CN111233608A - A kind of raw material conversion method containing naphtha - Google Patents

Abstract

The present application discloses a method for converting a raw material containing naphtha, which includes the following steps: a) after the raw material containing naphtha and a catalyst are contacted and reacted in a riser reactor, pass into a fluidized bed reactor, and pass through a fluidized bed reactor. Separation in the enlarged section of the fluidized bed reactor to obtain a product gas I and a catalyst pre-deposited; the catalyst pre-deposited goes down to the reaction section of the fluidized bed reactor; b) will contain naphtha and/or Or the raw material of methanol is input from the bottom of the fluidized-bed reactor, and goes up to the reaction section of the fluidized-bed reactor to contact with the catalyst after carbon deposition, to obtain product gas II and the catalyst to be regenerated; After the regenerated catalyst descends into the regenerator for regeneration, a regenerated catalyst is obtained; c) returns to the riser reactor through the regenerated catalyst. The method is used in the catalytic cracking of naphtha, and has the advantage of adjustable product types.

Description

A kind of raw material conversion method containing naphtha

technical field

The invention relates to a method for converting raw materials containing naphtha into low-carbon olefins, aromatic hydrocarbons and high-quality gasoline, and belongs to the field of catalysis.

Background technique

Naphtha is one of the most important raw materials for the production of ethylene and propylene. High-temperature steam cracking of naphtha to produce chemical products such as ethylene and propylene is a huge petrochemical industry. Every year, hundreds of millions of tons of naphtha are used to produce ethylene propylene, and its output accounts for more than 50% of the total ethylene propylene production. After years of development, steam cracking technology has reached a high level, and its conversion rate is high. After one reaction, the product yield can reach a high level. However, the disadvantages are also obvious, the selectivity is poor, a large amount of methane is generated in the product, the reaction temperature is high, and the energy consumption is high. Its development potential is already very small. To this end, catalytic cracking technology that uses catalysts to reduce the cracking temperature has been vigorously developed. At present, the naphtha catalytic cracking technology is mainly carried out through a riser reactor to improve the yield of ethylene and propylene. But the relatively adjustable range is small.

With the application of technologies such as coal-to-olefin technology and propane dehydrogenation to propylene, the sources of ethylene and propylene are increasingly abundant. This requires the naphtha catalytic cracking technology to have higher adjustable variability to meet changes in market demand. This application solves this problem very well.

SUMMARY OF THE INVENTION

According to one aspect of the present application, a method for converting a naphtha-containing feedstock into light olefins, aromatics and high-quality gasoline is provided. The method is used in the catalytic cracking of naphtha, and has the advantage of adjustable product types.

In order to achieve the above purpose, the present application provides a method for converting a naphtha-containing feedstock into low-carbon olefins, aromatic hydrocarbons and high-quality gasoline, the method comprising the following steps: the feedstock including the naphtha enters a riser reactor and a catalyst Contact, the generated product and catalyst stream enter the expansion section of the fluidized bed reactor for separation, the product enters the product gas outlet line, and the catalyst enters the reaction section of the fluidized bed reactor, and the raw materials including naphtha or/and methanol are reacted through the fluidized bed The feed port of the reactor enters the reaction section of the fluidized bed reactor to react with the catalyst, the generated product enters the product gas outlet pipeline, and the catalyst descends into the stripping section of the fluidized bed reactor. , into the regenerator, the regenerated catalyst enters the riser reactor through the regenerator stripping section and the regeneration inclined pipe; the product gas enters the separation system through the product gas outlet pipeline to obtain different products.

In the above scheme, the conditions of the riser reactor: the reaction temperature is 580～720℃, the reaction pressure is 0.01～0.3MPa in gauge pressure, and the gas phase linear velocity is 3～10m/s; the fluidized bed reactor conditions: The reaction temperature is 580-720°C, the reaction pressure is 0.01-0.3Pa in gauge pressure, the gas phase linear velocity is 0.5-1.5m/s, and the mass space velocity is 0.5-2h ^-1 .

The carbon content of the regenerated catalyst is less than 0.2% by mass.

The transformation method of the raw material containing naphtha is characterized in that, comprises the following steps:

a) after the raw material containing naphtha and the catalyst are contacted and reacted in the riser reactor, they are passed into the fluidized bed reactor and separated through the enlarged section of the fluidized bed reactor to obtain product gas I and the catalyst through pre-carbon deposition; The pre-carbonized catalyst descends to the reaction section of the fluidized bed reactor;

b) inputting the raw material containing naphtha and/or methanol from the bottom of the fluidized bed reactor, and going up to the reaction section of the fluidized bed reactor to contact with the carbon deposited catalyst to obtain product gas II and the catalyst to be regenerated; after the catalyst to be regenerated goes down into the regenerator for regeneration, the regenerated catalyst is obtained;

c) returning the regenerated catalyst to the riser reactor;

Among them, product gas I and product gas II are mixed and output, and after separation, olefins, aromatics and gasoline are obtained.

Optionally, the olefin includes ethylene, propylene, butene.

Optionally, the aromatic hydrocarbons include benzene, toluene, and xylene.

Optionally, the conditions of the riser reactor: the reaction temperature is 580-720° C., the reaction pressure is 0.01-0.3 MPa in gauge pressure, and the gas phase linear velocity is 3-10 m/s;

The conditions of the fluidized bed reactor: the reaction temperature is 580-720°C, the reaction pressure is 0.01-0.3Pa in gauge pressure, the gas phase linear velocity is 0.5-1.5m/s, and the total mass of methanol and/or naphtha is empty. The speed is 0.5～2h ^-1 . Among them, the ratio of methanol and naphtha can be adjusted arbitrarily.

Optionally, the upper limit of the reaction temperature in the riser reactor is selected from 590°C, 600°C, 610°C, 620°C, 630°C, 640°C, 650°C, 660°C, 670°C, 680°C, 690°C , 700°C, 710°C or 720°C; the lower limit is selected from 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 °C or 710 °C.

Optionally, the upper limit of the reaction pressure in the riser reactor is selected from 0.02MPa, 0.05MPa, 0.08MPa, 0.1MPa, 0.15MPa, 0.2MPa, 0.25MPa or 0.3MPa in gauge pressure; the lower limit is selected from 0.01MPa , 0.02MPa, 0.05MPa, 0.08MPa, 0.1MPa, 0.15MPa, 0.2MPa or 0.25MPa.

Optionally, the upper limit of the linear velocity of the gas phase in the riser reactor is selected from 3m/s, 4m/s, 5m/s, 6m/s, 7m/s, 8m/s, 9m/s or 10m/s ; the lower limit is selected from 2m/s, 3m/s, 4m/s, 5m/s, 6m/s, 7m/s, 8m/s or 9m/s.

Optionally, the upper limit of the reaction temperature in the fluidized bed reactor is selected from 590°C, 600°C, 610°C, 620°C, 630°C, 640°C, 650°C, 660°C, 670°C, 680°C, 690°C ℃, 700℃, 710℃ or 720℃; the lower limit is selected from 580℃, 590℃, 600℃, 610℃, 620℃, 630℃, 640℃, 650℃, 660℃, 670℃, 680℃, 690℃, 700°C or 710°C.

Optionally, the upper limit of the reaction pressure in the fluidized bed reactor is selected from 0.02MPa, 0.05MPa, 0.08MPa, 0.1MPa, 0.15MPa, 0.2MPa, 0.25MPa or 0.3MPa in gauge pressure; the lower limit is selected from 0.01 MPa, 0.02MPa, 0.05MPa, 0.08MPa, 0.1MPa, 0.15MPa, 0.2MPa or 0.25MPa.

Optionally, the upper limit of the linear velocity of the gas phase in the fluidized bed reactor is selected from 1 m/s or 1.5 m/s; the lower limit is selected from 0.5 m/s or 1 m/s.

Optionally, the upper limit of the total mass space velocity in the fluidized bed reactor is selected from 1h ^-1 , 1.5h ^-1 , or 2h ^-1 ; the lower limit is selected from 0.5h ^{-1 ,} 1h ^-1 or 1.5h -1 ¹ .

Optionally, the mass ratio of the feed amount of the riser reactor and the fluidized bed reactor is 1:9-9:1.

Optionally, the mass ratio of the feed amount of the riser reactor and the fluidized bed reactor is 1:9, 1:7, 1:5, 1:3, 1:1, 3:1, 5 :1, 9:1, and the range between any two ratios.

Optionally, step a) includes: the raw material containing naphtha is contacted and reacted with the catalyst in the riser, and the obtained stream including the pre-reacted catalyst and the product gas I ascends to the fluidized bed reactor; including the catalyst and the product gas The stream of I is separated in the expansion section of the fluidized bed reactor, the product gas I enters the product gas outlet line, and the pre-reacted catalyst descends to the reaction section of the fluidized bed reactor.

Optionally, step b) includes: inputting the raw material containing naphtha and methanol from the bottom of the fluidized bed reactor, and ascending to the reaction section of the fluidized bed reactor and the pre-reacted catalyst contact to obtain product gas II and the catalyst to be regenerated; the product gas II goes up to the expansion section of the fluidized bed reactor and enters the product gas outlet pipeline; the catalyst to be regenerated goes down to the stripping section of the fluidized bed reactor , enter the regenerator through the inclined tube and the riser to be regenerated.

Optionally, step c) includes: returning the regenerated catalyst to the riser reactor through the regenerator stripping section and the regeneration inclined pipe.

Optionally, the carbon content of the regenerated catalyst is less than 0.5% by mass.

Optionally, the carbon content of the regenerated catalyst is less than 0.2% by mass.

Optionally, the carbon content of the regenerated catalyst is less than 0.1% by mass.

Optionally, the catalyst is a microsphere catalyst containing naphtha catalytic cracking activity; the diameter of the microsphere catalyst is 30-300 μm.

Optionally, the weight content of the molecular sieve in the microsphere catalyst is 10-50%.

Optionally, the upper limit of the weight content of molecular sieve in the microsphere catalyst is selected from 20%, 30%, 40% or 50%; the upper limit is selected from 10%, 20%, 30% or 40%.

Optionally, the diameter of the microsphere catalyst is preferably 50-150 μm.

Optionally, the catalyst is a microsphere catalyst containing ZSM-5 molecular sieve.

Optionally, the forming of the microsphere catalyst includes: spray-drying the slurry containing the molecular sieve and the binder.

Optionally, the distillation range of the naphtha is between 20 and 200°C.

As an embodiment, the described method comprises the following steps: the raw material containing naphtha enters the riser reactor to contact with the catalyst, the generated product I and the catalyst stream enter the fluidized bed reactor expansion section for separation, and the product I enters the The product gas outlet pipeline, the catalyst enters the reaction section of the fluidized bed reactor, the raw material containing naphtha and/or methanol enters the reaction section of the fluidized bed reactor through the feed port of the fluidized bed reactor and reacts with the catalyst to generate product II After entering the product gas outlet pipeline, the catalyst descends into the stripping section of the fluidized bed reactor. After stripping, it enters the regenerator through the inclined tube to be regenerated and the riser. The regenerated catalyst passes through the stripping section of the regenerator and the inclined tube for regeneration. Enter the riser reactor; the product gas enters the separation system through the product gas outlet line to obtain products including olefins, aromatics and gasoline.

Optionally, in the method, the mass yields of olefins, aromatics and gasoline can be adjusted.

Optionally, the mass yield of olefins is 42-72%, the mass yield of aromatics is 16-24%, and the mass yield of gasoline is 6-21%.

The beneficial effects that this application can produce include:

1) The riser reactor and the fluidized bed reactor of the device of the present application can simultaneously or independently carry out the catalytic cracking reaction of naphtha.

2) In the present application, the content of product components can be regulated in a wide range by adjusting the feed ratio of the riser reactor and the fluidized bed reactor.

3) The present application provides a conversion method containing naphtha raw materials, the products are low-carbon olefins, light aromatic hydrocarbons and high-quality gasoline, and the product ratio can be adjusted. In the method, the raw materials including naphtha are simultaneously fed into the riser reactor and the fluidized bed reactor, and the reaction products are merged at the top outlet of the fluidized bed reactor and then enter the separation system to obtain low-carbon olefins, light aromatics and high-quality Gasoline; the catalyst enters the fluidized bed reactor from the regenerator through the riser reactor, and returns to the regenerator for regeneration after the catalytic cracking is completed. The method improves the modulation range of the naphtha catalytic cracking product and improves the ability of the device to resist the risk of market fluctuations.

Description of drawings

FIG. 1 is a schematic flowchart of the device described in the present application.

List of parts and reference numbers:

1: feed inlet of riser reactor, 2: riser reactor, 3: fluidized bed reactor, 4: feed inlet of fluidized bed reactor, 5: inlet of stripping section of fluidized bed reactor, 6: Riser riser inlet, 7: Product gas outlet line, 8: Flue gas outlet line, 9: Regenerator, 10: Regeneration air inlet, 11: Regenerator stripping section inlet, 12: Regeneration inclined pipe, 13: Inclined pipe to be grown, 14: Expanded section of fluidized bed reactor, 15: Reacted section of fluidized bed reactor, 16: Stripping section of fluidized bed reactor, 17: Expanded section of regenerator, 18: Regeneration of regenerator Section, 19: Regenerator stripping section, 20: Riser 20.

Detailed ways

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

Unless otherwise specified, the raw materials in the examples of this application are all purchased through commercial channels.

In the embodiment, the catalyst is "microspheres containing naphtha catalytic cracking activity", and the catalyst is prepared according to the method of patent CN200710118286.3.

The analytical method in the embodiment of the application is as follows:

Product analysis was performed using Agilent gas chromatography.

In the embodiment of the application, conversion rate, selectivity are calculated as follows:

In the embodiment of this application, the olefin yield, aromatics yield, and methane yield are all calculated based on mass:

Olefin yield=(olefin mass content in product*product mass flow rate)/(product mass flow rate+coking rate); aromatics yield=(aromatic mass content in product*product mass flow rate)/(product mass flow rate + coke formation rate); methane yield=(methane mass content in product*product mass flow rate)/(product mass flow rate+ coke formation rate).

Fig. 1 is the device adopted in the method for converting the raw material containing naphtha into light olefins and aromatic hydrocarbons of the application, and the method comprises the following steps: the raw material including naphtha enters the riser reactor 2 to contact with the catalyst, and the generated products and The catalyst stream enters the expansion section 14 of the fluidized bed reactor for separation, the product enters the product gas outlet pipeline, and the catalyst enters the reaction section 15 of the fluidized bed reactor, and the raw materials including naphtha or/and methanol pass through the fluidized bed reactor feed port 4. Enter the reaction section of the fluidized bed reactor to react with the catalyst, the generated product enters the product gas outlet pipeline, and the catalyst descends into the stripping section 16 of the fluidized bed reactor. , enter the regenerator 9, the regenerated catalyst enters the riser reactor 2 through the regenerator stripping section 19 and the regeneration inclined pipe 12; the product gas enters the separation system through the product gas outlet pipeline to obtain different products. ,

Example 1

In the device shown in Figure 1, the catalyst is a microsphere catalyst containing naphtha catalytic cracking activity, the weight content of molecular sieve in the catalyst is 30%, and the particle size range is 50-150 microns. The raw material including naphtha enters the riser reactor to contact the catalyst, the generated product and catalyst stream enter the expansion section of the fluidized bed reactor for separation, the product enters the product gas outlet line, and the catalyst enters the reaction section of the fluidized bed reactor, including the The raw materials of naphtha or/and methanol enter the reaction section of the fluidized bed reactor through the feed port of the fluidized bed reactor to react with the catalyst, the generated product enters the product gas outlet pipeline, and the catalyst descends into the stripping section of the fluidized bed reactor, After stripping, it enters the regenerator through the inclined tube to be grown and the riser, and the regenerated catalyst enters the riser reactor through the stripping section of the regenerator and the regeneration inclined tube. The product gas enters the separation system through the product gas outlet line to obtain different products. The amount of catalyst circulating is controlled by a plug valve or spool valve. The mass fraction of carbon content of the regenerated catalyst is less than 0.1%. The composition of naphtha is shown in Table 1. Conditions of the riser reactor: the reaction temperature was 700°C, the reaction pressure was 0.01 MPa in gauge pressure, and the gas phase linear velocity was 3 m/s; fluidized bed reactor conditions: the reaction temperature was 690°C, and the reaction pressure was gauged as 0.01MPa, the linear velocity of the gas phase is 1m/s, and the mass ratio of naphtha and methanol is 2. The mass ratio of the feed to the riser reactor and the fluidized bed reactor was 1:1. Keep the catalyst circulation stable, and the mass space velocity of the fluidized bed reactor is 1h ^-1 . The product gas was analyzed by online chromatography, and the mass yield of olefin was 54%, the mass yield of BTX was 23%, and the mass yield of high-quality gasoline was 15%.

Table 1 Naphtha Composition

Composition (wt%) Naphtha (IBP-150℃) Naphtha (IBP-180℃) n-alkanes 41 35 isoparaffin twenty four 29 Naphthenic 15 28 Aromatic hydrocarbons 14 7

Example 2

According to the conditions and steps described in Example 1, the catalyst is a microsphere containing naphtha catalytic cracking activity, the weight content of molecular sieve in the catalyst is 30%, and the particle size range is 50-150 microns. The carbon content mass fraction of the regenerated catalyst is less than 0.5%. Conditions of the riser reactor: the reaction temperature was 680°C, the reaction pressure was 0.01 MPa in gauge pressure, and the gas phase linear velocity was 3 m/s; fluidized bed reactor conditions: the reaction temperature was 670°C, and the reaction pressure was gauged as 0.01MPa, the linear velocity of the gas phase is 1m/s, and the mass ratio of naphtha and methanol is 10. The mass ratio of the feed to the riser reactor and the fluidized bed reactor was 9:1. Keep the catalyst circulation stable, and the mass space velocity of the fluidized bed reactor is 0.5h ^-1 . The product gas was analyzed by online chromatography, and the mass yield of olefin was 45%, the mass yield of BTX was 18%, and the mass yield of high-quality gasoline was 13%.

Example 3

According to the conditions and steps described in Example 1, the catalyst is a microsphere containing naphtha catalytic cracking activity, the weight content of molecular sieve in the catalyst is 30%, and the particle size range is 50-150 microns. The carbon content mass fraction of the regenerated catalyst is less than 0.5%. Conditions of the riser reactor: the reaction temperature was 680°C, the reaction pressure was 0.01 MPa in gauge pressure, and the gas phase linear velocity was 3 m/s; fluidized bed reactor conditions: the reaction temperature was 670°C, and the reaction pressure was gauged as 0.01MPa, the linear velocity of the gas phase is 1m/s, and the mass ratio of naphtha and methanol is 0.5. The mass ratio of the feed to the riser reactor and the fluidized bed reactor was 1:9. Keep the catalyst circulation stable, and the mass space velocity of the fluidized bed reactor is 1.5h ^-1 . The product gas was analyzed by online chromatography, and the mass yield of olefin was 72%, the mass yield of BTX was 16%, and the mass yield of high-quality gasoline was 6%.

Example 4

According to the conditions and steps described in Example 1, the catalyst is a microsphere containing naphtha catalytic cracking activity, the weight content of molecular sieve in the catalyst is 30%, and the particle size range is 50-150 microns. The carbon content mass fraction of the regenerated catalyst is less than 0.5%. Conditions of the riser reactor: the reaction temperature was 720°C, the reaction pressure was 0.01 MPa in gauge pressure, and the gas phase linear velocity was 3 m/s; fluidized bed reactor conditions: the reaction temperature was 700°C, and the reaction pressure was gauged as 0.01MPa, the linear velocity of the gas phase is 1m/s, and the mass ratio of naphtha and methanol is 50. The mass ratio of the feed to the riser reactor and the fluidized bed reactor was 1:1. Keep the catalyst circulation stable, and the mass space velocity of the fluidized bed reactor is 1.0h ^-1 . The product gas was analyzed by online chromatography, and the mass yield of olefin was 42%, the mass yield of BTX was 24%, and the mass yield of high-quality gasoline was 21%.

Example 5

According to the conditions and steps described in Example 1, the catalyst is a microsphere containing naphtha catalytic cracking activity, the weight content of molecular sieve in the catalyst is 30%, and the particle size range is 50-150 microns. The carbon content mass fraction of the regenerated catalyst is less than 0.5%. Conditions of the riser reactor: the reaction temperature was 720°C, the reaction pressure was 0.01MPa in gauge pressure, and the gas phase linear velocity was 3m/s; fluidized bed reactor conditions: the reaction temperature was 700°C, and the reaction pressure was gauged as 0.01MPa, the linear velocity of the gas phase is 1m/s, and the mass ratio of naphtha and methanol is 1. The mass ratio of the naphtha feed to the riser reactor and the fluidized bed reactor was 1:1. To keep the catalyst circulation stable, the total mass space velocity of the fluidized bed reactor is 1.0h ^-1 . The product gas was analyzed by online chromatography, and the mass yield of olefin was 61%, the mass yield of BTX was 19%, and the mass yield of high-quality gasoline was 9%.

Example 6

According to the conditions and steps described in Example 1, the catalyst is a microsphere containing naphtha catalytic cracking activity, the weight content of molecular sieve in the catalyst is 10%, and the particle size range is 50-150 microns. The carbon content mass fraction of the regenerated catalyst is less than 0.5%. The height-diameter ratio of the catalyst bed in the reaction section of the fluidized bed reactor was 0.3. Conditions of the riser reactor: the reaction temperature was 680°C, the reaction pressure was 0.01 MPa in gauge pressure, and the gas phase linear velocity was 3 m/s; fluidized bed reactor conditions: the reaction temperature was 670°C, and the reaction pressure was gauged as 0.01MPa, the linear velocity of the gas phase is 1m/s, and the mass ratio of naphtha and methanol is 10. The mass ratio of the feed to the riser reactor and the fluidized bed reactor was 9:1. Keep the catalyst circulation stable, and the mass space velocity of the fluidized bed reactor is 0.5h ^-1 . The product gas was analyzed by online chromatography, and the mass yield of olefin was 42%, the mass yield of BTX was 17%, and the mass yield of high-quality gasoline was 15%.

Example 7

According to the conditions and steps described in Example 1, the catalyst is a microsphere containing naphtha catalytic cracking activity, the weight content of molecular sieve in the catalyst is 50%, and the particle size range is 50-150 microns. The carbon content mass fraction of the regenerated catalyst is less than 0.5%. The height-diameter ratio of the catalyst bed in the reaction section of the fluidized bed reactor was 0.3. Conditions of the riser reactor: the reaction temperature was 680°C, the reaction pressure was 0.01 MPa in gauge pressure, and the gas phase linear velocity was 3 m/s; fluidized bed reactor conditions: the reaction temperature was 670°C, and the reaction pressure was gauged as 0.01MPa, the linear velocity of the gas phase is 1m/s, and the mass ratio of naphtha and methanol is 10. The mass ratio of the feed to the riser reactor and the fluidized bed reactor was 9:1. Keep the catalyst circulation stable, and the mass space velocity of the fluidized bed reactor is 0.5h ^-1 . The product gas was analyzed by online chromatography, and the mass yield of olefin was 78%, the mass yield of BTX was 22%, and the mass yield of high-quality gasoline was 11%.

The above are only a few embodiments of the present application, and are not intended to limit the present application in any form. Although the present application is disclosed as above with preferred embodiments, it is not intended to limit the present application. Without departing from the scope of the technical solution of the present application, any changes or modifications made by using the technical content disclosed above are equivalent to equivalent implementation cases and fall within the scope of the technical solution.

Claims (10)

1. A process for converting a naphtha containing feedstock comprising the steps of:

a) after the raw material containing naphtha and the catalyst are in contact reaction in a riser reactor, introducing the raw material into a fluidized bed reactor, and separating the raw material and the catalyst through an expansion section of the fluidized bed reactor to obtain product gas I and the catalyst subjected to pre-deposited carbon; the pre-deposited catalyst descends to the reaction section of the fluidized bed reactor;

b) inputting raw materials containing naphtha and/or methanol from the bottom of the fluidized bed reactor, ascending to a reaction section of the fluidized bed reactor to contact with the carbon deposited catalyst to obtain product gas II and a catalyst to be regenerated; the catalyst to be regenerated is descended into a regenerator to be regenerated, and then a regenerated catalyst is obtained;

c) returning the regenerated catalyst to the riser reactor;

wherein, the product gas I and the product gas II are mixed and output, and are separated to obtain olefin, aromatic hydrocarbon and gasoline.

2. The method of claim 1, wherein the conditions of the riser reactor are: the reaction temperature is 580-720 ℃, the reaction pressure is 0.01-0.3 MPa in terms of gauge pressure, and the gas-phase linear speed is 3-10 m/s;

the fluidized bed reactor conditions: the reaction temperature is 580-720 ℃, the reaction pressure is 0.01-0.3 Pa in terms of gauge pressure, the gas-phase linear speed is 0.5-1.5 m/s, and the total mass space velocity of naphtha and/or methanol is 0.5-2 h^-1。

3. The method according to claim 1, wherein the mass ratio of the feeding amounts of the riser reactor and the fluidized bed reactor is 1: 9-9: 1.

4. The method of claim 1, wherein step a) comprises: contacting and reacting raw materials containing naphtha and a catalyst in a riser to obtain a material flow which comprises the pre-reacted catalyst and a product gas I and flows upwards to a fluidized bed reactor; the method comprises the steps of separating material flows of a catalyst and a product gas I in an expansion section of a fluidized bed reactor, enabling the product gas I to enter a product gas outlet pipeline, and enabling the pre-reacted catalyst to descend to a reaction section of the fluidized bed reactor.

5. The method of claim 1, wherein step b) comprises: inputting raw materials containing naphtha and methanol from the bottom of the fluidized bed reactor, ascending to a reaction section of the fluidized bed reactor to contact with the pre-reacted catalyst to obtain product gas II and a catalyst to be regenerated; the product gas II ascends to the expansion section of the fluidized bed reactor and enters a product gas outlet pipeline; the catalyst to be regenerated descends to a stripping section of the fluidized bed reactor and enters a regenerator for regeneration through a to-be-regenerated inclined pipe and a riser.

6. The method of claim 1, wherein step c) comprises: the regenerated catalyst returns to the riser reactor through the regenerator stripping section and the regeneration inclined tube.

7. The method according to claim 1, wherein the regenerated catalyst has a carbon content of less than 0.5% by mass.

8. The method of claim 1, wherein the catalyst is a microsphere catalyst comprising naphtha catalytic cracking activity; the diameter of the microspherical catalyst is 30-300 mu m.

9. The method of claim 1, wherein the microspheroidal catalyst has a diameter of 50 to 150 μm.

10. The method according to claim 1, wherein the naphtha boiling range is between 20 and 200 ℃.

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