone from top to bottom. The reaction zone is provided with a reactor distributor, which includes n sub-distributors, arranged in order from bottom to top from the first sub-distributor to the nth sub-distributor, where n≧2 and n≦10. The first sub-distributor is used to pass naphtha feedstock, and the second to nth sub-distributors are used to pass methanol feedstock.

[0014] Preferably, the first gas-solid separation section is provided with a gas-solid separation device I, a gas-solid separation device II and a reactor gas collection chamber, the gas outlet of the gas-solid separation device I is connected to the reactor gas collection chamber, The reactor gas collection chamber is connected to the product gas transport pipe, the inlet of the gas-solid separation device II is connected to the lift pipe reactor, the gas outlet of the gas-solid separation device II is connected to the reactor gas collection chamber, and the catalyst outlet end of the gas-solid separation device II is located above the open end of the reactor stripper inlet pipe and between the first sub-distributor and the second sub-distributor.

[0015] Preferably, the reactor gas collection chamber is located at the top of the interior of the reactor housing.

[0016] Preferably, the gas-solid separation device I uses one or more sets of gas-solid cyclone separators, each set of gas-solid cyclone separators including one first-class gas-solid cyclone separator and one second-class gas-solid cyclone separator.

[0017] Preferably, the fluidized bed regenerator is connected to the fluidized bed reactor and is used to pass a regeneration gas through it to regenerate the spent catalyst from the fluidized bed reactor to obtain a regenerated catalyst.

[0018] Preferably, the fluidized-bed reactor is sequentially connected to the fluidized-bed regenerator via a reactor stripper, a spent sliding valve, and a spent agent transport pipe, and the inlet of the reactor stripper extends into the reactor housing of the fluidized-bed reactor, and its open end is located below the catalyst outlet end of the gas-solid separation device I and above the first sub-distributor.

[0019] Preferably, the fluidized bed regenerator includes a regenerator housing, and the area enclosed by the regenerator housing is divided from top to bottom into a second gas-solid separation section and a regeneration section. The second gas-solid separation section is provided with a regenerator gas-solid separator and a regenerator gas collecting chamber. The regenerator gas collecting chamber is located at the top of the regenerator housing and has an exhaust gas transport pipe installed thereon. The gas outlet of the regenerator gas-solid separator is connected to the regenerator gas collecting chamber. A regenerator distributor is installed at the bottom of the regeneration section and is used to pass the regeneration gas.

[0020] Preferably, the regenerator gas-solid separation device uses one or more sets of gas-solid cyclone separators, each set of gas-solid cyclone separators including one first-class gas-solid cyclone separator and one second-class gas-solid cyclone separator.

[0021] Preferably, the lift tube reactor is used to pass a lift tube reactor feed and a catalyst to produce aromatics, and a stream containing unreacted lift tube reactor feed, aromatics, and catalyst enters a fluidized bed reactor through an outlet of the lift tube reactor.

[0022] Preferably, the inlet of the lift tube reactor is connected to a fluidized bed regenerator, and the catalyst passed through the lift tube reactor is a regenerated catalyst produced in the fluidized bed regenerator.

[0023] Preferably, the fluidized bed regenerator is connected by piping to the inlet of the lift tube reactor via a regenerator stripper, a regeneration slide valve, and then the fluidized bed regenerator.

[0024] Preferably, the inlet of the regenerator stripper extends into the regenerator housing of the fluidized bed regenerator and is located above the regenerator distributor.

[0025] According to another aspect of the present application, there is provided an application method based on the above-described apparatus, which method uses the circulating fluidized bed reactor regenerator and the metal zeolite bifunctional catalyst to produce aromatics.

[0026] Preferably, the method comprises: The naphtha feedstock is introduced into a reaction zone of the fluidized bed reactor through a first sub-distributor of the reactor distributor and contacted with the catalyst from the lift tube reactor to produce a product gas stream containing BTX, low carbon olefins, hydrogen, low carbon paraffins, combustible gases, heavy aromatics, and unreacted naphtha; The methanol feedstock is fed through the second sub-distributor to the nth sub-distributor of the reactor distributor into the reaction zone of the fluidized bed reactor, where it undergoes a methylation reaction with the benzene and toluene in the product gas stream to produce paraxylene; A fluidized bed reactor outputs the product gas to a downstream process.

[0027] Preferably, the metal zeolite bifunctional catalyst uses a metal-modified HZSM-5 zeolite molecular sieve; The metal used for the metal modification is at least one selected from La, Zn, Ga, Fe, Mo, and Cr, The metal modification method includes immersing HZSM-5 zeolite molecular sieve in a metal salt solution, drying, and calcining to obtain the metal-modified HZSM-5 zeolite molecular sieve.

[0028] Preferably, before the fluidized bed reactor outputs the product gas, a gas-solid separation device I is used to first perform gas-solid separation to remove spent catalyst entrained in the product gas stream.

[0029] Preferably, after the catalyst from the lift tube reactor enters the fluidized bed reactor, it is first subjected to gas-solid separation using a gas-solid separator II, and the catalyst from which the gas has been removed passes through the catalyst outlet of the gas-solid separator II and enters between the first sub-distributor and the second sub-distributor.

[0030] Preferably, the low carbon olefins refer to ethylene and propylene; The low carbon paraffin refers to ethane and propane; the flammable gas includes methane and CO; The heavy aromatics refer to aromatics having 9 or more carbon atoms in the molecule.

[0031] Preferably, the naphtha is at least one selected from direct coal liquefaction naphtha, indirect coal liquefaction naphtha, straight-run naphtha, and hydrocracked naphtha.

[0032] Preferably, the naphtha further comprises unreacted naphtha separated from the product gas stream, the unreacted naphtha being predominantly C4-C 12 These are straight-chain, branched aliphatic hydrocarbons and naphthenes.

[0033] Preferably, the process conditions in the reaction zone of the fluidized bed reactor are: gas superficial linear velocity of 0.5-2.0 m / s, reaction temperature of 500-600°C, reaction pressure of 100-500 kPa, bed density of 150-700 kg / m 3 is.

[0034] Alternatively, the superficial linear velocity of the gas in the reaction zone of the fluidized bed reactor can be independently selected from 0.5 m / s, 0.6 m / s, 0.7 m / s, 0.8 m / s, 0.9 m / s, 1.0 m / s, 1.1 m / s, 1.2 m / s, 1.3 m / s, 1.4 m / s, 1.5 m / s, 1.6 m / s, 1.7 m / s, 1.8 m / s, 1.9 m / s, and 2.0 m / s, or a range between any two of these values.

[0035] Alternatively, the reaction temperature of the reaction zone of the fluidized bed reactor can be independently selected from 500°C, 510°C, 520°C, 530°C, 540°C, 550°C, 560°C, 570°C, 580°C, 590°C, and 600°C, or a range between any two of these values.

[0036] Alternatively, the reaction pressure in the reaction zone of the fluidized bed reactor can be independently selected from 100 kPa, 125 kPa, 150 kPa, 175 kPa, 200 kPa, 225 kPa, 250 kPa, 275 kPa, 300 kPa, 325 kPa, 350 kPa, 375 kPa, 400 kPa, 425 kPa, 450 kPa, 475 kPa, and 500 kPa, or a range between any two values.

[0037] Optionally, the bed density of the reaction zone of the fluidized bed reactor is 150 kg / m 3 , 200 kg / m 3 , 250 kg / m 3 , 300 kg / m 3 , 350 kg / m 3 , 400 kg / m 3 , 450 kg / m 3 , 500 kg / m 3 , 550 kg / m 3 , 600 kg / m 3 , 650 kg / m 3 , 700 kg / m 3 Any value, or range between any two values, can be independently selected.

[0038] Preferably, the method further includes placing the spent catalyst produced in the fluidized bed reactor in a fluidized bed regenerator, passing a regeneration gas through the regeneration section of the fluidized bed regenerator to contact the spent catalyst, and obtaining exhaust gas and regenerated catalyst by reaction.

[0039] Preferably, the exhaust gas enters a regenerator gas-solid separator to remove the regenerated catalyst mixed therein, then enters a regenerator gas collection chamber, and enters a downstream process through an exhaust gas transport pipe.

[0040] Preferably, the method further comprises the regenerated catalyst sequentially passing through a regenerator stripper and a regeneration slide valve into a lift tube reactor.

[0041] Preferably, the carbon content in the spent catalyst is 1.0-3.0 wt %.

[0042] Preferably, the carbon content in the regenerated catalyst is 0.5 wt % or less.

[0043] Preferably, the regeneration gas is at least one selected from oxygen, air, and oxygen-enriched air.

[0044] Preferably, the process conditions of the regeneration section of the fluidized bed regenerator are: gas superficial linear velocity 0.5-2.0 m / s, regeneration temperature 600-750°C, regeneration pressure 100-500 kPa, bed density 150-700 kg / m 3 is.

[0045] Alternatively, the superficial linear velocity of the gas in the regeneration section of the fluidized bed regenerator may be independently selected from the group consisting of 0.5 m / s, 0.6 m / s, 0.7 m / s, 0.8 m / s, 0.9 m / s, 1.0 m / s, 1.1 m / s, 1.2 m / s, 1.3 m / s, 1.4 m / s, 1.5 m / s, 1.6 m / s, 1.7 m / s, 1.8 m / s, 1.9 m / s, and 2.0 m / s, or a range between any two of these values.

[0046] Alternatively, the regeneration temperature of the regeneration section of the fluidized bed regenerator can be independently selected from 600°C, 615°C, 630°C, 645°C, 660°C, 675°C, 690°C, 705°C, 720°C, 735°C, and 750°C, or a range between any two of these values.

[0047] Alternatively, the regeneration pressure of the regeneration section of the fluidized bed regenerator can be independently selected from 100 kPa, 125 kPa, 150 kPa, 175 kPa, 200 kPa, 225 kPa, 250 kPa, 275 kPa, 300 kPa, 325 kPa, 350 kPa, 375 kPa, 400 kPa, 425 kPa, 450 kPa, 475 kPa, and 500 kPa, or a range between any two of these values.

[0048] Optionally, the bed density of the regeneration section of the fluidized bed regenerator is 150 kg / m 3 , 200 kg / m 3 , 250 kg / m 3 , 300 kg / m 3, 350 kg / m 3 , 400 kg / m 3 , 450 kg / m 3 , 500 kg / m 3 , 550 kg / m 3 , 600 kg / m 3 , 650 kg / m 3 , 700 kg / m 3 Any value, or range between any two values, can be independently selected.

[0049] Preferably, the method further comprises passing the lift tube reactor feed and catalyst through a lift tube reactor to produce aromatics; A stream containing unreacted lift tube reactor feed, aromatics and catalyst enters gas-solid separator II of the fluidized bed reactor from the outlet of the lift tube reactor.

[0050] Preferably, the catalyst is regenerated catalyst from a fluidized bed regenerator.

[0051] Preferably, the lift tube reactor feed comprises steam and low carbon paraffins separated from the product gas stream.

[0052] Preferably, the steam content in the lift tube reactor feed is 0-50 wt%.

[0053] Preferably, the process conditions of the lift tube reactor are: gas superficial linear velocity 3.0-10.0 m / s, temperature 580-700°C, pressure 100-500 kPa, bed density 50-150 kg / m 3 is.

[0054] Alternatively, the gas superficial linear velocity of the lift tube reactor can be independently selected from 3.0 m / s, 3.5 m / s, 4.0 m / s, 4.5 m / s, 5.0 m / s, 5.5 m / s, 6.0 m / s, 6.5 m / s, 7.0 m / s, 7.5 m / s, 8.0 m / s, 8.5 m / s, 9.0 m / s, 9.5 m / s, and 10.0 m / s, or a range between any two of these values.

[0055] Optionally, the temperature of the lift tube reactor can be independently selected from any value or range between any two of the following: 580°C, 590°C, 600°C, 610°C, 620°C, 630°C, 640°C, 650°C, 660°C, 670°C, 680°C, 690°C, 700°C.

[0056] Alternatively, the pressure in the lift tube reactor can be independently selected from 100 kPa, 125 kPa, 150 kPa, 175 kPa, 200 kPa, 225 kPa, 250 kPa, 275 kPa, 300 kPa, 325 kPa, 350 kPa, 375 kPa, 400 kPa, 425 kPa, 450 kPa, 475 kPa, and 500 kPa, or any range between any two of these values.

[0057] Optionally, the bed density of the lift tube reactor is 50 kg / m 3 , 60 kg / m 3 , 70 kg / m 3 , 80 kg / m 3 , 90kg / m 3 , 100 kg / m 3 , 110 kg / m 3 , 120 kg / m 3 , 130 kg / m 3 , 140 kg / m 3 , 150 kg / m 3 Any value, or range between any two values, can be independently selected.

[0058] The aromatic hydrocarbon potential content of the naphtha feedstock is 0-80 wt%, the naphtha conversion per pass is 60-80 wt%, and the methanol conversion per pass is approximately 100 wt%. The unconverted naphtha is separated from the product gas and returned to the fluidized-bed reactor as feedstock, and a portion of the low-carbon alkanes is separated from the product gas and returned to the lift-tube reactor as feedstock. The final product distribution is 60-71 wt% BTX, 9-16 wt% low-carbon olefins, 3-7 wt% hydrogen, 2-7 wt% low-carbon alkanes, 4-6 wt% combustible gases, 3-7 wt% heavy aromatic hydrocarbons, and 0.5-1 wt% coke. The paraxylene content of the mixed xylenes in the product is 60-75 wt%. [Effects of the Invention]

[0059] 1) In the present invention, linear and branched aliphatic hydrocarbons can be converted to aromatic hydrocarbons with high selectivity, so that the range of applicable raw materials is wide, and aromatic hydrocarbons can be produced using naphtha with a low aromatic potential content as the raw material. 2) In this application, the aromatization of low-carbon alkanes was realized by using a lift tube reactor and a metal zeolite bifunctional catalyst, and the yield of aromatic hydrocarbons in naphtha aromatics technology was significantly improved. 3) The circulating fluidized bed reaction regeneration apparatus of the present application is equipped with a fluidized bed reactor, which is equipped with multiple sub-distributors and a gas-solid separation unit II. Naphtha enters the reaction zone through the first sub-distributor, and methanol enters the reaction zone from the second sub-distributor through the nth sub-distributor. The gas-solid separation unit II directly delivers hot catalyst from the lift tube reactor above the first sub-distributor. The fluidized bed reactor is suitable for staged reaction control. Naphtha is first converted to benzene, toluene, etc. in the lower part of the reaction zone, then flows upward. In the middle and upper parts of the reaction zone, benzene and toluene undergo methylation with methanol to further produce paraxylene, thereby increasing paraxylene production. The hot catalyst from the lift tube reactor directly enters the lower part of the reaction zone, providing the reaction heat necessary for the conversion of naphtha to aromatic hydrocarbons and improving the naphtha conversion rate. By directly injecting methanol into the middle and top of the reaction zone, the residence time of paraxylene in the reaction zone is effectively shortened, the paraxylene isomerization reaction is inhibited, the paraxylene content in xylene (which reaches 75 wt% under optimal industrial conditions) is improved, and the energy consumption for paraxylene separation is significantly reduced. In short, in the above-mentioned fluidized bed reactor, naphtha feedstock flows from bottom to top, and during the conversion process to aromatic hydrocarbons, the methylation feedstock (methanol) is introduced in stages to control the progress of the staged reactions (naphtha → benzene, toluene → paraxylene), thereby increasing the production amount of paraxylene. 4) In this application, the aromatization reaction of naphtha is a strongly endothermic reaction, absorbing 1.1 to 1.6 MJ of heat when 1 kg of naphtha is converted to aromatic hydrocarbons, while the methylation reaction of methanol with aromatic hydrocarbons is a strongly exothermic reaction, releasing more than 2.0 MJ of heat when 1 kg of methanol adds a methyl group to aromatic hydrocarbons. Therefore, by producing paraxylene using benzene, toluene, and methanol, the heat required for the aromatization reaction by coupling naphtha with methanol can be supplied on-site, achieving autothermal equilibrium. 5) The circulating fluidized bed reaction regeneration apparatus of the present application is equipped with an independent lift tube reactor. Low-carbon alkanes are very stable and require high reaction temperatures. Therefore, in the circulating fluidized bed reaction regeneration apparatus of the present application, the high-temperature regeneration catalyst first enters the lift tube reactor and comes into contact with the low-carbon alkanes. The catalyst then causes the low-carbon alkanes to aromatize, improving the reaction rate and the yield of aromatic hydrocarbons. The circulating fluidized bed reaction regeneration apparatus of the present application connects a high-temperature lift tube reactor and a relatively low-temperature fluidized bed reactor in series, thereby achieving the beneficial effects of reducing the yield of low-carbon alkanes and improving the yield of aromatic hydrocarbons. [Brief explanation of the drawings]

[0060] [Figure 1] 1 is a diagram showing a circulating fluidized bed reaction regeneration apparatus according to an embodiment of the present application; DETAILED DESCRIPTION OF THE INVENTION

[0061] The present application will be described in detail below with reference to embodiments, but is not limited to these embodiments.

[0062] This application provides a circulating fluidized bed reaction regeneration apparatus. The apparatus includes a fluidized bed reactor, a fluidized bed regenerator, and a lift tube reactor. The fluidized bed reactor is used to introduce a naphtha feedstock and a methanol feedstock. The naphtha feedstock contacts the catalyst from the lift tube reactor to produce a product gas stream containing BTX and spent catalyst. The methanol feedstock undergoes a methylation reaction with benzene and toluene in the product gas stream to produce paraxylene. The product gas stream is subjected to gas-solid separation, and the separated product gas is sent to a downstream process, unconverted naphtha is returned to the fluidized bed reactor as a feedstock, a portion of the low-carbon alkanes are returned to the lift tube reactor as a feedstock, and the spent catalyst is sent to the fluidized bed regenerator.

[0063] The inlet of the lift tube reactor is connected to a fluidized bed regenerator, and the outlet of the lift tube reactor is connected to a fluidized bed reactor.

[0064] See Figure 1. The apparatus includes a fluidized bed reactor 1, a fluidized bed regenerator 2 and a lift tube reactor 3.

[0065] The fluidized bed reactor 1 includes a reactor housing 1-1, a reactor distributor 1-2, a gas-solid separator I1-3, a reactor gas collection chamber 1-4, a product gas transport pipe 1-5, a reactor stripper 1-6, a spent sliding valve 1-7, a spent agent transport pipe 1-8, and a gas-solid separator II1-9.

[0066] The reactor distributor 1-2 includes a first sub-distributor 1-2-1, a second sub-distributor 1-2-2, and a third sub-distributor 1-2-3.

[0067] The reactor housing 1-1 includes an upper reactor housing and a lower reactor housing, the upper reactor housing forming a gas-solid separation section, and the lower reactor housing forming a reaction section. The reactor housing 1-1 is provided with an outlet for the lift tube reactor 3.

[0068] The reaction zone is equipped with a reactor distributor 1-2, which includes three sub-distributors, arranged in order from bottom to top, from the first sub-distributor 1-2-1 to the third sub-distributor 1-2-3. The first sub-distributor 1-2-1 is used to introduce naphtha feedstock, and the second sub-distributor 1-2-2 to the third sub-distributor 1-2-3 are used to introduce methanol feedstock.

[0069] The reactor housing 1-1 further includes a gas-solid separator I1-3, a gas-solid separator II1-9, and a reactor gas collection chamber 1-4. The reactor gas collection chamber 1-4 is located at the top of the reactor housing, and the gas outlet of the gas-solid separator I1-3 is connected to the reactor gas collection chamber 1-4. The reactor gas collection chamber 1-4 is connected to a product gas transport pipe 1-5, and the catalyst outlet of the gas-solid separator I1-3 is located above the open end of the inlet pipe of the reactor stripper 1-6. The inlet of the gas-solid separator II1-9 is connected to the lift tube reactor 3, and the gas outlet of the gas-solid separator II1-9 is connected to the reactor gas collection chamber 1-4. The catalyst outlet of the gas-solid separator II1-9 is located above the open end of the inlet pipe of the reactor stripper 1-6 and between the first sub-distributor 1-2-1 and the second sub-distributor 1-2-2.

[0070] A reactor stripper 1-6 is installed below the reaction zone, with its inlet located inside the reactor housing 1-1 and its outlet located outside the housing and connected to a used sliding valve 1-7. The open end of the inlet of the reactor stripper 1-6 is located above the first sub-distributor.

[0071] A spent slide valve 1-7 is installed below the reactor stripper 1-6, and its inlet is connected to the outlet of the reactor stripper 1-6, and its outlet is connected to the inlet of a spent agent transport pipe 1-8, the outlet of which is connected to the regenerator housing 2-1.

[0072] The spent slide valve 1-7 is used to control the circulation rate of the spent catalyst.

[0073] In a preferred embodiment, the gas-solid separation device I1-3 uses one or more sets of gas-solid cyclone separators, each set of gas-solid cyclone separators including one first-class gas-solid cyclone separator and one second-class gas-solid cyclone separator.

[0074] The fluidized bed regenerator 2 includes a regenerator housing 2-1, a regenerator distributor 2-2, a regenerator gas-solid separator 2-3, a regenerator gas collection chamber 2-4, an exhaust gas transport pipe 2-5, a regenerator stripper 2-6, and a regenerator slide valve 2-7.

[0075] The regenerator housing 2-1 includes an upper regenerator housing and a lower regenerator housing, the upper regenerator housing forming a gas-solid separation section, and the lower regenerator housing forming a regeneration section. The regenerator housing 2-1 is provided with an outlet for a spent agent transport pipe 1-8.

[0076] The regenerator distributor 2-2 is installed at the bottom of the regeneration section, and is used to introduce the regeneration gas.

[0077] The regenerator housing 2-1 further includes a regenerator gas-solid separator 2-3 and a regenerator gas collection chamber 2-4. The regenerator gas collection chamber 2-4 is located at the top of the regenerator housing 2-1, and the gas outlet of the regenerator gas-solid separator 2-3 is connected to the collection chamber. The regenerator gas collection chamber 2-4 is connected to an exhaust gas transport pipe 2-5, and the catalyst outlet of the regenerator gas-solid separator 2-3 is located above the open end of the inlet pipe of the regenerator stripper 2-6.

[0078] A regenerator stripper 2-6 is installed below the regenerator section, with its inlet located inside the regenerator housing 2-1 and its outlet located outside the housing and connected to a regenerator slide valve 2-7. The open end of the inlet of the regenerator stripper 2-6 is located above the regenerator distributor 2-2.

[0079] A regenerator slide valve 2-7 is installed below the regenerator stripper 2-6, and the inlet of the slide valve is connected to the outlet of the regenerator stripper 2-6.

[0080] The regeneration slide valve 2-7 is used to control the amount of regenerated catalyst circulated.

[0081] In a preferred embodiment, the regenerator gas-solid separator 2-3 uses one or more sets of gas-solid cyclone separators, each set of gas-solid cyclone separators including one first-class gas-solid cyclone separator and one second-class gas-solid cyclone separator.

[0082] The inlet of the lift pipe reactor 3 is connected to a regeneration slide valve 2-7, and the outlet of the reactor is connected to the inlet of a gas-solid separator II1-9.

[0083] The present application further provides an application method based on the above-mentioned apparatus, in particular a method for producing aromatic hydrocarbons by coupling naphtha with methanol, which includes producing aromatic hydrocarbons using the above-mentioned circulating fluidized bed reactor and metal zeolite bifunctional catalyst.

[0084] The metal zeolite bifunctional catalysts described in Examples 1 to 5 all use a metal-modified HZSM-5 zeolite molecular sieve. The metal used for the metal modification is at least one selected from La, Zn, Ga, Fe, Mo, and Cr, and the metal modification method includes immersing the HZSM-5 zeolite molecular sieve in a metal salt solution, drying, and calcining the resulting product.

[0085] In a preferred embodiment, the method comprises the steps of: a) Naphtha enters the reaction zone of fluidized-bed reactor 1 through first sub-distributor 1-2-1 of reactor distributor 1-2 and contacts with catalyst from lift tube reactor 3 to produce a product gas stream containing BTX, low-carbon olefins, hydrogen, low-carbon alkanes, combustible gases, heavy aromatic hydrocarbons, and unconverted naphtha. The catalyst from lift tube reactor 3 enters gas-solid separation device II1-9 for gas-solid separation, and the catalyst from which the gas has been removed enters between first sub-distributor 1-2-1 and second sub-distributor 1-2-2. Methanol enters the reaction zone of fluidized-bed reactor 1 through second sub-distributor 1-2-2 to third sub-distributor 1-2-3 of reactor distributor 1-2, respectively, and undergoes a methylation reaction with benzene and toluene in the product gas stream to produce paraxylene. The catalyst from lift tube reactor 3 is condensed in fluidized-bed reactor 1 and converted into spent catalyst. The product gas flow enters the gas-solid separator I1-3 to remove the entrained spent catalyst, then enters the reactor gas collection chamber 1-4 and passes through the product gas transport pipe 1-5 to enter the downstream process. The spent catalyst from the reaction zone enters the reactor stripper 1-6 through the open end of the inlet pipe, is stripped, and then passes through the spent slide valve 1-7 and the spent catalyst transport pipe 1-8 to enter the fluidized bed regenerator 2. b) The regeneration gas is introduced into the regeneration section of the fluidized-bed regenerator 2 through the regenerator distributor 2-2 and contacts the spent catalyst. The coke on the spent catalyst reacts with the regeneration gas to produce exhaust gas, and the spent catalyst is converted into regenerated catalyst. The exhaust gas enters the regenerator gas-solid separator 2-3 to remove the entrained regenerated catalyst. The exhaust gas then enters the regenerator gas collection chamber 2-4 and the exhaust gas transport pipe 2-5 to enter the downstream process. The regenerated catalyst then passes through the regenerator stripper 2-6 and the regeneration slide valve 2-7 to enter the lift tube reactor 3. c) The lift tube reactor feed is introduced into the lift tube reactor 3 and reacts with the regenerated catalyst from the fluidized bed regenerator 2. After the lift tube reactor feed is converted into aromatic hydrocarbons by the action of the catalyst, the stream containing the unreacted lift tube reactor feed, aromatic hydrocarbons, and catalyst enters the gas-solid separator II1-9 in the fluidized bed reactor 1 from the outlet of the lift tube reactor 3.

[0086] The low-carbon olefins refer to ethylene and propylene, the low-carbon alkanes refer to ethane and propane, the combustible gases include methane and CO, and the heavy aromatic hydrocarbons refer to aromatic hydrocarbons with 9 or more carbon atoms in the molecule.

[0087] In a preferred embodiment, the naphtha is at least one selected from direct coal liquefaction naphtha, indirect coal liquefaction naphtha, straight-run naphtha, and hydrocracked naphtha, and may further include unconverted naphtha separated from the product gas stream.

[0088] In a preferred embodiment, the carbon content of the used catalyst is 1.0 to 3.0 wt %, and the carbon content of the regenerated catalyst is 0.5 wt % or less.

[0089] In a preferred embodiment, the industrial conditions for the reaction zone are as follows: gas superficial linear velocity 0.5-2.0 m / s, reaction temperature 500-600°C, reaction pressure 100-500 kPa, bed density 150-700 kg / m 3 .

[0090] Optionally, the gas apparent linear velocity can be independently selected from 0.5 m / s, 0.6 m / s, 0.7 m / s, 0.8 m / s, 0.9 m / s, 1.0 m / s, 1.1 m / s, 1.2 m / s, 1.3 m / s, 1.4 m / s, 1.5 m / s, 1.6 m / s, 1.7 m / s, 1.8 m / s, 1.9 m / s, and 2.0 m / s, or a range between any two of these values.

[0091] Alternatively, the reaction temperature can be independently selected from 500°C, 510°C, 520°C, 530°C, 540°C, 550°C, 560°C, 570°C, 580°C, 590°C, and 600°C, or any range between any two of these values.

[0092] Alternatively, the reaction pressure can be independently selected from 100 kPa, 125 kPa, 150 kPa, 175 kPa, 200 kPa, 225 kPa, 250 kPa, 275 kPa, 300 kPa, 325 kPa, 350 kPa, 375 kPa, 400 kPa, 425 kPa, 450 kPa, 475 kPa, and 500 kPa, or a range between any two of these values.

[0093] Optionally, the bed density is 150 kg / m 3 , 200 kg / m 3 , 250 kg / m 3 , 300 kg / m 3 , 350 kg / m 3 , 400 kg / m 3 , 450 kg / m 3 , 500 kg / m 3 , 550 kg / m 3 , 600 kg / m 3 , 650 kg / m 3 , 700 kg / m 3 Any value, or range between any two values, can be independently selected.

[0094] In a preferred embodiment, the regeneration gas is at least one selected from oxygen, air, and oxygen-enriched air, and the industrial conditions of the regeneration zone are as follows: gas superficial linear velocity 0.5-2.0 m / s, regeneration temperature 600-750°C, regeneration pressure 100-500 kPa, bed density 150-700 kg / m 3 .

[0095] Optionally, the gas apparent linear velocity can be independently selected from 0.5 m / s, 0.6 m / s, 0.7 m / s, 0.8 m / s, 0.9 m / s, 1.0 m / s, 1.1 m / s, 1.2 m / s, 1.3 m / s, 1.4 m / s, 1.5 m / s, 1.6 m / s, 1.7 m / s, 1.8 m / s, 1.9 m / s, and 2.0 m / s, or a range between any two of these values.

[0096] Optionally, the regeneration temperature can be independently selected from any value among 600°C, 615°C, 630°C, 645°C, 660°C, 675°C, 690°C, 705°C, 720°C, 735°C, and 750°C, or a range between any two values.

[0097] Optionally, the regeneration pressure can be independently selected from any value among 100 kPa, 125 kPa, 150 kPa, 175 kPa, 200 kPa, 225 kPa, 250 kPa, 275 kPa, 300 kPa, 325 kPa, 350 kPa, 375 kPa, 400 kPa, 425 kPa, 450 kPa, 475 kPa, 500 kPa, or a range between any two values.

[0098] Optionally, the bed density is 150 kg / m 3 , 200 kg / m 3 , 250 kg / m 3 , 300 kg / m 3 , 350 kg / m 3 , 400 kg / m 3 , 450 kg / m 3 , 500 kg / m 3 , 550 kg / m 3 , 600 kg / m 3 , 650 kg / m 3 , 700 kg / m 3 Any value, or range between any two values, can be independently selected.

[0099] In a preferred embodiment, the lift tube reactor feed comprises steam and low carbon alkanes separated from the product gas stream, and the steam content is 0-50 wt%.

[0100] The industrial conditions for the lift tube reactor are as follows: gas superficial linear velocity 3.0-10.0 m / s, temperature 580-700°C, pressure 100-500 kPa, bed density 50-150 kg / m 3 .

[0101] Alternatively, the gas apparent linear velocity can be independently selected from 3.0 m / s, 3.5 m / s, 4.0 m / s, 4.5 m / s, 5.0 m / s, 5.5 m / s, 6.0 m / s, 6.5 m / s, 7.0 m / s, 7.5 m / s, 8.0 m / s, 8.5 m / s, 9.0 m / s, 9.5 m / s, and 10.0 m / s, or a range between any two values.

[0102] Optionally, the temperature can be independently selected from any value among 580°C, 590°C, 600°C, 610°C, 620°C, 630°C, 640°C, 650°C, 660°C, 670°C, 680°C, 690°C, and 700°C, or a range between any two of these values.

[0103] Optionally, the pressure can be independently selected from any value among 100 kPa, 125 kPa, 150 kPa, 175 kPa, 200 kPa, 225 kPa, 250 kPa, 275 kPa, 300 kPa, 325 kPa, 350 kPa, 375 kPa, 400 kPa, 425 kPa, 450 kPa, 475 kPa, 500 kPa, or a range between any two values.

[0104] Optionally, the bed density is 50 kg / m 3 , 60 kg / m 3 , 70 kg / m 3 , 80 kg / m 3 , 90kg / m 3 , 100 kg / m 3 , 110 kg / m 3 , 120 kg / m 3 , 130 kg / m 3 , 140 kg / m 3 , 150 kg / m 3 Any value, or range between any two values, can be independently selected.

[0105] In an embodiment of the present application, the aromatic potential content of the naphtha feedstock is 0-80 wt%, the naphtha single-pass conversion is 60-80 wt%, and the methanol single-pass conversion is approximately 100 wt%. The unconverted naphtha is separated from the product gas and returned to the fluidized-bed reactor as feedstock, and a portion of the low-carbon alkanes is separated from the product gas and returned to the lift-tube reactor as feedstock. The final product distribution is as follows: 60-71 wt% BTX, 9-16 wt% low-carbon olefins, 3-7 wt% hydrogen, 2-7 wt% low-carbon alkanes, 4-6 wt% combustible gases, 3-7 wt% heavy aromatic hydrocarbons, and 0.5-1 wt% coke. The content of paraxylene in the mixed xylenes in the product is 60-75 wt%.

[0106] Example 1 In this embodiment, the device shown in FIG. 1 is used.

[0107] In this embodiment, the naphtha feedstock supplied to the fluidized bed reactor is a direct coal liquefaction naphtha having an aromatics potential content of 78 wt %. The naphtha feedstock supplied to the fluidized bed reactor also includes unconverted naphtha separated from the product gas stream.

[0108] The industrial conditions for the reaction zone of the fluidized bed reactor are as follows: gas superficial linear velocity 0.5 m / s, reaction temperature 600°C, reaction pressure 100 kPa, bed density 700 kg / m 3 .

[0109] Air is used as the regeneration gas.

[0110] The industrial conditions for the regeneration zone of the fluidized bed regenerator are as follows: gas superficial linear velocity 0.5 m / s, regeneration temperature 745°C, regeneration pressure 100 kPa, bed density 700 kg / m 3 .

[0111] The lift tube reactor feed is made from low carbon alkanes separated from the product gas stream.

[0112] The industrial conditions for the lift tube reactor are as follows: gas superficial linear velocity 3.0 m / s, temperature 690°C, pressure 100 kPa, bed density 150 kg / m 3 .

[0113] The carbon content of the spent catalyst is 1.0 wt%, and the carbon content of the regenerated catalyst is 0.1 wt%.

[0114] The single-pass conversion of the naphtha feedstock fed to the fluidized bed reactor is 60 wt%.

[0115] The product distribution is as follows: BTX 71 wt%, low-carbon olefins 9 wt%, hydrogen 4 wt%, low-carbon alkanes 2 wt%, combustible gases 6 wt%, heavy aromatic hydrocarbons 7 wt%, and coke 1 wt%. The content of paraxylene in the mixed xylenes in the product is 66 wt%.

[0116] Example 2 In this embodiment, the device shown in FIG. 1 is used.

[0117] In this embodiment, the naphtha feedstock supplied to the fluidized bed reactor is an indirect coal liquefaction naphtha having an aromatics potential content of 0.1 wt %. The naphtha feedstock supplied to the fluidized bed reactor also includes unconverted naphtha separated from the product gas stream.

[0118] The industrial conditions for the reaction zone of the fluidized bed reactor were as follows: gas superficial linear velocity 2.0 m / s, reaction temperature 510°C, reaction pressure 500 kPa, bed density 150 kg / m 3 .

[0119] Oxygen is used as the regeneration gas.

[0120] The industrial conditions of the regeneration zone of the fluidized bed regenerator are as follows: gas superficial linear velocity 2.0 m / s, regeneration temperature 610°C, regeneration pressure 500 kPa, bed density 150 kg / m 3 .

[0121] The lift tube reactor feed contains steam (50 wt % content) and low carbon alkanes separated from the product gas stream.

[0122] The industrial conditions for the lift tube reactor were as follows: gas superficial linear velocity 10.0 m / s, temperature 580°C, pressure 500 kPa, bed density 50 kg / m 3 .

[0123] The carbon content of the spent catalyst is 3.0 wt%, and the carbon content of the regenerated catalyst is 0.3 wt%.

[0124] The single-pass conversion of the naphtha feedstock fed to the fluidized bed reactor is 77 wt%.

[0125] The product distribution is as follows: BTX 62 wt%, low-carbon olefins 15 wt%, hydrogen 7 wt%, low-carbon alkanes 4 wt%, combustible gases wt%, heavy aromatic hydrocarbons 5.5 wt%, coke 0.5 wt%. The content of paraxylene in the mixed xylenes in the product is 70 wt%.

[0126] Example 3 In this embodiment, the device shown in FIG. 1 is used.

[0127] In this embodiment, the naphtha feedstock supplied to the fluidized bed reactor is an indirect coal liquefaction naphtha having an aromatic potential content of 3 wt %, and also includes unconverted naphtha separated from the product gas stream.

[0128] The industrial conditions for the reaction zone of the fluidized bed reactor were as follows: gas superficial linear velocity 1.2 m / s, reaction temperature 550°C, reaction pressure 120 kPa, bed density 260 kg / m 3 .

[0129] Oxygen-enriched air is used as the regeneration gas.

[0130] The industrial conditions of the regeneration zone of the fluidized bed regenerator are as follows: gas superficial linear velocity 1.2 m / s, regeneration temperature 650°C, regeneration pressure 120 kPa, bed density 260 kg / m 3 .

[0131] The lift tube reactor feed contains steam (25 wt % content) and low carbon alkanes separated from the product gas stream.

[0132] The industrial conditions for the lift tube reactor are as follows: gas superficial linear velocity 7.0 m / s, temperature 630°C, pressure 120 kPa, bed density 80 kg / m 3 .

[0133] The carbon content of the spent catalyst is 2.4 wt%, and the carbon content of the regenerated catalyst is 0.2 wt%.

[0134] The naphtha feedstock fed to the fluidized bed reactor has a single-pass conversion of 80 wt%.

[0135] The product distribution is as follows: BTX 61 wt%, low-carbon olefins 16 wt%, hydrogen 7 wt%, low-carbon alkanes 7 wt%, combustible gases 5 wt%, heavy aromatic hydrocarbons 3 wt%, and coke 1 wt%. The content of paraxylene in the mixed xylenes in the product is 60 wt%.

[0136] Example 4 In this embodiment, the device shown in FIG. 1 is used.

[0137] In this embodiment, the naphtha feedstock fed to the fluidized bed reactor is straight-run naphtha having an aromatics potential content of 46 wt % and also includes unconverted naphtha separated from the product gas stream.

[0138] The industrial conditions for the reaction zone of the fluidized bed reactor were as follows: gas superficial linear velocity 1.8 m / s, reaction temperature 590°C, reaction pressure 200 kPa, bed density 220 kg / m 3 .

[0139] Air is used as the regeneration gas.

[0140] The industrial conditions of the regeneration zone of the fluidized bed regenerator are as follows: gas superficial linear velocity 1.8 m / s, regeneration temperature 700°C, regeneration pressure 200 kPa, bed density 220 kg / m 3 .

[0141] The lift tube reactor feed contains steam (50 wt. %) and low carbon alkanes separated from the product gas stream.

[0142] The industrial conditions for the lift tube reactor were as follows: gas superficial linear velocity 5.0 m / s, temperature 660°C, pressure 200 kPa, bed density 110 kg / m 3 .

[0143] The carbon content of the spent catalyst is 1.8 wt%, and the carbon content of the regenerated catalyst is 0.1 wt%.

[0144] The single-pass conversion of the naphtha feedstock fed to the fluidized bed reactor is 66 wt%.

[0145] The product distribution is as follows: BTX 66 wt%, low-carbon olefins 14 wt%, hydrogen 3 wt%, low-carbon alkanes 6 wt%, combustible gases 4 wt%, heavy aromatic hydrocarbons 6.4 wt%, coke 0.6 wt%. The content of paraxylene in the mixed xylenes in the product is 75 wt%.

[0146] Example 5 In this embodiment, the device shown in FIG. 1 is used.

[0147] In this embodiment, the naphtha feedstock fed to the fluidized bed reactor is a hydrocracked naphtha having an aromatic potential content of 64 wt % and also includes unconverted naphtha separated from the product gas stream.

[0148] The industrial conditions for the reaction zone of the fluidized bed reactor were as follows: gas superficial linear velocity 1.0 m / s, reaction temperature 580°C, reaction pressure 150 kPa, bed density 350 kg / m3 .

[0149] Air is used as the regeneration gas.

[0150] The industrial conditions of the regeneration zone of the fluidized bed regenerator are as follows: gas superficial linear velocity 1.0 m / s, regeneration temperature 680°C, regeneration pressure 150 kPa, bed density 350 kg / m 3 .

[0151] The lift tube reactor feed contains steam (40 wt %) and low carbon alkanes separated from the product gas stream.

[0152] The industrial conditions for the lift tube reactor are as follows: gas superficial linear velocity 7.0 m / s, temperature 650°C, pressure 150 kPa, bed density 80 kg / m 3 .

[0153] The carbon content of the spent catalyst is 1.4 wt%, and the carbon content of the regenerated catalyst is 0.5 wt%.

[0154] The single-pass conversion of the naphtha feedstock fed to the fluidized bed reactor is 71 wt%.

[0155] The product distribution is as follows: BTX 70wt%, low-carbon olefins 11.3wt%, hydrogen 5wt%, low-carbon alkanes 2wt%, combustible gases 5wt%, heavy aromatic hydrocarbons 6wt%, and coke 0.7wt%. The content of paraxylene in the mixed xylenes in the product is 71wt%.

[0156] The above description is only a partial example of the present application and does not limit the present application in any way. In the present application, more preferred embodiments are disclosed as above, but they are not intended to limit the present application. Various variations and modifications made by a person skilled in the art using the technical content disclosed above without departing from the technical solution of the present application are all equivalent to equivalent embodiments, and all fall within the scope of the technical solution. [Explanation of symbols]

[0157] 1. Fluidized bed reactor 1-1 Reactor housing 1-2 Reactor distributor 1-3 First solid-gas separator of fluidized bed reactor 1-4 Reactor gas collection chamber 1-5 Produced gas transport pipe 1-6 Fluidized bed reactor stripper 1-7 Used sliding valve 1-8 Spent agent transport pipe 1-9 Second solid-gas separator for fluidized bed reactor 1-2-1 First child distributor 1-2-2 2nd child distributor 1-2-3 Third child distributor 2 Fluidized bed regenerator 2-1 Regenerator housing 2-2 Regenerator distributor 2-3 First solid-gas separator of the regenerator 2-4 Regenerator gas collection chamber 2-5 Exhaust gas transport pipe 2-6 Regenerator stripper 2-7 Regenerative sliding valve 3. Lift tube reactor

Claims

1. A circulating fluidized bed reaction regeneration apparatus comprising a fluidized bed reactor, a fluidized bed regenerator and a lift tube reactor, the fluidized bed reactor is used to pass a naphtha feedstock and a methanol feedstock, the naphtha feedstock contacting the catalyst from the lift tube reactor to produce a product gas stream containing BTX and spent catalyst, the methanol feedstock undergoing a methylation reaction with benzene and toluene in the BTX-containing product gas stream to produce paraxylene; subjecting the product gas stream to gas-solid separation, transporting the separated product gas to a downstream process, returning unreacted naphtha as a feedstock to the fluidized bed reactor, returning a portion of low-carbon paraffins as a feedstock to the lift tube reactor, and passing the spent catalyst through the fluidized bed regenerator; A circulating fluidized bed reaction regeneration apparatus, characterized in that the inlet of the lift tube reactor is connected to a fluidized bed regenerator, and the outlet of the lift tube reactor is connected to a fluidized bed reactor.

2. The fluidized bed reactor includes a reactor housing, and the area enclosed by the reactor housing is divided into a first gas-solid separation section and a reaction section from top to bottom. The reaction section is provided with a reactor distributor, and includes n sub-distributors, which are arranged from the first sub-distributor to the nth sub-distributor from bottom to top, where n≧2 and n≦10. the first sub-distributor is used to pass naphtha feedstock; 2. The circulating fluidized bed reaction regeneration apparatus according to claim 1, wherein the second to n-th sub-distributors are used to pass a methanol raw material.

3. The first gas-solid separation section is equipped with a gas-solid separation device I, a gas-solid separation device II and a reactor gas collection chamber; The gas outlet of the gas-solid separation device I is in communication with the reactor gas collection chamber; the reactor gas collection chamber is in communication with a product gas transport pipe; The inlet of the gas-solid separation device II communicates with the lift tube reactor; The gas outlet of the gas-solid separator II is in communication with the reactor gas collection chamber; 3. The circulating fluidized bed reaction regeneration apparatus according to claim 2, wherein the catalyst outlet end of the gas-solid separation device II is located above the open end of the reactor stripper inlet pipe and between the first sub-distributor and the second sub-distributor.

4. 4. The circulating fluidized bed reaction regeneration apparatus according to claim 3, wherein the reactor gas collection chamber is located at the inner top of the reactor housing.

5. 4. The circulating fluidized bed reaction regeneration apparatus according to claim 3, wherein the gas-solid separation device I uses one or more sets of gas-solid cyclone separators, and each set of gas-solid cyclone separators includes one first-class gas-solid cyclone separator and one second-class gas-solid cyclone separator.

6. 2. The circulating fluidized bed reaction regeneration apparatus according to claim 1, wherein the fluidized bed regenerator is connected to the fluidized bed reactor and is used to pass a regeneration gas through the fluidized bed regenerator to regenerate the spent catalyst from the fluidized bed reactor and obtain a regenerated catalyst.

7. The fluidized bed reactor is sequentially connected to the fluidized bed regenerator via a reactor stripper, a spent slide valve, and a spent agent transport pipe; 7. The circulating fluidized bed reaction regeneration apparatus according to claim 6, wherein the inlet of the reactor stripper extends into the reactor housing of the fluidized bed reactor, and the open end is located below the catalyst outlet end of the gas-solid separation device I and above the first sub-distributor.

8. The fluidized bed regenerator includes a regenerator housing, and the area enclosed by the regenerator housing is divided into a second gas-solid separation section and a regeneration section from top to bottom; The second gas-solid separation section is provided with a regenerator gas-solid separation device and a regenerator gas collection chamber; The regenerator gas collecting chamber is located at the inner top of the regenerator housing, and an exhaust gas transport pipe is provided thereon; a gas outlet of the regenerator gas-solid separation device communicating with the regenerator gas collection chamber; 2. The circulating fluidized bed reactor regeneration apparatus according to claim 1, wherein a regenerator distributor is provided in the lower part of the regeneration section, for passing regeneration gas therethrough.

9. 9. The circulating fluidized bed reaction regeneration apparatus according to claim 8, wherein the regenerator gas-solid separation device uses one or more sets of gas-solid cyclone separators, and each set of gas-solid cyclone separators includes one first-class gas-solid cyclone separator and one second-class gas-solid cyclone separator.

10. 2. The circulating fluidized bed reaction regeneration apparatus according to claim 1, wherein the lift tube reactor is used to pass a lift tube reactor feedstock and a catalyst to produce aromatics, and a stream containing unreacted lift tube reactor feedstock, aromatics, and catalyst enters a fluidized bed reactor through the outlet of the lift tube reactor.

11. 2. The circulating fluidized bed reaction regeneration apparatus according to claim 1, wherein the inlet of the lift tube reactor is connected to a fluidized bed regenerator, and the catalyst passed through the lift tube reactor is a regenerated catalyst produced in the fluidized bed regenerator.

12. 12. The circulating fluidized bed reaction regeneration apparatus according to claim 11, wherein the fluidized bed regenerator is connected to the inlet of the lift pipe reactor by piping through a regenerator stripper and a regeneration slide valve in this order.

13. 13. The circulating fluidized bed reactor regenerator according to claim 12, wherein the inlet of the regenerator stripper extends into the regenerator housing of the fluidized bed regenerator and is located above the regenerator distributor.

14. 14. A method for applying the apparatus according to any one of claims 1 to 13, comprising producing aromatics using the circulating fluidized bed reactor regenerator and a metal zeolite bifunctional catalyst.

15. The metal zeolite bifunctional catalyst uses a metal-modified HZSM-5 zeolite molecular sieve; The metal used for the metal modification is at least one selected from La, Zn, Ga, Fe, Mo, and Cr, 15. The method of claim 14, wherein the metal modification method comprises immersing HZSM-5 zeolite molecular sieve in a metal salt solution, drying, and calcining to obtain the metal-modified HZSM-5 zeolite molecular sieve.

16. The method comprises: a naphtha feedstock is introduced into a reaction zone of a fluidized bed reactor through a first sub-distributor of a reactor distributor and contacted with the catalyst from the lift tube reactor to produce a product gas stream comprising BTX, light olefins, hydrogen, light paraffins, combustible gases, heavy aromatics, and unreacted naphtha; the methanol feedstock is fed through the second sub-distributor to the nth sub-distributor of the reactor distributor into the reaction zone of the fluidized bed reactor, where it undergoes a methylation reaction with the benzene and toluene in the product gas stream to produce paraxylene; 15. The method of claim 14, further comprising: the fluidized bed reactor outputting the product gas to a downstream process.

17. 17. The method of claim 16, wherein before the fluidized bed reactor outputs the product gas, a gas-solid separation device I is used to first perform gas-solid separation to remove spent catalyst entrained in the product gas flow.

18. 17. The method of claim 16, wherein the catalyst from the lift tube reactor enters the fluidized bed reactor and then is first separated into gas and solid by a gas-solid separator II, and the catalyst from which the gas has been removed passes through the catalyst outlet of the gas-solid separator II and enters between the first sub-distributor and the second sub-distributor.

19. The low carbon olefins refer to ethylene and propylene; The low carbon paraffin refers to ethane and propane; the flammable gas includes methane and CO; 17. The method of claim 16, wherein the heavy aromatic refers to an aromatic having 9 or more carbon atoms in the molecule.

20. 17. The method of claim 16, wherein the naphtha is at least one selected from the group consisting of direct coal liquefaction naphtha, indirect coal liquefaction naphtha, straight-run naphtha, and hydrocracked naphtha.

21. The naphtha further comprises unreacted naphtha separated from the product gas stream, the unreacted naphtha comprising a major component of C ４ -C １２ 21. The method of claim 20, wherein the hydrocarbons are linear, branched, aliphatic hydrocarbons and naphthenes.

22. The process conditions of the reaction zone of the fluidized bed reactor are: gas superficial linear velocity 0.5-2.0 m / s, reaction temperature 500-600°C, reaction pressure 100-500 kPa, bed density 150-700 kg / m ３ 17. The method of claim 16, wherein:

23. 17. The application method of claim 16, further comprising: introducing the spent catalyst produced in the fluidized bed reactor into a fluidized bed regenerator; passing a regeneration gas through the regeneration section of the fluidized bed regenerator to contact the spent catalyst, and obtaining exhaust gas and regenerated catalyst by reaction.

24. The application method of claim 23, wherein the exhaust gas enters the regenerator gas-solid separation device to remove the regenerated catalyst mixed therein, then enters the regenerator gas collection chamber, and then enters the downstream process through the exhaust gas transport pipe.

25. 24. The method of claim 23, further comprising: the regenerated catalyst sequentially passing through a regenerator stripper and a regeneration slide valve into a lift tube reactor.

26. The method of claim 23, wherein the carbon content in the spent catalyst is 1.0-3.0 wt%.

27. 24. The method of claim 23, wherein the carbon content in the regenerated catalyst is less than 0.5 wt.%.

28. 24. The method of claim 23, wherein the regeneration gas is at least one selected from the group consisting of oxygen, air, and oxygen-enriched air.

29. The process conditions of the regeneration section of the fluidized bed regenerator are: gas superficial linear velocity 0.5-2.0 m / s, regeneration temperature 600-750°C, regeneration pressure 100-500 kPa, bed density 150-700 kg / m ３ 24. The method of claim 23, wherein:

30. The method further includes passing the lift tube reactor feed and the catalyst through a lift tube reactor to produce aromatics; 17. The method of claim 16, further comprising: feeding a stream containing unreacted lift tube reactor feed, aromatics, and catalyst from the outlet of the lift tube reactor into a gas-solid separator II of the fluidized bed reactor.

31. 31. The method of claim 30, wherein the catalyst is regenerated catalyst from a fluidized bed regenerator.

32. 31. The method of claim 30, wherein the lift tube reactor feed comprises steam and low carbon paraffins separated from the product gas stream.

33. 31. The method of claim 30, wherein the steam content in the lift tube reactor feed is 0-50 wt%.

34. The process conditions of the lift tube reactor are: gas superficial linear velocity 3.0-10.0 m / s, temperature 580-700°C, pressure 100-500 kPa, bed density 50-150 kg / m ３ 31. The method of claim 30, wherein:

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