Device and method for producing aromatic hydrocarbons from naphtha

Abstract

A device and a method for producing aromatic hydrocarbons from naphtha are disclosed in this application. The device comprises a fluidized bed reactor and a riser reactor. The fluidized bed reactor is used to introduce naphtha raw material and contact it with the catalyst flowing in from the riser reactor in order to generate a product gas stream containing BTX and spent catalyst; the product gas stream is subjected to gas-solid separation; the separated product gas stream is sent to a working section located downstream; the unreacted naphtha after separation returns to the fluidized bed reactor as raw material; a part of the separated lower carbon alkanes returns to the riser reactor as raw material and is further converted into aromatic hydrocarbons and other components. In this application, by connecting a high-temperature riser reactor in series with a relatively low-temperature fluidized bed reactor, the yield of lower carbon alkanes decreases and the yield of aromatic hydrocarbons increases. Also, straight-chain and branched-chain aliphatic hydrocarbons can be effectively converted into aromatic hydrocarbons with high selectivity, and the content of p-xylene in the xylene mixture exceeds 50 wt%.

Description

Technical Field

[0001] The present application relates to a fluidized bed device and a method for using the device, belonging to the technical field of the chemical industry, and particularly relates to a device and a method for producing aromatic hydrocarbons from naphtha.

Background Art

[0002] Aromatic hydrocarbons (benzene, toluene, and xylene, generally referred to as BTX) are important organic chemical raw materials, and p-xylene (PX) is the most notable product among aromatic hydrocarbons. PX is mainly used to produce 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 continuously increasing. In 2021, the total import volume of PX in China was about 13.65 million tons, and the trade dependence was about 38%.

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

Summary of the Invention

Problems to be Solved by the Invention

[0004] The distillation range of the naphtha fraction is wide, and it is difficult to effectively separate straight-chain and branched-chain aliphatic hydrocarbons from naphthenic hydrocarbons and aromatic hydrocarbons by general separation methods. In addition, it is difficult to convert straight-chain and branched-chain aliphatic hydrocarbons into aromatic hydrocarbons by catalytic reforming technology. In order to increase the potential content of the raw material aromatic hydrocarbons used in catalytic reforming, generally, it is necessary to distill the naphtha raw material used in catalytic reforming to separate the topping oil with a boiling point of less than 60°C. However, the fraction with a boiling point above 60°C still contains a large number of straight-chain and branched-chain aliphatic hydrocarbons that are difficult to convert into aromatic hydrocarbons. Therefore, the problem of converting straight-chain and branched-chain aliphatic hydrocarbons into aromatic hydrocarbons in a highly selective manner has always existed as a difficult and intense argument in the technological development for producing aromatic hydrocarbons using naphtha.

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

Means for Solving the Problem

[0006] In one aspect of the present application, a device for producing aromatic hydrocarbons from naphtha is presented, which enables the production of aromatic hydrocarbons from naphtha with a low potential content of aromatic hydrocarbons, increases the content of p-xylene in the mixed xylene, and can reduce the energy consumption in production.

[0007] The naphtha in the present application contains components consisting of straight-chain and branched-chain aliphatic hydrocarbons, naphthenic hydrocarbons, and aromatic hydrocarbons. 12

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

[0009] The device for producing aromatic hydrocarbons from naphtha comprises a fluidized bed reactor and a riser reactor, The outlet of the riser reactor is connected to the fluidized bed reactor, The fluidized bed reactor is used to introduce naphtha raw material, contact it with the catalyst flowing in from the riser reactor, and react with it to produce a product gas stream containing BTX and spent catalyst. The product gas stream is subjected to gas-solid separation, The separated product gas stream is sent to a downstream working section, The unreacted naphtha after separation returns to the fluidized bed reactor as raw material, A part of the separated lower carbon alkanes returns to the riser reactor as raw material.

[0010] Preferably, the riser reactor is used to introduce the riser reactor raw material and catalyst, react it to produce aromatic hydrocarbons, and the stream containing unreacted riser reactor raw material, aromatic hydrocarbons, and catalyst enters the fluidized bed reactor through the outlet of the riser reactor.

[0011] Preferably, the raw material includes water vapor and lower carbon alkanes separated from the product gas stream.

[0012] Preferably, the water vapor content in the riser reactor raw material is 0 wt% to 50 wt%.

[0013] Preferably, the inlet of the riser reactor is connected to a fluidized bed regenerator, and the catalyst introduced into the riser reactor is the regenerated catalyst produced by the fluidized bed regenerator.

[0014] Preferably, the fluidized bed regenerator continuously passes through a regeneration slide valve connected to the inlet of the riser reactor through a regenerator stripper and a pipeline.

[0015] Preferably, the inlet of the regenerator stripper extends to the inside of the regenerator shell of the fluidized bed regenerator and is located above the regenerator distributor.

[0016] Preferably, the fluidized bed reactor comprises a reactor shell, and the region surrounded by the reactor shell is divided from the top to the bottom into a first gas-solid separation zone and a reaction zone, and a gas-solid separation device and a reactor gas collection chamber are provided in the first gas-solid separation zone, the reactor gas collection chamber is located on the inner uppermost part of the reactor shell, the inlet of the reactor gas collection chamber communicates with the gas outlet of the reactor gas-solid separation device, and the outlet of the reactor gas collection chamber communicates with the product gas transfer pipe, and a reactor distributor for introducing naphtha raw materials is provided on the lower part of the reaction zone.

[0017] Preferably, the reactor 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.

[0018] Preferably, the device further comprises a fluidized bed regenerator connected to the fluidized bed reactor, and the fluidized bed regenerator is used to introduce a regeneration gas to convert the used catalyst into a regenerated catalyst.

[0019] Preferably, the fluidized bed reactor continuously passes through a reactor stripper, a used slide valve, and a used chemical transfer pipe connected to the fluidized bed regenerator, and the inlet of the reactor stripper extends to the inside of the fluidized bed reactor shell and is located below the catalyst outlet end of the reactor gas-solid separation device.

[0020] Preferably, the fluidized bed regenerator comprises a regenerator shell, and the region surrounded by the regenerator shell is divided from the topmost part to the lowermost part into a second gas-solid separation zone and a regeneration zone. A regenerator gas-solid separation device and a regenerator gas collection chamber are arranged and configured within the second gas-solid separation zone. The regenerator gas collection chamber is located on the inner uppermost part of the regenerator shell, and a flue gas transfer pipe is provided on the regenerator gas collection chamber. The gas outlet of the regenerator gas-solid separation device communicates with the regenerator gas collection chamber, and a regenerator distributor for introducing regenerated gas is provided on the inner lower part of the regeneration zone.

[0021] 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.

[0022] In another aspect of the present application, a method for producing aromatic hydrocarbons from naphtha is presented, which includes the step of producing aromatic hydrocarbons by using the device and catalyst for producing aromatic hydrocarbons from the naphtha.

[0023] Preferably, the catalyst is a metal molecular sieve dual-functional catalyst.

[0024] Preferably, the metal molecular sieve dual-functional catalyst is a metal-modified HZSM-5 zeolite molecular sieve.

[0025] For metal modification, the metal is selected from at least one of La, Zn, Ga, Fe, Mo, and Cr. The method for metal modification includes the steps of placing the HZSM-5 zeolite molecular sieve in a metal salt solution, soaking it, drying it, and calcining it to obtain a metal-modified HZSM-5 zeolite molecular sieve.

[0026] Preferably, the method allows naphtha to enter the reaction zone of the fluidized bed reactor through a reactor distributor to produce a product gas stream containing BTX, lower olefins, hydrogen, lower alkanes, combustible gas, heavy aromatic hydrocarbons, and unconverted naphtha by contacting with the catalyst flowing in from the riser reactor, while simultaneously binding and converting the catalyst into used catalyst; allowing the product gas stream to enter a reactor gas - solid separation device, then enter a reactor gas collection chamber, and enter a working section located downstream through a product gas transfer pipe to remove the used catalyst contained in the product gas stream; and includes.

[0027] Preferably, the unconverted naphtha after separation returns to the fluidized bed reactor as a raw material.

[0028] Preferably, a portion of the lower alkanes after separation returns to the riser reactor as a raw material.

[0029] Preferably, BTX refers to benzene, toluene, and xylene; lower olefins refer to ethylene and propylene; lower alkanes refer to ethane and propane; combustible gas includes methane, CO, etc.; heavy aromatic hydrocarbons refer to aromatic hydrocarbons with 9 or more carbon atoms in the molecule.

[0030] Preferably, naphtha is selected from at least one of directly coal - liquefied naphtha, indirectly coal - liquefied naphtha, straight - run naphtha, and hydrocracked naphtha.

[0031] Preferably, naphtha also contains unconverted naphtha separated from the product gas stream, and the unconverted naphtha mainly comprises C4 - C 12 linear and branched aliphatic hydrocarbons, and naphthenic hydrocarbons.

[0032] Preferably, the carbon content in the used catalyst is 1.0 wt% to 3.0 wt%.

[0033] Preferably, the process conditions in the reaction zone are a superficial linear velocity of the gas of 0.5 m / s to 2.0 m / s, a reaction temperature of 500 °C to 650 °C, a reaction pressure of 100 kPa to 500 kPa, and a bed density of 150 kg / m 3 ~700 kg / m 3 .

[0034] Optionally, the superficial linear velocity of the gas in the reaction zone is independently selected from any value, or a value within the range of 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.

[0035] Optionally, the reaction temperature in the reaction zone is independently selected from any value, or a value included in the range between any two values among 500 °C, 510 °C, 520 °C, 530 °C, 540 °C, 550 °C, 560 °C, 570 °C, 580 °C, 590 °C, 600 °C, 610 °C, 620 °C, 630 °C, 640 °C, and 650 °C.

[0036] Optionally, the reaction pressure in the reaction zone is independently selected from any value, or a value included in 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.

[0037] Optionally, the bed density in the reaction zone is any value, or 150 kg / m 3 , 200 kg / m 3 , 250 kg / m 3 , 300 kg / m 3 , 350 kg / m 3 , 400 kg / m 3, 450 kg / m 3 , 500 kg / m 3 , 550 kg / m 3 , 600 kg / m 3 , 650 kg / m 3 , and 700 kg / m 3 is independently selected from values included in the range between any two of these values.

[0038] Preferably, the method includes the steps of introducing a riser reactor raw material and a catalyst into the riser reactor to react to produce an aromatic hydrocarbon, and enabling a stream containing unreacted riser reactor raw material, aromatic hydrocarbon, and catalyst to enter the fluidized bed reactor from the outlet of the riser reactor. It further includes.

[0039] Preferably, the catalyst is a regenerated catalyst flowing in from a fluidized bed regenerator.

[0040] Preferably, the regenerated catalyst continuously passes through a regenerator stripper and a regenerated slide valve and enters the riser reactor.

[0041] Preferably, the carbon content in the regenerated catalyst is 0.5 wt% or less.

[0042] Preferably, the riser reactor raw material includes steam and lower carbon alkanes separated from the product gas stream.

[0043] Preferably, the steam content in the riser reactor raw material is 0 wt% to 50 wt%.

[0044] Preferably, the process conditions of the riser reactor are a superficial linear velocity of the gas of 3.0 m / s to 10.0 m / s, a temperature of 580 °C to 700 °C, a pressure of 100 kPa to 500 kPa, and a bed density of 50 kg / m 3 ~ 150 kg / m 3 are.

[0045] Optionally, the apparent linear velocity of the gas is independently selected from any value or a value within a range between 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, and 10.0 m / s.

[0046] Optionally, the temperature is independently selected from any value or a value within a range between 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, and 700 °C.

[0047] Optionally, the pressure is independently selected from any value or a value within a range between 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, and 500 kPa.

[0048] Optionally, the layer density is any value or a value within a range between any two values of 50 kg / m 3 , 60 kg / m 3 , 70 kg / m 3 , 80 kg / m 3 , 90 kg / m 3 , 100 kg / m 3 , 110 kg / m 3 , 120 kg / m 3 , 130 kg / m 3 , 140 kg / m 3 , and 150 kg / m 3 and is independently selected from a value within a range between any two of these values.

[0049] Preferably, the method further includes enabling the spent catalyst to enter the reactor stripper from the open end of the inlet pipe of the reactor stripper, and after the spent catalyst is stripped by the reactor stripper, enabling the spent catalyst to enter the downstream region through the spent slide valve and the spent chemical conveying pipe.

[0050] Preferably, the downstream region is a fluidized bed regenerator.

[0051] Preferably, the regeneration gas is introduced into the regeneration zone of the fluidized bed regenerator through the regenerator distributor to contact the spent catalyst flowing in from the fluidized bed reactor. The coke on the spent catalyst reacts with the regeneration gas to generate flue gas, and at the same time, the spent catalyst is converted into a regenerated catalyst.

[0052] Preferably, the spent catalyst continuously passes through the reactor stripper, the spent slide valve, and the spent chemical conveying pipe and enters the fluidized bed regenerator, contacts the regeneration gas, and reacts with it to obtain flue gas and a regenerated catalyst. The flue gas enters the regenerator gas-solid separation device to remove the regenerated catalyst contained in the flue gas, then enters the regenerator gas collection chamber, and enters the working section located downstream through the flue gas conveying pipe.

[0053] Preferably, the regeneration gas is selected from at least one of oxygen, air, and oxygen-rich air.

[0054] Optionally, the process conditions in the regeneration zone are a superficial linear velocity of the gas of 0.5 m / s to 2.0 m / s, a regeneration temperature of 600 °C to 750 °C, a regeneration pressure of 100 kPa to 500 kPa, and a bed density of 150 kg / m 3 ~700 kg / m 3 3.

[0055] Optionally, the apparent linear velocity of the gas is independently selected from any numerical value or a numerical value within a range between any two of the following values: 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.

[0056] Optionally, the regeneration temperature is independently selected from any numerical value or a numerical value within a range between any two of the following values: 600 °C, 615 °C, 630 °C, 645 °C, 660 °C, 675 °C, 690 °C, 705 °C, 720 °C, 735 °C, and 750 °C.

[0057] Optionally, the regeneration pressure is independently selected from any numerical value or a numerical value within a range between any two of the following values: 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.

[0058] Optionally, the layer density is independently selected from any numerical value or a numerical value within a range between any two of the following values: 150 kg / m3, 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 3 3, and is independently selected from a numerical value within a range between any two of the above values.

[0059] In this application, the potential content of aromatic hydrocarbons in the naphtha raw material is 0 wt% to 80 wt%, and the single-pass conversion rate of naphtha is 70 wt% to 95 wt%. By using a device for producing aromatic hydrocarbons from naphtha and a method for producing aromatic hydrocarbons from naphtha based on the device, the finally obtained product is composed of 60 wt% to 75 wt% of BTX, 7 wt% to 15 wt% of light olefins, 3 wt% to 8 wt% of hydrogen, 2 wt% to 7 wt% of light alkanes, 4 wt% to 6 wt% of combustible gas, 3 wt% to 7 wt% of heavy aromatic hydrocarbons, and 0.5 wt% to 1 wt% of coke. The content of p-xylene in the mixed xylene in the product is 50 wt% to 65 wt%.

[0060] This application may have the following beneficial effects. 1) According to this application, linear and branched aliphatic hydrocarbons can be effectively converted into aromatic hydrocarbons in a highly selective manner. The raw material has a wide range of applications, and aromatic hydrocarbons can be produced from naphtha with a low potential content of aromatic hydrocarbons. 2) According to this application, the aromatization of light alkanes is achieved by a riser reactor and a metal molecular sieve dual-functional catalyst. By doing so, in the technology for producing aromatic hydrocarbons from naphtha, the yield of aromatic hydrocarbons increases significantly. 3) In the aromatic hydrocarbon product generated by this application, the content of p-xylene in the xylene mixture exceeds 50 wt%, which is much higher than the thermodynamic equilibrium content (about 24 wt%). Therefore, the yield of p-xylene can be effectively increased, and the energy consumption required for the separation of p-xylene can be significantly reduced. 4) The device for producing aromatic hydrocarbons from naphtha in the present application comprises a fluidized bed reactor and a riser reactor. Since low-carbon alkanes are very stable and require a high reaction temperature, in the device for producing aromatic hydrocarbons from naphtha described in the present application, a high-temperature regenerated catalyst first enters the riser reactor and contacts the low-carbon alkane. The low-carbon alkane becomes the target of the aromatization reaction under catalysis, thereby increasing the yield of aromatic hydrocarbons. However, when a catalyst with a lower temperature is then introduced into the fluidized bed reactor and contacts the naphtha, the local high-temperature zone in the fluidized bed reactor is eliminated. Therefore, the yield of low-carbon alkanes effectively decreases, and the yield of aromatic hydrocarbons increases. According to the device for producing aromatic hydrocarbons from naphtha described in the present application, by connecting a riser reactor at a high temperature and a fluidized bed reactor at a relatively low temperature in series, the beneficial effect of reducing the yield of low-carbon alkanes and increasing the yield of aromatic hydrocarbons is achieved.

Brief Description of the Drawings

[0061]

Figure 1

Modes for Carrying Out the Invention

[0062] The present application will be described in detail below with reference to embodiments, but the present application is not limited to these embodiments.

[0063] This application provides a device for producing aromatic hydrocarbons from naphtha, comprising a fluidized bed reactor and a riser reactor, wherein the outlet of the riser reactor is connected to the fluidized bed reactor, and the fluidized bed reactor is used to introduce naphtha raw material, contact it with the catalyst flowing in from the riser reactor, react with it to generate a product gas stream containing BTX and spent catalyst; the product gas stream is subjected to gas-solid separation; the separated product gas stream is sent to a working section located downstream; the unreacted naphtha after separation returns to the fluidized bed reactor as raw material; and a part of the separated low-carbon alkanes returns to the riser reactor as raw material.

[0064] BTX refers to benzene, toluene, and xylene.

[0065] In one embodiment, the low-carbon olefins refer to ethylene and propylene.

[0066] The low-carbon alkanes refer to ethane and propane.

[0067] The combustible gas includes methane, CO, etc.

[0068] The heavy aromatic hydrocarbons refer to aromatic hydrocarbons with 9 or more carbon atoms in the molecule.

[0069] In one embodiment, the naphtha is selected from at least one of direct coal liquefaction naphtha, indirect coal liquefaction naphtha, straight-run naphtha, and hydrocracked naphtha.

[0070] In one embodiment, the naphtha also contains unreacted naphtha separated from the product gas stream, and the unreacted naphtha contains a main component consisting of straight-chain and branched-chain aliphatic hydrocarbons and naphthenic hydrocarbons. 12

[0071] In one embodiment, the riser reactor raw material includes steam and low-carbon alkanes separated from the product gas stream.

[0072] In one embodiment, the water vapor content in the riser reactor raw material is 0 wt% to 50 wt%.

[0073] In one embodiment, the inlet of the riser reactor is connected to a fluidized bed regenerator, and the catalyst introduced into the riser reactor is the regenerated catalyst produced by the fluidized bed regenerator.

[0074] In one embodiment, the fluidized bed regenerator continuously passes through a regeneration slide valve that connects to the inlet of the riser reactor through a regenerator stripper and a pipeline.

[0075] In one embodiment, the inlet of the regenerator stripper extends to the inside of the regenerator shell of the fluidized bed regenerator and is located above the regenerator distributor.

[0076] In one embodiment, the riser reactor is used to introduce the riser reactor raw material and the catalyst to react to produce aromatic hydrocarbons, and a stream containing unreacted riser reactor raw material, aromatic hydrocarbons, and catalyst enters the fluidized bed reactor through the outlet of the riser reactor.

[0077] In one embodiment, the fluidized bed reactor includes a reactor shell, and the region surrounded by the reactor shell is divided from the top to the bottom into a first gas-solid separation zone and a reaction zone, and a gas-solid separation device and a reactor gas collection chamber are provided in the first gas-solid separation zone. The reactor gas collection chamber is located on the inner uppermost part of the reactor shell. The inlet of the reactor gas collection chamber communicates with the gas outlet of the reactor gas-solid separation device, and the outlet of the reactor gas collection chamber communicates with a product gas transfer pipe. A reactor distributor for introducing naphtha raw material is provided on the lower part of the reaction zone.

[0078] In one embodiment, the reactor 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.

[0079] In a preferred embodiment, the device further comprises a fluidized bed regeneration device connected to the fluidized bed reactor, and the fluidized bed regeneration device is used to introduce a regeneration gas to convert the used catalyst into a regenerated catalyst. Referring to FIG. 1, the device comprises a fluidized bed reactor 1, a fluidized bed regeneration device 2, and a riser reactor 3.

[0080] The fluidized bed reactor 1 comprises a reactor shell 1-1, a reactor distributor 1-2, a reactor gas-solid separation device 1-3, a reactor gas collection chamber 1-4, a product gas transfer pipe 1-5, a reactor stripper 1-6, a used slide valve 1-7, and a used chemical transfer pipe 1-8.

[0081] The reactor shell 1-1 comprises an upper reactor shell and a lower reactor shell. The upper reactor shell surrounds a first gas-solid separation zone, and the lower reactor shell surrounds a reaction zone. An outlet of the riser reactor 3 is provided within the reactor shell 1-1.

[0082] A reactor distributor 1-2 is provided above the lower portion of the reaction zone, and the reactor distributor 1-2 is used to introduce the naphtha raw material.

[0083] Inside the reactor shell 1-1, a reactor gas-solid separation device 1-3 and a reactor gas collection chamber 1-4 are also provided. The reactor gas collection chamber 1-4 is located at the uppermost inner part of the reactor shell. The gas outlet of the reactor gas-solid separation device 1-3 communicates with the reactor gas collection chamber 1-4. The reactor gas collection chamber 1-4 communicates with the product gas transport pipe 1-5. Also, the catalyst outlet end of the reactor gas-solid separation device 1-3 is located above the opening end of the inlet pipe of the reactor stripper 1-6.

[0084] A reactor stripper 1-6 is provided below the reaction zone. The inlet of the reactor stripper 1-6 is located inside the reactor shell 1-1, and the outlet of the reactor stripper 1-6 is located outside the reactor shell 1-1 and is connected to the used slide valve 1-7. And the opening end of the inlet of the reactor stripper 1-6 is located above the reactor distributor 1-2.

[0085] A used slide valve 1-7 is provided below the reactor stripper 1-6. The inlet of the used slide valve 1-7 is connected to the outlet of the reactor stripper 1-6. The outlet of the used slide valve 1-7 is connected to the inlet of the used chemical transport pipe 1-8. And the outlet of the used chemical transport pipe 1-8 is connected to the regeneration device shell 2-1.

[0086] The used slide valve 1-7 is used to control the circulating amount of the used catalyst.

[0087] In a preferred embodiment, the reactor gas-solid separation device 1-3 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.

[0088] The fluidized bed regeneration device 2 includes a regeneration device shell 2-1, a regeneration device distributor 2-2, a regeneration device gas-solid separation device 2-3, a regeneration device gas collection chamber 2-4, a flue gas transfer pipe 2-5, a regeneration device stripper 2-6, and a regeneration slide valve 2-7.

[0089] The regeneration device shell 2-1 includes an upper regeneration device shell and a lower regeneration device shell. The upper regeneration device shell surrounds a second gas-solid separation zone, and the lower regeneration device shell surrounds a regeneration zone. The outlet of the used chemical transfer pipe 1-8 is arranged and configured inside the regeneration device shell 2-1.

[0090] A regeneration device distributor 2-2 is provided above the lower part of the regeneration zone, and the regeneration device distributor 2-2 is used to introduce regeneration gas.

[0091] Inside the regeneration device shell 2-1, a regeneration device gas-solid separation device 2-3 and a regeneration device gas collection chamber 2-4 are also provided. The regeneration device gas collection chamber 2-4 is located at the uppermost inner part of the regeneration device shell 2-1. The gas outlet of the regeneration device gas-solid separation device 2-3 communicates with the regeneration device gas collection chamber 2-4. The regeneration device gas collection chamber 2-4 communicates with the flue gas transfer pipe 2-5. The catalyst outlet end of the regeneration device gas-solid separation device 2-3 is located above the inlet pipe opening end of the regeneration device stripper 2-6.

[0092] A regeneration device stripper 2-6 is provided below the regeneration zone. The inlet of the regeneration device stripper 2-6 is located inside the regeneration device shell 2-1. The outlet of the regeneration device stripper 2-6 is located outside the regeneration device shell 2-1 and is connected to the regeneration slide valve 2-7. The opening end of the inlet of the regeneration device stripper 2-6 is located above the regeneration device distributor 2-2.

[0093] A regeneration slide valve 2-7 is provided below the regenerator stripper 2-6, and the inlet of the regeneration slide valve 2-7 is connected to the outlet of the regenerator stripper 2-6.

[0094] The regeneration slide valve 2-7 is used to control the amount of the circulating regeneration catalyst.

[0095] In a preferred embodiment, the regenerator gas-solid separation device 2-3 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.

[0096] The inlet of the riser reactor 3 is connected to the regeneration slide valve 2-7, and the outlet of the riser reactor 3 is connected to the reactor shell 1-1.

[0097] In order to realize the aromatization of straight-chain and branched-chain aliphatic hydrocarbons and increase the yield of aromatic hydrocarbons and the p-xylene content in mixed xylene, the present application presents a method for producing aromatic hydrocarbons from naphtha, including a step of producing aromatic hydrocarbons by using the device and catalyst for producing aromatic hydrocarbons from the above naphtha.

[0098] In one embodiment, the catalyst is a metal molecular sieve dual-functional catalyst.

[0099] In a preferred embodiment, the metal molecular sieve dual-functional catalyst is a metal-modified HZSM-5 zeolite molecular sieve.

[0100] The metal for metal modification is selected from at least one of La, Zn, Ga, Fe, Mo, and Cr.

[0101] The method for metal modification includes the steps of placing HZSM-5 zeolite molecular sieve in a metal salt solution, impregnating, drying, and calcining to obtain a metal-modified HZSM-5 zeolite molecular sieve. The metal-modified HZSM-5 zeolite molecular sieve is used in Examples 1 to 5 below.

[0102] In a preferred embodiment, the method includes the following steps. a) Naphtha enters the reaction zone of fluidized bed reactor 1 through reactor distributor 1-2 and contacts the catalyst flowing in from riser reactor 3 to generate a product gas stream containing BTX, light olefins, hydrogen, light alkanes, combustible gas, heavy aromatic hydrocarbons, and unconverted naphtha. At the same time, the catalyst is agglomerated and converted into used catalyst. The product gas stream enters reactor gas-solid separation device 1-3 to remove the used catalyst contained in the product gas stream, then enters reactor gas collection chamber 1-4, and enters the working section located downstream through product gas transfer pipe 1-5. The used catalyst in the reaction zone enters reactor stripper 1-6 from the open end of the inlet pipe of reactor stripper 1-6 for stripping. After the used catalyst is stripped, the used catalyst enters fluidized bed reactor 2 through used slide valve 1-7 and used chemical transfer pipe 1-8. b) The regeneration gas is introduced into the regeneration zone of fluidized bed regenerator 2 through regenerator distributor 2-2 and contacts the used catalyst. The coke on the used catalyst reacts with the regeneration gas to generate flue gas. At the same time, the used catalyst is converted into regenerated catalyst. The flue gas enters regenerator gas-solid separation device 2-3 to remove the regenerated catalyst contained in the flue gas, then enters regenerator gas collection chamber 2-4, and enters the working section located downstream through flue gas transfer pipe 2-5. The regenerated catalyst continuously passes through regenerator stripper 2-6 and regeneration slide valve 2-7 and enters riser reactor 3. c) The riser reactor raw materials are introduced into the riser reactor 3, come into contact with and react with the regenerated catalyst flowing in from the fluidized bed regenerator 2, and are converted into aromatic hydrocarbons under catalysis. Next, the flow containing unreacted riser reactor raw materials, aromatic hydrocarbons, and catalyst enters the fluidized bed reactor 1 from the outlet of the riser reactor 3.

[0103] Light olefins refer to ethylene and propylene.

[0104] Light alkanes refer to ethane and propane.

[0105] Combustible gas includes methane, CO, etc.

[0106] Heavy aromatic hydrocarbons refer to aromatic hydrocarbons with 9 or more carbon atoms in the molecule.

[0107] 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.

[0108] In a preferred embodiment, the naphtha also contains unconverted naphtha separated from the product gas stream.

[0109] In a preferred embodiment, the carbon content in the used catalyst is 1.0 wt% - 3.0 wt%.

[0110] In a preferred embodiment, the process conditions in the reaction zone are a superficial linear velocity of the gas of 0.5 m / s - 2.0 m / s, a reaction temperature of 500 °C - 650 °C, a reaction pressure of 100 kPa - 500 kPa, and a bed density of 150 kg / m 3 ~700 kg / m 3 3.

[0111] Optionally, the apparent linear velocity of the gas in the reaction zone is independently selected from any value or a value within the range between any two values of 0.5 m / s, 0.6 m / s, 0.7 m / s, 0.8 m / s, 0.9 m / s, 1.0 m / s, 1.1 m / s, 1.2 m / s, 1.3 m / s, 1.4 m / s, 1.5 m / s, 1.6 m / s, 1.7 m / s, 1.8 m / s, 1.9 m / s, and 2.0 m / s.

[0112] Optionally, the reaction temperature in the reaction zone is independently selected from any value or a value within the range between any two values of 500 °C, 510 °C, 520 °C, 530 °C, 540 °C, 550 °C, 560 °C, 570 °C, 580 °C, 590 °C, 600 °C, 610 °C, 620 °C, 630 °C, 640 °C, and 650 °C.

[0113] Optionally, the reaction pressure in the reaction zone is independently selected from any value or a value within the range between 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, and 500 kPa.

[0114] Optionally, the bed density in the reaction zone is any value or a value within the range between any two values of 150 kg / m 3 , 200 kg / m 3 , 250 kg / m 3 , 300 kg / m 3 , 350 kg / m 3 , 400 kg / m 3 , 450 kg / m 3 , 500 kg / m 3 , 550 kg / m 3 , 600 kg / m 3 , 650 kg / m 3 , and 700 kg / m 3 and is independently selected from a value within the range between any two of these values.

[0115] In a preferred embodiment, the carbon content in the regenerated catalyst is 0.5 wt% or less.

[0116] In a preferred embodiment, the regeneration gas is selected from at least one of oxygen, air, and oxygen-rich air.

[0117] In a preferred embodiment, the process conditions in the regeneration zone are a superficial linear velocity of the gas of 0.5 m / s to 2.0 m / s, a regeneration temperature of 600 °C to 750 °C, a regeneration pressure of 100 kPa to 500 kPa, and a bed density of 150 kg / m 3 ~700 kg / m 3 3.

[0118] Optionally, the superficial linear velocity of the gas is independently selected from any value or a value within a range between any two values of 0.5 m / s, 0.6 m / s, 0.7 m / s, 0.8 m / s, 0.9 m / s, 1.0 m / s, 1.1 m / s, 1.2 m / s, 1.3 m / s, 1.4 m / s, 1.5 m / s, 1.6 m / s, 1.7 m / s, 1.8 m / s, 1.9 m / s, and 2.0 m / s.

[0119] Optionally, the regeneration temperature is independently selected from any value or a value within a range between any two values of 600 °C, 615 °C, 630 °C, 645 °C, 660 °C, 675 °C, 690 °C, 705 °C, 720 °C, 735 °C, and 750 °C.

[0120] Optionally, the regeneration pressure is independently selected from any value or a value within a range between 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, and 500 kPa.

[0121] Optionally, the bed density is any value or 150 kg / m 3 , 200 kg / m 3 , 250 kg / m 3 , 300 kg / m 3 , 350 kg / m 3 , 400 kg / m3 , 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 is independently selected from values included in the range between any two of these values.

[0122] In a preferred embodiment, the riser reactor raw material includes steam separated from the product gas stream and low-carbon alkanes.

[0123] In a preferred embodiment, the steam content in the riser reactor raw material is 0 wt% to 50 wt%.

[0124] In a preferred embodiment, the process conditions of the riser reactor are a superficial gas linear velocity of 3.0 m / s to 10.0 m / s, a temperature of 580 °C to 700 °C, a pressure of 100 kPa to 500 kPa, and a bed density of 50 kg / m 3 to 150 kg / m 3 .

[0125] Optionally, the superficial gas linear velocity is independently selected from any value or values included in the range between any two 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, and 10.0 m / s.

[0126] Optionally, the temperature is independently selected from any value or values included in the range between any two of 580 °C, 590 °C, 600 °C, 610 °C, 620 °C, 630 °C, 640 °C, 650 °C, 660 °C, 670 °C, 680 °C, 690 °C, and 700 °C.

[0127] Optionally, the pressure is independently selected from any numerical value or a numerical value within a range between any two of the following values: 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.

[0128] Optionally, the layer density is independently selected from any numerical value or a numerical value within a range between any two of the following values: 50 kg / m3, 60 kg / m 3 、70 kg / m 3 、80 kg / m 3 、90 kg / m 3 、100 kg / m 3 、110 kg / m 3 、120 kg / m 3 、130 kg / m 3 、140 kg / m 3 、and 150 kg / m 3 and is independently selected from a numerical value within a range between any two of the above values.

[0129] In the embodiments of the present application, the potential content of aromatic hydrocarbons in the naphtha raw material is 0 wt% - 80 wt%, the single-pass conversion rate of naphtha is 70 wt% - 95 wt%, the unconverted naphtha is separated from the product gas and then returned to the fluidized bed reactor as a raw material, a part of the low-carbon alkane is separated from the product gas and then returned to the riser reactor as a raw material, and the finally obtained product is composed of 60 wt% - 75 wt% BTX, 7 wt% - 15 wt% low-carbon olefins, 3 wt% - 8 wt% hydrogen, 2 wt% - 7 wt% low-carbon alkanes, 4 wt% - 6 wt% combustible gas, 3 wt% - 7 wt% heavy aromatic hydrocarbons, and 0.5 wt% - 1 wt% coke. The content of p-xylene in the mixed xylene in the product is 50 wt% - 65 wt%.

Example

[0130] The device shown in Figure 1 is adopted in this embodiment.

[0131] In this embodiment, the naphtha raw material entering the fluidized bed reactor is directly coal liquefaction naphtha, and the potential content of aromatic hydrocarbons in the naphtha is 78 wt%. The naphtha raw material entering the fluidized bed reactor further includes unconverted naphtha separated from the product gas stream.

[0132] The process conditions in the reaction zone of the fluidized bed reactor are a superficial gas linear velocity of 0.5 m / s, a reaction temperature of 645 °C, a reaction pressure of 100 kPa, and a bed density of 700 kg / m 3 is.

[0133] The regeneration gas is air.

[0134] The process conditions in the regeneration zone of the fluidized bed regenerator are a superficial gas linear velocity of 0.5 m / s, a regeneration temperature of 745 °C, a regeneration pressure of 100 kPa, and a bed density of 700 kg / m 3 is.

[0135] The riser reactor raw material is low-carbon alkane separated from the product gas stream.

[0136] The process conditions of the riser reactor are a superficial gas linear velocity of 3.0 m / s, a temperature of 690 °C, a pressure of 100 kPa, and a bed density of 150 kg / m 3 is.

[0137] The carbon content in the used catalyst is 1.1 wt%, and the carbon content in the regenerated catalyst is 0.1 wt%.

[0138] The single-pass conversion rate of the naphtha raw material entering the fluidized bed reactor is 71 wt%.

[0139] The product is composed of 74.5 wt% BTX, 7 wt% low-carbon olefins, 3 wt% hydrogen, 2 wt% low-carbon alkanes, 6 wt% combustible gas, 7 wt% heavy aromatic hydrocarbons, and 0.5 wt% coke. The content of p-xylene in the mixed xylene in the product is 51 wt%.

Example

[0140] The device shown in FIG. 1 is adopted in this embodiment.

[0141] In this embodiment, the naphtha raw material entering the fluidized bed reactor is indirect coal liquefaction naphtha, and the potential content of aromatic hydrocarbons in the naphtha is 0.1 wt%. The naphtha raw material entering the fluidized bed reactor further includes unconverted naphtha separated from the product gas stream.

[0142] The process conditions in the reaction zone of the fluidized bed reactor are an apparent linear gas velocity of 2.0 m / s, a reaction temperature of 510 °C, a reaction pressure of 500 kPa, and a bed density of 150 kg / m 3 It is.

[0143] The regeneration gas is oxygen.

[0144] The process conditions in the regeneration zone of the fluidized bed regenerator are an apparent linear gas velocity of 2.0 m / s, a regeneration temperature of 610 °C, a regeneration pressure of 500 kPa, and a bed density of 150 kg / m 3 It is.

[0145] The riser reactor raw material includes steam and lower alkanes separated from the product gas stream, and the steam content in the riser reactor raw material is 50 wt%.

[0146] The process conditions of the riser reactor are an apparent linear gas velocity of 10.0 m / s, a temperature of 580 °C, a pressure of 500 kPa, and a bed density of 50 kg / m 3 It is.

[0147] The carbon content in the used catalyst is 2.8 wt%, and the carbon content in the regenerated catalyst is 0.3 wt%.

[0148] The single-pass conversion rate of the naphtha raw material entering the fluidized bed reactor is 75 wt%.

[0149] The product is composed of 66 wt% BTX, 12 wt% light olefins, 7 wt% hydrogen, 3 wt% light alkanes, 5 wt% combustible gas, 6 wt% heavy aromatic hydrocarbons, and 1.0 wt% coke. The content of p-xylene in the mixed xylene in the product is 61 wt%.

Example

[0150] The device shown in FIG. 1 is adopted in this embodiment.

[0151] In this embodiment, the naphtha raw material entering the fluidized bed reactor is indirect coal liquefaction naphtha, and the potential content of aromatic hydrocarbons in the naphtha is 3 wt%. The naphtha raw material entering the fluidized bed reactor further includes unconverted naphtha separated from the product gas stream.

[0152] The process conditions in the reaction zone of the fluidized bed reactor are a superficial gas linear velocity of 1.2 m / s, a reaction temperature of 550 °C, a reaction pressure of 120 kPa, and a bed density of 260 kg / m 3 3.

[0153] The regeneration gas is air rich in oxygen.

[0154] The technical conditions in the regeneration zone of the fluidized bed regenerator are a superficial gas linear velocity of 1.2 m / s, a regeneration temperature of 650 °C, a regeneration pressure of 120 kPa, and a bed density of 260 kg / m 3 3.

[0155] The riser reactor raw material includes steam and light alkanes separated from the product gas stream, and the steam content in the riser reactor raw material is 25 wt%.

[0156] The process conditions of the riser reactor are a superficial gas linear velocity of 7.0 m / s, a temperature of 630 °C, a pressure of 120 kPa, and a bed density of 80 kg / m 3 3.

[0157] The carbon content in the used catalyst is 2.1 wt%, and the carbon content in the regenerated catalyst is 0.2 wt%.

[0158] The single-pass conversion rate of the naphtha raw material entering the fluidized bed reactor is 95 wt%.

[0159] The product consists of 61 wt% BTX, 15 wt% lower olefins, 8 wt% hydrogen, 7 wt% lower alkanes, 5.2 wt% combustible gas, 3 wt% heavy aromatic hydrocarbons, and 0.8 wt% coke. The content of p-xylene in the mixed xylene in the product is 65 wt%.

Example

[0160] The device shown in Figure 1 is adopted in this embodiment.

[0161] In this embodiment, the naphtha raw material entering the fluidized bed reactor is straight-run naphtha, and the potential content of aromatic hydrocarbons in the naphtha is 46 wt%. The naphtha raw material entering the fluidized bed reactor further includes unreacted naphtha separated from the product gas stream.

[0162] The process conditions in the reaction zone of the fluidized bed reactor are a superficial gas linear velocity of 1.8 m / s, a reaction temperature of 600 °C, a reaction pressure of 200 kPa, and a bed density of 220 kg / m 3 is.

[0163] The regeneration gas is air.

[0164] The process conditions in the regeneration zone of the fluidized bed regenerator are a superficial gas linear velocity of 1.8 m / s, a regeneration temperature of 700 °C, a regeneration pressure of 200 kPa, and a bed density of 220 kg / m 3 is.

[0165] The riser reactor raw material includes steam and lower alkanes separated from the product gas stream, and the steam content in the riser reactor raw material is 50 wt%.

[0166] The process conditions of the riser reactor are a superficial gas linear velocity of 5.0 m / s, a temperature of 660 °C, a pressure of 200 kPa, and a bed density of 110 kg / m3 It is as follows.

[0167] The carbon content in the used catalyst is 1.5 wt%, and the carbon content in the regenerated catalyst is 0.1 wt%.

[0168] The single-pass conversion rate of the naphtha raw material entering the fluidized bed reactor is 86 wt%.

[0169] The product is composed of 68 wt% BTX, 10 wt% light olefins, 6 wt% hydrogen, 5 wt% light alkanes, 4 wt% combustible gas, 6 wt% heavy aromatic hydrocarbons, and 1.0 wt% coke. The content of p-xylene in the mixed xylene in the product is 63 wt%.

Example

[0170] The device shown in FIG. 1 is adopted in this embodiment.

[0171] In this embodiment, the naphtha raw material entering the fluidized bed reactor is hydrocracked naphtha, and the potential content of aromatic hydrocarbons in the naphtha is 64 wt%. The naphtha raw material entering the fluidized bed reactor further includes unreacted naphtha separated from the product gas stream.

[0172] The process conditions in the reaction zone of the fluidized bed reactor are a superficial gas linear velocity of 1.0 m / s, a reaction temperature of 580 °C, a reaction pressure of 150 kPa, and a bed density of 350 kg / m 3 It is as follows.

[0173] The regeneration gas is air.

[0174] The process conditions in the regeneration zone of the fluidized bed regenerator are a superficial gas linear velocity of 1.0 m / s, a regeneration temperature of 680 °C, a regeneration pressure of 150 kPa, and a bed density of 350 kg / m 3 It is as follows.

[0175] The riser reactor raw material contains water vapor and low-carbon alkanes separated from the product gas stream, and the water vapor content in the riser reactor raw material is 40 wt%.

[0176] The process conditions of the riser reactor are a superficial gas linear velocity of 7.0 m / s, a temperature of 650 °C, a pressure of 150 kPa, and a bed density of 80 kg / m 3 is.

[0177] The carbon content in the used catalyst is 1.4 wt%, and the carbon content in the regenerated catalyst is 0.5 wt%.

[0178] The single-pass conversion rate of the naphtha raw material entering the fluidized bed reactor is 77 wt%.

[0179] The product is composed of 71.3 wt% BTX, 9 wt% low-carbon olefins, 5 wt% hydrogen, 2 wt% low-carbon alkanes, 6 wt% combustible gas, 6 wt% heavy aromatic hydrocarbons, and 0.7 wt% coke. The content of p-xylene in the mixed xylene in the product is 58 wt%.

[0180] The above are only some embodiments of the present application, and in no form is it intended to limit the present application. Although the present application is disclosed in the above-described preferred embodiments, such preferred embodiments are not intended to limit the present application. Without departing from the scope of the technical solution of the present application, changes or modifications made by those skilled in the art by using the above-disclosed technical content are equivalent to equivalent embodiments and all fall within the scope of the technical solution of the present application.

Description of Reference Numerals

[0181] 1 Fluidized bed reactor 1-1 Reactor shell 1-2 Reactor distributor 1-3 Reactor gas-solid separation device 1-4 Reactor gas collection chamber 1-5 Product gas transfer pipe 1-6 Reactor stripper 1-7 Used slide valve 1-8 Used chemical transfer pipe 2 Fluidized bed regeneration device 2-1 Regeneration device shell 2-2 Regeneration device distributor 2-3 Regeneration device gas-solid separation device 2-4 Regeneration device gas collection chamber 2-5 Flue gas transfer pipe 2-6 Regeneration device stripper 2-7 Regeneration slide valve 3 Riser reactor

Claims

1. A device for producing aromatic hydrocarbons from naphtha, comprising: a fluidized bed reactor and a riser reactor; the outlet of the riser reactor is connected to the fluidized bed reactor; the fluidized bed reactor is used to introduce naphtha raw materials, contact them with the catalyst flowing in from the riser reactor, react with them to produce a product gas stream containing BTX and spent catalyst; the product gas stream is subjected to gas-solid separation; the separated product gas stream is sent to a downstream working section; the unreacted naphtha after separation returns to the fluidized bed reactor as raw material; a portion of the separated lower-carbon alkanes returns to the riser reactor as raw material; the device.

2. The riser reactor is used to introduce riser reactor raw materials and a catalyst, react them to produce aromatic hydrocarbons, and a stream containing unreacted riser reactor raw materials, aromatic hydrocarbons, and catalyst enters the fluidized bed reactor through the outlet of the riser reactor. The device for producing aromatic hydrocarbons from naphtha according to Claim 1.

3. The riser reactor raw materials include steam and lower-carbon alkanes separated from the product gas stream. The device for producing aromatic hydrocarbons from naphtha according to Claim 2.

4. The steam content in the riser reactor raw materials is 0 wt% to 50 wt%. The device for producing aromatic hydrocarbons from naphtha according to Claim 2 or 3.

5. The inlet of the riser reactor is connected to a fluidized bed regenerator, and the catalyst introduced into the riser reactor is the regenerated catalyst produced by the fluidized bed regenerator. The device for producing aromatic hydrocarbons from naphtha according to Claim 1.

6. The fluidized bed regenerator continuously passes through a regeneration slide valve connected to the inlet of the riser reactor through a regenerator stripper and a pipeline. The device for producing aromatic hydrocarbons from naphtha according to Claim 5.

7. The inlet of the regenerator stripper extends to the inside of the regenerator shell of the fluidized bed regenerator and is located above the regenerator distributor. The device for producing aromatic hydrocarbons from naphtha according to Claim 6.

8. The fluidized bed reactor comprises a reactor shell, and the region surrounded by the reactor shell is divided from the uppermost part to the lowermost part into a first gas-solid separation zone and a reaction zone. A gas-solid separation device and a reactor gas collection chamber are provided in the first gas-solid separation zone. The reactor gas collection chamber is located on the inner uppermost part of the reactor shell. The inlet of the reactor gas collection chamber communicates with the gas outlet of the reactor gas-solid separation device, and the outlet of the reactor gas collection chamber communicates with the product gas transport pipe. A reactor distributor for introducing naphtha raw materials is provided on the lower part of the reaction zone. A device for producing aromatic hydrocarbons from naphtha according to claim 1.

9. The reactor 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. A device for producing aromatic hydrocarbons from naphtha according to claim 8.

10. The device further comprises a fluidized bed regenerator connected to the fluidized bed reactor, and the fluidized bed regenerator is used to introduce a regeneration gas to convert the used catalyst into a regenerated catalyst. A device for producing aromatic hydrocarbons from naphtha according to claim 1.

11. The fluidized bed reactor continuously passes through a reactor stripper, a used slide valve, and a used chemical transport pipe connected to the fluidized bed regenerator. The inlet of the reactor stripper extends to the inside of the fluidized bed reactor shell and is located below the catalyst outlet of the reactor gas-solid separation device. A device for producing aromatic hydrocarbons from naphtha according to claim 1.

12. The fluidized bed regenerator comprises a regenerator shell, and the region surrounded by the regenerator shell is divided from the uppermost part to the lowermost part into a second gas-solid separation zone and a regeneration zone. A regenerator gas-solid separation device and a regenerator gas collection chamber are provided in the second gas-solid separation zone. The regenerator gas collection chamber is located on the inner uppermost part of the regenerator shell, and a flue gas transport pipe is provided on the regenerator gas collection chamber; The gas outlet of the regeneration device gas-solid separation device communicates with the regeneration device gas collection chamber; a regeneration device distributor for introducing regeneration gas is provided on the inner lower part of the regeneration zone, the device for producing aromatic hydrocarbons from naphtha according to claim 1.

13. The regeneration device 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, the device for producing aromatic hydrocarbons from naphtha according to claim 12.

14. A method for producing aromatic hydrocarbons from naphtha, which includes the step of producing aromatic hydrocarbons by using the device and catalyst for producing aromatic hydrocarbons from naphtha according to any one of claims 1 to 13.

15. The method for producing aromatic hydrocarbons from naphtha according to claim 14, wherein the catalyst is a metal molecular sieve dual-functional catalyst.

16. The metal molecular sieve dual-functional catalyst is a metal-modified HZSM-5 zeolite molecular sieve, the metal for metal modification is selected from at least one of La, Zn, Ga, Fe, Mo, and Cr, the method for 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 a metal-modified HZSM-5 zeolite molecular sieve, the method for producing aromatic hydrocarbons from naphtha according to claim 15.

17. To contact with the catalyst flowing in from the riser reactor to generate a product gas stream containing BTX, low-carbon olefins, hydrogen, low-carbon alkanes, combustible gas, heavy aromatic hydrocarbons, and unconverted naphtha, enabling naphtha to enter the reaction zone of the fluidized bed reactor through the reactor distributor, while at the same time enabling the catalyst to be agglomerated and converted into used catalyst; To enable the product gas stream containing the used catalyst to enter the reactor gas-solid separation device, then enter the reactor gas collection chamber, and enter the working section located downstream through the product gas transport pipe for the purpose of removing the used catalyst contained in the product gas stream The method for producing aromatic hydrocarbons from naphtha according to claim 14, comprising

18. The method for producing aromatic hydrocarbons from naphtha according to claim 17, further comprising a step that enables the unreacted naphtha after separation to return to the fluidized bed reactor as a raw material.

19. The method for producing aromatic hydrocarbons from naphtha according to claim 17, further comprising a step that enables a part of the low-carbon alkanes after separation to return to the riser reactor as a raw material.

20. Low-carbon olefins refer to ethylene and propylene, Low-carbon alkanes refer to ethane and propane, The combustible gas contains methane and CO, Heavy aromatic hydrocarbons refer to aromatic hydrocarbons having 9 or more carbon atoms in the molecule, The method for producing aromatic hydrocarbons from naphtha according to claim 17.

21. The method for producing aromatic hydrocarbons from naphtha according to claim 17, wherein the naphtha is selected from at least one of direct coal liquefaction naphtha, indirect coal liquefaction naphtha, straight-run naphtha, and hydrocracked naphtha.

22. The naphtha also contains unconverted naphtha separated from the product gas stream, and the unconverted naphtha contains C 4 to C 12 The method for producing aromatic hydrocarbons from naphtha according to claim 21, comprising a main component consisting of linear and branched aliphatic hydrocarbons and naphthenic hydrocarbons.

23. The method for producing aromatic hydrocarbons from naphtha according to claim 17, wherein the carbon content in the used catalyst is 1.0 wt% to 3.0 wt%.

24. The process conditions of the reaction zone are a superficial linear velocity of the gas of 0.5 m / s to 2.0 m / s, a reaction temperature of 500 °C to 650 °C, a reaction pressure of 100 kPa to 500 kPa, and a bed density of 150 kg / m 3 to 700 kg / m 3 A process for producing aromatic hydrocarbons from naphtha according to claim 17, wherein the process conditions are as described above.

25. A step of introducing the riser reactor raw material and the catalyst into the riser reactor for reaction to produce aromatic hydrocarbons; and A step that enables the flow containing the unreacted riser reactor raw material, aromatic hydrocarbons, and the catalyst to enter the fluidized bed reactor from the outlet of the riser reactor The method for producing aromatic hydrocarbons from naphtha according to claim 17, further comprising.

26. The method for producing aromatic hydrocarbons from naphtha according to claim 25, wherein the catalyst is a regenerated catalyst flowing in from a fluidized bed regenerator.

27. The method for producing aromatic hydrocarbons from naphtha according to claim 26, wherein the regenerated catalyst continuously passes through a regenerator stripper and a regeneration slide valve and enters the riser reactor.

28. The method for producing aromatic hydrocarbons from naphtha according to claim 26, wherein the carbon content in the regenerated catalyst is 0.5 wt% or less.

29. The method for producing aromatic hydrocarbons from naphtha according to claim 25, wherein the riser reactor raw material contains steam and low-carbon alkanes separated from the product gas stream.

30. The method for producing aromatic hydrocarbons from naphtha according to claim 25, wherein the water vapor content in the riser reactor raw material is 0 wt% to 50 wt%.

31. The process conditions of the riser reactor are a superficial gas linear velocity of 3.0 m / s to 10.0 m / s, a temperature of 580 °C to 700 °C, a pressure of 100 kPa to 500 kPa, and a bed density of 50 kg / m 3 to 150 kg / m 3 A method for producing aromatic hydrocarbons from naphtha according to claim 25, wherein the method is as described above.

32. The method for producing aromatic hydrocarbons from naphtha according to claim 17, further comprising a step of allowing the spent catalyst to enter the reactor stripper from the open end of the inlet pipe of the reactor stripper, and after the spent catalyst is stripped by the reactor stripper, allowing the spent catalyst to enter the downstream region through the spent slide valve and the spent chemical transfer pipe.

33. The method for producing aromatic hydrocarbons from naphtha according to claim 32, wherein the downstream region is a fluidized bed regenerator.

34. The method for producing aromatic hydrocarbons from naphtha according to claim 32, further comprising a step of introducing a regeneration gas into the regeneration zone of the fluidized bed regenerator through a regenerator distributor to contact the spent catalyst flowing in from the fluidized bed reactor, allowing the coke on the spent catalyst to react with the regeneration gas to generate flue gas, and at the same time allowing the spent catalyst to be converted into a regenerated catalyst.

35. The spent catalyst continuously passes through the reactor stripper, the spent slide valve, and the spent chemical transfer pipe and enters the fluidized bed regenerator, contacts and reacts with the regeneration gas to obtain flue gas and regenerated catalyst, the flue gas enters a regenerator gas-solid separation device to remove the regenerated catalyst contained in the flue gas, then enters a regenerator gas collection chamber, and enters a working section located downstream through a flue gas transfer pipe, The method for producing aromatic hydrocarbons from naphtha according to claim 34.

36. The method for producing aromatic hydrocarbons from naphtha according to claim 34, wherein the regeneration gas is selected from at least one of oxygen, air, and oxygen-rich air.

37. The process conditions of the regeneration zone are a superficial linear velocity of the gas of 0.5 m / s to 2.0 m / s, a regeneration temperature of 600°C to 750°C, a regeneration pressure of 100 kPa to 500 kPa, and a bed density of 150 kg / m 3 to 700 kg / m 3 A method for producing aromatic hydrocarbons from naphtha according to claim 34, wherein the method is as described above.

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