Apparatus and method for preparing aromatic hydrocarbons by coupling naphtha and methanol

Abstract

The present application discloses an apparatus and a method for preparing aromatic hydrocarbons by coupling naphtha and methanol. By adopting the said apparatus, under the action of a catalyst, naphtha and methanol react to produce a product gas mainly composed of aromatic hydrocarbons and light olefins. By the method of the present application, linear aliphatic hydrocarbons and branched aliphatic hydrocarbons can be efficiently and highly selectively converted into aromatic hydrocarbons, the yield of p-xylene is also improved through the methylation reaction of aromatic hydrocarbons, and the content of p-xylene in the xylene mixture is over 75 wt%. By the naphtha-methanol coupling aromatic hydrocarbon preparation reactor in the present application, by controlling the process of the cascade reaction (naphtha → benzene and toluene → p-xylene), the yield of p-xylene is improved. Furthermore, through the methylation reaction of benzene, toluene and methanol, heat is supplied at that position for the naphtha-methanol coupling aromatic hydrocarbon preparation reaction, and as a result, a self-heating balance is achieved.

Description

Detailed Description of the Invention

[0001] 〔Technical Field〕 The present application relates to a fluidized bed apparatus and a method for using the apparatus, and belongs to the technical field of the chemical industry. The present application particularly relates to an apparatus and a method for preparing aromatic hydrocarbons by coupling naphtha and methanol.

[0002] 〔Background〕 Aromatic hydrocarbons (benzene, toluene, and xylene (collectively referred to as BTX)) are important organic chemical raw materials. p-Xylene (PX) is the most concerned product among aromatic hydrocarbons. p-Xylene (PX) is mainly used in the production of polyesters such as terephthalic acid (PTA), polyethylene terephthalate (PET), polybutylene terephthalate (PBT), and polytrimethylene terephthalate (PTT). In recent years, the production and consumption of p-xylene in China have been on the rise. In 2021, the total import volume of PX in China was approximately 13.65 million tons, and the foreign trade dependence was approximately 38%.

[0003] The catalytic reforming technology of naphtha is the main technical route for producing aromatic hydrocarbons. The composition of naphtha is very complex. Naphtha is not only the main raw material for catalytic reforming, but also the main raw material for ethylene production by cracking. The composition of naphtha plays an important role in the economic benefits of the device. Generally speaking, a high potential content of raw material aromatic hydrocarbons and a medium distillation range are advantageous for catalytic reforming. On the other hand, a high content of linear-chain aliphatic hydrocarbons and branched-chain aliphatic hydrocarbons and a low content of naphthenic hydrocarbons and aromatic hydrocarbons are suitable for ethylene production by cracking. Usually, in order to make full use of naphtha resources and improve economic benefits, it is necessary to first separate the linear-chain aliphatic hydrocarbons and branched-chain aliphatic hydrocarbons in naphtha from naphthenic hydrocarbons and aromatic hydrocarbons. The former is used as the raw material for ethylene production, and the latter is used as the raw material for the catalytic reforming device.

[0004] The distillation range of naphtha fractions is wide. With common separation methods, it is difficult to efficiently separate linear-chain aliphatic hydrocarbons and branched-chain aliphatic hydrocarbons from naphthenic hydrocarbons and aromatic hydrocarbons. In addition, it is also difficult to convert linear-chain aliphatic hydrocarbons and branched-chain aliphatic hydrocarbons into aromatic hydrocarbons by catalytic reforming technology. Generally, the naphtha raw material used for catalytic reforming needs to be distilled to separate the topped oil with a boiling point below 60°C in order to increase the potential content of raw material aromatic hydrocarbons for catalytic reforming. However, the fraction with a boiling point exceeding 60°C still contains a lot of linear-chain aliphatic hydrocarbons and branched-chain aliphatic hydrocarbons that are difficult to be converted into aromatic hydrocarbons. Therefore, the highly selective conversion of linear-chain aliphatic hydrocarbons and branched-chain aliphatic hydrocarbons into aromatic hydrocarbons has always been a hot and difficult point in the development of technologies for preparing aromatic hydrocarbons from naphtha.

[0005] Due to the constraints of thermodynamic equilibrium, p-xylene in the xylene mixture produced by a naphtha catalytic reforming unit only accounts for ~24%, and it is necessary to further increase the yield of p-xylene through isomerization separation technology. Therefore, increasing the content of p-xylene in the xylene mixture is an important method for reducing the energy consumption for the production of p-xylene.

[0006] 〔Overview〕 The naphtha molecules contain only a small amount of methyl groups (methyl group / benzene ring = ~1.3 (molar ratio)). Due to the molecular structure of naphtha molecules, it is determined that a large amount of benzene will inevitably be by-produced in the catalytic reforming / aromatic compound complex unit.

[0007] The aromatization of methanol is a new process for preparing aromatic hydrocarbons. In methanol molecules, there are excessive hydrogen atoms compared with aromatic hydrocarbons. Therefore, in the preparation of aromatic hydrocarbons using methanol, a large amount of alkanes and a large amount of hydrogen will inevitably be by-produced. According to the molecular structure and reaction mechanism, methanol can bring about methyl groups for aromatic hydrocarbons. This increases the yields of toluene and xylene. Thus, a new technical route for preparing aromatic hydrocarbons by coupling naphtha and methanol is brought about.

[0008] In one aspect of the present application, an apparatus capable of preparing aromatic hydrocarbons using naphtha and methanol as raw materials is provided. By this apparatus, the content of p-xylene in the mixed xylene increases, and the energy consumption for separation is reduced.

[0009] The components of naphtha in the present application include C 4 -C 12 linear aliphatic hydrocarbons and branched aliphatic hydrocarbons, naphthenic hydrocarbons, as well as aromatic hydrocarbons.

[0010] The aromatic hydrocarbons in the present application refer to benzene, toluene, and xylene. These are collectively referred to as BTX.

[0011] An apparatus for preparing aromatic hydrocarbons by coupling naphtha and methanol includes a light hydrocarbon aromatization reactor and a naphtha-methanol coupling aromatic hydrocarbon preparation reactor. The light hydrocarbon aromatization reactor is used to introduce raw materials and a high-temperature catalyst, and at least one outlet of the light hydrocarbon aromatization reactor is connected to the naphtha-methanol coupling aromatic hydrocarbon preparation reactor for transporting the catalyst and the generated light hydrocarbon aromatization product gas to the naphtha-methanol coupling aromatic hydrocarbon preparation reactor. The naphtha-methanol coupling aromatic hydrocarbon preparation reactor is used to introduce naphtha and methanol, contact the naphtha with the catalyst from the light hydrocarbon aromatization reactor, and generate a BTX-containing product gas stream after the reaction. The methanol is also used for a methylation reaction with benzene and toluene in the product gas stream to generate p-xylene.

[0012] When the catalyst enters the naphtha-methanol coupling aromatic hydrocarbon preparation reactor, the temperature of the catalyst decreases to a certain extent, and at the same time, the catalyst contacts the naphtha. As a result, a local high-temperature zone in the naphtha-methanol coupling aromatic hydrocarbon preparation reactor can disappear. Consequently, the yield of low-carbon alkanes can be effectively reduced, and the yield of aromatic hydrocarbons increases.

[0013] Preferably, the naphtha-methanol coupling aromatic hydrocarbon preparation reactor is at least divided into a first gas-solid separation zone and a naphtha-methanol coupling aromatic hydrocarbon preparation reaction zone from top to bottom. The two zones communicate with each other. In the naphtha-methanol coupling aromatic hydrocarbon preparation reaction zone, a naphtha-methanol coupling aromatic hydrocarbon preparation reactor disperser is provided. The naphtha-methanol coupling aromatic hydrocarbon preparation reactor disperser includes n sub-dispersers. The serial numbers of the plurality of sub-dispersers are 1 to n (n≥2) in order from bottom to top. The first sub-disperser is used to introduce the naphtha raw material, and from the second sub-disperser to the nth sub-disperser are used to introduce the methanol raw material.

[0014] Preferably, n≤10.

[0015] Preferably, a gas-solid separation device I and a gas collection chamber I are provided in the first gas-solid separation zone. The gas outlet of the gas-solid separation device I communicates with the gas collection chamber I. The outlet of the gas collection chamber I communicates with a product gas transfer pipe I. The product gas transfer pipe I is used to let the BTX-containing product gas flow after gas-solid separation flow out (output) to a downstream processing section.

[0016] Preferably, the gas collection chamber I is located on the inner top of the naphtha-methanol coupling aromatic hydrocarbon preparation reactor shell.

[0017] Preferably, the gas-solid separation device I is one or a plurality of groups of a plurality of gas-solid cyclone separators. Each group of the plurality of gas-solid cyclone separators includes a first-stage gas-solid cyclone separator and a second-stage gas-solid cyclone separator.

[0018] Preferably, the light hydrocarbon aromatization reactor is at least divided into a second gas-solid separation zone and a light hydrocarbon aromatization reaction zone from top to bottom, a bed reactor is formed, the two zones are in communication, a gas-solid separator II and a gas collection chamber II are provided in the second gas-solid separation zone, a gas outlet of the gas-solid separator II communicates with the gas collection chamber II, and a bed reactor disperser for introducing bed reactor raw materials is provided on the inner lower part of the light hydrocarbon aromatization reaction zone.

[0019] Preferably, the gas collection chamber II is provided on the inner top of the bed reactor.

[0020] Furthermore, the bed reactor raw materials include C 4 hydrocarbons and C 5 hydrocarbons. The C 4 hydrocarbons and the C 5 hydrocarbons refer to hydrocarbons having 4 carbon atoms and hydrocarbons having 5 carbon atoms.

[0021] Preferably, the bed reactor raw materials include C 3 hydrocarbons, C 4 hydrocarbons, and C 5 hydrocarbons. The C 3 hydrocarbons, the C 4 hydrocarbons, and the C 5 hydrocarbons refer to hydrocarbons having 3 carbon atoms, hydrocarbons having 4 carbon atoms, and hydrocarbons having 5 carbon atoms.

[0022] Preferably, in addition to the bed reactor, the light hydrocarbon aromatization reactor further includes a riser reactor, an outlet end of the riser reactor extends into the inner lower part of the light hydrocarbon aromatization reaction zone, and a catalyst outlet of the gas-solid separator II is disposed above the riser reactor.

[0023] Preferably, an inlet end of the riser reactor is used to introduce the catalyst and riser reactor raw materials.

[0024] Preferably, the second gas-solid separation zone communicates with the first gas-solid separation zone, and the light hydrocarbon aromatization reaction zone communicates with the naphtha-methanol coupling aromatic hydrocarbon preparation reaction zone.

[0025] Preferably, the gas collection chamber II communicates with the first gas-solid separation zone through the product gas transfer pipe II.

[0026] Preferably, a light hydrocarbon aromatization slide valve is provided on the pipeline connecting the naphtha-methanol coupling aromatic hydrocarbon preparation reaction zone and the light hydrocarbon aromatization reaction zone.

[0027] Preferably, the position of the outlet of the light hydrocarbon aromatization reaction zone is higher than the position of the inlet of the naphtha-methanol coupling aromatic hydrocarbon preparation reaction zone.

[0028] Preferably, the position of the catalyst inlet of the naphtha-methanol coupling aromatic hydrocarbon preparation reaction zone is located between the first sub-disperser and the second sub-disperser.

[0029] Preferably, the gas-solid separation device II is a gas-solid cyclone separator.

[0030] Preferably, the device further includes a regenerator, and at least one inlet of the light hydrocarbon aromatization reactor is connected to the regenerator to obtain the high-temperature regenerated catalyst generated by the regenerator.

[0031] Preferably, the inlet end of the riser reactor of the light hydrocarbon aromatization reactor communicates with the regenerator.

[0032] Preferably, the regenerator is at least divided into a third gas-solid separation zone and a regeneration zone from top to bottom, and the two zones communicate with each other. In the third gas-solid separation zone, a regenerator gas-solid separator and a regenerator gas collection chamber are provided. The gas outlet of the regenerator gas-solid separator communicates with the regenerator gas collection chamber. An exhaust gas transfer pipe is provided on the regenerator gas collection chamber. A regenerator disperser for introducing regenerated gas is provided on the inner lower part of the regeneration zone.

[0033] Preferably, the regeneration zone is connected to the riser reactor through a regenerator stripper and a regeneration slide valve in sequence. The inlet pipe of the regenerator stripper extends into the regenerator shell and is located above the regenerator disperser. The catalyst outlet end of the regenerator gas-solid separator is located above the opening end of the inlet pipe of the regenerator stripper.

[0034] Preferably, the regenerator gas collection chamber is located on the inner top of the regenerator shell.

[0035] Preferably, the regenerator gas-solid separator is one or a plurality of groups of a plurality of gas-solid cyclone separators. Each group of the plurality of gas-solid cyclone separators includes a first-stage gas-solid cyclone separator and a second-stage gas-solid cyclone separator.

[0036] Preferably, at least one outlet of the naphtha-methanol coupling aromatic hydrocarbon preparation reactor is connected to the inlet of the regenerator to introduce the spent catalyst generated by the reaction of the naphtha-methanol coupling aromatic hydrocarbon preparation reactor into the regenerator. The regenerator is used to introduce regenerated gas to convert the spent catalyst into a regenerated catalyst.

[0037] Preferably, the naphtha-methanol coupling aromatic hydrocarbon preparation reaction zone is connected to the inlet of the regenerator through a reactor stripper, a used slide valve, and a used agent transfer pipe in sequence. The inlet pipe of the reactor stripper extends into the naphtha-methanol coupling aromatic hydrocarbon preparation reactor shell and is located above the first disperser. The catalyst outlet end of the reactor gas-solid separation device is located above the open end of the inlet pipe of the reactor stripper.

[0038] Preferably, the inlet of the regenerator is located in the regeneration zone and provided on the regenerator shell.

[0039] In another aspect of the present application, a method for preparing aromatic hydrocarbons by coupling naphtha and methanol is provided. The method includes a step of preparing aromatic hydrocarbons by using an apparatus and a catalyst for preparing aromatic hydrocarbons by coupling the above-mentioned naphtha and methanol.

[0040] Preferably, the catalyst is a metal molecular sieve bifunctional catalyst. Preferably, the metal molecular sieve bifunctional catalyst is a metal modified HZSM-5 zeolite molecular sieve. The metal for the metal modification is selected from at least one of La, Zn, Ga, Fe, Mo, and Cr. The method for the metal modification includes a step of putting the HZSM-5 zeolite molecular sieve into a metal salt solution, immersing it, drying it, and roasting it to obtain the metal modified HZSM-5 zeolite molecular sieve.

[0041] Furthermore, the method includes introducing the raw material and the high-temperature catalyst into the light hydrocarbon aromatization reactor to produce the light hydrocarbon aromatization product gas; introducing the naphtha and the catalyst from the light hydrocarbon aromatization reactor into the naphtha-methanol coupling aromatic hydrocarbon preparation reactor to produce a BTX-containing product gas stream; and introducing the methanol into the naphtha-methanol coupling aromatic hydrocarbon preparation reactor to subject it to a methylation reaction with benzene and toluene in the BTX-containing product gas stream to produce p-xylene.

[0042] Preferably, the spent catalyst contained in all the gas streams generated in the naphtha-methanol coupling aromatic hydrocarbon preparation reactor is removed through the gas-solid separation device I, the gas stream enters the gas collection chamber I, and then enters the downstream processing section through the product gas transport pipe I.

[0043] Preferably, the components of the light hydrocarbon aromatization product gas include BTX, low-carbon olefins, and H 2 is included.

[0044] Preferably, in addition to the BTX, the BTX-containing product gas stream further includes low-carbon olefins, hydrogen, low-carbon alkanes, combustible gas, heavy aromatic hydrocarbons, and unconverted naphtha.

[0045] Preferably, 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, and the heavy aromatic hydrocarbons refer to aromatic hydrocarbons having 9 or more carbon atoms in the molecule.

[0046] Preferably, the naphtha is selected from at least one of direct coal liquefaction naphtha, indirect coal liquefaction naphtha, straight-run naphtha, and hydrocracked naphtha.

[0047] Preferably, the naphtha also contains unconverted naphtha separated from the product gas stream, and the unconverted naphtha contains straight-chain aliphatic hydrocarbons and branched-chain aliphatic hydrocarbons of C 4 -C 12 and mainly contains naphthenic hydrocarbons as the main components.

[0048] Preferably, the carbon content in the used catalyst is 1.0 wt% to 3.0 wt%.

[0049] Preferably, the process conditions of the naphtha-methanol coupling aromatic hydrocarbon preparation reaction zone are a superficial linear velocity of the gas of 0.5 m / s to 2.0 m / s, a reaction temperature of 500 °C to 600 °C, a reaction pressure of 100 kPa to 500 kPa, and a bed density of 150 kg / m 3 ~700 kg / m 3 is.

[0050] Optionally, the superficial linear velocity of the gas in the naphtha-methanol coupling aromatic hydrocarbon preparation reaction zone is independently selected from any value among 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 value within the range between any two values.

[0051] Optionally, the reaction temperature in the naphtha-methanol coupling aromatic hydrocarbon preparation reaction zone is independently selected from any value among 500 °C, 520 °C, 530 °C, 540 °C, 550 °C, 560 °C, 570 °C, 580 °C, 590 °C, and 600 °C or a value within the range between any two values.

[0052] Optionally, the reaction pressure in the naphtha-methanol coupling aromatic hydrocarbon preparation reaction zone is independently selected from any value among 100 kPa, 125 kPa, 150 kPa, 175 kPa, 200 kPa, 225 kPa, 250 kPa, 275 kPa, 300 kPa, 325 kPa, 350 kPa, 375 kPa, 400 kPa, 425 kPa, 450 kPa, 475 kPa, and 500 kPa, or a value within the range between any two of these values.

[0053] Optionally, the bed density in 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 、and 700 kg / m 3 and is independently selected from any value or a value within the range between any two of these values.

[0054] Preferably, the light hydrocarbon aromatization product gas enters the gas-solid separator II. After the catalyst contained in the light hydrocarbon aromatization product gas is removed, it enters the gas collection chamber II and then enters the first gas-solid separation zone of the naphtha-methanol coupling aromatic hydrocarbon preparation reactor through the product gas transfer pipe II. The catalyst in the light hydrocarbon aromatization reaction zone enters the naphtha-methanol coupling aromatic hydrocarbon preparation reactor through the light hydrocarbon aromatization slide valve.

[0055] Optionally, the process conditions in the light hydrocarbon aromatization reaction zone are a superficial linear velocity of the gas of 0.5 m / s to 2.0 m / s, a reaction temperature of 550 °C to 665 °C, a reaction pressure of 100 kPa to 500 kPa, and a bed density of 150 kg / m 3~700 kg / m 3 is as follows.

[0056] Optionally, the apparent linear velocity of the gas in the light hydrocarbon aromatization reaction zone is independently selected from any value among 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 value within the range between any two of these values.

[0057] Optionally, the reaction temperature in the light hydrocarbon aromatization reaction zone is independently selected from any value among 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 a value within the range between any two of these values.

[0058] Optionally, the reaction pressure is independently selected from any value among 100 kPa, 125 kPa, 150 kPa, 175 kPa, 200 kPa, 225 kPa, 250 kPa, 275 kPa, 300 kPa, 325 kPa, 350 kPa, 375 kPa, 400 kPa, 425 kPa, 450 kPa, 475 kPa, and 500 kPa, or a value within the range between any two of these values.

[0059] Optionally, the bed density is 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 , and 700 kg / m 3 and is independently selected from any value or a value within the range between any two of these values.

[0060] Preferably, the method further includes a step of introducing a regeneration gas and a used catalyst into a regenerator to obtain a high-temperature regenerated catalyst, and a step of transporting the high-temperature regenerated catalyst to the light hydrocarbon aromatization reactor.

[0061] Preferably, the regeneration gas is introduced into the regeneration zone of the regenerator through a regenerator disperser.

[0062] Preferably, the regeneration gas is selected from at least one of oxygen, air, and oxygen-enriched air.

[0063] Preferably, the carbon content in the used catalyst is 1.0 wt% to 3.0 wt%.

[0064] Preferably, the carbon content in the regenerated catalyst is 0.5 wt% or less.

[0065] Preferably, the process conditions in the regeneration zone of the regenerator are as follows: the apparent linear velocity of the gas is 0.5 m / s to 2.0 m / s, the regeneration temperature is 600 °C to 750 °C, the regeneration pressure is 100 kPa to 500 kPa, and the bed density is 150 kg / m 3 ~700 kg / m 3 is.

[0066] Optionally, the apparent linear velocity of the gas is independently selected from any value among 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 value within the range between any two of these values.

[0067] Optionally, the regeneration temperature is independently selected from any value among 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 value within the range between any two of these values.

[0068] Optionally, the regeneration pressure is independently selected from any value among 100 kPa, 125 kPa, 150 kPa, 175 kPa, 200 kPa, 225 kPa, 250 kPa, 275 kPa, 300 kPa, 325 kPa, 350 kPa, 375 kPa, 400 kPa, 425 kPa, 450 kPa, 475 kPa, and 500 kPa or a value within the range between any two of these values.

[0069] Optionally, the bed density is 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 , and 700 kg / m 3 and is independently selected from any value or a value within the range between any two of these values.

[0070] Preferably, the coke on the used catalyst reacts with the regeneration gas to generate exhaust gas, and the exhaust gas enters a third gas-solid separation zone, where the regenerated catalyst contained in the exhaust gas is removed.

[0071] Preferably, the exhaust gas enters the third gas-solid separation zone, where the regenerated catalyst contained in the exhaust gas is removed. Specifically, this includes that the exhaust gas first enters a regenerator gas-solid separation device, and after the regenerated catalyst contained in the exhaust gas is removed, the exhaust gas passes through a regenerator gas collection chamber and an exhaust gas transfer pipe and enters a downstream processing section.

[0072] Preferably, the regenerated catalyst enters the light hydrocarbon aromatization reactor through a regenerator stripper and a regeneration slide valve.

[0073] Preferably, the method further includes: introducing a riser reactor raw material into an inlet end of the riser reactor of the light hydrocarbon aromatization reactor; introducing the regenerated catalyst into the riser reactor through a regenerator stripper and a regeneration slide valve; converting the riser reactor raw material into the BTX-containing stream under the action of the regenerated catalyst; and allowing the BTX-containing stream to enter an inner lower part of a light hydrocarbon aromatization reaction zone in a bed reactor through an outlet end of the riser reactor.

[0074] Preferably, the method further includes: introducing a catalyst into an inlet end of the riser reactor of the light hydrocarbon aromatization reactor; and allowing the catalyst to enter the bed reactor through the riser reactor.

[0075] Preferably, the riser reactor raw material includes steam and the lower-carbon alkane separated from the product gas stream.

[0076] Preferably, the steam content in the riser reactor raw material is 0 wt% to 80 wt%.

[0077] Preferably, the process conditions of the riser reactor are: an apparent linear velocity of the gas of 3.0 m / s to 10.0 m / s, a temperature of 580 °C to 700 °C, a pressure of 100 kPa to 500 kPa, and a bed density of 50 kg / m 3 ~150 kg / m 3 Thereby.

[0078] Optionally, the apparent linear velocity of the gas is independently selected from any value among 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 value within a range between any two of these values.

[0079] Optionally, the temperature is independently selected from any value or a value within a range between any two values among 580 °C, 590 °C, 600 °C, 610 °C, 620 °C, 630 °C, 640 °C, 650 °C, 660 °C, 670 °C, 680 °C, 690 °C, and 700 °C.

[0080] Optionally, the pressure is independently selected from any value or a value within a range between any two values among 100 kPa, 125 kPa, 150 kPa, 175 kPa, 200 kPa, 225 kPa, 250 kPa, 275 kPa, 300 kPa, 325 kPa, 350 kPa, 375 kPa, 400 kPa, 425 kPa, 450 kPa, 475 kPa, and 500 kPa.

[0081] Optionally, the bed density is independently selected from any value or a value within a range between any two values among 50 kg / m3, 60 kg / m 3 , 70 kg / m 3 , 80 kg / m 3 , 90 kg / m 3 , 100 kg / m 3 , 110 kg / m 3 , 120 kg / m 3 , 130 kg / m 3 , 140 kg / m 3 , and 150 kg / m 3 of any value or a value within a range between any two values.

[0082] Preferably, the method further includes introducing a fluidized bed reactor feedstock into the light hydrocarbon aromatization reaction zone through a fluidized bed reactor disperser and contacting it with the catalyst from the riser reactor to produce the light hydrocarbon aromatization product gas.

[0083] Optionally, the fluidized bed reactor feedstock includes C 4 hydrocarbons and C 5 hydrocarbons. The C 4 hydrocarbons and the C 5 hydrocarbons are derived from C 4 hydrocarbons and C 5 hydrocarbons separated from the product gas stream.

[0084] Preferably, the bed reactor feedstock is C 3 hydrocarbons, C 4 hydrocarbons, and C 5 hydrocarbons. The C 3 hydrocarbons, the C 4 hydrocarbons, and the C 5 hydrocarbons are separated from the product gas stream and are C 3 hydrocarbons, C 4 hydrocarbons, and C 5 hydrocarbons.

[0085] Preferably, the components of the BTX-containing stream include BTX, light olefins, and H 2 .

[0086] Preferably, the method further includes introducing the spent catalyst in the naphtha-methanol coupling aromatic hydrocarbon preparation reaction zone into the reactor stripper, and enabling the spent catalyst to enter the downstream area through the spent slide valve and the spent agent transfer pipe after stripping. Preferably, the downstream area is a regenerator.

[0087] In this application, the potential content of aromatic hydrocarbons in the naphtha feedstock is 0 wt% to 80 wt%, and the per-pass conversion rate of the naphtha is 60 wt% to 80 wt%. By using the apparatus for preparing aromatic hydrocarbons by coupling naphtha and methanol according to this application, and the method for preparing aromatic hydrocarbons by coupling naphtha and methanol based on the apparatus, the unconverted naphtha, after being separated from the product gas, returns as a feedstock to the naphtha-methanol coupling aromatic hydrocarbon preparation reactor, and a part of the lower alkanes, after being separated from the product gas, returns as a feedstock to the riser reactor in the light hydrocarbon aromatization reactor, C 3 hydrocarbons, C 4 hydrocarbons, and C 5After being separated from the product gas, the hydrocarbon returns as a raw material to the bed reactor in the light hydrocarbon aromatization reactor. The composition of the finally obtained product is as follows: BTX 60 wt% - 73 wt%, lower olefins 9 wt% - 16 wt%, hydrogen 3 wt% - 6 wt%, lower alkanes 3 wt% - 8 wt%, combustible gas 4 wt% - 6 wt%, heavy aromatic hydrocarbons 4 wt% - 8 wt%, and coke 0.5 wt% - 1 wt%. The content of p-xylene in the mixed xylene in the product is 60 wt% - 75 wt%.

[0088] According to the present application, the following beneficial effects can be achieved.

[0089] 1) According to the present application, linear aliphatic hydrocarbons and branched aliphatic hydrocarbons can be efficiently converted into aromatic hydrocarbons with high selectivity. The raw materials have a wide range of adaptability, and aromatic hydrocarbons can be prepared from naphtha with a low potential content of aromatic hydrocarbons.

[0090] 2) According to the present application, the aromatization of lower alkanes and C 4 hydrocarbons and C 5 hydrocarbons is achieved by the light hydrocarbon aromatization reactor and the metal molecular sieve dual-functional catalyst. As a result, the yield (recovery rate) of aromatic hydrocarbons in the technology for preparing aromatic hydrocarbons using naphtha is significantly improved.

[0091] 3) According to the present application, an apparatus for preparing aromatic hydrocarbons by coupling naphtha and methanol is provided with a naphtha-methanol coupling aromatic hydrocarbon preparation reactor. The naphtha-methanol coupling aromatic hydrocarbon preparation reactor includes a plurality of sub-dispersers. Naphtha enters the naphtha-methanol coupling aromatic hydrocarbon preparation reaction zone through a first sub-disperser, and methanol enters the naphtha-methanol coupling aromatic hydrocarbon preparation reaction zone through each of the second sub-disperser to the nth sub-disperser. The naphtha-methanol coupling aromatic hydrocarbon preparation reactor is a fluidized bed reactor suitable for cascade reaction. Naphtha is converted into benzene and toluene at the lower part of the naphtha-methanol coupling aromatic hydrocarbon preparation reaction zone, and then flows upward to reach the central and upper parts of the naphtha-methanol coupling aromatic hydrocarbon preparation reaction zone. Benzene and toluene are subjected to a methylation reaction with methanol to further produce p-xylene. As a result, the yield of p-xylene increases. The high-temperature catalyst from the light hydrocarbon aromatization reactor directly enters the lower part of the naphtha-methanol coupling aromatic hydrocarbon preparation reaction zone. This is advantageous for supplying the heat required for the reaction of converting naphtha into aromatic hydrocarbons and improving the conversion rate of naphtha. Methanol directly enters the central and upper parts of the naphtha-methanol coupling aromatic hydrocarbon preparation reaction zone. Thereby, the residence time of p-xylene in the reaction zone is effectively shortened, the isomerization reaction of p-xylene is suppressed, the content of p-xylene in xylene increases (up to 75 wt% at most under optimal technical conditions), and at the same time, the energy consumption for the separation of p-xylene is significantly reduced. In summary, in the naphtha-methanol coupling aromatic hydrocarbon preparation reactor, the naphtha raw material flows from bottom to top, and in the process of converting naphtha into aromatic hydrocarbons, the methylation raw material (methanol) is added step by step to control the process of cascade reaction (naphtha → benzene and toluene → p-xylene). As a result, the yield of p-xylene increases.

[0092] 4) The aromatization reaction of naphtha is a strong endothermic reaction. To convert 1 kg of naphtha into aromatic hydrocarbons, 1.1 MJ to 1.6 MJ of heat needs to be absorbed. The methylation reaction of methanol and aromatic hydrocarbons is a strong exothermic reaction. When converting 1 kg of methanol into methyl groups on aromatic hydrocarbons, more than 2.0 MJ of heat can be released. Therefore, by preparing p-xylene from benzene, toluene, and methanol, heat for the naphtha-methanol coupling aromatic hydrocarbon preparation reaction can be supplied in situ. As a result, self-heating balance is achieved.

[0093] 5) According to the present application, in an apparatus for preparing aromatic hydrocarbons by coupling naphtha and methanol, an independent light hydrocarbon aromatization reactor is provided. Lower alkanes are very stable and require a high reaction temperature. The temperature of the light hydrocarbon aromatization reactor is higher than that of the naphtha-methanol coupling aromatic hydrocarbon preparation reactor. Lower alkanes, as well as C 4 hydrocarbons and C 5 hydrocarbons are subjected to an aromatization reaction in an independent light hydrocarbon aromatization reactor. As a result, the reaction rate and the yield of aromatic hydrocarbons increase.

[0094] 〔Brief Description of the Drawings〕 FIG. 1 is a schematic diagram of an apparatus for preparing aromatic hydrocarbons by coupling naphtha and methanol according to an embodiment of the present application.

[0095] List of members and reference symbols: 1 refers to a naphtha-methanol coupling aromatic hydrocarbon preparation reactor; 1-1 refers to a naphtha-methanol coupling aromatic hydrocarbon preparation reactor shell; 1-2 refers to a naphtha-methanol coupling aromatic hydrocarbon preparation reactor disperser; 1-3 refers to gas-solid separator I, 1-4 refers to gas collection chamber I, and 1-5 refers to product gas transfer pipe I; 1-6 refers to the reactor stripper, 1-7 refers to the used slide valve, and 1-8 refers to the used agent transfer pipe; 1-2-1 refers to the first sub-disperser, 1-2-2 refers to the second sub-disperser, and 1-2-3 refers to the third sub-disperser; 2 refers to the regenerator; 2-1 refers to the regenerator shell, and 2-2 refers to the regenerator disperser; 2-3 refers to the regenerator gas-solid separator, 2-4 refers to the regenerator gas collection chamber, and 2-5 refers to the exhaust gas transfer pipe; 2-6 refers to the regenerator stripper, and 2-7 refers to the regeneration slide valve; 3 refers to the light hydrocarbon aromatization reactor; 3-1 refers to the inlet end of the riser reactor, and 3-2 refers to the central part of the riser reactor; 3-3 refers to the outlet end of the riser reactor, and 3-4 refers to the bed reactor shell; 3-5 refers to the bed reactor disperser, and 3-6 refers to the gas-solid separator II; 3-7 refers to the gas collection chamber II, 3-8 refers to the product gas transfer pipe II, and 3-9 refers to the light hydrocarbon aromatization slide valve.

[0096] 〔Detailed Description〕 Hereinafter, the present application will be described in detail with reference to the examples. However, the present application is not limited to these examples.

[0097] The present application provides an apparatus for preparing aromatic hydrocarbons by coupling naphtha and methanol. This apparatus includes a light hydrocarbon aromatization reactor, and a naphtha-methanol coupling aromatic hydrocarbon preparation reactor, and includes 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-methanol coupling aromatic hydrocarbon preparation reactor for transporting the catalyst and the produced light hydrocarbon aromatization product gas to the naphtha-methanol coupling aromatic hydrocarbon preparation reactor. The naphtha-methanol coupling aromatic hydrocarbon preparation reactor is used to introduce the naphtha and the methanol, bring the naphtha into contact with the catalyst from the light hydrocarbon aromatization reactor, and generate a BTX-containing product gas stream after the reaction. The methanol is also used for methylation reaction with benzene and toluene in the product gas stream to produce p-xylene.

[0098] The components of the naphtha in this application include C 4 -C 12 linear aliphatic hydrocarbons and branched aliphatic hydrocarbons, naphthenic hydrocarbons, and aromatic hydrocarbons.

[0099] BTX in this application is an aromatic hydrocarbon and refers to benzene, toluene, and xylene.

[0100] 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 to obtain the high-temperature regenerated catalyst generated by the regenerator.

[0101] Referring to FIG. 1, an apparatus for preparing aromatic hydrocarbons by coupling naphtha and methanol in a preferred embodiment of this application includes a naphtha-methanol coupling aromatic hydrocarbon preparation reactor 1, a regenerator 2, and a light hydrocarbon aromatization reactor 3.

[0102] The naphtha-methanol coupling aromatic hydrocarbon preparation reactor 1 includes a naphtha-methanol coupling aromatic hydrocarbon preparation reactor shell 1-1, a naphtha-methanol coupling aromatic hydrocarbon preparation reactor disperser 1-2, a gas-solid separation device I 1-3, a gas collection chamber I 1-4, a product gas transfer pipe I 1-5, a reactor stripper 1-6, a used slide valve 1-7, and a used agent transfer pipe 1-8.

[0103] The naphtha-methanol coupling aromatic hydrocarbon preparation reactor disperser 1-2 includes a first sub-disperser 1-2-1, a second sub-disperser 1-2-2, and a third sub-disperser 1-2-3.

[0104] The naphtha-methanol coupling aromatic hydrocarbon preparation reactor 1 includes a naphtha-methanol coupling aromatic hydrocarbon preparation reactor shell 1-1. The naphtha-methanol coupling aromatic hydrocarbon preparation reactor shell 1-1 includes a naphtha-methanol coupling aromatic hydrocarbon preparation reactor upper shell and a naphtha-methanol coupling aromatic hydrocarbon preparation reactor lower shell. The first gas-solid separation zone is surrounded by the naphtha-methanol coupling aromatic hydrocarbon preparation reactor upper shell, and the naphtha-methanol coupling aromatic hydrocarbon preparation reaction zone is surrounded by the naphtha-methanol coupling aromatic hydrocarbon preparation reactor lower shell. The outlet of the light hydrocarbon aromatization reactor 3 is provided on the naphtha-methanol coupling aromatic hydrocarbon preparation reactor shell 1-1.

[0105] The naphtha-methanol coupling aromatic hydrocarbon preparation reactor disperser 1-2 is provided in the naphtha-methanol coupling aromatic hydrocarbon preparation reaction zone. The naphtha-methanol coupling aromatic hydrocarbon preparation reactor disperser 1-2 includes three sub-dispersers, which are, from bottom to top, the first sub-disperser 1-2-1 to the third sub-disperser 1-2-3. The first sub-disperser 1-2-1 is used to introduce the naphtha raw material. The second sub-disperser 1-2-2 to the third sub-disperser 1-2-3 are used to introduce the methanol raw material.

[0106] In the naphtha-methanol coupling aromatic hydrocarbon preparation reactor shell 1-1, a gas-solid separator I 1-3 and a gas collection chamber I 1-4 are provided. The gas collection chamber I 1-4 is located on the inner top of the naphtha-methanol coupling aromatic hydrocarbon preparation reactor shell. The gas outlet of the gas-solid separator I 1-3 communicates with the gas collection chamber I 1-4. The gas collection chamber I 1-4 communicates with the product gas transfer pipe I 1-5. The catalyst outlet end of the gas-solid separator I 1-3 is located above the opening end of the inlet pipe of the reactor stripper 1-6.

[0107] The reactor stripper 1-6 is provided below the naphtha-methanol coupling aromatic hydrocarbon preparation reaction zone. The inlet of the reactor stripper 1-6 is located inside the naphtha-methanol coupling aromatic hydrocarbon preparation reactor shell 1-1. The outlet of the reactor stripper 1-6 is located outside the naphtha-methanol coupling aromatic hydrocarbon preparation reactor shell 1-1 and is connected to the used slide valve 1-7. The opening end of the inlet of the reactor stripper 1-6 is located above the first sub-disperser 1-2-1.

[0108] Below the reactor stripper 1-6, a used slide valve 1-7 is provided. 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 the used agent transfer pipe 1-8. The outlet of the used agent transfer pipe 1-8 is connected to the regenerator shell 2-1.

[0109] The used slide valve 1-7 is used to control the circulation amount of the used catalyst.

[0110] In a preferred embodiment, the gas-solid separator I 1-3 is one or a plurality of groups of a plurality of gas-solid cyclone separators, and each group of the plurality of gas-solid cyclone separators includes a first-stage gas-solid cyclone separator and a second-stage gas-solid cyclone separator.

[0111] The regenerator 2 includes a regenerator shell 2-1, a regenerator disperser 2-2, a regenerator gas-solid separator 2-3, a regenerator gas collection chamber 2-4, an exhaust gas transfer pipe 2-5, a regenerator stripper 2-6, and a regeneration slide valve 2-7.

[0112] The regenerator shell 2-1 includes an upper regenerator shell and a lower regenerator shell. The upper regenerator shell surrounds a third gas-solid separation zone, and the lower regenerator shell surrounds a regeneration zone. An outlet of the used agent transfer pipe 1-8 is provided in the regenerator shell 2-1.

[0113] A regenerator disperser 2-2 is provided above the lower part of the regeneration zone. The regenerator disperser 2-2 is used to introduce regeneration gas.

[0114] The regenerator shell 2-1 is also provided with a regenerator gas-solid separator 2-3 and a regenerator gas collection chamber 2-4. The regenerator gas collection chamber 2-4 is located on the inner top of the regenerator shell 2-1. The gas outlet of the regenerator gas-solid separator 2-3 communicates with the regenerator gas collection chamber 2-4. The regenerator gas collection chamber 2-4 communicates with the exhaust gas transfer pipe 2-5. The catalyst outlet end of the regenerator gas-solid separator 2-3 is located above the opening end of the inlet pipe of the regenerator stripper 2-6.

[0115] The regenerator stripper 2-6 is provided below the regeneration zone. The inlet of the regenerator stripper 2-6 is located inside the regenerator shell 2-1. The outlet of the regenerator stripper 2-6 is located outside the regenerator shell 2-1 and is connected to the regeneration slide valve 2-7. The opening end of the inlet of the regenerator stripper 2-6 is located above the regenerator disperser 2-2.

[0116] Below the regenerator stripper 2-6, a regeneration slide valve 2-7 is provided, and the inlet of the regeneration slide valve 2-7 is connected to the outlet of the regenerator stripper 2-6.

[0117] The regeneration slide valve 2-7 is used to control the circulation amount of the regenerated catalyst.

[0118] In a preferred embodiment, the regenerator gas-solid separator 2-3 is one or a plurality of groups of a plurality of gas-solid cyclone separators, and each group of the plurality of gas-solid cyclone separators includes a first-stage gas-solid cyclone separator and a second-stage gas-solid cyclone separator.

[0119] The light hydrocarbon aromatization reactor includes an inlet end 3-1 of the riser reactor, a central part 3-2 of the riser reactor, an outlet end 3-3 of the riser reactor, a bed reactor shell 3-4, a bed reactor disperser 3-5, a gas-solid separator II 3-6, a gas collection chamber II 3-7, a product gas transfer pipe II 3-8, and a light hydrocarbon aromatization slide valve 3-9.

[0120] The bed reactor shell 3-4 includes an upper shell of the bed reactor and a lower shell of the bed reactor. The upper shell of the bed reactor surrounds the second gas-solid separation zone, and the lower shell of the bed reactor surrounds the light hydrocarbon aromatization reaction zone. A bed reactor disperser 3-5 is provided on the inner lower part of the light hydrocarbon aromatization reaction zone, and a light hydrocarbon aromatization slide valve 3-9 is provided outside the light hydrocarbon aromatization reaction zone. The upper section of the riser reactor penetrates the bottom of the bed reactor and is axially inserted into the bed reactor. The outlet end 3-3 of the riser reactor is located on the inner lower part of the light hydrocarbon aromatization reaction zone.

[0121] The light hydrocarbon aromatization slide valve 3-9 is used to convey the catalyst to the next reactor, for example, to convey the catalyst to the naphtha-methanol coupling aromatic hydrocarbon preparation reactor 1.

[0122] In the second gas-solid separation zone, a gas-solid separator II 3-6 and a gas collection chamber II 3-7 are provided. The gas outlet of the gas-solid separator II 3-6 communicates with the gas collection chamber II 3-7. The catalyst outlet of the gas-solid separator II 3-6 is located within the light hydrocarbon aromatization reaction zone. The gas collection chamber II 3-7 communicates with a product gas transfer pipe II 3-8 located outside the bed reactor.

[0123] In a preferred embodiment, the gas-solid separator II 3-6 is a gas-solid cyclone separator.

[0124] In a preferred embodiment, a gas collection chamber II 3-7 is provided on 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.

[0125] In a preferred embodiment, the bed reactor disperser 3-5 is used to introduce the bed reactor raw material.

[0126] In a preferred embodiment, the inlet end 3-1 of the riser reactor is used to introduce the catalyst and the riser reactor raw material.

[0127] 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·methanol coupling aromatic hydrocarbon preparation reactor 1.

[0128] In a preferred embodiment, the inlet end 3-1 of the riser reactor is connected to the regeneration slide valve 2-7 through a pipeline. The light hydrocarbon aromatization slide valve 3-9 is connected to the shell 1-1 of the naphtha·methanol coupling aromatic hydrocarbon preparation reactor through a pipeline. It is located between the first sub-disperser 1-2-1 and the second sub-disperser 1-2-2.

[0129] In a preferred embodiment, the product gas transfer pipe II 3-8 is connected to the naphtha-methanol coupling aromatic hydrocarbon preparation reactor shell 1-1.

[0130] This application further provides a method for preparing aromatic hydrocarbons by coupling naphtha and methanol. This method includes the step of preparing aromatic hydrocarbons by using the above-mentioned apparatus and catalyst for preparing aromatic hydrocarbons by coupling naphtha and methanol.

[0131] The catalyst is a metal molecular sieve dual-functional catalyst. In Examples 1 to 5, a metal-modified HZSM-5 zeolite molecular sieve is used.

[0132] The metal for metal modification is selected from at least one of La, Zn, Ga, Fe, Mo, and Cr.

[0133] The method for metal modification includes the steps of putting the HZSM-5 zeolite molecular sieve into a metal salt solution, soaking it, drying it, and roasting it to obtain a metal-modified HZSM-5 zeolite molecular sieve.

[0134] In a preferred embodiment, this method includes the following steps.

[0135] a) Naphtha enters the naphtha-methanol coupling aromatic hydrocarbon preparation reaction zone of the naphtha-methanol coupling aromatic hydrocarbon preparation reactor 1 through the first sub-disperser 1-2-1 of the naphtha-methanol coupling aromatic hydrocarbon preparation reactor disperser 1-2, contacts the catalyst from the light hydrocarbon aromatization reactor 3, and a product gas stream containing BTX, low-carbon olefins, hydrogen, low-carbon alkanes, combustible gas, heavy aromatic hydrocarbons, and unconverted naphtha is generated; Methanol enters the naphtha-methanol coupling aromatic hydrocarbon preparation reaction zone through the second sub-disperser 1-2-2 and the third sub-disperser 1-2-3 of the naphtha-methanol coupling aromatic hydrocarbon preparation reactor disperser 1-2 respectively, and is subjected to a methylation reaction with benzene and toluene in the product gas stream to produce p-xylene; The catalyst from the light hydrocarbon aromatization reactor 3 is covered with coke in the naphtha-methanol coupling aromatic hydrocarbon preparation reaction zone and is converted into a used catalyst; The product gas stream enters the gas-solid separator I 1-3, the used catalyst contained in the product gas stream is removed, then enters the gas collection chamber I 1-4, and enters the downstream processing section through the product gas transport pipe I 1-5; And the used catalyst in the naphtha-methanol coupling aromatic hydrocarbon preparation reaction zone enters the reactor stripper 1-6 from the open end of the inlet pipe of the reactor stripper 1-6, is stripped, and then enters the regenerator 2 through the used slide valve 1-7 and the used agent transport pipe 1-8.

[0136] b) The regeneration gas is introduced into the regeneration zone of the regenerator 2 through the regenerator disperser 2-2, contacts the used catalyst, and the coke on the used catalyst reacts with the regeneration gas to generate exhaust gas. During this process, the used catalyst is converted into a regenerated catalyst; The exhaust gas enters the regenerator gas-solid separator 2-3, and after the regenerated catalyst contained in the exhaust gas is removed, it enters the regenerator gas collection chamber 2-4 and enters the downstream processing section through the exhaust gas transport pipe 2-5; The regenerated catalyst enters the light hydrocarbon aromatization reactor 3 sequentially through the regenerator stripper 2-6 and the regeneration slide valve 2-7.

[0137] c) The riser reactor feedstock is introduced into the riser reactor through the inlet end 3-1 of the riser reactor, contacts and reacts with the regenerated catalyst from the regenerator. Under the action of the catalyst, the riser reactor feedstock is converted into a stream containing components such as BTX, light olefins, and H 2 and the like, and then enters the inner lower part of the light hydrocarbon aromatization reaction zone in the bed reactor through the outlet end 3-3 of the riser reactor; the bed reactor feedstock is introduced into the light hydrocarbon aromatization reaction zone through the bed reactor disperser 3-5, contacts with the catalyst from the riser reactor, and generates light hydrocarbon aromatization product gas containing components such as BTX, light olefins, and H 2 and the like; the light hydrocarbon aromatization product gas enters the gas-solid separator II 3-6. After the catalyst contained in the light hydrocarbon aromatization product gas is removed, it enters the gas collection chamber II 3-7, enters the first gas-solid separation zone through the product gas transfer pipe II 3-8, and the catalyst in the light hydrocarbon aromatization reaction zone enters the naphtha-methanol coupling aromatic hydrocarbon preparation reactor 1 through the light hydrocarbon aromatization slide valve 3-9.

[0138] Light olefins refer to ethylene and propylene.

[0139] Light alkanes refer to ethane and propane.

[0140] The combustible gas includes methane, CO, etc.

[0141] Heavy aromatic hydrocarbons refer to aromatic hydrocarbons with 9 or more carbon atoms in the molecule.

[0142] 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.

[0143] In a preferred embodiment, the naphtha also contains unconverted naphtha separated from the product gas stream.

[0144] In a preferred embodiment, the carbon content in the used catalyst is 1.0 wt% to 3.0 wt%.

[0145] In a preferred embodiment, the process conditions of the naphtha-methanol coupling aromatic hydrocarbon preparation reaction zone are as follows: the apparent linear velocity of the gas is 0.5 m / s to 2.0 m / s, the reaction temperature is 500 °C to 600 °C, the reaction pressure is 100 kPa to 500 kPa, and the bed density is 150 kg / m 3 ~700 kg / m 3 is as follows.

[0146] Optionally, the apparent linear velocity of the gas in the naphtha-methanol coupling aromatic hydrocarbon preparation reaction zone is independently selected from any value among 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 value within the range between any two of these values.

[0147] Optionally, the reaction temperature in the naphtha-methanol coupling aromatic hydrocarbon preparation reaction zone is independently selected from any value among 500 °C, 520 °C, 530 °C, 540 °C, 550 °C, 560 °C, 570 °C, 580 °C, 590 °C, and 600 °C, or a value within the range between any two of these values.

[0148] Optionally, the reaction pressure in the naphtha-methanol coupling aromatic hydrocarbon preparation reaction zone is independently selected from any value among 100 kPa, 125 kPa, 150 kPa, 175 kPa, 200 kPa, 225 kPa, 250 kPa, 275 kPa, 300 kPa, 325 kPa, 350 kPa, 375 kPa, 400 kPa, 425 kPa, 450 kPa, 475 kPa, and 500 kPa, or a value within the range between any two of these values.

[0149] Optionally, the bed density in the naphtha-methanol coupling aromatic hydrocarbon preparation 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 , and 700 kg / m 3 are independently selected from any value or values within the range between any two of these values.

[0150] In a preferred embodiment, the carbon content in the regeneration catalyst is 0.5 wt% or less.

[0151] In a preferred embodiment, the regeneration gas is selected from at least one of oxygen, air, and oxygen-enriched air.

[0152] In a preferred embodiment, the process conditions in the regeneration zone are a superficial linear velocity of the gas of 0.5 m / s to 2.0 m / s, a regeneration temperature of 600 °C to 750 °C, a regeneration pressure of 100 kPa to 500 kPa, and a bed density of 150 kg / m 3 to 700 kg / m 3 .

[0153] Optionally, the superficial linear velocity of the gas in the regeneration zone is independently selected from any value or values within the range between any two of 0.5 m / s, 0.6 m / s, 0.7 m / s, 0.8 m / s, 0.9 m / s, 1.0 m / s, 1.1 m / s, 1.2 m / s, 1.3 m / s, 1.4 m / s, 1.5 m / s, 1.6 m / s, 1.7 m / s, 1.8 m / s, 1.9 m / s, and 2.0 m / s.

[0154] Optionally, the regeneration temperature in the regeneration zone is independently selected from any value or values within the 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.

[0155] Optionally, the regeneration pressure of the regeneration zone is independently selected from any value among 100 kPa, 125 kPa, 150 kPa, 175 kPa, 200 kPa, 225 kPa, 250 kPa, 275 kPa, 300 kPa, 325 kPa, 350 kPa, 375 kPa, 400 kPa, 425 kPa, 450 kPa, 475 kPa, and 500 kPa, or a value within the range between any two of these values.

[0156] Optionally, the bed density of the regeneration zone is 3 150 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 and 700 kg / m, and is independently selected from any value or a value within the range between any two of these values.

[0157] In a preferred embodiment, the riser reactor feedstock comprises steam and a low-carbon alkane separated from the product gas stream.

[0158] In a preferred embodiment, the steam content in the riser reactor feedstock is 0 wt% to 80 wt%.

[0159] In a preferred embodiment, the process conditions of the riser reactor are a superficial linear velocity of the gas of 3.0 m / s to 10.0 m / s, a temperature of 580 °C to 700 °C, a pressure of 100 kPa to 500 kPa, and a bed density of 50 kg / m 3 to 150 kg / m 3 .

[0160] Optionally, the apparent linear velocity of the gas in the riser reactor is independently selected from any value among 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 value within the range between any two of these values.

[0161] Optionally, the temperature of the riser reactor is independently selected from any value among 580 °C, 590 °C, 600 °C, 610 °C, 620 °C, 630 °C, 640 °C, 650 °C, 660 °C, 670 °C, 680 °C, 690 °C, and 700 °C or a value within the range between any two of these values.

[0162] Optionally, the pressure of the riser reactor is independently selected from any value among 100 kPa, 125 kPa, 150 kPa, 175 kPa, 200 kPa, 225 kPa, 250 kPa, 275 kPa, 300 kPa, 325 kPa, 350 kPa, 375 kPa, 400 kPa, 425 kPa, 450 kPa, 475 kPa, and 500 kPa or a value within the range between any two of these values.

[0163] Optionally, the bed density of the riser reactor is 50 kg / m3, 60 kg / m 3 、70 kg / m 3 、80 kg / m 3 、90 kg / m 3 、100 kg / m 3 、110 kg / m 3 、120 kg / m 3 、130 kg / m 3 、140 kg / m 3 、and 150 kg / m 3 and is independently selected from any value among these values or a value within the range between any two of these values.

[0164] The feedstock for the fluidized bed reactor contains C 4 hydrocarbons and C 5 hydrocarbons.

[0165] In a preferred embodiment, the fluidized bed reactor feedstock comprises C 3 hydrocarbons, C 4 hydrocarbons, and C 5 hydrocarbons.

[0166] In a preferred embodiment, the C 3 hydrocarbons, C 4 hydrocarbons, and C 5 hydrocarbons are derived from C 3 hydrocarbons, C 4 hydrocarbons, and C 5 hydrocarbons separated from the product gas stream.

[0167] The C 3 hydrocarbons, C 4 hydrocarbons, and C 5 hydrocarbons refer to hydrocarbons having 3 carbon atoms, hydrocarbons having 4 carbon atoms, and hydrocarbons having 5 carbon atoms.

[0168] In a preferred embodiment, the process conditions of the light hydrocarbon aromatization reaction zone are a superficial linear velocity of the gas of 0.5 m / s to 2.0 m / s, a reaction temperature of 550 °C to 665 °C, a reaction pressure of 100 kPa to 500 kPa, and a bed density of 150 kg / m 3 to 700 kg / m 3 .

[0169] Optionally, the superficial linear velocity of the gas in the light hydrocarbon aromatization reaction zone is independently selected from any value among 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 value within the range between any two of these values.

[0170] Optionally, the reaction temperature in the light hydrocarbon aromatization reaction zone is independently selected from any value among 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 a value within the range between any two of these values.

[0171] Optionally, the reaction pressure in the light hydrocarbon aromatization reaction zone is independently selected from any value among 100 kPa, 125 kPa, 150 kPa, 175 kPa, 200 kPa, 225 kPa, 250 kPa, 275 kPa, 300 kPa, 325 kPa, 350 kPa, 375 kPa, 400 kPa, 425 kPa, 450 kPa, 475 kPa, and 500 kPa or a value within the range between any two of these values.

[0172] Optionally, the bed density in 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 , and 700 kg / m 3 and is independently selected from any value among these values or a value within the range between any two of these values.

[0173] In the embodiments of the present application, the potential content of aromatic hydrocarbons in the naphtha feedstock is 0 wt% to 80 wt%, the single-pass conversion rate of naphtha is 60 wt% to 80 wt%, and the single-pass conversion rate of methanol is approximately 100 wt%. After the unconverted naphtha is separated from the product gas, it returns as a feedstock to the naphtha-methanol coupling aromatic hydrocarbon preparation reactor. A part of the lower alkanes returns as a feedstock to the riser reactor in the light hydrocarbon aromatization reactor after being separated from the product gas. C 3 hydrocarbons, C4 Hydrocarbons, and C 5 After being separated from the product gas, the hydrocarbons return as raw materials to the bed reactor in the light hydrocarbon aromatization reactor. The composition of the finally obtained product is as follows: BTX 60 wt% - 73 wt%, low-carbon olefins 9 wt% - 16 wt%, hydrogen 3 wt% - 6 wt%, low-carbon alkanes 3 wt% - 8 wt%, combustible gas 4 wt% - 6 wt%, heavy aromatic hydrocarbons 4 wt% - 8 wt%, and coke 0.5 wt% - 1 wt%. The content of p-xylene in the mixed xylene in the product is 60 wt% - 75 wt%.

[0174] (Example 1) In this embodiment, the apparatus shown in FIG. 1 is adopted.

[0175] In this embodiment, the naphtha raw material entering the naphtha-methanol coupling aromatic hydrocarbon preparation reactor is directly coal liquefaction naphtha, and the potential content of aromatic hydrocarbons in the naphtha is 78 wt%.

[0176] The process conditions of the naphtha-methanol coupling aromatic hydrocarbon preparation reaction zone of the naphtha-methanol coupling aromatic hydrocarbon preparation reactor are: apparent linear velocity of gas 0.5 m / s, reaction temperature 600 °C, reaction pressure 100 kPa, and bed density 700 kg / m 3 is.

[0177] The regeneration gas is air.

[0178] The process conditions of the regeneration zone of the regenerator are: apparent linear velocity of gas 0.5 m / s, regeneration temperature 745 °C, regeneration pressure 100 kPa, and bed density 700 kg / m 3 is.

[0179] The raw material of the riser reactor is the low-carbon alkane separated from the product gas stream.

[0180] The process conditions of the riser reactor are: apparent linear velocity of gas 3.0 m / s, temperature 690 °C, pressure 100 kPa, and bed density 150 kg / m3 It is.

[0181] The fluidized bed reactor feedstock is unconverted naphtha separated from the product gas stream, and the unconverted naphtha contains as main components straight-chain aliphatic hydrocarbons and branched-chain aliphatic hydrocarbons having C 4 -C 12 and naphthenic hydrocarbons.

[0182] The process conditions of the light hydrocarbon aromatization reaction zone are a superficial linear velocity of the gas of 0.5 m / s, a reaction temperature of 665°C, a reaction pressure of 100 kPa, and a bed density of 700 kg / m 3 It is.

[0183] The carbon content in the used catalyst is 1.0 wt%, and the carbon content in the regenerated catalyst is 0.2 wt%.

[0184] The single-pass conversion rate of the naphtha feedstock entering the naphtha-methanol coupling aromatic hydrocarbon preparation reactor is 61 wt%.

[0185] The composition of the product is 73 wt% BTX, 9 wt% light olefins, 3 wt% hydrogen, 3 wt% light alkanes, 5 wt% combustible gas, 6.5 wt% heavy aromatic hydrocarbons, and 0.5 wt% coke. The content of p-xylene in the mixed xylene in the product is 60 wt%.

[0186] (Example 2) In this embodiment, the apparatus shown in FIG. 1 is employed.

[0187] In this embodiment, the naphtha feedstock entering the naphtha-methanol coupling aromatic hydrocarbon preparation reactor is indirect coal liquefaction naphtha, and the potential content of aromatic hydrocarbons in the naphtha is 0.1 wt%. The naphtha feedstock entering the naphtha-methanol coupling aromatic hydrocarbon preparation reactor further contains unconverted naphtha separated from the product gas stream.

[0188] The process conditions of the naphtha-methanol coupling aromatic hydrocarbon preparation reaction zone in the naphtha-methanol coupling aromatic hydrocarbon preparation reactor are as follows: the apparent linear velocity of the gas is 2.0 m / s, the reaction temperature is 510 °C, the reaction pressure is 500 kPa, and the bed density is 150 kg / m 3 is as follows.

[0189] The regeneration gas is oxygen.

[0190] The process conditions of the regeneration zone in the regenerator are as follows: the apparent linear velocity of the gas is 2.0 m / s, the regeneration temperature is 610 °C, the regeneration pressure is 500 kPa, and the bed density is 150 kg / m 3 is as follows.

[0191] The riser reactor feedstock contains steam and low-carbon alkanes separated from the product gas stream, and the steam content in the riser reactor feedstock is 80 wt%.

[0192] The process conditions of the riser reactor are as follows: the apparent linear velocity of the gas is 10.0 m / s, the temperature is 580 °C, the pressure is 500 kPa, and the bed density is 50 kg / m 3 is as follows.

[0193] The bed reactor feedstock is C 3 hydrocarbons, C 4 hydrocarbons, and C 5 hydrocarbons.

[0194] The process conditions of the light hydrocarbon aromatization reaction zone are as follows: the apparent linear velocity of the gas is 2.0 m / s, the reaction temperature is 550 °C, the reaction pressure is 500 kPa, and the bed density is 150 kg / m 3 is as follows.

[0195] The carbon content in the used catalyst is 3.0 wt%, and the carbon content in the regenerated catalyst is 0.1 wt%.

[0196] The single-pass conversion rate of the naphtha feedstock entering the naphtha-methanol coupling aromatic hydrocarbon preparation reactor is 66 wt%.

[0197] The composition of the product is 65 wt% BTX, 13 wt% light olefins, 5 wt% hydrogen, 3.2 wt% light alkanes, 5 wt% combustible gas, 8 wt% heavy aromatic hydrocarbons, and 0.8 wt% coke. The p-xylene content in the mixed xylene in the product is 66 wt%.

[0198] (Example 3) In this embodiment, the apparatus shown in FIG. 1 is adopted.

[0199] In this embodiment, the naphtha feedstock entering the naphtha-methanol coupling aromatic hydrocarbon preparation reactor is indirect coal liquefaction naphtha, and the potential aromatic hydrocarbon content in the naphtha is 3 wt%. The naphtha feedstock entering the naphtha-methanol coupling aromatic hydrocarbon preparation reactor further includes unreacted naphtha separated from the product gas stream.

[0200] The process conditions of the naphtha-methanol coupling aromatic hydrocarbon preparation reaction zone in the naphtha-methanol coupling aromatic hydrocarbon preparation reactor are: apparent linear velocity of gas 1.2 m / s, reaction temperature 550 °C, reaction pressure 120 kPa, and bed density 260 kg / m 3 is.

[0201] The regeneration gas is oxygen-enriched air.

[0202] The process conditions of the regeneration zone in the regenerator are: apparent linear velocity of gas 1.2 m / s, regeneration temperature 650 °C, regeneration pressure 120 kPa, and bed density 260 kg / m 3 is.

[0203] The riser reactor feedstock includes steam and light alkanes separated from the product gas stream, and the steam content in the riser reactor feedstock is 25 wt%.

[0204] The process conditions of the riser reactor are: apparent linear velocity of gas 7.0 m / s, temperature 630 °C, pressure 120 kPa, and bed density 80 kg / m 3 is.

[0205] The bed reactor feedstock is C separated from the product gas stream 4 hydrocarbons and C 5 hydrocarbons.

[0206] The process conditions of the light hydrocarbon aromatization reaction zone are a superficial gas linear velocity of 1.2 m / s, a reaction temperature of 580 °C, a reaction pressure of 120 kPa, and a bed density of 260 kg / m 3 .

[0207] The carbon content in the used catalyst is 2.2 wt%, and the carbon content in the regenerated catalyst is 0.3 wt%.

[0208] The single-pass conversion rate of the naphtha feedstock entering the naphtha-methanol coupling aromatic hydrocarbon preparation reactor is 80 wt%.

[0209] The composition of the product is 60 wt% BTX, 16 wt% light olefins, 6 wt% hydrogen, 8 wt% light alkanes, 4.5 wt% combustible gas, 5 wt% heavy aromatic hydrocarbons, and 0.5 wt% coke. The content of p-xylene in the mixed xylene in the product is 75 wt%.

[0210] (Example 4) In this embodiment, the apparatus shown in FIG. 1 is employed.

[0211] In this embodiment, the naphtha feedstock entering the naphtha-methanol coupling aromatic hydrocarbon preparation reactor is straight-run naphtha, and the potential content of aromatic hydrocarbons in the naphtha is 46 wt%. The naphtha feedstock entering the naphtha-methanol coupling aromatic hydrocarbon preparation reactor further includes unreacted naphtha separated from the product gas stream.

[0212] The process conditions of the naphtha-methanol coupling aromatic hydrocarbon preparation reaction zone of the naphtha-methanol coupling aromatic hydrocarbon preparation reactor are a superficial gas linear velocity of 1.8 m / s, a reaction temperature of 590 °C, a reaction pressure of 200 kPa, and a bed density of 220 kg / m 3 .

[0213] The regeneration gas is air.

[0214] The process conditions in the regeneration zone of the regenerator are a superficial gas linear velocity of 1.8 m / s, a regeneration temperature of 700 °C, a regeneration pressure of 200 kPa, and a bed density of 220 kg / m 3 is.

[0215] The riser reactor feedstock includes steam and low-carbon alkanes separated from the product gas stream, and the steam content in the riser reactor feedstock is 50 wt%.

[0216] The process conditions of the riser reactor are a superficial gas linear velocity of 5.0 m / s, a temperature of 660 °C, a pressure of 200 kPa, and a bed density of 110 kg / m 3 is.

[0217] The bed reactor feedstock is C 4 hydrocarbons and C 5 hydrocarbons.

[0218] The process conditions of the light hydrocarbon aromatization reaction zone are a superficial gas linear velocity of 1.8 m / s, a reaction temperature of 630 °C, a reaction pressure of 200 kPa, and a bed density of 220 kg / m 3 is.

[0219] The carbon content in the used catalyst is 1.7 wt%, and the carbon content in the regenerated catalyst is 0.1 wt%.

[0220] The single-pass conversion rate of the naphtha feedstock entering the naphtha-methanol coupling aromatic hydrocarbon preparation reactor is 78 wt%.

[0221] The composition of the product is 68.1 wt% BTX, 12 wt% light olefins, 5 wt% hydrogen, 6 wt% low-carbon alkanes, 4 wt% combustible gas, 4 wt% heavy aromatic hydrocarbons, and 0.9 wt% coke. The content of p-xylene in the mixed xylene in the product is 71 wt%.

[0222] (Example 5) In this embodiment, the apparatus shown in FIG. 1 is adopted.

[0223] In this embodiment, the naphtha raw material entering the naphtha-methanol coupling aromatic hydrocarbon preparation reactor is hydrocracked naphtha, and the potential content of aromatic hydrocarbons in the naphtha is 64 wt%. The naphtha raw material entering the naphtha-methanol coupling aromatic hydrocarbon preparation reactor further includes unconverted naphtha separated from the product gas stream.

[0224] The process conditions of the naphtha-methanol coupling aromatic hydrocarbon preparation reaction zone of the naphtha-methanol coupling aromatic hydrocarbon preparation reactor are a superficial linear velocity of the gas of 1.0 m / s, a reaction temperature of 580 °C, a reaction pressure of 150 kPa, and a bed density of 350 kg / m 3 It is.

[0225] The regeneration gas is air.

[0226] The process conditions of the regeneration zone of the regenerator are a superficial linear velocity of the gas of 1.0 m / s, a regeneration temperature of 680 °C, a regeneration pressure of 150 kPa, and a bed density of 350 kg / m 3 It is.

[0227] The riser reactor raw material includes steam and low-carbon alkanes separated from the product gas stream, and the steam content in the riser reactor raw material is 40 wt%.

[0228] The process conditions of the riser reactor are a superficial linear velocity of the gas of 7.0 m / s, a temperature of 650 °C, a pressure of 150 kPa, and a bed density of 80 kg / m 3 It is.

[0229] The bed reactor raw material is C separated from the product gas stream 4 Hydrocarbons and C 5 Hydrocarbons.

[0230] The process conditions of the light hydrocarbon aromatization reaction zone are a superficial linear velocity of the gas of 1.0 m / s, a reaction temperature of 610 °C, a reaction pressure of 150 kPa, and a bed density of 350 kg / m 3 is as follows.

[0231] The carbon content in the used catalyst is 1.5 wt%, and the carbon content in the regenerated catalyst is 0.5 wt%.

[0232] The single-pass conversion rate of the naphtha raw material entering the naphtha-methanol coupling aromatic hydrocarbon preparation reactor is 72 wt%.

[0233] The composition of the product is 71 wt% BTX, 9 wt% light olefins, 4 wt% hydrogen, 3 wt% light alkanes, 6 wt% combustible gas, 6 wt% heavy aromatic hydrocarbons, and 1.0 wt% coke. The content of p-xylene in the mixed xylene in the product is 65 wt%.

[0234] The above are only some embodiments of the present application and are not intended to limit the present application in any way. Although the present application is disclosed in the above preferred embodiments, the preferred embodiments are not intended to limit the present application. Modifications or changes made by those skilled in the art using the technical content disclosed above without departing from the scope of the technical solution of the present application are equivalent to equivalent embodiments and all belong to the scope of the technical solution of the present application.

Brief Description of the Drawings

[0235]

Figure 1

Claims

1. An apparatus for preparing aromatic hydrocarbons by coupling naphtha and methanol, comprising: a light hydrocarbon aromatization reactor; a naphtha-methanol coupling aromatic hydrocarbon preparation reactor; wherein the light hydrocarbon aromatization reactor is used for introducing raw materials and a high-temperature catalyst, at least one outlet of the light hydrocarbon aromatization reactor is connected to the naphtha-methanol coupling aromatic hydrocarbon preparation reactor for transporting the catalyst and the produced light hydrocarbon aromatization product gas to the naphtha-methanol coupling aromatic hydrocarbon preparation reactor, the naphtha-methanol coupling aromatic hydrocarbon preparation reactor is used for introducing naphtha and methanol, bringing the naphtha into contact with the catalyst from the light hydrocarbon aromatization reactor, and generating a BTX-containing product gas stream after the reaction, and further subjecting the methanol to a methylation reaction with benzene and toluene in the product gas stream to generate p-xylene.

2. The naphtha-methanol coupling aromatic hydrocarbon preparation reactor is at least divided into a first gas-solid separation zone and a naphtha-methanol coupling aromatic hydrocarbon preparation reaction zone from top to bottom, the two zones communicate with each other, the naphtha-methanol coupling aromatic hydrocarbon preparation reaction zone is provided with a naphtha-methanol coupling aromatic hydrocarbon preparation reactor disperser, the naphtha-methanol coupling aromatic hydrocarbon preparation reactor disperser includes n sub-dispersers, the serial numbers of the plurality of sub-dispersers are 1 to n (n≥2) in sequence from bottom to top, the first sub-disperser is used for introducing naphtha raw materials, from the second sub-disperser to the nth sub-disperser are used for introducing methanol raw materials. The apparatus for preparing aromatic hydrocarbons by coupling naphtha and methanol according to Claim 1.

3. The apparatus for preparing aromatic hydrocarbons by coupling naphtha and methanol according to Claim 2, wherein n≤10.

4. 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 communicates with the gas collection chamber I. The outlet of the gas collection chamber I communicates with the product gas transfer pipe I. The product gas transfer pipe I is used to allow the BTX-containing product gas stream after gas-solid separation to flow out to a downstream processing section, and is an apparatus for preparing aromatic hydrocarbons by coupling naphtha and methanol according to claim 2.

5. The gas collection chamber I is located on the inner top of the naphtha-methanol coupling aromatic hydrocarbon preparation reactor shell, and is an apparatus for preparing aromatic hydrocarbons by coupling naphtha and methanol according to claim 4.

6. The gas-solid separation device I is one or more groups of a plurality of gas-solid cyclone separators. Each group of the plurality of gas-solid cyclone separators includes a first-stage gas-solid cyclone separator and a second-stage gas-solid cyclone separator, and is an apparatus for preparing aromatic hydrocarbons by coupling naphtha and methanol according to claim 4.

7. The light hydrocarbon aromatization reactor is at least divided into a second gas-solid separation zone and a light hydrocarbon aromatization reaction zone from top to bottom. The two zones communicate to form a bed reactor. The second gas-solid separation zone is provided with a gas-solid separation device II and a gas collection chamber II. The gas outlet of the gas-solid separation device II communicates with the gas collection chamber II. On the inner lower part of the light hydrocarbon aromatization reaction zone, a bed reactor disperser for introducing the bed reactor raw material is provided, and is an apparatus for preparing aromatic hydrocarbons by coupling naphtha and methanol according to claim 1.

8. The gas collection chamber II is provided on the inner top of the bed reactor, and is an apparatus for preparing aromatic hydrocarbons by coupling naphtha and methanol according to claim 7.

9. The bed reactor feedstock is C ４ hydrocarbons and C ５ An apparatus for preparing aromatic hydrocarbons by coupling naphtha and methanol according to claim 7, comprising hydrocarbons and C

10. The light hydrocarbon aromatization reactor further includes a riser reactor in addition to the bed reactor. The outlet end of the riser reactor extends into the inner lower part of the light hydrocarbon aromatization reaction zone. Above the riser reactor, the catalyst outlet of the gas-solid separation device II is provided, and is an apparatus for preparing aromatic hydrocarbons by coupling naphtha and methanol according to claim 7.

11. The inlet end of the riser reactor is an apparatus for preparing aromatic hydrocarbons by coupling naphtha and methanol according to claim 7, which is used for introducing the catalyst and the riser reactor raw materials.

12. The second gas-solid separation zone communicates with the first gas-solid separation zone. The light hydrocarbon aromatization reaction zone communicates with the naphtha-methanol coupling aromatic hydrocarbon preparation reaction zone. An apparatus for preparing aromatic hydrocarbons by coupling naphtha and methanol according to claim 7.

13. The gas collection chamber II communicates with the first gas-solid separation zone through the product gas transport pipe II. An apparatus for preparing aromatic hydrocarbons by coupling naphtha and methanol according to claim 7.

14. A light hydrocarbon aromatization slide valve is provided on the pipeline connecting the naphtha-methanol coupling aromatic hydrocarbon preparation reaction zone and the light hydrocarbon aromatization reaction zone. An apparatus for preparing aromatic hydrocarbons by coupling naphtha and methanol according to claim 12.

15. The position of the outlet of the light hydrocarbon aromatization reaction zone is higher than the position of the inlet of the naphtha-methanol coupling aromatic hydrocarbon preparation reaction zone. An apparatus for preparing aromatic hydrocarbons by coupling naphtha and methanol according to claim 7.

16. The position of the catalyst inlet of the naphtha-methanol coupling aromatic hydrocarbon preparation reaction zone is located between the first sub-disperser and the second sub-disperser. An apparatus for preparing aromatic hydrocarbons by coupling naphtha and methanol according to claim 15.

17. The gas-solid separation device II is a gas-solid cyclone separator. An apparatus for preparing aromatic hydrocarbons by coupling naphtha and methanol according to claim 7.

18. The apparatus further includes a regenerator. At least one inlet of the light hydrocarbon aromatization reactor is connected to the regenerator to obtain the high-temperature regenerated catalyst generated by the regenerator. An apparatus for preparing aromatic hydrocarbons by coupling naphtha and methanol according to claim 1.

19. The regenerator is the apparatus for preparing aromatic hydrocarbons by coupling naphtha and methanol according to claim 18, which communicates with the inlet end of the riser reactor of the light hydrocarbon aromatization reactor.

20. The regenerator is at least divided into a third gas-solid separation zone and a regeneration zone from top to bottom, the two zones communicate with each other, a regenerator gas-solid separation device and a regenerator gas collection chamber are provided in the third gas-solid separation zone, the gas outlet of the regenerator gas-solid separation device communicates with the regenerator gas collection chamber, an exhaust gas transfer pipe is provided on the regenerator gas collection chamber, a regenerator disperser for introducing regenerated gas is provided on the inner lower part of the regeneration zone, which is the apparatus for preparing aromatic hydrocarbons by coupling naphtha and methanol according to claim 18.

21. The regeneration zone is connected to the riser reactor sequentially through a regenerator stripper and a regeneration slide valve, the inlet pipe of the regenerator stripper extends into the regenerator shell and is located above the regenerator disperser, 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, which is the apparatus for preparing aromatic hydrocarbons by coupling naphtha and methanol according to claim 20.

22. The regenerator gas collection chamber is located on the inner top of the regenerator shell, which is the apparatus for preparing aromatic hydrocarbons by coupling naphtha and methanol according to claim 20.

23. The regenerator gas-solid separation device is one or a plurality of groups of a plurality of gas-solid cyclone separators, each group of the plurality of gas-solid cyclone separators includes a first-stage gas-solid cyclone separator and a second-stage gas-solid cyclone separator, which is the apparatus for preparing aromatic hydrocarbons by coupling naphtha and methanol according to claim 20.

24. At least one outlet of the naphtha-methanol coupling aromatic hydrocarbon preparation reactor is connected to the inlet of the regenerator for introducing the used catalyst generated by the reaction of the naphtha-methanol coupling aromatic hydrocarbon preparation reactor into the regenerator. The regenerator is used to introduce a regeneration gas to convert the used catalyst into a regenerated catalyst, and is an apparatus for preparing aromatic hydrocarbons by coupling naphtha and methanol according to claim 1.

25. The naphtha-methanol coupling aromatic hydrocarbon preparation reaction zone is connected to the inlet of the regenerator through a reactor stripper, a used slide valve, and a used agent transfer pipe in sequence. The inlet pipe of the reactor stripper extends into the naphtha-methanol coupling aromatic hydrocarbon preparation reactor shell and is located above the first disperser. The catalyst outlet end of the reactor gas-solid separation device is located above the open end of the inlet pipe of the reactor stripper, and is an apparatus for preparing aromatic hydrocarbons by coupling naphtha and methanol according to claim 2.

26. The inlet of the regenerator is located in the regeneration zone and is provided on the regenerator shell, and is an apparatus for preparing aromatic hydrocarbons by coupling naphtha and methanol according to claim 25.

27. A method for preparing aromatic hydrocarbons by coupling naphtha and methanol, comprising the step of preparing aromatic hydrocarbons by using an apparatus and a catalyst for preparing aromatic hydrocarbons by coupling naphtha and methanol according to any one of claims 1 to 6.

28. The catalyst is a metal molecular sieve dual-functional catalyst, and is a method for preparing aromatic hydrocarbons by coupling naphtha and methanol according to claim 27.

29. The metal molecular sieve dual-functional catalyst is a metal-modified HZSM-5 zeolite molecular sieve. The metal for the metal modification is selected from at least one of La, Zn, Ga, Fe, Mo, and Cr. The method for the metal modification includes the step of putting the HZSM-5 zeolite molecular sieve into a metal salt solution, soaking it, drying it, and calcining it to obtain the metal-modified HZSM-5 zeolite molecular sieve, and is a method for preparing aromatic hydrocarbons by coupling naphtha and methanol according to claim 28.

30. A step of introducing a raw material and a high-temperature catalyst into the light hydrocarbon aromatization reactor to generate the light hydrocarbon aromatization product gas. Introducing naphtha and the catalyst from the naphtha and light hydrocarbon aromatization reactor into the naphtha-methanol coupling aromatic hydrocarbon preparation reactor to produce a BTX-containing product gas stream; Introducing methanol into the naphtha-methanol coupling aromatic hydrocarbon preparation reactor and subjecting it to a methylation reaction with benzene and toluene in the BTX-containing product gas stream to produce p-xylene; A method for preparing aromatic hydrocarbons by coupling naphtha and methanol according to claim 27, comprising:

31. Removing the spent catalyst contained in all gas streams generated in the naphtha-methanol coupling aromatic hydrocarbon preparation reactor through the gas-solid separator I; A step of allowing the gas stream to enter the gas collection chamber I and then enter the downstream processing section through the product gas transfer pipe I; A method for preparing aromatic hydrocarbons by coupling naphtha and methanol according to claim 30, further comprising:

32. The components of the light hydrocarbon aromatization product gas include BTX, lower olefins, and H ２ A method for preparing aromatic hydrocarbons by coupling naphtha and methanol according to claim 30, wherein the method includes ２ .

33. The BTX-containing product gas stream further contains, in addition to the BTX, low-carbon olefins, hydrogen, low-carbon alkanes, combustible gases, heavy aromatic hydrocarbons, and unconverted naphtha. A method for preparing aromatic hydrocarbons by coupling naphtha and methanol according to claim 30.

34. The low-carbon olefins refer to ethylene and propylene, The low-carbon alkanes refer to ethane and propane, The combustible gas contains methane and CO, The heavy aromatic hydrocarbons refer to aromatic hydrocarbons having 9 or more carbon atoms in the molecule. A method for preparing aromatic hydrocarbons by coupling naphtha and methanol according to claim 33.

35. The naphtha is selected from at least one of direct coal liquefaction naphtha, indirect coal liquefaction naphtha, straight-run naphtha, and hydrocracked naphtha. A method for preparing aromatic hydrocarbons by coupling naphtha and methanol according to claim 30.

36. The naphtha also contains unconverted naphtha separated from the product gas stream, The unconverted naphtha is C ４ -C １２ A method for preparing aromatic hydrocarbons by coupling naphtha and methanol according to claim 35, which mainly contains linear aliphatic hydrocarbons and branched aliphatic hydrocarbons of C

37. The method for preparing aromatic hydrocarbons by coupling naphtha and methanol according to claim 31, wherein the carbon content in the used catalyst is 1.0 wt% to 3.0 wt%.

38. The process conditions of the naphtha-methanol coupling aromatic hydrocarbon preparation reaction zone in the naphtha-methanol coupling aromatic hydrocarbon preparation reactor are a superficial linear velocity of gas of 0.5 m / s to 2.0 m / s, a reaction temperature of 500 °C to 600 °C, a reaction pressure of 100 kPa to 500 kPa, and a bed density of 150 kg / m ３ to 700 kg / m ３ The method for preparing aromatic hydrocarbons by coupling naphtha and methanol according to claim 30, wherein the method is as described above.

39. The light hydrocarbon aromatization product gas enters the gas-solid separator II. After the catalyst contained in the light hydrocarbon aromatization product gas is removed, it enters the gas collection chamber II and enters the first gas-solid separation zone of the naphtha / methanol coupling aromatic hydrocarbon preparation reactor through the product gas transfer pipe II. The catalyst in the light hydrocarbon aromatization reaction zone enters the naphtha / methanol coupling aromatic hydrocarbon preparation reactor through the light hydrocarbon aromatization slide valve. The method for preparing aromatic hydrocarbons by coupling naphtha and methanol according to claim 30.

40. The process conditions of the light hydrocarbon aromatization reaction zone in the light hydrocarbon aromatization reactor are a superficial linear velocity of gas of 0.5 m / s to 2.0 m / s, a reaction temperature of 550 °C to 665 °C, a reaction pressure of 100 kPa to 500 kPa, and a bed density of 150 kg / m ３ to 700 kg / m ３ The method for preparing aromatic hydrocarbons by coupling naphtha and methanol according to claim 30, wherein the method is as described above.

41. A step of introducing a regeneration gas and a used catalyst into a regenerator to obtain a high-temperature regenerated catalyst; A step of transporting the high-temperature regenerated catalyst to the light hydrocarbon aromatization reactor; The method for preparing aromatic hydrocarbons by coupling naphtha and methanol according to claim 30, further comprising.

42. The regeneration gas is introduced into the regeneration zone of the regenerator through a regenerator disperser. The method for preparing aromatic hydrocarbons by coupling naphtha and methanol according to claim 41.

43. The regeneration gas is selected from at least one of oxygen, air, and oxygen-enriched air. The method for preparing aromatic hydrocarbons by coupling naphtha and methanol according to claim 41.

44. The carbon content in the used catalyst is 1.0 wt% to 3.0 wt%. The method for preparing aromatic hydrocarbons by coupling naphtha and methanol according to claim 41.

45. The carbon content in the regenerated catalyst is 0.5 wt% or less. The method for preparing aromatic hydrocarbons by coupling naphtha and methanol according to claim 41.

46. The process conditions of the regeneration zone of the regenerator are as follows: the apparent linear velocity of the gas is 0.5 m / s to 2.0 m / s, the regeneration temperature is 600°C to 750°C, the regeneration pressure is 100 kPa to 500 kPa, and the bed density is 150 kg / m ３ to 700 kg / m ３ A method for preparing aromatic hydrocarbons by coupling naphtha and methanol according to claim 41, wherein the method is as described above.

47. The coke on the used catalyst reacts with the regeneration gas to generate exhaust gas. The exhaust gas enters the third gas-solid separation zone, and the regenerated catalyst contained in the exhaust gas is removed. A method for preparing aromatic hydrocarbons by coupling naphtha and methanol according to claim 41.

48. The exhaust gas enters the third gas-solid separation zone, and the regenerated catalyst contained in the exhaust gas is removed. Specifically, the exhaust gas first enters a regenerator gas-solid separation device, and after the regenerated catalyst contained in the exhaust gas is removed, the exhaust gas passes through a regenerator gas collection chamber and an exhaust gas transfer pipe and enters a downstream processing section. A method for preparing aromatic hydrocarbons by coupling naphtha and methanol according to claim 47.

49. The regenerated catalyst enters the light hydrocarbon aromatization reactor through a regenerator stripper and a regeneration slide valve. A method for preparing aromatic hydrocarbons by coupling naphtha and methanol according to claim 41.

50. A step of introducing a riser reactor raw material into an inlet end of a riser reactor of the light hydrocarbon aromatization reactor; A step of introducing the regenerated catalyst into the riser reactor through a regenerator stripper and a regeneration slide valve; A step of converting the riser reactor raw material into the BTX-containing stream under the action of the regenerated catalyst; A step of allowing the BTX-containing stream to enter the inner lower part of a light hydrocarbon aromatization reaction zone in a bed reactor through an outlet end of the riser reactor; A method for preparing aromatic hydrocarbons by coupling naphtha and methanol according to claim 30, further comprising:

51. The riser reactor raw material is steam, and the lower-carbon alkane separated from the product gas stream, A method for preparing aromatic hydrocarbons by coupling naphtha and methanol according to claim 50.

52. The water vapor content in the riser reactor raw material is 0 wt% to 80 wt%. A method for preparing aromatic hydrocarbons by coupling naphtha and methanol according to claim 50.

53. The process conditions of the riser reactor are a superficial gas linear velocity of 3.0 m / s to 10.0 m / s, a temperature of 580°C to 700°C, a pressure of 100 kPa to 500 kPa, and a bed density of 50 kg / m ３ to 150 kg / m ３ A method for preparing aromatic hydrocarbons by coupling naphtha and methanol according to claim 50, wherein the method is as described above.

54. A step of introducing a catalyst into an inlet end of the riser reactor of the light hydrocarbon aromatization reactor; A step of allowing the catalyst to enter the bed reactor through the riser reactor; A method for preparing aromatic hydrocarbons by coupling naphtha and methanol according to claim 50, further comprising **Claim 55** A method for preparing aromatic hydrocarbons by coupling naphtha and methanol according to claim 54, further comprising the step of introducing a fluidized bed reactor feedstock into the fluidized bed hydrocarbon aromatization reaction zone through a fluidized bed reactor disperser and contacting it with the catalyst from the riser reactor to produce the fluidized bed hydrocarbon aromatization product gas. **Claim 56** The bed reactor feedstock is C ４ hydrocarbons and C ５ A method for preparing aromatic hydrocarbons by coupling naphtha and methanol according to claim 54, comprising hydrocarbons and C **Claim 57** Said C ４ hydrocarbons and said C ５ hydrocarbons are C separated from said product gas stream ４ hydrocarbons and C ５ hydrocarbons, a process for preparing aromatic hydrocarbons by coupling naphtha and methanol according to claim 56, which is derived from. **Claim 58** The components of the BTX-containing stream include BTX, lower olefins, and H ２ A process for preparing aromatic hydrocarbons by coupling naphtha and methanol according to claim 50, wherein the components include ２ . **Claim 59** A method for preparing aromatic hydrocarbons by coupling naphtha and methanol according to claim 30, further comprising the step of introducing the spent catalyst in the naphtha / methanol coupling aromatic hydrocarbon preparation reaction zone into the reactor stripper, and after stripping, allowing the spent catalyst to enter the downstream area through the spent slide valve and the spent agent transfer pipe. **Claim 60** A method for preparing aromatic hydrocarbons by coupling naphtha and methanol according to claim 59, wherein the downstream area is a regenerator.

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