Naphtha and methanol coupled aromatics plant and process

Abstract

The application discloses a naphtha and methanol coupling device for producing aromatic hydrocarbons and a method. By using the device, naphtha and methanol are reacted to generate product gas with aromatic hydrocarbons and low-carbon olefins as main components under the action of a catalyst. The method can efficiently and highly selectively convert linear and branched aliphatic hydrocarbons into aromatic hydrocarbons, realizes yield increase of p-xylene through methylation of the aromatic hydrocarbons, and the content of p-xylene in a xylene mixture is greater than 75 wt%. The naphtha and methanol coupling device for producing aromatic hydrocarbons realizes yield increase of p-xylene through control of the progress of cascade reactions (naphtha→benzene, toluene→p-xylene), and in addition, provides heat for the naphtha and methanol coupling device for producing aromatic hydrocarbons in situ through methylation of benzene, toluene and methanol, so that self-heating balance is achieved.

Description

Technical Field

[0001] This application relates to a fluidized bed apparatus and a method for using it, belonging to the field of chemical technology, and particularly to an apparatus and method for producing aromatics by coupling naphtha and methanol. Background Technology

[0002] Aromatic hydrocarbons (benzene, toluene, and xylene, collectively known as BTX) are important organic chemical raw materials. Among them, paraxylene (PX) is the most noteworthy product, mainly used in the production of polyesters such as terephthalic acid (PTA), polyethylene terephthalate (PET), polybutylene terephthalate (PBT), and PTT (polypropylene terephthalate). In recent years, China's production and consumption of paraxylene have continued to grow. In 2021, China's total PX imports were approximately 13.65 million tons, with an import dependency rate of about 38%.

[0003] Naphtha catalytic reforming is a major technical route for producing aromatics. Naphtha has a very complex composition; it is not only the main feedstock for catalytic reforming but also for ethylene production via cracking. Its composition plays a crucial role in the economic efficiency of the plant. Generally, a high aromatic content and a suitable distillation range are favorable for catalytic reforming, while a high content of straight-chain and branched aliphatic hydrocarbons and a low content of cycloalkanes and aromatics are suitable for ethylene production via cracking. Typically, to fully utilize naphtha resources and improve economic efficiency, it is necessary to first separate the straight-chain and branched aliphatic hydrocarbons from the cycloalkanes and aromatics in the naphtha. The former is used as feedstock for ethylene production, while the latter is used as feedstock for the catalytic reforming unit.

[0004] Naphtha fractions have a wide distillation range, making it difficult to efficiently separate straight-chain and branched aliphatic hydrocarbons from cycloalkanes and aromatics using conventional methods. Furthermore, catalytic reforming technology struggles to convert straight-chain and branched aliphatic hydrocarbons into aromatics. Naphtha feedstocks used for catalytic reforming typically require distillation to remove topping oil with a boiling point below 60°C to increase the aromatic potential content. However, fractions with boiling points above 60°C still contain significant amounts of straight-chain and branched aliphatic hydrocarbons that are difficult to convert into aromatics. Therefore, the highly selective conversion of straight-chain and branched aliphatic hydrocarbons into aromatics has always been a hot topic and a challenge in the development of naphtha-to-aromatics technology.

[0005] Due to thermodynamic equilibrium limitations, para-xylene accounts for only about 24% of the xylene mixture produced by naphtha catalytic reforming units. Further production of para-xylene is required through isomerization-separation processes. Therefore, increasing the para-xylene content in the xylene mixture is an important way to reduce the energy consumption of para-xylene production. Summary of the Invention

[0006] Naphtha molecules contain only a small amount of methyl groups (methyl / benzene ring = ~1.3 (molar ratio)), and their molecular structure determines that catalytic reforming / aromatics combined units will inevitably produce a large amount of benzene as a byproduct.

[0007] Methanol aromatization is an emerging process for producing aromatics. However, compared to aromatics, methanol molecules have an excess of hydrogen atoms. Therefore, the production of aromatics from methanol inevitably produces large amounts of alkanes and hydrogen as byproducts. Based on molecular structure and reaction mechanism, methanol can provide methyl groups for aromatics, thereby increasing the production of toluene and xylene. This provides a new technical route for the coupled production of aromatics from naphtha and methanol.

[0008] According to one aspect of this application, an apparatus is provided for preparing aromatics from naphtha and methanol, which increases the content of p-xylene in mixed xylenes and reduces separation energy consumption.

[0009] The naphtha components described in this application include C4-C 12 Straight-chain, branched aliphatic hydrocarbons, cycloalkanes, and aromatic hydrocarbons.

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

[0011] The naphtha and methanol coupled aromatics production unit includes a light hydrocarbon aromatization reactor and a naphtha and methanol coupled aromatics production reactor; wherein...

[0012] The light hydrocarbon aromatization reactor is used to introduce raw materials and a high-temperature catalyst; at least one outlet of the light hydrocarbon aromatization reactor is connected to the naphtha and methanol coupled aromatics reactor for conveying the catalyst and the generated light hydrocarbon aromatization product gas to the naphtha and methanol coupled aromatics reactor.

[0013] The naphtha and methanol coupled aromatics reactor is used to introduce naphtha and methanol, and to contact the naphtha with a catalyst from the light hydrocarbon aromatization reactor to generate a product gas stream containing BTX; the methanol is then subjected to a methylation reaction with benzene and toluene in the product gas stream to generate p-xylene.

[0014] When the catalyst enters the naphtha and methanol coupled aromatics production reactor, its temperature decreases. At this point, it comes into contact with the naphtha, which can eliminate the local high-temperature zone in the naphtha and methanol coupled aromatics production reactor, thereby effectively reducing the yield of low-carbon alkanes and increasing the yield of aromatics.

[0015] Preferably, the naphtha and methanol coupled aromatics production reactor is divided into at least a first gas-solid separation zone and a naphtha and methanol coupled aromatics production reaction zone from top to bottom; the naphtha and methanol coupled aromatics production reaction zone is provided with a naphtha and methanol coupled aromatics production reactor distributor, which includes n sub-distributors, the sub-distributors being numbered from 1 to n from bottom to top, n≥2, wherein the first sub-distributor is used to introduce naphtha feedstock, and the second to nth sub-distributors are used to introduce methanol feedstock.

[0016] Preferably, n≤10.

[0017] Preferably, the first gas-solid separation zone is provided with a gas-solid separation device I and a gas collection chamber I; the gas outlet of the gas-solid separation device I is connected to the gas collection chamber I; the outlet of the gas collection chamber I is connected to a product gas conveying pipe I, and the product gas conveying pipe I is used to output the product gas containing BTX after gas-solid separation to the downstream section.

[0018] Preferably, the gas collecting chamber I is located at the inner top of the shell of the naphtha and methanol coupled aromatics production reactor.

[0019] Preferably, the gas-solid separation device I employs one or more sets of gas-solid cyclone separators, each set of gas-solid cyclone separators including a first-stage gas-solid cyclone separator and a second-stage gas-solid cyclone separator.

[0020] Preferably, the light hydrocarbon aromatization reactor is divided into at least two interconnected zones: a second gas-solid separation zone and a light hydrocarbon aromatization reaction zone, forming a bed reactor. The second gas-solid separation zone is equipped with a gas-solid separation device II and a gas collection chamber II. The gas outlet of the gas-solid separation device II is connected to the gas collection chamber II. The lower part of the light hydrocarbon aromatization reaction zone is equipped with a bed reactor distributor for introducing raw materials into the bed reactor.

[0021] Preferably, the gas collection chamber II is located at the inner top of the bed reactor.

[0022] Furthermore, the feedstock of the bed reactor includes C4 and C5 hydrocarbons, which refer to hydrocarbons with 4 and 5 carbon atoms, respectively.

[0023] Preferably, the feedstock of the bed reactor includes C3, C4 and C5 hydrocarbons, wherein the C3, C4 and C5 hydrocarbons refer to hydrocarbons with 3, 4 and 5 carbon atoms.

[0024] Preferably, in addition to the bed reactor, the light hydrocarbon aromatization reactor also includes a riser reactor, the outlet of which extends into the lower part of the light hydrocarbon aromatization reaction zone, and the catalyst outlet of the gas-solid separation device II is located above it.

[0025] Preferably, the inlet end of the riser reactor is also used to introduce catalyst and feedstock into the riser reactor.

[0026] Preferably, the second gas-solid separation zone is connected to the first gas-solid separation zone, and the light hydrocarbon aromatization reaction zone is connected to the naphtha and methanol coupled aromatics production reaction zone.

[0027] Preferably, the gas collecting chamber II is connected to the first gas-solid separation zone via the product gas delivery pipe II.

[0028] Preferably, a light hydrocarbon aromatization slide valve is provided on the pipeline connecting the naphtha and methanol coupled aromatics production reaction zone and the light hydrocarbon aromatization reaction zone.

[0029] Preferably, the outlet position of the light hydrocarbon aromatization reaction zone is higher than the inlet position of the naphtha and methanol coupled aromatics production reaction zone.

[0030] Preferably, the catalyst inlet of the naphtha and methanol coupled aromatics production reaction zone is located between the first sub-distributor and the second sub-distributor.

[0031] Preferably, the gas-solid separation device II is a gas-solid cyclone separator.

[0032] Preferably, the apparatus further includes a regenerator, at least one inlet of the light hydrocarbon aromatization reactor being connected to the regenerator for obtaining a high-temperature regenerated catalyst generated by the regenerator.

[0033] Preferably, the inlet end of the riser reactor of the light hydrocarbon aromatization reactor is connected to the regenerator.

[0034] Preferably, the regenerator is divided into at least a third gas-solid separation zone and a regeneration zone from top to bottom; the third gas-solid separation zone is provided with a regenerator gas-solid separation device and a regenerator gas collection chamber; the gas outlet of the regenerator gas-solid separation device is connected to the regenerator gas collection chamber; a flue gas conveying pipe is provided on the regenerator gas collection chamber; a regenerator distributor is provided in the lower part of the regeneration zone for introducing regeneration gas.

[0035] Preferably, the regeneration zone is connected to the riser reactor in sequence via a regenerator stripper and a regeneration slide valve; the inlet pipe of the regenerator stripper extends into the shell of the regenerator and is located above the regenerator distributor; the catalyst outlet end of the regenerator gas-solid separation device is located above the opening end of the inlet pipe of the regenerator stripper.

[0036] Preferably, the regenerator gas collection chamber is located at the inner top of the regenerator housing.

[0037] Preferably, the regenerator gas-solid separation device employs one or more sets of gas-solid cyclone separators, each set of gas-solid cyclone separators including a first-stage gas-solid cyclone separator and a second-stage gas-solid cyclone separator.

[0038] Preferably, at least one outlet of the naphtha and methanol coupled aromatics production reactor is also connected to the inlet of a regenerator, for introducing the spent catalyst produced by the reaction in the naphtha and methanol coupled aromatics production reactor into the regenerator, and the regenerator is used to introduce regeneration gas to convert the spent catalyst into a regenerated catalyst.

[0039] Preferably, the naphtha and methanol coupled aromatics production reaction zone is connected to the inlet of the regenerator via a reactor stripper, a pre-generation slide valve, and a pre-generation agent delivery pipe in sequence; the inlet pipe of the reactor stripper extends into the shell of the naphtha and methanol coupled aromatics production reactor and is located above the first sub-distributor; the catalyst outlet end of the reactor gas-solid separation device is located above the opening end of the inlet pipe of the reactor stripper.

[0040] Preferably, the inlet of the regenerator is located in the regeneration zone and is disposed on the housing of the regenerator.

[0041] According to another aspect of this application, a method for producing aromatics by coupling naphtha and methanol is provided, the method comprising: preparing aromatics using the above-described naphtha and methanol coupled aromatics production apparatus and catalyst.

[0042] Preferably, the catalyst is a bifunctional metal molecular sieve catalyst;

[0043] Preferably, the metal molecular sieve bifunctional catalyst is a metal-modified HZSM-5 zeolite molecular sieve;

[0044] The metal used for metal modification is selected from at least one of La, Zn, Ga, Fe, Mo, and Cr;

[0045] The method of metal modification includes: placing HZSM-5 zeolite molecular sieve in a metal salt solution, impregnating, drying, and calcining to obtain the metal-modified HZSM-5 zeolite molecular sieve.

[0046] Furthermore, the method includes:

[0047] A light hydrocarbon aromatization reactor is fed with raw materials and a high-temperature catalyst to generate light hydrocarbon aromatization product gas.

[0048] A naphtha and methanol coupled aromatics production reactor is fed with naphtha and a catalyst from the light hydrocarbon aromatization reactor to generate a product gas stream containing BTX.

[0049] A naphtha and methanol coupled aromatics production reactor is introduced with methanol, which undergoes a methylation reaction with benzene and toluene in the product gas stream containing BTX to produce p-xylene.

[0050] Preferably, all gaseous streams generated in the naphtha and methanol coupled aromatics reactor are desorbed by gas-solid separation equipment I to remove the entrained catalyst, enter gas collection chamber I, and then enter the downstream section through product gas conveying pipe I.

[0051] Preferably, the components of the light hydrocarbon aromatization product gas include: BTX, low-carbon olefins and H2.

[0052] Preferably, the product gas stream containing BTX includes, in addition to BTX,: low-carbon olefins, hydrogen, low-carbon alkanes, combustible gases, heavy aromatics, and unconverted naphtha.

[0053] Preferably, the low-carbon olefins refer to ethylene and propylene;

[0054] The low-carbon alkanes refer to ethane and propane;

[0055] The combustible gas includes methane and CO;

[0056] The heavy aromatic hydrocarbons refer to aromatic hydrocarbons with 9 or more carbon atoms in their molecules.

[0057] Preferably, the naphtha is selected from at least one of direct coal liquefaction naphtha, indirect coal liquefaction naphtha, straight-run naphtha, and hydrocracked naphtha.

[0058] Preferably, the naphtha further comprises unconverted naphtha separated from the product gas stream, the main components of which are C4-C. 12 Straight-chain, branched aliphatic hydrocarbons and cycloalkanes.

[0059] Preferably, the carbon content in the catalyst is 1.0-3.0 wt%.

[0060] Preferably, the process conditions for the naphtha and methanol coupled aromatics production reaction zone are as follows: apparent gas linear velocity of 0.5-2.0 m / s, reaction temperature of 500-600℃, reaction pressure of 100-500 kPa, and bed density of 150-700 kg / m³. 3 .

[0061] Optionally, the apparent linear velocity of the gas in the naphtha and methanol coupled aromatics production reaction zone is independently selected from any value or a range between 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.

[0062] Optionally, the reaction temperature of the naphtha and methanol coupled aromatics production reaction zone is independently selected from any value or a range between 500℃, 520℃, 530℃, 540℃, 550℃, 560℃, 570℃, 580℃, 590℃, and 600℃.

[0063] Optionally, the reaction pressure in the naphtha and methanol coupled aromatics production reaction zone is independently selected from any value or a range between 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.

[0064] Optionally, the bed density of the naphtha and methanol coupled aromatics production reaction zone is independently selected from 150 kg / m³. 3 200kg / m 3 250kg / m 3 300kg / m 3 350kg / m 3 400kg / m 3 450kg / m 3 500kg / m 3 550kg / m 3 600kg / m 3 650kg / m 3 700kg / m 3 Any value in the range or any value between the two.

[0065] Preferably, the light hydrocarbon aromatization product gas enters the gas-solid separation device II to remove the entrained catalyst, and then enters the gas collection chamber II, and enters the first gas-solid separation zone of the naphtha and methanol coupled aromatics production reactor through the product gas delivery pipe II;

[0066] The catalyst in the light hydrocarbon aromatization reaction zone enters the naphtha and methanol coupled aromatics production reactor through the light hydrocarbon aromatization slide valve.

[0067] Optionally, the process conditions of the light hydrocarbon aromatization reaction zone are as follows: apparent gas linear velocity of 0.5-2.0 m / s, reaction temperature of 550-665℃, reaction pressure of 100-500 kPa, and bed density of 150-700 kg / m³. 3 .

[0068] Optionally, the apparent linear velocity of the gas in the light hydrocarbon aromatization reaction zone is independently selected from any value or a range between 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.

[0069] Optionally, the reaction temperature of the light hydrocarbon aromatization reaction zone is independently selected from any value or a range between any two of 550℃, 560℃, 570℃, 580℃, 590℃, 600℃, 610℃, 620℃, 630℃, 640℃, 650℃, 660℃, and 665℃.

[0070] Optionally, the reaction pressure is independently selected from any value or a range between any two of 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.

[0071] Optionally, the bed density is independently selected from 150 kg / m³. 3 200kg / m 3 250kg / m 3 300kg / m 3 350kg / m 3 400kg / m 3 450kg / m 3 500kg / m 3 550kg / m 3 600kg / m 3 650kg / m 3 700kg / m 3 Any value in the range or any value between the two.

[0072] Preferably, the method further includes introducing regeneration gas and a catalyst to be generated into the regenerator to obtain a high-temperature regenerated catalyst, which is then transported to the light hydrocarbon aromatization reactor.

[0073] Preferably, the regenerated gas is introduced into the regeneration zone of the regenerator via a regenerator distributor.

[0074] Preferably, the regenerated gas is selected from at least one of oxygen, air, and oxygen-enriched air.

[0075] Preferably, the carbon content in the catalyst is 1.0-3.0 wt%.

[0076] Preferably, the carbon content in the regenerated catalyst is ≤0.5wt%.

[0077] Preferably, the process conditions in the regeneration zone of the regenerator are: apparent gas linear velocity of 0.5-2.0 m / s, regeneration temperature of 600-750℃, regeneration pressure of 100-500 kPa, and bed density of 150-700 kg / m³. 3 .

[0078] Optionally, the apparent linear velocity of the gas is independently selected from any value or a range between 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.

[0079] Optionally, the regeneration temperature is independently selected from any value or a 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.

[0080] Optionally, the regeneration pressure is independently selected from any value or a range between any two of 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.

[0081] Optionally, the bed density is independently selected from 150 kg / m³. 3 200kg / m 3 250kg / m 3 300kg / m 3 350kg / m 3 400kg / m 3 450kg / m 3 500kg / m 3 550kg / m 3600kg / m 3 650kg / m 3 700kg / m 3 Any value in the range or any value between the two.

[0082] Preferably, the coke on the catalyst reacts with the regenerated gas to generate flue gas, which enters the third gas-solid separation zone to remove the regenerated catalyst carried therein.

[0083] Preferably, the flue gas enters the third gas-solid separation zone to remove the entrained regeneration catalyst, specifically including: the flue gas first enters the regenerator gas-solid separation equipment, and after removing the entrained regeneration catalyst, it enters the downstream section through the regenerator gas collection chamber and the flue gas conveying pipe.

[0084] Preferably, the regenerated catalyst enters the light hydrocarbon aromatization reactor through a regenerator stripper and a regenerated slide valve.

[0085] Preferably, the method further includes: introducing feedstock into the riser reactor at the inlet end of the riser reactor of the light hydrocarbon aromatization reactor; the regenerated catalyst is introduced into the riser reactor via a regenerator stripper and a regenerated slide valve, and the feedstock in the riser reactor is converted into a stream containing BTX under the action of the regenerated catalyst, which enters the lower part of the light hydrocarbon aromatization reaction zone in the bed reactor through the outlet end of the riser reactor.

[0086] Preferably, the method further includes: introducing a catalyst into the inlet end of the riser reactor of the light hydrocarbon aromatization reactor, and then into the bed reactor through the riser reactor.

[0087] Preferably, the feedstock of the riser reactor includes water vapor and low-carbon alkanes separated from the product gas stream.

[0088] Preferably, the water vapor content in the feedstock of the riser reactor is 0-80 wt%.

[0089] Preferably, the process conditions of the riser reactor are: apparent gas linear velocity of 3.0-10.0 m / s, temperature of 580-700℃, pressure of 100-500 kPa, and bed density of 50-150 kg / m³. 3 .

[0090] Optionally, the apparent linear velocity of the gas is independently selected from any value or a range between 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.

[0091] Optionally, the temperature is independently selected from any value or a range between any two of 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.

[0092] Optionally, the pressure is independently selected from any value or a range between any two of 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.

[0093] Optionally, the bed density is independently selected from 50 kg / m³. 3 60kg / m 3 70kg / m 3 80kg / m 3 90kg / m 3 100kg / m 3 110kg / m 3 120kg / m 3 130kg / m 3 140kg / m 3 150kg / m 3 Any value in the range or any value between the two.

[0094] Preferably, the feedstock of the bed reactor is introduced into the light hydrocarbon aromatization reaction zone through the bed reactor distributor, and comes into contact with the catalyst from the riser reactor to generate light hydrocarbon aromatization product gas.

[0095] Optionally, the feedstock of the bed reactor comprises C4 and C5 hydrocarbons. The C4 and C5 hydrocarbons are derived from C4 and C5 hydrocarbons separated from the product gas stream.

[0096] Preferably, the feedstock of the bed reactor comprises C3, C4, and C5 hydrocarbons. The C3, C4, and C5 hydrocarbons are derived from C3, C4, and C5 hydrocarbons separated from the product gas stream.

[0097] Preferably, the components of the BTX-containing stream include: BTX, low-carbon olefins, and H2.

[0098] Preferably, the method further includes:

[0099] The catalyst in the naphtha and methanol coupled aromatics production reaction zone is fed into the reactor stripper, and after stripping, it enters the downstream area through the catalyst slide valve and the catalyst delivery pipe.

[0100] Preferably, the downstream region is a regenerator.

[0101] In this application, the aromatics potential content of the naphtha feedstock is 0-80 wt%, and the single-pass conversion rate of naphtha is 60-80 wt%. Using the naphtha and methanol coupled aromatics production apparatus and method based on this application, unconverted naphtha is separated from the product gas and returned as feedstock to the naphtha and methanol coupled aromatics production reactor. Some low-carbon alkanes are separated from the product gas and returned as feedstock to the riser reactor in the light hydrocarbon aromatization reactor. C3, C4, and C5 hydrocarbons are separated from the product gas and returned as feedstock to the bed reactor in the light hydrocarbon aromatization reactor. The final product distribution is: 60-73 wt% BTX, 9-16 wt% low-carbon olefins, 3-6 wt% hydrogen, 3-8 wt% low-carbon alkanes, 4-6 wt% combustible gas, 4-8 wt% heavy aromatics, and 0.5-1 wt% coke. The p-xylene content in the mixed xylenes in the product is 60-75 wt%.

[0102] The beneficial effects that this application can produce include:

[0103] 1) This application can efficiently and selectively convert straight-chain and branched aliphatic hydrocarbons into aromatics. It has a wide range of feedstocks and can use naphtha with low aromatic content as a feedstock to prepare aromatics.

[0104] 2) This application realizes the aromatization of low-carbon alkanes, C4 and C5 hydrocarbons through a light hydrocarbon aromatization reactor and a metal molecular sieve bifunctional catalyst, which greatly improves the aromatics yield of naphtha to aromatics technology.

[0105] 3) The naphtha and methanol coupled aromatics production unit in this application includes a naphtha and methanol coupled aromatics production reactor, which contains multiple sub-distributors. Naphtha enters the naphtha and methanol coupled aromatics production reaction zone via the first sub-distributor, while methanol enters the same reaction zone via the second to nth sub-distributors. The naphtha and methanol coupled aromatics production reactor is a fluidized bed reactor adapted for cascade reactions. Naphtha is converted to benzene and toluene in the lower part of the reaction zone, and then flows upward to the middle and upper parts of the reaction zone. Benzene, toluene, and methanol undergo methylation reactions to further generate para-xylene, thereby increasing the yield of para-xylene. The high-temperature catalyst from the light hydrocarbon aromatization reactor directly enters the lower part of the reaction zone, which helps to provide the heat required for the conversion of naphtha to aromatics, thus improving the conversion rate of naphtha. Methanol is directly introduced into the middle and upper parts of the naphtha-methanol coupled aromatics production reactor, effectively reducing the residence time of para-xylene in the reaction zone, inhibiting the isomerization reaction of para-xylene, increasing the para-xylene content in xylene (up to 75 wt% under optimal process conditions), and simultaneously significantly reducing the energy consumption for para-xylene separation. In short, in the naphtha-methanol coupled aromatics production reactor, the naphtha feedstock flows from bottom to top. During its conversion to aromatics, the methylation feedstock (methanol) is added stepwise to control the cascade reaction (naphtha → benzene, toluene → para-xylene), thereby increasing the production of para-xylene.

[0106] 4) The aromatization of naphtha is a strongly endothermic reaction; converting 1 kg of naphtha into aromatics requires absorbing 1.1-1.6 MJ of heat. The methylation reaction of methanol and aromatics is a strongly exothermic reaction; converting 1 kg of methanol into a methyl group on an aromatic hydrocarbon releases more than 2.0 MJ of heat. Therefore, the preparation of p-xylene from benzene, toluene, and methanol can also provide in-situ heat for the coupled naphtha-methanol aromatics production reaction, allowing it to reach autothermal equilibrium.

[0107] 5) The naphtha and methanol coupled aromatics production unit in this application is equipped with a separate light hydrocarbon aromatization reactor. Low-carbon alkanes are very stable and require higher reaction temperatures. The temperature of the light hydrocarbon aromatization reactor is higher than that of the naphtha and methanol coupled aromatics production reactor. Low-carbon alkanes, C4 and C5 hydrocarbons undergo aromatization reactions in the separate light hydrocarbon aromatization reactor, which improves the reaction rate and aromatics yield. Attached Figure Description

[0108] Figure 1 This is a schematic diagram of an apparatus for producing aromatics by coupling naphtha and methanol in one embodiment of this application.

[0109] List of components and reference numerals:

[0110] 1. A reactor for the coupled production of aromatics from naphtha and methanol;

[0111] 1-1 Shell of a reactor for coupled naphtha and methanol production of aromatics;

[0112] 1-2 Distributor for naphtha and methanol coupled aromatics production reactor;

[0113] 1-3 Gas-solid separation equipment I; 1-4 Gas collection chamber I; 1-5 Product gas delivery pipe I;

[0114] 1-6 Reactor stripper; 1-7 Preparing slide valve; 1-8 Preparing agent delivery pipe;

[0115] 1-2-1 First sub-distributor; 1-2-2 Second sub-distributor; 1-2-3 Third sub-distributor.

[0116] 2 Regenerators;

[0117] 2-1 Regenerator housing; 2-2 Regenerator distributor;

[0118] 2-3 Regenerator gas-solid separation equipment; 2-4 Regenerator gas collection chamber; 2-5 Flue gas conveying pipe;

[0119] 2-6 Regenerator stripper; 2-7 Regeneration slide valve.

[0120] 3. Light hydrocarbon aromatization reactor;

[0121] 3-1 Inlet end of riser reactor; 3-2 Middle part of riser reactor;

[0122] 3-3 Outlet end of riser reactor; 3-4 Bed reactor shell;

[0123] 3-5 Bed reactor distributor; 3-6 Gas-solid separation equipment II;

[0124] 3-7 Gas collecting chamber II; 3-8 Product gas delivery pipe II; 3-9 Light hydrocarbon aromatization slide valve. Detailed Implementation

[0125] The present application is described in detail below with reference to the embodiments, but the present application is not limited to these embodiments.

[0126] This application provides a naphtha and methanol coupled aromatics production apparatus, comprising a light hydrocarbon aromatization reactor and a naphtha and methanol coupled aromatics production reactor; wherein...

[0127] The light hydrocarbon aromatization reactor is used to introduce raw materials and a high-temperature catalyst; at least one outlet of the light hydrocarbon aromatization reactor is connected to the naphtha and methanol coupled aromatics reactor for conveying the catalyst and the generated light hydrocarbon aromatization product gas to the naphtha and methanol coupled aromatics reactor.

[0128] The naphtha and methanol coupled aromatics reactor is used to introduce naphtha and methanol, and to contact the naphtha with a catalyst from the light hydrocarbon aromatization reactor to generate a product gas stream containing BTX; the methanol is then subjected to a methylation reaction with benzene and toluene in the product gas stream to generate p-xylene.

[0129] The naphtha components described in this application include C4-C 12 Straight-chain, branched aliphatic hydrocarbons, cycloalkanes, and aromatic hydrocarbons.

[0130] In this application, BTX refers to aromatic hydrocarbons, specifically benzene, toluene, and xylene.

[0131] In a preferred embodiment, the apparatus further includes a regenerator, at least one inlet of the light hydrocarbon aromatization reactor being connected to the regenerator for obtaining a high-temperature regenerated catalyst generated by the regenerator.

[0132] Please see Figure 1 It illustrates a preferred embodiment of the naphtha and methanol coupled aromatics production apparatus of this application, including a naphtha and methanol coupled aromatics production reactor 1, a regenerator 2, and a light hydrocarbon aromatization reactor 3.

[0133] The naphtha and methanol coupled aromatics production reactor 1 includes: a naphtha and methanol coupled aromatics production reactor shell 1-1, a naphtha and methanol coupled aromatics production reactor distributor 1-2, a gas-solid separation device 11-3, a gas collection chamber 11-4, a product gas conveying pipe 11-5, a reactor stripper 1-6, a pre-generation slide valve 1-7, a pre-generation agent conveying pipe 1-8.

[0134] The naphtha and methanol coupled aromatics production 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.

[0135] The naphtha and methanol coupled aromatics reactor 1 includes a naphtha and methanol coupled aromatics reactor shell 1-1. The naphtha and methanol coupled aromatics reactor shell 1-1 includes an upper shell and a lower shell. The upper shell of the naphtha and methanol coupled aromatics reactor forms a first gas-solid separation zone, and the lower shell of the naphtha and methanol coupled aromatics reactor forms a naphtha and methanol coupled aromatics reaction zone. The naphtha and methanol coupled aromatics reactor shell 1-1 is provided with an outlet for a light hydrocarbon aromatization reactor 3.

[0136] The naphtha and methanol coupled aromatics production reaction zone is equipped with a naphtha and methanol coupled aromatics production reactor distributor 1-2. The naphtha and methanol coupled aromatics production reactor distributor 1-2 comprises three sub-distributors, numbered from bottom to top as sub-distributor 1-2-1 to sub-distributor 1-2-3. Sub-distributor 1-2-1 is used to introduce naphtha feedstock; sub-distributors 1-2-2 to 1-2-3 are used to introduce methanol feedstock.

[0137] The reactor shell 1-1 for the coupled naphtha and methanol aromatics production is further provided with a gas-solid separation device I1-3 and a gas collecting chamber I1-4; the gas collecting chamber I1-4 is located at the inner top of the reactor shell; the gas outlet of the gas-solid separation device I1-3 is connected to the gas collecting chamber I1-4; the gas collecting chamber I1-4 is connected to the product gas conveying pipe I1-5; the catalyst outlet end of the gas-solid separation device I1-3 is located above the opening end of the inlet pipe of the reactor stripper 1-6.

[0138] Below the naphtha and methanol coupled aromatics production reaction zone is a reactor stripper 1-6; the inlet of the reactor stripper 1-6 is located inside the reactor shell 1-1 of the naphtha and methanol coupled aromatics production reactor; the outlet of the reactor stripper 1-6 is located outside the reactor shell 1-1 of the naphtha and methanol coupled aromatics production reactor and is connected to the waiting slide valve 1-7; the opening end of the inlet of the reactor stripper 1-6 is located above the first sub-distributor 1-2-1.

[0139] Below the reactor stripper 1-6, there is a regenerating slide valve 1-7; the inlet of the regenerating slide valve 1-7 is connected to the outlet of the reactor stripper 1-6, the outlet of the regenerating slide valve 1-7 is connected to the inlet of the regenerating agent delivery pipe 1-8, and the outlet of the regenerating agent delivery pipe 1-8 is connected to the regenerator housing 2-1.

[0140] The pre-generation slide valves 1-7 are used to control the circulation amount of the pre-generation catalyst.

[0141] In a preferred embodiment, the gas-solid separation device I1-3 employs one or more sets of gas-solid cyclone separators, each set of gas-solid cyclone separators including a first-stage gas-solid cyclone separator and a second-stage gas-solid cyclone separator.

[0142] The regenerator 2 includes: a regenerator housing 2-1, a regenerator distributor 2-2, a regenerator gas-solid separation device 2-3, a regenerator gas collection chamber 2-4, a flue gas conveying pipe 2-5, a regenerator stripper 2-6, and a regeneration slide valve 2-7.

[0143] The regenerator housing 2-1 includes an upper regenerator housing and a lower regenerator housing. The upper regenerator housing encloses a third gas-solid separation zone, and the lower regenerator housing encloses a regeneration zone. The regenerator housing 2-1 is provided with an outlet for a regenerator delivery pipe 1-8.

[0144] The lower part of the regeneration zone is provided with a regenerator distributor 2-2, which is used to introduce regeneration gas.

[0145] The regenerator housing 2-1 is further provided with a regenerator gas-solid separation device 2-3 and a regenerator gas collection chamber 2-4; the regenerator gas collection chamber 2-4 is located at the inner top of the regenerator housing 2-1; the gas outlet of the regenerator gas-solid separation device 2-3 is connected to the regenerator gas collection chamber 2-4; the regenerator gas collection chamber 2-4 is connected to the flue gas conveying pipe 2-5; the catalyst outlet end of the regenerator gas-solid separation device 2-3 is located above the inlet pipe opening end of the regenerator stripper 2-6.

[0146] Below the regeneration zone is a regenerator stripper 2-6; the inlet of the regenerator stripper 2-6 is located inside the regenerator housing 2-1; the outlet of the regenerator stripper 2-6 is located outside the regenerator housing 2-1 and is connected to the regeneration slide valve 2-7; the open end of the inlet of the regenerator stripper 2-6 is located above the regenerator distributor 2-2.

[0147] A regeneration slide valve 2-7 is provided below the regenerator stripper 2-6; the inlet of the regeneration slide valve 2-7 is connected to the outlet of the regenerator stripper 2-6.

[0148] The regeneration slide valves 2-7 are used to control the circulation rate of the regenerated catalyst.

[0149] In a preferred embodiment, the regenerator gas-solid separation device 2-3 employs one or more sets of gas-solid cyclone separators, each set of gas-solid cyclone separators including a first-stage gas-solid cyclone separator and a second-stage gas-solid cyclone separator.

[0150] The light hydrocarbon aromatization reactor comprises: an inlet end 3-1 of the riser reactor, a middle section of the riser reactor 3-2, an outlet end 3-3 of the riser reactor, a bed reactor shell 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 conveying pipe II 3-8, and a light hydrocarbon aromatization slide valve 3-9.

[0151] The bed reactor shell 3-4 includes an upper bed reactor shell and a lower bed reactor shell. The upper bed reactor shell encloses a second gas-solid separation zone, and the lower bed reactor shell encloses a light hydrocarbon aromatization reaction zone. A bed reactor distributor 3-5 is provided in the lower inner part of the light hydrocarbon aromatization reaction zone. A light hydrocarbon aromatization slide valve 3-9 is also provided outside the light hydrocarbon aromatization reaction zone. The upper section of the riser reactor penetrates the bottom of the bed reactor and is inserted axially into the bed reactor. The outlet end 3-3 of the riser reactor is located in the lower inner part of the light hydrocarbon aromatization reaction zone.

[0152] The light hydrocarbon aromatization slide valves 3-9 are used to deliver the catalyst to the next stage reactor, such as the naphtha and methanol coupled aromatics reactor 1.

[0153] The second gas-solid separation zone is equipped with a gas-solid separation device II 3-6 and a gas collection chamber II 3-7; the gas outlet of the gas-solid separation device II 3-6 is connected to the gas collection chamber II 3-7; the catalyst outlet of the gas-solid separation device II 3-6 is located in the light hydrocarbon aromatization reaction zone; the gas collection chamber II 3-7 is connected to the product gas delivery pipe II 3-8 located outside the bed reactor.

[0154] In a preferred embodiment, the gas-solid separation device II 3-6 is a gas-solid cyclone separator.

[0155] In a preferred embodiment, a gas collection chamber II 3-7 is provided at the inner top of the bed reactor; the catalyst outlet of the gas-solid cyclone separator 3-7 of the bed reactor is located above the outlet end 3-3 of the riser reactor.

[0156] In a preferred embodiment, the bed reactor distributor 3-5 is used to introduce feedstock into the bed reactor.

[0157] In a preferred embodiment, the inlet end 3-1 of the riser reactor is used to introduce the catalyst and the feedstock for the riser reactor.

[0158] 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 and methanol coupled aromatics production reactor 1.

[0159] In a preferred embodiment, the inlet end 3-1 of the riser reactor is connected to the regeneration slide valve 2-7 via a pipe, and the light hydrocarbon aromatization slide valve 3-9 is connected to the shell 1-1 of the naphtha and methanol coupled aromatics reactor via a pipe, and is located between the first sub-distributor 1-2-1 and the second sub-distributor 1-2-2.

[0160] In a preferred embodiment, the product gas delivery pipe II 3-8 is connected to the shell 1-1 of the naphtha and methanol coupled aromatics production reactor.

[0161] This application also provides a method for producing aromatics by coupling naphtha and methanol, comprising: preparing aromatics using the above-mentioned naphtha and methanol coupled aromatics production apparatus and catalyst.

[0162] The catalyst used is a bifunctional metal molecular sieve catalyst. Metal-modified HZSM-5 zeolite molecular sieves were used in Examples 1-5.

[0163] The metal used for metal modification is selected from at least one of La, Zn, Ga, Fe, Mo, and Cr;

[0164] The method of metal modification includes: placing HZSM-5 zeolite molecular sieve in a metal salt solution, impregnating, drying, and calcining to obtain the metal-modified HZSM-5 zeolite molecular sieve.

[0165] In a preferred embodiment, the method includes the following steps:

[0166] a) Naphtha enters the naphtha and methanol coupled aromatics production reactor 1's aromatics production zone via the first sub-distributor 1-2-1 of distributor 1-2, where it contacts the catalyst from light hydrocarbon aromatization reactor 3, generating a product gas stream containing BTX, low-carbon olefins, hydrogen, low-carbon alkanes, combustible gas, heavy aromatics, and unconverted naphtha. Methanol enters the naphtha and methanol coupled aromatics production zone via the second to third sub-distributors 1-2-2 and 1-2-3 of distributor 1-2, respectively, where it reacts with benzene and toluene in the product gas stream. Benzene undergoes a methylation reaction to produce p-xylene; the catalyst from the light hydrocarbon aromatization reactor 3 cokes and transforms into a reactive catalyst in the naphtha and methanol coupled aromatics production reaction zone; the product gas stream enters the gas-solid separation device I1-3 to remove the entrained reactive catalyst, then enters the gas collecting chamber I1-4, and enters the downstream section through the product gas conveying pipe I1-5; the reactive catalyst in the naphtha and methanol coupled aromatics production reaction zone enters the reactor stripper 1-6 through the open end of the inlet pipe of the reactor stripper 1-6 for stripping, and after stripping, it enters the regenerator 2 through the reactive catalyst slide valve 1-7 and the reactive catalyst conveying pipe 1-8.

[0167] b) The regenerated gas is introduced into the regeneration zone of regenerator 2 through regenerator distributor 2-2 and comes into contact with the catalyst to be regenerated. The coke on the catalyst to be regenerated reacts with the regenerated gas to generate flue gas. At the same time, the catalyst to be regenerated is converted into regenerated catalyst. The flue gas enters the gas-solid separation device 2-3 of regenerator to remove the regenerated catalyst entrained therein, and then enters the gas collection chamber 2-4 of regenerator, and enters the downstream section through the flue gas conveying pipe 2-5. The regenerated catalyst enters the light hydrocarbon aromatization reactor 3 in sequence through regenerator stripper 2-6 and regeneration slide valve 2-7.

[0168] c) The feedstock for the riser reactor is introduced into the riser reactor through the inlet end 3-1, where it contacts and reacts with the regenerated catalyst from the regenerator. Under the action of the catalyst, the feedstock in the riser reactor is converted into a stream containing components such as BTX, low-carbon olefins, and H2. Then, it enters the lower part of the light hydrocarbon aromatization reaction zone in the bed reactor through the outlet end 3-3 of the riser reactor. The feedstock in the bed reactor is introduced into the light hydrocarbon aromatization reaction zone through the bed reactor distributor 3-5, where it contacts the catalyst from the riser reactor to generate 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 II 3-6 to remove the entrained catalyst, and then enters the gas collecting chamber II 3-7. It then enters the first gas-solid separation zone through the product gas conveying pipe II 3-8. The catalyst in the light hydrocarbon aromatization reaction zone enters the naphtha and methanol coupled aromatics production reactor 1 through the light hydrocarbon aromatization slide valve 3-9.

[0169] The low-carbon olefins refer to ethylene and propylene.

[0170] The low-carbon alkanes refer to ethane and propane.

[0171] The combustible gas contains methane and CO, etc.

[0172] The heavy aromatic hydrocarbons refer to aromatic hydrocarbons with 9 or more carbon atoms in their molecules.

[0173] In a preferred embodiment, the naphtha is selected from at least one of direct coal liquefaction naphtha, indirect coal liquefaction naphtha, straight-run naphtha, and hydrocracked naphtha.

[0174] In a preferred embodiment, the naphtha further comprises unconverted naphtha separated from the product gas stream.

[0175] In a preferred embodiment, the carbon content in the generated catalyst is 1.0-3.0 wt%.

[0176] In a preferred embodiment, the process conditions of the naphtha and methanol coupled aromatics production reaction zone are as follows: apparent gas linear velocity of 0.5-2.0 m / s, reaction temperature of 500-600℃, reaction pressure of 100-500 kPa, and bed density of 150-700 kg / m³. 3 .

[0177] Optionally, the apparent linear velocity of the gas in the naphtha and methanol coupled aromatics production reaction zone is independently selected from any value or a range between 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.

[0178] Optionally, the reaction temperature of the naphtha and methanol coupled aromatics production reaction zone is independently selected from any value or a range between 500℃, 520℃, 530℃, 540℃, 550℃, 560℃, 570℃, 580℃, 590℃, and 600℃.

[0179] Optionally, the reaction pressure in the naphtha and methanol coupled aromatics production reaction zone is independently selected from any value or a range between 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.

[0180] Optionally, the bed density of the naphtha and methanol coupled aromatics production reaction zone is independently selected from 150 kg / m³. 3 200kg / m 3 250kg / m 3 300kg / m 3 350kg / m 3 400kg / m 3 450kg / m 3 500kg / m 3 550kg / m 3 600kg / m 3 650kg / m 3 700kg / m 3 Any value in the range or any value between the two.

[0181] In a preferred embodiment, the carbon content in the regenerated catalyst is ≤0.5wt%.

[0182] In a preferred embodiment, the regenerated gas is selected from at least one of oxygen, air, and oxygen-enriched air.

[0183] In a preferred embodiment, the process conditions in the regeneration zone are: apparent gas linear velocity of 0.5-2.0 m / s, regeneration temperature of 600-750℃, regeneration pressure of 100-500 kPa, and bed density of 150-700 kg / m³. 3 .

[0184] Optionally, the apparent linear velocity of the gas in the regeneration zone is independently selected from any value or a range between 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.

[0185] Optionally, the regeneration temperature of the regeneration zone is independently selected from any value or a range between 600°C, 615°C, 630°C, 645°C, 670°C, 685°C, 700°C, 715°C, 730°C, 745°C, and 750°C.

[0186] Optionally, the regeneration pressure in the regeneration zone is independently selected from any value or a range between any two of 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.

[0187] Optionally, the bed density in the regeneration zone is independently selected from 150 kg / m³. 3 200kg / m 3 250kg / m 3 300kg / m 3 350kg / m 3 400kg / m 3 450kg / m 3 500kg / m 3 550kg / m 3 600kg / m 3 650kg / m 3 700kg / m 3 Any value in the range or any value between the two.

[0188] In a preferred embodiment, the feedstock of the riser reactor comprises water vapor and low-carbon alkanes separated from the product gas stream.

[0189] In a preferred embodiment, the water vapor content in the feedstock of the riser reactor is 0-80 wt%.

[0190] In a preferred embodiment, the process conditions of the riser reactor are: apparent gas linear velocity of 3.0-10.0 m / s, temperature of 580-700℃, pressure of 100-500 kPa, and bed density of 50-150 kg / m³. 3 .

[0191] Optionally, the apparent linear velocity of the gas in the riser reactor is independently selected from any value or a range between 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.

[0192] Optionally, the temperature of the riser reactor is independently selected from any value or a range between any two of 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.

[0193] Optionally, the pressure of the riser reactor is independently selected from any value or a range between any two of 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.

[0194] Optionally, the bed density of the riser reactor is independently selected from 50 kg / m³. 3 60kg / m 3 70kg / m 3 80kg / m 3 90kg / m 3 100kg / m 3 110kg / m 3 120kg / m 3 130kg / m 3 140kg / m 3 150kg / m 3 Any value in the range or any value between the two.

[0195] The feedstock for the bed reactor contains C4 and C5 hydrocarbons.

[0196] In a preferred embodiment, the feedstock of the bed reactor comprises C3, C4 and C5 hydrocarbons.

[0197] In a preferred embodiment, the C3, C4, and C5 hydrocarbons are derived from C3, C4, and C5 hydrocarbons separated from the product gas stream.

[0198] The C3, C4, and C5 hydrocarbons refer to hydrocarbons with 3, 4, and 5 carbon atoms, respectively.

[0199] In a preferred embodiment, the process conditions of the light hydrocarbon aromatization reaction zone are as follows: apparent gas linear velocity of 0.5-2.0 m / s, reaction temperature of 550-665℃, reaction pressure of 100-500 kPa, and bed density of 150-700 kg / m³. 3 .

[0200] Optionally, the apparent linear velocity of the gas in the light hydrocarbon aromatization reaction zone is independently selected from any value or a range between 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.

[0201] Optionally, the reaction temperature of the light hydrocarbon aromatization reaction zone is independently selected from any value or a range between 550℃, 560℃, 570℃, 580℃, 590℃, 600℃, 610℃, 620℃, 630℃, 640℃, 650℃, 660℃, and 665℃.

[0202] Optionally, the reaction pressure in the light hydrocarbon aromatization reaction zone is independently selected from any value or a range between 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.

[0203] Optionally, the bed density of the light hydrocarbon aromatization reaction zone is independently selected from 150 kg / m³. 3 200kg / m 3 250kg / m 3 300kg / m 3 350kg / m3 400kg / m 3 450kg / m 3 500kg / m 3 550kg / m 3 600kg / m 3 650kg / m 3 700kg / m 3 Any value in the range or any value between the two.

[0204] In the embodiments described in this application, the aromatic potential content of the naphtha feedstock is 0-80 wt%, the single-pass conversion rate of naphtha is 60-80 wt%, and the single-pass conversion rate of methanol is approximately 100 wt%. Unconverted naphtha is separated from the product gas and returned as feedstock to the naphtha and methanol coupled aromatics reactor. Some low-carbon alkanes are separated from the product gas and returned as feedstock to the riser reactor in the light hydrocarbon aromatization reactor. C3, C4, and C5 hydrocarbons are separated from the product gas and returned as feedstock to the bed reactor in the light hydrocarbon aromatization reactor. The final product distribution is: 60-73 wt% BTX, 9-16 wt% low-carbon olefins, 3-6 wt% hydrogen, 3-8 wt% low-carbon alkanes, 4-6 wt% combustible gas, 4-8 wt% heavy aromatics, and 0.5-1 wt% coke. The para-xylene content in the mixed xylenes in the product is 60-75 wt%.

[0205] Example 1

[0206] This implementation plan adopts Figure 1 The apparatus shown.

[0207] In this embodiment, the naphtha feedstock entering the naphtha and methanol coupled aromatics production reactor is direct coal liquefaction naphtha with an aromatics potential content of 78 wt%.

[0208] The process conditions for the naphtha-methanol coupled aromatics production reactor in the reaction zone are as follows: apparent gas linear velocity of 0.5 m / s, reaction temperature of 600℃, reaction pressure of 100 kPa, and bed density of 700 kg / m³. 3 .

[0209] The regenerated gas is air.

[0210] The process conditions in the regeneration zone of the regenerator are as follows: apparent gas linear velocity of 0.5 m / s, regeneration temperature of 745℃, regeneration pressure of 100 kPa, and bed density of 700 kg / m³. 3 .

[0211] The feedstock for the riser reactor is low-carbon alkanes separated from the product gas stream.

[0212] The process conditions for the riser reactor are: apparent gas linear velocity of 3.0 m / s, temperature of 690℃, pressure of 100 kPa, and bed density of 150 kg / m³. 3 .

[0213] The feedstock for the bed reactor is unconverted naphtha separated from the product gas stream. The main components of the unconverted naphtha are C4-C. 12 Straight-chain, branched aliphatic hydrocarbons and cycloalkanes.

[0214] The process conditions for the light hydrocarbon aromatization reaction zone are as follows: apparent gas linear velocity of 0.5 m / s, reaction temperature of 665℃, reaction pressure of 100 kPa, and bed density of 700 kg / m³. 3 .

[0215] The carbon content in the unused catalyst is 1.0 wt%, and the carbon content in the regenerated catalyst is 0.2 wt%.

[0216] The single-pass conversion rate of naphtha feedstock entering the naphtha-methanol coupled aromatics reactor is 61 wt%.

[0217] The product composition is as follows: 73 wt% BTX, 9 wt% low-carbon olefins, 3 wt% hydrogen, 3 wt% low-carbon alkanes, 5 wt% combustible gases, 6.5 wt% heavy aromatics, and 0.5 wt% coke. The p-xylene content in the mixed xylenes in the product is 60 wt%.

[0218] Example 2

[0219] This implementation plan adopts Figure 1 The apparatus shown.

[0220] In this embodiment, the naphtha feedstock entering the naphtha and methanol coupled aromatics production reactor is coal-to-liquid naphtha with an aromatics potential content of 0.1 wt%. The naphtha feedstock entering the naphtha and methanol coupled aromatics production reactor also includes unconverted naphtha separated from the product gas stream.

[0221] The process conditions of the naphtha and methanol coupled aromatics production reactor in the naphtha and methanol coupled aromatics production reaction zone are as follows: apparent gas linear velocity of 2.0 m / s, reaction temperature of 510℃, reaction pressure of 500 kPa, and bed density of 150 kg / m³. 3 .

[0222] The regenerated gas is oxygen.

[0223] The process conditions in the regeneration zone of the regenerator are as follows: apparent gas linear velocity of 2.0 m / s, regeneration temperature of 610℃, regeneration pressure of 500 kPa, and bed density of 150 kg / m³. 3 .

[0224] The feedstock for the riser reactor comprises water vapor and low-carbon alkanes separated from the product gas stream, wherein the water vapor content is 80 wt%.

[0225] The process conditions for the riser reactor are: apparent gas linear velocity of 10.0 m / s, temperature of 580℃, pressure of 500 kPa, and bed density of 50 kg / m³. 3 .

[0226] The feedstock for the bed reactor consists of C3, C4, and C5 hydrocarbons separated from the product gas stream.

[0227] The process conditions for the light hydrocarbon aromatization reaction zone are as follows: apparent gas linear velocity of 2.0 m / s, reaction temperature of 550℃, reaction pressure of 500 kPa, and bed density of 150 kg / m³. 3 .

[0228] The carbon content in the unused catalyst is 3.0 wt%, and the carbon content in the regenerated catalyst is 0.1 wt%.

[0229] The single-pass conversion rate of naphtha feedstock entering the naphtha-methanol coupled aromatics reactor is 66 wt%.

[0230] The product composition is as follows: 65 wt% BTX, 13 wt% low-carbon olefins, 5 wt% hydrogen, 3.2 wt% low-carbon alkanes, 5 wt% combustible gases, 8 wt% heavy aromatics, and 0.8 wt% coke. The p-xylene content in the mixed xylenes in the product is 66 wt%.

[0231] Example 3

[0232] This implementation plan adopts Figure 1 The apparatus shown.

[0233] In this embodiment, the naphtha feedstock entering the naphtha and methanol coupled aromatics production reactor is coal-to-liquid naphtha with an aromatics potential content of 3 wt%. The naphtha feedstock entering the naphtha and methanol coupled aromatics production reactor also includes unconverted naphtha separated from the product gas stream.

[0234] The process conditions for the naphtha-methanol coupled aromatics production reactor in the reaction zone are as follows: apparent gas linear velocity of 1.2 m / s, reaction temperature of 550℃, reaction pressure of 120 kPa, and bed density of 260 kg / m³. 3 .

[0235] The regenerated gas is oxygen-rich air.

[0236] The process conditions in the regeneration zone of the regenerator are as follows: apparent gas linear velocity of 1.2 m / s, regeneration temperature of 650℃, regeneration pressure of 120 kPa, and bed density of 260 kg / m³. 3 .

[0237] The feedstock for the riser reactor comprises water vapor and low-carbon alkanes separated from the product gas stream, wherein the water vapor content is 25 wt%.

[0238] The process conditions for the riser reactor are: apparent gas linear velocity of 7.0 m / s, temperature of 630℃, pressure of 120 kPa, and bed density of 80 kg / m³. 3 .

[0239] The feedstock for the bed reactor consists of C4 and C5 hydrocarbons separated from the product gas stream.

[0240] The process conditions in the light hydrocarbon aromatization reaction zone are as follows: apparent gas linear velocity of 1.2 m / s, reaction temperature of 580℃, reaction pressure of 120 kPa, and bed density of 260 kg / m³. 3 .

[0241] The carbon content in the unused catalyst is 2.2 wt%, and the carbon content in the regenerated catalyst is 0.3 wt%.

[0242] The single-pass conversion rate of naphtha feedstock entering the naphtha-methanol coupled aromatics reactor is 80 wt%.

[0243] The product composition is as follows: 60 wt% BTX, 16 wt% low-carbon olefins, 6 wt% hydrogen, 8 wt% low-carbon alkanes, 4.5 wt% combustible gases, 5 wt% heavy aromatics, and 0.5 wt% coke. The p-xylene content in the mixed xylenes in the product is 75 wt%.

[0244] Example 4

[0245] This implementation plan adopts Figure 1 The apparatus shown.

[0246] In this embodiment, the naphtha feedstock entering the naphtha and methanol coupled aromatics reactor is straight-run naphtha with an aromatics potential content of 46 wt%. The naphtha feedstock entering the naphtha and methanol coupled aromatics reactor also includes unconverted naphtha separated from the product gas stream.

[0247] The process conditions of the naphtha and methanol coupled aromatics production reactor in the naphtha and methanol coupled aromatics production reaction zone are as follows: apparent gas linear velocity of 1.8 m / s, reaction temperature of 590℃, reaction pressure of 200 kPa, and bed density of 220 kg / m³. 3 .

[0248] The regenerated gas is air.

[0249] The process conditions in the regeneration zone of the regenerator are as follows: apparent gas linear velocity of 1.8 m / s, regeneration temperature of 700℃, regeneration pressure of 200 kPa, and bed density of 220 kg / m³. 3 .

[0250] The feedstock for the riser reactor comprises water vapor and low-carbon alkanes separated from the product gas stream, wherein the water vapor content is 50 wt%.

[0251] The process conditions for the riser reactor are: apparent gas linear velocity of 5.0 m / s, temperature of 660℃, pressure of 200 kPa, and bed density of 110 kg / m³. 3 .

[0252] The feedstock for the bed reactor consists of C4 and C5 hydrocarbons separated from the product gas stream.

[0253] The process conditions for the light hydrocarbon aromatization reaction zone are as follows: apparent gas linear velocity of 1.8 m / s, reaction temperature of 630℃, reaction pressure of 200 kPa, and bed density of 220 kg / m³. 3 .

[0254] The carbon content in the unused catalyst is 1.7 wt%, and the carbon content in the regenerated catalyst is 0.1 wt%.

[0255] The single-pass conversion rate of naphtha feedstock entering the naphtha-methanol coupled aromatics reactor is 78 wt%.

[0256] The product composition is as follows: 68.1 wt% BTX, 12 wt% low-carbon olefins, 5 wt% hydrogen, 6 wt% low-carbon alkanes, 4 wt% combustible gases, 4 wt% heavy aromatics, and 0.9 wt% coke. The p-xylene content in the mixed xylenes in the product is 71 wt%.

[0257] Example 5

[0258] This implementation plan adopts Figure 1 The apparatus shown.

[0259] In this embodiment, the naphtha feedstock entering the naphtha-methanol coupled aromatics reactor is hydrocracked naphtha with an aromatics potential content of 64 wt%. The naphtha feedstock entering the naphtha-methanol coupled aromatics reactor also includes unconverted naphtha separated from the product gas stream.

[0260] The process conditions for the naphtha-methanol coupled aromatics production reactor in the naphtha-methanol coupled aromatics production reaction zone are as follows: apparent gas linear velocity of 1.0 m / s, reaction temperature of 580℃, reaction pressure of 150 kPa, and bed density of 350 kg / m³.3 .

[0261] The regenerated gas is air.

[0262] The process conditions in the regeneration zone of the regenerator are as follows: apparent gas linear velocity of 1.0 m / s, regeneration temperature of 680℃, regeneration pressure of 150 kPa, and bed density of 350 kg / m³. 3 .

[0263] The feedstock for the riser reactor comprises water vapor and low-carbon alkanes separated from the product gas stream, wherein the water vapor content is 40 wt%.

[0264] The process conditions for the riser reactor are: apparent gas linear velocity of 7.0 m / s, temperature of 650℃, pressure of 150 kPa, and bed density of 80 kg / m³. 3 .

[0265] The feedstock for the bed reactor consists of C4 and C5 hydrocarbons separated from the product gas stream.

[0266] The process conditions for the light hydrocarbon aromatization reaction zone are as follows: apparent gas linear velocity of 1.0 m / s, reaction temperature of 610℃, reaction pressure of 150 kPa, and bed density of 350 kg / m³. 3 .

[0267] The carbon content in the unused catalyst is 1.5 wt%, and the carbon content in the regenerated catalyst is 0.5 wt%.

[0268] The single-pass conversion rate of naphtha feedstock entering the naphtha-methanol coupled aromatics reactor is 72 wt%.

[0269] The product composition is as follows: 71 wt% BTX, 9 wt% low-carbon olefins, 4 wt% hydrogen, 3 wt% low-carbon alkanes, 6 wt% combustible gases, 6 wt% heavy aromatics, and 1.0 wt% coke. The p-xylene content in the mixed xylenes in the product is 65 wt%.

[0270] The above description is merely a few embodiments of this application and is not intended to limit this application in any way. Although this application discloses preferred embodiments as described above, it is not intended to limit this application. Any changes or modifications made by those skilled in the art without departing from the scope of the technical solution of this application using the disclosed technical content are equivalent to equivalent implementation cases and fall within the scope of the technical solution.

Claims

1. A device for producing aromatics by coupling naphtha and methanol, characterized in that, The apparatus includes a light hydrocarbon aromatization reactor and a naphtha and methanol coupled aromatics production reactor; wherein... The light hydrocarbon aromatization reactor is used to introduce raw materials and a high-temperature catalyst; at least one outlet of the light hydrocarbon aromatization reactor is connected to the naphtha and methanol coupled aromatics reactor for conveying the catalyst and the generated light hydrocarbon aromatization product gas to the naphtha and methanol coupled aromatics reactor. The naphtha and methanol coupled aromatics reactor is used to introduce naphtha and methanol, contact the naphtha with a catalyst from the light hydrocarbon aromatization reactor, and generate a product gas stream containing BTX after the reaction; the methanol undergoes a methylation reaction with benzene and toluene in the product gas stream to generate p-xylene; The naphtha and methanol coupled aromatics production reactor is divided into at least two interconnected zones from top to bottom: a first gas-solid separation zone and a naphtha and methanol coupled aromatics production reaction zone. The naphtha and methanol coupled aromatics production reaction zone is equipped with a naphtha and methanol coupled aromatics production reactor distributor, which includes n sub-distributors. The sub-distributors are numbered from 1 to n from bottom to top, where n ≥ 2. The first sub-distributor is used to introduce naphtha feedstock, and the second to nth sub-distributors are used to introduce methanol feedstock. The catalyst inlet of the naphtha and methanol coupled aromatics production reaction zone is located between the first and second sub-distributors. The light hydrocarbon aromatization reactor is divided into at least two interconnected zones from top to bottom: a second gas-solid separation zone and a light hydrocarbon aromatization reaction zone, forming a bed reactor. The second gas-solid separation zone is equipped with a gas-solid separation device II and a gas collection chamber II. The gas outlet of the gas-solid separation device II is connected to the gas collection chamber II. The lower part of the light hydrocarbon aromatization reaction zone is equipped with a bed reactor distributor for introducing feedstock into the bed reactor. The feedstock includes C4 and C5 hydrocarbons. In addition to the bed reactor, the light hydrocarbon aromatization reactor also includes a riser reactor, the outlet of which extends into the lower part of the light hydrocarbon aromatization reaction zone, and the catalyst outlet of the gas-solid separation device II is located above it. The apparatus also includes a regenerator, at least one inlet of the light hydrocarbon aromatization reactor is connected to the regenerator for obtaining the high-temperature regenerated catalyst generated by the regenerator; the inlet end of the riser reactor of the light hydrocarbon aromatization reactor is connected to the regenerator. The gas collecting chamber II is located at the inner top of the bed reactor; The inlet end of the riser reactor is also used to introduce catalyst and feedstock for the riser reactor; the feedstock for the riser reactor includes water vapor and low-carbon alkanes separated from the product gas stream; The second gas-solid separation zone is connected to the first gas-solid separation zone, and the light hydrocarbon aromatization reaction zone is connected to the naphtha and methanol coupled aromatics production reaction zone; The gas collection chamber II is connected to the first gas-solid separation zone via the product gas delivery pipe II.

2. The naphtha and methanol coupled aromatics production apparatus according to claim 1, characterized in that, n≤10； The first gas-solid separation zone is equipped with a gas-solid separation device I and a gas collection chamber I; the gas outlet of the gas-solid separation device I is connected to the gas collection chamber I; the outlet of the gas collection chamber I is connected to the product gas conveying pipe I, and the product gas conveying pipe I is used to output the product gas containing BTX after gas-solid separation to the downstream section.

3. The naphtha and methanol coupled aromatics production apparatus according to claim 2, characterized in that, The gas collecting chamber I is located at the inner top of the shell of the naphtha and methanol coupled aromatics production reactor; The gas-solid separation device I employs one or more sets of gas-solid cyclone separators, each set of gas-solid cyclone separators including a first-stage gas-solid cyclone separator and a second-stage gas-solid cyclone separator.

4. The naphtha and methanol coupled aromatics production apparatus according to claim 1, characterized in that, A light hydrocarbon aromatization slide valve is installed on the pipeline connecting the naphtha and methanol coupled aromatics production reaction zone and the light hydrocarbon aromatization reaction zone. The outlet position of the light hydrocarbon aromatization reaction zone is higher than the inlet position of the naphtha and methanol coupled aromatics production reaction zone; The gas-solid separation device II is a gas-solid cyclone separator.

5. The naphtha and methanol coupled aromatics production apparatus according to claim 1, characterized in that, The regenerator is divided into at least two interconnected sections from top to bottom: a third gas-solid separation zone and a regeneration zone. The third gas-solid separation zone is equipped with a regenerator gas-solid separation device and a regenerator gas collection chamber. The gas outlet of the regenerator gas-solid separation device is connected to the regenerator gas collection chamber. A flue gas conveying pipe is provided on the regenerator gas collection chamber. A regenerator distributor is provided in the lower part of the regeneration zone for introducing regeneration gas. The regeneration zone is connected to the riser reactor in sequence via a regenerator stripper and a regeneration slide valve; the inlet pipe of the regenerator stripper extends into the shell of the regenerator and is located above the regenerator distributor; the catalyst outlet end of the regenerator gas-solid separation device is located above the opening end of the inlet pipe of the regenerator stripper.

6. The naphtha and methanol coupled aromatics production apparatus according to claim 5, characterized in that, The regenerator gas collection chamber is located at the inner top of the regenerator housing; The regenerator gas-solid separation equipment uses one or more sets of gas-solid cyclone separators, each set of gas-solid cyclone separators includes a first-stage gas-solid cyclone separator and a second-stage gas-solid cyclone separator.

7. The naphtha and methanol coupled aromatics production apparatus according to claim 2, characterized in that, At least one outlet of the naphtha and methanol coupled aromatics production reactor is also connected to the inlet of a regenerator, for introducing the spent catalyst produced by the reaction in the naphtha and methanol coupled aromatics production reactor into the regenerator, which is used to introduce regeneration gas to convert the spent catalyst into a regenerated catalyst.

8. The naphtha and methanol coupled aromatics production apparatus according to claim 7, characterized in that, The naphtha and methanol coupled aromatics production reaction zone is connected to the inlet of the regenerator via a reactor stripper, a pre-generation slide valve, and a pre-generation agent delivery pipe in sequence; the inlet pipe of the reactor stripper extends into the shell of the naphtha and methanol coupled aromatics production reactor and is located above the first sub-distributor; the outlet end of the gas-solid separation device I is located above the opening end of the inlet pipe of the reactor stripper. The inlet of the regenerator is located in the regeneration zone and is disposed on the housing of the regenerator.

9. A method for producing aromatics by coupling naphtha and methanol, characterized in that, The method includes: preparing aromatics using the naphtha and methanol coupled aromatics production apparatus and catalyst as described in any one of claims 1-8.

10. The method for producing aromatics by coupling naphtha and methanol according to claim 9, characterized in that, The catalyst is a bifunctional metal molecular sieve catalyst. The bifunctional metal molecular sieve catalyst uses metal-modified HZSM-5 zeolite molecular sieve. The metal used for metal modification is selected from at least one of La, Zn, Ga, Fe, Mo, and Cr; The method of metal modification includes: placing HZSM-5 zeolite molecular sieve in a metal salt solution, impregnating, drying, and calcining to obtain the metal-modified HZSM-5 zeolite molecular sieve.

11. The method for producing aromatics by coupling naphtha and methanol according to claim 9, characterized in that, The method includes: A light hydrocarbon aromatization reactor is fed with raw materials and a high-temperature catalyst to generate light hydrocarbon aromatization product gas. A naphtha and methanol coupled aromatics production reactor is fed with naphtha and a catalyst from the light hydrocarbon aromatization reactor to generate a product gas stream containing BTX. A naphtha and methanol coupled aromatics production reactor is introduced with methanol, which undergoes a methylation reaction with benzene and toluene in the product gas stream containing BTX to produce p-xylene.

12. The method for producing aromatics by coupling naphtha and methanol according to claim 11, characterized in that, All gaseous streams generated in the naphtha and methanol coupled aromatics reactor are desorbed by gas-solid separation equipment I to remove the entrained catalyst, enter gas collection chamber I, and then enter the downstream section through product gas delivery pipe I.

13. The method for producing aromatics by coupling naphtha and methanol according to claim 12, characterized in that, The components of the light hydrocarbon aromatization product gas include: BTX, low-carbon olefins and H2; In addition to BTX, the product gas stream containing BTX also includes: low-carbon olefins, hydrogen, low-carbon alkanes, combustible gases, heavy aromatics, and unconverted naphtha. The low-carbon olefins refer to ethylene and propylene; The low-carbon alkanes refer to ethane and propane; The combustible gas includes methane and CO; The heavy aromatic hydrocarbons refer to aromatic hydrocarbons with 9 or more carbon atoms in their molecules.

14. The method for producing aromatics by coupling naphtha and methanol according to claim 13, characterized in that, The naphtha is selected from at least one of direct coal liquefaction naphtha, indirect coal liquefaction naphtha, straight-run naphtha and hydrocracked naphtha. The naphtha also includes unconverted naphtha separated from the product gas stream, the main components of which are C4-C12 straight-chain and branched aliphatic hydrocarbons and cycloalkanes.

15. The method for producing aromatics by coupling naphtha and methanol according to claim 14, characterized in that, The carbon content in the catalyst is 1.0-3.0 wt%; The process conditions in the naphtha and methanol coupled aromatics production reactor are as follows: apparent gas linear velocity of 0.5-2.0 m / s, reaction temperature of 500-600℃, reaction pressure of 100-500 kPa, and bed density of 150-700 kg / m3.

16. The method for producing aromatics by coupling naphtha and methanol according to claim 15, characterized in that... The light hydrocarbon aromatization product gas enters the gas-solid separation equipment II to remove the entrained catalyst, and then enters the gas collection chamber II. It then enters the first gas-solid separation zone of the naphtha and methanol coupled aromatics reactor through the product gas delivery pipe II. The catalyst in the light hydrocarbon aromatization reaction zone enters the naphtha and methanol coupled aromatics production reactor through the light hydrocarbon aromatization slide valve. The process conditions for the light hydrocarbon aromatization reaction zone are as follows: apparent gas linear velocity of 0.5-2.0 m / s, reaction temperature of 550-665℃, reaction pressure of 100-500 kPa, and bed density of 150-700 kg / m3.

17. The method for producing aromatics by coupling naphtha and methanol according to any one of claims 11-16, characterized in that, The method also includes introducing regeneration gas and a catalyst to be generated into the regenerator to obtain a high-temperature regenerated catalyst, which is then transported to the light hydrocarbon aromatization reactor.

18. The method for producing aromatics by coupling naphtha and methanol according to claim 17, characterized in that, The regenerated gas is introduced into the regeneration zone of the regenerator via the regenerator distributor; The regenerated gas is selected from at least one of oxygen, air, and oxygen-enriched air; The carbon content in the catalyst is 1.0-3.0 wt%; The carbon content in the regenerated catalyst is ≤0.5wt%; The process conditions in the regeneration zone of the regenerator are as follows: apparent gas linear velocity of 0.5-2.0 m / s, regeneration temperature of 600-750℃, regeneration pressure of 100-500 kPa, and bed density of 150-700 kg / m3.

19. The method for producing aromatics by coupling naphtha and methanol according to claim 18, characterized in that, The coke on the catalyst reacts with the regeneration gas to generate flue gas, which enters the third gas-solid separation zone to remove the regeneration catalyst carried therein. The flue gas enters the third gas-solid separation zone to remove the entrained regeneration catalyst. Specifically, the flue gas first enters the regenerator gas-solid separation equipment to remove the entrained regeneration catalyst, and then enters the downstream section through the regenerator gas collection chamber and the flue gas conveying pipe. The regenerated catalyst enters the light hydrocarbon aromatization reactor through the regenerator stripper and the regenerated slide valve.

20. The method for producing aromatics by coupling naphtha and methanol according to claim 19, characterized in that, The method further includes: introducing feedstock into the riser reactor at the inlet end of the riser reactor of the light hydrocarbon aromatization reactor; the regenerated catalyst is introduced into the riser reactor via the regenerator stripper and the regenerated slide valve, and the feedstock in the riser reactor is converted into a stream containing BTX under the action of the regenerated catalyst, which enters the lower part of the light hydrocarbon aromatization reaction zone in the bed reactor through the outlet end of the riser reactor. The method further includes: introducing a catalyst into the inlet end of the riser reactor of the light hydrocarbon aromatization reactor, and then introducing the catalyst into the bed reactor through the riser reactor; The feedstock for the riser reactor includes steam and low-carbon alkanes separated from the product gas stream.

21. The method for producing aromatics by coupling naphtha and methanol according to claim 20, characterized in that, The water vapor content in the feedstock of the riser reactor is 0-80 wt%. The process conditions of the riser reactor are: apparent gas linear velocity of 3.0-10.0 m / s, temperature of 580-700℃, pressure of 100-500 kPa, and bed density of 50-150 kg / m3. The feedstock of the bed reactor is introduced into the light hydrocarbon aromatization reaction zone through the bed reactor distributor, and comes into contact with the catalyst from the riser reactor to generate light hydrocarbon aromatization product gas. The feedstock for the bed reactor includes C4 and C5 hydrocarbons; The C4 and C5 hydrocarbons are derived from C4 and C5 hydrocarbons separated from the product gas stream; The components of the BTX-containing stream include: BTX, low-carbon olefins, and H2.

22. The method for producing aromatics by coupling naphtha and methanol according to any one of claims 11-16, characterized in that, The method also includes: The catalyst in the naphtha and methanol coupled aromatics production reaction zone is fed into the reactor stripper, and after stripping, it enters the downstream area through the catalyst slide valve and the catalyst delivery pipe.

23. The method for producing aromatics by coupling naphtha and methanol according to claim 22, characterized in that, The downstream region is the regenerator.

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