Apparatus and method for producing aromatics from naphtha

Abstract

This application discloses an apparatus and method for producing aromatic compounds from naphtha. The apparatus for producing aromatic compounds from naphtha includes a naphtha-to-aromatic compounds reactor, a regenerator, and a light hydrocarbon aromatization reactor. The method for producing aromatic compounds from naphtha uses a bifunctional metal molecular sieve catalyst. The naphtha is converted into a product gas containing aromatic compounds, low-carbon alkanes, and other components through the action of the catalyst in the naphtha-to-aromatic compounds reactor. The low-carbon alkanes and C3, C4, and C5 hydrocarbons separated from the product gas enter the light hydrocarbon aromatization reactor and are further converted into aromatic compounds. This method can convert linear and branched aliphatic hydrocarbons to aromatic compounds with high selectivity, and the content of paraxylene in a mixture of ethylbenzene and xylene exceeds 50 wt%. The apparatus for producing aromatic compounds from naphtha of this application includes a high-temperature light hydrocarbon aromatization reactor and a relatively low-temperature naphtha-to-aromatic compounds reactor, thereby achieving the beneficial effects of reducing the yield of low-carbon alkanes and improving the yield of aromatic compounds.

Description

[Technical Field]

[0001] The present application relates to a fluidized bed apparatus and a method for using the same, and more particularly to an apparatus and a method for producing aromatics from naphtha, which belongs to the field of chemical engineering technology. [Background technology]

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

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

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

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

[0006] The present application provides an apparatus for producing aromatics from naphtha and a method for producing aromatics from naphtha, in order to produce aromatics using naphtha with a low aromatic potential content as a raw material, increase the content of para-xylene in mixed xylenes, and reduce production energy consumption. [Means for solving the problem]

[0007] According to one aspect of the present application, there is provided an apparatus for producing aromatics from naphtha, the apparatus including a reactor for producing aromatics from naphtha, a regenerator, and a light hydrocarbon aromatization reactor.

[0008] An apparatus for producing aromatics from naphtha, the apparatus including a naphtha aromatics reactor, a regenerator, and a light hydrocarbon aromatization reactor; The naphtha aromatic reactor is connected to a regenerator through a spent agent transport pipe I, and the regenerator is connected to the naphtha aromatic reactor through a regenerant transport pipe; The light hydrocarbon aromatization reactor comprises a lift tube reactor, and the lift tube reactor is connected to a bed reactor; The regenerator is connected to the lift pipe reactor via a regeneration slide valve II; The bed reactor is connected to the regenerator via a spent agent transport pipe II.

[0009] Optionally, a gas-solid separation section is provided in the upper part of the naphtha aromatics reactor, and a product gas transport pipe I is provided in the gas-solid separation section; The naphtha aromatics reactor is provided at the bottom with a reaction zone for producing aromatics from naphtha, and a regenerant transport pipe transports catalyst to the reaction zone for producing aromatics from naphtha. Below the reaction section where aromatics are produced from naphtha, a naphtha aromatics reactor distributor is provided for passing the naphtha feedstock.

[0010] Optionally, the naphtha aromatic reactor is further provided with a gas-solid separator I and a gas collection chamber I, the gas collection chamber I is located at the top of the gas-solid separation section, the gas outlet of the gas-solid separator I is connected to the gas collection chamber I, and the gas collection chamber I is connected to the product gas transport pipe I.

[0011] Optionally, a stripper I is provided below the naphtha-produced aromatics reaction section, and the reaction section for producing aromatics from naphtha is connected to a spent agent transport pipe I via the stripper I.

[0012] Optionally, the stripper I is connected to a spent agent transport line I via a spent slide valve I.

[0013] Optionally, the gas-solid separation device I uses one or more sets of gas-solid cyclone separators, each set of gas-solid cyclone separators including a first-class gas-solid cyclone separator and a second-class gas-solid cyclone separator.

[0014] Optionally, a gas-solid separation section of the regenerator is provided above the regenerator, and an exhaust gas transport pipe is provided in the gas-solid separation section of the regenerator.

[0015] The regenerator is provided with a regeneration section at the bottom, and the spent catalyst transport pipes I and II are used to transport the spent catalyst to the regeneration section. The regenerator is provided with a regenerator distributor at the bottom to allow the regeneration gas to pass through.

[0016] The regenerant transport pipe transports the regenerated catalyst from the regeneration section to the naphtha aromatics reactor, and the regeneration slide valve II transports the regenerated catalyst to the lift pipe reactor.

[0017] Optionally, the regenerator housing is further provided with a regenerator gas-solid separation device and a regenerator gas collection chamber, the regenerator gas collection chamber is located at the top of the regenerator gas-solid separation section, the gas outlet of the regenerator gas-solid separation device is connected to the regenerator gas collection chamber, and the regenerator gas collection chamber is connected to an exhaust gas transport pipe.

[0018] Optionally, a regenerator stripper is provided below the regenerator section, and the regenerator section is connected to the regenerator slide valve I and the regenerator slide valve II via the regenerator stripper.

[0019] Optionally, the regeneration slide valve I is connected to the naphtha aromatics reactor through a regenerant transport pipe, and the regeneration slide valve II is connected to the lift pipe reactor.

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

[0021] Optionally, a gas-solid separation section of the bed reactor is provided on the upper part of the bed reactor, and a product gas transport pipe II is provided in the gas-solid separation section of the bed reactor.

[0022] A light hydrocarbon aromatization reaction zone is provided at the bottom of the bed reactor, and a bed reactor distributor is provided at the lower part of the light hydrocarbon aromatization reaction zone. The bed reactor distributor is used to pass the bed reactor raw material, and the upper end of the lift pipe reactor penetrates the bottom of the bed reactor and is inserted axially into the bed reactor.

[0023] The regeneration slide valve II introduces catalyst into the feed inlet end of the lift tube reactor.

[0024] Optionally, the gas-solid separation section of the bed reactor is provided with a gas-solid separator II and a gas collection chamber II, the gas outlet of the gas-solid separator II is connected to the gas collection chamber II, the catalyst outlet of the gas-solid separator II is located in the light hydrocarbon aromatization reaction section, and the gas collection chamber II is connected to a product gas transport pipe II located outside the bed reactor.

[0025] Optionally, a stripper II is connected to the light hydrocarbon aromatization reaction zone, and the bed reactor is connected to a spent agent transport pipe II through the stripper II.

[0026] Optionally, the stripper II is connected to a spent agent transport pipe II via a spent slide valve II.

[0027] Optionally, the gas-solid separator II is a gas-solid cyclone separator, and the catalyst outlet of the gas-solid separator II is located above the outlet end of the lift tube reactor.

[0028] This application proposes a method for producing aromatics from naphtha using the above-mentioned apparatus, and employs a metal molecular sieve bifunctional catalyst as the catalyst. A feedstock containing naphtha is introduced into a naphtha aromatics reactor, a lift tube reactor feedstock containing low carbon alkanes is introduced into the lift tube reactor, a bed reactor feedstock containing C3, C4, and C5 hydrocarbons is introduced into the bed reactor, and a regeneration gas is introduced into the regenerator; The naphtha aromatic reactor and the bed reactor output product gas, and the spent catalyst is introduced into the regenerator through the spent agent transport pipe I and the spent agent transport pipe II. The spent catalyst is reacted with the regeneration gas in the regenerator to be regenerated, and then transported to the naphtha aromatic reactor and the lift pipe reactor, and the regenerator discharges exhaust gas.

[0029] The catalyst uses a metal-modified HZSM-5 zeolite molecular sieve, and the metal used for the metal modification is at least one selected from La, Zn, Ga, Fe, Mo, and Cr; The metal modification method is to immerse the HZSM-5 zeolite molecular sieve in a metal salt solution, dry, and calcinate it to obtain the metal-modified HZSM-5 zeolite molecular sieve.

[0030] The naphtha is at least one selected from direct coal liquefaction naphtha, indirect coal liquefaction naphtha, straight-run naphtha, and hydrocracked naphtha.

[0031] The naphtha-containing feedstock further includes unreacted naphtha separated from the product gas stream, and the unreacted naphtha is a C4 to C6 12 straight-chain, branched aliphatic hydrocarbons, and naphthenes.

[0032] The reaction conditions for the naphtha aromatics reaction section are: gas apparent linear velocity 0.5-2.0 m / s, reaction temperature 500-650°C, reaction pressure 100-500 kPa, bed density 150-700 kg / m 3 is.

[0033] Optionally, the gas apparent linear velocity is independently selected from any value of 0.5 m / s, 0.6 m / s, 0.7 m / s, 0.8 m / s, 0.9 m / s, 1.0 m / s, 1.1 m / s, 1.2 m / s, 1.3 m / s, 1.4 m / s, 1.5 m / s, 1.6 m / s, 1.7 m / s, 1.8 m / s, 1.9 m / s, 2.0 m / s, or a range of any two values.

[0034] Optionally, the reaction temperature is independently selected from any value or range of any two values ​​of 500°C, 520°C, 530°C, 540°C, 550°C, 560°C, 570°C, 580°C, 590°C, 600°C, 610°C, 620°C, 630°C, 640°C, 650°C.

[0035] Alternatively, the reaction pressure is independently selected from any value or range of any two values ​​of 100 kPa, 125 kPa, 150 kPa, 175 kPa, 200 kPa, 225 kPa, 250 kPa, 275 kPa, 300 kPa, 325 kPa, 350 kPa, 375 kPa, 400 kPa, 425 kPa, 450 kPa, 475 kPa, 500 kPa.

[0036] Optionally, the bed density is 150 kg / m 3 , 200 kg / m 3 , 250 kg / m 3 , 300 kg / m 3 , 350 kg / m 3 , 400 kg / m 3 , 450 kg / m 3 , 500 kg / m 3 , 550 kg / m 3 , 600 kg / m 3 , 650 kg / m 3 , 700 kg / m 3 Independently select any value or range of any two values.

[0037] Optionally, the carbon content in the regenerated catalyst is 0.5 wt% or less.

[0038] The regeneration gas is at least one selected from oxygen, air, and oxygen-enriched air.

[0039] The process conditions for the regeneration zone are: gas apparent linear velocity 0.5-2.0 m / s, regeneration temperature 600-750°C, regeneration pressure 100-500 kPa, bed density 150-700 kg / m 3 is.

[0040] Optionally, the gas apparent linear velocity is independently selected from any value of 0.5 m / s, 0.6 m / s, 0.7 m / s, 0.8 m / s, 0.9 m / s, 1.0 m / s, 1.1 m / s, 1.2 m / s, 1.3 m / s, 1.4 m / s, 1.5 m / s, 1.6 m / s, 1.7 m / s, 1.8 m / s, 1.9 m / s, 2.0 m / s, or a range of any two values.

[0041] Optionally, the regeneration temperature is independently selected from any value or range of any two values ​​of 600°C, 615°C, 630°C, 645°C, 670°C, 685°C, 700°C, 715°C, 730°C, 745°C, 750°C.

[0042] Optionally, the regeneration pressure is independently selected from any value or range of any two values ​​of 100 kPa, 125 kPa, 150 kPa, 175 kPa, 200 kPa, 225 kPa, 250 kPa, 275 kPa, 300 kPa, 325 kPa, 350 kPa, 375 kPa, 400 kPa, 425 kPa, 450 kPa, 475 kPa, 500 kPa.

[0043] Optionally, the bed density is 150 kg / m 3 , 200 kg / m 3 , 250 kg / m 3 , 300 kg / m 3 , 350 kg / m 3 , 400 kg / m 3 , 450 kg / m 3 , 500 kg / m 3 , 550 kg / m 3 , 600 kg / m 3 , 650 kg / m 3 , 700 kg / m 3 Independently select any value or range of any two values.

[0044] The lift tube reactor feed further contains water vapor, and the water vapor content in the lift tube reactor feed is 0 to 80 wt%.

[0045] The low carbon alkanes in the lift tube reactor feed are separated from the product gas stream.

[0046] The process conditions of the lift tube reactor are: apparent linear velocity of 3.0 to 10.0 m / s; temperature of 580 to 700°C; Pressure: 100-500kPa, bed density: 50-150kg / m 3 is.

[0047] Optionally, the gas apparent linear velocity is independently selected from any value or range of any two values ​​of 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, 10.0 m / s.

[0048] Optionally, the temperature is independently selected from any value or range of any two values ​​of 580°C, 590°C, 600°C, 610°C, 620°C, 630°C, 640°C, 650°C, 660°C, 670°C, 680°C, 690°C, 700°C.

[0049] Optionally, the pressure is independently selected from any value or range of any two values ​​of 100 kPa, 125 kPa, 150 kPa, 175 kPa, 200 kPa, 225 kPa, 250 kPa, 275 kPa, 300 kPa, 325 kPa, 350 kPa, 375 kPa, 400 kPa, 425 kPa, 450 kPa, 475 kPa, 500 kPa.

[0050] Optionally, the bed density is 50 kg / m 3 , 60 kg / m 3 , 70 kg / m 3 , 80 kg / m 3 , 90kg / m 3, 100 kg / m 3 , 110 kg / m 3 , 120 kg / m 3 , 130 kg / m 3 , 140 kg / m 3 , 150 kg / m 3 Independently select any value or range of any two values.

[0051] Optionally, the bed reactor feed comprises C3, C4 and C5 hydrocarbons.

[0052] Optionally, the C3, C4, and C5 hydrocarbons are separated from the product gas stream.

[0053] Optionally, the bed reactor feed comprises C4 and C5 hydrocarbons.

[0054] Optionally, the C4 and C5 hydrocarbons are separated from the product gas stream.

[0055] The process conditions for the light hydrocarbon aromatization reaction zone are: gas apparent linear velocity of 0.5-2.0 m / s, reaction temperature of 550-665°C, reaction pressure of 100-500 kPa, bed density of 150-700 kg / m 3 is.

[0056] Optionally, the gas apparent linear velocity is independently selected from any value of 0.5 m / s, 0.6 m / s, 0.7 m / s, 0.8 m / s, 0.9 m / s, 1.0 m / s, 1.1 m / s, 1.2 m / s, 1.3 m / s, 1.4 m / s, 1.5 m / s, 1.6 m / s, 1.7 m / s, 1.8 m / s, 1.9 m / s, 2.0 m / s, or a range of any two values.

[0057] Optionally, the reaction temperature is independently selected from any value or range of any two values ​​of 550°C, 560°C, 570°C, 580°C, 590°C, 600°C, 610°C, 620°C, 630°C, 640°C, 650°C, 660°C, 665°C.

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

[0059] Optionally, the bed density is 150 kg / m 3 , 200 kg / m 3 , 250 kg / m 3 , 300 kg / m 3 , 350 kg / m 3 , 400 kg / m 3 , 450 kg / m 3 , 500 kg / m 3 , 550 kg / m 3 , 600 kg / m 3 , 650 kg / m 3 , 700 kg / m 3 Independently select any value or range of any two values.

[0060] introducing naphtha through a naphtha aromatics reactor distributor into a naphtha aromatics reaction section of the naphtha aromatics reactor and contacting the naphtha with the catalyst from the regenerator to produce a product gas stream containing BTX, light olefins, hydrogen, light alkanes, combustible gases, heavy aromatics, and unreacted naphtha, and the catalyst is coked and converted to spent catalyst; The regeneration gas is introduced into the regeneration section of the regenerator through the regenerator distributor and contacted with the spent catalyst from the naphtha aromatics reactor and the spent catalyst from the light hydrocarbon aromatization reactor, and the coke on the spent catalyst reacts with the regeneration gas to produce exhaust gas, and the spent catalyst is converted into regenerated catalyst; The feedstock for the lift tube reactor is introduced into the lift tube reactor through the inlet end of the lift tube reactor, and is brought into contact with and reacted with the regenerated catalyst from the regenerator. The feedstock for the lift tube reactor is converted into a stream containing BTX, low-carbon olefins, and H2 through the action of the catalyst, and then introduced into the lower part of the light hydrocarbon aromatization reaction zone of the bed reactor through the outlet end of the lift tube reactor. The bed reactor feedstock is introduced into the light hydrocarbon aromatization reaction zone through the bed reactor distributor and contacted with the catalyst from the lift tube reactor to produce a light hydrocarbon aromatization product gas containing BTX, low carbon olefins, and H2, and the catalyst is coked and converted into spent catalyst.

[0061] Optionally, the product gas stream enters a gas-solid separator I to remove interposed spent catalyst, and then enters a gas collection chamber I and enters downstream processes via product gas delivery line I.

[0062] The spent catalyst from the naphtha aromatic reaction section enters the stripper I through the open end of the stripper I inlet pipe, undergoes stripping treatment, and then enters the downstream section through the spent slide valve I and the spent agent transport pipe I after stripping treatment.

[0063] Specifically, the downstream section is a regenerator.

[0064] The low carbon olefins refer to ethylene and propylene.

[0065] The low carbon alkanes refer to ethane and propane.

[0066] The combustible gases include methane and CO.

[0067] The heavy aromatic compounds refer to aromatic compounds having 9 or more carbon atoms in the molecule.

[0068] Optionally, the method includes the following: the spent catalyst in the naphtha-based aromatic reaction zone passes through a stripper I, a spent slide valve I and a spent agent transport pipe I in order into a regenerator, and reacts with the regeneration gas to obtain exhaust gas and regenerated catalyst; Optionally, the method includes the following: the spent catalyst in the light hydrocarbon aromatization reaction zone passes through a stripper II, a spent slide valve II and a spent agent transport pipe II in order into a regenerator, and contacts and reacts with a regeneration gas to obtain an exhaust gas and a regenerated catalyst; The exhaust gas enters the regenerator's gas-solid separator where entrained regenerated catalyst is removed, then enters the regenerator's gas collection chamber and passes through an exhaust gas transport pipe to downstream processes.

[0069] Optionally, the regenerated catalyst passes through the regenerator stripper, regeneration slide valve I, and regenerant transport line into the naphtha aromatics reactor.

[0070] Optionally, the regenerated catalyst passes through the regenerator stripper and regeneration slide valve II in sequence into the light hydrocarbon aromatization reactor.

[0071] Optionally, the product gas of the light hydrocarbon aromatization enters a gas-solid separator II, where the entrained catalyst is removed, and then enters a gas collection chamber II and passes through a product gas transport pipe II into downstream processes.

[0072] The catalyst in the light hydrocarbon aromatization reaction zone enters the downstream region through Stripper II, spent slide valve II and spent agent transport line II.

[0073] Specifically, the downstream region is a regenerator.

[0074] The naphtha components in this application are C4-C 12 These include straight-chain, branched aliphatic hydrocarbons, cyclic alkanes and aromatic compounds.

[0075] The aromatic compounds in this application refer to benzene, toluene, and xylene, collectively referred to as BTX.

[0076] In the method described in the present application, the aromatic potential content of the naphtha feedstock is 0-80 wt%, the naphtha turnover rate is 70-95 wt%, the unconverted naphtha is separated from the product gas and returned to the naphtha aromatics reactor as feedstock, some low-carbon alkanes are separated from the product gas and returned to the lift tube reactor of the light hydrocarbon aromatization reactor as feedstock, and C3, C4, and C5 hydrocarbons are separated from the product gas and returned to the bed reactor of the light hydrocarbon aromatization reactor as feedstock, and the final product composition is as follows: 60-75 wt% BTX, 6-14 wt% low-carbon olefins, 3-7 wt% hydrogen, 3-8 wt% low-carbon alkanes, 4-6 wt% combustible gas, 4-8 wt% heavy aromatic compounds, and 0.5-1 wt% coke. The content of para-xylene in the mixed xylenes in the product is 50-65 wt%. [Effects of the Invention]

[0077] 1) The method for producing aromatic compounds from naphtha described in the present application can convert linear and branched aliphatic hydrocarbons into aromatic compounds with high selectivity, and therefore has a wide range of applicable raw materials, and aromatic compounds can be produced using naphtha with a low aromatic potential content as a raw material. 2) This application realizes the aromatization of low-carbon alkanes, C4 and C5 hydrocarbons by using a light hydrocarbon aromatization reactor and a bifunctional catalyst of metal-containing zeolite, thereby significantly improving the aromatic yield of the technology for producing aromatic compounds from naphtha. 3) In the aromatic products produced by this application, the paraxylene content in the xylene mixture exceeds 50 wt%, which is significantly higher than the thermodynamic equilibrium content (about 24 wt%), effectively improving the yield of paraxylene and significantly reducing the energy required for separating paraxylene. 4) The naphtha aromatics unit of the present application includes a naphtha aromatics reactor and a light hydrocarbon aromatization reactor. Low-carbon alkanes are very stable and require high reaction temperatures. In the naphtha aromatics unit of the present application, the temperature of the light hydrocarbon aromatization reactor is higher than that of the naphtha aromatics reactor. Low-carbon alkanes, C4, and C5 hydrocarbons contact a catalyst in the light hydrocarbon aromatization reactor, where an aromatization reaction occurs, improving the reaction rate and aromatics yield. Meanwhile, naphtha contacts a catalyst in the naphtha aromatics reactor, where an aromatization reaction occurs, but the low reaction temperature reduces the naphtha coking rate. The naphtha aromatics unit of the present application achieves the beneficial effects of reducing the yield of low-carbon alkanes and improving the aromatics yield by providing a high-temperature light hydrocarbon aromatization reactor and a relatively low-temperature naphtha aromatics reactor, respectively. [Brief explanation of the drawings]

[0078] [Figure 1] FIG. 1 illustrates an apparatus for producing aromatics from naphtha according to an embodiment of the present application. DETAILED DESCRIPTION OF THE INVENTION

[0079] The present application will be described in detail below with reference to embodiments, but is not limited to these embodiments.

[0080] Possible embodiments are described below. The present application provides an apparatus for producing aromatic hydrocarbons from naphtha. As shown in Figure 1, the apparatus includes a naphtha aromatics reactor 1, a regenerator 2, and a light hydrocarbon aromatization reactor 3.

[0081] The naphtha aromatics reactor 1 includes: a naphtha aromatics reactor housing 1-1, a naphtha aromatics reactor distributor 1-2, a gas-solid separator I1-3, a gas collection chamber I1-4, a product gas transport pipe I1-5, a stripper I1-6, a spent sliding valve I1-7, and a spent agent transport pipe I1-8.

[0082] The naphtha aromatics reactor housing 1-1 includes an upper naphtha aromatics reactor housing and a lower naphtha aromatics reactor housing. The upper naphtha aromatics reactor housing encloses a gas-solid separation region, and the lower naphtha aromatics reactor housing encloses a naphtha aromatics reaction region. The naphtha aromatics reactor housing is provided with an outlet for a regenerant transport pipe 2-8.

[0083] A naphtha aromatics reactor distributor 1-2 is provided below the naphtha aromatics reaction zone, and this naphtha aromatics reactor distributor 1-2 is used to introduce naphtha raw material.

[0084] The naphtha aromatics reactor housing 1-1 also includes a gas-solid separator I1-3 and a gas collection chamber I1-4. The gas collection chamber I1-4 is located inside the upper part of the naphtha aromatics reactor housing. The gas outlet of the gas-solid separator I1-3 is connected to the gas collection chamber I1-4, which is connected to the product gas transport pipe I1-5. The catalyst outlet end of the gas-solid separator I1-3 is located above the open end of the inlet pipe of the stripper I1-6.

[0085] A stripper I1-6 is provided below the naphtha aromatics reaction zone. The inlet of the stripper I1-6 is located inside the naphtha aromatics reactor housing 1-1, and its outlet is located outside the naphtha aromatics reactor housing 1-1 and connected to a used slide valve I1-7. The open end of the inlet of the stripper I1-6 is located above the naphtha aromatics reactor distributor 1-2.

[0086] A spent slide valve I1-7 is provided below the stripper I1-6. The inlet of the spent slide valve I1-7 is connected to the outlet of the stripper I1-6, and the outlet of the spent slide valve I1-7 is connected to the inlet of a spent agent transport pipe I1-8, and the outlet of the spent agent transport pipe I1-8 is connected to the regenerator housing 2-1.

[0087] The spent slide valve I1-7 is used to control the circulation rate of spent catalyst.

[0088] In a preferred embodiment, the gas-solid separation device I1-3 employs one or more sets of gas-solid cyclone separators, each set of gas-solid cyclone separators including a first-class gas-solid cyclone separator and a second-class gas-solid cyclone separator.

[0089] The regenerator 2 includes: a regenerator housing 2-1, a regenerator distributor 2-2, a regenerator gas-solid separator 2-3, a regenerator gas collection chamber 2-4, an exhaust gas transport pipe 2-5, a regenerator stripper 2-6, a regenerator slide valve I 2-7, a regenerant transport pipe 2-8, and a regenerator slide valve II 2-9.

[0090] The regenerator housing 2-1 includes an upper regenerator housing and a lower regenerator housing. The upper regenerator housing encloses the gas-solid separation region, and the lower regenerator housing encloses the regeneration region. The regenerator housing 2-1 is provided with outlets for the spent reagent transport pipes I1-8 and II3-11.

[0091] A regenerator distributor 2-2 is provided at the bottom of the regeneration zone, and this regenerator distributor 2-2 is used to introduce the regeneration gas.

[0092] The regenerator housing 2-1 also contains a regenerator gas-solid separator 2-3 and a regenerator gas collection chamber 2-4. The regenerator gas collection chamber 2-4 is located at the top of the inside of the regenerator housing 2-1. The gas outlet of the regenerator gas-solid separator 2-3 communicates with the regenerator gas collection chamber 2-4, which in turn communicates with an exhaust gas transport pipe 2-5. The catalyst outlet end of the regenerator gas-solid separator 2-3 is located above the open end of the inlet pipe of the regenerator stripper 2-6.

[0093] Below the regeneration zone, a regenerator stripper 2-6 is provided. The inlet of the regenerator stripper 2-6 is located inside the regenerator housing 2-1, and its outlet is located outside the regenerator housing 2-1 and connected to the regeneration slide valves I2-7 and II2-9. The open end of the inlet of the regenerator stripper 2-6 is located above the regenerator distributor 2-2.

[0094] The regenerator slide valve I2-7 is connected to the inlet of the regenerator transport pipe 2-8, and the outlet of the regenerator transport pipe 2-8 is connected to the naphtha aromatic reactor housing 1-1. The regenerator slide valve I2-7 is used to control the circulation amount of the regenerated catalyst.

[0095] The regeneration slide valve II2-9 is also used to control the amount of regenerated catalyst circulated.

[0096] In a preferred embodiment, the regenerator gas-solid separator 2-3 employs one or more sets of gas-solid cyclone separators, each set of gas-solid cyclone separators including a first-class gas-solid cyclone separator and a second-class gas-solid cyclone separator.

[0097] The light hydrocarbon aromatization reactor 3 includes: a lift tube reactor inlet end 3-1, a lift tube reactor middle section 3-2, a lift tube reactor outlet end 3-3, a bed reactor housing 3-4, a bed reactor distributor 3-5, a gas-solid separator II3-6, a gas collection chamber II3-7, a product gas transport pipe II3-8, a stripper II3-9, a spent sliding valve II3-10, and a spent agent transport pipe II3-11.

[0098] The bed reactor housing 3-4 includes an upper bed reactor housing and a lower bed reactor housing. The upper bed reactor housing surrounds the gas-solid separation zone, and the lower bed reactor housing surrounds the light hydrocarbon aromatization reaction zone. A bed reactor distributor 3-5 is installed at the bottom inside the light hydrocarbon aromatization reaction zone. The upper section of the lift tube reactor penetrates the bottom of the bed reactor and is axially inserted into the bed reactor, and the outlet end 3-3 of the lift tube reactor is located at the bottom inside the light hydrocarbon aromatization reaction zone.

[0099] The gas-solid separation zone of the bed reactor is equipped with a gas-solid separator II3-6 and a gas collection chamber II3-7. The gas outlet of the gas-solid separator II3-6 is connected to the gas collection chamber II3-7, and the catalyst outlet of the gas-solid separator II3-6 is located in the light hydrocarbon aromatization reaction zone. The gas collection chamber II3-7 is connected to the product gas transport pipe II3-8 outside the bed reactor.

[0100] The stripper II3-9 and the spent sliding valve II3-10 are provided outside the bed reactor housing. The inlet of the stripper II3-9 is located in the lower bed reactor housing, and its outlet is connected to the inlet of the spent sliding valve II3-10. The outlet of the spent sliding valve II3-10 is connected to the inlet of the spent agent transport pipe II3-11, and the outlet of the spent agent transport pipe II3-11 is connected to the regenerator housing 2-1.

[0101] In a preferred embodiment, the gas-solid separator II3-6 is a gas-solid cyclone separator, and the catalyst outlet of the gas-solid separator II3-6 is located above the outlet end 3-3 of the lift tube reactor.

[0102] In a preferred embodiment, a gas collection chamber II3-7 is provided at the top inside the bed reactor.

[0103] In a preferred embodiment, the bed reactor distributor 3-5 is used to introduce the bed reactor feed.

[0104] In a preferred embodiment, the lift tube reactor inlet end 3-1 is piped to a regeneration slide valve II 2-9.

[0105] In a preferred embodiment, the lift tube reactor inlet end 3-1 is used to introduce catalyst and lift tube reactor feed.

[0106] In order to achieve aromatization of linear and branched aliphatic hydrocarbons, increase the yield of aromatic hydrocarbons, and increase the para-xylene content in mixed xylenes, the present application provides a method for producing aromatic hydrocarbons from naphtha using any of the above-mentioned apparatuses and a metal zeolite bifunctional catalyst.

[0107] The catalyst is a metal-modified HZSM-5 zeolite molecular sieve, where the metal used for metal modification is selected from at least one of La, Zn, Ga, Fe, Mo, and Cr.

[0108] The method of metal modification involves soaking the HZSM-5 zeolite molecular sieve in a metal salt solution, drying and calcining to obtain the metal-modified HZSM-5 zeolite molecular sieve.

[0109] The method comprises the steps of: a) Naphtha enters the naphtha aromatics reaction zone of the naphtha aromatics reactor 1 through the naphtha aromatics reactor distributor 1-2 and contacts the catalyst from the regenerator 2 to produce a product gas stream containing BTX, low-carbon olefins, hydrogen, low-carbon alkanes, combustible gases, heavy aromatic hydrocarbons, and unconverted naphtha. Simultaneously, the catalyst is coked and converted into spent catalyst. The product gas stream enters the gas-solid separator I1-3, where the entrained spent catalyst is removed. The product gas stream then enters the gas collection chamber I1-4 and is sent to downstream processes via the product gas transport pipe I1-5. The spent catalyst from the naphtha aromatics reaction zone enters the stripper I1-6 through the open end of its inlet pipe, undergoes stripping, and then enters the regenerator 2 via the spent slide valve I1-7 and the spent catalyst transport pipe I1-8. b) The regeneration gas is supplied to the regeneration zone of the regenerator 2 through the regenerator distributor 2-2 and contacts the spent catalyst. This contact causes the coke on the spent catalyst to react with the regeneration gas, producing smoke and converting the spent catalyst into regenerated catalyst. The generated smoke is introduced into the regenerator gas-solid separator 2-3 to separate the accompanying regenerated catalyst, then flows into the regenerator gas collection chamber 2-4 and is sent to the downstream process through the exhaust gas transport pipe 2-5. The regenerated catalyst is supplied to the naphtha aromatics reactor 1 via the regenerator stripper 2-6, the regeneration slide valve I2-7, and the regenerant transport pipe 2-8. The regenerated catalyst is also supplied to the light hydrocarbon aromatization reactor 3 via the regenerator stripper 2-6 and the regeneration slide valve II2-9. c) The lift tube reactor feedstock is fed to the lift tube reactor through the lift tube reactor inlet end 3-1 and reacts with the regenerated catalyst supplied from the regenerator. This reaction converts the lift tube reactor feedstock into a stream containing components such as BTX, low-carbon olefins, and H2, which is then introduced into the lower part of the light hydrocarbon aromatization reaction zone in the bed reactor through the lift tube reactor outlet end 3-3. Meanwhile, the bed reactor feedstock is fed to the light hydrocarbon aromatization reaction zone through the bed reactor distributor 3-5 and contacts the catalyst supplied from the lift tube reactor to produce a light hydrocarbon aromatization product gas containing components such as BTX, low-carbon olefins, and H2. The produced light hydrocarbon aromatization product gas is introduced into the gas-solid separator II3-6 to separate the entrained catalyst, then flows into the gas collection chamber II3-7 and is sent to downstream processes through the product gas transport pipe II3-8. The catalyst in the light hydrocarbon aromatization reaction zone is sent to the regenerator 2 via a stripper II3-9, a spent slide valve II3-10, and a spent agent transport pipe II3-11.

[0110] The low carbon olefins refer to ethylene and propylene.

[0111] The low carbon alkanes refer to ethane and propane.

[0112] The combustible gases include methane and CO, among others.

[0113] The heavy aromatic hydrocarbons refer to aromatic hydrocarbons having 9 or more carbon atoms in the molecule.

[0114] In a preferred embodiment, the naphtha is at least one selected from direct coal liquefaction naphtha, indirect coal liquefaction naphtha, straight-run naphtha, and hydrocracked naphtha.

[0115] In a preferred embodiment, the naphtha further comprises unconverted naphtha separated from the product gas stream.

[0116] In a preferred embodiment, the process conditions in the naphtha aromatics reaction zone are: apparent linear velocity of gas of 0.5 to 2.0 m / s, reaction temperature of 500 to 650°C, reaction pressure of 100 to 500 kPa, and bed density of 150 to 700 kg / m 3 is.

[0117] In a preferred embodiment, the carbon content in the regenerated catalyst is 0.5 wt% or less.

[0118] In a preferred embodiment, the regeneration gas is at least one selected from oxygen, air, and oxygen-enriched air.

[0119] In a preferred embodiment, the process conditions in the regeneration zone are a gas apparent linear velocity of 0.5 to 2.0 m / s, a regeneration temperature of 600 to 750°C, a regeneration pressure of 100 to 500 kPa, and a bed density of 150 to 700 kg / m 3 is.

[0120] In a preferred embodiment, the lift tube reactor feed comprises steam and lower carbon alkanes separated from the product gas stream.

[0121] In a preferred embodiment, the steam content in the feedstock of the lift tube reactor is 0 to 80 wt%.

[0122] In a preferred embodiment, the process conditions of the lift tube reactor are: apparent linear velocity of gas of 3.0 to 10.0 m / s, temperature of 580 to 700°C, pressure of 100 to 500 kPa, and bed density of 50 to 150 kg / m 3 is.

[0123] In a preferred embodiment, the bed reactor feed comprises C3, C4, and C5 hydrocarbons.

[0124] In a preferred embodiment, the bed reactor feed comprises C4 and C5 hydrocarbons.

[0125] In a preferred embodiment, the C3, C4, and C5 hydrocarbons are derived from C3, C4, and C5 hydrocarbons separated from a product gas stream.

[0126] In a preferred embodiment, the C4 and C5 hydrocarbons are derived from C4 and C5 hydrocarbons separated from a product gas stream.

[0127] The C3, C4, and C5 hydrocarbons refer to hydrocarbons having 3, 4, and 5 carbon atoms.

[0128] The C4 and C5 hydrocarbons refer to hydrocarbons having 4 and 5 carbon atoms.

[0129] In a preferred embodiment, the process conditions in the light hydrocarbon aromatization reaction zone are a gas apparent linear velocity of 0.5 to 2.0 m / s, a reaction temperature of 550 to 665°C, a reaction pressure of 100 to 500 kPa, and a bed density of 150 to 700 kg / m 3 is.

[0130] In the embodiment described herein, the aromatic hydrocarbon potential content of the naphtha feedstock is 0-80 wt%, and the naphtha conversion rate per pass is 70-95 wt%. The unconverted naphtha is separated from the product gas and returned to the naphtha aromatics reactor 1 as feedstock. A portion of the low-carbon alkanes is separated from the product gas and returned to the lift tube reactor of the light hydrocarbon aromatization reactor 3 as feedstock. C3, C4, and C5 hydrocarbons are separated from the product gas and returned to the bed reactor of the light hydrocarbon aromatization reactor 3 as feedstock. The final product distribution is 60-75 wt% BTX, 6-14 wt% low-carbon olefins, 3-7 wt% hydrogen, 3-8 wt% low-carbon alkanes, 4-6 wt% combustible gas, 4-8 wt% heavy aromatic hydrocarbons, and 0.5-1 wt% coke. The content of para-xylene in the mixed xylenes in the product is 50 to 65 wt %.

[0131] The catalysts in the following examples are prepared by the following method: 100 g of HZSM-5 zeolite molecular sieve (manufactured by Nankai University Catalyst Factory, Si / Al = 15) was immersed in a 10 wt% aqueous zinc nitrate solution. The mass ratio (i.e., solid-liquid ratio) of the HZSM-5 zeolite molecular sieve to the zinc nitrate solution was 1 / 10, and the solution was immersed at 80°C for 6 hours. After immersion, the solution was drained and the sample was dried in an air atmosphere at 120°C for 4 hours, followed by calcination in an air atmosphere at 550°C for 4 hours to obtain a [Zn]HZSM-5 molecular sieve sample. This sample was tableted, crushed, and sieved to obtain molded molecular sieve particles with a particle size of 40 to 60 mesh.

[0132] 100 g of [Zn]HZSM-5 molecular sieve sample is mixed with an amorphous binder containing aluminum or silicon, and then spray-dried and molded. The specific procedure is as follows: [Zn]HZSM-5 molecular sieve sample, pseudoboehmite, silica sol, xanthan gum (biogum), and water were uniformly mixed, and the mixture was mixed, colloid milled, and degassed to obtain a slurry. The weight parts of each component in the slurry were as follows: [Zn]HZSM-535 parts by weight Al2O320 parts by weight SiO245 parts by weight H2O240 parts by weight Xanthan gum 1 part by weight

[0133] The resulting slurry is spray-dried and molded to obtain a microsphere sample with a particle size distribution of 20 to 100 μm, which is then calcined in a muffle furnace at 550°C for 3 hours to obtain a [Zn]HZSM-5 molded molecular sieve with an abrasion index of 1.2.

[0134] Example 1 In this embodiment, the device shown in FIG. 1 is used.

[0135] In this embodiment, the naphtha feedstock entering the naphtha aromatics reactor is a direct coal liquefaction naphtha, whose aromatics potential content is 78 wt %, and the naphtha feedstock entering the naphtha aromatics reactor also includes unconverted naphtha separated from the product gas stream.

[0136] The process conditions of the naphtha aromatics reaction zone of the naphtha aromatics reactor are as follows: gas apparent linear velocity is 0.5 m / s, reaction temperature is 645°C, reaction pressure is 100 kPa, and bed density is 700 kg / m 3 .

[0137] The regeneration gas is air.

[0138] The engineering conditions of the regeneration area of ​​the regenerator were as follows: gas apparent linear velocity 0.5 m / s, regeneration temperature 745°C, regeneration pressure 100 kPa, bed density 700 kg / m 3 .

[0139] The carbon content in the regenerated catalyst is 0.2 wt%.

[0140] The lift tube reactor feed is low carbon olefins separated from the product gas stream.

[0141] The engineering conditions of the lift tube reactor were as follows: gas apparent linear velocity 3.0 m / s, temperature 690°C, pressure 100 kPa, bed density 150 kg / m 3 .

[0142] The bed reactor feed is C3, C4 and C5 hydrocarbons separated from the product gas stream.

[0143] The process conditions for the light hydrocarbon aromatization reaction zone were as follows: gas apparent linear velocity: 0.5 m / s, reaction temperature: 665°C, reaction pressure: 100 kPa, bed density: 700 kg / m 3 .

[0144] The single-stage conversion of naphtha feedstock entering the naphtha aromatics reactor is 70.3 wt%.

[0145] The product distribution is as follows: 74.6 wt% BTX, 6 wt% low-carbon olefins, 3 wt% hydrogen, 3.5 wt% low-carbon alkanes, 5.1 wt% combustible gases, 7 wt% heavy aromatics, and 0.8 wt% coke. The para-xylene content of the mixed xylenes in the product is 50.5 wt%.

[0146] Example 2 In this embodiment, the device shown in FIG. 1 is used.

[0147] In this embodiment, the naphtha feedstock entering the naphtha aromatics reactor is indirect coal liquefaction naphtha, and its aromatics potential content is 0.1 wt%. The naphtha feedstock entering the naphtha aromatics reactor also includes unconverted naphtha separated from the product gas stream.

[0148] The process conditions of the naphtha aromatics reaction zone of the naphtha aromatics reactor are as follows: gas apparent linear velocity is 2.0 m / s, reaction temperature is 510°C, reaction pressure is 500 kPa, and bed density is 150 kg / m 3 .

[0149] The regeneration gas is oxygen.

[0150] The engineering conditions of the regeneration area of ​​the regenerator were as follows: gas apparent linear velocity 2.0 m / s, regeneration temperature 610°C, regeneration pressure 500 kPa, bed density 150 kg / m 3 .

[0151] The carbon content in the regenerated catalyst is 0.1 wt%.

[0152] The lift tube reactor feed contains steam and low carbon olefins separated from the product gas stream, the steam content of which is 80 wt %.

[0153] The engineering conditions of the lift tube reactor were as follows: gas apparent linear velocity 10.0 m / s, temperature 580°C, pressure 500 kPa, bed density 50 kg / m 3 .

[0154] The bed reactor feed is C3, C4 and C5 hydrocarbons separated from the product gas stream.

[0155] The process conditions for the light hydrocarbon aromatization reaction zone were as follows: gas apparent linear velocity: 2.0 m / s, reaction temperature: 550°C, reaction pressure: 500 kPa, bed density: 150 kg / m 3 .

[0156] The single-stage conversion of naphtha feedstock entering the naphtha aromatics reactor is 74 wt%.

[0157] The product distribution is as follows: 67 wt% BTX, 11 wt% low-carbon olefins, 5.3 wt% hydrogen, 3 wt% low-carbon alkanes, 5 wt% combustible gases, 8 wt% heavy aromatics, and 0.7 wt% coke. The para-xylene content of the mixed xylenes in the product is 64 wt%.

[0158] Example 3 In this embodiment, the device shown in FIG. 1 is used.

[0159] In this embodiment, the naphtha feedstock entering the naphtha aromatics reactor is indirect coal liquefaction naphtha, and its aromatics potential content is 3 wt %. The naphtha feedstock entering the naphtha aromatics reactor also includes unconverted naphtha separated from the product gas stream.

[0160] The process conditions of the naphtha aromatics reaction zone of the naphtha aromatics reactor are as follows: gas apparent linear velocity is 1.2 m / s, reaction temperature is 550°C, reaction pressure is 120 kPa, and bed density is 260 kg / m 3 .

[0161] The regeneration gas is oxygen-enriched air.

[0162] The engineering conditions of the regeneration area of ​​the regenerator are as follows: gas apparent linear velocity 1.2 m / s, regeneration temperature 650 °C, regeneration pressure 120 kPa, bed density 260 kg / m 3 .

[0163] The carbon content in the regenerated catalyst is 0.3 wt%.

[0164] The lift tube reactor feed contains steam and low carbon olefins separated from the product gas stream, the steam content of which is 25 wt%.

[0165] The engineering conditions of the lift tube reactor were as follows: gas apparent linear velocity 7.0 m / s, temperature 630°C, pressure 120 kPa, bed density 80 kg / m 3 .

[0166] The bed reactor feed is C4 and C5 hydrocarbons separated from the product gas stream.

[0167] The process conditions for the light hydrocarbon aromatization reaction zone were as follows: gas apparent linear velocity 1.2 m / s, reaction temperature 580°C, reaction pressure 120 kPa, bed density 260 kg / m 3 .

[0168] The single-stage conversion of naphtha feedstock entering the naphtha aromatics reactor is 94.5 wt%.

[0169] The product distribution is as follows: 60 wt% BTX, 14 wt% low-carbon olefins, 7 wt% hydrogen, 8 wt% low-carbon alkanes, 5 wt% combustible gases, 5.5 wt% heavy aromatics, and 0.5 wt% coke. The para-xylene content of the mixed xylenes in the product is 65 wt%.

[0170] Example 4 In this embodiment, the device shown in FIG. 1 is used.

[0171] In this embodiment, the naphtha feedstock entering the naphtha aromatics reactor is straight-run naphtha, and its aromatics potential content is 46 wt %. The naphtha feedstock entering the naphtha aromatics reactor also includes unconverted naphtha separated from the product gas stream.

[0172] The process conditions of the naphtha aromatics reaction zone of the naphtha aromatics reactor are as follows: gas apparent linear velocity is 1.8 m / s, reaction temperature is 600 °C, reaction pressure is 200 kPa, bed density is 220 kg / m 3 .

[0173] The regeneration gas is air.

[0174] The engineering conditions of the regeneration area of ​​the regenerator are as follows: gas apparent linear velocity 1.8 m / s, regeneration temperature 700 °C, regeneration pressure 200 kPa, bed density 220 kg / m 3 .

[0175] The carbon content in the regenerated catalyst is 0.1 wt%.

[0176] The lift tube reactor feed contains steam and low carbon olefins separated from the product gas stream, wherein the steam content is 50 wt%.

[0177] The engineering conditions of the lift tube reactor were as follows: gas apparent linear velocity 5.0 m / s, temperature 660°C, pressure 200 kPa, bed density 110 kg / m 3 .

[0178] The bed reactor feed is C4 and C5 hydrocarbons separated from the product gas stream.

[0179] The process conditions for the light hydrocarbon aromatization reaction zone were as follows: gas apparent linear velocity: 1.8 m / s, reaction temperature: 630°C, reaction pressure: 200 kPa, bed density: 220 kg / m 3 .

[0180] The single-stage conversion of naphtha feedstock entering the naphtha aromatics reactor is 88 wt%.

[0181] The product distribution is as follows: 70.2 wt% BTX, 10 wt% low-carbon olefins, 6 wt% hydrogen, 5 wt% low-carbon alkanes, 4 wt% combustible gases, 4 wt% heavy aromatics, and 0.8 wt% coke. The para-xylene content of the mixed xylenes in the product is 61 wt%.

[0182] Example 5 In this embodiment, the device shown in FIG. 1 is used.

[0183] In this embodiment, the naphtha feedstock entering the naphtha aromatics reactor is hydrocracked naphtha, with a potential aromatics content of 64 wt %, and the naphtha feedstock entering the naphtha aromatics reactor also includes unconverted naphtha separated from the product gas stream.

[0184] The process conditions of the naphtha aromatics reaction zone of the naphtha aromatics reactor are as follows: gas apparent linear velocity is 1.0 m / s, reaction temperature is 580°C, reaction pressure is 150 kPa, and bed density is 350 kg / m 3 .

[0185] The regeneration gas is air.

[0186] The engineering conditions of the regeneration area of ​​the regenerator were as follows: gas apparent linear velocity 1.0 m / s, regeneration temperature 680°C, regeneration pressure 150 kPa, bed density 350 kg / m 3 .

[0187] The carbon content in the regenerated catalyst is 0.5 wt%.

[0188] The lift tube reactor feed contains steam and low carbon olefins separated from the product gas stream, the steam content of which is 40 wt%.

[0189] The engineering conditions of the lift tube reactor were as follows: gas apparent linear velocity 7.0 m / s, temperature 650°C, pressure 150 kPa, bed density 80 kg / m 3 .

[0190] The bed reactor feed is C4 and C5 hydrocarbons separated from the product gas stream.

[0191] The process conditions for the light hydrocarbon aromatization reaction zone were as follows: gas apparent linear velocity 1.0 m / s, reaction temperature 610°C, reaction pressure 150 kPa, bed density 350 kg / m 3 .

[0192] The single-stage conversion of naphtha feedstock entering the naphtha aromatics reactor is 76 wt%.

[0193] The product distribution is as follows: 72 wt% BTX, 8 wt% low-carbon olefins, 5 wt% hydrogen, 3 wt% low-carbon alkanes, 6 wt% combustible gases, 5 wt% heavy aromatics, and 1.0 wt% coke. The para-xylene content of the mixed xylenes in the product is 55 wt%.

[0194] The above description is only a partial example of the present application and does not limit the present application in any way. In the present application, more preferred embodiments are disclosed as above, but they are not intended to limit the present application. Various variations and modifications made by a person skilled in the art using the technical content disclosed above without departing from the technical solution of the present application are all equivalent to equivalent embodiments, and all fall within the scope of the technical solution. [Explanation of symbols]

[0195] 1. Naphtha aromatics reactor 1-1 Naphtha aromatic reactor housing 1-2 Naphtha aromatics reactor distributor 1-3 Gas-solid separator I 1-4 Gas Collection Chamber I 1-5 Produced gas transport pipe I 1-6 Stripper I 1-7 Used sliding valve I 1-8 Spent Agent Transport Pipe I 2 Regenerator 2-1 Regenerator housing 2-2 Regenerator distributor 2-3 Regenerator gas-solid separation device 2-4 Regenerator gas collection chamber 2-5 Exhaust gas transport pipe 2-6 Regenerator stripper 2-7 Regenerative Slide Valve I 2-8 Regenerant transport pipe 2-9 Regenerative Slide Valve II 3 Light hydrocarbon aromatization reactor 3-1 Lift tube reactor inlet end 3-2 Lift tube reactor center 3-3 Lift tube reactor outlet end 3-4 Bed Reactor Housing 3-5 Bed Reactor Distributor 3-6 Gas-solid separator II 3-7 Gas Collection Chamber II 3-8 Produced Gas Transport Pipe II 3-9 Stripper II 3-10 Used sliding valve II 3-11 Spent Agent Transport Pipe II

Claims

1. An apparatus for producing aromatics from naphtha, comprising: The apparatus includes a naphtha aromatics reactor, a regenerator, and a light hydrocarbon aromatization reactor; The naphtha aromatic reactor is connected to a regenerator through a spent agent transport pipe I; The regenerator is connected to the naphtha-based aromatic reactor via a regenerant transport pipe; The light hydrocarbon aromatization reactor comprises a lift tube reactor, the lift tube reactor being connected to a bed reactor; The regenerator is connected to the lift pipe reactor via a regeneration slide valve II; An apparatus for producing aromatics from naphtha, characterized in that the bed reactor is connected to the regenerator through a spent agent transport pipe II.

2. A gas-solid separation section is provided in the upper part of the naphtha aromatic reactor, and a product gas transport pipe I is provided in the gas-solid separation section; 2. The apparatus for producing aromatics from naphtha according to claim 1, wherein a naphtha aromatics reaction zone is provided in the lower part of the naphtha aromatics reactor, the regenerant transport pipe introduces the catalyst into the naphtha aromatics reaction zone, and a naphtha aromatics reactor distributor for introducing the naphtha raw material is provided in the lower part of the naphtha aromatics reaction zone.

3. 3. The apparatus for producing aromatics from naphtha according to claim 2, wherein the naphtha aromatics reactor is further provided with a gas-solid separation device I and a gas collection chamber I, the gas collection chamber I being located at the top of the gas-solid separation section, the gas outlet of the gas-solid separation device I being connected to the gas collection chamber I, and the gas collection chamber I being connected to a product gas transport pipe I.

4. 3. The apparatus for producing aromatics from naphtha according to claim 2, wherein a stripper I is provided below the naphtha-produced aromatics reaction section, and the naphtha-produced aromatics reaction section is connected to a spent agent transport pipe I via the stripper I.

5. 5. The apparatus for producing aromatics from naphtha according to claim 4, wherein the stripper I is connected to a spent agent transport pipe I via a spent slide valve I.

6. 5. The apparatus for producing aromatics from naphtha according to claim 4, wherein the gas-solid separation device I is composed of one or more sets of gas-solid cyclone separators, each set of gas-solid cyclone separators including a first-stage gas-solid cyclone separator and a second-stage gas-solid cyclone separator.

7. a gas-solid separation section of the regenerator is provided at the top of the regenerator, and an exhaust gas transport pipe is provided in the gas-solid separation section of the regenerator; A regeneration section is provided at the bottom of the regenerator, and spent catalyst is introduced into the regeneration section through spent catalyst transport pipes I and II. A regenerator distributor is provided at the bottom of the regenerator to introduce regeneration gas.

2. The apparatus for producing aromatics from naphtha according to claim 1, wherein the regenerant transport pipe transports the regenerated catalyst in the regeneration section to the naphtha aromatics reactor, and the regeneration slide valve II transports the regenerated catalyst to the lift pipe reactor.

8. The regenerator housing further includes a regenerator gas-solid separator and a regenerator gas collection chamber; 8. The apparatus for producing aromatics from naphtha according to claim 7, wherein the regenerator gas collecting chamber is located at the top of the regenerator gas-solid separation section, the gas outlet of the regenerator gas-solid separation device is connected to the regenerator gas collecting chamber, and the regenerator gas collecting chamber is connected to an exhaust gas transport pipe.

9. A regenerator stripper is provided below the regenerator section, and the regenerator section is connected to the regenerator slide valve I and the regenerator slide valve II via the regenerator stripper; 8. The apparatus for producing aromatics from naphtha according to claim 7, wherein the regeneration slide valve I is connected to the naphtha-produced aromatics reactor through a regenerant transport pipe, and the regeneration slide valve II is connected to the lift pipe reactor.

10. 9. The apparatus for producing aromatics from naphtha according to claim 8, wherein the regenerator gas-solid separation device is composed of one or more sets of gas-solid cyclone separators, each set of gas-solid cyclone separators including a first-stage gas-solid cyclone separator and a second-stage gas-solid cyclone separator.

11. A gas-solid separation section of the bed reactor is provided at the top of the bed reactor, and a product gas transport pipe II is provided in the gas-solid separation section of the bed reactor; A light hydrocarbon aromatization reaction zone is provided at the bottom of the bed reactor, and a bed reactor distributor is provided at the lower part of the light hydrocarbon aromatization reaction zone, which is used to introduce raw materials into the bed reactor. The upper end of the lift tube reactor penetrates the bottom of the bed reactor and is inserted axially into the bed reactor; 2. The apparatus for producing aromatics from naphtha according to claim 1, wherein the regeneration slide valve II introduces catalyst into the feed inlet end of the lift tube reactor.

12. 12. The apparatus for producing aromatics from naphtha according to claim 11, wherein the gas-solid separation section of the bed reactor is provided with a gas-solid separator II and a gas collection chamber II, the gas outlet of the gas-solid separator II is connected to the gas collection chamber II, the catalyst outlet of the gas-solid separator II is located in the light hydrocarbon aromatization reaction section, and the gas collection chamber II is connected to a product gas transport pipe II located outside the bed reactor.

13. 12. The apparatus for producing aromatics from naphtha according to claim 11, wherein a stripper II is connected to the light hydrocarbon aromatization reaction zone, and the bed reactor is connected to a spent agent transport pipe II via the stripper II.

14. 2. The apparatus for producing aromatics from naphtha according to claim 1, wherein the stripper II is connected to a spent agent transport pipe II via a spent slide valve II.

15. 13. The apparatus for producing aromatics from naphtha according to claim 12, wherein the gas-solid separation device II is a gas-solid cyclone separator, and a catalyst outlet of the gas-solid separation device II is located above an outlet end of the lift tube reactor.

16. A method for producing aromatics from naphtha using the apparatus according to any one of claims 1 to 15, comprising using a metal zeolite bifunctional catalyst as a catalyst, A feed containing naphtha is introduced into the naphtha aromatics reactor, and a lift tube reactor feed containing low carbon alkanes is introduced into the lift tube reactor; 3 , C 4 , and C 5 A bed reactor feed containing hydrocarbons is introduced into the bed reactor, and a regeneration gas is introduced into the regenerator; The naphtha aromatics reactor and the bed reactor output product gas, and the spent catalyst is introduced into a regenerator through a spent agent transport pipe I and a spent agent transport pipe II, the spent catalyst is reacted with the regeneration gas in the regenerator to be regenerated, and then transported to the naphtha aromatics reactor and the lift tube reactor, and the regenerator discharges exhaust gas.

17. The catalyst uses a metal-modified HZSM-5 zeolite molecular sieve, and the metal used for the metal modification is at least one selected from La, Zn, Ga, Fe, Mo, and Cr; 17. The method of claim 16, wherein the metal modification method comprises immersing the HZSM-5 zeolite molecular sieve in a metal salt solution, drying, and calcining the zeolite molecular sieve to obtain the metal-modified HZSM-5 zeolite molecular sieve.

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

19. The naphtha-containing feedstock further comprises unreacted naphtha separated from the product gas stream, the unreacted naphtha comprising C 4 ~C 12 17. The method of claim 16, wherein the hydrocarbons comprise linear, branched, aliphatic hydrocarbons, and naphthenes.

20. The reaction conditions for the naphtha aromatics reaction section are: apparent linear gas velocity of 0.5-2.0 m / s, reaction temperature of 500-650°C, reaction pressure of 100-500 kPa, and bed density of 150-700 kg / m 3 17. The method of claim 16, wherein:

21. 17. The method of claim 16, wherein the carbon content in the regenerated catalyst is 0.5 wt% or less.

22. 17. The method according to claim 16, wherein the regeneration gas is at least one selected from oxygen, air, and oxygen-enriched air.

23. The process conditions for the regeneration zone are: apparent linear gas velocity of 0.5-2.0 m / s, regeneration temperature of 600-750°C, regeneration pressure of 100-500 kPa, and bed density of 150-700 kg / m 3 17. The method of claim 16, wherein:

24. 17. The method of claim 16, wherein the lift tube reactor feed further comprises steam, and the steam content in the lift tube reactor feed is 0-80 wt%.

25. 17. The method of claim 16, wherein the lower carbon alkanes in the lift tube reactor feed are separated from a product gas stream.

26. The process conditions of the lift tube reactor are: apparent linear velocity of 3.0-10.0 m / s; temperature of 580-700°C; Pressure: 100 to 500 kPa, bed density: 50 to 150 kg / m 3 17. The method of claim 16, wherein:

27. The bed reactor feed is C 3 , C 4 , and C 5 The C 3 , C 4 , and C 5 17. The method of claim 16, wherein hydrocarbons are separated from the product gas stream.

28. The bed reactor feed is C 4 and C 5 17. The method of claim 16, wherein the product gas stream comprises C4 and C5 hydrocarbons, the C4 and C5 hydrocarbons being separated from the product gas stream.

29. The process conditions of the light hydrocarbon aromatization reaction zone are: gas apparent linear velocity of 0.5-2.0 m / s; Reaction temperature: 550 to 665°C, reaction pressure: 100 to 500 kPa, bed density: 150 to 700 kg / m 3 17. The method of claim 16, wherein:

30. introducing naphtha through a naphtha aromatics reactor distributor into a naphtha aromatics reaction section of the naphtha aromatics reactor and contacting the naphtha with the catalyst from the regenerator to produce a product gas stream containing BTX, light olefins, hydrogen, light alkanes, combustible gases, heavy aromatics, and unreacted naphtha, and the catalyst is coked and converted to spent catalyst; The regeneration gas is introduced into the regeneration section of the regenerator through the regenerator distributor and contacted with the spent catalyst from the naphtha aromatics reactor and the spent catalyst from the light hydrocarbon aromatization reactor, and the coke on the spent catalyst reacts with the regeneration gas to produce exhaust gas, and the spent catalyst is converted into regenerated catalyst; The lift tube reactor feed is introduced into the lift tube reactor through the inlet end of the lift tube reactor, where it contacts and reacts with the regenerated catalyst from the regenerator. The lift tube reactor feed is converted into BTX, low-carbon olefins, and H 2 and then introduced into the lower part of the light hydrocarbon aromatization reaction zone of the bed reactor through the outlet end of the lift tube reactor; The bed reactor feed is introduced into the light hydrocarbon aromatization reaction zone through the bed reactor distributor and contacted with the catalyst from the lift tube reactor to produce BTX, low carbon olefins, and H 2 17. The method of claim 16, wherein the catalyst is coked and converted to spent catalyst to produce a light hydrocarbon aromatization product gas comprising:

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