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] This application relates to a fluidized bed apparatus and a method for using such apparatus, and belongs to the technical field of the chemical industry. In particular, this application relates to an apparatus and method for preparing aromatic hydrocarbons by coupling naphtha and methanol.

[0002] 〔background〕 Aromatic hydrocarbons (benzene, toluene, and xylene, collectively known as BTX) are important organic chemical raw materials. p-xylene (PX) is the most noteworthy 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 steadily increasing. In 2021, the total import volume of PX in China was approximately 13.65 million tons, and its dependence on foreign trade was approximately 38%.

[0003] Naphtha catalytic reforming is a major technological route for producing aromatic hydrocarbons. Naphtha composition is highly complex, and it is not only the primary raw material for catalytic reforming but also for ethylene production by cracking. The composition of naphtha plays a crucial role in the economic benefits of the equipment. Generally speaking, a high potential content of raw material aromatic hydrocarbons and a moderate distillation range are advantageous for catalytic reforming. On the other hand, a high content of linear-chain and branched-chain aliphatic hydrocarbons, and a low content of naphthenic and aromatic hydrocarbons, is suitable for ethylene production by cracking. Typically, to fully utilize naphtha resources and improve economic benefits, it is necessary to first separate the linear-chain and branched-chain aliphatic hydrocarbons from the naphthenic and aromatic hydrocarbons in the naphtha. The former are used as raw materials for ethylene production, and the latter are used as raw materials for catalytic reforming equipment.

[0004] The distillation range of naphtha fractions is wide, and conventional separation methods make it difficult to efficiently separate linear and branched aliphatic hydrocarbons from naphthenic and aromatic hydrocarbons. Furthermore, it is difficult to convert linear and branched aliphatic hydrocarbons to aromatic hydrocarbons using catalytic reforming techniques. Generally, naphtha feedstocks used for catalytic reforming need to be distilled to separate the blubber oil with a boiling point below 60°C in order to increase the potential content of aromatic hydrocarbons for catalytic reforming. However, fractions with boiling points above 60°C still contain many linear and branched aliphatic hydrocarbons that are difficult to convert to aromatic hydrocarbons. Therefore, highly selective conversion of linear and branched aliphatic hydrocarbons to aromatic hydrocarbons has always been a hot and challenging point in the development of technologies for preparing aromatic hydrocarbons from naphtha.

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

[0006] 〔overview〕 Naphtha molecules contain only a small amount of methyl groups (methyl group / benzene ring = ~1.3 (molar ratio)). The molecular structure of naphtha molecules inevitably leads to the production of a large amount of benzene as a by-product in catalytic reforming / aromatic compound compounding plants.

[0007] The aromatization of methanol is a novel process for preparing aromatic hydrocarbons. Methanol molecules contain an excess of hydrogen atoms compared to aromatic hydrocarbons. Therefore, the preparation of aromatic hydrocarbons using methanol inevitably produces large amounts of alkanes and hydrogen as by-products. Based on its molecular structure and reaction mechanism, methanol can provide the methyl group necessary for aromatic hydrocarbons. This increases the yield of toluene and xylene. Thus, a novel technological route for preparing aromatic hydrocarbons by coupling naphtha and methanol is provided.

[0008] In one aspect of this application, an apparatus is provided that can prepare aromatic hydrocarbons using naphtha and methanol as raw materials. This apparatus increases the p-xylene content in the mixed xylene and reduces the energy consumption for separation.

[0009] The naphtha components in this application include C4-C 12 This includes straight-chain aliphatic hydrocarbons and branched-chain aliphatic hydrocarbons, naphthenic hydrocarbons, and aromatic hydrocarbons.

[0010] In this application, aromatic hydrocarbons 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 comprises a light hydrocarbon aromaticization reactor and a naphtha-methanol coupling aromatic hydrocarbon preparation reactor, wherein the light hydrocarbon aromaticization reactor is used to introduce raw materials and a high-temperature catalyst, and at least one outlet of the light hydrocarbon aromaticization reactor is connected to the naphtha-methanol coupling aromatic hydrocarbon preparation reactor to transport the catalyst and the resulting light hydrocarbon aromaticization product gas to the naphtha-methanol coupling aromatic hydrocarbon preparation reactor, wherein the naphtha-methanol coupling aromatic hydrocarbon preparation reactor is used to introduce naphtha and methanol, to contact the naphtha with the catalyst from the light hydrocarbon aromaticization reactor to produce a BTX-containing product gas stream after the reaction, and to subject the methanol to a methylation reaction with benzene and toluene in the product gas stream to produce p-xylene.

[0012] When the catalyst enters the naphtha-methanol coupling aromatic hydrocarbon reactor, its temperature decreases to a certain extent, and at the same time, the catalyst comes into contact with the naphtha. This can eliminate localized high-temperature zones in the naphtha-methanol coupling aromatic hydrocarbon reactor. As a result, the yield of low-carbon alkanes is effectively reduced, and the yield of aromatic hydrocarbons is increased.

[0013] Preferably, the naphtha-methanol coupling aromatic hydrocarbon preparation reactor is divided from top to bottom into at least a first gas-solid separation zone and a naphtha-methanol coupling aromatic hydrocarbon preparation reaction zone, the two zones being in communication with each other, and 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 comprising n sub-dispersors, the sub-dispersors numbered sequentially from bottom to top as 1 to n (n≧2), the first sub-dispersor being used to introduce naphtha feedstock, and the second to the nth sub-dispersors being used to introduce methanol feedstock.

[0014] Preferably, n ≤ 10.

[0015] Preferably, the first gas-solid separation zone is provided with a gas-solid separation device I and a gas collection chamber I, the gas outlet of the gas-solid separation device I is in communication with the gas collection chamber I, the outlet of the gas collection chamber I is in communication with a product gas transport pipe I, and the product gas transport pipe I is used to discharge (output) the BTX-containing product gas flow after gas-solid separation to the 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 apparatus I is one or more groups of gas-solid cyclone separators, and each group 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 divided from top to bottom into at least a second gas-solid separation zone and a light hydrocarbon aromatization reaction zone, forming a bed reactor, the two zones are in communication with each other, 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 is in communication with the gas collection chamber II, and a bed reactor disperser for introducing bed reactor raw materials is provided on the lower inside 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 feedstock includes C4 hydrocarbons and C5 hydrocarbons. The C4 hydrocarbons and C5 hydrocarbons refer to hydrocarbons having four carbon atoms and hydrocarbons having five carbon atoms.

[0021] Preferably, the bed reactor feedstock includes C3 hydrocarbons, C4 hydrocarbons, and C5 hydrocarbons. The C3 hydrocarbons, C4 hydrocarbons, and C5 hydrocarbons refer to hydrocarbons having 3 carbon atoms, 4 carbon atoms, and 5 carbon atoms, respectively.

[0022] Preferably, 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 lower inner part of the light hydrocarbon aromatization reaction zone, and the catalyst outlet of the gas-solid separation unit II is located above the riser reactor.

[0023] Preferably, the 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 is in communication with the first gas-solid separation zone, and the light hydrocarbon aromatization reaction zone is in communication with the naphtha-methanol coupling aromatic hydrocarbon preparation reaction zone.

[0025] Preferably, the gas collection chamber II is in communication with the first gas-solid separation zone through the product gas transport 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 outlet of the light hydrocarbon aromatization reaction zone is located higher than the inlet of the naphtha-methanol coupling aromatic hydrocarbon preparation reaction zone.

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

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

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

[0031] Preferably, the inlet end of the riser reactor of the light hydrocarbon aromaticization reactor is in communication with the regenerator.

[0032] Preferably, the regenerator is divided from top to bottom into at least a third gas-solid separation zone and a regeneration zone, the two zones are in communication with each other, the third gas-solid separation zone is provided with a regenerator gas-solid separation device and a regenerator gas collection chamber, the gas outlet of the regenerator gas-solid separation device is in communication with the regenerator gas collection chamber, an exhaust gas transport pipe is provided above the regenerator gas collection chamber, and a regenerator disperser for introducing regenerated gas is provided above the lower inside of the regeneration zone.

[0033] Preferably, the regeneration zone is connected to the riser reactor via 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, and the catalyst outlet end of the regenerator gas-solid separation device is located above the open end of the inlet pipe of the regenerator stripper.

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

[0035] Preferably, the regenerator gas-solid separation device is one or more groups of gas-solid cyclone separators, and each group 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 a regenerator to introduce the spent catalyst produced by the reaction in the naphtha-methanol coupling aromatic hydrocarbon preparation reactor into the regenerator, which is used to introduce regenerating gas to convert the spent catalyst into a regenerating catalyst.

[0037] Preferably, the naphtha-methanol coupling aromatic hydrocarbon preparation reaction zone is connected to the regenerator inlet via a reactor stripper, a used slide valve, and a used agent transport 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, and the catalyst outlet end of the reactor gas-solid separation unit is located above the open end of the inlet pipe of the reactor stripper.

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

[0039] In another embodiment of this application, a method for preparing aromatic hydrocarbons by coupling naphtha and methanol is provided. The method includes the step of preparing aromatic hydrocarbons by using an apparatus and catalyst for preparing aromatic hydrocarbons by coupling naphtha and methanol as described above.

[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, where the metal for the metal modification is selected from at least one of La, Zn, Ga, Fe, Mo, and Cr, and the method for the metal modification includes the steps of placing the HZSM-5 zeolite molecular sieve in 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 the steps of: introducing the raw materials 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 and subjecting 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 stream generated in the naphtha-methanol coupling aromatic hydrocarbon preparation reactor is removed through the gas-solid separator 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 aromaticization product gas include BTX, low-carbon olefin, and H2.

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

[0045] Preferably, the low-carbon olefin refers to ethylene and propylene, the low-carbon alkane refers to ethane and propane, the flammable gas includes methane and CO, and the heavy aromatic hydrocarbon refers to an aromatic hydrocarbon having 9 or more carbon atoms in its 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 is C4-C 12 It mainly contains linear aliphatic hydrocarbons, branched aliphatic hydrocarbons, and naphthenic hydrocarbons.

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

[0049] Preferably, the process conditions for the naphtha-methanol coupling aromatic hydrocarbon preparation reaction zone are: apparent linear gas velocity of 0.5 m / s to 2.0 m / s, reaction temperature of 500°C to 600°C, reaction pressure of 100 kPa to 500 kPa, and floor density of 150 kg / m³. 3 ~700kg / m 3 That is the case.

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

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

[0052] Optionally, the reaction pressure in the naphtha-methanol coupling aromatic hydrocarbon preparation reaction zone is independently selected from any value or a value within the 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.

[0053] Optionally, the bed density in the naphtha-methanol coupling aromatic hydrocarbon preparation reaction zone is 150 kg / m 3 3, 200 kg / m 3 3, 250 kg / m 3 3, 300 kg / m 3 3, 350 kg / m 3 3, 400 kg / m 3 3, 450 kg / m 3 3, 500 kg / m 3 3, 550 kg / m 3 3, 600 kg / m 3 3, 650 kg / m 3 3, and 700 kg / m 3It is independently selected from any value or a value within a range between any two values.

[0054] Preferably, the light hydrocarbon aromatization product gas enters the gas-solid separation unit II, and after the catalyst contained in the light hydrocarbon aromatization product gas is removed, it enters the gas collection chamber II, and through the product gas transport pipe II, it enters the first gas-solid separation zone of the naphtha-methanol coupling aromatic hydrocarbon preparation reactor, and 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 for the light hydrocarbon aromatization reaction zone are: apparent linear velocity of gas of 0.5 m / s to 2.0 m / s, reaction temperature of 550°C to 665°C, reaction pressure of 100 kPa to 500 kPa, and floor density of 150 kg / m³. 3 ~700kg / m 3 That is the case.

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

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

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

[0059] Optionally, the floor density is 150 kg / m³. 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 It is independently selected from any value or a value within a range between any two values.

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

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

[0062] Preferably, the regenerated 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 of the regeneration zone of the regenerator are an apparent linear velocity of 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 floor density of 150 kg / m³. 3 ~700kg / m 3 That is the case.

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

[0067] The regeneration temperature is optionally selected independently from any value or a value within the range between any two values ​​among 600°C, 615°C, 630°C, 645°C, 670°C, 685°C, 700°C, 715°C, 730°C, 745°C, and 750°C.

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

[0069] Optionally, the floor density is 150 kg / m³. 3 , 200 kg / m 3 , 250 kg / m 3 , 300 kg / m 3 , 350 kg / m 3 , 400 kg / m 3 , 450 kg / m 3 , 500 kg / m 3 , 550 kg / m 3 , 600 kg / m 3 , 650 kg / m3 , and 700 kg / m 3 It is independently selected from any value or a value within a range between any two values.

[0070] Preferably, the coke on the spent catalyst reacts with the regenerated gas to produce exhaust gas, which enters the third gas-solid separation zone, and the regenerated catalyst contained in the exhaust gas is removed.

[0071] Preferably, the exhaust gas enters the third gas-solid separation zone, where the regenerating catalyst contained in the exhaust gas is removed. Specifically, this includes the exhaust gas first entering the regenerator gas-solid separation unit, where the regenerating catalyst contained in the exhaust gas is removed, and then the exhaust gas passing through the regenerator gas collection chamber and exhaust gas transport pipe to enter the downstream processing section.

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

[0073] Preferably, the method further includes the steps of: introducing riser reactor raw materials into the inlet end of the riser reactor of the light hydrocarbon aromatization reactor; introducing the regenerating catalyst into the riser reactor through a regenerator stripper and a regenerating slide valve; converting the riser reactor raw materials into the BTX-containing flow under the action of the regenerating catalyst; and causing the BTX-containing flow to enter the lower inside of the light hydrocarbon aromatization reaction zone in the bed reactor through the outlet end of the riser reactor.

[0074] Preferably, the method further includes the steps of introducing a catalyst to the 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 feedstock includes steam and the low-carbon alkane separated from the product gas stream.

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

[0077] Preferably, the process conditions for the riser reactor are an apparent linear gas 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 floor density of 50 kg / m³. 3 ~150kg / m 3 That is the case.

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

[0079] The temperature is optionally selected independently from any value or a value within the 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 100kPa, 125kPa, 150kPa, 175kPa, 200kPa, 225kPa, 250kPa, 275kPa, 300kPa, 325kPa, 350kPa, 375kPa, 400kPa, 425kPa, 450kPa, 475kPa, and 500kPa.

[0081] Optionally, the floor density can be 50 kg / m³ or 60 kg / m³. 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 It is independently selected from any value or a value within a range between any two values.

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

[0083] Optionally, the bed reactor feedstock includes C4 hydrocarbons and C5 hydrocarbons. The C4 hydrocarbons and C5 hydrocarbons are derived from the C4 hydrocarbons and C5 hydrocarbons separated from the product gas stream.

[0084] Preferably, the bed reactor feedstock comprises C3 hydrocarbons, C4 hydrocarbons, and C5 hydrocarbons. The C3 hydrocarbons, C4 hydrocarbons, and C5 hydrocarbons are derived from C3 hydrocarbons, C4 hydrocarbons, and C5 hydrocarbons separated from the product gas stream.

[0085] Preferably, the components of the BTX-containing stream include BTX, low-carbon olefin, and H2.

[0086] Preferably, the method further includes 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 a downstream area through a spent slide valve and a spent agent transport pipe. 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 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 said apparatus, unconverted naphtha is separated from the product gas and returned as feedstock to the naphtha-methanol coupling aromatic hydrocarbon preparation reactor, a portion of the low-carbon alkanes is separated from the product gas and returned as feedstock to the riser reactor in the light hydrocarbon aromaticization reactor, and C3 hydrocarbons, C4 hydrocarbons, and C5 hydrocarbons are separated from the product gas and returned as feedstock to the bed reactor in the light hydrocarbon aromaticization reactor. The final product composition is as follows: BTX 60 wt% to 73 wt%, low-carbon olefins 9 wt% to 16 wt%, hydrogen 3 wt% to 6 wt%, low-carbon alkanes 3 wt% to 8 wt%, flammable gases 4 wt% to 6 wt%, heavy aromatic hydrocarbons 4 wt% to 8 wt%, and coke 0.5 wt% to 1 wt%. The p-xylene content in the mixed xylene in the product is 60 wt% to 75 wt%.

[0088] This application can achieve the following beneficial effects.

[0089] 1) According to this application, linear aliphatic hydrocarbons and branched aliphatic hydrocarbons can be efficiently converted to aromatic hydrocarbons with high selectivity, and aromatic hydrocarbons can be prepared from naphtha, which has a wide range of applications and a low potential content of aromatic hydrocarbons.

[0090] 2) According to this application, aromatization of low-carbon alkanes, as well as C4 and C5 hydrocarbons, is achieved using a light hydrocarbon aromatization reactor and a metal molecular sieve binary catalyst. As a result, the yield of aromatic hydrocarbons in techniques for preparing aromatic hydrocarbons using naphtha is significantly improved.

[0091] 3) According to this 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-dispersors, through which naphtha enters the naphtha-methanol coupling aromatic hydrocarbon preparation reaction zone through the first sub-dispersor, and methanol enters the naphtha-methanol coupling aromatic hydrocarbon preparation reaction zone through each of the second to nth sub-dispersors. The naphtha-methanol coupling aromatic hydrocarbon preparation reactor is a fluidized bed reactor suitable for cascade reactions, in which the naphtha is converted to benzene and toluene at the bottom of the naphtha-methanol coupling aromatic hydrocarbon preparation reaction zone, then flows upward to the middle and upper parts of the naphtha-methanol coupling aromatic hydrocarbon preparation reaction zone, where the benzene and toluene are subjected to a methylation reaction with methanol to further produce p-xylene. As a result, the yield of p-xylene is increased. The high-temperature catalyst from the light hydrocarbon aromatization reactor enters directly into the lower part of the naphtha-methanol coupling aromatic hydrocarbon preparation reaction zone. This is advantageous for supplying the heat necessary for the reaction to convert naphtha to aromatic hydrocarbons and improving the conversion rate of naphtha. Methanol enters directly into the central and upper parts of the naphtha-methanol coupling aromatic hydrocarbon preparation reaction zone. This effectively shortens the residence time of p-xylene in the reaction zone, suppresses the isomerization reaction of p-xylene, increases the p-xylene content in xylene (up to 75 wt% under optimal technical conditions), and significantly reduces the energy consumption for p-xylene separation. In summary, in the naphtha-methanol coupling aromatic hydrocarbon preparation reactor, the naphtha feedstock flows from bottom to top, and in the process of converting naphtha to aromatic hydrocarbons, the methylation feedstock (methanol) is added stepwise to control the cascade reaction (naphtha → benzene and toluene → p-xylene). As a result, the yield of p-xylene is increased.

[0092] 4) The aromatization reaction of naphtha is a strongly endothermic reaction; 1.1 MJ to 1.6 MJ of heat must be absorbed to convert 1 kg of naphtha into aromatic hydrocarbons. The methylation reaction of methanol and aromatic hydrocarbons is a strongly exothermic reaction; more than 2.0 MJ of heat may be released when converting 1 kg of methanol into methyl groups on aromatic hydrocarbons. 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, a self-heating balance (equilibrium) is achieved.

[0093] 5) According to this application, an apparatus for preparing aromatic hydrocarbons by coupling naphtha and methanol is provided with a separate light hydrocarbon aromatization reactor. Low-carbon alkanes are very stable and require high reaction temperatures, and the temperature of the light hydrocarbon aromatization reactor is higher than that of the naphtha-methanol coupling aromatic hydrocarbon preparation reactor, so that low-carbon alkanes, as well as C4 and C5 hydrocarbons, are subjected to the aromatization reaction in the separate light hydrocarbon aromatization reactor. As a result, the reaction rate and the yield of aromatic hydrocarbons are increased.

[0094] [Brief explanation of the drawing] Figure 1 is a schematic diagram of an apparatus for preparing aromatic hydrocarbons by coupling naphtha and methanol, according to one embodiment of this application.

[0095] List of components and reference symbols: 1 refers to a naphtha-methanol coupling aromatic hydrocarbon preparation reactor; 1-1 refers to the naphtha-methanol coupling aromatic hydrocarbon preparation reactor shell; 1-2 refers to naphtha-methanol coupling aromatic hydrocarbon preparation reactor disperser; 1-3 refers to the gas-solid separation apparatus I, 1-4 refers to the gas collection chamber I, and 1-5 refers to the product gas transport pipe I; 1-6 refer to reactor strippers, 1-7 refer to used slide valves, and 1-8 refer to used agent transport pipes; 1-2-1 refers to the first sub-distributor, 1-2-2 refers to the second sub-distributor, and 1-2-3 refers to the third sub-distributor; 2 refers to a regenerator; 2-1 refers to the regenerator shell, and 2-2 refers to the regenerator distributor; 2-3 refers to the regenerator gas-solid separation unit, 2-4 refers to the regenerator gas collection chamber, and 2-5 refers to the exhaust gas transport pipe; 2-6 refers to the regenerator stripper, and 2-7 refers to the regenerator slide valve; 3 refers to a 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 floor reactor shell; 3-5 refers to the bed reactor disperser, and 3-6 refers to the gas-solid separation unit II; 3-7 refers to gas collection chamber II, 3-8 refers to product gas transport pipe II, and 3-9 refers to light hydrocarbon aromatization slide valve.

[0096] [Detailed explanation] The present application will be described in detail below with reference to the examples provided. However, the present application is not limited to these examples.

[0097] This application provides an apparatus for preparing aromatic hydrocarbons by coupling naphtha and methanol. This apparatus is Light hydrocarbon aromaticization reactor, Naphtha-methanol coupling aromatic hydrocarbon preparation reactor, Includes, The light hydrocarbon aromatization reactor is used to introduce the raw materials and high-temperature catalyst. At least one outlet of the light hydrocarbon aromatization reactor is connected to the naphtha-methanol coupling aromatic hydrocarbon preparation reactor in order to transport 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, to contact the naphtha with the catalyst from the light hydrocarbon aromaticization reactor to generate a BTX-containing product gas stream after the reaction, and to subject the methanol to a methylation reaction with benzene and toluene in the product gas stream to produce p-xylene.

[0098] The naphtha components in this application include C4-C 12 This includes straight-chain aliphatic hydrocarbons and branched-chain aliphatic hydrocarbons, naphthenic hydrocarbons, and aromatic hydrocarbons.

[0099] In this application, BTX refers to aromatic hydrocarbons, specifically benzene, toluene, and xylene.

[0100] In one preferred embodiment, the apparatus further includes a regenerator, the inlet of which at least one inlet of the light hydrocarbon aromatization reactor is connected to the regenerator to obtain a high-temperature regenerated catalyst produced by the regenerator.

[0101] Referring to Figure 1, an apparatus for preparing aromatic hydrocarbons by coupling naphtha and methanol in a preferred embodiment of the present application includes a naphtha-methanol coupling aromatic hydrocarbon preparation reactor 1, a regenerator 2, and a light hydrocarbon aromaticization 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 unit I 1-3, a gas collection chamber I 1-4, a product gas transport pipe I 1-5, a reactor stripper 1-6, a used slide valve 1-7, and a used agent transport 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, which includes an upper naphtha-methanol coupling aromatic hydrocarbon preparation reactor shell and a lower naphtha-methanol coupling aromatic hydrocarbon preparation reactor shell 1-1, the upper naphtha-methanol coupling aromatic hydrocarbon preparation reactor shell 1-1 surrounds the first gas-solid separation zone, the lower naphtha-methanol coupling aromatic hydrocarbon preparation reactor shell 1-1 surrounds the naphtha-methanol coupling aromatic hydrocarbon preparation reaction zone, and the naphtha-methanol coupling aromatic hydrocarbon preparation reactor shell 1-1 is provided with an outlet for the light hydrocarbon aromaticization reactor 3.

[0105] The naphtha-methanol coupling aromatic hydrocarbon preparation reaction zone is provided with naphtha-methanol coupling aromatic hydrocarbon preparation reactor dispersers 1-2. The naphtha-methanol coupling aromatic hydrocarbon preparation reactor dispersers 1-2 include three sub-dispersers, which are numbered from bottom to top as 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 feedstock.

[0106] The naphtha-methanol coupling aromatic hydrocarbon preparation reactor shell 1-1 is equipped with a gas-solid separator I 1-3 and a gas collection chamber I 1-4. 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 is in communication with the gas collection chamber I 1-4, the gas collection chamber I 1-4 is in communication with the product gas transport pipe I 1-5, and the catalyst outlet end of the gas-solid separator I 1-3 is located above the open end of the inlet pipe of the reactor stripper 1-6.

[0107] The reactor strippers 1-6 are located below the naphtha-methanol coupling aromatic hydrocarbon preparation reaction zone, with the inlet of reactor strippers 1-6 located inside the naphtha-methanol coupling aromatic hydrocarbon preparation reactor shell 1-1 and the outlet of reactor strippers 1-6 located outside the naphtha-methanol coupling aromatic hydrocarbon preparation reactor shell 1-1 and connected to the used slide valve 1-7, and the open end of the inlet of reactor strippers 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 transport pipe 1-8, and the outlet of the used agent transport pipe 1-8 is connected to the regenerator shell 2-1.

[0109] The used slide valves 1-7 are used to control the circulation rate of the used catalyst.

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

[0111] 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 transport pipe 2-5, a regenerator stripper 2-6, and a regenerator slide valve 2-7.

[0112] The regenerator shell 2-1 includes a regenerator upper shell and a regenerator lower shell, the third gas-solid separation zone being surrounded by the regenerator upper shell and the regeneration zone being surrounded by the regenerator lower shell, and the regenerator shell 2-1 is provided with an outlet for the used agent transport pipe 1-8.

[0113] A regenerator disperser 2-2 is installed above the lower part of the regeneration zone, and the regenerator disperser 2-2 is used to introduce regenerated gas.

[0114] The regenerator shell 2-1 is also equipped 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 is in communication with the regenerator gas collection chamber 2-4, the regenerator gas collection chamber 2-4 is in communication with the exhaust gas transport pipe 2-5, and the catalyst outlet end of the regenerator gas-solid separator 2-3 is located above the open end of the inlet pipe of the regenerator stripper 2-6.

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

[0116] Below the regenerator stripper 2-6, a regenerator slide valve 2-7 is provided, and the inlet of the regenerator 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 rate of the regenerated catalyst.

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

[0119] The light hydrocarbon aromatization reactor includes a riser reactor inlet 3-1, a riser reactor central section 3-2, a riser reactor outlet 3-3, a bed reactor shell 3-4, a bed reactor disperser 3-5, a gas-solid separation unit II 3-6, a gas collection chamber II 3-7, a product gas transport pipe II 3-8, and a light hydrocarbon aromatization slide valve 3-9.

[0120] The bed reactor shell 3-4 includes a bed reactor upper shell and a bed reactor lower shell, the second gas-solid separation zone being surrounded by the bed reactor upper shell, the light hydrocarbon aromatization reaction zone being surrounded by the bed reactor lower shell, the bed reactor disperser 3-5 being provided above the lower inside of the light hydrocarbon aromatization reaction zone, the light hydrocarbon aromatization slide valve 3-9 being provided outside the light hydrocarbon aromatization reaction zone, the upper section of the riser reactor being inserted axially into the bed reactor through the bottom of the bed reactor, and the outlet end 3-3 of the riser reactor being located above the lower inside of the light hydrocarbon aromatization reaction zone.

[0121] The light hydrocarbon aromaticization slide valves 3-9 are used to transport the catalyst to the next reactor, for example, to the naphtha-methanol coupling aromatic hydrocarbon preparation reactor 1.

[0122] The second gas-solid separation zone is equipped with a gas-solid separation apparatus II 3-6 and a gas collection chamber II 3-7. The gas outlet of gas-solid separation apparatus II 3-6 is connected to gas collection chamber II 3-7, the catalyst outlet of gas-solid separation apparatus II 3-6 is located within the light hydrocarbon aromatization reaction zone, and gas collection chamber II 3-7 is connected to a product gas transport pipe II 3-8 located outside the floor reactor.

[0123] In one preferred embodiment, the gas-solid separation device 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, and 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 one preferred embodiment, the bed reactor dispersers 3-5 are used to introduce the bed reactor raw materials.

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

[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 a regeneration slide valve 2-7 via a pipeline, and the light hydrocarbon aromatization slide valve 3-9 is connected to a naphtha-methanol coupling aromatic hydrocarbon preparation reactor shell 1-1 via a pipeline. It is located between the first subdispersor 1-2-1 and the second subdispersor 1-2-2.

[0129] In a preferred embodiment, the product gas transport 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 apparatus and catalyst for preparing aromatic hydrocarbons by coupling naphtha and methanol as described above.

[0131] The catalyst is a metal molecular sieve binary function catalyst. In Examples 1-5, a metal-modified HZSM-5 zeolite molecular sieve was used.

[0132] The metal for metall 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 placing an HZSM-5 zeolite molecular sieve in a metal salt solution, immersing it, drying it, and roasting it to obtain a metal-modified HZSM-5 zeolite molecular sieve.

[0134] In one preferred embodiment, this method includes the following steps:

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

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

[0137] c) The riser reactor feedstock is introduced into the riser reactor through the riser reactor inlet end 3-1, where it comes into contact with the regenerated catalyst from the regenerator and reacts. Under the action of the catalyst, the riser reactor feedstock is converted into a stream containing components such as BTX, low-carbon olefins, and H2, and then enters the lower inner part of the light hydrocarbon aromatization reaction zone in the bed reactor through the riser reactor outlet end 3-3; the bed reactor feedstock is introduced into the light hydrocarbon aromatization reaction zone through the bed reactor disperser 3-5, where it comes into contact with the catalyst from the riser reactor to produce a light hydrocarbon aromatization product gas containing components such as BTX, low-carbon olefins, and H2; the light hydrocarbon aromatization product gas enters the gas-solid separation unit II 3-6, where the catalyst contained in the light hydrocarbon aromatization product gas is removed, and then enters the gas collection chamber II 3-7 and the product gas transport pipe II The catalyst enters the first gas-solid separation zone via 3-8, and then enters the naphtha-methanol coupling aromatic hydrocarbon preparation reactor 1 via the light hydrocarbon aromaticization slide valve 3-9.

[0138] Low-carbon olefins refer to ethylene and propylene.

[0139] Low-carbon alkanes refer to ethane and propane.

[0140] Flammable gases include methane, CO, etc.

[0141] Heavy aromatic hydrocarbons refer to aromatic hydrocarbons that have nine or more carbon atoms in their molecules.

[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 one preferred embodiment, the naphtha also includes unconverted naphtha separated from the product gas stream.

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

[0145] In a preferred embodiment, the process conditions for the naphtha-methanol coupling aromatic hydrocarbon preparation reaction zone are: apparent linear velocity of gas 0.5 m / s to 2.0 m / s, reaction temperature 500°C to 600°C, reaction pressure 100 kPa to 500 kPa, and floor density 150 kg / m³. 3 ~700kg / m 3 That is the case.

[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 or a value within the range between any two values ​​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.

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

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

[0149] Optionally, the floor density of the naphtha-methanol coupling aromatic hydrocarbon preparation reaction zone is 150 kg / m³. 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 It is independently selected from any value or a value within a range between any two values.

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

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

[0152] In a preferred embodiment, the process conditions for the regeneration zone are: apparent linear velocity of gas of 0.5 m / s to 2.0 m / s, regeneration temperature of 600°C to 750°C, regeneration pressure of 100 kPa to 500 kPa, and floor density of 150 kg / m³. 3 ~700kg / m 3 That is the case.

[0153] Optionally, the apparent linear velocity of the gas in the regeneration zone is independently selected from any value or a value within the range between any two values ​​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.

[0154] Optionally, the regeneration temperature of the regeneration zone is independently selected from any value or a range between any two values ​​among 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 in the regeneration zone is independently selected from any value or a range between any two values ​​among 100kPa, 125kPa, 150kPa, 175kPa, 200kPa, 225kPa, 250kPa, 275kPa, 300kPa, 325kPa, 350kPa, 375kPa, 400kPa, 425kPa, 450kPa, 475kPa, and 500kPa.

[0156] Optionally, the floor density of the regeneration zone is set to 150 kg / m³. 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 It is independently selected from any value or a value within a range between any two values.

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

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

[0159] In a preferred embodiment, the process conditions for the riser reactor are an apparent linear gas 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 floor density of 50 kg / m³. 3 ~150kg / m 3 That is the case.

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

[0161] Optionally, the temperature of the riser reactor is independently selected from any value or a value within the 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.

[0162] Optionally, the pressure of the riser reactor is independently selected from any value or a value within the 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.

[0163] Optionally, the bed density of the riser reactor is independently selected from any value or a value within the 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 among which it is independently selected from any value or a value within the range between any two values.

[0164] The feedstock of the bed reactor contains C4 hydrocarbons and C5 hydrocarbons.

[0165] In one preferred embodiment, the bed reactor feedstock includes C3 hydrocarbons, C4 hydrocarbons, and C5 hydrocarbons.

[0166] In one preferred embodiment, the C3 hydrocarbons, C4 hydrocarbons, and C5 hydrocarbons are derived from the C3 hydrocarbons, C4 hydrocarbons, and C5 hydrocarbons separated from the product gas stream.

[0167] C3 hydrocarbons, C4 hydrocarbons, and C5 hydrocarbons refer to hydrocarbons having three carbon atoms, four carbon atoms, and five carbon atoms, respectively.

[0168] In one preferred embodiment, the process conditions for the light hydrocarbon aromatization reaction zone are: apparent linear velocity of gas of 0.5 m / s to 2.0 m / s, reaction temperature of 550°C to 665°C, reaction pressure of 100 kPa to 500 kPa, and floor density of 150 kg / m³. 3 ~700kg / m 3 That is the case.

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

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

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

[0172] Optionally, the floor density of the light hydrocarbon aromatization reaction zone is set to 150 kg / m³. 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 It is independently selected from any value or a value within a range between any two values.

[0173] In the embodiments of this application, the potential content of aromatic hydrocarbons in the naphtha feedstock is 0 wt% to 80 wt%, the single-flow conversion rate of naphtha is 60 wt% to 80 wt%, and the single-flow conversion rate of methanol is approximately 100 wt%. After being separated from the product gas, the unconverted naphtha is returned as feedstock to the naphtha-methanol coupling aromatic hydrocarbon preparation reactor, some of the low-carbon alkanes are returned as feedstock to the riser reactor in the light hydrocarbon aromaticization reactor after being separated from the product gas, and C3 hydrocarbons, C4 hydrocarbons, and C5 hydrocarbons are returned as feedstock to the bed reactor in the light hydrocarbon aromaticization reactor after being separated from the product gas. The final product composition is as follows: BTX 60 wt% to 73 wt%, low-carbon olefins 9 wt% to 16 wt%, hydrogen 3 wt% to 6 wt%, low-carbon alkanes 3 wt% to 8 wt%, flammable gases 4 wt% to 6 wt%, heavy aromatic hydrocarbons 4 wt% to 8 wt%, and coke 0.5 wt% to 1 wt%. The p-xylene content in the mixed xylene in the product is 60 wt% to 75 wt%.

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

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

[0176] The process conditions in the naphtha-methanol coupling aromatic hydrocarbon preparation reaction zone of the naphtha-methanol coupling aromatic hydrocarbon preparation reactor are: apparent linear gas velocity of 0.5 m / s, reaction temperature of 600°C, reaction pressure of 100 kPa, and floor density of 700 kg / m³. 3 That is the case.

[0177] The regenerated gas is air.

[0178] The process conditions for the regeneration zone of the regenerator are: apparent linear gas velocity of 0.5 m / s, regeneration temperature of 745°C, regeneration pressure of 100 kPa, and floor density of 700 kg / m³. 3 That is the case.

[0179] The raw materials for the riser reactor are low-carbon alkanes separated from the product gas stream.

[0180] The riser reactor process conditions are: apparent linear gas velocity of 3.0 m / s, temperature of 690°C, pressure of 100 kPa, and floor density of 150 kg / m³. 3 That is the case.

[0181] The bed reactor feedstock is unconverted naphtha separated from the product gas stream, and the unconverted naphtha is C4-C 12 It mainly contains linear aliphatic hydrocarbons, branched aliphatic hydrocarbons, and naphthenic hydrocarbons.

[0182] The process conditions for the light hydrocarbon aromatization reaction zone are an apparent linear gas velocity of 0.5 m / s, a reaction temperature of 665°C, a reaction pressure of 100 kPa, and a floor density of 700 kg / m³. 3 That is the case.

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

[0184] The single-flow 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% low-carbon olefin, 3 wt% hydrogen, 3 wt% low-carbon alkane, 5 wt% flammable gas, 6.5 wt% heavy aromatic hydrocarbon, and 0.5 wt% coke. The p-xylene content in the mixed xylene in the product is 60 wt%.

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

[0187] In this embodiment, the naphtha feedstock entering the naphtha-methanol coupling aromatic hydrocarbon preparation reactor is indirectly liquefied coal 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 includes unconverted naphtha separated from the product gas stream.

[0188] The process conditions in the naphtha-methanol coupling aromatic hydrocarbon preparation reaction zone of the naphtha-methanol coupling aromatic hydrocarbon preparation reactor are: apparent linear gas velocity of 2.0 m / s, reaction temperature of 510°C, reaction pressure of 500 kPa, and floor density of 150 kg / m³. 3 That is the case.

[0189] The regenerated gas is oxygen.

[0190] The process conditions for the regeneration zone of the regenerator are: apparent linear gas velocity of 2.0 m / s, regeneration temperature of 610°C, regeneration pressure of 500 kPa, and floor density of 150 kg / m³. 3 That is the case.

[0191] The riser reactor feedstock consists of water vapor and low-carbon alkanes separated from the product gas stream, with a water vapor content of 80 wt%.

[0192] The riser reactor process conditions are: apparent linear gas velocity of 10.0 m / s, temperature of 580°C, pressure of 500 kPa, and floor density of 50 kg / m³. 3 That is the case.

[0193] The bed reactor feedstock consists of C3, C4, and C5 hydrocarbons separated from the product gas stream.

[0194] The process conditions for the light hydrocarbon aromatization reaction zone are an apparent linear gas velocity of 2.0 m / s, a reaction temperature of 550°C, a reaction pressure of 500 kPa, and a floor density of 150 kg / m³. 3 That is the case.

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

[0196] The single-flow 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% low-carbon olefin, 5 wt% hydrogen, 3.2 wt% low-carbon alkane, 5 wt% flammable gas, 8 wt% heavy aromatic hydrocarbon, 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 Figure 1 is employed.

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

[0200] The process conditions in the naphtha-methanol coupling aromatic hydrocarbon preparation reaction zone of the naphtha-methanol coupling aromatic hydrocarbon preparation reactor are: apparent linear gas velocity of 1.2 m / s, reaction temperature of 550°C, reaction pressure of 120 kPa, and floor density of 260 kg / m³. 3 That is the case.

[0201] Regenerated gas is oxygen-enriched air.

[0202] The process conditions for the regeneration zone of the regenerator are: apparent linear gas velocity of 1.2 m / s, regeneration temperature of 650°C, regeneration pressure of 120 kPa, and floor density of 260 kg / m³. 3 That is the case.

[0203] The riser reactor feedstock consists of water vapor and low-carbon alkanes separated from the product gas stream, with a water vapor content of 25 wt%.

[0204] The riser reactor process conditions are an apparent linear gas velocity of 7.0 m / s, a temperature of 630°C, a pressure of 120 kPa, and a floor density of 80 kg / m³. 3 That is the case.

[0205] The bed reactor feedstock consists of C4 and C5 hydrocarbons separated from the product gas stream.

[0206] The process conditions for the light hydrocarbon aromatization reaction zone are an apparent linear gas velocity of 1.2 m / s, a reaction temperature of 580°C, a reaction pressure of 120 kPa, and a floor density of 260 kg / m³. 3 That is the case.

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

[0208] The single-flow 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% low-carbon olefin, 6 wt% hydrogen, 8 wt% low-carbon alkane, 4.5 wt% flammable gas, 5 wt% heavy aromatic hydrocarbon, and 0.5 wt% coke. The p-xylene content in the mixed xylene in the product is 75 wt%.

[0210] (Example 4) In this embodiment, the apparatus shown in Figure 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 unconverted naphtha separated from the product gas stream.

[0212] The process conditions in the naphtha-methanol coupling aromatic hydrocarbon preparation reaction zone of the naphtha-methanol coupling aromatic hydrocarbon preparation reactor are: apparent linear gas velocity of 1.8 m / s, reaction temperature of 590°C, reaction pressure of 200 kPa, and floor density of 220 kg / m³. 3 That is the case.

[0213] The regenerated gas is air.

[0214] The process conditions for the regeneration zone of the regenerator are: apparent linear gas velocity of 1.8 m / s, regeneration temperature of 700°C, regeneration pressure of 200 kPa, and floor density of 220 kg / m³. 3 That is the case.

[0215] The riser reactor feedstock consists of water vapor and low-carbon alkanes separated from the product gas stream, with a water vapor content of 50 wt%.

[0216] The riser reactor process conditions are an apparent linear gas velocity of 5.0 m / s, a temperature of 660°C, a pressure of 200 kPa, and a floor density of 110 kg / m³. 3 That is the case.

[0217] The bed reactor feedstock consists of C4 and C5 hydrocarbons separated from the product gas stream.

[0218] The process conditions for the light hydrocarbon aromatization reaction zone are an apparent linear gas velocity of 1.8 m / s, a reaction temperature of 630°C, a reaction pressure of 200 kPa, and a floor density of 220 kg / m³. 3 That is the case.

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

[0220] The single-flow 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% low-carbon olefin, 5 wt% hydrogen, 6 wt% low-carbon alkane, 4 wt% flammable gas, 4 wt% heavy aromatic hydrocarbon, and 0.9 wt% coke. The p-xylene content in the mixed xylene in the product is 71 wt%.

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

[0223] In this embodiment, the naphtha feedstock 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 feedstock entering the naphtha-methanol coupling aromatic hydrocarbon preparation reactor further includes unconverted naphtha separated from the product gas stream.

[0224] The process conditions in the naphtha-methanol coupling aromatic hydrocarbon preparation reaction zone of the naphtha-methanol coupling aromatic hydrocarbon preparation reactor are: apparent linear gas velocity of 1.0 m / s, reaction temperature of 580°C, reaction pressure of 150 kPa, and floor density of 350 kg / m³. 3 That is the case.

[0225] The regenerated gas is air.

[0226] The process conditions for the regeneration zone of the regenerator are: apparent linear gas velocity of 1.0 m / s, regeneration temperature of 680°C, regeneration pressure of 150 kPa, and floor density of 350 kg / m³. 3 That is the case.

[0227] The riser reactor feedstock consists of water vapor and low-carbon alkanes separated from the product gas stream, with a water vapor content of 40 wt%.

[0228] The riser reactor process conditions are an apparent linear gas velocity of 7.0 m / s, a temperature of 650°C, a pressure of 150 kPa, and a floor density of 80 kg / m³. 3 That is the case.

[0229] The bed reactor feedstock consists of C4 and C5 hydrocarbons separated from the product gas stream.

[0230] The process conditions for the light hydrocarbon aromatization reaction zone are an apparent linear gas velocity of 1.0 m / s, a reaction temperature of 610°C, a reaction pressure of 150 kPa, and a floor density of 350 kg / m³. 3 That is the case.

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

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

[0233] The composition of the product is 71 wt% BTX, 9 wt% low-carbon olefin, 4 wt% hydrogen, 3 wt% low-carbon alkane, 6 wt% flammable gas, 6 wt% heavy aromatic hydrocarbon, and 1.0 wt% coke. The p-xylene content in the mixed xylene in the product is 65 wt%.

[0234] The above are only a few examples of the present application and are not intended to limit the present application in any way. The present application is disclosed in the preferred embodiments described above, but these preferred embodiments are not intended to limit the present application. Any changes or modifications made by a person skilled in the art using the technical content disclosed above without departing from the scope of the technical solutions of the present application are equivalent to equivalent embodiments and all fall within the scope of the technical solutions of the present application. [Brief explanation of the drawing]

[0235] [Figure 1] This is a schematic diagram of an apparatus for preparing aromatic hydrocarbons by coupling naphtha and methanol, according to one embodiment of the present application.

Claims

1. An apparatus for preparing aromatic hydrocarbons by coupling naphtha and methanol, Light hydrocarbon aromaticization reactor, Naphtha-methanol coupling aromatic hydrocarbon preparation reactor, Includes, The light hydrocarbon aromatization reactor is used to introduce the raw materials and high-temperature catalyst. At least one outlet of the light hydrocarbon aromatization reactor is connected to the naphtha-methanol coupling aromatic hydrocarbon preparation reactor in order to transport 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, An apparatus for introducing naphtha and methanol, contacting the naphtha with the catalyst from the light hydrocarbon aromaticization reactor to produce a BTX-containing product gas stream after the reaction, and subjecting the methanol to a methylation reaction with benzene and toluene in the product gas stream to produce p-xylene.

2. The naphtha-methanol coupling aromatic hydrocarbon preparation reactor is divided from top to bottom into at least a first gas-solid separation zone and a naphtha-methanol coupling aromatic hydrocarbon preparation reaction zone. The two aforementioned zones are in communication with each other. The naphtha-methanol coupling aromatic hydrocarbon preparation reaction zone is equipped with a naphtha-methanol coupling aromatic hydrocarbon preparation reactor disperser. The naphtha-methanol coupling aromatic hydrocarbon preparation reactor disperser includes n sub-dispersors, The sequential numbers of the multiple sub-distributors are 1 to n (n ≥ 2) in order from bottom to top. The first sub-disperser is used to introduce naphtha raw material. Apparatus for preparing aromatic hydrocarbons by coupling naphtha and methanol, as described in claim 1, wherein the second sub-disperser to the nth sub-disperser are used to introduce methanol feedstock.

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

4. The aforementioned first gas-solid separation zone is provided with a gas-solid separation apparatus I and a gas collection chamber I. The gas outlet of the gas-solid separation device I is in communication with the gas collection chamber I. The outlet of the gas collection chamber I is in communication with the product gas transport pipe I. The apparatus for preparing aromatic hydrocarbons by coupling naphtha and methanol, according to claim 2, wherein the product gas transport pipe I is used to discharge the BTX-containing product gas flow after gas-solid separation to a downstream processing section.

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

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

7. The light hydrocarbon aromatization reactor is divided from top to bottom into at least a second gas-solid separation zone and a light hydrocarbon aromatization reaction zone. The two aforementioned zones are connected to form a floor reactor. The aforementioned second gas-solid separation zone is equipped with a gas-solid separation apparatus II and a gas collection chamber II. The gas outlet of the gas-solid separation apparatus II is in communication with the gas collection chamber II. An apparatus for preparing aromatic hydrocarbons by coupling naphtha and methanol, according to claim 1 or 2, wherein a bed reactor disperser for introducing bed reactor raw materials is provided above the lower inside of the light hydrocarbon aromaticization reaction zone.

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

9. The bed reactor raw material is C ４ Hydrocarbons and C ５ An apparatus for preparing aromatic hydrocarbons by coupling naphtha and methanol according to claim 7, which contain hydrocarbons.

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 lower inner part of the light hydrocarbon aromatization reaction zone. The apparatus for preparing aromatic hydrocarbons by coupling naphtha and methanol according to claim 7, wherein the catalyst outlet of the gas-solid separation device II is provided above the riser reactor.

11. The apparatus for preparing aromatic hydrocarbons by coupling naphtha and methanol, according to claim 10, wherein the inlet end of the riser reactor is used to introduce the catalyst and riser reactor feedstock.

12. The second gas-solid separation zone is in communication with the first gas-solid separation zone. The apparatus for preparing aromatic hydrocarbons by coupling naphtha and methanol, according to claim 7, wherein the light hydrocarbon aromaticization reaction zone is in communication with the naphtha-methanol coupling aromatic hydrocarbon preparation reaction zone.

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

14. The apparatus for preparing aromatic hydrocarbons by coupling naphtha and methanol according to claim 12, wherein a light hydrocarbon aromaticization slide valve is provided on the pipeline connecting the naphtha-methanol coupling aromatic hydrocarbon preparation reaction zone and the light hydrocarbon aromaticization reaction zone.

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

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

17. The apparatus for preparing aromatic hydrocarbons by coupling naphtha and methanol, as described in claim 7, wherein the gas-solid separation apparatus II is a gas-solid cyclone separator.

18. The apparatus further includes a regenerator, Apparatus for preparing aromatic hydrocarbons by coupling naphtha and methanol according to claim 1 or 10, wherein at least one inlet of the light hydrocarbon aromaticization reactor is connected to the regenerator in order to obtain a high-temperature regenerated catalyst produced by the regenerator.

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

20. The regenerator is divided from top to bottom into at least a third gas-solid separation zone and a regeneration zone. The two aforementioned zones are in communication with each other. The third gas-solid separation zone is equipped with a regenerator gas-solid separation device and a regenerator gas collection chamber. The gas outlet of the regenerator gas-solid separation device is in communication with the regenerator gas collection chamber. An exhaust gas transport pipe is provided above the regenerator gas collection chamber. The apparatus for preparing aromatic hydrocarbons by coupling naphtha and methanol, according to claim 18, wherein a regenerator disperser for introducing regenerated gas is provided above the lower inside of the regeneration zone.

21. The regeneration zone is connected to the riser reactor sequentially via a regeneration 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 apparatus for preparing aromatic hydrocarbons by coupling naphtha and methanol, according to claim 20, wherein the catalyst outlet end of the regenerator gas-solid separation device is located above the open end of the inlet pipe of the regenerator stripper.

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

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

24. At least one outlet of the naphtha-methanol coupling aromatic hydrocarbon preparation reactor is connected to the inlet of the regenerator in order to introduce the spent catalyst produced by the reaction in the naphtha-methanol coupling aromatic hydrocarbon preparation reactor into the regenerator. The apparatus for preparing aromatic hydrocarbons by coupling naphtha and methanol according to claim 1, wherein the regenerator is used to introduce a regenerating gas and convert the spent catalyst into a regenerating catalyst.

25. The naphtha-methanol coupling aromatic hydrocarbon preparation reaction zone is connected to the regenerator inlet via a reactor stripper, a used slide valve, and a used agent transport 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 sub-disperser. The apparatus for preparing aromatic hydrocarbons by coupling naphtha and methanol, according to claim 4, wherein the catalyst outlet end of the gas-solid separation device of the reactor is located above the open end of the inlet pipe of the reactor stripper.

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

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

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

29. The aforementioned metal molecular sieve binary 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 metal modification, comprising the steps of placing the HZSM-5 zeolite molecular sieve in a metal salt solution, immersing it, drying it, and roasting it to obtain the metal-modified HZSM-5 zeolite molecular sieve, according to claim 28, for preparing aromatic hydrocarbons by coupling naphtha and methanol.

30. A step of introducing raw materials and a high-temperature catalyst into the light hydrocarbon aromatization reactor to produce the light hydrocarbon aromatization product gas, A step of introducing naphtha and the catalyst from the light hydrocarbon aromaticization reactor into the naphtha-methanol coupling aromatic hydrocarbon preparation reactor to generate a BTX-containing product gas stream, A step of 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. The process involves removing the spent catalyst contained in all the gas stream generated in the naphtha-methanol coupling aromatic hydrocarbon preparation reactor through a gas-solid separation unit I. The process involves ensuring that the gas flow enters the gas collection chamber I, and then enters the downstream processing section through the product gas transport 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 aromaticization product gas include BTX, low-carbon olefin, and H ２ A method for preparing aromatic hydrocarbons by coupling naphtha and methanol according to claim 30, comprising:

33. The method for preparing aromatic hydrocarbons by coupling naphtha and methanol according to claim 30, wherein the BTX-containing product gas stream further comprises, in addition to BTX, a low-carbon olefin, hydrogen, a low-carbon alkane, a flammable gas, a heavy aromatic hydrocarbon, and unconverted naphtha.

34. The low-carbon olefins mentioned above refer to ethylene and propylene. The low-carbon alkanes mentioned above refer to ethane and propane. The aforementioned flammable gas includes methane and CO, The method for preparing an aromatic hydrocarbon by coupling naphtha and methanol according to claim 33, wherein the heavy aromatic hydrocarbon refers to an aromatic hydrocarbon having 9 or more carbon atoms in its molecule.

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

36. The naphtha also includes unconverted naphtha separated from the product gas stream. The aforementioned unconverted naphtha is C ４ -C １２ A method for preparing aromatic hydrocarbons by coupling naphtha and methanol according to claim 35, comprising linear aliphatic hydrocarbons and branched aliphatic hydrocarbons, as well as naphthenic hydrocarbons, as the main components.

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

38. The process conditions in the naphtha-methanol coupling aromatic hydrocarbon preparation reaction zone of the naphtha-methanol coupling aromatic hydrocarbon preparation reactor are: apparent linear velocity of gas of 0.5 m / s to 2.0 m / s, reaction temperature of 500°C to 600°C, reaction pressure of 100 kPa to 500 kPa, and floor density of 150 kg / m³. ３ ~700 kg / m ３ A method for preparing aromatic hydrocarbons by coupling naphtha and methanol according to claim 30.

39. The light hydrocarbon aromaticization product gas enters the gas-solid separation unit II, where the catalyst contained in the light hydrocarbon aromaticization product gas is removed, then enters the gas collection chamber II, and through the product gas transport pipe II, enters the first gas-solid separation zone of the naphtha-methanol coupling aromatic hydrocarbon preparation reactor. The method for preparing aromatic hydrocarbons by coupling naphtha and methanol according to claim 30, wherein the catalyst in the light hydrocarbon aromaticization reaction zone enters the naphtha-methanol coupling aromatic hydrocarbon preparation reactor through a light hydrocarbon aromaticization slide valve.

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

41. A process of introducing regenerated gas and spent catalyst into a regenerator to obtain a high-temperature regenerated catalyst, A step of transporting the high-temperature regenerating catalyst to the light hydrocarbon aromaticization reactor, A method for preparing aromatic hydrocarbons by coupling naphtha and methanol according to claim 30, further comprising:

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

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

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

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

46. The process conditions for the regeneration zone of the regenerator are: apparent linear velocity of gas of 0.5 m / s to 2.0 m / s, regeneration temperature of 600°C to 750°C, regeneration pressure of 100 kPa to 500 kPa, and floor density of 150 kg / m³. ３ ~700 kg / m ３ A method for preparing aromatic hydrocarbons by coupling naphtha and methanol according to claim 41.

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

48. The exhaust gas enters the third gas-solid separation zone, where the regenerative catalyst contained in the exhaust gas is removed. This is a method for preparing aromatic hydrocarbons by coupling naphtha and methanol according to claim 47, wherein the exhaust gas first enters a regenerator gas-solid separator, the regenerator catalyst contained in the exhaust gas is removed, and then the exhaust gas passes through a regenerator gas collection chamber and an exhaust gas transport pipe to enter a downstream processing section.

49. The method for preparing aromatic hydrocarbons by coupling naphtha and methanol according to claim 41, wherein the regenerating catalyst enters the light hydrocarbon aromatic reactor through a regenerating stripper and a regenerating slide valve.

50. A step of introducing riser reactor raw materials to the inlet end of the riser reactor of the light hydrocarbon aromatization reactor, A step of introducing the regenerating catalyst into the riser reactor through a regenerating stripper and a regenerating slide valve, A step of converting the riser reactor raw material into a BTX-containing stream under the action of the regenerating catalyst, The step of causing the BTX-containing flow to enter the lower inner part of the light hydrocarbon aromatization reaction zone in the bed reactor through the 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 materials are, Water vapor and, A low-carbon alkane separated from the gaseous flow of the aforementioned product, A method for preparing aromatic hydrocarbons by coupling naphtha and methanol according to claim 50, comprising:

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

53. The process conditions for the riser reactor are an apparent linear velocity of 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 floor density of 50 kg / m³. ３ ~150 kg / m ３ A method for preparing aromatic hydrocarbons by coupling naphtha and methanol according to claim 50.

54. A step of introducing a catalyst to the 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:

55. A method for preparing aromatic hydrocarbons by coupling naphtha and methanol according to claim 54, further comprising the step of introducing bed reactor raw materials into the light hydrocarbon aromaticization reaction zone through a bed reactor disperser and contacting them with the catalyst from the riser reactor to produce the light hydrocarbon aromaticization product gas.

56. The bed reactor raw material is C ４ Hydrocarbons and C ５ A method for preparing aromatic hydrocarbons by coupling naphtha and methanol according to claim 54, which include hydrocarbons.

57. Said C ４ Hydrocarbons and the C ５ Hydrocarbons are C separated from the product gas stream. ４ Hydrocarbons and C ５ A method for preparing aromatic hydrocarbons by coupling the naphtha and methanol according to claim 56, which are derived from hydrocarbons.

58. The components of the BTX-containing stream include BTX, low-carbon olefin, and H ２ A method for preparing aromatic hydrocarbons by coupling naphtha and methanol according to claim 50, comprising:

59. A method for preparing aromatic hydrocarbons by coupling naphtha and methanol according to claim 30, further comprising the steps of introducing the spent catalyst in the naphtha-methanol coupling aromatic hydrocarbon preparation reaction zone into a reactor stripper, and after stripping, allowing the spent catalyst to enter the downstream area through a spent slide valve and a spent agent transport pipe.

60. The downstream area is a regenerator, a method for preparing aromatic hydrocarbons by coupling naphtha and methanol according to claim 59.

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