High-density fast fluidized bed reactor and use method therefor

Abstract

A high-density fast fluidized bed reactor and a use method therefor. The high-density fast fluidized bed reactor comprises: a reactor outer housing (1), a reactor inner housing (2), a transport pipe (3), a raw material distributor (4), a first gas-solid separation device (5), a gas collection chamber (6), fluidized steam distributors (7), catalyst distribution pipes (8), a second gas-solid separation device (9), a product gas transport pipe (10), a catalyst input pipe (11) and a catalyst extraction pipe (12). The main functional areas of the reactor are a reaction area (A), a catalyst retention area (B) and a gas-solid separation area (C), the bottom of the reaction area (A) is communicated with the bottom of the catalyst retention area (B), and the circulation intensity of a catalyst flowing from the catalyst retention area (B) to the reaction area (A) is as high as 500-1000 kg / (m2·s), thereby obtaining high bed density in the reaction area (A) under the condition of a high superficial linear velocity.

Description

A high-density fast fluidized bed reactor and its use method Technical Field

[0001] The present application relates to a high-density fast fluidized bed reactor and a method of using the same, and belongs to the field of chemical catalysis. Background Art

[0002] Low-carbon olefins such as ethylene and propylene are important basic organic chemical raw materials and the cornerstone of the modern chemical industry. Traditional production technologies are highly dependent on petroleum resources. Therefore, it is of great strategic significance to use my country's relatively abundant coal resources to replace petroleum resources.

[0003] Olefin production technologies primarily include naphtha cracking to olefins, methanol to olefins, propane dehydrogenation to propylene, and alkane cracking to olefins. Light olefins are highly reactive and prone to polymerization, alkylation, aromatization, and other reactions, generating byproducts that reduce light olefin yields.

[0004] Methanol-to-olefins (MTO) technology targets ethylene and propylene. Methanol is converted over a molecular sieve catalyst into a mixture of ethylene, propylene, butenes, pentenes, and alkanes. In 2010, the Shenhua Baotou Methanol-to-olefins plant, utilizing DMTO technology developed by the Dalian Institute of Chemical Physics, Chinese Academy of Sciences, was completed and commissioned. This marked the world's first industrial application of MTO technology. By 2023, 16 DMTO industrial plants were operational, with a total annual production capacity of approximately 9.3 million tons of light olefins. Using DMTO technology as an example, carbon-based selectivity for ethylene and propylene is approximately 80% by weight, while selectivity for butenes and pentenes is approximately 15% by weight.

[0005] Improving the yield of ethylene and propylene is a major goal of technological advancement in olefin production.

[0006] Summary of the Invention

[0007] Methanol to olefins technology uses SAPO molecular sieve catalysts. The hydrocarbon pool mechanism believes that methanol is converted into ethylene, propylene and other products through aromatic hydrocarbon cycles or olefin cycles in the molecular sieve catalyst. The main reactions include: CH3OH→C2H4+C3H6 (1) C2H4+CH3OH→C3H6 (2) C3H6+CH3OH→C4H8 (3) C4H8+CH3OH→C5H 10 (4)

[0008] Reactions (1) and (2) produce ethylene and propylene, while reactions (2), (3) and (4) show that small molecule olefins are more active and further converted into large molecule olefins, thereby reducing the yields of ethylene and propylene.

[0009] Methanol-to-olefins (MTO) technology utilizes fluidized bed reactors. Improving the capacity of a single reactor and suppressing the conversion of small olefins to larger olefins are key development goals. One effective method for increasing the capacity of a single reactor is to increase the superficial velocity of the fluidized bed reactor to increase the feedstock rate. Furthermore, increasing the superficial velocity and reducing the residence time of the product gas in the reactor can effectively suppress the formation of larger olefins. However, increasing the superficial velocity typically significantly reduces the bed density in the fluidized bed reactor's reaction zone, leading to a significant decrease in catalyst storage and, consequently, a decrease in methanol conversion. This indicates a negative correlation between feedstock rate and bed density in the fluidized bed reaction zone.

[0010] In order to solve the above technical difficulties, the present application discloses a high-density fast fluidized bed reactor, which achieves high bed density under high superficial velocity conditions, improves the raw material conversion rate, and inhibits side reactions such as polymerization, alkylation, and aromatization of small molecule olefins.

[0011] According to a first aspect of the present application, a high-density fast fluidized bed reactor is provided.

[0012] A high-density fast fluidized bed reactor, comprising an outer reactor shell, an inner reactor shell, a conveying pipe, a first gas-solid separation device, and a second gas-solid separation device;

[0013] The reactor inner shell is located at the lower part of the reactor outer shell;

[0014] The delivery pipe is located in the central area of ​​the upper middle part of the high-density fast fluidized bed reactor;

[0015] The area enclosed by the inner shell of the reactor is the reaction zone;

[0016] The bottom end of the delivery pipe is connected to the top end of the reaction zone;

[0017] The annular area enclosed by the reactor outer shell and the reactor inner shell is the catalyst retention area;

[0018] The bottom of the reaction zone is connected to the bottom of the catalyst retention zone;

[0019] The area enclosed by the reactor shell and the delivery pipe is the gas-solid separation area;

[0020] The catalyst retention zone is connected to the gas-solid separation zone and is located below the gas-solid separation zone;

[0021] The first gas-solid separation equipment and the second gas-solid separation equipment are both located in the gas-solid separation zone;

[0022] The upper opening of the delivery pipe is connected to the inlet of the first gas-solid separation device;

[0023] The catalyst outlet of the first gas-solid separation device is located at the lower part of the gas-solid separation zone.

[0024] Optionally, the inlet of the second gas-solid separation device is located in the gas-solid separation zone, and the catalyst outlet of the second gas-solid separation device is located at the lower part of the gas-solid separation zone.

[0025] Optionally, the first gas-solid separation equipment and the second gas-solid separation equipment each independently adopt 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.

[0026] Optionally, the high-density fast fluidized bed reactor includes a reactor gas collecting chamber and a product gas conveying pipe;

[0027] The reactor gas collecting chamber is located at the top of the high-density fast fluidized bed reactor;

[0028] The product gas delivery pipe is connected to the top of the reactor gas collecting chamber;

[0029] The gas outlet of the first gas-solid separation device and the gas outlet of the second gas-solid separation device are both connected to the reactor gas collecting chamber.

[0030] Optionally, the high-density fast fluidized bed reactor includes a catalyst distribution pipe, a fluidizing steam distributor, a raw material distributor, a catalyst extraction pipe, and a catalyst input pipe;

[0031] The catalyst distribution pipe passes through the inner shell of the reactor and connects the catalyst retention zone and the reaction zone;

[0032] The fluidizing steam distributor is located at the bottom of the catalyst retention zone;

[0033] The raw material distributor is located at the bottom of the reaction zone;

[0034] The catalyst extraction pipe passes through the outer shell of the reactor and is located at the lower part of the catalyst retention area;

[0035] The catalyst inlet pipe passes through the outer shell of the reactor and is located at the lower part of the gas-solid separation zone.

[0036] Optionally, the lower surface of the catalyst distribution tube is opened.

[0037] As a preferred embodiment, the high-density fast fluidized bed reactor comprises: a reactor outer shell, a reactor inner shell, a conveying pipe, a raw material distributor, a first gas-solid separation device, a gas collecting chamber, a fluidized steam distributor, a catalyst distribution pipe, a second gas-solid separation device, a product gas conveying pipe, a catalyst input pipe and a catalyst extraction pipe.

[0038] The area enclosed by the inner shell of the reactor is the reaction zone, the annular area enclosed by the outer shell of the reactor and the inner shell of the reactor is the catalyst retention zone, the bottom of the reaction zone is connected to the bottom of the catalyst retention zone, the area enclosed by the outer shell of the reactor and the conveying pipe is the gas-solid separation zone, the catalyst retention zone is connected to the gas-solid separation zone and is located below the gas-solid separation zone.

[0039] The raw material distributor is located at the bottom of the reaction zone, the delivery pipe is located in the central area of ​​the upper part of the high-density fast fluidized bed reactor, the bottom end of the delivery pipe is connected to the top of the reaction zone, and the upper part of the delivery pipe is connected to the inlet of the first gas-solid separation equipment.

[0040] The first gas-solid separation device is located in the gas-solid separation zone, the gas outlet of the first gas-solid separation device is connected to the gas collecting chamber, and the catalyst outlet of the first gas-solid separation device is located at the lower part of the gas-solid separation zone.

[0041] The fluidizing steam distributor is located at the bottom of the catalyst retention zone.

[0042] The catalyst distribution pipe passes through the inner shell of the reactor and is connected with the catalyst retention zone and the reaction zone, and a hole is opened on the lower surface of the catalyst distribution pipe.

[0043] The second gas-solid separation device is located in the gas-solid separation zone, the inlet of the second gas-solid separation device is located in the gas-solid separation zone, the gas outlet of the second gas-solid separation device is connected to the gas collecting chamber, and the catalyst outlet of the second gas-solid separation device is located at the lower part of the gas-solid separation zone.

[0044] The gas collecting chamber is located at the top of the high-density fast fluidized bed reactor, and the product gas conveying pipe is connected to the top of the gas collecting chamber.

[0045] The catalyst inlet pipe passes through the outer shell of the reactor and is located at the lower part of the gas-solid separation zone.

[0046] The catalyst extraction pipe passes through the outer shell of the reactor and is located at the lower part of the catalyst retention zone.

[0047] According to a second aspect of the present application, a method for using the high-density fast fluidized bed reactor described above is provided.

[0048] The method for using the high-density fast fluidized bed reactor described above comprises:

[0049] (S-1) The catalyst enters the gas-solid separation zone through the catalyst inlet pipe and then enters the catalyst retention zone;

[0050] (S-2) The gasified raw material enters the reaction zone from the raw material distributor, contacts the catalyst, and generates product gas. The product gas carries the catalyst through the delivery pipe and enters the first gas-solid separation equipment. After gas-solid separation, the catalyst enters the catalyst retention zone;

[0051] (S-3) Steam enters the catalyst retention zone from the fluidized steam distributor, and the steam carries a small amount of catalyst from the catalyst retention zone to the second gas-solid separation device in the gas-solid separation zone. After gas-solid separation, the catalyst returns to the catalyst retention zone;

[0052] (S-4) the catalyst in the catalyst retention zone enters the reaction zone through the catalyst distribution pipe; the catalyst in the catalyst retention zone enters the bottom of the reaction zone through the bottom of the catalyst retention zone;

[0053] (S-5) The catalyst in the catalyst retention zone is discharged through the catalyst extraction pipe.

[0054] Optionally, the product gas in step (S-2) and the steam in step (S-3) enter the reactor gas collecting chamber and enter the downstream section through the product gas conveying pipe.

[0055] Optionally, the process operating conditions of the reaction zone are: gas superficial velocity of 1.5-7.0 m / s, temperature of 350-700°C, pressure of 50-500 kPa, bed density of 100-500 kg / m 3 , the reaction contact time is 0.5 to 4s.

[0056] Optionally, the process operating conditions of the catalyst retention zone are: gas superficial velocity of 0.02-0.2 m / s, temperature of 350-700 ° C, bed density of 500-900 kg / m 3 .

[0057] Optionally, the catalyst circulation intensity flowing from the catalyst retention zone to the reaction zone is 500-1000 kg / (m 2 ·s).

[0058] Optionally, the product gas is a product gas containing olefins.

[0059] Optionally, the feedstock comprises methanol and / or dimethyl ether.

[0060] When the feedstock comprises methanol and / or dimethyl ether, the catalyst is a SAPO molecular sieve.

[0061] Optionally, the SAPO molecular sieve is selected from SAPO-34 and / or SAPO-18 molecular sieves.

[0062] Optionally, the feedstock comprises C3+ hydrocarbons.

[0063] Specifically, the feedstock is mixed C4 or naphtha.

[0064] When the feedstock comprises C3+ hydrocarbons, the catalyst is a ZSM-5 molecular sieve.

[0065] Among them, C3+ hydrocarbons refer to hydrocarbons with 3 or more carbon atoms in their molecules.

[0066] As a preferred embodiment, the method for using the high-density fast fluidized bed reactor comprises:

[0067] a. The catalyst enters the gas-solid separation zone through the catalyst inlet pipe and then enters the catalyst retention zone;

[0068] b. The gasified raw materials enter the reaction zone from the raw material distributor, come into contact with the catalyst, and generate product gas containing olefins. The product gas carries the catalyst through the delivery pipe and enters the first gas-solid separation equipment. After gas-solid separation, the product gas enters the gas collection chamber and the catalyst enters the catalyst retention area;

[0069] c. Steam enters the catalyst retention zone from the fluidized steam distributor. The steam carries a small amount of catalyst from the catalyst retention zone into the second gas-solid separation device in the gas-solid separation zone. After gas-solid separation, the steam enters the gas collection chamber and the catalyst returns to the catalyst retention zone.

[0070] d. Product gas and steam enter the downstream process section through the product gas transmission pipe;

[0071] f. The catalyst in the catalyst retention zone enters the reaction zone through the catalyst distribution pipe; the catalyst in the catalyst retention zone enters the bottom of the reaction zone through the bottom of the catalyst retention zone;

[0072] g. The catalyst in the catalyst retention area is discharged through the catalyst extraction pipe.

[0073] The beneficial effects of this application include:

[0074] (1) The high-density fast fluidized bed reactor provided in this application mainly comprises a reaction zone, a catalyst retention zone and a gas-solid separation zone. The catalyst circulation intensity flowing from the catalyst retention zone to the reaction zone is as high as 500-1000 kg / (m 2 ·s), thereby increasing the bed density in the reaction zone, achieving high bed density under high superficial velocity conditions, and overcoming the negative correlation between the raw material feed rate and the bed density in the fluidized bed reaction zone.

[0075] (2) The high-density fast fluidized bed reactor provided in the present application adopts a structure in which the first gas-solid separation device is directly connected to the conveying pipe, thereby achieving rapid separation of the product gas and the catalyst, greatly shortening the gas-solid contact time, and suppressing side reactions.

[0076] (3) The high-density fast fluidized bed reactor provided in this application is suitable for molecular sieve catalytic reaction processes with small molecule olefins as target products. BRIEF DESCRIPTION OF THE DRAWINGS

[0077] FIG1 is a schematic diagram of a high-density fast fluidized bed reactor according to one embodiment of the present application.

[0078] The reference numerals in FIG1 are explained as follows: 1- reactor outer shell 2- reactor inner shell 3- conveying pipe 4- raw material distributor 5- first gas-solid separation equipment 6- gas collecting chamber 7- fluidized steam distributor 8- catalyst distribution pipe 9- second gas-solid separation equipment 10- product gas conveying pipe 11- catalyst input pipe 12- catalyst extraction pipe. DETAILED DESCRIPTION

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

[0080] Unless otherwise specified, the raw materials and catalysts in the examples of this application were purchased from commercial sources.

[0081] In a specific embodiment, the schematic diagram of the high-density fast fluidized bed reactor described in the present application is shown in FIG1 , which mainly comprises a reaction zone (A), a catalyst retention zone (B), and a gas-solid separation zone (C), which are described as follows:

[0082] 1. The high-density fast fluidized bed reactor comprises: a reactor outer shell (1), a reactor inner shell (2), a conveying pipe (3), a raw material distributor (4), a first gas-solid separation device (5), a gas collecting chamber (6), a fluidized steam distributor (7), a catalyst distribution pipe (8), a second gas-solid separation device (9), a product gas conveying pipe (10), a catalyst input pipe (11) and a catalyst extraction pipe (12); the area enclosed by the reactor inner shell (2) is a reaction zone (A), the annular area enclosed by the reactor outer shell (1) and the reactor inner shell (2) is a catalyst retention zone (B), the bottom of the reaction zone (A) is connected to the bottom of the catalyst retention zone (B), the area enclosed by the reactor outer shell (1) and the conveying pipe (3) is a gas-solid separation zone (C), the catalyst retention zone (B) is connected to the gas-solid separation zone (C) and is located below the gas-solid separation zone (C);

[0083] 2. The raw material distributor (4) is located at the bottom of the reaction zone (A), the delivery pipe (3) is located in the central area of ​​the middle and upper part of the high-density fast fluidized bed reactor, the bottom end of the delivery pipe (3) is connected to the top of the reaction zone (A), and the upper part of the delivery pipe (3) is connected to the inlet of the first gas-solid separation device (5); the first gas-solid separation device (5) is located in the gas-solid separation zone (C), the gas outlet of the first gas-solid separation device (5) is connected to the gas collecting chamber (6), and the catalyst outlet of the first gas-solid separation device (5) is located at the lower part of the gas-solid separation zone (C); the fluidized steam distributor (7) is located at the bottom of the catalyst retention zone (B); the catalyst distribution pipe (8) passes through the reactor inner shell (2) to connect the catalyst retention zone (B) and the reaction zone (A) ), the lower surface of the catalyst distribution pipe (8) is opened; the second gas-solid separation device (9) is located in the gas-solid separation zone (C), the inlet of the second gas-solid separation device (9) is located in the gas-solid separation zone (C), the gas outlet of the second gas-solid separation device (9) is connected to the gas collecting chamber (6), and the catalyst outlet of the second gas-solid separation device (9) is located in the lower part of the gas-solid separation zone (C); the gas collecting chamber (6) is located at the top of the high-density fast fluidized bed reactor, the product gas conveying pipe (10) is connected to the top of the gas collecting chamber (6), the catalyst input pipe (11) passes through the reactor outer shell (1) and is located in the lower part of the gas-solid separation zone (C); the catalyst extraction pipe (12) passes through the reactor outer shell (1) and is located in the lower part of the catalyst retention zone (B).

[0084] Specifically, the first gas-solid separation equipment (5) adopts multiple 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.

[0085] Specifically, the second gas-solid separation equipment (9) adopts multiple 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.

[0086] In a specific embodiment, a method for using a high-density fast fluidized bed reactor described in the present application comprises the following steps:

[0087] a. The catalyst enters the gas-solid separation zone (C) through the catalyst inlet pipe (11) and then enters the catalyst retention zone (B);

[0088] b. The gasified raw materials enter the reaction zone (A) from the raw material distributor (4), come into contact with the catalyst, and generate product gas containing olefins. The product gas carries the catalyst through the delivery pipe (3) and enters the first gas-solid separation device (5). After gas-solid separation, the product gas enters the gas collection chamber (6), and the catalyst enters the catalyst retention zone (B);

[0089] c. Steam enters the catalyst retention zone (B) from the fluidized steam distributor (7), and the steam carries a small amount of catalyst from the catalyst retention zone (B) into the second gas-solid separation device (9) in the gas-solid separation zone (C). After gas-solid separation, the steam enters the gas collecting chamber (6), and the catalyst returns to the catalyst retention zone (B);

[0090] d. The product gas and steam enter the downstream section via the product gas delivery pipe (10);

[0091] e. The catalyst in the catalyst retention zone (B) enters the reaction zone (A) through the catalyst distribution pipe (8); the catalyst in the catalyst retention zone (B) enters the bottom of the reaction zone (A) through the bottom of the catalyst retention zone (B);

[0092] f. The catalyst in the catalyst retention zone (B) is discharged through the catalyst extraction pipe (12).

[0093] The method described in this application, the calculation method of raw material single-pass conversion rate and product selectivity is as follows:

[0094] Raw material single-pass conversion rate = (1-mass flow rate of raw material in product gas / mass flow rate of raw material feed) × 100%

[0095] Selectivity of "target product" = mass flow rate of "target product" in product gas / (mass flow rate of product gas - mass flow rate of raw materials in product gas - mass flow rate of water in product gas) × 100%

[0096] Example 1

[0097] This embodiment adopts the device shown in Figure 1.

[0098] In this embodiment, the raw material is methanol. The catalyst is a SAPO-34 molecular sieve catalyst. The process operating conditions of the reaction zone (A) are: gas superficial linear velocity of 7.0 m / s, temperature of 450°C, pressure of 50 kPa, bed density of 100 kg / m 3 The process operating conditions of the catalyst retention zone (B) are: gas superficial velocity of 0.2 m / s, temperature of 450°C, bed density of 500 kg / m 3 The catalyst circulation intensity flowing from the catalyst retention zone (B) to the reaction zone (A) is 1000 kg / (m 2 ·s).

[0099] In this Example 1, the single-pass conversion rate of methanol is 99.9%, and the composition of the product is 50%wt ethylene, 41%wt propylene and 9%wt other components, and the other components are methane, ethane, propane, butane, butene, C5+ hydrocarbons, hydrogen, CO, CO2 and coke.

[0100] Example 2

[0101] This embodiment adopts the device shown in Figure 1.

[0102] In this embodiment, the raw material is methanol. The catalyst is a SAPO-18 molecular sieve catalyst. The process operating conditions of the reaction zone (A) are: gas superficial linear velocity of 5.0 m / s, temperature of 360°C, pressure of 100 kPa, bed density of 200 kg / m 3 The process operating conditions of the catalyst retention zone (B) are: gas superficial velocity of 0.1 m / s, temperature of 360°C, bed density of 740 kg / m 3 The catalyst circulation intensity flowing from the catalyst retention zone (B) to the reaction zone (A) is 860 kg / (m 2 ·s).

[0103] In this Example 2, the single-pass conversion rate of methanol is 99.6%, and the composition of the product is 38%wt ethylene, 51%wt propylene and 11%wt other components, and the other components are methane, ethane, propane, butane, butene, C5+ hydrocarbons, hydrogen, CO, CO2 and coke.

[0104] Example 3

[0105] This embodiment adopts the device shown in Figure 1.

[0106] In this embodiment, the raw material is dimethyl ether. The catalyst is a SAPO-34 molecular sieve catalyst. The process operating conditions of the reaction zone (A) are: gas superficial linear velocity of 3.0 m / s, temperature of 410°C, pressure of 180 kPa, bed density of 270 kg / m 3 The process operating conditions of the catalyst retention zone (B) are: gas superficial velocity of 0.08 m / s, temperature of 410°C, bed density of 620 kg / m 3 The catalyst circulation intensity flowing from the catalyst retention zone (B) to the reaction zone (A) is 710 kg / (m 2 ·s).

[0107] In this Example 3, the single-pass conversion rate of methanol is 99.8%, and the composition of the product is 44%wt ethylene, 46%wt propylene and 10%wt other components, and the other components are methane, ethane, propane, butane, butene, C5+ hydrocarbons, hydrogen, CO, CO2 and coke.

[0108] Example 4

[0109] This embodiment adopts the device shown in Figure 1.

[0110] In this embodiment, the raw material is a mixed C4, which contains 34%wt butane, 63%wt butene, 1%wt pentane, and 2%wt pentene. The catalyst is a ZSM-5 molecular sieve catalyst. The process operating conditions of the reaction zone (A) are: gas superficial linear velocity of 2.0 m / s, temperature of 690°C, pressure of 500 kPa, bed density of 390 kg / m 3 The process operating conditions of the catalyst retention zone (B) are: gas superficial velocity of 0.05 m / s, temperature of 690°C, bed density of 830 kg / m 3 The catalyst circulation intensity flowing from the catalyst retention zone (B) to the reaction zone (A) is 660 kg / (m 2 ·s).

[0111] In this Example 4, the single-pass conversion rate of mixed C4 is 77%, and the composition of the product is 17%wt ethylene, 65%wt propylene and 18%wt other components, and the other components are methane, ethane, propane, butane, butene, C5+ hydrocarbons, hydrogen, CO, CO2 and coke.

[0112] Example 5

[0113] This embodiment adopts the device shown in Figure 1.

[0114] In this embodiment, the raw material is naphtha. The catalyst is a ZSM-5 molecular sieve catalyst. The process operating conditions of the reaction zone (A) are: gas superficial velocity of 1.5 m / s, temperature of 650°C, pressure of 300 kPa, bed density of 500 kg / m 3 The process operating conditions of the catalyst retention zone (B) are: gas superficial velocity of 0.02 m / s, temperature of 650°C, bed density of 900 kg / m 3 The catalyst circulation intensity flowing from the catalyst retention zone (B) to the reaction zone (A) is 500 kg / (m 2 ·s).

[0115] In this Example 5, the single-pass conversion rate of naphtha is 83%, and the composition of the product is 12%wt ethylene, 56%wt propylene, 19%wt butene and 13%wt other components, and the other components are methane, ethane, propane, butane, hydrogen, CO, CO2 and coke.

[0116] The above descriptions are merely a few embodiments of the present application and do not constitute any form of limitation to the present application. Although the present application discloses the preferred embodiments as above, they are not intended to limit the present application. Any technical personnel familiar with the present profession, without departing from the scope of the technical solution of the present application, using the technical content disclosed above to make slight changes or modifications are equivalent to equivalent implementation cases and fall within the scope of the technical solution.

Claims

1. A high-density fast fluidized bed reactor, characterized in that, The high-density fast fluidized bed reactor includes a reactor outer shell, a reactor inner shell, a conveying pipe, a first gas-solid separation device, and a second gas-solid separation device; The reactor inner shell is located at the lower part of the reactor outer shell; The conveying pipe is located in the central area in the upper-middle part of the high-density fast fluidized bed reactor; The area enclosed by the reactor inner shell is the reaction zone; The bottom end of the conveying pipe communicates with the top end of the reaction zone; The annular area enclosed by the reactor outer shell and the reactor inner shell is the catalyst residence zone; The bottom of the reaction zone communicates with the bottom of the catalyst residence zone; The area enclosed by the reactor outer shell and the conveying pipe is the gas-solid separation zone; The catalyst residence zone communicates with the gas-solid separation zone and is located below the gas-solid separation zone; Both the first gas-solid separation device and the second gas-solid separation device are located in the gas-solid separation zone; The upper opening of the conveying pipe is connected to the inlet of the first gas-solid separation device; The catalyst outlet of the first gas-solid separation device is located at the lower part of the gas-solid separation zone.

2. The high-density fast fluidized bed reactor according to claim 1, wherein The inlet of the second gas-solid separation device is located in the gas-solid separation zone, and the catalyst outlet of the second gas-solid separation device is located at the lower part of the gas-solid separation zone.

3. The high-density fast fluidized bed reactor according to any one of claims 1-2, characterized in that, The first gas-solid separation device and the second gas-solid separation device each independently adopt 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.

4. The high-density fast fluidized bed reactor according to any one of claims 1 to 3, characterized in that, The high-density fast fluidized bed reactor includes a reactor gas collection chamber and a product gas conveying pipe; The reactor gas collection chamber is located at the top of the high-density fast fluidized bed reactor; The product gas conveying pipe is connected to the top of the reactor gas collection chamber; The gas outlets of the first gas-solid separation device and the second gas-solid separation device are both connected to the reactor gas collection chamber.

5. The high-density fast fluidized bed reactor according to any one of claims 1-4, characterized in that The high-density fast fluidized bed reactor includes a catalyst distribution pipe, a fluidizing steam distributor, a raw material distributor, a catalyst extraction pipe, and a catalyst input pipe; The catalyst distribution pipe passes through the reactor inner shell to communicate the catalyst residence zone and the reaction zone; The fluidizing steam distributor is located at the bottom of the catalyst residence zone; The raw material distributor is located at the bottom of the reaction zone; The catalyst extraction pipe passes through the reactor outer shell and is located at the lower part of the catalyst residence zone; The catalyst input pipe passes through the reactor outer shell and is located at the lower part of the gas-solid separation zone.

6. The high-density fast fluidized bed reactor according to any one of claims 1-5, characterized in that The lower surface of the catalyst distribution pipe is perforated.

7. A method for using the high-density fast fluidized bed reactor according to any one of claims 1-6, characterized in that, The method includes: (S-1) The catalyst enters the gas-solid separation zone through the catalyst input pipe and then enters the catalyst residence zone; (S-2) The gasified raw material enters the reaction zone from the raw material distributor, contacts with the catalyst to generate product gas, and the product gas carries the catalyst through the conveying pipe into the first gas-solid separation device. After gas-solid separation, the catalyst enters the catalyst residence zone; (S-3) Steam enters the catalyst residence zone from the fluidizing steam distributor, and the steam carries a small amount of catalyst from the catalyst residence zone into the second gas-solid separation device in the gas-solid separation zone. After gas-solid separation, the catalyst returns to the catalyst residence zone; (S-4) The catalyst in the catalyst residence zone enters the reaction zone through the catalyst distribution pipe; the catalyst in the catalyst residence zone enters the bottom of the reaction zone through the bottom of the catalyst residence zone. (S-5) The catalyst in the catalyst residence zone is discharged through the catalyst extraction pipe.

8. The method according to claim 7, wherein The product gas in step (S-2) and the steam in step (S-3) enter the reactor gas collection chamber and enter the downstream section through the product gas transfer pipe.

9. The method according to any one of claims 7-8, characterized in that, The process operating conditions of the reaction zone are as follows: the apparent gas linear velocity is 1.5 - 7.0 m / s, the temperature is 350 - 700 °C, the pressure is 50 - 500 kPa, and the bed density is 100 - 500 kg / m 3 , and the reaction contact time is 0.5 - 4 s.

10. The method according to any one of claims 7-9, characterized in that, The process operating conditions of the catalyst residence zone are as follows: the apparent gas linear velocity is 0.02 - 0.2 m / s, the temperature is 350 - 700 °C, and the bed density is 500 - 900 kg / m 3 .

11. The method according to any one of claims 7 to 10, characterized in that The catalyst circulation intensity flowing from the catalyst residence zone to the reaction zone is 500 - 1000 kg / (m 2 ·s).

12. The method according to any one of claims 7-11, characterized in that, The product gas is a product gas containing olefins.

13. The method according to any one of claims 7-12, characterized in that, The raw material includes methanol and / or dimethyl ether.

14. The method according to any one of claims 7-13, characterized in that The catalyst is SAPO molecular sieve.

15. The method according to any one of claims 7 to 14, characterized in that The raw material includes C3+ hydrocarbons.

16. The method according to any one of claims 7-15, characterized in that, The catalyst is ZSM-5 molecular sieve.

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