CN108404818B - Methanol-to-olefin reaction system - Google Patents
Methanol-to-olefin reaction system Download PDFInfo
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- CN108404818B CN108404818B CN201810102554.0A CN201810102554A CN108404818B CN 108404818 B CN108404818 B CN 108404818B CN 201810102554 A CN201810102554 A CN 201810102554A CN 108404818 B CN108404818 B CN 108404818B
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- 238000006243 chemical reaction Methods 0.000 title claims abstract description 101
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims abstract description 303
- 238000000926 separation method Methods 0.000 claims abstract description 75
- 239000007787 solid Substances 0.000 claims abstract description 68
- 150000001336 alkenes Chemical class 0.000 claims abstract description 63
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 claims abstract description 57
- 239000007789 gas Substances 0.000 claims description 81
- 238000003860 storage Methods 0.000 claims description 25
- 238000005192 partition Methods 0.000 claims description 12
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 claims description 6
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 6
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 claims description 3
- 239000000919 ceramic Substances 0.000 claims description 3
- 239000001257 hydrogen Substances 0.000 claims description 3
- 229910052739 hydrogen Inorganic materials 0.000 claims description 3
- 125000004435 hydrogen atom Chemical class [H]* 0.000 claims description 3
- 239000001294 propane Substances 0.000 claims description 3
- HBMJWWWQQXIZIP-UHFFFAOYSA-N silicon carbide Chemical compound [Si+]#[C-] HBMJWWWQQXIZIP-UHFFFAOYSA-N 0.000 claims description 3
- 229910010271 silicon carbide Inorganic materials 0.000 claims description 3
- 238000004939 coking Methods 0.000 abstract description 12
- 230000000694 effects Effects 0.000 abstract description 12
- 239000002994 raw material Substances 0.000 abstract description 10
- 230000009286 beneficial effect Effects 0.000 description 8
- 238000005265 energy consumption Methods 0.000 description 6
- 238000007086 side reaction Methods 0.000 description 6
- 239000003054 catalyst Substances 0.000 description 5
- 238000005516 engineering process Methods 0.000 description 5
- 238000005406 washing Methods 0.000 description 5
- 230000002349 favourable effect Effects 0.000 description 4
- 238000010791 quenching Methods 0.000 description 4
- 230000000171 quenching effect Effects 0.000 description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 4
- 239000000463 material Substances 0.000 description 3
- 238000000034 method Methods 0.000 description 3
- 230000035484 reaction time Effects 0.000 description 3
- 239000004215 Carbon black (E152) Substances 0.000 description 2
- 239000000571 coke Substances 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 229930195733 hydrocarbon Natural products 0.000 description 2
- 150000002430 hydrocarbons Chemical class 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000011143 downstream manufacturing Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000003921 oil Substances 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 238000004321 preservation Methods 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 230000000452 restraining effect Effects 0.000 description 1
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/005—Separating solid material from the gas/liquid stream
- B01J8/0055—Separating solid material from the gas/liquid stream using cyclones
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C1/00—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon
- C07C1/20—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon starting from organic compounds containing only oxygen atoms as heteroatoms
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/00327—Controlling the temperature by direct heat exchange
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention provides a reaction system for preparing olefin from methanol. The methanol-to-olefin reaction system comprises a methanol-to-olefin reaction device and a gas-solid separation device. The gas-solid separation device is provided with an olefin product outlet, the gas-solid separation device is arranged inside the methanol-to-olefin reaction device, and the olefin product outlet is communicated with the inlet end of the gas-solid separation device; the methanol-to-olefin reaction device and the gas-solid separation device form a heat exchange structure so as to cool the olefin product gas separated from the gas-solid separation device. The methanol feed gas can absorb the heat of the high-temperature olefin product gas in an olefin product system in the gas-solid separation device, so that the heat exchange between the olefin product gas and the methanol-to-olefin reaction device is realized, the temperature of the olefin product gas can be reduced, the risk of coking of a heat exchanger in a subsequent flow path is reduced, and the heat exchange effect is improved; because the raw material methanol is heated by utilizing the heat of the olefin product gas, the selectivity of the reaction for preparing the olefin from the methanol is improved.
Description
Technical Field
The invention relates to the field of methanol-to-olefin, and particularly relates to a reaction system for preparing olefin from methanol.
Background
The Methanol To Olefin (MTO) technology mainly comprises DMTO technology of the institute of chemical and physical in the university of China academy of sciences, SMTO technology of China petrochemical group, and MTO technology of U.S. UOP company. The three technologies are industrialized in China.
In the DMTO process, the temperature of the product gas discharged from the reactor is high (above 450 ℃), and hydrocarbon substances in the product gas can generate coke-forming reaction and side reaction. Therefore, when the high-temperature product gas passes through the product gas and methanol heat exchanger, coking can occur, and further, the heat transfer coefficient of the product gas and the methanol heat exchanger (vertical heat exchanger) is reduced and the heat exchange effect is poor. The poor heat exchange effect of the product gas and the methanol heat exchanger can cause the temperature of the gas-phase methanol passing through the product gas and methanol heat exchanger to be only about 120 ℃, and after the gas-phase methanol enters the reactor, the gas-phase methanol can reach the required reaction temperature by consuming a large amount of reaction heat. Meanwhile, the poor heat exchange effect has great limitation on reducing energy consumption and improving olefin selectivity.
Disclosure of Invention
The invention mainly aims to provide a methanol-to-olefin reaction system, which aims to solve the problem that a product gas and methanol heat exchanger in the existing methanol-to-olefin reaction system are easy to coke, so that the heat exchange effect is poor.
In order to achieve the above object, the present invention provides a reaction system for producing olefins from methanol, comprising: the methanol-to-olefin reaction device is provided with an olefin product outlet; the gas-solid separation device is arranged inside the methanol-to-olefin reaction device, and an olefin product outlet is communicated with the inlet end of the gas-solid separation device; the methanol-to-olefin reaction device and the gas-solid separation device form a heat exchange structure so as to cool the olefin product gas separated from the gas-solid separation device.
Further, the methanol-to-olefin reaction device comprises: the methanol storage chamber is provided with a feeding hole; the reaction chamber is provided with a methanol inlet and an olefin product outlet, the reaction chamber is communicated with the methanol storage chamber through the methanol inlet, and at least part of the gas-solid separation device is arranged in the methanol storage chamber.
Further, a methanol input pipeline is arranged in the methanol storage chamber, the feed inlet is communicated with the methanol input pipeline, and part of the methanol input pipeline is coiled outside the gas-solid separation device.
Further, the gas-solid separation device is a cyclone separator or a quick separator.
Further, the gas-solid separation device comprises a separation part and a dipleg communicated with the separation part, the separation part is arranged in the methanol storage chamber and communicated with the olefin product outlet, and at least part of the dipleg is arranged in the reaction chamber.
Further, the dipleg is a corrugated pipe.
Further, the gas-solid separation device also comprises a dipleg sleeve, and the dipleg sleeve is sleeved outside the dipleg.
Further, a wear-resistant layer is arranged on the dipleg; preferably, the wear resistant layer is selected from a concrete layer, a ceramic layer or a silicon carbide layer.
Further, fins are arranged on the outer wall of the gas-solid separation device.
Further, methanol-to-olefin reaction unit still includes the baffle, and the baffle sets up in the inside of methanol storage room, and in the axis direction of methanol storage room, the baffle sets up in the free end below of methanol input pipeline.
Further, the space between the partition plate and the reaction chamber located below the partition plate is filled with an insulating gas.
Further, the heat insulating gas is selected from one or more of a mixed gas of methane and hydrogen, propane, and ethane.
By applying the technical scheme of the invention, when the gas-solid separation device is arranged in the methanol-to-olefin reaction device, the pressure bearing problem of equipment does not need to be considered, so that the wall thickness of the gas-solid separation device is smaller, and the effective heat exchange between the methanol-to-olefin reaction device and the gas-solid separation device can be realized. In the reaction system for preparing the olefin from the methanol, which is provided by the invention, the reaction device for preparing the olefin from the methanol and the gas-solid separation device form a heat exchange structure, the methanol raw material gas can absorb the heat of the high-temperature olefin product gas in an olefin product system in the gas-solid separation device, so that the heat exchange between the olefin product gas and the reaction device for preparing the olefin from the methanol is realized, the temperature of the olefin product gas can be reduced, the risk of coking of a heat exchanger in a subsequent flow path is favorably reduced, and the heat exchange effect is improved; meanwhile, the temperature of the raw material methanol is raised by utilizing the heat of the olefin product gas, so that the reaction heat of the methanol-to-olefin is prevented from being absorbed, and the selectivity of the methanol-to-olefin reaction is improved. In addition, after heat exchange, partial energy consumption of the raw material gas in the methanol-to-olefin reaction device for raising the temperature to the reaction temperature can be saved, so that the reaction time can be shortened, and the occurrence of side reactions can be reduced.
Drawings
The accompanying drawings, which are incorporated in and constitute a part of this application, illustrate embodiments of the invention and, together with the description, serve to explain the invention and not to limit the invention. In the drawings:
fig. 1 is a schematic diagram illustrating a methanol-to-olefin reaction system according to an exemplary embodiment of the present invention;
fig. 2 is a schematic structural diagram of a methanol-to-olefin reaction system according to another preferred embodiment of the present invention.
Wherein the figures include the following reference numerals:
10. a methanol-to-olefin reaction device; 11. a methanol storage chamber; 12. a reaction chamber; 20. a gas-solid separation device; 21. a separation section; 22. a dipleg; 23. a dipleg sleeve; 30. a separator.
Detailed Description
It should be noted that the embodiments and features of the embodiments in the present application may be combined with each other without conflict. The present invention will be described in detail below with reference to the embodiments with reference to the attached drawings.
As described in the background art, the product gas and the methanol heat exchanger in the existing methanol-to-olefin reaction device are easy to coke, so that the heat exchange effect is poor. In order to solve the above technical problem, the present invention provides a reaction system for preparing olefins from methanol, as shown in fig. 1, including a methanol-to-olefins reaction apparatus 10 and a gas-solid separation apparatus 20, where the methanol-to-olefins reaction apparatus 10 includes an olefin product outlet 121. The gas-solid separation device 20 is arranged inside the methanol-to-olefin reaction device 10, and the olefin product outlet 121 is communicated with the inlet end of the gas-solid separation device 20. The methanol-to-olefin reaction device 10 and the gas-solid separation device 20 form a heat exchange structure to cool the olefin product gas separated from the gas-solid separation device 20.
Since solid particles are entrained in the product gas after the methanol-to-olefin reaction is completed, the product gas needs to be separated by a gas-solid separation device 20. And because the product gas has higher temperature, the higher temperature of the olefin product gas easily causes the risk of coking of the product gas and the methanol heat exchanger.
When the gas-solid separation device 20 is arranged inside the methanol-to-olefin reaction device 10, the pressure bearing problem of equipment does not need to be considered, so that the wall thickness of the gas-solid separation device 20 is smaller, and effective heat exchange between the methanol-to-olefin reaction device 10 and the gas-solid separation device 20 can be realized. In the reaction system for preparing the olefin from the methanol, which is provided by the invention, the reaction device 10 for preparing the olefin from the methanol and the gas-solid separation device 20 form a heat exchange structure, the methanol raw material gas can absorb the heat of the high-temperature olefin product gas in an olefin product system in the gas-solid separation device 20, so that the heat exchange between the olefin product gas and the reaction device 10 for preparing the olefin from the methanol is realized, the temperature of the olefin product gas can be reduced, the risk of coking of a heat exchanger in a subsequent flow path is favorably reduced, and the heat exchange effect is improved; meanwhile, the temperature of the raw material methanol is raised by utilizing the heat of the olefin product gas, so that the reaction heat of the methanol-to-olefin is prevented from being absorbed, and the selectivity of the methanol-to-olefin reaction is improved. In addition, after heat exchange, partial energy consumption of the raw material gas in the methanol-to-olefin reaction device 10 when the raw material gas is heated to the reaction temperature can be saved, so that the reaction time can be shortened, and the occurrence of side reactions can be reduced.
In the actual production process, the temperature of the product gas is preferably lowered to 400 ℃. Reducing the temperature to the temperature range is favorable for further reducing the coking reaction of hydrocarbon substances in the product gas, thereby further improving the heat exchange effect of the product gas/methanol gas and improving the heat recovery efficiency.
In the reaction system for preparing olefin from methanol, the heat exchange process of the methanol gas and the product gas can be realized only by forming the heat exchange structure between the methanol input pipeline 101 and the gas-solid separation device 20, and the coking risk is reduced.
In a preferred embodiment, as shown in fig. 1, the methanol to olefin reaction apparatus 10 includes a methanol storage chamber 11 and a reaction chamber 12. The methanol storage chamber 11 is provided with a feed port 111, and the feed port 111 communicates with the methanol input line 101. The reaction chamber 12 is provided with an olefin product outlet 121 and a methanol inlet 122, the reaction chamber 12 is communicated with the methanol storage chamber 11 through the methanol inlet 122, and at least part of the gas-solid separation device 20 is arranged inside the methanol storage chamber 11.
At least part of the gas-solid separation device 20 is arranged in the methanol storage chamber 11, so that the methanol gas entering the methanol storage chamber 11 can exchange heat with the gas-solid separation device 20, the temperature of the olefin product gas can be effectively reduced, and the risk of coking of a subsequent heat exchanger is reduced.
In a preferred embodiment, the methanol input pipeline 101 extends to the inside of the methanol storage chamber 11 through the feed inlet 111, and a part of the methanol input pipeline 101 is coiled outside the gas-solid separation device 20. Set up the outside of gas-solid separator 20 with methyl alcohol input pipeline 101 coiling, this one side can make the methyl alcohol gas in the methyl alcohol input pipeline 101 carry out the heat transfer with gas-solid separator for the first time, and the inside methyl alcohol gas of filling in methyl alcohol apotheca 11 can also carry out the heat transfer for the second time with gas-solid separator 20, is favorable to further improving the heat transfer degree of methyl alcohol feed gas and alkene product gas through above-mentioned two heat transfer processes to further reduce the risk of heat exchanger coking.
In the above reaction system for producing olefins from methanol, the gas-solid separation device 20 may be a gas-solid separation device 20 commonly used in the art. In a preferred embodiment, the gas-solid separation device 20 includes, but is not limited to, a cyclone. The gas-solid separation device 20 has a large external surface area, so that when the gas-solid separation device 20 is used for heat exchange between the product gas and the methanol gas, the heat exchange efficiency between the product gas and the methanol gas is further improved, the risk of coking of the product gas and the methanol gas heat exchanger is further reduced, the energy consumption for heating the methanol gas is reduced, and the generation of side reactions is reduced.
In a preferred embodiment, the gas-solid separation device 20 is a cyclone separator, as shown in fig. 1, and comprises a separation part 21 and a dipleg 22 communicated with the separation part 21, the separation part 21 is disposed in the methanol storage chamber 11, the separation part 21 is communicated with the olefin product outlet 121, and at least a part of the dipleg 22 is disposed in the reaction chamber 12. The dipleg 22 has less material and therefore has poor heat supply, resulting in a tendency for the catalyst in the dipleg 22 to be at too low a temperature and mud. By disposing part of the dipleg 22 in the reaction chamber 12, the catalyst can be heated by the reaction heat of the reaction chamber 12, which is beneficial to avoiding the phenomena of catalyst and mud.
In a preferred embodiment, when the gas-solid separation device 20 is a cyclone, the gas-solid separation device 20 comprises a dipleg 22 and the dipleg 22 is a bellows. The bellows has a good heat preservation effect, thereby being beneficial to reducing the risk of the catalyst in the dipleg 22 appearing and mud due to too low temperature.
In a preferred embodiment, as shown in FIG. 1, when the gas-solid separation device 20 is a cyclone, it comprises a dipleg 22 and a dipleg sleeve 23, the dipleg sleeve 23 is sleeved outside the dipleg 22. Set up dipleg sleeve pipe 23 in the dipleg 22 outside, be favorable to further improving dipleg 22's heat insulating ability to be favorable to restraining the heat transfer between methanol gas and the dipleg 22, avoid appearing the phenomenon that oil gas condensation leads to catalyst and mud.
In a preferred embodiment, the inner wall of the dipleg 22 is provided with a wear resistant layer. Preferably, the wear layer includes, but is not limited to, a concrete layer, a ceramic layer, or a silicon carbide layer. The materials have high thermal resistance and low cost, so that the wear-resistant layer formed by the materials is beneficial to prolonging the service life of the dipleg 22.
When the gas-solid separating device 20 is a cyclone, it is preferable that fins are provided on the outer wall of the cyclone. The fins arranged on the outer wall of the cyclone separation device are beneficial to further improving the heat transfer efficiency of the cyclone separator, and further improving the heat exchange efficiency of the product gas and the methanol gas.
In the above reaction system for preparing olefin from methanol, the heat exchange structure formed by the reaction device 10 for preparing olefin from methanol and the gas-solid separation device 20 is not only beneficial to reducing the coking risk of the product gas and the methanol gas heat exchanger, but also beneficial to reducing the energy consumption for heating methanol gas. In a preferred embodiment, as shown in fig. 2, the reaction system further includes a partition plate 30, the partition plate 30 is disposed inside the methanol storage chamber 11, and the partition plate 30 is disposed below the outlet end of the methanol input pipe 101 in the axial direction of the methanol storage chamber 11. The partition plate 30 is provided below the free end of the methanol feed line 101, which is advantageous for suppressing the heat exchange between the methanol gas and the dipleg 22, and is advantageous for further suppressing the temperature decrease of the dipleg 22.
In a preferred embodiment, the reaction system further comprises a reaction unit, and an insulating gas is filled between the partition plate 30 and the reaction chamber located therebelow. The insulating gas has a characteristic of large thermal resistance, and thus filling the insulating gas between the partition plate 30 and the reaction unit is advantageous for further suppressing the loss of temperature in the dipleg 22.
In a preferred embodiment, the insulating gas includes, but is not limited to, one or more of a mixture of methane and hydrogen, propane and ethane, and the like. The gas participates in the methanol-to-olefin reaction, and therefore, the gas is selected for filling, so that the temperature of the dipleg 22 can be further inhibited from being reduced, and a new side reaction is not generated in the methanol-to-olefin reaction.
When the gas-solid separation device 20 is a cyclone separator, the inner wall of the cyclone separator may be preferably provided with a heat-insulating wear-resistant lining with low thermal resistance, or not provided with a lining. When the inner wall of the gas-solid separation device 20 is provided with the heat-insulating wear-resistant lining, the thickness of the lining is preferably 10-30 mm. The thickness of the heat insulating liner is not limited to the above range, but when the heat insulating liner is set within the above range, the heat resistance of the liner is small, which is advantageous for improving the heat exchange efficiency of the methanol gas and the product gas.
In a preferred embodiment, the reaction system for preparing olefins from methanol further comprises a quenching unit and a water washing unit, and the quenching unit and the water washing unit are sequentially arranged on the olefin product gas conveying pipeline in the flowing direction of the olefin product gas. The methanol-to-olefin reaction device 10 and the gas-solid separation device 20 form a heat exchange structure, which is beneficial to further reducing the temperature of the product gas entering the quenching unit and reducing the loads of the quenching unit and the water washing unit. The arrangement of the cold washing unit and the water washing unit is also beneficial to further reducing the temperature of the product gas so as to be convenient for the application of downstream processes.
From the above description, it can be seen that the above-described embodiments of the present invention achieve the following technical effects:
the methanol feed gas can absorb the heat of the high-temperature olefin product gas in an olefin product system in the gas-solid separation device, so that the heat exchange between the olefin product gas and the methanol-to-olefin reaction device is realized, the temperature of the olefin product gas can be reduced, the risk of coking of a heat exchanger in a subsequent flow path is reduced, and the heat exchange effect is improved; meanwhile, the temperature of the raw material methanol is raised by utilizing the heat of the olefin product gas, so that the reaction heat of the methanol-to-olefin is prevented from being absorbed, and the selectivity of the methanol-to-olefin reaction is improved. In addition, after heat exchange, partial energy consumption of the raw material gas in the methanol-to-olefin reaction device for raising the temperature to the reaction temperature can be saved, so that the reaction time can be shortened, and the occurrence of side reactions can be reduced.
The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention, and various modifications and changes may be made by those skilled in the art. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (11)
1. A reaction system for preparing olefins from methanol is characterized by comprising:
a methanol-to-olefin reaction device (10) provided with an olefin product outlet (121);
the gas-solid separation device (20) is arranged inside the methanol-to-olefin reaction device (10), and the olefin product outlet (121) is communicated with the inlet end of the gas-solid separation device (20);
the methanol-to-olefin reaction device (10) and the gas-solid separation device (20) form a heat exchange structure so as to cool the olefin product gas separated from the gas-solid separation device (20);
the methanol-to-olefin reaction apparatus (10) includes:
a methanol storage chamber (11) provided with a feed inlet (111);
the reaction chamber (12) is provided with the olefin product outlet (121) and a methanol inlet (122), the reaction chamber (12) is communicated with the methanol storage chamber (11) through the methanol inlet (122), and at least part of the gas-solid separation device (20) is arranged in the methanol storage chamber (11);
a methanol input pipeline (101) is arranged in the methanol storage chamber (11), the feed port (111) is communicated with the methanol input pipeline (101), and part of the methanol input pipeline (101) is coiled outside the gas-solid separation device (20).
2. The reaction system according to claim 1, wherein the gas-solid separation device (20) is a cyclone.
3. The reaction system according to claim 2, wherein the gas-solid separation device (20) comprises a separation part (21) and a dipleg (22) communicated therewith, the separation part (21) is arranged in the methanol storage chamber (11), the separation part (21) is communicated with the olefin product outlet (121), and at least part of the dipleg (22) is arranged in the reaction chamber (12).
4. A reaction system according to claim 3, wherein the dipleg (22) is a bellows.
5. The reaction system according to claim 3, wherein the gas-solid separation device (20) further comprises a dipleg sleeve (23), and the dipleg sleeve (23) is sleeved outside the dipleg (22).
6. A reaction system according to claim 5, characterised in that the dipleg (22) is provided with a wear resistant layer.
7. The reaction system of claim 6 wherein the wear resistant layer is selected from a concrete layer, a ceramic layer or a silicon carbide layer.
8. Reaction system according to claim 2, wherein fins are provided on the outer wall of the gas-solid separation device (20).
9. The reaction system according to claim 1, wherein the methanol-to-olefin reaction apparatus (10) further comprises a partition plate (30), the partition plate (30) is disposed inside the methanol storage chamber (11), and the partition plate (30) is disposed below a free end of the methanol input pipe (101) in an axial direction of the methanol storage chamber (11).
10. A reaction system according to claim 9, wherein the partition (30) and the reaction chamber (12) therebelow are filled with an insulating gas therebetween.
11. The reaction system of claim 10, wherein the insulating gas is selected from one or more of a mixed gas of methane and hydrogen, propane, and ethane.
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| CN201810102554.0A CN108404818B (en) | 2018-02-01 | 2018-02-01 | Methanol-to-olefin reaction system |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104478643A (en) * | 2014-12-12 | 2015-04-01 | 神华集团有限责任公司 | Device and method for preparing alkene from methanol and/or dimethyl ether |
| CN104474978A (en) * | 2014-12-12 | 2015-04-01 | 神华集团有限责任公司 | Device and method for preparing alkene from methanol and/or dimethyl ether |
| CN104549073A (en) * | 2015-01-05 | 2015-04-29 | 中国石油大学(华东) | Circulating fluidized bed reaction device for preparing olefins by using paraffin dehydrogenation |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| US6768036B2 (en) * | 2001-12-31 | 2004-07-27 | Exxonmobil Chemical Patents Inc. | Method for adding heat to a reactor system used to convert oxygenates to olefins |
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Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104478643A (en) * | 2014-12-12 | 2015-04-01 | 神华集团有限责任公司 | Device and method for preparing alkene from methanol and/or dimethyl ether |
| CN104474978A (en) * | 2014-12-12 | 2015-04-01 | 神华集团有限责任公司 | Device and method for preparing alkene from methanol and/or dimethyl ether |
| CN104549073A (en) * | 2015-01-05 | 2015-04-29 | 中国石油大学(华东) | Circulating fluidized bed reaction device for preparing olefins by using paraffin dehydrogenation |
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