CN116571171A - A system for producing light olefins from methanol and its preparation method - Google Patents

Abstract

The invention provides a system for producing low-carbon olefins from methanol and a preparation method thereof, which belong to the technical field of petrochemical industry, and solve the problems of the existing fluidized dense-phase bed methanol-to-low-carbon olefins device with small processing capacity, low operating flexibility, and energy consumption. advanced questions. It includes a riser reactor, the riser reactor is connected with a reaction settler, the reaction settler is connected with a regenerator, the bottom of the regenerator is connected with a regeneration inclined pipe connected with the riser reactor, and the reaction settler is connected with a first external The heat extractor, the first external heat extractor communicates with the riser reactor. The mixed gas generated by the reaction enters the reaction settler to separate the product from the catalyst, the regenerator burns the catalyst, and finally passes the catalyst into the riser reactor to continue to participate in the reaction; the first external heat collector is installed Part of the cooled catalyst is introduced into the riser reactor to reduce the temperature, and the requirements of reaction time and reaction depth can be flexibly adjusted according to the change of methanol processing capacity.

Description

A system for producing light olefins from methanol and its preparation method

technical field

The invention belongs to the technical field of petrochemical industry, in particular to a system for producing light olefins from methanol and a preparation method thereof.

Background technique

Ethylene, propylene, and butene are important basic chemicals in the field of petrochemicals, and are widely used in plastics, fibers, medicine, textiles and other fields. Production of ethylene, propylene, and butene mainly includes catalytic cracking, naphtha steam cracking, ethane, propane, and butane dehydrogenation, and methanol to ethylene, propylene, and butene. Among them, methanol-to-ethylene, propylene, butene and other low-carbon olefins have been paid more and more attention due to the wide range of raw materials, low investment, and the close combination of coal chemical industry and petrochemical industry. The methanol-to-low-carbon alkanes reaction is a reaction with strong exotherm and short reaction time. Once the "carbon pool" is formed in the reaction of methanol to light olefins, the reaction of methanol to light olefins can be completed in less than 0.2S, and a large amount of heat is released. The methanol conversion products ethylene, propylene, butene, etc. are very active. Under the acid catalysis of molecular sieves, they can be further reacted by cyclization, dehydrogenation, hydrogen transfer, condensation, and alkylation to generate saturated hydrocarbons with different molecular weights, C6+ olefins and coke. Controlling the reaction time and removing heat in time are the key to producing light olefins from methanol. In the industrialized production equipment, there are mainly dense-phase fluidized bed reactors and special catalysts based on small-pore SAPO molecular sieves.

Existing industrial methanol-to-light olefins are based on the reaction form of fluidized catalytic devices. According to the specific characteristics of methanol to light olefins, special catalysts based on small-pore SAPO molecular sieves and dense-phase fluidized bed reactors are used. This kind of dense-phase fluidized bed reactor needs to maintain a good height of the catalyst dense-phase bed and a certain reaction time, lacks good operating flexibility, and has a low throughput of the device.

Existing special catalysts based on small-pore SAPO molecular sieves have high activity, so that the catalyst circulation between the dense-phase fluidized bed reactor and the regenerator is small, and the respective characteristics of the reactor and the regenerator cannot be exerted through a large amount of catalyst circulation.

Patent No. CN114133309A discloses the use of a two-stage fluidized bed reactor, the upper section is the MTO reaction section, and the lower section is the C4C5 reaction section. Both reactors are fluidized bed reactors, and the dense-phase bed reactor limits the change of processing scale, and the heat extraction equipment is set in the dense-phase bed layer, which makes the operation complicated and the flexibility of the device is limited.

Patent No. CN114377729A discloses a fluidized bed regenerator, a device for preparing low-carbon olefins and its application. The fluidized bed regenerator includes a second activation zone, a first activation zone, and a gas-solid separation zone from bottom to top; the invention is also a dense-phase fluidized bed reactor, and the equipment involved in the invention is complex and difficult to engineer Large, the obvious disadvantage is that the processing scale of the device is limited, the operation is difficult, and the energy consumption is high.

Patent No. CN112546974A discloses a fluidized bed reactor for methanol to olefins. It includes a fast-bed reactor, a double-dense bed, and a cross-type feed distributor, which includes one or more horizontal feed distribution branches, one or more inclined feed distribution branches and a feed main pipe , wherein the horizontal feed distribution branch pipe and the inclined feed distribution branch pipe are connected to the feed main pipe, and the connection port between the feed main pipe and the fast bed reactor is arranged at the lower part of the fast bed reactor. When the fluidized bed reactor of the present invention is used for producing olefins from methanol, it has the advantage of high conversion rate of oxides when the oxides are smelted back. Its invention is mainly to solve the difficulty of increasing the conversion rate of oxides during re-refining. Compared with the previous fluidized bed, the reaction in the bed has been greatly improved, but for the raw material of methanol, the operation flexibility is still small, and the change of reaction heat cannot be adjusted in time. .

Contents of the invention

Aiming at the problems of the existing fluidized dense-bed methanol-to-low-carbon olefins device, such as small processing capacity, low operating flexibility, and high energy consumption, the purpose of the present invention is to provide a system for producing low-carbon olefins from methanol and its preparation method. The riser reactor reacts with the catalyst, and the mixed gas produced enters the reaction settler to separate the product from the catalyst. The regenerator then burns the separated catalyst to restore the activity of the catalyst, and finally passes the regenerated catalyst into the The riser reactor continues to participate in the reaction, and the first external heat collector is set to recover the heat in the reaction settler, and a part of the cooled catalyst is introduced into the riser reactor to reduce the temperature in the riser reactor. According to the change of methanol processing capacity, the requirements of reaction time and reaction depth can be flexibly adjusted.

The technical scheme that the present invention adopts is as follows:

A system for producing low-carbon olefins from methanol, comprising a riser reactor, the gas outlet of the riser reactor is connected to a reaction settler, the reaction settler is connected to a regenerator, and the bottom of the regenerator is connected to a regeneration inclined tube, the regenerator is communicated with the riser reactor through the regeneration inclined tube, the reaction settler is communicated with a first external heat extractor, and the first external heat extractor is connected with a feeding pipe, and the discharging The tube communicates with the riser reactor.

Preferably, the junction of the feed pipe and the riser reactor is located above the junction of the regeneration inclined pipe and the riser reactor.

Preferably, the first external heat extractor is connected with a return pipe, and the return pipe communicates with the reaction settler.

Preferably, the riser reactor includes a standpipe and a horizontal pipe connected to the upper end of the standpipe, the bottom of the standpipe is provided with a first lifting medium inlet, and the riser is provided with a Inlet.

Preferably, the reaction settler includes a reaction settler shell, and the reaction settler shell is provided with a coarse cyclone separator and a single stage cyclone separator, and the inlet end of the coarse cyclone separator reacts with the riser The gas outlet of the reactor is connected, and the inner lower end of the shell of the reaction settler is provided with a first stripping section.

Preferably, the regenerator includes a regenerator shell and an introduction pipe running through the bottom of the regenerator shell, the bottom of the introduction pipe is provided with a second lifting medium inlet, the introduction pipe is connected to the inclined pipe to be produced, and the inclined pipe to be produced The pipe communicates with the first stripping section, and the inner lower end of the regenerator housing is provided with a second stripping section.

Preferably, the upper end of the introduction pipe is connected with a spent catalyst distributor, and the regenerator casing is connected with a main air distributor located below the spent catalyst distributor.

Preferably, a cyclone separator set is arranged inside the shell of the regenerator.

A method for producing light olefins from methanol, comprising the following steps:

S1. Input methanol and catalyst into the riser reactor, and the reaction gas generated by the reaction is transported to the reaction settler by the lifting medium;

S2. The reaction gas enters the coarse-stage cyclone separator and the single-stage cyclone separator in turn, and the ungenerated catalyst is separated to obtain the ungenerated catalyst. Part of the ungenerated catalyst enters the regenerator after stripping, and the other part enters the first external extraction. Cooled in the heater, and enter the riser reactor through the feed pipe;

S3. The spent catalyst located in the regenerator is burnt to obtain a regenerated catalyst, and the regenerated catalyst flows into the riser reactor from the regenerated inclined pipe after being stripped.

The temperature in the riser reactor is 350-550°C, the pressure is 0.1-0.5MPa, and the reaction time is 0.5-5s; the temperature in the regenerator is 550-700°C.

In summary, owing to adopting above-mentioned technical scheme, the beneficial effect of the present invention is:

Methanol reacts with the catalyst in the riser reactor, and the resulting mixed gas enters the reaction settler to separate the product from the catalyst, and the regenerator burns the separated catalyst to restore the activity of the catalyst, and finally regenerates the regenerated catalyst Pass into the riser reactor to continue to participate in the reaction, and set the first external heat collector to recover the heat in the reaction settler, and introduce a part of the cooled catalyst into the riser reactor to reduce the temperature in the riser reactor , can flexibly adjust the requirements of reaction time and reaction depth according to the change of methanol processing capacity, increase the flexibility of operation, and increase the processing capacity of methanol.

Description of drawings

In order to illustrate the technical solutions of the embodiments of the present invention more clearly, the accompanying drawings used in the embodiments will be briefly introduced below. It should be understood that the following drawings only show some embodiments of the present invention, and thus It should be regarded as a limitation on the scope, and those skilled in the art can also obtain other related drawings based on these drawings without creative work.

Fig. 1 is a schematic flow diagram provided by the first embodiment of the present invention;

Fig. 2 is a schematic flow diagram provided by the second embodiment of the present invention;

Fig. 3 is a schematic flow chart provided by the third embodiment of the present invention;

Fig. 4 is a schematic flowchart provided by a fourth embodiment of the present invention.

Description of the drawings: 1-riser reactor; 2-regenerated flue gas outlet; 3-horizontal pipe; 4-coarse cyclone separator; 5-reaction settler; 6-cyclone separator group; 7-reaction oil and gas collection Chamber; 8-the first feeding pipe; 9-return pipe; 10-the first external heat extractor; 11-the first fluidizing air inlet; 12-feeding pipe; 13-the first stripping section; 14-wait for raw Inclined pipe; 15-feed inlet; 16-first lifting medium inlet; 17-regeneration inclined pipe; 18-third slide valve; 19-second lifting medium inlet; 20-second slide valve; 21-main air distribution 22-the second stripping section; 23-the second fluidization air inlet; 24-the second feed pipe; 25-the second external heat extractor; - first slide valve; 29 - inlet pipe; 30 - single-stage cyclone separator; 31 - collecting partition.

Detailed ways

In order to make the purpose, technical solutions and advantages of the embodiments of the present invention clearer, the technical solutions in the embodiments of the present invention will be clearly and completely described below in conjunction with the drawings in the embodiments of the present invention. Obviously, the described embodiments It is a part of embodiments of the present invention, but not all embodiments. The components of the embodiments of the invention generally described and illustrated in the figures herein may be arranged and designed in a variety of different configurations.

Accordingly, the following detailed description of the embodiments of the invention provided in the accompanying drawings is not intended to limit the scope of the claimed invention, but merely represents selected embodiments of the invention. Based on the embodiments of the present invention, all other embodiments obtained by persons of ordinary skill in the art without creative efforts fall within the protection scope of the present invention.

In the description of the present invention, it should be noted that if the terms "center", "upper", "lower", "left", "right", "vertical", "horizontal", "inner", "outer" " and other indications are based on the orientation or positional relationship shown in the attached drawings, or the orientation or positional relationship that is usually placed when the application product is in use, and are only for the convenience of describing the present invention and simplifying the description, rather than indicating Or imply that the device or element referred to must have a specific orientation, be constructed and operate in a specific orientation, and therefore should not be construed as limiting the invention.

The present invention will be described in detail below with reference to FIGS. 1-4 .

Example

Example 1:

A system for producing low-carbon olefins from methanol, comprising a riser reactor 1, the gas outlet end of the riser reactor 1 is connected with a reaction settler 5, and the reaction settler 5 is connected with a regenerator 27, and the regenerator The bottom of 27 is connected with a regeneration inclined pipe 17, and the regenerator 27 is communicated with the riser reactor 1 through the regeneration inclined pipe 17, and the reaction settler 5 is communicated with a first external heat extractor 10, and the first external heat extractor The heater 10 is connected with a feed pipe 12 , and the feed pipe 12 communicates with the riser reactor 1 .

As shown in Figure 1, pass into the riser reactor 1 through the feed pipe 12 and the regeneration inclined pipe 17 (the carbon content on the riser reactor 1 is 1 to 7%), ensuring that the riser reactor 1 At the same time, it can provide the temperature required for methanol to light olefins, and can maintain a large amount of catalyst circulation, so as to maintain the reaction heat capacity of the catalyst in the riser reactor 1, so that the temperature of the riser reactor 1 can be controlled and controlled. It can be adjusted flexibly according to the change of methanol processing volume.

The outlet of the lower feed pipe 12 can be set above or below the outlet of the regeneration inclined pipe 17, and in order to better react methanol and reduce energy loss, the connection between the lower feed pipe 12 and the riser reactor 1 is arranged on the regeneration inclined pipe 17. Above the connection between pipe 17 and riser reactor 1, the high-temperature catalyst is first contacted with methanol, thereby heating the methanol. The temperature reaches about 350°C, reaching the initial reaction temperature of methanol, and then contacts the low-temperature catalyst. The catalyst contains carbon pools that allow methanol to react rapidly.

The first external heat extractor 10 is connected with a first feed pipe 8, the first feed pipe 8 communicates with the reaction settler 5, and the first feed pipe 8 is inclined to the first external heat extractor 10 to facilitate catalyst flow to the first external heat extractor 10. In an external heat extractor 10; the first external heat extractor 10 is also connected with a heat extraction pipe, and after the heat extraction tube absorbs heat, the water in the tube is evaporated to obtain heat; the bottom of the first external heat extraction apparatus 10 is also provided with a second A fluidizing air inlet 11, the first fluidizing air inlet 11 is passed into gas to keep the catalyst in the first external heat collector 10 and the reaction settler 5 in a flowing state, ensuring that the pipeline will not be blocked; and the setting is communicated with the reaction settler 5 The return pipe 9 can pass the excess fluidizing air into the first external heat extractor 10 for reuse, increasing the utilization rate of the fluidizing air.

The riser reactor 1 includes a riser and a horizontal pipe 3 connected to the upper end of the riser. The bottom of the riser is provided with a first lift medium inlet 16 , and the riser is provided with a feed inlet 15 above the first lift medium inlet 16 . Methanol is introduced into the standpipe through the feed inlet 15, and the lifting gas is input through the first lifting medium inlet 16 to mix and react the methanol and the catalyst, and the reaction gas enters the reaction settler 5 through the horizontal pipe 3.

The reaction settler 5 comprises a reaction settler shell, and the reaction settler shell is provided with a coarse cyclone separator 4 and a single stage cyclone separator 30, the inlet end of the coarse cyclone separator 4 and the gas outlet end of the riser reactor 1 Connected, the inner lower end of the shell of the reaction settler is provided with a first stripping section 13 . The coarse-level cyclone separator 4 performs solid-gas separation on the reaction gas generated by the riser reactor 1, and separates the catalyst into the reaction gas; in the coarse-level cyclone separator 4, the reaction gas and the catalyst are separated in a very short time. The side reactions (cracking, condensation, coking and other reactions of olefin-rich reaction gas) are greatly reduced, and the selectivity of methanol to light olefins is guaranteed. The separated catalyst falls into the first stripping section 13, and steam is passed into the first stripping section 13 to replace the reaction gas entrained in the catalyst, so as to prevent the reaction gas of methanol from entraining into the regenerator 27 or the riser reactor 1 In the process, it causes waste of raw materials and increases the cracking of olefins in the reaction product. The coarse-stage cyclone separator 4 is not connected to the single-stage cyclone separator 30, so that other gases in the reaction settler 5 are conveniently entered into the single-stage cyclone separator 30; Separation, the gas discharged from the coarse-stage cyclone separator 4 enters the air inlet of the single-stage cyclone separator 30 for separation again; 7. Collect the reaction gas. The efficiency of the coarse-stage cyclone separator 4 and the single-stage cyclone separator 30 both reaches more than 90%, and the coarse-stage cyclone separator 4 and the single-stage cyclone separator 30 are arranged in 6 or 8 groups, and the total separation efficiency is above 99.99%.

The regenerator 27 comprises a regenerator shell and an introduction pipe 29 that runs through the bottom of the regenerator shell. The bottom of the introduction pipe 29 is provided with a second lifting medium inlet 19. The introduction pipe 29 is connected to the inclined pipe 14 to be produced, and the inclined pipe 14 to be produced is connected to the first The stripping section 13 is connected, and a second stripping section 22 is provided at the inner lower end of the shell of the regenerator. The raw catalyst flows into the lower end of the introduction pipe 29 through the raw inclined pipe 14, and the lifting gas is input from the second lifting medium inlet 19 to transport the raw catalyst to the regenerator 27 for burning operation to obtain the regenerated catalyst (the carbon content on the regenerated catalyst 0.1% to 1%); due to the use of lifting gas to transport the standby catalyst, the standby catalyst can be dispersed into the regenerator 27 to ensure the effect of burning; Replacement is performed to prevent air from being entrained into the regeneration inclined pipe 17 . The first stripping section 13 and the second stripping section 22 are equipped with annular and disk-shaped grilles, which can break up air bubbles, increase the probability of vapor-solid contact, and improve the effect of stripping.

A first slide valve 28 is arranged in the feeding pipe 12 to prevent the gas in the riser reactor 1 from entering the first external heat collector 10; a second slide valve 20 is arranged in the regeneration inclined pipe 17 to prevent the riser from reacting The gas in the regenerator 1 enters the regenerator 27; the third slide valve 18 is arranged in the inclined pipe 14 to prevent the gas in the regenerator 27 from entering the reaction settler 5.

In order to further increase the scorch effect of the catalyst, it is necessary to increase the contact area between the catalyst and the air. Therefore, the upper end of the inlet pipe 29 is connected with a standby catalyst distributor 26, and the regenerator shell is connected with the main air distribution device located below the standby catalyst distributor 26. The device 21 uniformly disperses the catalyst and the air through the distributor, so that the two can be evenly mixed with each other, thereby improving the efficiency of coking. The standby catalyst distributor 26 is arranged opposite to the air outlet of the main air distributor 21, so that the catalyst and air are mixed and burnt in countercurrent to ensure the burning time and burning effect.

A cyclone separator group 6 is arranged inside the shell of the regenerator, and the cyclone separator group 6 further separates the catalyst in the gas to reduce the loss of the catalyst. The gas outlet of the cyclone separator group 6 is connected with the regenerated flue gas outlet 2, and excess gas is discharged from the regenerated flue gas outlet 2, and then discharged to the waste heat recovery unit through the regenerated flue gas outlet 2.

Setting the cyclone separator group 6 as a two-stage cyclone separator can ensure the separation effect of the catalyst; the gas enters from the air inlet of the first-stage cyclone separator, and after preliminary separation, it enters the second-stage cyclone separator through a pipeline separated again.

The regenerator 27 is connected to the second external heat receiver 25, and the second external heat receiver 25 recovers and reuses the heat in the regenerator 27. The second external heat extractor 25 is connected with a second feed pipe 24, and the second feed pipe 24 communicates with the regenerator 27; The water evaporates, thereby taking heat; The bottom of the second external heat extractor 25 is also provided with a second fluidizing air inlet 23, and the second fluidizing air inlet 23 is passed into the gas to make the second external heat extractor 25 and the regenerator 27 The catalyst keeps flowing, ensuring that the pipes will not be blocked.

Example 2:

The second arrangement of the riser reactor 1 , the reaction settler 5 and the regenerator 27 of the present application is shown in FIG. 2 . Shown in Fig. 2 is the coaxial arrangement structure of riser reactor 1 and reaction settler 5, namely riser reactor 1 penetrates from the bottom of reaction settler 5 and stretches in the reaction settler 5, riser reactor 1 communicates with the coarse cyclone separator 4. At this time, the riser reactor 1 is an outer folded riser.

The reaction gas is separated by the coarse cyclone separator 4 and the single-stage cyclone separator 30 to obtain the raw catalyst, and the raw catalyst enters the regenerator 27 from the inclined pipe 14 after being stripped by the first stripping section 13. Since the outlet of the standby inclined pipe 14 is arranged above the main air distributor 21 , the spent catalyst can directly flow to the main air distributor 21 to be mixed with air for charring.

The use of this layout structure has the advantages of simple operation, strong anti-accident ability, and small footprint.

Example 3:

The third arrangement structure of the riser reactor 1 , the reaction settler 5 and the regenerator 27 of the present application is shown in FIG. 3 . Compared with the second arrangement structure, the difference of the third arrangement structure lies in the growth of the dilute phase section and the dense phase section of the regenerator 27, so that the regenerator 27 and the reaction settler 5 are located at the same height, which can be adopted according to the pressure balance. The second or third arrangement structure.

Example 4:

The fourth arrangement of the riser reactor 1 , the reaction settler 5 and the regenerator 27 of the present application is shown in FIG. 4 . The fourth arrangement structure and the first arrangement structure both adopt the method that the riser reactor 1 is externally installed, while the fourth arrangement structure combines the reaction settler 5 and the regenerator 27, which can also reduce the occupation of the equipment. land area.

In this arrangement, the regenerator 27 is located below the reaction settler 5, and the inclined pipe 14 to be produced is replaced with a vertical pipe to directly communicate with the first stripping section 13 and the introduction pipe 29, and the catalyst to be produced is steamed through the first stripping section 13. After lifting, it falls into the introduction pipe 29, and the second lifting medium inlet 19 inputs the lifting medium to transport the standby catalyst to the standby catalyst distributor 26, and evenly sprays it out from the standby catalyst distributor 26, so that the standby catalyst is fully Combustion reaction: the regenerated catalyst is obtained after the raw catalyst is burnt, and the regenerated catalyst flows into the riser reactor 1 from the regenerated inclined pipe 17 after being stripped by the second stripping section 22 .

Wherein the reaction settler 5 is provided with a collection partition 31, the collection partition 31 and the shell of the reaction settler form a collection tank structure, which facilitates the catalyst separated by the coarse cyclone separator 4 to enter the first feed pipe 8.

A method for producing light olefins from methanol, comprising the following steps:

S1, input methanol and catalyst into the riser reactor 1, and the reaction gas generated by the reaction is transported to the reaction settler 5 by the lifting medium;

S2. The reaction gas enters the coarse-stage cyclone separator 4 and the single-stage cyclone separator 30 in turn, and separates the ungenerated catalyst, wherein a part of the ungenerated catalyst enters the regenerator 27 after being stripped, and another part of the ungenerated catalyst enters the first Cooling in an external heat extractor 10, the temperature of the ungenerated catalyst is reduced by 50-150°C, and enters the riser reactor 1 through the feeding pipe 12. This part of the ungenerated catalyst accounts for 30% of the catalyst amount in the riser reactor 1. -80w%;

S3. The spent catalyst located in the regenerator 27 is burnt to obtain a regenerated catalyst, and the regenerated catalyst flows into the riser reactor 1 from the regenerated inclined pipe 17 after being stripped.

The temperature in the riser reactor 1 is 350-550°C, the pressure is 0.1-0.5MPa, and the reaction time is 0.5-5s; the preferred temperature in the riser reactor 1 is 450-500°C, the pressure is 0.1-0.25MPa, The reaction time is 1-2s. The temperature in the regenerator 27 is 550-700°C, which can ensure that the waste heat recovery of the rear regeneration flue gas does not require CO incinerators and other equipment, which reduces investment and increases the stability of device operation; after complete combustion, the catalyst performance can be improved. Good performance can increase catalyst efficiency. The methanol-to-low-carbon olefin reaction can be carried out under the condition of an agent-to-alcohol ratio of 0.1-8, and the reaction can be completed rapidly, and the preferred agent-to-alcohol ratio is 0.2-6.

The catalyst used in this application is a methanol-to-light olefin acidic catalyst based on small-pore SAPO molecular sieves. The catalyst is used in a riser fluidized bed with a reaction pressure of 0.01-1 MPa, a temperature of 350-550°C, and a mass space velocity of 0.3-8h; the methanol-to-low-carbon olefins catalyst includes the following components in mass fractions based on the total mass of the methanol-to-low-carbon olefins catalyst on a dry basis: 0.1-30% of aluminum oxide, and 0.1-10% of the first auxiliary agent , the second auxiliary agent is 0.1-60%, and the balance is a fluidized bed carrier; the first auxiliary agent is SAPO molecular sieve with good pore size distribution, so that the catalyst has higher target product selectivity; the second auxiliary agent is an inert agent, The strength and stability of the catalyst are significantly enhanced, the catalyst has a longer service life, and the catalyst circulation is increased. The catalyst circulation is increased from less than 100t/h to about 1000t/h, which is similar to that of a catalytic cracking unit. Large catalyst-to-oil ratio operation; due to the increase in catalyst circulation, the heat capacity of the catalyst in riser reactor 1 is increased, which can truly realize a large catalyst-to-oil ratio similar to that of a catalytic cracking unit, and can timely adjust the reaction of riser reactor 1 Temperature control greatly increases the processing scale of a single device, and also increases the excellent selectivity and stability of the catalyst.

This riser fluidized bed reactor can quickly increase the methanol processing scale of a single device from 2 million tons per year to 5 million tons per year. This reaction form will greatly reduce investment, reduce energy consumption, and ensure the production of methanol to olefins. selective.

The above are only preferred embodiments of the present invention, and are not intended to limit the present invention. For those skilled in the art, the present invention may have various modifications and changes. Any modifications, equivalent replacements, improvements, etc. made within the spirit and principles of the present invention shall be included within the protection scope of the present invention.

Claims (10)

1. A system for methanol production of light olefins, comprising a riser reactor (1), the outlet end of the riser reactor (1) is connected with a reaction settler (5), and the reaction settler (5) Connected with a regenerator (27), the bottom of the regenerator (27) is connected with a regeneration inclined pipe (17), and the regenerator (27) communicates with the riser reactor (1) through the regeneration inclined pipe (17), It is characterized in that, the reaction settler (5) is communicated with a first external heat extractor (10), and the first external heat extractor (10) is connected with a feeding pipe (12), and the feeding pipe ( 12) Communicate with the riser reactor (1). 2. a kind of methanol production system of light olefins according to claim 1, is characterized in that, the joint of described feeding pipe (12) and riser reactor (1) is positioned at regeneration inclined pipe (17) and Above the junction of the riser reactor (1). 3. a kind of methanol production system of light olefins according to claim 1, is characterized in that, described first external heat extractor (10) is connected with return pipe (9), and described return pipe (9) and The reaction settler (5) is communicated. 4. a kind of methanol production system of light olefins according to claim 1, is characterized in that, described riser reactor (1) comprises standpipe and the horizontal pipe (3) that is connected at standpipe upper end, and described The bottom of the standpipe is provided with a first lifting medium inlet (16), and the standpipe is provided with a feed opening (15) above the first lifting medium inlet (16). 5. a kind of methanol production system of light olefins according to claim 1, is characterized in that, described reaction settler (5) comprises reaction settler shell, and described reaction settler shell is provided with rough stage cyclone separation device (4) and a single-stage cyclone separator (30), the inlet end of the coarse-stage cyclone separator (4) is connected with the gas outlet end of the riser reactor (1), and the inner lower end of the shell of the reaction settler A first stripping section (13) is provided. 6. A system for producing low-carbon olefins from methanol according to claim 5, characterized in that, the regenerator (27) comprises a regenerator shell and an introduction pipe (29) that runs through the bottom of the regenerator shell, and the introduction The bottom of the pipe (29) is provided with a second lifting medium inlet (19), and the introduction pipe (29) is communicated with the inclined pipe (14) to be produced, and the inclined pipe (14) to be produced is connected to the first stripping section (13). ) is communicated, and the inner lower end of the regenerator housing is provided with a second stripping section (22). 7. The system for producing light olefins from methanol according to claim 6, characterized in that, the upper end of the introduction pipe (29) is connected with a live catalyst distributor (26), and the regenerator shell is connected with a The main air distributor (21) below the spent catalyst distributor (26). 8 . The system for producing light olefins from methanol according to claim 6 , characterized in that, a cyclone separator group ( 6 ) is arranged inside the shell of the regenerator. 9. A method for preparing low-carbon olefins from methanol, characterized in that, comprising the following steps: S1. Input methanol and catalyst into the riser reactor (1), and the reaction gas generated by the reaction is transported to the reaction settler (5) by the lifting medium; S2, the reaction gas enters the coarse cyclone separator (4) and the single-stage cyclone separator (30) successively, and separates to obtain the raw catalyst, wherein a part of the raw catalyst enters the regenerator (27) after stripping, and the other part The raw catalyst enters into the first external heat extractor (10) for cooling, and enters the riser reactor (1) through the feed pipe (12); S3. The spent catalyst located in the regenerator (27) is burnt to obtain a regenerated catalyst, and the regenerated catalyst flows into the riser reactor (1) from the regenerated inclined pipe (17) after being stripped. 10. A method for producing light olefins from methanol according to claim 9, characterized in that, the temperature in the riser reactor (1) is 350-550° C., the pressure is 0.1-0.5 MPa, and the reaction The time is 0.5-5s; the temperature in the regenerator (27) is 550-700°C.