Naphtha-based aromatic fluidized bed apparatus and method

Abstract

This application discloses a naphtha aromatics fluidized bed apparatus and method. The apparatus includes at least a light hydrocarbon aromatization reactor and a naphtha aromatics reactor connected in series, where a high-temperature regenerated catalyst first enters the light hydrocarbon aromatization reactor and then, after its temperature has been reduced, enters the naphtha aromatics reactor. The application's method involves producing aromatics using the apparatus and a metal zeolite bifunctional catalyst. The naphtha can be converted into a product gas containing aromatics, low-carbon paraffins, and other components under the action of the catalyst. The low-carbon paraffins and other components separated from the product gas enter the light hydrocarbon aromatization reactor and are further converted into aromatics and other components. The application's method can convert linear and branched aliphatic hydrocarbons into aromatics with high selectivity, and the paraxylene content in the xylene mixture exceeds 50 wt%.

Description

[Technical Field]

[0001] The present application relates to a fluidized bed apparatus and a method for using the same, and belongs to the chemical industry technical field, and in particular to a naphtha aromatics fluidized bed apparatus 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] Naphtha fractions have a relatively broad distillation range, making it 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. Naphtha feedstocks used in catalytic reforming typically require distillation to remove light fractions with boiling points below 60°C to increase the aromatic potential of the 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 aromatic compound production technologies from naphtha. Summary of the Invention [Problem to be solved by the invention]

[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. [Means for solving the problem]

[0006] One aspect of the present application provides a fluidized bed apparatus capable of producing aromatics using naphtha having a low aromatic potential content as a feedstock, the apparatus increasing the content of para-xylene in mixed xylenes and reducing production energy consumption.

[0007] In this application, naphtha components are C4-C 12 These include straight chain aliphatic hydrocarbons, branched aliphatic hydrocarbons, cyclic alkanes and aromatic hydrocarbons.

[0008] In this application, aromatic hydrocarbons refer to benzene, toluene, and xylene, collectively referred to as BTX.

[0009] the naphtha aromatics fluidized bed apparatus comprises a light hydrocarbon aromatization reactor and a naphtha aromatics reactor; The light hydrocarbon aromatization reactor has at least one inlet for passing a feedstock and a hot catalyst; At least one outlet of the light hydrocarbon aromatization reactor is connected to the naphtha aromatics reactor and is used to transport the catalyst and the produced light hydrocarbon aromatization product gas to the naphtha aromatics reactor; The naphtha aromatics reactor is used to pass naphtha through and react with the catalyst from the light hydrocarbon aromatization reactor, and then produce a product gas stream containing BTX, wherein the BTX-containing product gas stream comprises a light hydrocarbon aromatization product gas.

[0010] The catalyst temperature decreases when it enters the reactor for producing aromatic compounds from naphtha. At this time, contact with naphtha can eliminate local high temperature areas in the reactor for producing aromatic compounds from naphtha, thereby effectively reducing the yield of low carbon number alkanes and increasing the yield of aromatic compounds.

[0011] Preferably, the naphtha aromatics reactor is further provided with a product gas transport pipe I, which is used to output the product gas stream containing BTX to a downstream process.

[0012] Preferably, the light hydrocarbon aromatization reactor further comprises a regenerator, and at least one inlet of the light hydrocarbon aromatization reactor is connected to the regenerator and used to obtain the high-temperature regenerated catalyst produced in the regenerator.

[0013] Preferably, the light hydrocarbon aromatization reactor is divided into a gas-solid separation section II and a light hydrocarbon aromatization reaction section II, which are at least connected from top to bottom, and constitutes a bed reactor; The gas-solid separation section II is provided with a gas-solid separator II and a gas collecting chamber II, and the gas outlet of the gas-solid separator II is connected to the gas collecting chamber II; The lower part of the light hydrocarbon aromatization reaction section is provided with a bed reactor distributor, which is used to pass the bed reactor feed.

[0014] Preferably, the gas collection chamber II is installed at the inner top of the bed reactor.

[0015] Preferably, the bed reactor feed comprises C4 and C5 hydrocarbons.

[0016] Preferably, the light hydrocarbon aromatization reactor further comprises a lift tube reactor in addition to the bed reactor; an inlet end of said lift tube reactor communicating with said regenerator; The outlet end of the lift tube reactor extends to the lower part of the light hydrocarbon aromatization reaction zone, and the upper part is the catalyst outlet of the gas-solid separation device II.

[0017] Preferably, the inlet end of the lift tube reactor is further used to pass catalyst and lift tube reactor feed.

[0018] Preferably, the naphtha aromatics reactor is divided into a gas-solid separation section I and a naphtha aromatics reaction section I, which are at least connected from top to bottom; The gas-solid separation section I is provided with a gas-solid separation device I and a gas collection chamber I; The gas outlet of the gas-solid separator I is in communication with the gas collection chamber I; A naphtha aromatics reactor distributor is provided in the lower part of the naphtha aromatics reaction section, and is used to pass the naphtha raw material.

[0019] Preferably, the gas-solid separation device I uses at least one set of gas-solid cyclone separators, each set of gas-solid cyclone separators including a first-class gas-solid cyclone separator and a second-class gas-solid cyclone separator. Preferably, the gas collection chamber I is located at the top of the naphtha aromatic reactor.

[0020] Preferably, the gas collection chamber I communicates with the product gas transport pipe I.

[0021] Preferably, the gas-solid separation section I communicates with the gas-solid separation section II, and the naphtha aromatics reaction section of the naphtha aromatics reactor communicates with the light hydrocarbon aromatization reaction section.

[0022] Preferably, the gas-solid separation section I is connected to a gas collection chamber II via a product gas transport pipe II.

[0023] Preferably, a light hydrocarbon aromatization slide valve is installed in the pipeline connected between the naphtha aromatics reaction section and the light hydrocarbon aromatization reaction section of the naphtha aromatics reactor.

[0024] Preferably, the outlet position of the light hydrocarbon aromatization reaction section is higher than the inlet position of the naphtha aromatics reaction section of the naphtha aromatics reactor.

[0025] Preferably, the regenerator is divided into a gas-solid separation section III and a catalyst regeneration section III, which are at least connected from top to bottom; The gas-solid separation section III is provided with a regenerator gas-solid separation device and a regenerator gas collecting chamber; a gas outlet of the regenerator gas-solid separation device communicating with the regenerator gas collection chamber; The regenerator gas collection chamber is provided with an exhaust gas transport pipe; A regenerator distributor is provided at the bottom of the catalyst regeneration section, and is used to pass the regeneration gas.

[0026] Preferably, the catalyst regeneration section is connected to the light hydrocarbon aromatization reactor via a regenerator stripper and a regeneration slide valve; the regenerator stripper inlet pipe extends into the regenerator housing and is located above the regenerator distributor; The catalyst outlet end of the regenerator gas-solid separation device is located above the open end of the inlet pipe of the regenerator stripper.

[0027] Preferably, the regenerator gas collection chamber is located at the top of the interior of the regenerator housing.

[0028] Preferably, at least one outlet of the naphtha aromatics reactor is further connected to the inlet of the regenerator, and is used to pass the spent catalyst produced by the reaction in the naphtha aromatics reactor through the regenerator; The regenerator is used to pass a regeneration gas through it to convert the spent catalyst into a regenerated catalyst.

[0029] Preferably, the naphtha aromatics reaction section of the naphtha aromatics reactor is connected to the inlet of the regenerator through a reactor stripper, a spent slide valve, and a spent reagent transport pipe; the reactor stripper inlet pipe extends into the naphtha aromatics reactor housing and is located above the naphtha aromatics reactor distributor; The catalyst outlet end of the gas-solid separator I is located above the open end of the inlet pipe of the reactor stripper.

[0030] Preferably, the catalyst inlet of the regenerator is located on the regenerator housing.

[0031] According to another aspect of the present application, there is provided a method for producing aromatic compounds from naphtha, the method including producing aromatic compounds using the above-described fluidized bed apparatus for producing aromatic compounds from naphtha.

[0032] Furthermore, this method is as follows: passing the feedstock and the hot catalyst through a light hydrocarbon aromatization reactor to produce a light hydrocarbon aromatization product gas; 24. The method for producing aromatics from naphtha according to claim 23, further comprising passing the naphtha and the catalyst from the light hydrocarbon aromatization reactor and the light hydrocarbon aromatization product gas through a naphtha aromatics reactor to produce a product gas stream comprising BTX.

[0033] Preferably, the catalyst is a metal zeolite bifunctional catalyst.

[0034] Preferably, the metal zeolite bifunctional catalyst uses a metal-modified HZSM-5 zeolite molecular sieve, and 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.

[0035] Preferably, the components of the light hydrocarbon aromatization product gas include BTX, low carbon olefins, and H2.

[0036] Preferably, the BTX-containing product gas stream contains, in addition to BTX, light olefins, hydrogen, light paraffins, combustible gases, heavy aromatics, and unreacted naphtha.

[0037] Preferably, the low carbon olefins refer to ethylene and propylene. The low carbon paraffins refer to ethane and propane; The combustible gases include methane and CO, and the heavy aromatics refer to aromatics having 9 or more carbon atoms in the molecule.

[0038] Preferably, the step of passing the feedstock and the high-temperature catalyst through the light hydrocarbon aromatization reactor to produce a light hydrocarbon aromatization product gas specifically comprises: The method includes passing the bed reactor feedstock through a bed reactor distributor to a light hydrocarbon aromatization reaction zone, where it contacts with the catalyst passed through the bed reactor, and producing a light hydrocarbon aromatization product gas.

[0039] 32. The method for producing aromatics from naphtha according to claim 31, wherein the bed reactor feed preferably comprises C4 and C5 hydrocarbons.

[0040] Additionally, the bed reactor feed contains C4 and C5 hydrocarbons.

[0041] Preferably, the bed reactor feed comprises C3, C4, and C5 hydrocarbons.

[0042] Preferably, the C4 and C5 hydrocarbons are derived from C4 and C5 hydrocarbons separated from the product gas stream.

[0043] Preferably, the C3, C4, and C5 hydrocarbons are derived from C3, C4, and C5 hydrocarbons separated from the product gas stream.

[0044] The C3, C4 and C5 hydrocarbons mentioned above refer to hydrocarbons with 3, 4 and 5 carbon atoms, respectively.

[0045] Preferably, the process conditions for the light hydrocarbon aromatization reaction zone are: gas superficial linear velocity of 0.5-2.0 m / s, reaction temperature of 550-665°C, reaction pressure of 100-500 kPa, and bed density of 150-700 kg / m 3 is.

[0046] Alternatively, the gas apparent linear velocity may 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.

[0047] Alternatively, the reaction temperature can be independently selected from 550°C, 560°C, 570°C, 580°C, 590°C, 600°C, 610°C, 620°C, 630°C, 640°C, 650°C, 660°C, and 665°C, or any value in a range between any two of these values.

[0048] 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.

[0049] 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 value between any two values ​​can be independently selected.

[0050] Preferably, the method further comprises removing catalyst entrained in the light hydrocarbon aromatization product gas in gas-solid separation section II of the light hydrocarbon aromatization reactor.

[0051] Preferably, the catalyst in the light hydrocarbon aromatization reaction zone enters the naphtha aromatics reactor through the light hydrocarbon aromatization slide valve.

[0052] Preferably, the step of removing the catalyst mixed in the light hydrocarbon aromatization product gas in the gas-solid separation section II specifically comprises: The light hydrocarbon aromatization product gas is introduced into the gas-solid separation device II, and after removing the catalyst mixed in, it enters the gas collection chamber II and then enters the gas-solid separation section I of the naphtha aromatics reactor through the product gas transport pipe II.

[0053] Preferably, the naphtha enters the naphtha aromatics reaction zone of the naphtha aromatics reactor through a naphtha aromatics reactor distributor and contacts the catalyst from the light hydrocarbon aromatization reactor to produce a product gas stream comprising BTX, while the catalyst is coked and converted to spent catalyst.

[0054] Preferably, the method further comprises removing spent catalyst from the BTX-containing product gas stream in gas-solid separation section I of the naphtha aromatics reactor and transporting it to downstream processing.

[0055] Preferably, the naphtha is at least one selected from direct coal liquefaction naphtha, indirect coal liquefaction naphtha, straight-run naphtha, and hydrocracked naphtha.

[0056] Preferably, the naphtha further comprises unreacted naphtha separated from the product gas stream, the unreacted naphtha being primarily composed of C4-C12 linear and branched aliphatics and naphthenes.

[0057] Preferably, the process conditions of the naphtha aromatics reaction section are: gas superficial linear velocity of 0.5-2.0 m / s, reaction temperature of 500-650°C, reaction pressure of 100-500 kPa, bed density of 150-700 kg / m 3 is.

[0058] Alternatively, the gas apparent linear velocity may 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.

[0059] Alternatively, the reaction temperature can be independently selected from 500°C, 520°C, 530°C, 540°C, 550°C, 560°C, 570°C, 580°C, 590°C, 600°C, 610°C, 620°C, 630°C, 640°C, and 650°C, or any value within a range between any two of these values.

[0060] 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.

[0061] 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 value between any two values ​​can be independently selected.

[0062] Additionally, the method further includes passing the regeneration gas and the spent catalyst through a regenerator to obtain hot regenerated catalyst, which is transported to the light hydrocarbon aromatization reactor.

[0063] Preferably, the regeneration gas is passed to the regeneration section of the regenerator via a regenerator distributor.

[0064] Preferably, the regeneration gas is at least one selected from oxygen, air, and oxygen-enriched air.

[0065] Preferably, the carbon content in the spent catalyst is 1.0-3.0 wt %.

[0066] Preferably, the carbon content in the regenerated catalyst is 0.5 wt % or less.

[0067] Preferably, the process conditions of the regeneration section of the 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.

[0068] Alternatively, the gas apparent linear velocity may 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.

[0069] Alternatively, the regeneration temperature can be independently selected from any value or range between any two of 600°C, 615°C, 630°C, 645°C, 670°C, 685°C, 700°C, 715°C, 730°C, 745°C, and 750°C.

[0070] Alternatively, the regeneration pressure may 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 value within a range between any two of these values.

[0071] 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 3Any value or range value between any two values ​​can be independently selected.

[0072] Preferably, the coke on the spent catalyst reacts with the regeneration gas to produce exhaust gas, which enters gas-solid separation section III to remove the regenerated catalyst entrained therein.

[0073] Preferably, the process of the exhaust gas entering the gas-solid separation section III and removing the regenerated catalyst mixed therein specifically includes the following: the exhaust gas first enters the regenerator gas-solid separation device, and after removing the regenerated catalyst mixed therein, passes through the regenerator gas collection chamber and the exhaust gas transport pipe and enters the downstream process.

[0074] Preferably, the regenerated catalyst enters the light hydrocarbon aromatization reactor via a regenerator stripper and a regeneration slide valve.

[0075] Preferably, the method further includes passing a lift tube reactor feedstock through the inlet end of the lift tube reactor of the light hydrocarbon aromatization reactor, passing the regenerated catalyst through a regenerator stripper and a regeneration slide valve into the lift tube reactor, and converting the lift tube reactor feedstock into a stream containing BTX under the action of the regenerated catalyst, which then enters the lower part of the light hydrocarbon aromatization reaction zone in the bed reactor through the outlet end of the lift tube reactor.

[0076] Additionally, the method further comprises passing the catalyst through the inlet end of a lift tube reactor of the light hydrocarbon aromatization reactor, through the lift tube reactor, and into the bed reactor.

[0077] Preferably, the lift tube reactor feedstock contains steam and low-carbon paraffins separated from the product gas stream. Low-carbon alkanes are highly stable and require relatively high reaction temperatures. Therefore, in this application, a high-temperature regenerated catalyst is first introduced into the light hydrocarbon aromatization reactor and contacted with low-carbon alkanes, C4, and C5 hydrocarbons. This allows the low-carbon alkanes, C4, and C5 hydrocarbons to aromatize under the action of the catalyst, thereby improving the yield of aromatic hydrocarbons.

[0078] Preferably, the steam content in the lift tube reactor feed is 0-80 wt%.

[0079] 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.

[0080] Alternatively, the gas apparent linear velocity may 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.

[0081] Alternatively, the temperature can be independently selected from 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.

[0082] Alternatively, the pressure may 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, 500 kPa, or a range between any two of these values.

[0083] 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 from, or a range value between, any two values ​​can be independently selected.

[0084] Preferably, the components of the BTX-containing stream include BTX, low carbon olefins, and H2.

[0085] Preferably, the method further comprises: The spent catalyst in the naphtha aromatics reaction section of the naphtha aromatics reactor is passed through a reactor stripper, stripped, and then enters a downstream region via a spent slide valve and a spent agent transport pipe.

[0086] Preferably, the downstream region is a regenerator.

[0087] In the present application, the aromatic potential content of the naphtha feedstock is 0 to 80 wt%, and the single-pass conversion rate of the naphtha is 70 to 95 wt%. By using the fluidized bed apparatus for producing aromatic compounds from naphtha and the method for producing aromatic compounds from naphtha based on the apparatus of the present application, the final product composition is as follows: 60 to 75 wt% BTX, 6 to 14 wt% low-carbon olefins, 3 to 7 wt% hydrogen, 3 to 8 wt% low-carbon alkanes, 4 to 6 wt% combustible gases, 4 to 8 wt% heavy aromatic hydrocarbons, and 0.5 to 1 wt% coke. The content of paraxylene in the mixed xylenes in the product is 50 to 65 wt%. [Effects of the Invention]

[0088] 1) This invention can convert linear and branched aliphatic hydrocarbons into aromatic hydrocarbons with high selectivity. It can be used with a wide range of raw materials, and can produce aromatic hydrocarbons using naphtha with a low aromatic potential content as a raw material. 2) In this application, by using a light hydrocarbon aromatization reactor and a metal molecular sieve bifunctional catalyst, the aromatization reaction of low-carbon alkanes, C4 and C5 hydrocarbons was realized, and the yield of aromatic hydrocarbons in the technology of producing aromatic compounds from naphtha was significantly improved. 3) In the aromatic hydrocarbon product produced in this application, the content of paraxylene in the xylene mixture exceeds 50 wt%, which is much higher than the content at thermodynamic equilibrium (about 24 wt%), which effectively increases the yield of paraxylene and significantly reduces the energy consumption required for paraxylene separation. 4) In this application, unconverted naphtha is separated from the product gas and returned to the naphtha aromatics reactor as a feedstock, some low-carbon alkanes are separated from the product gas and returned to the lift tube reactor of the light hydrocarbon aromatization reactor as a feedstock, and C3, C4, and C5 hydrocarbons are separated from the product gas and returned to the bed reactor of the light hydrocarbon aromatization reactor as a feedstock.Furthermore, a regenerator is provided to regenerate the catalyst, thereby realizing closed-loop production of aromatic hydrocarbons. 5) In this application, a high-temperature light hydrocarbon aromatization reactor and a relatively low-temperature naphtha aromatics reactor are connected in series. A high-temperature catalyst first enters the light hydrocarbon aromatization reactor, and the low-carbon alkanes, C4, and C5 hydrocarbons in the reactor undergo aromatization under the action of the catalyst, improving the yield of aromatic hydrocarbons. The lower-temperature catalyst then enters the naphtha aromatics reactor and comes into contact with the naphtha, thereby eliminating localized high-temperature areas in the naphtha aromatics reactor, effectively reducing the yield of low-carbon alkanes and increasing the yield of aromatic hydrocarbons. [Brief explanation of the drawings]

[0089] [Figure 1] FIG. 1 illustrates a naphtha aromatic fluidized bed apparatus according to an embodiment of the present application. DETAILED DESCRIPTION OF THE INVENTION

[0090] The present application will be described in detail below with reference to embodiments, but is not limited to these embodiments.

[0091] The present application provides a naphtha aromatics fluidized bed apparatus including a light hydrocarbon aromatization reactor and a naphtha aromatics reactor, wherein: The light hydrocarbon aromatization reactor has at least one inlet, which is used to introduce a raw material and a high-temperature catalyst; and at least one outlet of the light hydrocarbon aromatization reactor is connected to the naphtha aromatics reactor, which is used to send the catalyst and the light hydrocarbon aromatization product gas produced to the naphtha aromatics reactor. The naphtha aromatics reactor receives naphtha and reacts it with the catalyst from the light hydrocarbon aromatization reactor to produce a product gas stream comprising BTX.

[0092] The components of naphtha in this application are C4-C 12 These include straight-chain, branched aliphatic hydrocarbons, naphthenic and aromatic hydrocarbons.

[0093] In this application, BTX or aromatic hydrocarbons refers to benzene, toluene, and xylene.

[0094] In a preferred embodiment, the naphtha aromatics reactor is further equipped with a product gas delivery line I, which is used to deliver the BTX-containing product gas stream to downstream processes.

[0095] In a preferred embodiment, the apparatus further includes a regenerator, and at least one inlet of the light hydrocarbon aromatization reactor is connected to the regenerator and used to obtain the high-temperature regenerated catalyst produced in the regenerator.

[0096] Please refer to Figure 1. This figure shows a naphtha aromatics fluidized bed apparatus in a preferred embodiment of the present application, which includes a naphtha aromatics reactor 1, a regenerator 2 and a light hydrocarbon aromatization reactor 3.

[0097] The naphtha aromatics reactor 1 includes a naphtha aromatics reactor housing 1-1, a naphtha aromatics reactor distributor 1-2, a gas-solid separator I1-3, a gas collection chamber I1-4, a product gas transport pipe I1-5, a reactor stripper 1-6, a spent sliding valve 1-7, and a spent agent transport pipe 1-8.

[0098] The naphtha aromatics reactor housing 1-1 includes an upper reactor housing and a lower reactor housing, the upper reactor housing forms a gas-solid separation section, and the lower reactor housing forms a naphtha aromatics reaction section. The naphtha aromatics reactor housing 1-1 is provided with an outlet for the light hydrocarbon aromatization reactor 3.

[0099] The naphtha aromatics reactor distributor 1-2 is installed below the naphtha aromatics reaction section and is used to introduce naphtha raw material.

[0100] The naphtha aromatic reactor housing 1-1 is also provided with a gas-solid separator I1-3 and a gas collection chamber I1-4. The gas collection chamber I1-4 is located at the inner top of the naphtha aromatic reactor housing. The gas outlet of the gas-solid separator I1-3 communicates with the gas collection chamber I1-4, and the gas collection chamber I1-4 communicates with the product gas transport pipe I1-5. The catalyst outlet end of the gas-solid separator I1-3 is located above the open end of the inlet pipe of the reactor stripper 1-6.

[0101] A reactor stripper 1-6 is provided below the naphtha aromatics reaction section, the inlet of which is located inside the naphtha aromatics reactor housing 1-1, and the outlet of which is located outside the naphtha aromatics reactor housing 1-1 and connected to a used slide valve 1-7. The open end of the inlet of the reactor stripper 1-6 is located above the naphtha aromatics reactor distributor 1-2.

[0102] A used slide valve 1-7 is provided below the reactor stripper 1-6. The inlet of the used slide valve 1-7 is connected to the outlet of the reactor stripper 1-6, the outlet of the used slide valve 1-7 is connected to the inlet of a used agent transport pipe 1-8, and the outlet of the used agent transport pipe 1-8 is connected to the regenerator housing 2-1.

[0103] The spent slide valve 1-7 is used to control the circulation rate of the spent catalyst.

[0104] 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.

[0105] The 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.

[0106] 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.

[0107] The regenerator housing 2-1 is provided with an outlet for a spent agent transport pipe 1-8.

[0108] A regenerator distributor 2-2 is installed at the bottom of the regeneration section, and is used to introduce regeneration gas.

[0109] The regenerator housing 2-1 is also provided with a regenerator gas-solid separator 2-3 and a regenerator gas collecting chamber 2-4. The regenerator gas collecting chamber 2-4 is located at the inner top of the regenerator housing 2-1. The gas outlet of the regenerator gas-solid separator 2-3 communicates with the regenerator gas collecting chamber 2-4, which in turn communicates with an exhaust gas transport pipe 2-5. The catalyst outlet end of the regenerator gas-solid separator 2-3 is located above the open end of the inlet pipe of the regenerator stripper 2-6.

[0110] A regenerator stripper 2-6 is installed below the regenerator section. The inlet of the regenerator stripper 2-6 is located inside the regenerator housing 2-1, and the outlet of the regenerator stripper 2-6 is located outside the regenerator housing 2-1 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.

[0111] A regeneration slide valve 2-7 is provided below the regenerator stripper 2-6, and the inlet of the regeneration slide valve 2-7 is connected to the outlet of the regenerator stripper 2-6.

[0112] The regeneration slide valve 2-7 is used to control the circulation rate of the regenerated catalyst.

[0113] 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.

[0114] The light hydrocarbon aromatization reactor includes a lift tube reactor inlet end 3-1, a lift tube reactor middle section 3-2, a lift tube reactor outlet end 3-3, a bed reactor housing 3-4, a bed reactor distributor 3-5, a gas-solid separation device II 3-6, a gas collection chamber II 3-7, a product gas transport pipe II 3-8, and a light hydrocarbon aromatization slide valve 3-9.

[0115] The bed reactor housing 3-4 includes an upper bed reactor housing and a lower bed reactor housing, the upper bed reactor housing forms a gas-solid separation zone, and the lower bed reactor housing forms a light hydrocarbon aromatization reaction zone. A bed reactor distributor 3-5 is installed at the bottom of the light hydrocarbon aromatization reaction zone, and a light hydrocarbon aromatization slide valve 3-9 is installed outside the light hydrocarbon aromatization reaction zone. The upper section of the lift tube reactor is inserted axially into the bed reactor through the bottom of the bed reactor, and the outlet end 3-3 of the lift tube reactor is located at the bottom of the light hydrocarbon aromatization reaction zone.

[0116] The light hydrocarbon aromatization sliding valve 3-9 is used to send the catalyst to the next reactor, such as the naphtha aromatics reactor 1. Furthermore, the outlet position of the light hydrocarbon aromatization reaction section is higher than the inlet position of the naphtha aromatics reaction section of the naphtha aromatics reactor.

[0117] The gas-solid separation section of the bed reactor is equipped with a gas-solid separator II3-6 and a gas collection chamber II3-7. The gas outlet of the gas-solid separator II3-6 is connected to the gas collection chamber II3-7, and the catalyst outlet of the gas-solid separator II3-6 is located in the light hydrocarbon aromatization reaction section. The gas collection chamber II3-7 is connected to the product gas transport pipe II3-8 outside the bed reactor.

[0118] In a preferred embodiment, the gas-solid separator II3-6 is a gas-solid cyclone separator.

[0119] In a preferred embodiment, a gas collection chamber II 3-7 is provided at the inner top of the bed reactor, and the catalyst outlet of the bed reactor gas-solid cyclone separator 3-7 is located above the outlet end 3-3 of the lift tube reactor.

[0120] In a preferred embodiment, the bed reactor distributor 3-5 is used to introduce the bed reactor feed.

[0121] In a preferred embodiment, the lift tube reactor inlet end 3-1 is used to introduce catalyst and lift tube reactor feed.

[0122] The inlet of the light hydrocarbon aromatization reactor 3 is connected to the regenerator 2 , and the outlet of the light hydrocarbon aromatization reactor 3 is connected to the naphtha aromatics reactor 1 .

[0123] In a preferred embodiment, the lift pipe reactor inlet end 3-1 is connected to the regeneration slide valve 2-7 via piping, and the light hydrocarbon aromatization slide valve 3-9 is connected to the naphtha aromatics reactor housing 1-1 via piping.

[0124] In a preferred embodiment, the product gas transport pipe II3-8 is connected to the naphtha aromatic reactor housing 1-1.

[0125] To achieve aromatization of linear and branched aliphatic hydrocarbons, improve the yield of aromatic hydrocarbons, and increase the para-xylene content in mixed xylenes, the present application provides a method for producing aromatic hydrocarbons from naphtha, which includes producing aromatic hydrocarbons using the naphtha-based aromatic fluidized bed apparatus described above.

[0126] The method further includes: introducing a feedstock and a high-temperature catalyst into a light hydrocarbon aromatization reactor to produce a light hydrocarbon aromatization product gas; and introducing naphtha, the catalyst from the light hydrocarbon aromatization reactor, and the light hydrocarbon aromatization product gas into a naphtha aromatics reactor to produce a product gas stream comprising BTX.

[0127] In a preferred embodiment, the catalyst is a metal molecular sieve bifunctional catalyst.

[0128] The metal molecular sieve 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.

[0129] In a preferred embodiment, the method comprises the following steps: a) Naphtha enters the naphtha aromatics reaction zone of naphtha aromatics reactor 1 through naphtha aromatics reactor distributor 1-2 and contacts the catalyst from light hydrocarbon aromatization reactor 3 to produce a product gas stream containing BTX, light olefins, hydrogen, light alkanes, combustible gases, heavy aromatic hydrocarbons, and unconverted naphtha. At the same time, the catalyst cokes and converts to spent catalyst. The product gas flow enters gas-solid separator I1-3, where the entrained spent catalyst is removed, then enters gas collection chamber I1-4 and passes through product gas transport pipe I1-5 to enter downstream processes. The spent catalyst from the naphtha aromatic reaction section enters reactor stripper 1-6 through the open end of its inlet pipe, undergoes stripping, and then passes through spent slide valve 1-7 and spent catalyst transport pipe 1-8 to enter regenerator 2. b) The regeneration gas is introduced into the regeneration section of the 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 simultaneously converted into regenerated catalyst. The exhaust gas enters the regenerator gas-solid separator 2-3, where the entrained regenerated catalyst is removed. After that, the exhaust gas enters the regenerator gas collection chamber 2-4 and then the exhaust gas transport pipe 2-5 for downstream processing. The regenerated catalyst passes through the regenerator stripper 2-6 and the regeneration slide valve 2-7 sequentially to enter the light hydrocarbon aromatization reactor 3. c) The lift tube reactor feedstock is introduced into the lift tube reactor through the lift tube reactor inlet end 3-1 and reacts with the regenerated catalyst from the regenerator. The lift tube reactor feedstock is converted into a stream containing components such as BTX, low-carbon olefins, and H2 under the action of the catalyst, and then passes through the lift tube reactor outlet end 3-3 into the lower part of the light hydrocarbon aromatization reaction zone of the bed reactor. The bed reactor feedstock passes through the bed reactor distributor 3-5 into the light hydrocarbon aromatization reaction zone and contacts the catalyst from the lift tube reactor to produce a light hydrocarbon aromatization product gas containing components such as BTX, low-carbon olefins, and H2. The light hydrocarbon aromatization product gas enters the gas-solid separation device II3-6, where the entrained catalyst is removed. After that, it enters the gas collection chamber II3-7 and passes through the product gas transport pipe II3-8 into the gas-solid separation zone of the naphtha aromatics reactor. The catalyst from the light hydrocarbon aromatization reaction zone passes through the light hydrocarbon aromatization slide valve 3-9 into the naphtha aromatics reactor 1.

[0130] The low carbon olefins refer to ethylene and propylene.

[0131] The low carbon alkanes refer to ethane and propane.

[0132] The combustible gases include methane and CO.

[0133] The heavy aromatic hydrocarbons refer to aromatic hydrocarbons having 9 or more carbon atoms in the molecule.

[0134] In a preferred embodiment, 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.

[0135] In a preferred embodiment, the naphtha also includes unconverted naphtha separated from the product gas stream.

[0136] In a preferred embodiment, the carbon content of the spent catalyst is 1.0-3.0 wt%.

[0137] In a preferred embodiment, the industrial conditions for the naphtha aromatics reaction zone are: gas apparent linear velocity of 0.5-2.0 m / s, reaction temperature of 500-650°C, reaction pressure of 100-500 kPa, and bed density of 150-700 kg / m 3 is.

[0138] Alternatively, the apparent linear gas velocity in the naphtha aromatic reaction zone 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.

[0139] Alternatively, the reaction temperature of the naphtha aromatic reaction section can be independently selected from 500°C, 520°C, 530°C, 540°C, 550°C, 560°C, 570°C, 580°C, 590°C, 600°C, 610°C, 620°C, 630°C, 640°C, and 650°C, or any range between any two of these values.

[0140] Alternatively, the reaction pressure in the naphtha aromatic reaction section 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.

[0141] Alternatively, the bed density of the naphtha aromatics reaction zone 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 / m3 , 700 kg / m 3 Any value from, or a range value between, any two values ​​can be independently selected.

[0142] In a preferred embodiment, the carbon content of the regenerated catalyst is 0.5 wt% or less.

[0143] In a preferred embodiment, the regeneration gas is at least one selected from the group consisting of oxygen, air, and oxygen-enriched air.

[0144] In a preferred embodiment, the industrial conditions of the regeneration zone are: apparent gas velocity of 0.5-2.0 m / s, regeneration temperature of 600-750°C, regeneration pressure of 100-500 kPa, and bed density of 150-700 kg / m 3 is.

[0145] Alternatively, the apparent linear velocity of the gas in the regeneration zone 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.

[0146] Alternatively, the regeneration temperature of the regeneration zone can be independently selected from 600°C, 615°C, 630°C, 645°C, 670°C, 685°C, 700°C, 715°C, 730°C, 745°C, and 750°C, or a range between any two of these values.

[0147] Alternatively, the regeneration pressure in the regeneration zone 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.

[0148] Optionally, the bed density of the regeneration area 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 from, or a range value between, any two values ​​can be independently selected.

[0149] In a preferred embodiment, the lift tube reactor feed comprises steam and lower carbon alkanes separated from the product gas stream.

[0150] In a preferred embodiment, the steam content of the lift tube reactor feed is 0-80 wt%.

[0151] In a preferred embodiment, the industrial conditions of the lift tube reactor are: gas apparent linear velocity 3.0-10.0 m / s, temperature 580-700°C, pressure 100-500 kPa, bed density 50-150 kg / m 3 is.

[0152] Alternatively, the gas superficial linear velocity in 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.

[0153] Alternatively, the temperature of the lift tube reactor can be independently selected from 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, or any range between any two of these values.

[0154] 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, 500 kPa, or any range between any two of these values.

[0155] Alternatively, 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 from, or a range value between, any two values ​​can be independently selected.

[0156] The bed reactor feed comprises C4 and C5 hydrocarbons.

[0157] In a preferred embodiment, the bed reactor feed comprises C3, C4 and C5 hydrocarbons.

[0158] In a preferred embodiment, the C3, C4 and C5 hydrocarbons are derived from C3, C4 and C5 hydrocarbons separated from a product gas stream.

[0159] The C3, C4 and C5 hydrocarbons refer to hydrocarbons having 3, 4 and 5 carbon atoms, respectively.

[0160] In a preferred embodiment, the industrial conditions for the light hydrocarbon aromatization reaction zone are: gas apparent linear velocity of 0.5-2.0 m / s, reaction temperature of 550-665°C, reaction pressure of 100-500 kPa, and bed density of 150-700 kg / m 3 is.

[0161] Alternatively, the gas apparent linear velocity in the light hydrocarbon aromatization reaction zone 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.

[0162] Alternatively, the reaction temperature of the light hydrocarbon aromatization reaction zone can be independently selected from 550°C, 560°C, 570°C, 580°C, 590°C, 600°C, 610°C, 620°C, 630°C, 640°C, 650°C, 660°C, and 665°C, or any range between any two of these values.

[0163] Alternatively, the reaction pressure in the light hydrocarbon aromatization reaction zone 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.

[0164] Optionally, the bed density of the light hydrocarbon aromatization reaction zone 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 from, or a range value between, any two values ​​can be independently selected.

[0165] In the embodiment described herein, the aromatic potential content of the naphtha feedstock is 0-80 wt%, and the naphtha has a single-pass conversion of 70-95 wt%. The unconverted naphtha is separated from the product gas and returned to the naphtha aromatics reactor as feedstock. A portion of the low-carbon alkanes is separated from the product gas and returned to the lift tube reactor of the light hydrocarbon aromatization reactor as feedstock. C3, C4, and C5 hydrocarbons are separated from the product gas and returned to the bed reactor of the light hydrocarbon aromatization reactor as feedstock. The final product has the following composition: 60-75 wt% BTX, 6-14 wt% low-carbon olefins, 3-7 wt% hydrogen, 3-8 wt% low-carbon alkanes, 4-6 wt% combustible gases, 4-8 wt% heavy aromatic hydrocarbons, and 0.5-1 wt% coke. The mixed xylenes in the product contain 50-65 wt% paraxylene.

[0166] Example 1 In this implementation, the device shown in Figure 1 is used.

[0167] In this embodiment, the naphtha feedstock supplied to the naphtha aromatics reactor is a direct coal liquefaction naphtha having an aromatics potential content of 78 wt %. The naphtha feedstock supplied to the naphtha aromatics reactor also includes unconverted naphtha separated from the product gas stream.

[0168] The industrial conditions of the naphtha aromatics reaction section of the naphtha aromatics reactor are as follows: gas apparent linear velocity 0.5 m / s, reaction temperature 645°C, reaction pressure 100 kPa, bed density 700 kg / m 3 .

[0169] The regeneration gas is air.

[0170] The industrial conditions of the regeneration section of the regenerator are as follows: gas apparent linear velocity 0.5 m / s, regeneration temperature 745°C, regeneration pressure 100 kPa, bed density 700 kg / m 3 .

[0171] The lift tube reactor feed is a low carbon alkane separated from the product gas stream.

[0172] The industrial conditions for the lift tube reactor are as follows: gas apparent linear velocity 3.0 m / s, temperature 690°C, pressure 100 kPa, bed density 150 kg / m 3 .

[0173] The bed reactor feed is C3, C4 and C5 hydrocarbons separated from the product gas stream.

[0174] The industrial conditions for the light hydrocarbon aromatization reaction zone are as follows: gas apparent linear velocity 0.5 m / s, reaction temperature 665°C, reaction pressure 100 kPa, bed density 700 kg / m 3 .

[0175] The carbon content of the spent catalyst is 1.2 wt%, and the carbon content of the regenerated catalyst is 0.2 wt%.

[0176] The naphtha feedstock fed to the naphtha aromatics reactor has a single-pass conversion of 70 wt%.

[0177] The product composition is as follows: 74.4 wt% BTX, 6 wt% low-carbon olefins, 3 wt% hydrogen, 4 wt% low-carbon alkanes, 5 wt% combustible gases, 7 wt% heavy aromatic hydrocarbons, and 0.6 wt% coke. The content of paraxylene in the mixed xylenes in the product is 51 wt%.

[0178] Example 2 In this implementation, the device shown in Figure 1 is used.

[0179] In this embodiment, the naphtha feedstock supplied to the naphtha aromatics reactor is an indirect coal liquefaction naphtha having an aromatics potential content of 0.1 wt%. The naphtha feedstock supplied to the naphtha aromatics reactor also includes unconverted naphtha separated from the product gas stream.

[0180] The industrial conditions of the naphtha aromatics reaction section of the naphtha aromatics reactor are as follows: gas apparent linear velocity 2.0 m / s, reaction temperature 510°C, reaction pressure 500 kPa, bed density 150 kg / m 3 .

[0181] The regeneration gas is oxygen.

[0182] The industrial conditions of the regeneration section of the regenerator are as follows: gas apparent linear velocity 2.0 m / s, regeneration temperature 610°C, regeneration pressure 500 kPa, bed density 150 kg / m 3 .

[0183] The lift tube reactor feed contains steam and low carbon alkanes separated from the product gas stream, of which the steam content is 80 wt%.

[0184] The industrial conditions for the lift tube reactor are as follows: gas apparent linear velocity 10.0 m / s, temperature 580°C, pressure 500 kPa, bed density 50 kg / m 3 .

[0185] The bed reactor feed is C3, C4 and C5 hydrocarbons separated from the product gas stream.

[0186] The industrial conditions for the light hydrocarbon aromatization reaction zone are as follows: gas apparent linear velocity 2.0 m / s, reaction temperature 550°C, reaction pressure 500 kPa, bed density 150 kg / m 3 .

[0187] The carbon content of the spent catalyst is 2.9 wt%, and the carbon content of the regenerated catalyst is 0.1 wt%.

[0188] The naphtha feedstock fed to the naphtha aromatics reactor has a single-pass conversion of 76 wt%.

[0189] The product composition is as follows: 66 wt% BTX, 11.3 wt% low-carbon olefins, 6 wt% hydrogen, 3 wt% low-carbon alkanes, 5 wt% combustible gases, 8 wt% heavy aromatic hydrocarbons, and 0.7 wt% coke. The content of paraxylene in the mixed xylenes in the product is 62 wt%.

[0190] Example 3 In this implementation, the device shown in Figure 1 is used.

[0191] In this embodiment, the naphtha feedstock supplied to the naphtha aromatics reactor is an indirect coal liquefaction naphtha having an aromatics potential content of 3 wt %. The naphtha feedstock supplied to the naphtha aromatics reactor also includes unconverted naphtha separated from the product gas stream.

[0192] The industrial conditions of the naphtha aromatics reaction section of the naphtha aromatics reactor are as follows: gas apparent linear velocity 1.2 m / s, reaction temperature 550 °C, reaction pressure 120 kPa, bed density 260 kg / m 3 .

[0193] The regeneration gas is oxygen-enriched air.

[0194] The industrial conditions of the regeneration section of the regenerator are as follows: gas apparent linear velocity 1.2 m / s, regeneration temperature 650°C, regeneration pressure 120 kPa, bed density 260 kg / m 3 .

[0195] The lift tube reactor feed contains steam and low carbon alkanes separated from the product gas stream, of which the steam content is 25 wt%.

[0196] The industrial conditions for the lift tube reactor are as follows: apparent gas velocity 7.0 m / s, temperature 630°C, pressure 120 kPa, bed density 80 kg / m 3 .

[0197] The bed reactor feed is the C4 and C5 hydrocarbons separated from the product gas stream.

[0198] The industrial conditions for the light hydrocarbon aromatization reaction zone are as follows: gas apparent linear velocity 1.2 m / s, reaction temperature 580 °C, reaction pressure 120 kPa, bed density 260 kg / m 3 .

[0199] The carbon content of the spent catalyst is 2.0 wt%, and the carbon content of the regenerated catalyst is 0.3 wt%.

[0200] The naphtha feedstock fed to the naphtha aromatics reactor has a single-pass conversion of 94 wt%.

[0201] The product composition is as follows: 60wt% BTX, 14wt% low-carbon olefins, 7wt% hydrogen, 8wt% low-carbon alkanes, 4.5wt% combustible gases, 6wt% heavy aromatic hydrocarbons, and 0.5wt% coke. The content of paraxylene in the mixed xylenes in the product is 65wt%.

[0202] Example 4 In this implementation, the device shown in Figure 1 is used.

[0203] In this embodiment, the naphtha feedstock supplied to the naphtha aromatics reactor is a straight-run naphtha having an aromatics potential content of 46 wt %. The naphtha feedstock supplied to the naphtha aromatics reactor also includes unconverted naphtha separated from the product gas stream.

[0204] The industrial conditions of the naphtha aromatics reaction section of the naphtha aromatics reactor are as follows: gas apparent linear velocity 1.8 m / s, reaction temperature 600 °C, reaction pressure 200 kPa, bed density 220 kg / m 3 .

[0205] The regeneration gas is air.

[0206] The industrial conditions of the regeneration section of the regenerator are as follows: gas apparent linear velocity 1.8 m / s, regeneration temperature 700 °C, regeneration pressure 200 kPa, bed density 220 kg / m 3 .

[0207] The lift tube reactor feed contains steam and low carbon alkanes separated from the product gas stream, of which the steam content is 50 wt%.

[0208] The industrial conditions for the lift tube reactor are as follows: apparent gas velocity 5.0 m / s, temperature 660°C, pressure 200 kPa, bed density 110 kg / m 3 .

[0209] The bed reactor feed is the C4 and C5 hydrocarbons separated from the product gas stream.

[0210] The industrial conditions for the light hydrocarbon aromatization reaction zone are as follows: gas apparent linear velocity 1.8 m / s, reaction temperature 630 °C, reaction pressure 200 kPa, bed density 220 kg / m 3 .

[0211] The carbon content of the spent catalyst is 1.7 wt%, and the carbon content of the regenerated catalyst is 0.1 wt%.

[0212] The naphtha feedstock fed to the naphtha aromatics reactor has a single-pass conversion of 87 wt%.

[0213] The product composition is as follows: 70wt% BTX, 10wt% low-carbon olefins, 6wt% hydrogen, 5wt% low-carbon alkanes, 4wt% combustible gases, 4wt% heavy aromatic hydrocarbons, and 1.0wt% coke. The content of paraxylene in the mixed xylenes in the product is 63wt%.

[0214] Example 5 In this implementation, the device shown in Figure 1 is used.

[0215] In this embodiment, the naphtha feedstock supplied to the naphtha aromatics reactor is a hydrocracked naphtha having an aromatics potential content of 64 wt %. The naphtha feedstock supplied to the naphtha aromatics reactor also includes unconverted naphtha separated from the product gas stream.

[0216] The industrial conditions of the naphtha aromatics reaction section of the naphtha aromatics reactor are as follows: gas apparent linear velocity 1.0 m / s, reaction temperature 580°C, reaction pressure 150 kPa, bed density 350 kg / m 3 .

[0217] The regeneration gas is air.

[0218] The industrial conditions of the regeneration section of the regenerator are as follows: gas apparent linear velocity 1.0 m / s, regeneration temperature 680°C, regeneration pressure 150 kPa, bed density 350 kg / m 3 .

[0219] The lift tube reactor feed contains steam and low carbon alkanes separated from the product gas stream, of which the steam content is 40 wt%.

[0220] The industrial conditions for the lift tube reactor are as follows: apparent gas velocity 7.0 m / s, temperature 650°C, pressure 150 kPa, bed density 80 kg / m 3 .

[0221] The bed reactor feed is the C4 and C5 hydrocarbons separated from the product gas stream.

[0222] The industrial conditions for the light hydrocarbon aromatization reaction zone are as follows: gas apparent linear velocity 1.0 m / s, reaction temperature 610°C, reaction pressure 150 kPa, bed density 350 kg / m 3 .

[0223] The carbon content of the spent catalyst is 1.5 wt%, and the carbon content of the regenerated catalyst is 0.5 wt%.

[0224] The naphtha feedstock fed to the naphtha aromatics reactor has a single-pass conversion of 77 wt%.

[0225] The product composition is as follows: 71 wt% BTX, 8 wt% low-carbon olefins, 5 wt% hydrogen, 3 wt% low-carbon alkanes, 6 wt% combustible gases, 6 wt% heavy aromatic hydrocarbons, and 1.0 wt% coke. The content of paraxylene in the mixed xylenes in the product is 57 wt%.

[0226] 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]

[0227] 1: Naphtha aromatics reactor 1-1: Naphtha aromatic reactor housing 1-2: Naphtha aromatic reactor distributor 1-3: Gas-solid separator I 1-4: Gas Collection Chamber I 1-5: Produced gas transport pipe I 1-6: Reactor stripper 1-7: Used sliding valve 1-8: Used agent transport pipe 2:Regenerator 2-1: Regenerator housing 2-2: Regenerator distributor 2-3: Regenerator gas-solid separation device 2-4: Regenerator gas collection chamber 2-5: Exhaust gas transport pipe 2-6: Regenerator stripper 2-7: Regenerative sliding valve 3: Light hydrocarbon aromatization reactor 3-1: Lift tube reactor inlet end 3-2: Middle part of lift tube reactor 3-3: Lift tube reactor outlet end 3-4: Bed reactor housing 3-5: Bed reactor distributor 3-6: Gas-solid separator II 3-7: Gas Collection Chamber II 3-8: Produced gas transport pipe II 3-9: Light hydrocarbon aromatization sliding valve

Claims

1. A naphtha aromatics fluidized bed apparatus comprising a light hydrocarbon aromatization reactor and a naphtha aromatics reactor, the light hydrocarbon aromatization reactor has at least one inlet for passing a feedstock and a hot catalyst therethrough; At least one outlet of the light hydrocarbon aromatization reactor is connected to the naphtha aromatics reactor and is used to transport the catalyst and the produced light hydrocarbon aromatization product gas to the naphtha aromatics reactor; The naphtha aromatics reactor is used to pass naphtha through and react with the catalyst from the light hydrocarbon aromatization reactor to produce a product gas stream comprising BTX.

2. 2. The naphtha-based aromatics fluidized bed apparatus according to claim 1, wherein the naphtha-based aromatics reactor is further provided with a product gas transport pipe I, which is used to output the product gas stream containing the BTX to a downstream process.

3. 2. The naphtha aromatics fluidized bed apparatus according to claim 1, further comprising a regenerator, wherein at least one inlet of the light hydrocarbon aromatization reactor is connected to the regenerator and is used to obtain the high-temperature regenerated catalyst produced in the regenerator.

4. The light hydrocarbon aromatization reactor is divided into a gas-solid separation section II and a light hydrocarbon aromatization reaction section, which are at least connected from top to bottom, and constitutes a bed reactor; The gas-solid separation section II is provided with a gas-solid separator II and a gas collection chamber II, and the gas outlet of the gas-solid separator II is connected to the gas collection chamber II; The naphtha aromatics fluidized bed apparatus according to claim 1, characterized in that a bed reactor distributor is provided in the lower part of the light hydrocarbon aromatization reaction zone, and is used to pass the bed reactor raw material.

5. 5. The naphtha aromatic fluidized bed apparatus according to claim 4, wherein the gas collection chamber II is installed at the inner top of the bed reactor.

6. The bed reactor feed is C 4 and C 5 5. The naphtha aromatic fluidized bed apparatus of claim 4, wherein the apparatus contains hydrocarbons.

7. The light hydrocarbon aromatization reactor further comprises a lift tube reactor in addition to the bed reactor; the inlet end of the lift tube reactor communicates with the regenerator; 5. The naphtha aromatics fluidized bed apparatus according to claim 4, wherein the outlet end of the lift tube reactor extends to the lower part of the light hydrocarbon aromatization reaction zone, and the upper part thereof is the catalyst outlet of the gas-solid separation device II.

8. 8. The naphtha aromatic fluidized bed apparatus according to claim 7, wherein the inlet end of the lift tube reactor is further used for passing catalyst and lift tube reactor feed.

9. The naphtha aromatics reactor is divided into a gas-solid separation section I and a naphtha aromatics reaction section which are at least connected from top to bottom, The gas-solid separation section I is provided with a gas-solid separation device I and a gas collection chamber I; The gas outlet of the gas-solid separator I is in communication with the gas collection chamber I; 2. The naphtha aromatics fluidized bed apparatus according to claim 1, wherein a naphtha aromatics reactor distributor is provided in the lower part of the naphtha aromatics reaction zone, and is used to pass the naphtha raw material.

10. The naphtha aromatics fluidized bed apparatus according to claim 9, characterized in that the gas-solid separation device I uses at least one set of gas-solid cyclone separators, and each set of gas-solid cyclone separators includes a first-class gas-solid cyclone separator and a second-class gas-solid cyclone separator.

11. 10. The naphtha aromatic fluidized bed apparatus according to claim 9, wherein the gas collection chamber I is located at the top of the naphtha aromatic reactor.

12. 10. The naphtha aromatic fluidized bed apparatus according to claim 9, wherein the gas collection chamber I is in communication with the product gas transport pipe I.

13. 10. The naphtha aromatics fluidized bed apparatus according to claim 9, wherein the gas-solid separation section I is connected to the gas-solid separation section II, and the naphtha aromatics reaction section of the naphtha aromatics reactor is connected to the light hydrocarbon aromatization reaction section.

14. 14. The naphtha aromatics fluidized bed apparatus according to claim 13, wherein the gas-solid separation section I is connected to the gas collection chamber II through a product gas transport pipe II.

15. 14. The naphtha aromatics fluidized bed apparatus according to claim 13, wherein a light hydrocarbon aromatization slide valve is installed in a pipeline connected between the naphtha aromatics reaction section and the light hydrocarbon aromatization reaction section of the naphtha aromatics reactor.

16. 14. The naphtha aromatics fluidized bed apparatus according to claim 13, wherein the outlet position of the light hydrocarbon aromatization reaction section is higher than the inlet position of the naphtha aromatics reaction section of the naphtha aromatics reactor.

17. The regenerator is divided into a gas-solid separation section III and a catalyst regeneration section, which are at least connected from top to bottom, The gas-solid separation section III is provided with a regenerator gas-solid separation device and a regenerator gas collection chamber; a gas outlet of the regenerator gas-solid separation device communicating with the regenerator gas collection chamber; The regenerator gas collecting chamber is provided with an exhaust gas transport pipe, 4. The naphtha aromatic fluidized bed apparatus according to claim 3, wherein a regenerator distributor is provided in the lower part of the catalyst regeneration zone, and is used to pass regeneration gas.

18. The catalyst regeneration section is connected to the light hydrocarbon aromatization reactor through a regenerator stripper and a regeneration slide valve; an inlet pipe of the regenerator stripper extending into the regenerator housing and positioned above the regenerator distributor; 18. The naphtha aromatics fluidized bed apparatus according to claim 17, wherein the catalyst outlet end of the regenerator gas-solid separation device is located above the open end of the inlet pipe of the regenerator stripper.

19. 18. The naphtha aromatic fluidized bed apparatus according to claim 17, wherein the regenerator gas collection chamber is located at the top of the regenerator housing.

20. At least one outlet of the naphtha aromatics reactor is further connected to the inlet of the regenerator, and is used to pass the spent catalyst produced by the reaction in the naphtha aromatics reactor through the regenerator; 4. The naphtha aromatic fluidized bed apparatus according to claim 3, wherein the regenerator is used to pass a regeneration gas through it to convert the spent catalyst into a regenerated catalyst.

21. The naphtha aromatics reaction section of the naphtha aromatics reactor is connected to the inlet of the regenerator through a reactor stripper, a spent slide valve, and a spent reagent transport pipe; the reactor stripper inlet pipe extends into the naphtha aromatics reactor housing and is located above the naphtha aromatics reactor distributor; 21. The naphtha aromatics fluidized bed apparatus according to claim 20, wherein the catalyst outlet end of the gas-solid separation device I is located above the open end of the inlet pipe of the reactor stripper.

22. 22. The naphtha aromatic fluidized bed apparatus according to claim 21, wherein the catalyst inlet of the regenerator is located on the regenerator housing.

23. A method for producing aromatics from naphtha, characterized in that aromatics are produced using the naphtha-based aromatics fluidized bed apparatus according to any one of claims 1 to 22.

24. passing the feedstock and the hot catalyst through a light hydrocarbon aromatization reactor to produce a light hydrocarbon aromatization product gas; 24. The method for producing aromatics from naphtha according to claim 23, further comprising passing the naphtha and the catalyst from the light hydrocarbon aromatization reactor and the light hydrocarbon aromatization product gas through a naphtha aromatics reactor to produce a product gas stream comprising BTX.

25. 25. The method for producing aromatics from naphtha according to claim 23 or 24, wherein the catalyst is a metal zeolite bifunctional catalyst.

26. 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, 26. The method for producing aromatics from naphtha according to claim 25, wherein the metal modification method comprises immersing an HZSM-5 zeolite molecular sieve in a metal salt solution, drying, and roasting the HZSM-5 zeolite molecular sieve to obtain the metal-modified HZSM-5 zeolite molecular sieve.

27. The components of the light hydrocarbon aromatization product gas are BTX, low carbon olefins, and H 2 25. The method for producing aromatics from naphtha according to claim 24, comprising:

28. 25. The method for producing aromatics from naphtha according to claim 24, wherein the BTX-containing product gas stream contains, in addition to BTX, light olefins, hydrogen, light paraffins, combustible gases, heavy aromatics, and unreacted naphtha.

29. 29. The method for producing aromatics from naphtha according to claim 27 or 28, wherein the low-carbon olefins refer to ethylene and propylene.

30. The low carbon paraffins refer to ethane and propane; the flammable gas comprises methane and CO; 29. The method for producing aromatics from naphtha according to claim 28, wherein the heavy aromatics refer to aromatics having 9 or more carbon atoms in the molecule.

31. Specifically, the step of passing a raw material and a high-temperature catalyst through the light hydrocarbon aromatization reactor to generate a light hydrocarbon aromatization product gas includes:

25. The method for producing aromatics from naphtha according to claim 24, comprising passing the bed reactor feedstock through a bed reactor distributor to a light hydrocarbon aromatization reaction zone, where it is contacted with the catalyst passed through the bed reactor, to produce a light hydrocarbon aromatization product gas.

32. The bed reactor feed is C 4 and C 5 32. The method for producing aromatics from naphtha according to claim 31, wherein the naphtha contains hydrocarbons.

33. The bed reactor feed is C 3 , C 4 , and C 5 33. The method for producing aromatics from naphtha according to claim 32, wherein the naphtha contains hydrocarbons.

34. Said C 4 and C 5 Hydrocarbons are separated from the product gas stream. 4 and C 5 33. The method for producing aromatics from naphtha according to claim 32, wherein the aromatics are derived from hydrocarbons.

35. Said C 3 , C 4 , and C 5 Hydrocarbons are separated from the product gas stream. 3 , C 4 , and C 5 34. The method for producing aromatics from naphtha according to claim 33, characterized in that the aromatics are derived from hydrocarbons.

36. The process conditions for the light hydrocarbon aromatization reaction zone are: gas superficial linear velocity 0.5-2.0 m / s, reaction temperature 550-665°C, reaction pressure 100-500 kPa, bed density 150-700 kg / m 3 32. The method for producing aromatics from naphtha according to claim 31, wherein

37. 32. The method for producing aromatics from naphtha according to claim 31, further comprising removing a catalyst entrained in the light hydrocarbon aromatization product gas in gas-solid separation section II of the light hydrocarbon aromatization reactor.

38. 32. The method for producing aromatics from naphtha according to claim 31, wherein the catalyst in the light hydrocarbon aromatization reaction zone enters the naphtha aromatics reactor through a light hydrocarbon aromatization slide valve.

39. The step of removing the catalyst mixed in the light hydrocarbon aromatization product gas in the gas-solid separation section II specifically includes the following steps:

38. The method for producing aromatics from naphtha according to claim 37, wherein the light hydrocarbon aromatization product gas is introduced into a gas-solid separation device II, and after removing the mixed catalyst, the gas enters into a gas collection chamber II, and then enters into the gas-solid separation section I of the naphtha aromatics reactor through a product gas transport pipe II.

40. 25. The method for producing aromatics from naphtha according to claim 24, wherein the naphtha enters the naphtha aromatics reaction zone of the naphtha aromatics reactor through a naphtha aromatics reactor distributor and contacts the catalyst from the light hydrocarbon aromatization reactor to produce a product gas stream comprising BTX, and the catalyst is coked and converted into spent catalyst.

41. 41. The method for producing aromatics from naphtha according to claim 40, further comprising removing spent catalyst from the BTX-containing product gas stream in gas-solid separation section I of the naphtha aromatics reactor and transporting it to downstream processing.

42. 25. The method for producing aromatics from naphtha according to claim 24, 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.

43. 43. The method for producing aromatics from naphtha of claim 42, wherein the naphtha further comprises unreacted naphtha separated from the product gas stream, the unreacted naphtha comprising primarily C4-C12 linear and branched aliphatics and naphthenes.

44. The process conditions for the naphtha aromatics reaction section are: gas superficial linear velocity 0.5-2.0 m / s, reaction temperature 500-650°C, reaction pressure 100-500 kPa, bed density 150-700 kg / m 3 41. The method for producing aromatics from naphtha according to claim 40, wherein

45. 25. The method for producing aromatics from naphtha according to claim 24, further comprising passing the regeneration gas and the spent catalyst through a regenerator to obtain a hot regenerated catalyst, which is then transported to the light hydrocarbon aromatization reactor.

46. 46. ​​The method for producing aromatics from naphtha according to claim 45, wherein the regeneration gas is passed through a regenerator distributor to the regeneration section of the regenerator.

47. 46. ​​The method for producing aromatics from naphtha according to claim 45, wherein the regeneration gas is at least one selected from oxygen, air, and oxygen-enriched air.

48. 46. ​​The method for producing aromatics from naphtha according to claim 45, wherein the carbon content in the spent catalyst is 1.0-3.0 wt%.

49. 46. ​​The method for producing aromatics from naphtha according to claim 45, wherein the carbon content in the regenerated catalyst is 0.5 wt% or less.

50. The process conditions of the regeneration section of the 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 46. ​​The method for producing aromatics from naphtha according to claim 45, wherein

51. 46. ​​The method for producing aromatics from naphtha according to claim 45, wherein the coke on the spent catalyst reacts with the regeneration gas to produce exhaust gas, and the exhaust gas enters gas-solid separation section III to remove the regenerated catalyst mixed therein.

52. 52. The method for producing aromatics from naphtha according to claim 51, wherein the process of the exhaust gas entering the gas-solid separation section III and removing the regenerated catalyst mixed therein specifically includes: the exhaust gas first entering a regenerator gas-solid separation device, removing the regenerated catalyst mixed therein, and then passing through a regenerator gas collection chamber and an exhaust gas transport pipe into a downstream process.

53. 52. The method for producing aromatics from naphtha according to claim 51, wherein the regenerated catalyst enters the light hydrocarbon aromatization reactor through a regenerator stripper and a regeneration slide valve.

54. 25. The method for producing aromatics from naphtha according to claim 24, further comprising: passing a lift tube reactor feedstock through the inlet end of the lift tube reactor of the light hydrocarbon aromatization reactor; passing the regenerated catalyst through a regenerator stripper and a regenerated slide valve into the lift tube reactor; converting the lift tube reactor feedstock into a stream containing BTX under the action of the regenerated catalyst; and passing the stream through the outlet end of the lift tube reactor into a lower part of the light hydrocarbon aromatization reaction zone in the bed reactor.

55. 55. The method for producing aromatics from naphtha according to claim 54, wherein the method further comprises passing a catalyst through an inlet end of a lift tube reactor of a light hydrocarbon aromatization reactor, passing through the lift tube reactor, and into the bed reactor.

56. 56. The method for producing aromatics from naphtha of claim 55, wherein the lift tube reactor feed comprises steam and low carbon paraffins separated from the product gas stream.

57. 56. The method for producing aromatics from naphtha according to claim 55, wherein the steam content in the lift tube reactor feed is 0-80 wt%.

58. 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 56. The method for producing aromatics from naphtha according to claim 55, wherein

59. The components of the BTX-containing stream are BTX, low-carbon olefins, and H 2 55. The method for producing aromatics from naphtha according to claim 54, comprising:

60. The method further comprises:

25. The method for producing aromatics from naphtha according to claim 24, comprising passing spent catalyst in the naphtha aromatics reaction section of the naphtha aromatics reactor through a reactor stripper, stripping the spent catalyst, and then entering a downstream region through a spent slide valve and a spent agent transport pipe.

61. 61. The method for producing aromatics from naphtha according to claim 60, wherein the downstream region is a regenerator.

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