Process for the conversion of by-product mixed oxygenates in a methanol to olefins process

Abstract

The present application provides a feed distributor and a method for converting by-product mixed oxygen-containing compounds in a methanol-to-olefin process, the feed distributor comprising one or more horizontal feed distribution branches and one or more inclined feed distribution branches and a feed main pipe, the horizontal feed distribution branches and the inclined feed distribution branches being connected to the feed main pipe; an included angle β between the horizontal feed distribution main pipe and the inclined feed distribution branches being 90+α; a water solution of the by-product mixed oxygen-containing compounds separated from a methanol-to-olefin separation unit being fed into a fast bed reactor through the feed distributor and being reacted with regenerated catalysts fed into the reactor through a regenerated inclined pipe, the products and coked catalysts generated in the reaction going upwards. The method of the present application can efficiently convert the by-product mixed oxygen-containing compounds into low-carbon hydrocarbons, avoiding the generation of heavy hydrocarbons and phenolic compounds.

Description

Technical Field

[0001] This invention belongs to the field of methanol-to-olefins, specifically relating to a feed distributor and a method for converting mixed oxygen-containing compounds by-products in the methanol-to-olefins process. Background Technology

[0002] Methanol, as a chemical feedstock, can be reacted with SAPO-34 and ZSM-5 catalysts to produce ethylene, propylene, and aromatics. Ethylene and propylene (light olefins) are used in various methods for preparing plastics and other chemical compounds. The process of producing methanol from coal or natural gas is well-established and can achieve production scales of millions of tons. The MTO process produces oxygen-containing compounds such as ketones, aldehydes, and ethers as byproducts. To reduce carbon-based loss of the feedstock, current technologies directly return these oxygen-containing compounds and unconverted methanol to the MTO reactor or discharge them from the oxygen-containing compound conversion reactor for downstream product recovery. This recovery and subsequent treatment are often subject to various limitations and constraints. Currently, there is a need to improve the processing technology and system for converting oxygen-containing compounds to olefins, enabling the recovery of oxygen-containing compounds from suitable product streams. However, existing technologies suffer from low conversion rates of byproduct oxides, requiring large quantities to be disposed of externally.

[0003] CN105745012 discloses a method for enhancing the conversion of recycled oxygen-containing materials in MTO, comprising two fluidized bed reactors, wherein the oxygen-rich material stream obtained from the separation unit reacts with a portion of the regenerated catalyst stream in the second reactor. This method is complex due to the presence of two reactors, and the conversion details of the oxygen-rich material stream are not provided. Summary of the Invention

[0004] The technical problem to be solved by this invention is that the conversion rate of by-product oxides is low when the mixed oxygen-containing compounds are recycled during the methanol-to-olefins process. To this end, this invention provides a method for converting the mixed oxygen-containing compounds by-products during the methanol-to-olefins process. This method has the advantage of high oxide conversion rate when the oxides are recycled.

[0005] On the one hand, the present invention provides a method for converting mixed oxygen-containing compounds by-products in the methanol-to-olefins process, comprising: the mixed oxygen-containing compound aqueous solution feedstock (11) by-products of the methanol-to-olefins separation unit enters the fast bed reactor (1) through a cross-type feed distributor (9) and reacts with the regenerated catalyst (12) entering through the regenerated inclined tube (14), and the products generated by the reaction and the coking catalyst rise upward.

[0006] According to some embodiments of the present invention, the method further includes: methanol feedstock (10) enters the fast bed reactor (1) via methanol feedstock distributor (8) and reacts with the catalyst above the methanol feedstock distributor (8), thereby generating the product which rises to the secondary dense bed (2) for separation to obtain olefin-rich reaction product (13) and catalysts (16a), (16b) and (16c) to be generated.

[0007] According to some embodiments of the present invention, the method further includes: the reaction product (13) enters the subsequent separation unit through the cyclone separator (4) to obtain the mixed oxygen-containing aqueous solution raw material (11); the catalyst to be generated (16a) enters the regenerator for regeneration through the catalyst to be generated inclined tube (15); the catalyst to be generated (16b) returns to the fast bed reactor (1) through the circulating inclined tube (5); and the catalyst to be generated (16c) is heated by the external heat exchanger (3) and then returned to the fast bed reactor (1) through the external removal inclined tube (6).

[0008] According to some embodiments of the present invention, the cross-type feed distributor (9) includes one or more horizontal feed distribution branches (17), one or more inclined feed distribution branches (19), and a feed main (18), wherein the horizontal feed distribution branches (17) and the inclined feed distribution branches (19) are connected to the feed main (18), and the connection port of the feed main (18) to the fast bed reactor (1) is located at the lower part of the fast bed reactor.

[0009] According to some embodiments of the present invention, the mixed oxygen-containing aqueous solution feedstock (11) enters from the feed main pipe (18).

[0010] According to some embodiments of the present invention, the circulating inclined tube (5) is connected to the secondary dense bed (2) and the fast bed reactor (1), the regeneration inclined tube (14) is connected to the fast bed reactor (1), the waiting inclined tube (15) is connected to the secondary dense bed (2), and the externally removed inclined tube (6) is connected to the external heat exchanger (3) and the fast bed reactor (1).

[0011] According to some embodiments of the present invention, the methanol feedstock distributor (8) is located at the bottom of the fast bed reactor (1).

[0012] According to some embodiments of the present invention, the connection port between the regeneration inclined tube (14) and the fast bed reactor (1) is located above the cross-type feed distributor (9).

[0013] According to some embodiments of the present invention, the connection port of the circulating inclined tube (5) and the fast bed reactor (1) is located above the methanol feedstock distributor (8).

[0014] According to some embodiments of the present invention, the connection port between the external inclined tube (6) and the fast bed reactor (1) is located above the methanol feedstock distributor (8).

[0015] According to some embodiments of the present invention, the methanol feedstock distributor (8) is located above the connection port between the regeneration inclined tube (14) and the fast bed reactor (1).

[0016] According to some embodiments of the present invention, the included angle β between the horizontal feed distribution main pipe (17) and the inclined feed distribution branch pipe (19) is 90+α, where α is the included angle between the catalyst inclined pipe (20) and the fast bed reactor (1).

[0017] According to some embodiments of the present invention, the vertical distance H between the non-connecting end of the inclined feed distribution branch (19) and the horizontal feed distribution branch (17), and the distance L from the connection point of the inclined feed distribution branch (19) and the horizontal feed distribution branch (17) to the reactor wall, wherein the relationship between α, H and L is as follows:

[0018]

[0019] According to some embodiments of the present invention, the horizontal feed distribution branch pipe (17) and the inclined feed distribution branch pipe (19) are provided with at least one row of small holes (21).

[0020] According to a preferred embodiment of the present invention, when the horizontal feed distribution branch pipe (17) and the inclined feed distribution branch pipe (19) are provided with a row of small holes (21), the holes are opened along the reactor axis.

[0021] According to some embodiments of the present invention, the shape of the small hole (21) includes at least one selected from circles, ellipses and rectangles.

[0022] According to some embodiments of the present invention, the small hole (21) is circular.

[0023] According to some embodiments of the present invention, the orifices (21) are evenly distributed in parallel or evenly distributed in an alternating manner.

[0024] According to some embodiments of the present invention, the aperture ratio of the orifice (21) is 0.05 to 0.2. The aperture ratio refers to the ratio of the total area of ​​the apertures to the cross-sectional area of ​​the reactor bed.

[0025] According to some embodiments of the present invention, the diameter ratio of the horizontal feed distribution main pipe (17) and the inclined feed distribution branch pipe (19) is (0.5~1.5):1.

[0026] According to some embodiments of the present invention, the diameter ratio of the main feed pipe (18) and the inclined feed distribution branch pipe (19) is (0.5~1):1.

[0027] According to some embodiments of the present invention, the included angle α between the catalyst inclined tube (20) and the reactor is 30° to 70°.

[0028] According to some embodiments of the present invention, the ratio of the horizontal length of the cross-type feed distributor (9) to the diameter of the fast bed reactor (1) is (0.3 to 0.6):1.

[0029] According to some embodiments of the present invention, the ratio of the distance L from the connection point of the inclined feed distribution branch (19) and the horizontal feed distribution branch (17) to the reactor wall to the length of the cross-type feed distributor (9) in the horizontal direction is (0.1 to 0.5):1.

[0030] According to some embodiments of the present invention, the distance between the methanol feed distributor (8) and the cross-type feed distributor (9) is 1%-5% of the total height of the fast bed reactor (1).

[0031] According to some embodiments of the present invention, the mass percentage of the mixed oxygen-containing compounds in the mixed oxygen-containing compound aqueous solution raw material (11) is 5% to 70%.

[0032] According to a preferred embodiment of the present invention, the mixed oxygen-containing compound includes methanol and at least one selected from ethanol, propanol, butanol, acetaldehyde, propionaldehyde, butyraldehyde, acetone, butanone, formic acid, acetic acid, and propionic acid.

[0033] According to a preferred embodiment of the present invention, the mass percentage of ketones in the mixed oxygen-containing compound is 30% to 80%.

[0034] According to some embodiments of the present invention, the temperature inside the fast bed reactor (1) is 450–520°C, the gas velocity is 0.5–3 m / s, the catalyst bed density is 30–200 kg / m³, the reaction gauge pressure is 0–0.4 MPa, and the mass hourly space velocity of the methanol feedstock (10) is 3–30 h⁻¹. -1 The mass hourly space velocity (MSV) of the mixed oxygen-containing aqueous solution feedstock (11) is 0.05–1 h⁻¹. -1 .

[0035] According to some embodiments of the present invention, the regenerated catalyst (12) has a carbon content of less than 0.1% based on the total mass of the catalyst.

[0036] In another aspect, the present invention provides an application of the method according to the first aspect in the industrial production of methanol-to-olefins.

[0037] The method for converting mixed oxygen-containing compounds byproducts in the methanol-to-olefins process provided by this invention employs a cross-feed distributor, allowing the aqueous solution of mixed oxygen-containing compounds to fully and uniformly contact and react with the regenerated catalyst, thereby efficiently converting them into low-carbon hydrocarbons and avoiding the formation of heavy hydrocarbons and phenolic compounds. Using the technical solution of this invention, the oxide conversion rate is high during oxide reprocessing, and the total carbon-based yield of ethylene and propylene can reach over 82%, achieving good technical results. Attached Figure Description

[0038] Figure 1 The diagram below shows a fluidized bed reactor according to the present invention, wherein 1 is a fast bed reactor; 2 is a double-dense bed reactor; 3 is an external heat exchanger; 4 is a cyclone separator; 5 is a circulating inclined tube; 6 is an external lower inclined tube; 7 is an external upper inclined tube; 8 is a methanol feed distributor; 9 is a cross-feed distributor; 10 is methanol feed; 11 is a mixed oxygen-containing compound aqueous solution feed; 12 is a regenerated catalyst; 13 is the reaction product; 14 is a regenerated inclined tube; 15 is a pre-regenerated inclined tube; and 16 is a pre-regenerated catalyst.

[0039] Figure 2 The diagram below shows a cross-feed distributor according to the present invention, wherein 17 is a horizontal feed distribution main pipe; 18 is a feed main pipe; 19 is an inclined feed distribution branch pipe; 20 is a catalyst inclined pipe; and 21 is a small hole. Detailed Implementation

[0040] The present invention will be further illustrated by the following embodiments, but is not limited to these embodiments.

[0041]

Example 1

[0042] A fluidized bed reactor employing SAPO-34 catalyst and a cross-feed distributor includes a fast bed reactor (1), a secondary dense bed (2), an external heat exchanger (3), a circulating inclined tube (5), an external heat exchanger (6), a regeneration inclined tube (14), a pre-regeneration inclined tube (15), a methanol feed distributor (8), and a cross-feed distributor (9). The circulating inclined tube (5) connects the secondary dense bed (2) and the fast bed reactor (1); the regeneration inclined tube (14) is connected to the fast bed reactor (1); the pre-regeneration inclined tube (15) is connected to the secondary dense bed (2); the external heat exchanger (6) connects the external heat exchanger (3) and the fast bed reactor (1); and the methanol feed distributor... (8) and the cross-type feed distributor (9) are both located at the bottom of the fast bed reactor (1); the connection port between the regeneration inclined tube (14) and the fast bed reactor (1) is located directly above the cross-type feed distributor (9); the connection port between the circulation inclined tube (5) and the fast bed reactor (1) is located above the methanol feed distributor (8); the connection port between the externally removed inclined tube (6) and the fast bed reactor (1) is located above the methanol feed distributor (8); the methanol feed distributor (8) is located above the connection port between the regeneration inclined tube (14) and the fast bed reactor (1); the distance between the methanol feed distributor (8) and the cross-type feed distributor (9) is 1% of the total height of the fast bed reactor (1).

[0043] The mixed oxygenated compound aqueous solution feedstock (11) produced by the MTO separation unit enters the fast bed reactor (1) through the cross-type feed distributor (9) and reacts with the regenerated catalyst (12) from the regeneration inclined tube (14). The reaction products and coking catalyst rise upwards. The methanol feedstock (10) enters the fast bed reactor (1) through the methanol feedstock distributor (8) and reacts with the catalyst. The resulting olefin-rich reaction products and the spent catalyst (16) rise upwards and enter the secondary dense bed (2) for separation. The spent catalyst (16) enters the regenerator for regeneration through the spent inclined tube (15). The reaction products (13) enter the subsequent separation unit through the cyclone separator (4) to obtain the mixed oxygenated compound aqueous solution feedstock (11). The spent catalyst (16) in the secondary dense bed (2) returns to the fast bed reactor (1) through the circulating inclined tube (5). The catalyst after being heated by the external heat exchanger (3) returns to the fast bed reactor (1) through the external removal inclined tube (6).

[0044] The cross-type feed distributor (9) includes: 6 horizontal feed distribution branches (17) and 6 inclined feed distribution branches (19) and a feed main (18); the included angle β between the horizontal feed distribution main (17) and the inclined feed distribution branches (19) is 90+α, where α is the included angle between the catalyst inclined tube (20) and the reactor; the horizontal feed distribution main (17) and the inclined feed distribution branches (19) are provided with a row of small holes (21); the horizontal feed distribution branches (17) and the inclined feed distribution branches (19) are connected to the feed main (18), and the mixed oxygen-containing aqueous solution raw material (11) enters from the feed main (18).

[0045] The small holes (21) on the horizontal feed distribution main pipe (17) and the inclined feed distribution branch pipe (19) are arranged in a row and are opened along the reactor axis.

[0046] The small holes (21) on the horizontal feed distribution main pipe (17) and the inclined feed distribution branch pipe (19) are circular, and the small holes (21) are evenly distributed side by side, with an opening ratio of 0.1.

[0047] The diameter ratio of the horizontal feed distribution main pipe (17) to the inclined feed distribution branch pipe (19) is 1.2:1; the diameter ratio of the feed main pipe (18) to the inclined feed distribution branch pipe (19) is 0.8:1; the included angle α between the catalyst inclined tube (20) and the reactor is 50°.

[0048] The ratio of the horizontal length of the cross-type feed distributor (9) to the diameter of the fast bed reactor (1) is 0.45:1; the ratio of the distance L from the connection point of the inclined feed distribution branch (19) and the horizontal feed distribution branch (17) to the reactor wall to the horizontal length of the cross-type feed distributor (9) is 0.3:1.

[0049] The mixed oxygen-containing compound aqueous solution raw material (11) contains 30% by mass of mixed oxygen-containing compounds, which include methanol, ethanol, propanol, butanol, acetaldehyde, propionaldehyde, butyraldehyde, acetone, butanone, formic acid, acetic acid, and propionic acid. The ketone content in the mixed oxygen-containing compound is 60% by mass.

[0050] The temperature inside the fast bed reactor (1) was 490℃, the gas velocity was 2.2 m / s, the catalyst bed density was 140 kg / m³, the reaction gauge pressure was 0.25 MPa, and the mass hourly space velocity (MHSV) of the methanol feedstock (10) was 20 h⁻¹. -1 The mass hourly space velocity (MSV) of the mixed oxygen-containing aqueous solution feedstock (11) was 0.6 h⁻¹. -1 The regenerated catalyst (12) has a carbon content of 0.06% based on the total mass of the catalyst.

[0051] The methanol conversion rate was 99.9%, and the total carbon-based yield of ethylene and propylene was 83.4% by weight.

[0052]

Example 2

[0053] A fluidized bed reactor employing SAPO-34 catalyst and a cross-feed distributor includes a fast bed reactor (1), a secondary dense bed (2), an external heat exchanger (3), a circulating inclined tube (5), an external heat exchanger (6), a regeneration inclined tube (14), a pre-regeneration inclined tube (15), a methanol feed distributor (8), and a cross-feed distributor (9). The circulating inclined tube (5) connects the secondary dense bed (2) and the fast bed reactor (1); the regeneration inclined tube (14) is connected to the fast bed reactor (1); the pre-regeneration inclined tube (15) is connected to the secondary dense bed (2); the external heat exchanger (6) connects the external heat exchanger (3) and the fast bed reactor (1); and the methanol feed distributor... (8) and the cross-type feed distributor (9) are both located at the bottom of the fast bed reactor (1); the connection port between the regeneration inclined tube (14) and the fast bed reactor (1) is located directly above the cross-type feed distributor (9); the connection port between the circulation inclined tube (5) and the fast bed reactor (1) is located above the methanol feed distributor (8); the connection port between the externally removed inclined tube (6) and the fast bed reactor (1) is located above the methanol feed distributor (8); the methanol feed distributor (8) is located above the connection port between the regeneration inclined tube (14) and the fast bed reactor (1); the distance between the methanol feed distributor (8) and the cross-type feed distributor (9) is 5% of the total height of the fast bed reactor (1).

[0054] The mixed oxygenated compound aqueous solution feedstock (11) produced by the MTO separation unit enters the fast bed reactor (1) through the cross-type feed distributor (9) and reacts with the regenerated catalyst (12) from the regeneration inclined tube (14). The reaction products and coking catalyst rise upwards. The methanol feedstock (10) enters the fast bed reactor (1) through the methanol feedstock distributor (8) and reacts with the catalyst. The resulting olefin-rich reaction products and the spent catalyst (16) rise upwards and enter the secondary dense bed (2) for separation. The spent catalyst (16) enters the regenerator for regeneration through the spent inclined tube (15). The reaction products (13) enter the subsequent separation unit through the cyclone separator (4) to obtain the mixed oxygenated compound aqueous solution feedstock (11). The spent catalyst (16) in the secondary dense bed (2) returns to the fast bed reactor (1) through the circulating inclined tube (5). The catalyst after being heated by the external heat exchanger (3) returns to the fast bed reactor (1) through the external removal inclined tube (6).

[0055] The cross-type feed distributor (9) includes: 7 horizontal feed distribution branches (17) and 7 inclined feed distribution branches (19) and a feed main (18); the included angle β between the horizontal feed distribution main (17) and the inclined feed distribution branches (19) is 90+α, where α is the included angle between the catalyst inclined tube (20) and the reactor; the horizontal feed distribution main (17) and the inclined feed distribution branches (19) are provided with 2 rows of small holes (21); the horizontal feed distribution branches (17) and the inclined feed distribution branches (19) are connected to the feed main (18), and the mixed oxygen-containing aqueous solution raw material (11) enters from the feed main (18).

[0056] The small holes (21) on the horizontal feed distribution main pipe (17) and the inclined feed distribution branch pipe (19) are arranged in a row and are opened along the reactor axis.

[0057] The holes (21) on the horizontal feed distribution main pipe (17) and the inclined feed distribution branch pipe (19) are circular and are evenly distributed in an alternating pattern, with an opening ratio of 0.1.

[0058] The diameter ratio of the horizontal feed distribution main pipe (17) to the inclined feed distribution branch pipe (19) is 1.2:1; the diameter ratio of the feed main pipe (18) to the inclined feed distribution branch pipe (19) is 0.8:1; the included angle α between the catalyst inclined tube (20) and the reactor is 50°.

[0059] The ratio of the horizontal length of the cross-type feed distributor (9) to the diameter of the fast bed reactor (1) is 0.45:1; the ratio of the distance L from the connection point of the inclined feed distribution branch (19) and the horizontal feed distribution branch (17) to the reactor wall to the horizontal length of the cross-type feed distributor (9) is 0.3:1.

[0060] The mixed oxygen-containing compound aqueous solution raw material (11) contains 30% by mass of mixed oxygen-containing compounds, which include methanol, ethanol, propanol, butanol, acetaldehyde, propionaldehyde, butyraldehyde, acetone, butanone, formic acid, acetic acid, and propionic acid. The ketone content in the mixed oxygen-containing compound is 60% by mass.

[0061] The temperature inside the fast bed reactor (1) was 470℃, the gas velocity was 1.2 m / s, the catalyst bed density was 180 kg / m³, the reaction gauge pressure was 0.2 MPa, and the mass hourly space velocity (MHSV) of the methanol feedstock (10) was 12 h⁻¹. -1 The mass hourly space velocity (MSV) of the mixed oxygen-containing aqueous solution feedstock (11) was 0.2 h⁻¹. -1 The regenerated catalyst (12) has a carbon content of 0.03% based on the total mass of the catalyst.

[0062] The methanol conversion rate was 99.9%, and the total carbon-based yield of ethylene and propylene was 84.9% by weight.

[0063]

Example 3

[0064] A fluidized bed reactor employing SAPO-34 catalyst and a cross-feed distributor includes a fast bed reactor (1), a secondary dense bed (2), an external heat exchanger (3), a circulating inclined tube (5), an external heat exchanger (6), a regeneration inclined tube (14), a pre-regeneration inclined tube (15), a methanol feed distributor (8), and a cross-feed distributor (9). The circulating inclined tube (5) connects the secondary dense bed (2) and the fast bed reactor (1); the regeneration inclined tube (14) is connected to the fast bed reactor (1); the pre-regeneration inclined tube (15) is connected to the secondary dense bed (2); the external heat exchanger (6) connects the external heat exchanger (3) and the fast bed reactor (1); and the methanol feed distributor... (8) and the cross-type feed distributor (9) are both located at the bottom of the fast bed reactor (1); the connection port between the regeneration inclined tube (14) and the fast bed reactor (1) is located directly above the cross-type feed distributor (9); the connection port between the circulation inclined tube (5) and the fast bed reactor (1) is located above the methanol feed distributor (8); the connection port between the externally removed inclined tube (6) and the fast bed reactor (1) is located above the methanol feed distributor (8); the methanol feed distributor (8) is located above the connection port between the regeneration inclined tube (14) and the fast bed reactor (1); the distance between the methanol feed distributor (8) and the cross-type feed distributor (9) is 4% of the total height of the fast bed reactor (1).

[0065] The mixed oxygenated compound aqueous solution feedstock (11) produced by the MTO separation unit enters the fast bed reactor (1) through the cross-type feed distributor (9) and reacts with the regenerated catalyst (12) from the regeneration inclined tube (14). The reaction products and coking catalyst rise upwards. The methanol feedstock (10) enters the fast bed reactor (1) through the methanol feedstock distributor (8) and reacts with the catalyst. The resulting olefin-rich reaction products and the spent catalyst (16) rise upwards and enter the secondary dense bed (2) for separation. The spent catalyst (16) enters the regenerator for regeneration through the spent inclined tube (15). The reaction products (13) enter the subsequent separation unit through the cyclone separator (4) to obtain the mixed oxygenated compound aqueous solution feedstock (11). The spent catalyst (16) in the secondary dense bed (2) returns to the fast bed reactor (1) through the circulating inclined tube (5). The catalyst after being heated by the external heat exchanger (3) returns to the fast bed reactor (1) through the external removal inclined tube (6).

[0066] The cross-type feed distributor (9) includes: 9 horizontal feed distribution branches (17) and 9 inclined feed distribution branches (19) and a feed main (18); the included angle β between the horizontal feed distribution main (17) and the inclined feed distribution branches (19) is 90+α, where α is the included angle between the catalyst inclined tube (20) and the reactor; the horizontal feed distribution main (17) and the inclined feed distribution branches (19) are provided with 3 rows of small holes (21); the horizontal feed distribution branches (17) and the inclined feed distribution branches (19) are connected to the feed main (18), and the mixed oxygen-containing aqueous solution raw material (11) enters from the feed main (18).

[0067] The small holes (21) on the horizontal feed distribution main pipe (17) and the inclined feed distribution branch pipe (19) are arranged in a row and are opened along the reactor axis.

[0068] The small holes (21) on the horizontal feed distribution main pipe (17) and the inclined feed distribution branch pipe (19) are circular, and the small holes (21) are evenly distributed side by side, with an opening ratio of 0.05.

[0069] The diameter ratio of the horizontal feed distribution main pipe (17) to the inclined feed distribution branch pipe (19) is 1:1; the diameter ratio of the feed main pipe (18) to the inclined feed distribution branch pipe (19) is 0.5:1; the included angle α between the catalyst inclined pipe (20) and the reactor is 50°.

[0070] The ratio of the horizontal length of the cross-type feed distributor (9) to the diameter of the fast bed reactor (1) is 0.42:1; the ratio of the distance L from the connection point of the inclined feed distribution branch (19) and the horizontal feed distribution branch (17) to the reactor wall to the horizontal length of the cross-type feed distributor (9) is 0.35:1.

[0071] The mixed oxygen-containing compound aqueous solution raw material (11) contains 50% by mass of mixed oxygen-containing compounds, which include methanol, ethanol, propanol, butanol, acetaldehyde, propionaldehyde, butyraldehyde, acetone, butanone, formic acid, acetic acid, and propionic acid. The ketone content in the mixed oxygen-containing compound is 35% by mass.

[0072] The temperature inside the fast bed reactor (1) is 500℃, the gas velocity is 2.8 m / s, the catalyst bed density is 120 kg / m³, the reaction gauge pressure is 0.26 MPa, and the mass hourly space velocity of the methanol feedstock (10) is 15 h⁻¹. -1 The mass hourly space velocity (MSV) of the mixed oxygen-containing aqueous solution feedstock (11) was 0.7 h⁻¹. -1 The regenerated catalyst (12) has a carbon content of 0.08% based on the total mass of the catalyst.

[0073] The methanol conversion rate was 99.9%, and the total carbon-based yield of ethylene and propylene was 83.4% by weight.

[0074]

Example 4

[0075] A fluidized bed reactor employing SAPO-34 catalyst and a cross-feed distributor includes a fast bed reactor (1), a secondary dense bed (2), an external heat exchanger (3), a circulating inclined tube (5), an external heat exchanger (6), a regeneration inclined tube (14), a pre-regeneration inclined tube (15), a methanol feed distributor (8), and a cross-feed distributor (9). The circulating inclined tube (5) connects the secondary dense bed (2) and the fast bed reactor (1); the regeneration inclined tube (14) is connected to the fast bed reactor (1); the pre-regeneration inclined tube (15) is connected to the secondary dense bed (2); the external heat exchanger (6) connects the external heat exchanger (3) and the fast bed reactor (1); and the methanol feed distributor... (8) and the cross-type feed distributor (9) are both located at the bottom of the fast bed reactor (1); the connection port between the regeneration inclined tube (14) and the fast bed reactor (1) is located directly above the cross-type feed distributor (9); the connection port between the circulation inclined tube (5) and the fast bed reactor (1) is located above the methanol feed distributor (8); the connection port between the externally removed inclined tube (6) and the fast bed reactor (1) is located above the methanol feed distributor (8); the methanol feed distributor (8) is located above the connection port between the regeneration inclined tube (14) and the fast bed reactor (1); the distance between the methanol feed distributor (8) and the cross-type feed distributor (9) is 3% of the total height of the fast bed reactor (1).

[0076] The mixed oxygenated compound aqueous solution feedstock (11) produced by the MTO separation unit enters the fast bed reactor (1) through the cross-type feed distributor (9) and reacts with the regenerated catalyst (12) from the regeneration inclined tube (14). The reaction products and coking catalyst rise upwards. The methanol feedstock (10) enters the fast bed reactor (1) through the methanol feedstock distributor (8) and reacts with the catalyst. The resulting olefin-rich reaction products and the spent catalyst (16) rise upwards and enter the secondary dense bed (2) for separation. The spent catalyst (16) enters the regenerator for regeneration through the spent inclined tube (15). The reaction products (13) enter the subsequent separation unit through the cyclone separator (4) to obtain the mixed oxygenated compound aqueous solution feedstock (11). The spent catalyst (16) in the secondary dense bed (2) returns to the fast bed reactor (1) through the circulating inclined tube (5). The catalyst after being heated by the external heat exchanger (3) returns to the fast bed reactor (1) through the external removal inclined tube (6).

[0077] The cross-feed distributor (9) includes: 15 horizontal feed distribution branches (17) and 10 inclined feed distribution branches (19) and a main feed pipe (18); the included angle β between the horizontal feed distribution main pipe (17) and the inclined feed distribution branches (19) is 90+α, where α is the included angle between the catalyst inclined tube (20) and the reactor; the horizontal feed distribution main pipe (17) and the inclined feed distribution branches (19) are provided with a row of small holes (21); the horizontal feed distribution branches (17) and the inclined feed distribution branches (19) are connected to the main feed pipe (18), and the mixed oxygen-containing aqueous solution raw material (11) enters from the main feed pipe (18).

[0078] The small holes (21) on the horizontal feed distribution main pipe (17) and the inclined feed distribution branch pipe (19) are arranged in a row and are opened along the reactor axis.

[0079] The small holes (21) on the horizontal feed distribution main pipe (17) and the inclined feed distribution branch pipe (19) are circular, and the small holes (21) are evenly distributed side by side, with an opening ratio of 0.2.

[0080] The diameter ratio of the horizontal feed distribution main pipe (17) to the inclined feed distribution branch pipe (19) is 1:1; the diameter ratio of the feed main pipe (18) to the inclined feed distribution branch pipe (19) is 0.5:1; the included angle α between the catalyst inclined pipe (20) and the reactor is 50°.

[0081] The ratio of the horizontal length of the cross-type feed distributor (9) to the diameter of the fast bed reactor (1) is 0.42:1; the ratio of the distance L from the connection point of the inclined feed distribution branch (19) and the horizontal feed distribution branch (17) to the reactor wall to the horizontal length of the cross-type feed distributor (9) is 0.35:1.

[0082] The mixed oxygen-containing compound aqueous solution raw material (11) contains 50% by mass of mixed oxygen-containing compounds, which include methanol, ethanol, propanol, butanol, acetaldehyde, propionaldehyde, butyraldehyde, acetone, butanone, formic acid, acetic acid, and propionic acid. The ketone content in the mixed oxygen-containing compound is 35% by mass.

[0083] The temperature inside the fast bed reactor (1) was 510℃, the gas velocity was 2.8 m / s, the catalyst bed density was 100 kg / m³, the reaction gauge pressure was 0.32 MPa, and the mass hourly space velocity (MSV) of the methanol feedstock (10) was 28 h⁻¹. -1 The mass hourly space velocity (MSV) of the mixed oxygen-containing aqueous solution feedstock (11) was 0.8 h⁻¹. -1 The regenerated catalyst (12) has a carbon content of 0.08% based on the total mass of the catalyst.

[0084] The methanol conversion rate was 99.9%, and the total carbon-based yield of ethylene and propylene was 85.2% by weight.

[0085]

Example 5

[0086] A fluidized bed reactor employing SAPO-34 catalyst and a cross-feed distributor includes a fast bed reactor (1), a secondary dense bed (2), an external heat exchanger (3), a circulating inclined tube (5), an external heat exchanger (6), a regeneration inclined tube (14), a pre-regeneration inclined tube (15), a methanol feed distributor (8), and a cross-feed distributor (9). The circulating inclined tube (5) connects the secondary dense bed (2) and the fast bed reactor (1); the regeneration inclined tube (14) is connected to the fast bed reactor (1); the pre-regeneration inclined tube (15) is connected to the secondary dense bed (2); the external heat exchanger (6) connects the external heat exchanger (3) and the fast bed reactor (1); and the methanol feed distributor... (8) and the cross-type feed distributor (9) are both located at the bottom of the fast bed reactor (1); the connection port between the regeneration inclined tube (14) and the fast bed reactor (1) is located directly above the cross-type feed distributor (9); the connection port between the circulation inclined tube (5) and the fast bed reactor (1) is located above the methanol feed distributor (8); the connection port between the externally removed inclined tube (6) and the fast bed reactor (1) is located above the methanol feed distributor (8); the methanol feed distributor (8) is located above the connection port between the regeneration inclined tube (14) and the fast bed reactor (1); the distance between the methanol feed distributor (8) and the cross-type feed distributor (9) is 2% of the total height of the fast bed reactor (1).

[0087] The mixed oxygenated compound aqueous solution feedstock (11) produced by the MTO separation unit enters the fast bed reactor (1) through the cross-type feed distributor (9) and reacts with the regenerated catalyst (12) from the regeneration inclined tube (14). The reaction products and coking catalyst rise upwards. The methanol feedstock (10) enters the fast bed reactor (1) through the methanol feedstock distributor (8) and reacts with the catalyst. The resulting olefin-rich reaction products and the spent catalyst (16) rise upwards and enter the secondary dense bed (2) for separation. The spent catalyst (16) enters the regenerator for regeneration through the spent inclined tube (15). The reaction products (13) enter the subsequent separation unit through the cyclone separator (4) to obtain the mixed oxygenated compound aqueous solution feedstock (11). The spent catalyst (16) in the secondary dense bed (2) returns to the fast bed reactor (1) through the circulating inclined tube (5). The catalyst after being heated by the external heat exchanger (3) returns to the fast bed reactor (1) through the external removal inclined tube (6).

[0088] The cross-feed distributor (9) includes: 8 horizontal feed distribution branches (17) and 6 inclined feed distribution branches (19) and a feed main (18); the included angle β between the horizontal feed distribution main (17) and the inclined feed distribution branches (19) is 90+α, where α is the included angle between the catalyst inclined tube (20) and the reactor; the horizontal feed distribution main (17) and the inclined feed distribution branches (19) are provided with 2 rows of small holes (21); the horizontal feed distribution branches (17) and the inclined feed distribution branches (19) are connected to the feed main (18), and the mixed oxygen-containing aqueous solution raw material (11) enters from the feed main (18).

[0089] The small holes (21) on the horizontal feed distribution main pipe (17) and the inclined feed distribution branch pipe (19) are arranged in a row and are opened along the reactor axis.

[0090] The small holes (21) on the horizontal feed distribution main pipe (17) and the inclined feed distribution branch pipe (19) are circular, and the small holes (21) are evenly distributed side by side, with an opening ratio of 0.15.

[0091] The diameter ratio of the horizontal feed distribution main pipe (17) to the inclined feed distribution branch pipe (19) is 1.5:1; the diameter ratio of the feed main pipe (18) to the inclined feed distribution branch pipe (19) is 1:1; the included angle α between the catalyst inclined tube (20) and the reactor is 60°.

[0092] The ratio of the horizontal length of the cross-type feed distributor (9) to the diameter of the fast bed reactor (1) is 0.55:1; the ratio of the distance L from the connection point of the inclined feed distribution branch (19) and the horizontal feed distribution branch (17) to the reactor wall to the horizontal length of the cross-type feed distributor (9) is 0.15:1.

[0093] The mixed oxygen-containing compound aqueous solution raw material (11) contains 20% mixed oxygen-containing compounds by mass, and the mixed oxygen-containing compounds contain methanol, ethanol, propanol, butanol, acetaldehyde, propionaldehyde, butyraldehyde, acetone, butanone, formic acid, acetic acid, and propionic acid by mass. The mixed oxygen-containing compounds contain 70% ketones by mass.

[0094] The temperature inside the fast bed reactor (1) is 480℃, the gas velocity is 2 m / s, the catalyst bed density is 150 kg / m³, the reaction gauge pressure is 0.18 MPa, and the mass hourly space velocity of the methanol feedstock (10) is 12 h⁻¹. -1 The mass hourly space velocity (MSV) of the mixed oxygen-containing aqueous solution feedstock (11) was 0.3 h⁻¹. -1 The regenerated catalyst (12) has a carbon content of 0.05% based on the total mass of the catalyst.

[0095] The methanol conversion rate was 99.9%, and the total carbon-based yield of ethylene and propylene was 83.2% by weight.

[0096]

Example 6

[0097] A fluidized bed reactor employing SAPO-34 catalyst and a cross-feed distributor includes a fast bed reactor (1), a secondary dense bed (2), an external heat exchanger (3), a circulating inclined tube (5), an external heat exchanger (6), a regeneration inclined tube (14), a pre-regeneration inclined tube (15), a methanol feed distributor (8), and a cross-feed distributor (9). The circulating inclined tube (5) connects the secondary dense bed (2) and the fast bed reactor (1); the regeneration inclined tube (14) is connected to the fast bed reactor (1); the pre-regeneration inclined tube (15) is connected to the secondary dense bed (2); the external heat exchanger (6) connects the external heat exchanger (3) and the fast bed reactor (1); and the methanol feed distributor... (8) and the cross-type feed distributor (9) are both located at the bottom of the fast bed reactor (1); the connection port between the regeneration inclined tube (14) and the fast bed reactor (1) is located directly above the cross-type feed distributor (9); the connection port between the circulation inclined tube (5) and the fast bed reactor (1) is located above the methanol feed distributor (8); the connection port between the externally removed inclined tube (6) and the fast bed reactor (1) is located above the methanol feed distributor (8); the methanol feed distributor (8) is located above the connection port between the regeneration inclined tube (14) and the fast bed reactor (1); the distance between the methanol feed distributor (8) and the cross-type feed distributor (9) is 4% of the total height of the fast bed reactor (1).

[0098] The mixed oxygenated compound aqueous solution feedstock (11) produced by the MTO separation unit enters the fast bed reactor (1) through the cross-type feed distributor (9) and reacts with the regenerated catalyst (12) from the regeneration inclined tube (14). The reaction products and coking catalyst rise upwards. The methanol feedstock (10) enters the fast bed reactor (1) through the methanol feedstock distributor (8) and reacts with the catalyst. The resulting olefin-rich reaction products and the spent catalyst (16) rise upwards and enter the secondary dense bed (2) for separation. The spent catalyst (16) enters the regenerator for regeneration through the spent inclined tube (15). The reaction products (13) enter the subsequent separation unit through the cyclone separator (4) to obtain the mixed oxygenated compound aqueous solution feedstock (11). The spent catalyst (16) in the secondary dense bed (2) returns to the fast bed reactor (1) through the circulating inclined tube (5). The catalyst after being heated by the external heat exchanger (3) returns to the fast bed reactor (1) through the external removal inclined tube (6).

[0099] The cross-feed distributor (9) includes: three horizontal feed distribution branches (17) and three inclined feed distribution branches (19) and a main feed pipe (18); the included angle β between the horizontal feed distribution main pipe (17) and the inclined feed distribution branches (19) is 90+α, where α is the included angle between the catalyst inclined tube (20) and the reactor; the horizontal feed distribution main pipe (17) and the inclined feed distribution branches (19) are provided with a row of small holes (21); the horizontal feed distribution branches (17) and the inclined feed distribution branches (19) are connected to the main feed pipe (18), and the mixed oxygen-containing aqueous solution raw material (11) enters from the main feed pipe (18).

[0100] The small holes (21) on the horizontal feed distribution main pipe (17) and the inclined feed distribution branch pipe (19) are arranged in a row and are opened along the reactor axis.

[0101] The small holes (21) on the horizontal feed distribution main pipe (17) and the inclined feed distribution branch pipe (19) are circular, and the small holes (21) are evenly distributed side by side, with an opening ratio of 0.15.

[0102] The diameter ratio of the horizontal feed distribution main pipe (17) to the inclined feed distribution branch pipe (19) is 0.5:1; the diameter ratio of the feed main pipe (18) to the inclined feed distribution branch pipe (19) is 1:1; the included angle α between the catalyst inclined tube (20) and the reactor is 60°.

[0103] The ratio of the horizontal length of the cross-type feed distributor (9) to the diameter of the fast bed reactor (1) is 0.55:1; the ratio of the distance L from the connection point of the inclined feed distribution branch (19) and the horizontal feed distribution branch (17) to the reactor wall to the horizontal length of the cross-type feed distributor (9) is 0.15:1.

[0104] The mixed oxygen-containing compound aqueous solution raw material (11) contains 20% mixed oxygen-containing compounds by mass, and the mixed oxygen-containing compounds contain methanol, ethanol, propanol, butanol, acetaldehyde, propionaldehyde, butyraldehyde, acetone, butanone, formic acid, acetic acid, and propionic acid by mass. The mixed oxygen-containing compounds contain 70% ketones by mass.

[0105] The temperature inside the fast bed reactor (1) is 500℃, the gas velocity is 2 m / s, the catalyst bed density is 150 kg / m³, the reaction gauge pressure is 0.2 MPa, and the mass hourly space velocity of the methanol feedstock (10) is 17 h⁻¹. -1 The mass hourly space velocity (MSV) of the mixed oxygen-containing aqueous solution feedstock (11) was 0.7 h⁻¹. -1 The regenerated catalyst (12) has a carbon content of 0.09% based on the total mass of the catalyst.

[0106] The methanol conversion rate was 99.9%, and the total carbon-based yield of ethylene and propylene was 84.7% by weight.

[0107]

Example 7

[0108] A fluidized bed reactor employing SAPO-34 catalyst and a cross-feed distributor includes a fast bed reactor (1), a secondary dense bed (2), an external heat exchanger (3), a circulating inclined tube (5), an external heat exchanger (6), a regeneration inclined tube (14), a pre-regeneration inclined tube (15), a methanol feed distributor (8), and a cross-feed distributor (9); wherein the circulating inclined tube (5) connects the secondary dense bed (2) and the fast bed reactor (1); the regeneration inclined tube (14) is connected to the fast bed reactor (1); the pre-regeneration inclined tube (15) is connected to the secondary dense bed (2); the external heat exchanger (6) connects the external heat exchanger (3) and the fast bed reactor (1); the methanol feed distributor (8) 8) and the cross-type feed distributor (9) are both located at the bottom of the fast bed reactor (1); the connection port between the regeneration inclined tube (14) and the fast bed reactor (1) is located directly above the cross-type feed distributor (9); the connection port between the circulation inclined tube (5) and the fast bed reactor (1) is located above the methanol feed distributor (8); the connection port between the externally removed inclined tube (6) and the fast bed reactor (1) is located above the methanol feed distributor (8); the methanol feed distributor (8) is located above the connection port between the regeneration inclined tube (14) and the fast bed reactor (1); the distance between the methanol feed distributor (8) and the cross-type feed distributor (9) is 4.5% of the total height of the fast bed reactor (1).

[0109] The mixed oxygenated compound aqueous solution feedstock (11) produced by the MTO separation unit enters the fast bed reactor (1) through the cross-type feed distributor (9) and reacts with the regenerated catalyst (12) from the regeneration inclined tube (14). The reaction products and coking catalyst rise upwards. The methanol feedstock (10) enters the fast bed reactor (1) through the methanol feedstock distributor (8) and reacts with the catalyst. The resulting olefin-rich reaction products and the spent catalyst (16) rise upwards and enter the secondary dense bed (2) for separation. The spent catalyst (16) enters the regenerator for regeneration through the spent inclined tube (15). The reaction products (13) enter the subsequent separation unit through the cyclone separator (4) to obtain the mixed oxygenated compound aqueous solution feedstock (11). The spent catalyst (16) in the secondary dense bed (2) returns to the fast bed reactor (1) through the circulating inclined tube (5). The catalyst after being heated by the external heat exchanger (3) returns to the fast bed reactor (1) through the external removal inclined tube (6).

[0110] The cross-feed distributor (9) includes: four horizontal feed distribution branches (17) and four inclined feed distribution branches (19) and a main feed pipe (18); the included angle β between the horizontal feed distribution main pipe (17) and the inclined feed distribution branches (19) is 90+α, where α is the included angle between the catalyst inclined tube (20) and the reactor; the horizontal feed distribution main pipe (17) and the inclined feed distribution branches (19) are provided with a row of small holes (21); the horizontal feed distribution branches (17) and the inclined feed distribution branches (19) are connected to the main feed pipe (18), and the mixed oxygen-containing aqueous solution raw material (11) enters from the main feed pipe (18).

[0111] The small holes (21) on the horizontal feed distribution main pipe (17) and the inclined feed distribution branch pipe (19) are arranged in a row and are opened along the reactor axis.

[0112] The small holes (21) on the horizontal feed distribution main pipe (17) and the inclined feed distribution branch pipe (19) are circular, and the small holes (21) are evenly distributed side by side, with an opening ratio of 0.13.

[0113] The diameter ratio of the horizontal feed distribution main pipe (17) to the inclined feed distribution branch pipe (19) is 1.2:1; the diameter ratio of the feed main pipe (18) to the inclined feed distribution branch pipe (19) is 0.85:1; the included angle α between the catalyst inclined tube (20) and the reactor is 30°.

[0114] The ratio of the horizontal length of the cross-type feed distributor (9) to the diameter of the fast bed reactor (1) is 0.3:1; the ratio of the distance L from the connection point of the inclined feed distribution branch (19) and the horizontal feed distribution branch (17) to the reactor wall to the horizontal length of the cross-type feed distributor (9) is 0.5:1.

[0115] The mixed oxygen-containing compound aqueous solution raw material (11) contains 10% by mass of mixed oxygen-containing compounds, which include methanol, ethanol, propanol, butanol, acetaldehyde, propionaldehyde, butyraldehyde, acetone, butanone, formic acid, acetic acid, and propionic acid. The ketone content in the mixed oxygen-containing compound is 70% by mass.

[0116] The temperature inside the fast bed reactor (1) is 475℃, the gas velocity is 1 m / s, the catalyst bed density is 200 kg / m³, the reaction gauge pressure is 0.1 MPa, and the mass hourly space velocity of the methanol feedstock (10) is 8 h⁻¹. -1 The mass hourly space velocity (MSV) of the mixed oxygen-containing aqueous solution feedstock (11) was 0.1 h⁻¹. -1 The regenerated catalyst (12) has a carbon content of less than 0.06% by total catalyst mass.

[0117] The methanol conversion rate was 99.9%, and the total carbon-based yield of ethylene and propylene was 83.9% by weight.

[0118]

Example 8

[0119] A fluidized bed reactor employing SAPO-34 catalyst and a cross-feed distributor includes a fast bed reactor (1), a secondary dense bed (2), an external heat exchanger (3), a circulating inclined tube (5), an external heat exchanger (6), a regeneration inclined tube (14), a pre-regeneration inclined tube (15), a methanol feed distributor (8), and a cross-feed distributor (9). The circulating inclined tube (5) connects the secondary dense bed (2) and the fast bed reactor (1); the regeneration inclined tube (14) is connected to the fast bed reactor (1); the pre-regeneration inclined tube (15) is connected to the secondary dense bed (2); the external heat exchanger (6) connects the external heat exchanger (3) and the fast bed reactor (1); and the methanol feed distributor... (8) and the cross-type feed distributor (9) are both located at the bottom of the fast bed reactor (1); the connection port between the regeneration inclined tube (14) and the fast bed reactor (1) is located directly above the cross-type feed distributor (9); the connection port between the circulation inclined tube (5) and the fast bed reactor (1) is located above the methanol feed distributor (8); the connection port between the externally removed inclined tube (6) and the fast bed reactor (1) is located above the methanol feed distributor (8); the methanol feed distributor (8) is located above the connection port between the regeneration inclined tube (14) and the fast bed reactor (1); the distance between the methanol feed distributor (8) and the cross-type feed distributor (9) is 4% of the total height of the fast bed reactor (1).

[0120] The mixed oxygenated compound aqueous solution feedstock (11) produced by the MTO separation unit enters the fast bed reactor (1) through the cross-type feed distributor (9) and reacts with the regenerated catalyst (12) from the regeneration inclined tube (14). The reaction products and coking catalyst rise upwards. The methanol feedstock (10) enters the fast bed reactor (1) through the methanol feedstock distributor (8) and reacts with the catalyst. The resulting olefin-rich reaction products and the spent catalyst (16) rise upwards and enter the secondary dense bed (2) for separation. The spent catalyst (16) enters the regenerator for regeneration through the spent inclined tube (15). The reaction products (13) enter the subsequent separation unit through the cyclone separator (4) to obtain the mixed oxygenated compound aqueous solution feedstock (11). The spent catalyst (16) in the secondary dense bed (2) returns to the fast bed reactor (1) through the circulating inclined tube (5). The catalyst after being heated by the external heat exchanger (3) returns to the fast bed reactor (1) through the external removal inclined tube (6).

[0121] The cross-type feed distributor (9) includes: 10 horizontal feed distribution branches (17) and 5 inclined feed distribution branches (19) and a feed main (18); the included angle β between the horizontal feed distribution main (17) and the inclined feed distribution branches (19) is 90+α, where α is the included angle between the catalyst inclined tube (20) and the reactor; the horizontal feed distribution main (17) and the inclined feed distribution branches (19) are provided with 3 rows of small holes (21); the horizontal feed distribution branches (17) and the inclined feed distribution branches (19) are connected to the feed main (18), and the mixed oxygen-containing aqueous solution raw material (11) enters from the feed main (18).

[0122] The small holes (21) on the horizontal feed distribution main pipe (17) and the inclined feed distribution branch pipe (19) are arranged in a row and are opened along the reactor axis.

[0123] The holes (21) on the horizontal feed distribution main pipe (17) and the inclined feed distribution branch pipe (19) are circular, and the holes (21) are evenly distributed side by side, with an opening ratio of 0.12.

[0124] The diameter ratio of the horizontal feed distribution main pipe (17) to the inclined feed distribution branch pipe (19) is 1.2:1; the diameter ratio of the feed main pipe (18) to the inclined feed distribution branch pipe (19) is 0.76:1; the included angle α between the catalyst inclined pipe (20) and the reactor is 70°.

[0125] The ratio of the horizontal length of the cross-type feed distributor (9) to the diameter of the fast bed reactor (1) is 0.6:1; the ratio of the distance L from the connection point of the inclined feed distribution branch (19) and the horizontal feed distribution branch (17) to the reactor wall to the horizontal length of the cross-type feed distributor (9) is 0.1:1.

[0126] The mixed oxygen-containing compound aqueous solution raw material (11) contains 60% mixed oxygen-containing compounds by mass. The mixed oxygen-containing compounds contain methanol, ethanol, propanol, butanol, acetaldehyde, propionaldehyde, butyraldehyde, acetone, butanone, formic acid, acetic acid, and propionic acid by mass. The mixed oxygen-containing compounds contain 30% ketones by mass.

[0127] The temperature inside the fast bed reactor (1) was 495℃, the gas velocity was 2.5 m / s, the catalyst bed density was 130 kg / m³, the reaction gauge pressure was 0.2 MPa, and the mass hourly space velocity (MHSV) of the methanol feedstock (10) was 25 h⁻¹. -1 The mass hourly space velocity (MSV) of the mixed oxygen-containing aqueous solution feedstock (11) was 0.2 h⁻¹. -1 The regenerated catalyst (12) has a carbon content of 0.05% based on the total mass of the catalyst.

[0128] The methanol conversion rate was 99.9%, and the total carbon-based yield of ethylene and propylene was 84.6% by weight.

[0129]

Example 9

[0130] A fluidized bed reactor employing SAPO-34 catalyst and a cross-feed distributor includes a fast bed reactor (1), a secondary dense bed (2), an external heat exchanger (3), a circulating inclined tube (5), an external heat exchanger (6), a regeneration inclined tube (14), a pre-regeneration inclined tube (15), a methanol feed distributor (8), and a cross-feed distributor (9). The circulating inclined tube (5) connects the secondary dense bed (2) and the fast bed reactor (1); the regeneration inclined tube (14) is connected to the fast bed reactor (1); the pre-regeneration inclined tube (15) is connected to the secondary dense bed (2); the external heat exchanger (6) connects the external heat exchanger (3) and the fast bed reactor (1); and the methanol feed distributor... (8) and the cross-type feed distributor (9) are both located at the bottom of the fast bed reactor (1); the connection port between the regeneration inclined tube (14) and the fast bed reactor (1) is located directly above the cross-type feed distributor (9); the connection port between the circulation inclined tube (5) and the fast bed reactor (1) is located above the methanol feed distributor (8); the connection port between the externally removed inclined tube (6) and the fast bed reactor (1) is located above the methanol feed distributor (8); the methanol feed distributor (8) is located above the connection port between the regeneration inclined tube (14) and the fast bed reactor (1); the distance between the methanol feed distributor (8) and the cross-type feed distributor (9) is 3% of the total height of the fast bed reactor (1).

[0131] The mixed oxygenated compound aqueous solution feedstock (11) produced by the MTO separation unit enters the fast bed reactor (1) through the cross-type feed distributor (9) and reacts with the regenerated catalyst (12) from the regeneration inclined tube (14). The reaction products and coking catalyst rise upwards. The methanol feedstock (10) enters the fast bed reactor (1) through the methanol feedstock distributor (8) and reacts with the catalyst. The resulting olefin-rich reaction products and the spent catalyst (16) rise upwards and enter the secondary dense bed (2) for separation. The spent catalyst (16) enters the regenerator for regeneration through the spent inclined tube (15). The reaction products (13) enter the subsequent separation unit through the cyclone separator (4) to obtain the mixed oxygenated compound aqueous solution feedstock (11). The spent catalyst (16) in the secondary dense bed (2) returns to the fast bed reactor (1) through the circulating inclined tube (5). The catalyst after being heated by the external heat exchanger (3) returns to the fast bed reactor (1) through the external removal inclined tube (6).

[0132] The cross-type feed distributor (9) includes: multiple horizontal feed distribution branches (17) and multiple inclined feed distribution branches (19) and a feed main (18); the included angle β between the horizontal feed distribution main (17) and the inclined feed distribution branches (19) is 90+α, where α is the included angle between the catalyst inclined tube (20) and the reactor; the horizontal feed distribution main (17) and the inclined feed distribution branches (19) are provided with 4 rows of small holes (21); the horizontal feed distribution branches (17) and the inclined feed distribution branches (19) are connected to the feed main (18), and the mixed oxygen-containing aqueous solution raw material (11) enters from the feed main (18).

[0133] The small holes (21) on the horizontal feed distribution main pipe (17) and the inclined feed distribution branch pipe (19) are arranged in a row and are opened along the reactor axis.

[0134] The holes (21) on the horizontal feed distribution main pipe (17) and the inclined feed distribution branch pipe (19) are circular and are evenly distributed in an alternating pattern, with an opening ratio of 0.1.

[0135] The diameter ratio of the horizontal feed distribution main pipe (17) to the inclined feed distribution branch pipe (19) is 1.3:1; the diameter ratio of the feed main pipe (18) to the inclined feed distribution branch pipe (19) is 0.5:1; the included angle α between the catalyst inclined tube (20) and the reactor is 40°.

[0136] The ratio of the horizontal length of the cross-type feed distributor (9) to the diameter of the fast bed reactor (1) is 0.4:1; the ratio of the distance L from the connection point of the inclined feed distribution branch (19) and the horizontal feed distribution branch (17) to the reactor wall to the horizontal length of the cross-type feed distributor (9) is 0.4:1.

[0137] The mixed oxygen-containing compound aqueous solution raw material (11) contains 5% by mass of mixed oxygen-containing compounds, which contain methanol, ethanol, propanol, butanol, acetaldehyde, propionaldehyde, butyraldehyde, acetone, butanone, formic acid, acetic acid, and propionic acid. The ketone content in the mixed oxygen-containing compound is 80% by mass.

[0138] The temperature inside the fast bed reactor (1) was 515℃, the gas velocity was 2.8 m / s, the catalyst bed density was 70 kg / m³, the reaction gauge pressure was 0.15 MPa, and the mass hourly space velocity (MHSV) of the methanol feedstock (10) was 12 h⁻¹. -1 The mass hourly space velocity (MSV) of the mixed oxygen-containing aqueous solution feedstock (11) was 0.3 h⁻¹. -1 The regenerated catalyst (12) has a carbon content of 0.08% based on the total mass of the catalyst.

[0139] The methanol conversion rate was 99.9%, and the total carbon-based yield of ethylene and propylene was 85.0% by weight.

[0140]

Example 10

[0141] A fluidized bed reactor employing SAPO-34 catalyst and a cross-feed distributor includes a fast bed reactor (1), a secondary dense bed (2), an external heat exchanger (3), a circulating inclined tube (5), an external heat exchanger (6), a regeneration inclined tube (14), a pre-regeneration inclined tube (15), a methanol feed distributor (8), and a cross-feed distributor (9). The circulating inclined tube (5) connects the secondary dense bed (2) and the fast bed reactor (1); the regeneration inclined tube (14) is connected to the fast bed reactor (1); the pre-regeneration inclined tube (15) is connected to the secondary dense bed (2); the external heat exchanger (6) connects the external heat exchanger (3) and the fast bed reactor (1); and the methanol feed distributor... (8) and the cross-type feed distributor (9) are both located at the bottom of the fast bed reactor (1); the connection port between the regeneration inclined tube (14) and the fast bed reactor (1) is located directly above the cross-type feed distributor (9); the connection port between the circulation inclined tube (5) and the fast bed reactor (1) is located above the methanol feed distributor (8); the connection port between the externally removed inclined tube (6) and the fast bed reactor (1) is located above the methanol feed distributor (8); the methanol feed distributor (8) is located above the connection port between the regeneration inclined tube (14) and the fast bed reactor (1); the distance between the methanol feed distributor (8) and the cross-type feed distributor (9) is 4% of the total height of the fast bed reactor (1).

[0142] The mixed oxygenated compound aqueous solution feedstock (11) produced by the MTO separation unit enters the fast bed reactor (1) through the cross-type feed distributor (9) and reacts with the regenerated catalyst (12) from the regeneration inclined tube (14). The reaction products and coking catalyst rise upwards. The methanol feedstock (10) enters the fast bed reactor (1) through the methanol feedstock distributor (8) and reacts with the catalyst. The resulting olefin-rich reaction products and the spent catalyst (16) rise upwards and enter the secondary dense bed (2) for separation. The spent catalyst (16) enters the regenerator for regeneration through the spent inclined tube (15). The reaction products (13) enter the subsequent separation unit through the cyclone separator (4) to obtain the mixed oxygenated compound aqueous solution feedstock (11). The spent catalyst (16) in the secondary dense bed (2) returns to the fast bed reactor (1) through the circulating inclined tube (5). The catalyst after being heated by the external heat exchanger (3) returns to the fast bed reactor (1) through the external removal inclined tube (6).

[0143] The cross-feed distributor (9) includes: multiple horizontal feed distribution branches (17) and multiple inclined feed distribution branches (19) and a main feed pipe (18); the included angle β between the horizontal feed distribution main pipe (17) and the inclined feed distribution branches (19) is 90+α, where α is the included angle between the catalyst inclined tube (20) and the reactor; the horizontal feed distribution main pipe (17) and the inclined feed distribution branches (19) are provided with two rows of small holes (21); the horizontal feed distribution branches (17) and the inclined feed distribution branches (19) are connected to the main feed pipe (18), and the mixed oxygen-containing aqueous solution raw material (11) enters from the main feed pipe (18).

[0144] The small holes (21) on the horizontal feed distribution main pipe (17) and the inclined feed distribution branch pipe (19) are arranged in a row and are opened along the reactor axis.

[0145] The holes (21) on the horizontal feed distribution main pipe (17) and the inclined feed distribution branch pipe (19) are circular and evenly distributed with an opening ratio of 0.13.

[0146] The diameter ratio of the horizontal feed distribution main pipe (17) to the inclined feed distribution branch pipe (19) is 0.8:1; the diameter ratio of the feed main pipe (18) to the inclined feed distribution branch pipe (19) is 0.5:1; the included angle α between the catalyst inclined pipe (20) and the reactor is 40°.

[0147] The ratio of the horizontal length of the cross-type feed distributor (9) to the diameter of the fast bed reactor (1) is 0.4:1; the ratio of the distance L from the connection point of the inclined feed distribution branch (19) and the horizontal feed distribution branch (17) to the reactor wall to the horizontal length of the cross-type feed distributor (9) is 0.4:1.

[0148] The mixed oxygen-containing compound aqueous solution raw material (11) contains 70% mixed oxygen-containing compounds by mass. The mixed oxygen-containing compounds contain methanol, ethanol, propanol, butanol, acetaldehyde, propionaldehyde, butyraldehyde, acetone, butanone, formic acid, acetic acid, and propionic acid by mass. The mixed oxygen-containing compounds contain 30% ketones by mass.

[0149] The temperature inside the fast bed reactor (1) was 505℃, the gas velocity was 2.7 m / s, the catalyst bed density was 90 kg / m³, the reaction gauge pressure was 0.15 MPa, and the mass hourly space velocity (MHSV) of the methanol feedstock (10) was 12 h⁻¹. -1 The mass hourly space velocity (MSV) of the mixed oxygen-containing aqueous solution feedstock (11) was 0.7 h⁻¹. -1 The regenerated catalyst (12) has a carbon content of 0.08% based on the total mass of the catalyst.

[0150] The methanol conversion rate was 99.9%, and the total carbon-based yield of ethylene and propylene was 84.6% by weight.

[0151]

Example 11

[0152] A fluidized bed reactor employing SAPO-34 catalyst and a cross-feed distributor includes a fast bed reactor (1), a secondary dense bed (2), an external heat exchanger (3), a circulating inclined tube (5), an external heat exchanger (6), a regeneration inclined tube (14), a pre-regeneration inclined tube (15), a methanol feed distributor (8), and a cross-feed distributor (9). The circulating inclined tube (5) connects the secondary dense bed (2) and the fast bed reactor (1); the regeneration inclined tube (14) is connected to the fast bed reactor (1); the pre-regeneration inclined tube (15) is connected to the secondary dense bed (2); the external heat exchanger (6) connects the external heat exchanger (3) and the fast bed reactor (1); and the methanol feed distributor... (8) and the cross-type feed distributor (9) are both located at the bottom of the fast bed reactor (1); the connection port between the regeneration inclined tube (14) and the fast bed reactor (1) is located directly above the cross-type feed distributor (9); the connection port between the circulation inclined tube (5) and the fast bed reactor (1) is located above the methanol feed distributor (8); the connection port between the externally removed inclined tube (6) and the fast bed reactor (1) is located above the methanol feed distributor (8); the methanol feed distributor (8) is located above the connection port between the regeneration inclined tube (14) and the fast bed reactor (1); the distance between the methanol feed distributor (8) and the cross-type feed distributor (9) is 2% of the total height of the fast bed reactor (1).

[0153] The mixed oxygenated compound aqueous solution feedstock (11) produced by the MTO separation unit enters the fast bed reactor (1) through the cross-type feed distributor (9) and reacts with the regenerated catalyst (12) from the regeneration inclined tube (14). The reaction products and coking catalyst rise upwards. The methanol feedstock (10) enters the fast bed reactor (1) through the methanol feedstock distributor (8) and reacts with the catalyst. The resulting olefin-rich reaction products and the spent catalyst (16) rise upwards and enter the secondary dense bed (2) for separation. The spent catalyst (16) enters the regenerator for regeneration through the spent inclined tube (15). The reaction products (13) enter the subsequent separation unit through the cyclone separator (4) to obtain the mixed oxygenated compound aqueous solution feedstock (11). The spent catalyst (16) in the secondary dense bed (2) returns to the fast bed reactor (1) through the circulating inclined tube (5). The catalyst after being heated by the external heat exchanger (3) returns to the fast bed reactor (1) through the external removal inclined tube (6).

[0154] The cross-feed distributor (9) includes: multiple horizontal feed distribution branches (17) and multiple inclined feed distribution branches (19) and a main feed pipe (18); the included angle β between the horizontal feed distribution main pipe (17) and the inclined feed distribution branches (19) is 90+α, where α is the included angle between the catalyst inclined tube (20) and the reactor; the horizontal feed distribution main pipe (17) and the inclined feed distribution branches (19) are provided with two rows of small holes (21); the horizontal feed distribution branches (17) and the inclined feed distribution branches (19) are connected to the main feed pipe (18), and the mixed oxygen-containing aqueous solution raw material (11) enters from the main feed pipe (18).

[0155] The small holes (21) on the horizontal feed distribution main pipe (17) and the inclined feed distribution branch pipe (19) are arranged in a row and are opened along the reactor axis.

[0156] The holes (21) on the horizontal feed distribution main pipe (17) and the inclined feed distribution branch pipe (19) are circular and evenly distributed with an opening ratio of 0.13.

[0157] The diameter ratio of the horizontal feed distribution main pipe (17) to the inclined feed distribution branch pipe (19) is 1:1; the diameter ratio of the feed main pipe (18) to the inclined feed distribution branch pipe (19) is 0.9:1; the included angle α between the catalyst inclined pipe (20) and the reactor is 50°.

[0158] The ratio of the horizontal length of the cross-type feed distributor (9) to the diameter of the fast bed reactor (1) is 0.45:1; the ratio of the distance L from the connection point of the inclined feed distribution branch (19) and the horizontal feed distribution branch (17) to the reactor wall to the horizontal length of the cross-type feed distributor (9) is 0.3:1.

[0159] The mass percentage of mixed oxygen-containing compounds in the mixed oxygen-containing aqueous solution raw material (11) is 40%. The mixed oxygen-containing compounds contain methanol, ethanol, propanol, butanol, acetaldehyde, propionaldehyde, butyraldehyde, acetone, butanone, formic acid, acetic acid, and propionic acid. The mass percentage of ketones in the mixed oxygen-containing compounds is 40%.

[0160] The temperature inside the fast bed reactor (1) is 450℃, the gas velocity is 0.5 m / s, the catalyst bed density is 200 kg / m³, the reaction gauge pressure is 0 MPa, and the mass hourly space velocity of the methanol feedstock (10) is 3 h⁻¹. -1 The mass hourly space velocity (MSV) of the mixed oxygen-containing aqueous solution feedstock (11) was 0.05 h⁻¹. -1 The regenerated catalyst (12) has a carbon content of 0.05% based on the total mass of the catalyst.

[0161] The methanol conversion rate was 99.9%, and the total carbon-based yield of ethylene and propylene was 82.5% by weight.

[0162]

Example 12

[0163] A fluidized bed reactor employing SAPO-34 catalyst and a cross-feed distributor includes a fast bed reactor (1), a secondary dense bed (2), an external heat exchanger (3), a circulating inclined tube (5), an external heat exchanger (6), a regeneration inclined tube (14), a pre-regeneration inclined tube (15), a methanol feed distributor (8), and a cross-feed distributor (9); wherein the circulating inclined tube (5) connects the secondary dense bed (2) and the fast bed reactor (1); the regeneration inclined tube (14) is connected to the fast bed reactor (1); the pre-regeneration inclined tube (15) is connected to the secondary dense bed (2); the external heat exchanger (6) connects the external heat exchanger (3) and the fast bed reactor (1); the methanol feed distributor (8) 8) and the cross-type feed distributor (9) are both located at the bottom of the fast bed reactor (1); the connection port between the regeneration inclined tube (14) and the fast bed reactor (1) is located directly above the cross-type feed distributor (9); the connection port between the circulation inclined tube (5) and the fast bed reactor (1) is located above the methanol feed distributor (8); the connection port between the externally removed inclined tube (6) and the fast bed reactor (1) is located above the methanol feed distributor (8); the methanol feed distributor (8) is located above the connection port between the regeneration inclined tube (14) and the fast bed reactor (1); the distance between the methanol feed distributor (8) and the cross-type feed distributor (9) is 3.5% of the total height of the fast bed reactor (1).

[0164] The mixed oxygenated compound aqueous solution feedstock (11) produced by the MTO separation unit enters the fast bed reactor (1) through the cross-type feed distributor (9) and reacts with the regenerated catalyst (12) from the regeneration inclined tube (14). The reaction products and coking catalyst rise upwards. The methanol feedstock (10) enters the fast bed reactor (1) through the methanol feedstock distributor (8) and reacts with the catalyst. The resulting olefin-rich reaction products and the spent catalyst (16) rise upwards and enter the secondary dense bed (2) for separation. The spent catalyst (16) enters the regenerator for regeneration through the spent inclined tube (15). The reaction products (13) enter the subsequent separation unit through the cyclone separator (4) to obtain the mixed oxygenated compound aqueous solution feedstock (11). The spent catalyst (16) in the secondary dense bed (2) returns to the fast bed reactor (1) through the circulating inclined tube (5). The catalyst after being heated by the external heat exchanger (3) returns to the fast bed reactor (1) through the external removal inclined tube (6).

[0165] The cross-feed distributor (9) includes: multiple horizontal feed distribution branches (17) and multiple inclined feed distribution branches (19) and a main feed pipe (18); the included angle β between the horizontal feed distribution main pipe (17) and the inclined feed distribution branches (19) is 90+α, where α is the included angle between the catalyst inclined tube (20) and the reactor; the horizontal feed distribution main pipe (17) and the inclined feed distribution branches (19) are provided with two rows of small holes (21); the horizontal feed distribution branches (17) and the inclined feed distribution branches (19) are connected to the main feed pipe (18), and the mixed oxygen-containing aqueous solution raw material (11) enters from the main feed pipe (18).

[0166] The small holes (21) on the horizontal feed distribution main pipe (17) and the inclined feed distribution branch pipe (19) are arranged in a row and are opened along the reactor axis.

[0167] The holes (21) on the horizontal feed distribution main pipe (17) and the inclined feed distribution branch pipe (19) are circular and evenly distributed with an opening ratio of 0.13.

[0168] The diameter ratio of the horizontal feed distribution main pipe (17) to the inclined feed distribution branch pipe (19) is 0.5:1; the diameter ratio of the feed main pipe (18) to the inclined feed distribution branch pipe (19) is 0.6:1; the included angle α between the catalyst inclined pipe (20) and the reactor is 50°.

[0169] The ratio of the horizontal length of the cross-type feed distributor (9) to the diameter of the fast bed reactor (1) is 0.45:1; the ratio of the distance L from the connection point of the inclined feed distribution branch (19) and the horizontal feed distribution branch (17) to the reactor wall to the horizontal length of the cross-type feed distributor (9) is 0.3:1.

[0170] The mass percentage of mixed oxygen-containing compounds in the mixed oxygen-containing aqueous solution raw material (11) is 40%. The mixed oxygen-containing compounds contain methanol, ethanol, propanol, butanol, acetaldehyde, propionaldehyde, butyraldehyde, acetone, butanone, formic acid, acetic acid, and propionic acid. The mass percentage of ketones in the mixed oxygen-containing compounds is 40%.

[0171] The temperature inside the fast bed reactor (1) is 520℃, the gas velocity is 3 m / s, the catalyst bed density is 30 kg / m³, the reaction gauge pressure is 0.4 MPa, and the mass hourly space velocity of the methanol feedstock (10) is 30 h⁻¹. -1 The mass hourly space velocity (MSV) of the mixed oxygen-containing aqueous solution feedstock (11) is 1 hour. -1 The regenerated catalyst (12) has a carbon content of 0.09% based on the total mass of the catalyst.

[0172] The methanol conversion rate was 99.9%, and the total carbon-based yield of ethylene and propylene was 84.7% by weight.

[0173] Comparative Example 1

[0174] A fluidized bed reactor employing SAPO-34 catalyst and a cross-feed distributor includes a fast bed reactor (1), a secondary dense bed (2), an external heat exchanger (3), a circulating inclined tube (5), an external heat exchanger (6), a regeneration inclined tube (14), a pre-regeneration inclined tube (15), a methanol feed distributor (8), and a cross-feed distributor (9); wherein the circulating inclined tube (5) connects the secondary dense bed (2) and the fast bed reactor (1); the regeneration inclined tube (14) is connected to the fast bed reactor (1); the pre-regeneration inclined tube (15) is connected to the secondary dense bed (2); the external heat exchanger (6) connects the external heat exchanger (3) and the fast bed reactor (1); the methanol feed distributor (8) 8) and the cross-type feed distributor (9) are both located at the bottom of the fast bed reactor (1); the connection port between the regeneration inclined tube (14) and the fast bed reactor (1) is located directly above the cross-type feed distributor (9); the connection port between the circulation inclined tube (5) and the fast bed reactor (1) is located above the methanol feed distributor (8); the connection port between the externally removed inclined tube (6) and the fast bed reactor (1) is located above the methanol feed distributor (8); the methanol feed distributor (8) is located above the connection port between the regeneration inclined tube (14) and the fast bed reactor (1); the distance between the methanol feed distributor (8) and the cross-type feed distributor (9) is 0.5% of the total height of the fast bed reactor (1).

[0175] The mixed oxygenated compound aqueous solution feedstock (11) produced by the MTO separation unit enters the fast bed reactor (1) through the cross-type feed distributor (9) and reacts with the regenerated catalyst (12) from the regeneration inclined tube (14). The reaction products and coking catalyst rise upwards. The methanol feedstock (10) enters the fast bed reactor (1) through the methanol feedstock distributor (8) and reacts with the catalyst. The resulting olefin-rich reaction products and the spent catalyst (16) rise upwards and enter the secondary dense bed (2) for separation. The spent catalyst (16) enters the regenerator for regeneration through the spent inclined tube (15). The reaction products (13) enter the subsequent separation unit through the cyclone separator (4) to obtain the mixed oxygenated compound aqueous solution feedstock (11). The spent catalyst (16) in the secondary dense bed (2) returns to the fast bed reactor (1) through the circulating inclined tube (5). The catalyst after being heated by the external heat exchanger (3) returns to the fast bed reactor (1) through the external removal inclined tube (6).

[0176] The cross-feed distributor (9) includes: multiple horizontal feed distribution branches (17) and multiple inclined feed distribution branches (19) and a main feed pipe (18); the included angle β between the horizontal feed distribution main pipe (17) and the inclined feed distribution branches (19) is 90+α, where α is the included angle between the catalyst inclined tube (20) and the reactor; the horizontal feed distribution main pipe (17) and the inclined feed distribution branches (19) are provided with two rows of small holes (21); the horizontal feed distribution branches (17) and the inclined feed distribution branches (19) are connected to the main feed pipe (18), and the mixed oxygen-containing aqueous solution raw material (11) enters from the main feed pipe (18).

[0177] The small holes (21) on the horizontal feed distribution main pipe (17) and the inclined feed distribution branch pipe (19) are arranged in a row and are opened along the reactor axis.

[0178] The holes (21) on the horizontal feed distribution main pipe (17) and the inclined feed distribution branch pipe (19) are circular and evenly distributed with an opening ratio of 0.03.

[0179] The diameter ratio of the horizontal feed distribution main pipe (17) to the inclined feed distribution branch pipe (19) is 1.8:1; the diameter ratio of the feed main pipe (18) to the inclined feed distribution branch pipe (19) is 1.2:1; the included angle α between the catalyst inclined pipe (20) and the reactor is 20°.

[0180] The ratio of the horizontal length of the cross-type feed distributor (9) to the diameter of the fast bed reactor (1) is 0.2:1; the ratio of the distance L from the connection point of the inclined feed distribution branch (19) and the horizontal feed distribution branch (17) to the reactor wall to the horizontal length of the cross-type feed distributor (9) is 0.05:1.

[0181] The mass percentage of mixed oxygen-containing compounds in the mixed oxygen-containing aqueous solution raw material (11) is 3%. The mixed oxygen-containing compounds contain methanol, ethanol, propanol, butanol, acetaldehyde, propionaldehyde, butyraldehyde, acetone, butanone, formic acid, acetic acid, and propionic acid. The mass percentage of ketones in the mixed oxygen-containing compounds is 85%.

[0182] The temperature inside the fast bed reactor (1) is 480℃, the gas velocity is 2 m / s, the catalyst bed density is 150 kg / m³, the reaction gauge pressure is 0.18 MPa, and the mass hourly space velocity of the methanol feedstock (10) is 12 h⁻¹. -1 The mass hourly space velocity (MSV) of the mixed oxygen-containing aqueous solution feedstock (11) was 0.3 h⁻¹. -1 The regenerated catalyst (12) has a carbon content of 0.05% based on the total mass of the catalyst.

[0183] The methanol conversion rate was 99.9%, and the total carbon-based yield of ethylene and propylene was 80.1% by weight.

[0184] Comparative Example 2

[0185] A fluidized bed reactor employing SAPO-34 catalyst and a cross-feed distributor includes a fast bed reactor (1), a secondary dense bed (2), an external heat exchanger (3), a circulating inclined tube (5), an external heat exchanger (6), a regeneration inclined tube (14), a pre-regeneration inclined tube (15), a methanol feed distributor (8), and a cross-feed distributor (9). The circulating inclined tube (5) connects the secondary dense bed (2) and the fast bed reactor (1); the regeneration inclined tube (14) is connected to the fast bed reactor (1); the pre-regeneration inclined tube (15) is connected to the secondary dense bed (2); the external heat exchanger (6) connects the external heat exchanger (3) and the fast bed reactor (1); and the methanol feed distributor... (8) and the cross-type feed distributor (9) are both located at the bottom of the fast bed reactor (1); the connection port between the regeneration inclined tube (14) and the fast bed reactor (1) is located directly above the cross-type feed distributor (9); the connection port between the circulation inclined tube (5) and the fast bed reactor (1) is located above the methanol feed distributor (8); the connection port between the externally removed inclined tube (6) and the fast bed reactor (1) is located above the methanol feed distributor (8); the methanol feed distributor (8) is located above the connection port between the regeneration inclined tube (14) and the fast bed reactor (1); the distance between the methanol feed distributor (8) and the cross-type feed distributor (9) is 8% of the total height of the fast bed reactor (1).

[0186] The mixed oxygenated compound aqueous solution feedstock (11) produced by the MTO separation unit enters the fast bed reactor (1) through the cross-type feed distributor (9) and reacts with the regenerated catalyst (12) from the regeneration inclined tube (14). The reaction products and coking catalyst rise upwards. The methanol feedstock (10) enters the fast bed reactor (1) through the methanol feedstock distributor (8) and reacts with the catalyst. The resulting olefin-rich reaction products and the spent catalyst (16) rise upwards and enter the secondary dense bed (2) for separation. The spent catalyst (16) enters the regenerator for regeneration through the spent inclined tube (15). The reaction products (13) enter the subsequent separation unit through the cyclone separator (4) to obtain the mixed oxygenated compound aqueous solution feedstock (11). The spent catalyst (16) in the secondary dense bed (2) returns to the fast bed reactor (1) through the circulating inclined tube (5). The catalyst after being heated by the external heat exchanger (3) returns to the fast bed reactor (1) through the external removal inclined tube (6).

[0187] The cross-feed distributor (9) includes: multiple horizontal feed distribution branches (17) and multiple inclined feed distribution branches (19) and a main feed pipe (18); the included angle β between the horizontal feed distribution main pipe (17) and the inclined feed distribution branches (19) is 90+α, where α is the included angle between the catalyst inclined tube (20) and the reactor; the horizontal feed distribution main pipe (17) and the inclined feed distribution branches (19) are provided with two rows of small holes (21); the horizontal feed distribution branches (17) and the inclined feed distribution branches (19) are connected to the main feed pipe (18), and the mixed oxygen-containing aqueous solution raw material (11) enters from the main feed pipe (18).

[0188] The small holes (21) on the horizontal feed distribution main pipe (17) and the inclined feed distribution branch pipe (19) are arranged in a row and are opened along the reactor axis.

[0189] The holes (21) on the horizontal feed distribution main pipe (17) and the inclined feed distribution branch pipe (19) are circular and evenly distributed with an opening ratio of 0.3.

[0190] The diameter ratio of the horizontal feed distribution main pipe (17) to the inclined feed distribution branch pipe (19) is 0.4:1; the diameter ratio of the feed main pipe (18) to the inclined feed distribution branch pipe (19) is 0.4:1; the included angle α between the catalyst inclined pipe (20) and the reactor is 80°.

[0191] The ratio of the horizontal length of the cross-type feed distributor (9) to the diameter of the fast bed reactor (1) is 0.7:1; the ratio of the distance L from the connection point of the inclined feed distribution branch (19) and the horizontal feed distribution branch (17) to the reactor wall to the horizontal length of the cross-type feed distributor (9) is 0.55:1.

[0192] The mixed oxygen-containing compound aqueous solution raw material (11) contains 75% mixed oxygen-containing compounds by mass. The mixed oxygen-containing compounds contain methanol, ethanol, propanol, butanol, acetaldehyde, propionaldehyde, butyraldehyde, acetone, butanone, formic acid, acetic acid, and propionic acid by mass. The mixed oxygen-containing compounds contain 20% ketones by mass.

[0193] The temperature inside the fast bed reactor (1) was 495℃, the gas velocity was 2.5 m / s, the catalyst bed density was 130 kg / m³, the reaction gauge pressure was 0.2 MPa, and the mass hourly space velocity (MHSV) of the methanol feedstock (10) was 25 h⁻¹. -1 The mass hourly space velocity (MSV) of the mixed oxygen-containing aqueous solution feedstock (11) was 0.2 h⁻¹. -1 The regenerated catalyst (12) has a carbon content of 0.08% based on the total mass of the catalyst.

[0194] The methanol conversion rate was 99.9%, and the total carbon-based yield of ethylene and propylene was 81.2% by weight.

[0195] Comparative Example 3

[0196] A fluidized bed reactor employing SAPO-34 catalyst and a cross-feed distributor includes a fast bed reactor (1), a secondary dense bed (2), an external heat exchanger (3), a circulating inclined tube (5), an external heat exchanger (6), a regeneration inclined tube (14), a pre-regeneration inclined tube (15), a methanol feed distributor (8), and a cross-feed distributor (9). The circulating inclined tube (5) connects the secondary dense bed (2) and the fast bed reactor (1); the regeneration inclined tube (14) is connected to the fast bed reactor (1); the pre-regeneration inclined tube (15) is connected to the secondary dense bed (2); the external heat exchanger (6) connects the external heat exchanger (3) and the fast bed reactor (1); and the methanol feed distributor... (8) and the cross-type feed distributor (9) are both located at the bottom of the fast bed reactor (1); the connection port between the regeneration inclined tube (14) and the fast bed reactor (1) is located directly above the cross-type feed distributor (9); the connection port between the circulation inclined tube (5) and the fast bed reactor (1) is located above the methanol feed distributor (8); the connection port between the externally removed inclined tube (6) and the fast bed reactor (1) is located above the methanol feed distributor (8); the methanol feed distributor (8) is located above the connection port between the regeneration inclined tube (14) and the fast bed reactor (1); the distance between the methanol feed distributor (8) and the cross-type feed distributor (9) is 4% of the total height of the fast bed reactor (1).

[0197] The mixed oxygenated compound aqueous solution feedstock (11) produced by the MTO separation unit enters the fast bed reactor (1) through the cross-type feed distributor (9) and reacts with the regenerated catalyst (12) from the regeneration inclined tube (14). The reaction products and coking catalyst rise upwards. The methanol feedstock (10) enters the fast bed reactor (1) through the methanol feedstock distributor (8) and reacts with the catalyst. The resulting olefin-rich reaction products and the spent catalyst (16) rise upwards and enter the secondary dense bed (2) for separation. The spent catalyst (16) enters the regenerator for regeneration through the spent inclined tube (15). The reaction products (13) enter the subsequent separation unit through the cyclone separator (4) to obtain the mixed oxygenated compound aqueous solution feedstock (11). The spent catalyst (16) in the secondary dense bed (2) returns to the fast bed reactor (1) through the circulating inclined tube (5). The catalyst after being heated by the external heat exchanger (3) returns to the fast bed reactor (1) through the external removal inclined tube (6).

[0198] The cross-feed distributor (9) includes: multiple horizontal feed distribution branches (17) and multiple inclined feed distribution branches (19) and a main feed pipe (18); the included angle β between the horizontal feed distribution main pipe (17) and the inclined feed distribution branches (19) is 90+α, where α is the included angle between the catalyst inclined tube (20) and the reactor; the horizontal feed distribution main pipe (17) and the inclined feed distribution branches (19) are provided with two rows of small holes (21); the horizontal feed distribution branches (17) and the inclined feed distribution branches (19) are connected to the main feed pipe (18), and the mixed oxygen-containing aqueous solution raw material (11) enters from the main feed pipe (18).

[0199] The small holes (21) on the horizontal feed distribution main pipe (17) and the inclined feed distribution branch pipe (19) are arranged in a row and are opened along the reactor axis.

[0200] The holes (21) on the horizontal feed distribution main pipe (17) and the inclined feed distribution branch pipe (19) are circular and evenly distributed with an opening ratio of 0.13.

[0201] The diameter ratio of the horizontal feed distribution main pipe (17) to the inclined feed distribution branch pipe (19) is 0.8:1; the diameter ratio of the feed main pipe (18) to the inclined feed distribution branch pipe (19) is 0.5:1; the included angle α between the catalyst inclined pipe (20) and the reactor is 40°.

[0202] The ratio of the horizontal length of the cross-type feed distributor (9) to the diameter of the fast bed reactor (1) is 0.4:1; the ratio of the distance L from the connection point of the inclined feed distribution branch (19) and the horizontal feed distribution branch (17) to the reactor wall to the horizontal length of the cross-type feed distributor (9) is 0.4:1.

[0203] The mixed oxygen-containing compound aqueous solution raw material (11) contains 70% mixed oxygen-containing compounds by mass. The mixed oxygen-containing compounds contain methanol, ethanol, propanol, butanol, acetaldehyde, propionaldehyde, butyraldehyde, acetone, butanone, formic acid, acetic acid, and propionic acid by mass. The mixed oxygen-containing compounds contain 30% ketones by mass.

[0204] The temperature inside the fast bed reactor (1) was 440℃, the gas velocity was 0.4 m / s, the catalyst bed density was 20 kg / m³, the reaction gauge pressure was 0 MPa, and the mass hourly space velocity of the methanol feedstock (10) was 2 h⁻¹. -1 The mass hourly space velocity (MSV) of the mixed oxygen-containing aqueous solution feedstock (11) was 0.02 h⁻¹. -1 The regenerated catalyst (12) has a carbon content of 0.05% based on the total mass of the catalyst.

[0205] The methanol conversion rate was 99.9%, and the total carbon-based yield of ethylene and propylene was 75.9% by weight.

[0206] Comparative Example 4

[0207] A fluidized bed reactor employing SAPO-34 catalyst and a cross-feed distributor includes a fast bed reactor (1), a secondary dense bed (2), an external heat exchanger (3), a circulating inclined tube (5), an external heat exchanger (6), a regeneration inclined tube (14), a pre-regeneration inclined tube (15), a methanol feed distributor (8), and a cross-feed distributor (9); wherein the circulating inclined tube (5) connects the secondary dense bed (2) and the fast bed reactor (1); the regeneration inclined tube (14) is connected to the fast bed reactor (1); the pre-regeneration inclined tube (15) is connected to the secondary dense bed (2); the external heat exchanger (6) connects the external heat exchanger (3) and the fast bed reactor (1); the methanol feed distributor (8) 8) and the cross-type feed distributor (9) are both located at the bottom of the fast bed reactor (1); the connection port between the regeneration inclined tube (14) and the fast bed reactor (1) is located directly above the cross-type feed distributor (9); the connection port between the circulation inclined tube (5) and the fast bed reactor (1) is located above the methanol feed distributor (8); the connection port between the externally removed inclined tube (6) and the fast bed reactor (1) is located above the methanol feed distributor (8); the methanol feed distributor (8) is located above the connection port between the regeneration inclined tube (14) and the fast bed reactor (1); the distance between the methanol feed distributor (8) and the cross-type feed distributor (9) is 3.5% of the total height of the fast bed reactor (1).

[0208] The mixed oxygenated compound aqueous solution feedstock (11) produced by the MTO separation unit enters the fast bed reactor (1) through the cross-type feed distributor (9) and reacts with the regenerated catalyst (12) from the regeneration inclined tube (14). The reaction products and coking catalyst rise upwards. The methanol feedstock (10) enters the fast bed reactor (1) through the methanol feedstock distributor (8) and reacts with the catalyst. The resulting olefin-rich reaction products and the spent catalyst (16) rise upwards and enter the secondary dense bed (2) for separation. The spent catalyst (16) enters the regenerator for regeneration through the spent inclined tube (15). The reaction products (13) enter the subsequent separation unit through the cyclone separator (4) to obtain the mixed oxygenated compound aqueous solution feedstock (11). The spent catalyst (16) in the secondary dense bed (2) returns to the fast bed reactor (1) through the circulating inclined tube (5). The catalyst after being heated by the external heat exchanger (3) returns to the fast bed reactor (1) through the external removal inclined tube (6).

[0209] The cross-feed distributor (9) includes: multiple horizontal feed distribution branches (17) and multiple inclined feed distribution branches (19) and a main feed pipe (18); the included angle β between the horizontal feed distribution main pipe (17) and the inclined feed distribution branches (19) is 90+α, where α is the included angle between the catalyst inclined tube (20) and the reactor; the horizontal feed distribution main pipe (17) and the inclined feed distribution branches (19) are provided with two rows of small holes (21); the horizontal feed distribution branches (17) and the inclined feed distribution branches (19) are connected to the main feed pipe (18), and the mixed oxygen-containing aqueous solution raw material (11) enters from the main feed pipe (18).

[0210] The small holes (21) on the horizontal feed distribution main pipe (17) and the inclined feed distribution branch pipe (19) are arranged in a row and are opened along the reactor axis.

[0211] The holes (21) on the horizontal feed distribution main pipe (17) and the inclined feed distribution branch pipe (19) are circular and evenly distributed with an opening ratio of 0.2.

[0212] The diameter ratio of the horizontal feed distribution main pipe (17) to the inclined feed distribution branch pipe (19) is 1:1; the diameter ratio of the feed main pipe (18) to the inclined feed distribution branch pipe (19) is 0.5:1; the included angle α between the catalyst inclined pipe (20) and the reactor is 50°.

[0213] The ratio of the horizontal length of the cross-type feed distributor (9) to the diameter of the fast bed reactor (1) is 0.42:1; the ratio of the distance L from the connection point of the inclined feed distribution branch (19) and the horizontal feed distribution branch (17) to the reactor wall to the horizontal length of the cross-type feed distributor (9) is 0.35:1.

[0214] The mixed oxygen-containing compound aqueous solution raw material (11) contains 50% by mass of mixed oxygen-containing compounds, which include methanol, ethanol, propanol, butanol, acetaldehyde, propionaldehyde, butyraldehyde, acetone, butanone, formic acid, acetic acid, and propionic acid. The ketone content in the mixed oxygen-containing compound is 35% by mass.

[0215] The temperature inside the fast bed reactor (1) was 530℃, the gas velocity was 3.2 m / s, the catalyst bed density was 250 kg / m³, the reaction gauge pressure was 0.5 MPa, and the mass hourly space velocity (MHSV) of the methanol feedstock (10) was 35 h⁻¹. -1 The mass hourly space velocity (MSV) of the mixed oxygen-containing aqueous solution feedstock (11) was 1.2 h⁻¹. -1 The regenerated catalyst (12) has a carbon content of 0.2% based on the total mass of the catalyst.

[0216] The methanol conversion rate was 99.9%, and the total carbon-based yield of ethylene and propylene was 78.3% by weight.

[0217] Comparative Example 5

[0218] A fluidized bed reactor employing SAPO-34 catalyst and a cross-type feed distributor includes a fast bed reactor (1), a secondary dense bed (2), an external heat exchanger (3), a circulating inclined tube (5), an external feed down inclined tube (6), a regeneration inclined tube (14), a pre-regeneration inclined tube (15), a methanol feed distributor (8), and a horizontal feed distributor; wherein the circulating inclined tube (5) connects the secondary dense bed (2) and the fast bed reactor (1); the regeneration inclined tube (14) is connected to the fast bed reactor (1); the pre-regeneration inclined tube (15) is connected to the secondary dense bed (2); the external feed down inclined tube (6) connects the external heat exchanger (3) and the fast bed reactor (1); the methanol feed down inclined tube (6) connects the secondary dense bed reactor (2) and the external heat exchanger (3 ... The feed distributor (8) and the horizontal feed distributor are both located at the bottom of the fast bed reactor (1); the connection port between the regeneration inclined tube (14) and the fast bed reactor (1) is located directly above the horizontal feed distributor; the connection port between the circulation inclined tube (5) and the fast bed reactor (1) is located above the methanol feed distributor (8); the connection port between the externally removed inclined tube (6) and the fast bed reactor (1) is located above the methanol feed distributor (8); the methanol feed distributor (8) is located above the connection port between the regeneration inclined tube (14) and the fast bed reactor (1); the distance between the methanol feed distributor (8) and the horizontal feed distributor is 4% of the total height of the fast bed reactor (1).

[0219] The mixed oxygen-containing aqueous solution feedstock (11) produced by the MTO separation unit enters the fast bed reactor (1) via a horizontal feed distributor and reacts with the regenerated catalyst (12) via the regeneration inclined tube (14). The reaction products and coking catalyst rise upwards. The methanol feedstock (10) enters the fast bed reactor (1) via a methanol feedstock distributor (8) and reacts with the catalyst. The resulting olefin-rich reaction products and the spent catalyst (16) rise upwards and enter the secondary dense bed (2) for separation. The spent catalyst (16) enters the regenerator via the spent inclined tube (15) for regeneration. The reaction products (13) enter the subsequent separation unit via a cyclone separator (4) to obtain the mixed oxygen-containing aqueous solution feedstock (11). The spent catalyst (16) in the secondary dense bed (2) returns to the fast bed reactor (1) via the circulating inclined tube (5). The catalyst, after being heated by the external heat exchanger (3), returns to the fast bed reactor (1) via the external removal inclined tube (6).

[0220] The horizontal feed distributor has a row of holes (21) along the reactor axis. The holes (21) are circular and evenly distributed, with an opening ratio of 0.15. The angle α between the catalyst inclined tube (20) and the reactor is 60°.

[0221] The ratio of the horizontal length of the horizontal feed distributor to the diameter of the fast bed reactor (1) is 0.55:1.

[0222] The mixed oxygen-containing compound aqueous solution raw material (11) contains 20% mixed oxygen-containing compounds by mass, and the mixed oxygen-containing compounds contain methanol, ethanol, propanol, butanol, acetaldehyde, propionaldehyde, butyraldehyde, acetone, butanone, formic acid, acetic acid, and propionic acid by mass. The mixed oxygen-containing compounds contain 70% ketones by mass.

[0223] The temperature inside the fast bed reactor (1) is 500℃, the gas velocity is 2 m / s, the catalyst bed density is 150 kg / m³, the reaction gauge pressure is 0.2 MPa, and the mass hourly space velocity of the methanol feedstock (10) is 17 h⁻¹. -1 The mass hourly space velocity (MSV) of the mixed oxygen-containing aqueous solution feedstock (11) was 0.7 h⁻¹. -1 The regenerated catalyst (12) has a carbon content of 0.09% based on the total mass of the catalyst.

[0224] The methanol conversion rate was 99.9%, and the total carbon-based yield of ethylene and propylene was 79.8% by weight.

[0225]

Example 13

[0226] The only difference from Example 1 is that in the fluidized bed reactor, the distance between the methanol feed distributor (8) and the cross-feed distributor (9) is 0.5% of the total height of the fast bed reactor (1). After the reaction, the methanol conversion rate was 99.4%, and the total yield of ethylene and propylene carbon-based products was 80.5% by weight.

[0227]

Example 14

[0228] The only difference from Example 1 is that in the fluidized bed reactor, the distance between the methanol feed distributor (8) and the cross-feed distributor (9) is 8% of the total height of the fast bed reactor (1). After the reaction, the methanol conversion rate was 98.3%, and the total yield of ethylene and propylene carbon-based products was 78.3% by weight.

[0229]

Example 15

[0230] The only difference between this example and Example 1 is that the fluidized bed reactor has an opening ratio of 0.03. After the reaction, the methanol conversion rate was 99.1%, and the total yield of ethylene and propylene carbon-based products was 79.6% by weight.

[0231]

Example 16

[0232] The only difference between this example and Example 1 is that the fluidized bed reactor has an opening ratio of 0.3. After the reaction, the methanol conversion rate was 99.5%, and the total carbon-based yield of ethylene and propylene was 81.8% by weight.

[0233]

Example 17

[0234] The only difference between this example and Example 1 is that in the fluidized bed reactor, the diameter ratio of the horizontal feed distribution main pipe (17) and the inclined feed distribution branch pipe (19) is 0.4. After the reaction, the methanol conversion rate was 98.7%, and the total carbon-based yield of ethylene and propylene was 82.0% by weight.

[0235]

Example 18

[0236] The only difference between this example and Example 1 is that in the fluidized bed reactor, the diameter ratio of the horizontal feed distribution main pipe (17) and the inclined feed distribution branch pipe (19) is 1.8. After the reaction, the methanol conversion rate was 99.6%, and the total carbon-based yield of ethylene and propylene was 80.8% by weight.

[0237]

Example 19

[0238] The only difference between this example and Example 1 is that in the fluidized bed reactor, the diameter ratio of the main feed pipe (18) and the inclined feed distribution branch pipe (19) is 0.4. After the reaction, the methanol conversion rate was 98.6%, and the total yield of ethylene and propylene carbon-based products was 78.4% by weight.

[0239]

Example 20

[0240] The only difference between this example and Example 1 is that in the fluidized bed reactor, the diameter ratio of the main feed pipe (18) and the inclined feed distribution branch pipe (19) is 1.2. After the reaction, the methanol conversion rate was 99.5%, and the total yield of ethylene and propylene carbon-based products was 81.4% by weight.

[0241]

Example 21

[0242] The only difference between this example and Example 1 is that in the fluidized bed reactor, the angle α between the catalyst inclined tube (20) and the reactor is 20°. After the reaction, the methanol conversion rate was 99.6%, and the total yield of ethylene and propylene carbon-based products was 81.7% by weight.

[0243]

Example 22

[0244] The only difference between this example and Example 1 is that in the fluidized bed reactor, the angle α between the catalyst inclined tube (20) and the reactor is 80°. After the reaction, the methanol conversion rate was 99.5%, and the total carbon-based yield of ethylene and propylene was 80.1% by weight.

[0245]

Example 23

[0246] The only difference between this example and Example 1 is that in the fluidized bed reactor, the ratio of the horizontal length l of the cross-type feed distributor (9) to the diameter of the fast bed reactor (1) is 0.2. After the reaction, the methanol conversion rate was 99.4%, and the total carbon-based yield of ethylene and propylene was 79.3% by weight.

[0247]

Example 24

[0248] The only difference between this example and Example 1 is that in the fluidized bed reactor, the ratio of the horizontal length l of the cross-type feed distributor (9) to the diameter of the fast bed reactor (1) is 0.7. After the reaction, the methanol conversion rate was 99.3%, and the total carbon-based yield of ethylene and propylene was 81.2% by weight.

[0249]

Example 25

[0250] The only difference between this example and Example 1 is that in the fluidized bed reactor, the ratio of the distance L from the connection point of the inclined feed distribution branch (19) and the horizontal feed distribution branch (17) to the reactor wall and the horizontal length of the cross-type feed distributor (9) is 0.05. After the reaction, the methanol conversion rate was 99.3%, and the total yield of ethylene and propylene carbon-based products was 80.9% by weight.

[0251]

Example 26

[0252] The only difference between this example and Example 1 is that in the fluidized bed reactor, the ratio of the distance L from the connection point of the inclined feed distribution branch (19) and the horizontal feed distribution branch (17) to the reactor wall and the horizontal length of the cross-type feed distributor (9) is 0.55. After the reaction, the methanol conversion rate was 99.5%, and the total yield of ethylene and propylene carbon-based products was 81.4% by weight.

[0253] The specific parameters of the reactor devices used in the above embodiments and comparative examples are shown in Tables 1-3.

[0254] Table 1 List of Examples

[0255]

[0256] Table 2 Continuation of Examples

[0257]

[0258] Table 3 Continuation of Examples

[0259]

[0260] Table 4 Continuation of Examples

[0261]

[0262] Table 5 Comparative Example List

[0263]

[0264] According to some embodiments of the present invention, using the technical solution of the present invention, and employing SAPO-34 catalyst in the methanol-to-olefins reaction, the total carbon-based yield of ethylene and propylene can reach 85.2% by weight.

[0265] It should be noted that the embodiments described above are only for explaining the present invention and do not constitute any limitation on the present invention. The present invention has been described with reference to typical embodiments, but it should be understood that the words used therein are descriptive and explanatory terms, not limiting terms. Modifications can be made to the present invention within the scope of the claims, and revisions can be made to the present invention without departing from the scope and spirit of the present invention. Although the present invention described herein relates to specific methods, materials, and embodiments, it does not mean that the present invention is limited to the specific examples disclosed herein; on the contrary, the present invention can be extended to all other methods and applications with the same function.

Claims

1. A fluidized bed reactor with a cross-type feed distributor, characterized in that, The reactor includes a rapid bed reactor (1), a double-density bed reactor (2), an external heat exchanger (3), a circulating inclined tube (5), an external heat exchanger inclined tube (6), a regeneration inclined tube (14), a waiting-to-be-regenerated inclined tube (15), a methanol feed distributor (8), and a cross-feed distributor (9). The circulating inclined tube (5) connects the double-density bed reactor (2) and the rapid bed reactor (1); the regeneration inclined tube (14) is connected to the rapid bed reactor (1); the waiting-to-be-regenerated inclined tube (15) is connected to the double-density bed reactor (2); the external heat exchanger inclined tube (6) connects the external heat exchanger (3) and the rapid bed reactor (1); the methanol feed distributor (8) and the cross-feed distributor (9) are connected to each other. The connection between the regeneration inclined tube (14) and the fast bed reactor (1) is located at the bottom of the fast bed reactor (1); the connection between the regeneration inclined tube (14) and the fast bed reactor (1) is located directly above the cross-type feed distributor (9); the connection between the circulation inclined tube (5) and the fast bed reactor (1) is located above the methanol feed distributor (8); the connection between the externally removed inclined tube (6) and the fast bed reactor (1) is located above the methanol feed distributor (8); the methanol feed distributor (8) is located above the connection between the regeneration inclined tube (14) and the fast bed reactor (1); the distance between the methanol feed distributor (8) and the cross-type feed distributor (9) is 1-5% of the total height of the fast bed reactor (1); A cyclone separator (4) is installed inside the double-density bed (2), and the outlet of the cyclone separator (4) is connected to the separation unit; The ratio of the horizontal length of the cross-type feed distributor (9) to the diameter of the fast bed reactor (1) is (0.3-0.6):1; The cross-type feed distributor (9) includes one or more horizontal feed distribution branches (17) and one or more oblique feed distribution branches (19) and a feed main (18), wherein the horizontal feed distribution branches (17) and the oblique feed distribution branches (19) are connected to the feed main (18); the included angle β between the horizontal feed distribution branches (17) and the oblique feed distribution branches (19) is 90 + α; The vertical distance H between the non-connecting end of the inclined feed distribution branch (19) and the horizontal feed distribution branch (17), and the distance L from the connection point of the inclined feed distribution branch (19) and the horizontal feed distribution branch (17) to the reactor wall, wherein the relationship between α, H and L is as follows: ; The horizontal feed distribution branch pipe (17) and the inclined feed distribution branch pipe (19) are provided with at least one row of small holes (21). The diameter ratio of the main feed pipe (18) and the inclined feed distribution branch pipe (19) is (0.5-1.2):

1.

2. The fluidized bed reactor according to claim 1, characterized in that, α is 20° to 80°.

3. The fluidized bed reactor according to claim 1, characterized in that, α is 20° to 60°.

4. The fluidized bed reactor according to claim 1, characterized in that, α is 40° to 80°.

5. The fluidized bed reactor according to claim 1, characterized in that, α is 50° to 80°.

6. The fluidized bed reactor according to claim 1, characterized in that, α is 60° to 80°.

7. The fluidized bed reactor according to claim 1, characterized in that, α is 30° to 70°.

8. The fluidized bed reactor according to claim 1, characterized in that, α is 40° to 60°.

9. The fluidized bed reactor according to claim 1, characterized in that, α is 20° to 50°.

10. The fluidized bed reactor according to claim 1, characterized in that, α is 20° to 40°.

11. The fluidized bed reactor according to claim 1, characterized in that, α is 40° to 50°.

12. The fluidized bed reactor according to claim 1, characterized in that, β is 110° to 170°.

13. The fluidized bed reactor according to claim 1, characterized in that, β is 110° to 130°.

14. The fluidized bed reactor according to claim 1, characterized in that, β is 110° to 140°.

15. The fluidized bed reactor according to claim 1, characterized in that, β is 110° to 150°.

16. The fluidized bed reactor according to claim 1, characterized in that, β is 150° to 170°.

17. The fluidized bed reactor according to claim 1, characterized in that, β is 140° to 170°.

18. The fluidized bed reactor according to claim 1, characterized in that, β is 130° to 170°.

19. The fluidized bed reactor according to claim 1, characterized in that, β is 120° to 160°.

20. The fluidized bed reactor according to claim 1, characterized in that, β is 130° to 150°.

21. The fluidized bed reactor according to claim 1, characterized in that, β is 130° to 140°.

22. The fluidized bed reactor according to any one of claims 1-21, characterized in that, When the small holes (21) are in a row, they are opened along the axial direction of the fast bed reactor (1), and / or the small holes (21) are evenly distributed in parallel or evenly distributed in an alternating manner, and / or the opening ratio of the small holes (21) is 0.05-0.2, and / or the small holes (21) are circular, and / or the connection port between the feed main pipe (18) and the fast bed reactor (1) is located at the lower part of the fast bed reactor.

23. The fluidized bed reactor according to any one of claims 1-21, characterized in that, The diameter ratio of the horizontal feed distribution branch pipe (17) and the inclined feed distribution branch pipe (19) is (0.5-1.8):1, and / or the diameter ratio of the feed main pipe (18) and the inclined feed distribution branch pipe (19) is (0.5-1):

1.

24. The fluidized bed reactor according to any one of claims 1-21, characterized in that, The diameter ratio of the horizontal feed distribution branch (17) and the inclined feed distribution branch (19) is (0.5-1.5):

1.

25. A method for converting mixed oxygen-containing compounds as a byproduct in a methanol-to-olefins process carried out in a fluidized bed reactor according to any one of claims 1-24, comprising: The mixed oxygenated compound aqueous solution feedstock produced by the methanol-to-olefins separation unit enters the fast bed reactor (1) through the cross-type feed distributor (9) and reacts with the regenerated catalyst (12) that enters through the regeneration inclined tube (14). The products generated by the reaction and the coking catalyst rise upward.

26. The method for converting mixed oxygen-containing compounds as a byproduct in the methanol-to-olefins process according to claim 25, wherein the methanol feedstock (10) enters the fast bed reactor (1) via the methanol feedstock distributor (8) and reacts with the catalyst above the methanol feedstock distributor (8), and the resulting product rises to the secondary dense bed (2) for separation to obtain olefin-rich reaction product (13) and catalysts to be generated (16a), (16b) and (16c); and / or, the reaction product (13) enters the subsequent separation unit via the cyclone separator (4) to obtain mixed oxygen-containing compound aqueous solution feedstock (11), the catalyst to be generated (16a) enters the regenerator for regeneration via the catalyst to be generated inclined tube (15), the catalyst to be generated (16b) returns to the fast bed reactor (1) via the circulating inclined tube (5), and the catalyst to be generated (16c) is heated by the external heat exchanger (3) and then returned to the fast bed reactor (1) via the external removal inclined tube (6).

27. The method for converting mixed oxygen-containing compounds as a byproduct in the methanol-to-olefins process according to claim 25 or 26, characterized in that, The mass percentage of mixed oxygen-containing compounds in the mixed oxygen-containing aqueous solution feedstock (11) is 5-70%; and / or the temperature in the fast bed reactor (1) is 450-520℃, the gas velocity is 0.5-3 m / s, the catalyst bed density is 30-200 kg / m³, the reaction gauge pressure is 0-0.4 MPa, and the mass hourly space velocity of the methanol feedstock (10) is 3-30 h⁻¹. -1 The mass hourly space velocity (MSV) of the mixed oxygen-containing aqueous solution feedstock (11) is 0.05–1 h⁻¹. -1 And / or regenerated catalyst (12), with a carbon content of less than 0.1% by total catalyst mass, and / or the mixed oxygen-containing compound includes methanol and at least one selected from ethanol, propanol, butanol, acetaldehyde, propionaldehyde, butyraldehyde, acetone, butanone, formic acid, acetic acid and propionic acid, and / or the mass percentage of ketones in the mixed oxygen-containing compound is 30 to 80%.

28. The method for converting mixed oxygen-containing compounds as a byproduct in the methanol-to-olefins process according to claim 25 or 26, wherein the olefins include ethylene and propylene, and the total carbon-based yield of ethylene and propylene can reach more than 82%.

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