Method for preparing low-carbon olefins by coupling methanol with mixed hydrocarbons

Abstract

Disclosed is a method for preparing low-carbon olefins by coupling methanol with mixed hydrocarbons. The method comprises: introducing gasified methanol and mixed hydrocarbon raw materials into a reaction zone for contact with a catalyst for a reaction to generate stream I containing a product gas and the catalyst; subjecting stream I to gas-solid separation, then the catalyst entering a catalyst residence zone, and the product gas entering a downstream section; and part of the catalyst in the catalyst residence zone entering the reaction region, conveying part of the catalyst to a fluidized bed regenerator for regeneration, and the regenerated catalyst entering a fluidized bed reactor. By means of a fluidized bed reaction-regeneration process, the method achieves continuous preparation of low-carbon olefins by coupling methanol with mixed hydrocarbons. The reaction of preparing the low-carbon olefins from methanol is exothermic, thus providing heat for the catalytic cracking of the mixed hydrocarbons to prepare the low-carbon olefins, achieving self-heat balance. The reaction contact time of the product gas in the reactor is less than 2 s, the carbon-based selectivity for "ethylene + propylene" is greater than or equal to 75% wt, the single-pass conversion rate of methanol is greater than or equal to 99% wt, and the single-pass conversion rate of the mixed hydrocarbons is greater than or equal to 50% wt.

Description

A method for producing light olefins by coupling methanol and mixed hydrocarbons Technical Field

[0001] The present application relates to the field of chemical catalysis technology, and in particular to a method for producing light olefins by coupling methanol and mixed hydrocarbons. Background Art

[0002] Olefins are important basic organic chemical raw materials and the cornerstone of the modern chemical industry. Olefin production technologies primarily include naphtha cracking, methanol to olefins, propane dehydrogenation to propylene, alkane cracking to olefins, and olefin cracking to olefins. Light olefins are highly reactive and prone to reactions such as polymerization, alkylation, and aromatization, generating byproducts that reduce light olefin yields.

[0003] 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. The MTO reaction is highly exothermic, typically requiring a heat extractor to remove the heat released by the reaction and charring.

[0004] UOP has developed olefin catalytic cracking (OCP) technology, which converts C4-C8 olefin feedstocks into ethylene and propylene at high temperature and low pressure, with a propylene-to-ethylene ratio of approximately 4:1. The OCP unit consists of two radial flow reactors, one operating online and the other in standby after regeneration. The reactor regeneration cycle is 48 hours. Switching between online and offline regeneration is accomplished using valves located at the reactor inlet and outlet.

[0005] Sinopec has developed olefin catalytic cracking (OCC) technology, which cracks olefins contained in mixed C4-C6 feedstocks into propylene, ethylene, and other products over a molecular sieve catalyst. The OCC unit consists of two fixed-bed reactors, one in operation and one in standby. The reaction system operates using a continuous switching mechanism, and the catalyst regeneration process is controlled by an automatic switching regeneration program.

[0006] Catalytic cracking to produce light olefins is a highly endothermic process. Radial flow reactors and fixed-bed reactors typically use elevated feed temperatures to provide heat. However, excessively high preheat temperatures for feedstock components such as olefins, diolefins, and alkynes can lead to coking, hindering continuous operation. Furthermore, the catalyst gradually loses activity during the reaction, necessitating switching reactors to achieve continuous operation. These heating and deactivation challenges have limited the development and advancement of radial flow and fixed-bed reactor technologies.

[0007] Summary of the Invention

[0008] In view of this, the present application provides a method for producing light olefins by coupling methanol and mixed hydrocarbons, the main purpose of which is to solve the technical problems of low light olefin yield, low mixed hydrocarbon conversion rate and mixed hydrocarbon cracking heat supply.

[0009] Light olefins are highly reactive and prone to polymerization, alkylation, aromatization, and other reactions, generating byproducts that reduce light olefin yield. Reaction contact time is a key factor influencing light olefin selectivity in the catalytic cracking of mixed hydrocarbons to produce light olefins. Increasing the superficial linear velocity in the reaction zone of a fluidized bed reactor can reduce reaction contact time and improve light olefin selectivity. However, this typically results in a significant decrease in bed density and catalyst inventory, leading to a decrease in cracking feedstock conversion. Consequently, there is a negative correlation between light olefin selectivity and feedstock conversion.

[0010] In order to improve the yield of light olefins and the conversion rate of raw materials, the present application provides a high-density fast fluidized bed reactor, which includes a reactor outer shell, a reactor inner shell and a conveying pipe;

[0011] The reactor outer shell is provided with at least a raw material inlet, a catalyst inlet, a gas phase product outlet and a catalyst outlet;

[0012] The reactor outer shell encloses an inner area;

[0013] The inner shell of the reactor is located at the lower part of the internal area, and the area enclosed by the inner shell of the reactor is the reaction zone;

[0014] The delivery pipe is located in the upper middle portion of the inner region, and the bottom of the delivery pipe is connected to the reaction zone;

[0015] The area enclosed by the reactor shell and the delivery pipe is a gas-solid separation area;

[0016] The delivery pipe is provided with an outlet, and the delivery pipe is connected to the gas-solid separation 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 catalyst retention zone is communicated with the gas-solid separation zone and is located below the gas-solid separation zone.

[0020] Optionally, the high-density fast fluidized bed reactor includes a catalyst distribution pipe, a fluidizing steam distributor, and a raw material distributor;

[0021] The catalyst distribution pipe passes through the inner shell of the reactor and connects the catalyst retention zone and the reaction zone;

[0022] The fluidizing steam distributor is arranged at the bottom of the catalyst retention zone;

[0023] The raw material distributor is arranged at the bottom of the reaction zone.

[0024] Optionally, a through hole is opened on the lower surface of the catalyst distribution tube.

[0025] Optionally, the high-density fast fluidized bed reactor includes a first gas-solid separation device and a second gas-solid separation device;

[0026] The first gas-solid separation equipment and the second gas-solid separation equipment are located in the gas-solid separation zone;

[0027] The inlet of the first gas-solid separation device is connected to the outlet of the conveying pipe;

[0028] The catalyst outlet of the first gas-solid separation device is located at the lower part of the gas-solid separation zone, and the gas outlet of the first gas-solid separation device is located at the upper part of the gas-solid separation zone;

[0029] Preferably, the inlet of the second gas-solid separation device is located at the upper part of the gas-solid separation zone;

[0030] The catalyst outlet of the second gas-solid separation device is located at the lower part of the gas-solid separation zone;

[0031] Optionally, the first gas-solid separation equipment is an inertial separator.

[0032] Optionally, the second gas-solid separation equipment 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.

[0033] Optionally, the high-density fast fluidized bed reactor includes a reactor gas collecting chamber and a product gas conveying pipe;

[0034] The reactor gas collecting chamber is located at the top of the high-density fast fluidized bed reactor;

[0035] The product gas delivery pipe is connected to the top of the reactor gas collecting chamber;

[0036] The gas outlet of the second gas-solid separation device is communicated with the reactor gas collecting chamber.

[0037] In a second aspect, the present application provides a device for producing light olefins from methanol and mixed hydrocarbons, the device comprising the above-mentioned high-density fast fluidized bed reactor and fluidized bed regenerator;

[0038] A catalyst extraction pipe passes through the outer shell of the reactor and is located at the lower part of the catalyst retention zone, and the catalyst extraction pipe is connected to the reactor stripper;

[0039] The inlet of the spent catalyst slide valve is connected to the bottom of the reactor stripper, the outlet of the spent catalyst slide valve is connected to the inlet of the spent catalyst delivery pipe, and the outlet of the spent catalyst delivery pipe is connected to the fluidized bed regenerator;

[0040] The regenerator stripper is located at the bottom of the fluidized bed regenerator; the inlet of the regeneration slide valve is connected to the bottom of the regenerator stripper, the outlet of the regeneration slide valve is connected to the inlet of the regeneration agent delivery pipe, and the outlet of the regeneration agent delivery pipe is connected to the lower part of the gas-solid separation zone of the high-density fast fluidized bed reactor.

[0041] Optionally, the fluidized bed regenerator includes a regenerator shell, a regenerator distributor, a third gas-solid separation device, a regenerator gas collecting chamber, and a flue gas conveying pipe;

[0042] The regenerator distributor is located at the bottom of the fluidized bed regenerator;

[0043] The third gas-solid separation equipment is located at the upper part of the fluidized bed regenerator, the inlet of the third gas-solid separation equipment is located at the upper part of the fluidized bed regenerator, the gas outlet of the third gas-solid separation equipment is connected to the regenerator gas collecting chamber, the catalyst outlet of the third gas-solid separation equipment is located at the lower part of the fluidized bed regenerator, the regenerator gas collecting chamber is located at the top of the fluidized bed regenerator, and the flue gas conveying pipe is connected to the top of the regenerator gas collecting chamber.

[0044] Optionally, the inlet pipe of the regenerator stripper penetrates the regenerator shell and opens above the regenerator distributor.

[0045] Optionally, the third gas-solid separation equipment adopts 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.

[0046] In a third aspect, the present application provides a method for producing light olefins by coupling methanol and mixed hydrocarbons, which is carried out using the above-mentioned device.

[0047] Optionally, the method for preparing light olefins comprises the following steps:

[0048] The vaporized raw materials including methanol and mixed hydrocarbons are introduced into the reaction zone, contacted with the catalyst, and reacted to generate a product gas containing light olefins and a stream I of the catalyst;

[0049] The stream I is subjected to gas-solid separation to obtain a product gas and a catalyst;

[0050] The product gas is transported to the downstream section;

[0051] A portion of the catalyst enters the reaction zone, and another portion of the catalyst is regenerated, and the regenerated catalyst enters the reaction zone.

[0052] Optionally, the logistics I enters the first gas-solid separation equipment through a conveying pipe, and the catalyst after the first gas-solid separation enters the catalyst retention area.

[0053] Optionally, the mixed hydrocarbons in the feedstock are C4+ hydrocarbons, including alkanes and alkenes with carbon atoms ≥4.

[0054] Optionally, the catalyst is selected from ZSM-5 molecular sieve catalyst.

[0055] Optionally, the process operating conditions of the reaction zone of the high-density fast fluidized bed reactor include:

[0056] The gas superficial velocity is 1.5-7.0 m / s, the temperature is 500-680°C, the pressure is 50-250 kPa, and the bed density is 150-500 kg / m 3 , the reaction contact time is 0.5 to 2s.

[0057] Optionally, the superficial linear velocity of the gas in the reaction zone is selected from any value among 1.5m / s, 2m / s, 2.5m / s, 3m / s, 3.5m / s, 4m / s, 4.5m / s, 5m / s, 5.5m / s, 6m / s, 6.5m / s, 7m / s or any range between two of them.

[0058] Optionally, the temperature of the reaction zone is selected from any value among 500°C, 550°C, 600°C, 650°C, 680°C or any range therebetween.

[0059] Optionally, the pressure of the reaction zone is selected from any value among 50 kPa, 100 kPa, 150 kPa, 200 kPa, 250 kPa, or any range between the two values.

[0060] Optionally, the bed density in the reaction zone is selected from 150 kg / m 3 , 200kg / m 3 , 250kg / m 3 300kg / m 3 、350kg / m 3 , 400kg / m 3 450kg / m 3 , 500kg / m 3 Any value in between or any range of values ​​between them.

[0061] Optionally, the reaction contact time of the reaction zone is selected from any value among 0.5s, 1s, 1.5s, 2s or any range value therebetween.

[0062] Optionally, the process operating conditions of the catalyst residence zone include:

[0063] The gas superficial velocity is 0.02-0.2 m / s, the temperature is 500-680°C, and the bed density is 600-800 kg / m 3 .

[0064] Optionally, the catalyst circulation intensity from the catalyst retention zone to the reaction zone is 500 to 1000 kg / m 2 ·s.

[0065] Optionally, the superficial linear velocity of the gas in the catalyst residence zone is selected from any value among 0.02 m / s, 0.05 m / s, 0.08 m / s, 0.1 m / s, 0.12 m / s, 0.15 m / s, 0.18 m / s, 0.20 m / s or any range between two values.

[0066] Optionally, the temperature of the catalyst residence zone is selected from any value among 500°C, 550°C, 600°C, 650°C, 680°C or any range between them.

[0067] Optionally, the bed density of the catalyst retention zone is 600 kg / m 3 、650kg / m 3 , 700kg / m 3 , 750kg / m 3 , 800kg / m 3 Any value in between or any range of values ​​between them.

[0068] Optionally, the catalyst circulation intensity is selected from any value among 500, 550, 600, 650, 700, 750, 800, 850, 900, 950, 1000 or any range between two values, and the unit is kg / (m 2 ·s).

[0069] Optionally, the process operating conditions of the fluidized bed regenerator are: gas superficial velocity of 0.5-2.0 m / s, regeneration temperature of 600-750°C, regeneration pressure of 50-250 kPa, bed density of 200-800 kg / m 3 .

[0070] Optionally, the superficial linear velocity of the gas in the fluidized bed regenerator is selected from any value among 0.5 m / s, 1 m / s, 1.5 m / s, 2 m / s, or any range between the two values.

[0071] Optionally, the regeneration temperature of the fluidized bed regenerator is selected from any value among 600, 650, 700, 750 or any range between them.

[0072] Optionally, the regeneration pressure of the fluidized bed regenerator is any value among 50 kPa, 100 kPa, 150 kPa, 200 kPa, 250 kPa, or a range between any two values.

[0073] Optionally, the bed density of the fluidized bed regenerator is 200 kg / m 3 , 250kg / m 3 300kg / m 3 、350kg / m 3 , 400kg / m 3 450kg / m 3 , 500kg / m 3 , 550kg / m 3 、600kg / m 3 、650kg / m 3 , 700kg / m 3 , 750kg / m 3 , 800kg / m 3 Any value in between or any range of values ​​between them.

[0074] Optionally, the regeneration gas is air.

[0075] Optionally, steam enters the catalyst retention zone from the fluidized steam distributor, and the steam carries a portion of the catalyst in the catalyst retention zone into the gas-solid separation zone; the product gas in the gas-solid separation zone and a portion of the catalyst carried by the steam enter the second gas-solid separation equipment, and the gas after the second gas-solid separation enters the reactor gas collection chamber, and the separated catalyst returns to the catalyst retention zone.

[0076] Optionally, the product gas and steam after the second gas-solid separation enter the downstream section through the product gas conveying pipe; the first part of the catalyst in the catalyst retention area enters the reaction zone through the catalyst distribution pipe; the second part of the catalyst in the catalyst retention area enters the bottom of the reaction zone through the bottom of the catalyst retention area; the third part of the catalyst in the catalyst retention area enters the reactor stripper through the catalyst extraction pipe.

[0077] The present application provides a specific methanol and mixed hydrocarbon production light olefins device, comprising: a reactor outer shell, a reactor inner shell, a delivery pipe, a raw material distributor, a first gas-solid separation device, a fluidized steam distributor, a catalyst distribution pipe, a second gas-solid separation device, a reactor gas collecting chamber, a product gas delivery pipe, a catalyst extraction pipe, a reactor stripper, a slide valve to be regenerated, and a delivery pipe for the catalyst to be regenerated;

[0078] The area enclosed by the reactor inner shell is the reaction zone, the annular area enclosed by the reactor outer shell and the reactor inner shell 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 reactor outer shell and the delivery 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;

[0079] 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 outlet of the delivery pipe is connected to the inlet of the first gas-solid separation device; the first gas-solid separation device is located in the gas-solid separation zone, the catalyst outlet of the first gas-solid separation device is located at the lower part of the gas-solid separation zone, and the gas outlet of the first gas-solid separation device is located at the upper part of the gas-solid separation zone;

[0080] The fluidized steam distributor is located at the bottom of the catalyst retention zone; the catalyst distribution pipe passes through the inner shell of the reactor to connect the catalyst retention zone and the reaction zone, and the lower surface of the catalyst distribution pipe has holes;

[0081] 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 reactor gas collecting chamber, and the catalyst outlet of the second gas-solid separation device is located at the bottom of the gas-solid separation zone; the reactor 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 reactor gas collecting chamber;

[0082] The catalyst extraction pipe passes through the reactor shell and is located at the lower part of the catalyst retention zone; the reactor stripper is connected to the catalyst extraction pipe, the inlet of the spent catalyst slide valve is connected to the bottom of the reactor stripper, the outlet of the spent catalyst slide valve is connected to the inlet of the spent catalyst delivery pipe, and the outlet of the spent catalyst delivery pipe is connected to the fluidized bed regenerator;

[0083] The first gas-solid separation equipment adopts an inertial separator to achieve rapid separation of product gas and catalyst; the second gas-solid separation equipment adopts one or more groups of gas-solid cyclone separators, each group of gas-solid cyclone separators includes a first-stage gas-solid cyclone separator and a second-stage gas-solid cyclone separator;

[0084] The fluidized bed regenerator for regenerating the catalyst comprises: a regenerator shell, a regenerator distributor, a third gas-solid separation device, a regenerator gas collecting chamber, a flue gas conveying pipe, a regenerator stripper, a regeneration slide valve and a regeneration agent conveying pipe;

[0085] The regenerator distributor is located at the bottom of the fluidized bed regenerator; the third gas-solid separation device is located at the upper part of the fluidized bed regenerator, the inlet of the third gas-solid separation device is located at the upper part of the fluidized bed regenerator, the gas outlet of the third gas-solid separation device is connected to the regenerator gas collecting chamber, the catalyst outlet of the third gas-solid separation device is located at the lower part of the fluidized bed regenerator, the regenerator gas collecting chamber is located at the top of the fluidized bed regenerator, and the flue gas conveying pipe is connected to the top of the regenerator gas collecting chamber;

[0086] The regenerator stripper is located outside the regenerator shell, the inlet pipe of the regenerator stripper penetrates the regenerator shell and opens above the regenerator distributor, the inlet of the regeneration slide valve is connected to the bottom of the regenerator stripper, the outlet of the regeneration slide valve is connected to the inlet of the regeneration agent delivery pipe, and the outlet of the regeneration agent delivery pipe is connected to the lower part of the gas-solid separation zone of the high-density fast fluidized bed reactor;

[0087] The third gas-solid separation equipment adopts 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 present application provides a specific method for producing light olefins by coupling methanol and mixed hydrocarbons, comprising:

[0089] a. The catalyst from the regeneration agent delivery pipe enters the gas-solid separation zone of the high-density fast fluidized bed reactor and then enters the catalyst retention zone;

[0090] The gasified raw materials enter the reaction zone from the raw material distributor, contact with the catalyst, and generate product gas containing light olefins. The product gas carries the catalyst through the conveying pipe and enters the first gas-solid separation equipment. After gas-solid separation, the catalyst enters the catalyst retention area; steam enters the catalyst retention area from the fluidized steam distributor, and the steam carries a small amount of catalyst from the catalyst retention area into the gas-solid separation area; the product gas and steam in the gas-solid separation area carry the catalyst and enter the second gas-solid separation equipment. After gas-solid separation, the gas enters the reactor gas collection chamber, and the catalyst returns to the catalyst retention area; the product gas and steam enter the downstream section through the product gas conveying pipe; the catalyst in the catalyst retention area enters the reaction zone through the catalyst distribution pipe; the catalyst in the catalyst retention area enters the bottom of the reaction zone through the bottom of the catalyst retention area; the catalyst in the catalyst retention area enters the reactor stripper through the catalyst extraction pipe. After stripping, the catalyst enters the middle part of the fluidized bed regenerator through the regenerated slide valve and the regenerated agent conveying pipe;

[0091] b. The regeneration gas enters the bottom of the fluidized bed regenerator from the regenerator distributor. In the fluidized bed regenerator, the regeneration gas contacts the catalyst, and the carbon deposits in the catalyst are burned and eliminated. The flue gas generated by the combustion carries the catalyst into the third gas-solid separation device. After gas-solid separation, the flue gas enters the regenerator gas collection chamber and then enters the downstream flue gas treatment system through the flue gas conveying pipe. The catalyst returns to the bottom of the fluidized bed regenerator. The catalyst in the fluidized bed regenerator enters the regenerator stripper. After stripping, it enters the high-density fast fluidized bed reactor through the regeneration slide valve and the regeneration agent conveying pipe.

[0092] The raw materials are methanol and mixed hydrocarbons, preferably, the mixed hydrocarbons are C4+ hydrocarbons, including alkanes and olefins with carbon atoms ≥ 4; the catalyst is a ZSM-5 molecular sieve catalyst;

[0093] The process operating conditions of the reaction zone of the high-density fast fluidized bed reactor are: gas superficial linear velocity of 1.5-7.0 m / s, temperature of 500-680°C, pressure of 50-250 kPa, bed density of 150-500 kg / m 3 , the reaction contact time is 0.5-2s;

[0094] The process operating conditions of the catalyst retention zone are: gas superficial velocity of 0.02-0.2m / s, temperature of 500-680℃, bed density of 600-800kg / m 3 The catalyst circulation intensity of the catalyst retention zone to the reaction zone is 500-1000kg / (m 2 ·s); the regeneration gas is air;

[0095] The process operating conditions of the fluidized bed regenerator are: gas superficial velocity of 0.5-2.0 m / s, regeneration temperature of 600-750 ° C, regeneration pressure of 50-250 kPa, bed density of 200-800 kg / m 3 .

[0096] The method described in this application has a methanol single-pass conversion rate of ≥99% wt, a mixed hydrocarbon single-pass conversion rate of ≥50% wt, an "ethylene + propylene" carbon-based selectivity of ≥75% wt, and a propylene / ethylene (mass ratio) of ≥3.

[0097] The method described in this application, the calculation method of methanol single-pass conversion rate, mixed hydrocarbon single-pass conversion rate, and "ethylene + propylene" carbon-based selectivity is as follows:

[0098] Methanol single-pass conversion rate = (1-mass flow rate of methanol in product gas / mass flow rate of methanol feed) × 100%

[0099] Mixed hydrocarbon single-pass conversion rate = (1-mass flow rate of C4+ hydrocarbons in product gas / mass flow rate of C4+ hydrocarbon feed) × 100%;

[0100] "Ethylene + propylene" carbon-based selectivity = mass flow rate of "ethylene + propylene" in product gas / (mass flow rate of product gas - mass flow rate of water in product gas - mass flow rate of methanol in product gas - mass flow rate of C4 + hydrocarbons in product gas) × 100%

[0101] Compared with the prior art, this application has the following beneficial effects:

[0102] (1) This application discloses a high-density fast fluidized bed reactor, which 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 light olefin selectivity and feed conversion rate.

[0103] (2) According to the method described in the present application, the reaction contact time of the product gas in the high-density fast fluidized bed reactor is less than 2s, which effectively improves the carbon-based selectivity of "ethylene + propylene".

[0104] (3) In the method described in the present application, the methanol to light olefins reaction releases heat, which provides heat for the catalytic cracking of C4+ hydrocarbons to light olefins reaction, thus achieving self-heating balance.

[0105] (4) The method described in this application realizes a continuous process of producing light olefins by coupling methanol and mixed hydrocarbons through a fluidized bed reaction-regeneration process. BRIEF DESCRIPTION OF THE DRAWINGS

[0106] FIG1 is a schematic diagram of an apparatus according to an embodiment of the present application.

[0107] The reference numerals in Figure 1 are explained as follows: 1-high-density fast fluidized bed reactor; 1-1 reactor outer shell, 1-2 reactor inner shell, 1-3 conveying pipe, 1-4 raw material distributor, 1-5 first gas-solid separation equipment, 1-6 fluidized steam distributor, 1-7 catalyst distribution pipe, 1-8 reactor heat extractor, 1-9 reactor gas collecting chamber; 1-10 product gas conveying pipe; 1-11 catalyst extraction pipe; 1-12 reactor stripper; 1-13 slide valve to be regenerated; 1-14 regenerated agent conveying pipe; 2-fluidized bed regenerator; 2-1 regenerator shell, 2-2 regenerator distributor, 2-3 third gas-solid separation equipment, 2-4 regenerator gas collecting chamber, 2-5 flue gas conveying pipe, 2-6 regenerator stripper, 2-7 regeneration slide valve, 2-8 regeneration agent conveying pipe. DETAILED DESCRIPTION

[0108] The present application is described in detail below with reference to embodiments, but the present application is not limited to these embodiments.

[0109] Unless otherwise specified, the raw materials and catalysts in the examples of this application were purchased from commercial sources.

[0110] In a specific embodiment, the present application provides an apparatus of an embodiment, a schematic structural diagram of which is shown in FIG1 , and the apparatus comprises a high-density fast fluidized bed reactor (1) and a fluidized bed regenerator (2).

[0111] a. The high-density fast fluidized bed reactor (1) comprises: a reactor outer shell (1-1), a reactor inner shell (1-2), a conveying pipe (1-3), a raw material distributor (1-4), a first gas-solid separation device (1-5), a fluidized steam distributor (1-6), a catalyst distribution pipe (1-7), a second gas-solid separation device (1-8), a reactor gas collecting chamber (1-9), a product gas conveying pipe (1-10), a catalyst extraction pipe (1-11), a reactor stripper (1-12), a slide valve to be regenerated (1-13) and a conveying pipe for a catalyst to be regenerated (1-14); the area enclosed by the reactor inner shell (1-2) is a reaction zone (A), and the area enclosed by the reactor outer shell (1-1) and the reactor inner shell (1-2) is a reaction zone (A). The annular area is the catalyst retention area (B), the bottom of the reaction area (A) and the bottom of the catalyst retention area (B) are connected, the area enclosed by the reactor shell (1-1) and the conveying pipe (1-3) is the gas-solid separation area (C), the catalyst retention area (B) and the gas-solid separation area (C) are connected and located below the gas-solid separation area (C); the raw material distributor (1-4) is located at the bottom of the reaction area (A), the conveying pipe (1-3) is located in the central area of ​​the middle and upper parts of the high-density fast fluidized bed reactor, the bottom end of the conveying pipe (1-3) is connected to the top of the reaction area (A), and the outlet of the conveying pipe (1-3) is connected to the inlet of the first gas-solid separation device (1-5); the first gas-solid separation device (1-5) is located in the gas-solid separation area (C) The catalyst outlet of the first gas-solid separation device (1-5) is located at the lower part of the gas-solid separation zone (C), and the gas outlet of the first gas-solid separation device (1-5) is located at the upper part of the gas-solid separation zone (C); the fluidized steam distributor (1-6) is located at the bottom of the catalyst retention zone (B); the catalyst distribution pipe (1-7) passes through the inner shell (1-2) of the reactor to connect the catalyst retention zone (B) and the reaction zone (A), and the lower surface of the catalyst distribution pipe (1-7) is opened; the second gas-solid separation device (1-8) is located in the gas-solid separation zone (C), the inlet of the second gas-solid separation device (1-8) is located in the gas-solid separation zone (C), the gas outlet of the second gas-solid separation device (1-8) is connected to the reactor gas collecting chamber (1-9), and the second gas-solid separation device (1-8) is connected to the reactor gas collecting chamber (1-9). The catalyst outlet of the preparation (1-8) is located at the lower part of the gas-solid separation zone (C); the reactor gas collecting chamber (1-9) is located at the top of the high-density fast fluidized bed reactor, and the product gas conveying pipe (1-10) is connected to the top of the reactor gas collecting chamber (1-9); the catalyst extraction pipe (1-11) passes through the reactor outer shell (1-1) and is located at the lower part of the catalyst retention zone (B); the reactor stripper (1-12) is connected to the catalyst extraction pipe (1-11), the inlet of the to-be-generated slide valve (1-13) is connected to the bottom of the reactor stripper (1-12), the outlet of the to-be-generated slide valve (1-13) is connected to the inlet of the to-be-generated catalyst conveying pipe (1-14), and the outlet of the to-be-generated catalyst conveying pipe (1-14) is connected to the fluidized bed regenerator (2).

[0112] b. The fluidized bed regenerator (2) comprises: a regenerator shell (2-1), a regenerator distributor (2-2), a third gas-solid separation device (2-3), a regenerator gas collecting chamber (2-4), a flue gas conveying pipe (2-5), a regenerator stripper (2-6), a regeneration slide valve (2-7) and a regeneration agent conveying pipe (2-8); the regenerator distributor (2-2) is located at the bottom of the fluidized bed regenerator (2); the third gas-solid separation device (2-3) is located at the upper part of the fluidized bed regenerator (2), the inlet of the third gas-solid separation device (2-3) is located at the upper part of the fluidized bed regenerator (2), the gas outlet of the third gas-solid separation device (2-3) is connected to the regenerator gas collecting chamber (2-4), and the catalyst outlet of the third gas-solid separation device (2-3) is connected to the catalyst outlet of the third gas-solid separation device (2-3). The inlet of the regenerator stripper (2-6) is located at the lower part of the fluidized bed regenerator (2), the regenerator gas collecting chamber (2-4) is located at the top of the fluidized bed regenerator (2), and the flue gas conveying pipe (2-5) is connected to the top of the regenerator gas collecting chamber (2-4); the regenerator stripper (2-6) is located outside the regenerator shell (2-1), the inlet pipe of the regenerator stripper (2-6) penetrates the regenerator shell (2-1) and opens above the regenerator distributor (2-2), the inlet of the regeneration slide valve (2-7) is connected to the bottom of the regenerator stripper (2-6), the outlet of the regeneration slide valve (2-7) is connected to the inlet of the regeneration agent conveying pipe (2-8), and the outlet of the regeneration agent conveying pipe (2-8) is connected to the lower part of the gas-solid separation zone (C) of the high-density fast fluidized bed reactor (1).

[0113] In a preferred embodiment, the first gas-solid separation device (1-5) uses an inertial separator to achieve rapid separation of the product gas and the catalyst.

[0114] In a preferred embodiment, the second gas-solid separation equipment (1-8) adopts 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.

[0115] In a preferred embodiment, the third gas-solid separation equipment (2-3) adopts 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.

[0116] In a specific embodiment, a method for producing light olefins by coupling methanol and mixed hydrocarbons of the present application comprises the following steps:

[0117] a. The catalyst from the regeneration agent delivery pipe (2-8) enters the gas-solid separation zone (C) of the high-density fast fluidized bed reactor (1) and then enters the catalyst retention zone (B); the gasified raw material enters the reaction zone (A) from the raw material distributor (1-4), contacts with the catalyst, and generates product gas containing light olefins. The product gas carries the catalyst through the delivery pipe (1-3) and enters the first gas-solid separation device (1-5). After gas-solid separation, the catalyst enters the catalyst retention zone (B); steam enters the catalyst retention zone (B) from the fluidized steam distributor (1-6), and the steam carries a small amount of catalyst from the catalyst retention zone (B) into the gas-solid separation zone (C); the product gas and steam in the gas-solid separation zone (C) carry the catalyst into the first gas-solid separation device (1-5). Second gas-solid separation equipment (1-8), after gas-solid separation, the gas enters the reactor gas collecting chamber (1-9), and the catalyst returns to the catalyst retention zone (B); the product gas and steam enter the downstream section through the product gas conveying pipe (1-10); the catalyst in the catalyst retention zone (B) enters the reaction zone (A) through the catalyst distribution pipe (1-7); 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); the catalyst in the catalyst retention zone (B) enters the reactor stripper (1-12) through the catalyst extraction pipe (1-11), and after stripping, the catalyst enters the middle part of the fluidized bed regenerator (2) through the regeneration slide valve (1-13) and the regeneration agent conveying pipe (1-14);

[0118] b. The regeneration gas enters the bottom of the fluidized bed regenerator (2) from the regenerator distributor (2-2). In the fluidized bed regenerator (2), the regeneration gas contacts the catalyst, and the carbon deposits in the catalyst are burned and eliminated. The flue gas formed by the combustion carries the catalyst into the third gas-solid separation device (2-3). After gas-solid separation, the flue gas enters the regenerator gas collection chamber (2-4) and then enters the downstream flue gas treatment system through the flue gas conveying pipe (2-5). The catalyst returns to the bottom of the fluidized bed regenerator (2). The catalyst in the fluidized bed regenerator (2) enters the regenerator stripper (2-6). After stripping, it enters the high-density fast fluidized bed reactor (1) through the regeneration slide valve (2-7) and the regeneration agent conveying pipe (2-8).

[0119] Example 1

[0120] This embodiment 1 adopts the device shown in Figure 1.

[0121] In Example 1, the raw materials are methanol and C4-C6 hydrocarbons, the methanol feed amount / C4-C6 hydrocarbon feed amount is about 1, the olefin content in the C4-C6 hydrocarbons is 91% by weight, and the alkane content is 9% by weight. The catalyst is a ZSM-5 molecular sieve catalyst.

[0122] The process operating conditions of the reaction zone (A) of the high-density fast fluidized bed reactor (1) are: gas superficial linear velocity of 1.5 m / s, temperature of 500°C, pressure of 250 kPa, bed density of 500 kg / m 3 , the reaction contact time is 2s.

[0123] The process operating conditions of the catalyst retention zone (B) are: gas superficial velocity of 0.10 m / s, temperature of 500 °C, bed density of 670 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).

[0124] The regeneration gas is air. The process operating conditions of the fluidized bed regenerator (2) are: gas superficial linear velocity of 0.5m / s, regeneration temperature of 600℃, regeneration pressure of 250kPa, bed density of 800kg / m 3 .

[0125] The single-pass conversion rate of methanol is 99% wt, the single-pass conversion rate of mixed hydrocarbons is 79% wt, the "ethylene + propylene" carbon-based selectivity is 87% wt, and the propylene / ethylene (mass ratio) is 3.1.

[0126] Example 2

[0127] This embodiment 2 adopts the device shown in Figure 1.

[0128] In Example 2, the raw materials are methanol and C4-C6 hydrocarbons, the methanol feed amount / C4-C6 hydrocarbon feed amount is about 1, the olefin content in the C4-C6 hydrocarbons is 46% wt, and the alkane content is 54% wt. The catalyst is a ZSM-5 molecular sieve catalyst.

[0129] The process operating conditions of the reaction zone (A) of the high-density fast fluidized bed reactor (1) are: gas superficial linear velocity of 2.6 m / s, temperature of 600°C, pressure of 170 kPa, bed density of 310 kg / m 3 , the reaction contact time is 1.2s.

[0130] The process operating conditions of the catalyst retention zone (B) are: gas superficial velocity of 0.2 m / s, temperature of 600 ° C, bed density of 600 kg / m 3 The catalyst circulation intensity flowing from the catalyst retention zone (B) to the reaction zone (A) is 720 kg / (m 2 ·s).

[0131] The regeneration gas is air. The process operating conditions of the fluidized bed regenerator (2) are: gas superficial linear velocity of 2.0 m / s, regeneration temperature of 650°C, regeneration pressure of 170 kPa, bed density of 200 kg / m 3 .

[0132] The single-pass conversion rate of methanol is 99.8% wt, the single-pass conversion rate of mixed hydrocarbons is 50% wt, the "ethylene + propylene" carbon-based selectivity is 78% wt, and the propylene / ethylene (mass ratio) is 4.4.

[0133] Example 3

[0134] This embodiment 3 adopts the device shown in Figure 1.

[0135] In this embodiment 3, the raw materials are methanol and C5-C 12 Hydrocarbon, methanol feed / C5-C 12 The hydrocarbon feed amount is about 1, C5-C 12 The olefin content in the hydrocarbons is 64% wt, and the alkane content is 36% wt. The catalyst is a ZSM-5 molecular sieve catalyst.

[0136] The process operating conditions of the reaction zone (A) of the high-density fast fluidized bed reactor (1) are: gas superficial linear velocity of 4.1 m / s, temperature of 650°C, pressure of 110 kPa, bed density of 190 kg / m 3 , the reaction contact time is 0.8s.

[0137] The process operating conditions of the catalyst retention zone (B) are: gas superficial velocity of 0.08 m / s, temperature of 650°C, bed density of 720 kg / m 3 The catalyst circulation intensity flowing from the catalyst retention zone (B) to the reaction zone (A) is 810 kg / (m 2 ·s).

[0138] The regeneration gas is air. The process operating conditions of the fluidized bed regenerator (2) are: gas superficial linear velocity of 1.6 m / s, regeneration temperature of 690°C, regeneration pressure of 110 kPa, bed density of 340 kg / m 3 .

[0139] The methanol single-pass conversion rate was 99.9% wt, the mixed hydrocarbon single-pass conversion rate was 77% wt, the "ethylene + propylene" carbon-based selectivity was 81% wt, and the propylene / ethylene (mass ratio) was 7.8.

[0140] Example 4

[0141] This embodiment 4 uses the device shown in Figure 1.

[0142] In this embodiment 4, the raw materials are methanol and C5-C12 Hydrocarbon, methanol feed / C5-C 12 The hydrocarbon feed amount is about 1, C5-C 12 The olefin content in the hydrocarbon is 8% wt, and the alkane content is 92% wt. The catalyst is a ZSM-5 molecular sieve catalyst.

[0143] The process operating conditions of the reaction zone (A) of the high-density fast fluidized bed reactor (1) are: gas superficial linear velocity of 7.0 m / s, temperature of 680°C, pressure of 50 kPa, bed density of 150 kg / m 3 , the reaction contact time is 0.5s.

[0144] The process operating conditions of the catalyst retention zone (B) are: gas superficial velocity of 0.02 m / s, temperature of 680°C, bed density of 800 kg / m 3 The catalyst circulation intensity of the catalyst flowing from the catalyst retention zone (B) to the reaction zone (A) is 1000 kg / (m 2 ·s).

[0145] The regeneration gas is air. The process operating conditions of the fluidized bed regenerator (2) are: gas superficial linear velocity of 0.9 m / s, regeneration temperature of 750°C, regeneration pressure of 50 kPa, bed density of 520 kg / m 3 .

[0146] The methanol single-pass conversion rate was 99.9% wt, the mixed hydrocarbon single-pass conversion rate was 65% wt, the "ethylene + propylene" carbon-based selectivity was 75% wt, and the propylene / ethylene (mass ratio) was 9.3.

[0147] 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 method for coupling methanol and mixed hydrocarbons to produce light olefins, characterized in that, Comprising the following steps: Feeding the gasified raw material including methanol and mixed hydrocarbons into the reaction zone, contacting with a catalyst, and reacting to generate a product gas containing light olefins and a catalyst stream I; After gas-solid separation of the stream I, a product gas and a catalyst are obtained; The product gas is transported to a downstream section; Part of the catalyst enters the reaction zone, and another part of the catalyst is regenerated, and the regenerated catalyst enters the reaction zone.

2. A method for coupling methanol and mixed hydrocarbons to produce light olefins according to claim 1, characterized in that, The mixed hydrocarbons in the raw material are C4+ hydrocarbons, including alkanes and olefins with carbon atom number ≥4.

3. A method for coupling methanol and mixed hydrocarbons to produce light olefins according to claim 1 or 2, characterized in that, The catalyst is selected from ZSM-5 molecular sieve catalysts.

4. A method for coupling methanol and mixed hydrocarbons to produce light olefins according to any one of claims 1 to 3, characterized in that, The process operating conditions of the reaction zone include: the apparent gas linear velocity is 1.5 to 7.0 m / s, the temperature is 500 to 680 °C, the pressure is 50 to 250 kPa, and the bed density is 150 to 500 kg / m 3 , and the reaction contact time is 0.5 to 2 s.

5. A method for coupling methanol and mixed hydrocarbons to produce light olefins according to any one of claims 1 to 4, characterized in that, The method is carried out in a methanol and mixed hydrocarbon to light olefin device, and the device includes a high-density fast fluidized bed reactor and a fluidized bed regenerator.

6. The method for coupling methanol and mixed hydrocarbons to produce light olefins according to claim 5, wherein, The high-density fast fluidized bed reactor includes a reactor outer shell, a reactor inner shell, and a conveying pipe; at least a raw material inlet, a catalyst inlet, a gas-phase product outlet, and a catalyst outlet are provided on the reactor outer shell; The reactor outer shell encloses an internal area; the reactor inner shell is located in the lower part of the internal area, and the area enclosed by the reactor inner shell is the reaction zone; The conveying pipe is located in the upper-middle part of the internal area, and the bottom of the conveying pipe is communicated with the reaction zone; The area enclosed by the reactor outer shell and the conveying pipe is the gas-solid separation zone; An outlet is provided on the conveying pipe, and the conveying pipe is communicated with the gas-solid separation 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 is communicated with the bottom of the catalyst residence zone; The catalyst residence zone is communicated with the gas-solid separation zone and is located below the gas-solid separation zone.

7. A method for coupling methanol and mixed hydrocarbons to produce light olefins according to claim 6, characterized in that, The process operating conditions of the catalyst residence zone include: the apparent gas linear velocity is 0.02 - 0.2 m / s, the temperature is 500 - 680 °C, and the bed density is 600 - 800 kg / m 3 .

8. A method for coupling methanol and mixed hydrocarbons to produce light olefins according to claim 6 or 7, characterized in that, The catalyst circulation intensity of the catalyst flowing from the catalyst residence zone to the reaction zone is 500 - 1000 kg / m 2 ·s.

9. A method for coupling methanol and mixed hydrocarbons to produce light olefins according to any one of claims 6 to 8, characterized in that, The high-density fast fluidized bed reactor includes a catalyst distribution pipe, a fluidizing steam distributor, and a raw material distributor; 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 arranged at the bottom of the catalyst residence zone; The raw material distributor is arranged at the bottom of the reaction zone; through holes are formed on the lower surface of the catalyst distribution pipe.

10. A method for coupling methanol and mixed hydrocarbons to produce light olefins according to any one of claims 6 to 9, characterized in that, The high-density fast fluidized bed reactor includes a first gas-solid separation device and a second gas-solid separation device; The first gas-solid separation device and the second gas-solid separation device are located in the gas-solid separation zone; The inlet of the first gas-solid separation device is communicated with the outlet of the conveying pipe; The catalyst outlet of the first gas-solid separation device is located in the lower part of the gas-solid separation zone, and the gas outlet of the first gas-solid separation device is located in the upper part of the gas-solid separation zone.

11. A method for coupling methanol and mixed hydrocarbons to produce light olefins according to claim 10, characterized in that, The inlet of the second gas-solid separation device is located in the upper part of the gas-solid separation zone; the catalyst outlet of the second gas-solid separation device is located in the lower part of the gas-solid separation zone.

12. A method for coupling methanol and mixed hydrocarbons to produce light olefins according to claim 10, characterized in that, The first gas-solid separation device is selected as an inertial separator.

13. A method for coupling methanol and mixed hydrocarbons to produce light olefins according to claim 10, characterized in that, The second gas-solid separation device is selected as one group or 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.

14. A method for coupling methanol and mixed hydrocarbons to produce light olefins according to any one of claims 5 to 13, characterized in that, The high-density fast fluidized bed reactor includes a reactor gas collecting chamber and a product gas delivery pipe; the reactor gas collecting chamber is located at the top of the high-density fast fluidized bed reactor; the product gas delivery pipe is connected to the top of the reactor gas collecting chamber; the gas outlet of the second gas-solid separation device is communicated with the reactor gas collecting chamber.

15. A method for coupling methanol and mixed hydrocarbons to produce light olefins according to any one of claims 5 to 14, characterized in that, The device includes a catalyst extraction pipe, which passes through the reactor outer shell and is located at the lower part of the catalyst residence zone, and the catalyst extraction pipe is communicated with the reactor stripper; The inlet of the spent catalyst slide valve is connected to the bottom of the reactor stripper, the outlet of the spent catalyst slide valve is connected to the inlet of the spent catalyst delivery pipe, and the outlet of the spent catalyst delivery pipe is communicated with the fluidized bed regenerator communicated; The regenerator stripper is located at the bottom of the fluidized bed regenerator; the inlet of the regenerated catalyst slide valve is connected to the bottom of the regenerator stripper, the outlet of the regenerated catalyst slide valve is connected to the inlet of the regenerated catalyst delivery pipe, and the outlet of the regenerated catalyst delivery pipe is connected to the lower part of the gas-solid separation zone of the high-density fast fluidized bed reactor.

16. A method for coupling methanol and mixed hydrocarbons to produce light olefins according to any one of claims 5 to 15, characterized in that, The fluidized bed regenerator includes a regenerator shell, a regenerator distributor, a third gas-solid separation device, a regenerator gas collecting chamber, and a flue gas delivery pipe; The regenerator distributor is located at the bottom of the fluidized bed regenerator; The third gas-solid separation device is located at the upper part of the fluidized bed regenerator. The inlet of the third gas-solid separation device is located at the upper part of the fluidized bed regenerator. The gas outlet of the third gas-solid separation device is communicated with the regenerator gas collecting chamber. The catalyst outlet of the third gas-solid separation device is located at the lower part of the fluidized bed regenerator. The regenerator gas collecting chamber is located at the top of the fluidized bed regenerator. The flue gas delivery pipe is connected to the top of the regenerator gas collecting chamber.

17. A method for coupling methanol and mixed hydrocarbons to produce light olefins according to claim 16, characterized in that, The inlet pipe of the regenerator stripper penetrates the regenerator shell and opens above the regenerator distributor.

18. A method for coupling methanol and mixed hydrocarbons to produce light olefins according to claim 16 or 17, characterized in that, The third gas-solid separation device adopts one or more groups of gas-solid cyclone separators. Each group of gas-solid cyclone separators includes a first-stage gas-solid cyclone separator and a second-stage gas-solid cyclone separator.

19. A method for coupling methanol and mixed hydrocarbons to produce light olefins according to any one of claims 5 to 18, characterized in that, The process operating conditions of the regenerator are as follows: the apparent gas linear velocity is 0.5 - 2.0 m / s, the regeneration temperature is 600 - 750 °C, the regeneration pressure is 50 - 250 kPa, and the bed density is 200 - 800 kg / m 3 .

20. A method for coupling methanol and mixed hydrocarbons to produce light olefins according to any one of claims 5 to 19, characterized in that, The regeneration gas of the fluidized bed regenerator is air.

21. A method for coupling methanol and mixed hydrocarbons to produce light olefins according to any one of claims 10 to 20, characterized in that, The stream I enters the first gas-solid separation device through a delivery pipe, and the catalyst after the first gas-solid separation enters the catalyst residence zone.

22. A method for coupling methanol and mixed hydrocarbons to produce light olefins according to any one of claims 6 to 20, characterized in that, Steam enters the catalyst residence zone from the fluidizing steam distributor. The steam carries a part of the catalyst in the catalyst residence zone into the gas-solid separation zone; the product gas and a part of the catalyst carried by the steam in the gas-solid separation zone enter the second gas-solid separation device. The gas after the second gas-solid separation enters the reactor gas collecting chamber, and the separated catalyst returns to the catalyst residence zone.

23. A method for coupling methanol and mixed hydrocarbons to produce light olefins according to claim 22, characterized in that, The product gas and steam after the second gas-solid separation enter the downstream section through the product gas delivery pipe; The first part of the catalyst in the catalyst residence zone enters the reaction zone through the catalyst distribution pipe; The second part of the catalyst in the catalyst residence zone enters the bottom of the reaction zone through the bottom of the catalyst residence zone; The third part of the catalyst in the catalyst residence zone enters the reactor stripper through the catalyst extraction pipe.

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