System for preparing olefin from methanol

Abstract

A system for preparing olefin from methanol, for use in solving the problem in the prior art that the reaction speed is affected due to methanol being directly delivered to participate in a reaction. The system comprises a feeding system (5). The feeding system (5) comprises a purified water heat exchanger (501), a condensate water heat exchanger (502), a steam vaporizer (503), a reaction gas heat exchanger A (505) and a methanol feeding pipe (121) which are connected in sequence. A pipeline between the purified water heat exchanger (501) and the condensate water heat exchanger (502) is communicated with a quench methanol delivery pipe (507) connected to the methanol feeding pipe (121). A heating furnace (506) is connected to the reaction gas heat exchanger A (505). After methanol passes through the purified water heat exchanger (501) and the condensate water heat exchanger (502) for heat exchange, the temperature of the methanol is increased; the steam vaporizer (503) vaporizes the methanol and then heat exchange is performed by the reaction gas heat exchanger A (505) to increase the temperature; the quench methanol delivery pipe (507) delivers low-temperature methanol to be mixed with high-temperature methanol to control the temperature of fed methanol; and the heating furnace (506) is used for heating methanol during operation. After heat exchange, vaporization, overheating and temperature control operation, the methanol is kept at an appropriate temperature to participate in the reaction, thereby ensuring the reaction speed.

Description

A methanol to olefins system Technical Field

[0001] The invention belongs to the technical field of petrochemical industry, and in particular to a system for preparing olefins from methanol. Background Art

[0002] Ethylene and propylene belong to the olefin family of hydrocarbons, unsaturated hydrocarbons used to synthesize specialized polymer materials. They are important building blocks in organic synthesis and are widely used in fields such as plastics, fibers, environmental protection, medicine, textiles, and basic research. The main methods for producing ethylene and propylene include catalytic cracking, naphtha steam cracking, dehydrogenation, and methanol to ethylene and propylene. The methanol to ethylene, propylene, and other low-carbon olefins method are gaining increasing attention due to its wide availability of raw materials, low investment, and ability to closely integrate coal chemical industry with petrochemical industry. Once the "carbon pool" is formed in the methanol to olefins reaction, the olefin formation reaction is rapid, completing in less than 0.1 seconds and releasing significant heat. Methanol conversion products such as ethylene and propylene are highly reactive. Under the acidic catalysis of molecular sieves, they can undergo further reactions such as cyclization, dehydrogenation, hydrogen transfer, condensation, and alkylation to produce saturated hydrocarbons of varying molecular weights, C6+ olefins, and coke. Controlling reaction time and temperature is crucial for methanol to olefins.

[0003] When methanol is produced from olefins, methanol needs to be transported to a riser reactor through a feed system to react with a catalyst. In the existing technology, when transporting methanol, methanol directly enters the riser reactor through a buffer tank. Since the temperature of methanol is relatively low, it needs to be heated after entering the riser reactor to effectively react, which affects the reaction rate.

[0004] Summary of the Invention

[0005] In response to the above problems, the present invention aims to provide a methanol to olefins system, in which the temperature of the methanol is increased after heat exchange through a purified water heat exchanger and a condensate heat exchanger; the steam vaporizer vaporizes the methanol and then heat-exchanges it through a reaction gas heat exchanger A to increase its temperature; a quenched methanol delivery pipe mixes the low-temperature methanol with the high-temperature methanol to control the methanol feed temperature; a heating furnace is used to heat the methanol at startup; and through heat exchange, vaporization, superheating and temperature control operations, the methanol is maintained at a suitable temperature to participate in the reaction, thereby ensuring the reaction rate.

[0006] The technical solution adopted in the present invention is as follows:

[0007] A methanol to olefins system includes a feeding system, wherein the feeding system includes a purified water heat exchanger, a condensate heat exchanger, a steam vaporizer, a reaction gas heat exchanger A and a methanol feed pipe connected in sequence, the pipeline between the purified water heat exchanger and the condensate heat exchanger is connected to a quenching methanol delivery pipe connected to the methanol feed pipe, and the reaction gas heat exchanger A is connected to a heating furnace.

[0008] Preferably, a stripping gas vaporizer is provided in parallel with the steam vaporizer.

[0009] Preferably, the methanol to olefins system also includes a reaction system, which includes a riser reactor, the gas outlet end of the riser reactor is connected to a reaction settler, a first-level cyclone separator and a second-level cyclone separator are provided in the reaction settler, the gas outlet end of the second-level cyclone separator is connected to a reaction gas collecting chamber, a reaction stripping section is provided at the bottom of the reaction settler, the reaction stripping section is connected to an inclined pipe to be regenerated, the inclined pipe to be regenerated is connected to a regenerator, a flue gas collecting chamber and a cyclone separator group connected to the flue gas collecting chamber are provided in the regenerator, a regeneration stripping section is provided at the bottom of the regenerator, and the regeneration stripping section is connected to a regeneration inclined pipe connected to the riser reactor.

[0010] Preferably, the reaction settler is connected to a first feed pipe, the first feed pipe is connected to a first external heat exchanger, the regenerator is connected to a second feed pipe, and the second feed pipe is connected to a second external heat exchanger.

[0011] Preferably, the first external heat exchanger is connected to a first discharge pipe communicating with the riser reactor.

[0012] Preferably, the methanol to olefins system also includes a reaction gas dust removal system, which includes a first self-cleaning dust collector group, the bottom of the first self-cleaning dust collector group is connected to a first collection tank, the gas outlet end of the first self-cleaning dust collector group is connected to a reaction gas heat exchanger B, and the reaction gas heat exchanger B is connected to a steam generator.

[0013] Preferably, the methanol to olefins system further includes a sedimentation system, which includes a quenching tower connected to a steam generator, a first settler connected to the bottom of the quenching tower, an olefin separation heat exchanger and an air cooler connected in sequence to the water outlet end of the first settler, the air cooler connected to the quenching tower, a gas outlet end of the quenching tower connected to a water washing tower, the bottom of the water washing tower is connected to the water outlet end of the second settler connected to the water washing tower, and the slurry outlet ends of the first settler and the second settler are connected to a mud pool.

[0014] Preferably, the methanol to olefins system also includes a flue gas dust removal system, which includes a second self-cleaning dust collector group, the bottom of the second self-cleaning dust collector group is connected to a second collecting tank, and the gas outlet end of the second self-cleaning dust collector group is sequentially connected to a first water seal tank, a CO incinerator, a waste heat boiler, a flue gas dust removal device and a chimney.

[0015] Preferably, the air outlet end of the second self-cleaning dust collector group is also connected to a second water seal tank connected to the chimney.

[0016] Preferably, a double-acting slide valve and a pressure-reducing orifice plate are provided in the air outlet duct of the second self-cleaning dust collector group, and the double-acting slide valve is located between the second self-cleaning dust collector group and the pressure-reducing orifice plate.

[0017] In summary, due to the adoption of the above technical solution, the beneficial effects of the present invention are:

[0018] After the methanol passes through the purified water heat exchanger and the condensate heat exchanger, the temperature of the methanol is increased, and the purified water and condensate in the production process are cooled, so as to reduce the use of air coolers for cooling the purified water and condensate; the steam vaporizer vaporizes the methanol to facilitate the transportation of the methanol; the reaction gas heat exchanger A then exchanges heat to increase the temperature of the vaporized methanol, and at the same time reduces the temperature of the reaction gas to prevent the high temperature from affecting the operation of the compressor used to transport the reaction gas; the quenching methanol delivery pipe delivers the lower temperature methanol to the methanol feed pipe to mix with the higher temperature methanol to control the feed temperature of the methanol and prevent the reaction from being affected by excessive temperature; the heating furnace is used to heat the methanol when starting the operation and to preheat the reactor before starting the operation. After the above-mentioned heat exchange, vaporization, superheating and temperature control operations, the methanol is kept at a suitable temperature to participate in the reaction, thereby ensuring the reaction rate. BRIEF DESCRIPTION OF THE DRAWINGS

[0019] In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the following briefly introduces the drawings required for use in the embodiments. It should be understood that the following drawings only illustrate certain embodiments of the present invention and therefore should not be regarded as limiting the scope. For ordinary technicians in this field, other relevant drawings can be obtained based on these drawings without paying any creative work.

[0020] FIG1 is a schematic diagram of a process according to an embodiment of the present invention;

[0021] FIG2 is a schematic flow diagram of a reaction system according to an embodiment of the present invention;

[0022] FIG3 is a schematic flow diagram of a reaction gas dust removal system according to an embodiment of the present invention;

[0023] FIG4 is a schematic flow chart of a flue gas dust removal system according to an embodiment of the present invention;

[0024] FIG5 is a schematic diagram of a sedimentation system flow chart according to an embodiment of the present invention;

[0025] FIG6 is a schematic flow chart of a feeding system according to an embodiment of the present invention.

[0026] Description of the drawings: 1-reaction system; 101-reaction settler; 102-regenerator; 103-riser reactor; 104-first cyclone separator; 105-second cyclone separator; 106-reaction gas collecting chamber; 107-first external heat exchanger; 108-second external heat exchanger; 109-cyclone separator group; 110-first feed pipe; 111-first discharge pipe; 112-second feed pipe; 113-second discharge pipe; 114-reaction stripping Section; 115-regeneration stripping section; 116-regeneration inclined pipe; 117-regeneration inclined pipe; 118-steam riser; 119-nitrogen riser; 120-main air distribution pipe; 121-methanol feed pipe; 122-regeneration catalyst distribution pipe; 123-flue gas collecting chamber; 2-reaction gas dust removal system; 201-first self-cleaning dust collector group; 202-reaction gas heat exchanger B; 203-steam generator; 204-first collection tank; 3-flue gas dust removal system; 301 - Second self-cleaning dust collector assembly; 302 - Second collection tank; 303 - Double-acting slide valve; 304 - Pressure-reducing orifice plate; 305 - First water seal tank; 306 - Second water seal tank; 307 - CO incinerator; 308 - Waste heat boiler; 309 - Flue gas dust removal device; 310 - Chimney; 4 - Sedimentation system; 401 - Quench tower; 402 - Cooling and deaeration water pipe; 403 - First settler; 404 - Water zone; 405 - Tray; 406 - Catalyst zone; 407-first delivery pump; 408-second delivery pump; 409-olefin separation heat exchanger; 410-air cooler; 411-water scrubber; 412-second settler; 413-mud tank; 414-third delivery pump; 5-feeding system; 501-purified water heat exchanger; 502-condensate heat exchanger; 503-steam vaporizer; 504-stripping gas vaporizer; 505-reaction gas heat exchanger A; 506-heating furnace; 507-quenching methanol delivery pipe. DETAILED DESCRIPTION

[0027] To make the objectives, technical solutions, and advantages of the embodiments of the present invention more clear, the technical solutions of the embodiments of the present invention will be clearly and completely described below in conjunction with the accompanying drawings of the embodiments of the present invention. Obviously, the described embodiments are only part of the embodiments of the present invention, not all of the embodiments. Generally, the components of the embodiments of the present invention described and shown in the drawings herein can be arranged and designed in various different configurations.

[0028] Therefore, the following detailed description of the embodiments of the present invention provided in the accompanying drawings is not intended to limit the scope of the invention as claimed, but rather merely represents selected embodiments of the present invention. All other embodiments derived by persons of ordinary skill in the art based on the embodiments of the present invention without creative effort shall fall within the scope of protection of the present invention.

[0029] In the description of the present invention, it should be noted that if the terms "center", "up", "down", "left", "right", "vertical", "horizontal", "inside", "outside" and the like appear, the orientation or position relationship indicated is based on the orientation or position relationship shown in the accompanying drawings, or is the orientation or position relationship in which the product of the application is usually placed when in use. It is only for the convenience of describing the present invention and simplifying the description, and does not indicate or imply that the device or element referred to must have a specific orientation, be constructed and operated in a specific orientation, and therefore cannot be understood as a limitation on the present invention.

[0030] The present invention will be described in detail below with reference to FIG. 1 to FIG. 6 .

[0031] Example

[0032] A methanol-to-olefins system includes a feed system 5, which includes a purified water heat exchanger 501, a condensate heat exchanger 502, a steam vaporizer 503, a reaction gas heat exchanger A505, and a methanol feed pipe 121, which are connected in sequence. The pipeline between the purified water heat exchanger 501 and the condensate heat exchanger 502 is connected to a quenched methanol delivery pipe 507 connected to the methanol feed pipe 121. The reaction gas heat exchanger A505 is connected to a heating furnace 506. The heating furnace 506 and the reaction gas heat exchanger A505 can be arranged in parallel or in series.

[0033] As shown in Figure 6, methanol is transported to purified water heat exchanger 501 for heating and then sequentially passes through condensate heat exchanger 502 for heating, steam vaporizer 503 for vaporization, and reaction gas heat exchanger A505 for further heating. Finally, it is transported out of methanol feed pipe 121. Rapid-cooling methanol delivery pipe 507 transports some of the heated methanol in purified water heat exchanger 501, mixing the low-temperature methanol with the high-temperature methanol and controlling the temperature at which the methanol finally participates in the reaction. The installation of heating furnace 506 not only heats the methanol at the start of production, but also heats the reaction unit before production begins to meet the initial reaction temperature requirements. The specific operation is as follows: nitrogen is first introduced into the feed system 5, and heating furnace 506 heats the nitrogen. The nitrogen enters the reaction unit through methanol feed pipe 121 to heat the entire reaction unit. After heating, methanol is added and the nitrogen is slowly removed.

[0034] In order to reduce the use of pure steam in the steam vaporizer 503, a stripping gas vaporizer 504 is set in parallel with the steam vaporizer 503. The stripping gas vaporizer 504 uses the stripping gas in the production process as the heat exchange medium, saving the use of pure steam, that is, reducing the energy consumption of the relevant steam production equipment.

[0035] The methanol to olefins system also includes a reaction system 1. As shown in Figure 2, the reaction system 1 includes a riser reactor 103, the gas outlet end of the riser reactor 103 is connected to a reaction settler 101, a primary cyclone separator 104 and a secondary cyclone separator 105 are provided in the reaction settler 101, the gas outlet end of the secondary cyclone separator 105 is connected to a reaction gas collecting chamber 106, a reaction stripping section 114 is provided at the bottom of the reaction settler 101, the reaction stripping section 114 is connected to an inclined pipe to be regenerated 117, the inclined pipe to be regenerated 117 is connected to a regenerator 102, a flue gas collecting chamber 123 and a cyclone separator group 109 connected to the flue gas collecting chamber 123 are provided in the regenerator 102, a regeneration stripping section 115 is provided at the bottom of the regenerator 102, and the regeneration stripping section 115 is connected to a regeneration inclined pipe 116 connected to the riser reactor 103.

[0036] Steam is delivered by a steam riser 118 at the bottom of the riser reactor 103. The delivered methanol-mixed catalyst reacts in the riser reactor 103, generating reaction gas. The reaction gas enters the reactor settler 101, where the catalyst and reaction gas are separated by a primary cyclone 104 and a secondary cyclone 105. This rapid separation of the reaction gas and catalyst significantly reduces side reactions and ensures methanol-to-olefins selectivity. The separated reaction gas enters the reaction gas collection chamber 106 for collection, while the catalyst falls into the reaction stripping section 114 for stripping. Steam is introduced into the reaction stripping section 114 to displace any entrained reaction gas within the catalyst, preventing methanol reaction gas from entering the regenerator 102 and causing waste of raw materials and increased cracking of olefins in the reaction product. In the first-stage cyclone separator 104, larger particles of catalyst are captured with an efficiency of 80% to 90%. The outlet gas phase enters the second-stage cyclone separator 105 along the riser. The single-stage cyclone separation efficiency is 80% to 90%. The total efficiency after separation in the first and second-stage cyclone separators is above 90% to 99%.

[0037] After stripping, the catalyst enters the regenerator 102 from the waiting inclined pipe 117. At this time, the nitrogen lifting pipe 119 connected to the waiting inclined pipe 117 outputs nitrogen to provide lifting power for the catalyst to enter the regenerator 102. The regenerator 102 is also provided with a main air distribution pipe 120 and a waiting catalyst distribution pipe 122 connected to the waiting inclined pipe 117. The raw catalyst distribution pipe 122 evenly sprays the transported catalyst to fully burn and regenerate the catalyst. The main air distribution pipe 120 is arranged below the raw catalyst distribution pipe 122, and the nozzle of the main air distribution pipe 120 is arranged opposite to the nozzle of the raw catalyst distribution pipe 122. The main air distribution pipe 120 sprays air or oxygen, so that the catalyst and air or oxygen are mixed in countercurrent and burned, ensuring the burning time and burning effect. The burned catalyst falls into the regeneration stripping section 115 for stripping to prevent air from being entrained into the regeneration inclined tube 116; after stripping, the catalyst enters the riser reactor 103 from the regeneration inclined tube 116 to continue participating in the reaction.

[0038] The reaction settler 101 is connected to a first feed pipe 110, which is connected to a first external heat exchanger 107. The regenerator 102 is connected to a second feed pipe 112, which is connected to a second external heat exchanger 108. The first external heat exchanger 107 and the second external heat exchanger 108 are provided to recover heat from a portion of the high-temperature catalyst to reduce heat waste. The first external heat exchanger 107 is connected to a first discharge pipe 111 connected to the riser reactor 103. After heat recovery, the high-temperature catalyst is cooled and transported to the riser reactor 103 to reduce the temperature in the riser reactor 103. The reaction time and reaction depth requirements can be flexibly adjusted according to changes in the methanol processing capacity, increasing operational flexibility and also increasing the methanol processing capacity. In addition, the first discharge pipe 111 and the regeneration inclined pipe 116 simultaneously transport the catalyst, ensuring the concentration of the catalyst in the riser reactor 103. The second external heat exchanger 108 is also connected to a second discharge pipe 113, which transports the cooled catalyst to the regenerator 102 for continued catalyst recycling. Annular grilles are installed in the reaction stripping section 114 and the regeneration stripping section 115, respectively. These grilles break up bubbles, increase vapor-solid contact, and enhance the stripping effect.

[0039] The methanol to olefins system also includes a reaction gas dust removal system 2. As shown in Figure 3, this system comprises a first self-cleaning dust collector assembly 201, which consists of three self-cleaning dust collectors arranged in parallel. A first collection tank 204 is connected to the bottom of the first self-cleaning dust collector assembly 201, and the gas outlet of the first self-cleaning dust collector assembly 201 is connected to a reaction gas heat exchanger B202, which is connected to a steam generator 203. The first self-cleaning dust collector assembly 201 is connected to the reaction gas collection chamber 106 and removes dust from the reaction gas. The first collection tank 204 collects catalyst dust. After being filtered by the first self-cleaning dust collector assembly 201, the catalyst has a temperature greater than 200°C, making it less likely to form bridges at this temperature, facilitating unloading from the first collection tank 204. The dedusted gas then passes through the reaction gas heat exchanger B202 for heat exchange and temperature increase. The steam generator 203 then vaporizes the reaction gas, maintaining a temperature of 120-150°C after steam production, reducing the load on the downstream water system. The reaction gas heat exchanger B202 recovers the heat from the reaction gas and generates steam through the steam generator 203, reducing energy consumption and lowering the temperature of the reaction gas, facilitating the operation of the compressor that transports the reaction gas.

[0040] The methanol to olefins system also includes a sedimentation system 4. As shown in Figure 5, the sedimentation system 4 includes a quenching tower 401 connected to the steam generator 203. The bottom of the quenching tower 401 is connected to a first settler 403. The water outlet end of the first settler 403 is connected to an olefin separation heat exchanger 409 and an air cooler 410 in sequence. The air cooler 410 is connected to the quenching tower 401. The gas outlet end of the quenching tower 401 is connected to a water washing tower 411. The bottom of the water washing tower 411 is connected to the water outlet end of a second settler 412, which is connected to the water washing tower 411. The slurry outlet ends of the first settler 403 and the second settler 412 are connected to a mud pool 413. The first settler 403 and the second settler 412 are provided with a water zone 404, a catalyst zone 406 and a tower plate 405. The water zone 404 and the catalyst zone 406 are separated by a filter screen to facilitate separation of the catalyst and water. The tower plate 405 is arranged above the water zone 404 and the catalyst zone 406 to buffer the flowing water to be filtered and ensure that the filter screen is not damaged.

[0041] The quenching water in quench tower 401 is introduced into first settler 403. After separation, the slurry carrying a large amount of catalyst is sent to mud pool 413. The separated water is transported by second delivery pump 408 to olefin separation heat exchanger 409 for heat exchange and cooling, thereby reducing the use of steam in olefin separation heat exchanger 409. After cooling in air cooler 410, it is returned to quench tower 401 for reuse. Quench tower 401 is equipped with five layers of scrubbing trays. Cooled deoxygenated water is delivered to the scrubbing trays by cooling deoxygenated water pipe 402 for scrubbing, effectively reducing the amount of catalyst carried by the reaction gas. After scrubbing, the reaction gas enters water scrubber 411 for water washing. First delivery pump 407 delivers gasoline produced in water scrubber 411. The wash water in water scrubber 411 enters second settler 412 for sedimentation. The separated water is transported by third delivery pump 414 to water scrubber 411 for further use. The slurry containing catalyst in second settler 412 is then sent to mud pool 413. By performing the sedimentation separation on the quenching water and the washing water, most of the slurry containing the catalyst is separated out, and the quenching water and the washing water are recycled, so that the sedimentation system 4 can operate for a long period of time.

[0042] The methanol to olefins system also includes a flue gas dust removal system 3. As shown in Figure 4, the flue gas dust removal system 3 includes a second self-cleaning dust collector group 301. The second self-cleaning dust collector group 301 is composed of three self-cleaning dust collectors arranged in parallel. The bottom of the second self-cleaning dust collector group 301 is connected to a second collecting tank 302, and the gas outlet end of the second self-cleaning dust collector group 301 is connected to a first water seal tank 305, a CO incinerator 307, a waste heat boiler 308, a flue gas dust removal device 309 and a chimney 310 in sequence.

[0043] The second self-cleaning dust collector assembly 301 is connected to the flue gas collection chamber 123, filtering out the catalyst from the flue gas. The catalyst is then collected in the second collection tank 302. The filtered flue gas passes through the first water seal tank 305 and enters the CO incinerator 307 for combustion. The heat from the combustion is recovered by the waste heat boiler 308. Finally, the flue gas dust removal device 309 removes dust from the post-combustion gases before they are discharged through the chimney 310. The first water seal tank 305 is provided to prevent explosions during furnace ignition.

[0044] The outlet of the second self-cleaning dust collector assembly 301 is also connected to a second water seal tank 306, which is connected to a chimney 310. The second water seal tank 306, connected to the chimney 310, provides another channel for flue gas. This channel is used to discharge flue gas after an accident occurs in the channel of the first water seal tank 305.

[0045] The outlet duct of the second self-cleaning dust collector assembly 301 is equipped with a double-acting slide valve 303 and a pressure-reducing orifice plate 304. Double-acting slide valve 303 is located between the second self-cleaning dust collector assembly 301 and the pressure-reducing orifice plate 304. Double-acting slide valve 303 is used to regulate the air pressure between the second self-cleaning dust collector assembly 301 and the water seal tank. Pressure-reducing orifice plate 304 reduces the flue gas pressure, preventing excessive pressure differentials that could damage equipment and affect production.

[0046] The catalyst involved in the reaction is a methanol to olefins acidic catalyst (RMTO) based on small-pore SAPO-34 molecular sieve. The catalyst is used in a riser fluidized bed at a reaction pressure of 0.1-0.4 MPa, a temperature of 400-500°C, and a mass space velocity of 1-8 h -1 The methanol to olefins catalyst comprises the following components in mass fractions based on the total mass on dry basis: 20-30% alumina, 10-20% first auxiliary agent, 50-60% second auxiliary agent, and the remainder being a fluidized bed carrier; the first auxiliary agent is a SAPO-34 molecular sieve having a good pore size distribution, which enables the catalyst to have a higher selectivity for the target product; the second auxiliary agent is an inert agent, which significantly enhances the strength and stability of the catalyst, thereby extending the service life of the catalyst and increasing the catalyst circulation rate from the original 50t / h to about 300t / h. Due to the increase in the catalyst circulation rate, the heat capacity of the catalyst in the riser reactor 103 is increased, achieving a large catalyst-to-alcohol ratio operation similar to that of a catalytic cracking unit, and realizing the reaction temperature control of the riser reactor 103, and also increasing the excellent selectivity and stability of the catalyst.

[0047] The present application improves production efficiency, reduces production energy consumption, improves olefin selectivity, and reduces operating costs by configuring a reaction gas dust removal system 2, a flue gas dust removal system 3, a sedimentation system 4, and a feeding system 5 for the reaction system 1.

[0048] The above are merely preferred embodiments of the present invention and are not intended to limit the present invention. Those skilled in the art will readily appreciate that various modifications and variations of the present invention are possible. Any modifications, equivalent substitutions, or improvements made within the spirit and principles of the present invention shall be included within the scope of protection of the present invention.

Claims

1. A methanol to olefin system, characterized in that: The invention comprises a feeding system (5), wherein the feeding system (5) comprises a purified water heat exchanger (501), a condensed water heat exchanger (502), a steam vaporizer (503), a reaction gas heat exchanger A (505) and a methanol feed pipe (121) which are connected in sequence, wherein the pipeline between the purified water heat exchanger (501) and the condensed water heat exchanger (502) is connected to a quenched methanol delivery pipe (507) which is connected to the methanol feed pipe (121), and the reaction gas heat exchanger A (505) is connected to a heating furnace (506).

2. A methanol to olefin system according to claim 1, characterized in that: A stripping gas vaporizer (504) is arranged in parallel with the steam vaporizer (503).

3. A methanol to olefin system according to claim 1, characterized in that: The methanol to olefin system further comprises a reaction system (1), wherein the reaction system (1) comprises a riser reactor (103), wherein the gas outlet end of the riser reactor (103) is connected to a reaction settler (101), wherein a primary cyclone separator (104) and a secondary cyclone separator (105) are arranged in the reaction settler (101), wherein the gas outlet end of the secondary cyclone separator (105) is connected to a reaction gas collecting chamber (106), and a reaction stripping section is arranged at the bottom of the reaction settler (101). (114), the reaction stripping section (114) is connected to an inclined tube to be regenerated (117), the inclined tube to be regenerated (117) is connected to a regenerator (102), a flue gas collecting chamber (123) and a cyclone separator group (109) connected to the flue gas collecting chamber (123) are provided in the regenerator (102), a regeneration stripping section (115) is provided at the bottom of the regenerator (102), and the regeneration stripping section (115) is connected to a regeneration inclined tube (116) connected to the riser reactor (103).

4. A methanol to olefin system according to claim 3, characterized in that: The reaction settler (101) is connected to a first feed pipe (110), the first feed pipe (110) is connected to a first external heat exchanger (107), the regenerator (102) is connected to a second feed pipe (112), and the second feed pipe (112) is connected to a second external heat exchanger (108).

5. A methanol to olefin system according to claim 4, characterized in that: The first external heat extractor (107) is connected to a first discharge pipe (111) which is in communication with the riser reactor (103).

6. A methanol to olefin system according to claim 1, characterized in that: The methanol to olefin system further comprises a reaction gas dust removal system (2), the reaction gas dust removal system (2) comprising a first self-cleaning dust collector group (201), the bottom of the first self-cleaning dust collector group (201) is connected to a first collecting tank (204), the gas outlet end of the first self-cleaning dust collector group (201) is connected to a reaction gas heat exchanger B (202), and the reaction gas heat exchanger B (202) is connected to a steam generator (203).

7. A methanol to olefin system according to claim 6, characterized in that: The methanol to olefin system further comprises a settling system (4), wherein the settling system (4) comprises a quenching tower (401) connected to the steam generator (203), the bottom of the quenching tower (401) is connected to a first settler (403), the water outlet end of the first settler (403) is sequentially connected to an olefin separation heat exchanger (409) and an air cooler (410), the air cooler (410) is connected to the quenching tower (401), the gas outlet end of the quenching tower (401) is connected to a water washing tower (411), the bottom of the water washing tower (411) is connected to the water outlet end of a second settler (412), and the slurry outlet ends of the first settler (403) and the second settler (412) are connected to a mud pool (413).

8. A methanol to olefin system according to claim 1, characterized in that: The methanol to olefin system further comprises a flue gas dust removal system (3), the flue gas dust removal system (3) comprising a second self-cleaning dust collector group (301), the bottom of the second self-cleaning dust collector group (301) is connected to a second collecting tank (302), and the gas outlet end of the second self-cleaning dust collector group (301) is sequentially connected to a first water seal tank (305), a CO incinerator (307), a waste heat boiler (308), a flue gas dust removal device (309) and a chimney (310).

9. A methanol to olefin system according to claim 8, characterized in that: The air outlet end of the second self-cleaning dust collector group (301) is also connected to a second water seal tank (306) connected to the chimney (310).

10. A methanol to olefin system according to claim 8, characterized in that: A double-acting slide valve (303) and a pressure-reducing orifice plate (304) are provided in the air outlet duct of the second self-cleaning dust collector group (301), and the double-acting slide valve (303) is located between the second self-cleaning dust collector group (301) and the pressure-reducing orifice plate (304).

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