CN207973691U - The lighter hydrocarbons piece-rate system of MTO product mix gas - Google Patents
The lighter hydrocarbons piece-rate system of MTO product mix gas Download PDFInfo
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- CN207973691U CN207973691U CN201820168191.6U CN201820168191U CN207973691U CN 207973691 U CN207973691 U CN 207973691U CN 201820168191 U CN201820168191 U CN 201820168191U CN 207973691 U CN207973691 U CN 207973691U
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
- Y02P30/40—Ethylene production
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Abstract
The utility model discloses a kind of lighter hydrocarbons piece-rate systems of MTO product mixes gas, the purpose of to produce ethylene and propylene product, this method is MTO reactor outlet gas through cooling, compression, washing, three phase separation is carried out after alkali cleaning, lime set is sent to lime set Cutting Tap, debutanizing tower detaches, gas phase is sent to high pressure depropanizer, the tower base stream of high pressure depropanizer is sent through low pressure depropanizer to debutanizing tower, the top gaseous phase logistics of high pressure depropanizer is sent to dethanizer, the top gaseous phase logistics of dethanizer is successively through domethanizing column, solvent recovery tower, ethylene rectifying column isolates ethylene product, the tower base stream of dethanizer isolates propylene product through propylene rectification tower.There is the advantages that low energy consumption, high ethylene, propylene recovery rate, the cycle of operation is long using the utility model method.
Description
Technical field
It is specifically a kind of to go out from MTO reactors the utility model is related to a kind of lighter hydrocarbons piece-rate system of MTO product mixes gas
Mouth gaseous mixture (includes methanol, dimethyl ether, hydrogen, nitrogen, methane, carbon monoxide, carbon dioxide, ethylene, ethane, acetylene, third
Alkene, propane, propine, C4、C5 +Deng) in isolate the piece-rate system of polymer grade ethylene and polymerization-grade propylene product.
Background technology
The 1970s Mobil companies the catalyst is chanced on during ZSM-5 catalyst preparations can be by methanol
It is converted into the hydrocarbon product of gasoline fraction, methanol-to-olefins (MTO) process is thus developed, has caused MTO new processes since then
Study tide.In recent years, MTO technology has become alkene and produces one of important route, with Chinese Academy of Sciences's Dalian chemistry
The DMTO techniques that physics Institute develops are the most typical, realized wide range of industrial applications.
Currently, MTO reactors are mostly using SAPO-n catalyst series, (e.g., DMTO is catalyzed using SAPO-34
Agent), reaction gas composition mainly have methanol, dimethyl ether, hydrogen, nitrogen, methane, carbon monoxide, carbon dioxide, ethylene, ethane,
Acetylene, propylene, propane, propine, C4、C5 +Deng.How from MTO reaction gas as far as possible low energy consumption, efficient isolate Gao Pin
The olefin product (polymer grade ethylene and polymerization-grade propylene product) of matter becomes MTO Olefin Separation Technologies and develops faced difficult point.
The MTO Olefin Separation Technologies of commercial Application mainly have the companies such as Lummus, KBR, Wison predepropanization separation process,
The front-end deethanization separation process etc. of Sinopec Luoyang Engineering Co., Ltd.
Lummus predepropanization technological processes are the most separation of olefins flows of current commercial Application, and early stage, the technique was de-
Methane tower carries out the deep cooling separating method used when carbon one is detached with C 2 hydrocarbon class, needs mating propylene refrigeration compressor and ethylene system
Cold compressor provides the cold of a variety of different temperatures grades, such as -100 DEG C of ethylene cold, causes piece-rate system complicated and equipment
Investment is big.In recent years, it is improved on the basis of former deep cooling process for separating, cold oil absorption pattern during domethanizing column uses, MTO is anti-
Device exit gas is answered to be sent into depropanizing tower after cooling, compression, washing, alkali cleaning, drying, depropanizing tower substrate is streamed to debutanization
Tower isolates mixing C4Component, depropanization overhead stream remove hydrogen through domethanizing column, send to dethanizer after one component of carbon, send to
Ethylene rectifying column isolates ethylene product, and deethanizer bottoms send to propylene rectification tower and isolate propylene product.Lummus works
Skill feature is：Use propylene for cryogen (i.e. 7 DEG C, -24 DEG C, -40 DEG C of three potential temperature grades), high and low pressure depropanizing tower is cold with 7 DEG C
Agent, dethanizer condenser -24 DEG C of cryogens of use, domethanizing column and ethylene rectifying column condenser etc. all use -40 DEG C of cryogens；Reaction gas
It carries out four sections of compressions and reaches domethanizing column inlet pressure, demethanation tower top uses the bottom of tower C of part dethanizer3Fraction and propylene
The bottom of tower propane of rectifying column is as absorbent.The flow is simple, and changes to feed composition adaptable；But due to domethanizing column
Top circulation loop of absorbent is long, easily leads to the separative element fluctuation of service in cycle and load is big.
The technological process of KBR predepropanizations uses the pre-separation of condensate stripper elder generation to go out part C compared with Lummus flows4
And C4The above component mitigates depropanizing tower load, and reaction gas compresses the operation requirement for reaching domethanizing column, piptonychia using three sections
Alkane tower is divided into two sections, i.e. stripping section and absorber portion.
The technological process of Wison predepropanizations compared with Lummus flows, propylene refrigerant have 7 DEG C, -6 DEG C, -24 DEG C, -40
DEG C four potential temperature grades, demethanation system first isolate big portion using precuting tower using precut+oily absorption and separation form, i.e.,
Divide C2And C2The above component is then fed into cold oil during oil-absorption tower carries out and absorbs ethylene in recycling tail gas.
The front-end deethanization separation process of Sinopec Luoyang Engineering Co., Ltd, MTO reactor outlet gas is through cooling, pressure
It is sent into dethanizer after contracting, washing, alkali cleaning, drying, the overhead stream of dethanizer is successively through domethanizing column, dethanizer, second
Alkene rectifying column isolates ethylene product, and the bottoms of dethanizer streams supreme pressure depropanizing tower, the tower top of high pressure depropanizer
Logistics is sent to propylene rectification tower and isolates propylene product, and the overhead materials of low pressure depropanizer, which are streamed to debutanizing tower, isolates mixing
C4Component.
In conclusion although existing MTO Olefin Separation Technologies are all improved in demethanation separative element, due to all adopting
It is middle cold oil absorption process, demethanation tower top circulation loop of absorbent is long to lead to later separation unit (especially propylene
Rectifying column) the problems such as load is big, device stability is poor, high energy consumption do not solve still, therefore, MTO Olefin Separation Technologies still have compared with
Big optimization, improved space.
Utility model content
The purpose of this utility model is that：A kind of lighter hydrocarbons piece-rate system of MTO product mixes gas is provided, the prior art is solved
Present in above-mentioned technical problem.
To achieve the above object, the technical solution adopted in the utility model is：
A kind of lighter hydrocarbons piece-rate system of MTO product mixes gas, have the chilling tower being connected with MTO product mixes gas sequence,
Compressor, water scrubber and caustic wash tower, it is characterised in that：
The tower overhead gas of the caustic wash tower is connected to three phases separator, the bottom of tower lime set connection of the three phase separator
To lime set Cutting Tap, the C that is cut into from the bottom of tower of the lime set Cutting Tap4Above component is connected to debutanizing tower, from institute
State the C that the tower top of lime set Cutting Tap comes out3Component below is back to the upstream of the caustic wash tower；
It is connected to high pressure depropanizer, the tower top of the high pressure depropanizer after the tower overhead gas drying of the three phase separator
Gaseous stream connects dethanizer；
The tower base stream of the dethanizer is connected to propylene rectification tower, and top gaseous phase logistics is connected to domethanizing column；
The tower base stream of the domethanizing column is sequentially connected acetylene converter and ethylene rectifying column.
The lighter hydrocarbons piece-rate system of the MTO product mix gas, wherein：The tower base stream of the high pressure depropanizer with it is low
The overhead stream heat exchange connection of depropanizing tower, the tower base stream of the low pressure depropanizer is pressed to be connected to the debutanizing tower.
The lighter hydrocarbons piece-rate system of the MTO product mix gas, wherein：The top gaseous phase logistics of the high pressure depropanizer
It is connected to the dethanizer by compressor；Alternatively, the top gaseous phase logistics of the dethanizer is connected to by compressor
The domethanizing column.
The lighter hydrocarbons piece-rate system of the MTO product mix gas, wherein：The tower base stream of the domethanizing column is connected to molten
The top gaseous phase logistics of agent recovery tower, the solvent recovery tower is then connected to the acetylene converter, the solvent recovery tower
Bottom of tower absorbent stream is all back to the tower top of the domethanizing column.
The lighter hydrocarbons piece-rate system of the MTO product mix gas, wherein：The ethylene rectifying column is from tower top to bottom of tower number
The 80th~110 shelf theory column plate at install in boil device, middle boiling device position stream temperature is adopted within the scope of -35~-26 DEG C
With -24 DEG C of cryogen heat supplies；Ethylene distillation bottom reboiler uses 7 DEG C of cryogen heat supplies.
The lighter hydrocarbons piece-rate system of the MTO product mix gas, wherein：The propylene rectification tower includes 1#Propylene rectification tower
With 2#The tower base stream of propylene rectification tower, the dethanizer is connected to described 2#Propylene rectification tower, described 2#Propylene rectification tower
Tower top liquid phase output polymerization-grade propylene, tower base stream are connected to described 1#Propylene rectification tower, described 1#The overhead materials of propylene rectification tower
Stream is back to described 2#Propylene rectification tower.
The utility model compared with prior art, has the superiority of the following aspects：
(1) order of placement for using depropanizing tower-dethanizer-domethanizing column, can reduce separative element load, reduce
Energy loss.
(2) method described in the utility model is used, solvent recovery tower is added after domethanizing column, absorbent can be solved and followed
Later separation unit (especially propylene rectification tower) load is big, device stability is poor caused by loop back path is long, high energy consumption etc. is asked
Topic.
(3) method described in the utility model is used, device is boiled in ethylene rectifying column and reboiler uses propylene refrigerant heat supply,
Can effective recovery waste heat, reduce propylene refrigerant dosage, reduce propylene refrigeration compressor power consumption.
(4) method described in the utility model is used, C is first isolated using dethanizer3It is sent after component to domethanizing column,
Domethanizing column and solvent recovery tower segregational load can be mitigated.
(5) use method described in the utility model, depropanizing tower that can realize depropanizing tower using high and low pressure double tower form
Interior Temperature Distribution and cryogen matching are more reasonable, and high pressure depropanizer bottom reboiler need to only use chilled water (chw) heat supply；With single de- third
Alkane tower is compared, and the double depropanizing tower total loads of high and low pressure are lower, and high pressure depropanizer top does not need liquid phase discharging, and low pressure de- third
Low-pressure steam dosage significantly reduces in alkane tower bottom reboiler, can save energy consumption to a certain extent；In addition, using high and low pressure-off
The combination of propane tower and lime set Cutting Tap can also reduce C4And C4The above unsaturated hydrocarbons (such as butadiene) generates in depropanizing tower
Polymer, fouling and clogging column plate, cause separative efficiency reduce, segregational load increase the problem of, so as to extend device operation week
Phase.
(6) method described in the utility model is used, under the premise of not increasing equipment investment, with MTO generally used now
Separation of olefins technology (cold oil absorption pattern demethanation in mainly) is compared, and comprehensive energy consumption reduces 1~3%.
(7) using method described in the utility model, it can be achieved that ethylene, propylene recovery rate are both greater than 99.6%.
Description of the drawings
Fig. 1 is the olefin separation system flow diagram (method one) of MTO product gas provided by the utility model.
Fig. 2 is the olefin separation system flow diagram (method two) of MTO product gas provided by the utility model.
Reference sign：1-MTO product mix gas；2- chilling towers；3- water strippers；4- purified waters；5- Methanol Recoveries
Tower；One section of 6- compressors；Two sections of 7- compressors；8- water scrubbers；Three sections of 9- compressors；10- caustic wash towers；11- Spent caustic treatments
Tower；12- spent lyes；13- three phases separators；14- lime set Cutting Taps；15- gas phase driers；16- high pressure depropanizers；
17- heat exchangers；18- low pressure depropanizers；19- dethanizers；Four sections of 20- compressors；21- domethanizing columns；22- solvent recoveries
Tower；23- acetylene converters；24- ethylene rectifying columns；25-2#Propylene rectification tower；26-1#Propylene rectification tower；27- debutanizing towers；28-
Fuel gas (hydrogen, methane)；29- polymer grade ethylenes；30- ethane；31- polymerization-grade propylenes；32- propane；33- mixing C4Component；
34- mixing C5And C5The above component.
Specific implementation mode
As shown in Figure 1, MTO reactor outlet product mixes gas 1 is first sent into chilling tower 2 and methanol distillation column 5 carries out heat
Recycling and Methanol Recovery, then compressed through one section 6 of compressor, two section 7 and send to water scrubber 8 remove oxide impurity (such as methanol,
Dimethyl ether etc.), it is then sent to caustic wash tower 10 after three section of 9 compression of compressor and removes sour gas (such as carbon dioxide).
Caustic wash tower 10 export MTO products pneumatic transmission to three phases separator 13 carry out split-phase, the lime set isolated send to
Lime set Cutting Tap 14, tower top gauge pressure is within the scope of 0.6~1.0MPa, and column bottom temperature is within the scope of 75~85 DEG C, lime set cutting
Major part C in tower4And C4The above heavy constituent is cut to send to debutanizing tower 27, C3And C3Following light component is returned to pressure
Three section of 7 entrance of contracting machine is recycled.The gas phase that three phases separator is isolated is sent supreme after the drying of gas phase drier 15
Press depropanizing tower 16.
16 tower top gauge pressure of high pressure depropanizer is within the scope of 1.6~2.0MPa, and tower top temperature is within the scope of 10~18 DEG C, tower
Bottoms stream is exchanged heat with 18 overhead stream of low pressure depropanizer by heat exchanger 17, and the logistics after heat exchange is sent to low pressure depropanization
3rd~10 shelf theory column plate of the tower 18 from tower top to bottom of tower number.18 tower top pressure of low pressure depropanizer is in 0.6~0.9MPa ranges
Interior, within the scope of 12~20 DEG C, 18 bottoms of low pressure depropanizer is streamed to debutanizing tower 27, high pressure depropanizer tower top temperature
16 top gaseous phase logistics are sent to dethanizer 19 (method one as shown in Figure 1), or are sent to de- after four section of 20 boosting of compressor
Ethane tower 19 (method two as shown in Figure 2).
In method one, as shown in Figure 1,19 tower top gauge pressure of dethanizer is within the scope of 1.6~2.0MPa, tower top temperature
Within the scope of -38~-30 DEG C, bottoms is streamed to 2#Propylene rectification tower 25, top gaseous phase logistics is through four section of 20 compression of compressor
After send to domethanizing column 21.
In method two, as shown in Fig. 2, 19 tower top gauge pressure of dethanizer is within the scope of 2.7~3.3MPa, tower top temperature
Within the scope of -20~-10 DEG C, bottoms is streamed to 2#Propylene rectification tower 25, top gaseous phase logistics are sent to domethanizing column 21.
21 tower top gauge pressure of domethanizing column is within the scope of 2.6~3.2MPa, and tower top temperature is within the scope of -38~-30 DEG C, tower top
- 38~-30 DEG C of propane absorbents are added；The 28 direct carrying device of tower top fuel gas (hydrogen, methane) logistics of domethanizing column 21
Or into fuel gas system, bottoms is streamed to solvent recovery tower 22.
22 tower top gauge pressure of solvent recovery tower is within the scope of 2.2~2.8MPa, and tower top temperature is within the scope of -26~-16 DEG C, tower
The absorbent stream of bottom recycling, which is cooled to after -38~-30 DEG C, is all back to 21 tower top of domethanizing column, and top gaseous phase logistics is through second
It is sent after 23 hydrotreating of alkynes converter to ethylene rectifying column 24.
24 tower top gauge pressure of ethylene rectifying column within the scope of 1.2~1.8MPa, tower top temperature within the scope of -38~-30 DEG C,
Polymer grade ethylene product 29, bottom of tower ethane logistics are produced by survey line from from tower top to the 2nd~10 shelf theory column plate of bottom of tower number
30 are used as ethane product or send to fuel gas system；Ethylene rectifying column 24 is in the 80th~110 shelf theory from tower top to bottom of tower number
Device is boiled in being installed at column plate, middle boiling device position stream temperature is within the scope of -35~-26 DEG C, using -24 DEG C of cryogen heat supplies；
24 bottom reboiler of ethylene rectifying column uses 7 DEG C of cryogen heat supplies.(note：Cryogen in the utility model preferably uses propane, and
And propane cryogen sets 7 DEG C, -24 DEG C, -40 DEG C of three potential temperature grades.)
2#25 tower top gauge pressure of propylene rectification tower is within the scope of 1.5~2.0MPa, and tower top temperature is within the scope of 40~50 DEG C, tower
It pushes up liquid phase and produces polymerization-grade propylene 31, bottoms is streamed to 1#Propylene rectification tower 26.1#26 overhead stream of propylene rectification tower is back to
2#Propylene rectification tower 25,32 carrying device of bottom of tower propylene oxide stream or the loss of 22 absorbent of supplementing solvent recovery tower.
27 tower top gauge pressure of debutanizing tower is within the scope of 0.1~0.6MPa, and tower top temperature is within the scope of 40~50 DEG C, liquid of top of the tower
Mix C433 carrying device of component or into follow-up C4Crack unit, bottom of tower mixing C5And C534 carrying device of the above component.
Using the utility model, it can be achieved that under the premise of not increasing equipment investment, with MTO separation of olefins generally used now
Technology (cold oil absorption pattern demethanation in mainly) is compared, and comprehensive energy consumption reduces by 1~3%.
Using the utility model, obtained ethylene product meets national standard GB/T 7715-2014, and propylene product meets national standard
GB/T 7716-2014, ethylene, propylene recovery rate can all be more than 99.6%.
Using the utility model, MTO product mixes gas first isolates C in the high pressure depropanizer 163Following components, so
Afterwards C is isolated in the dethanizer 192Following components, then carry out C in the domethanizing column 212Point of component and methane, hydrogen
From can reduce separative element load, reduce energy loss.
It is described above to be merely exemplary for the utility model, and not restrictive, those of ordinary skill in the art
Understand, in the case where not departing from spirit and scope defined by claim, can many modifications may be made, variation or it is equivalent, but
It falls within the scope of protection of the utility model.
Claims (6)
1. a kind of lighter hydrocarbons piece-rate system of MTO product mixes gas has the chilling tower being connected with MTO product mixes gas sequence, pressure
Contracting machine, water scrubber and caustic wash tower, it is characterised in that：
The tower overhead gas of the caustic wash tower is connected to three phases separator, and the bottom of tower lime set of the three phase separator is connected to solidifying
Liquid Cutting Tap, the C being cut into from the bottom of tower of the lime set Cutting Tap4Above component is connected to debutanizing tower, is coagulated from described
The C that the tower top of liquid Cutting Tap comes out3Component below is back to the upstream of the caustic wash tower；
It is connected to high pressure depropanizer, the top gaseous phase of the high pressure depropanizer after the tower overhead gas drying of the three phase separator
Logistics connects dethanizer；
The tower base stream of the dethanizer is connected to propylene rectification tower, and top gaseous phase logistics is connected to domethanizing column；
The tower base stream of the domethanizing column is sequentially connected acetylene converter and ethylene rectifying column.
2. the lighter hydrocarbons piece-rate system of MTO product mixes gas according to claim 1, it is characterised in that：The high pressure-off third
The overhead stream heat exchange of the tower base stream and low pressure depropanizer of alkane tower connects, the tower base stream connection of the low pressure depropanizer
To the debutanizing tower.
3. the lighter hydrocarbons piece-rate system of MTO product mixes gas according to claim 1, it is characterised in that：The high pressure-off third
The top gaseous phase logistics of alkane tower is connected to the dethanizer by compressor；Alternatively, the top gaseous phase object of the dethanizer
Circulation overcompression machine is connected to the domethanizing column.
4. the lighter hydrocarbons piece-rate system of MTO product mixes gas according to claim 1, it is characterised in that：The domethanizing column
Tower base stream be connected to solvent recovery tower, the top gaseous phase logistics of the solvent recovery tower is then connected to the acetylene conversion
Device, the bottom of tower absorbent stream of the solvent recovery tower are all back to the tower top of the domethanizing column.
5. the lighter hydrocarbons piece-rate system of MTO product mixes gas according to claim 1, it is characterised in that：The ethylene distillation
Tower boils device in installing at the 80th~110 shelf theory column plate from tower top to bottom of tower number, middle boiling device position stream temperature-
Within the scope of 35~-26 DEG C, using -24 DEG C of cryogen heat supplies；Ethylene distillation bottom reboiler uses 7 DEG C of cryogen heat supplies.
6. the lighter hydrocarbons piece-rate system of MTO product mixes gas according to claim 1, it is characterised in that：The propylene rectifying
Tower includes 1#Propylene rectification tower and 2#The tower base stream of propylene rectification tower, the dethanizer is connected to described 2#Propylene rectification tower,
Described 2#The tower top liquid phase output polymerization-grade propylene of propylene rectification tower, tower base stream are connected to described 1#Propylene rectification tower, described 1#
The overhead stream of propylene rectification tower is back to described 2#Propylene rectification tower.
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| CN201820168191.6U CN207973691U (en) | 2018-01-31 | 2018-01-31 | The lighter hydrocarbons piece-rate system of MTO product mix gas |
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109780743A (en) * | 2019-01-16 | 2019-05-21 | 中国寰球工程有限公司 | Multistage position cryogen distributes structure rationally |
| CN111102868A (en) * | 2018-10-25 | 2020-05-05 | 中国石化工程建设有限公司 | System and method for recycling waste heat of propane dehydrogenation device |
| CN111336715A (en) * | 2020-03-17 | 2020-06-26 | 苏应玺 | Energy-saving refrigeration system suitable for olefin separation process |
| CN111394116A (en) * | 2019-08-12 | 2020-07-10 | 中国石化工程建设有限公司 | Oil gas recovery method and device |
| CN113788735A (en) * | 2021-09-30 | 2021-12-14 | 中安联合煤化有限责任公司 | Light hydrocarbon recovery and start-up method suitable for methanol-to-olefin reaction short-time shutdown period |
| EP3981860A4 (en) * | 2019-06-06 | 2023-06-14 | Sinopec Engineering Incorporation | Oil and gas processing method and device |
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2018
- 2018-01-31 CN CN201820168191.6U patent/CN207973691U/en active Active
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN111102868A (en) * | 2018-10-25 | 2020-05-05 | 中国石化工程建设有限公司 | System and method for recycling waste heat of propane dehydrogenation device |
| CN111102868B (en) * | 2018-10-25 | 2021-07-02 | 中国石化工程建设有限公司 | System and method for recycling waste heat of propane dehydrogenation device |
| CN109780743A (en) * | 2019-01-16 | 2019-05-21 | 中国寰球工程有限公司 | Multistage position cryogen distributes structure rationally |
| EP3981860A4 (en) * | 2019-06-06 | 2023-06-14 | Sinopec Engineering Incorporation | Oil and gas processing method and device |
| CN111394116A (en) * | 2019-08-12 | 2020-07-10 | 中国石化工程建设有限公司 | Oil gas recovery method and device |
| CN111336715A (en) * | 2020-03-17 | 2020-06-26 | 苏应玺 | Energy-saving refrigeration system suitable for olefin separation process |
| CN111336715B (en) * | 2020-03-17 | 2021-09-24 | 华亭煤业集团有限责任公司 | Energy-saving refrigeration system suitable for olefin separation process |
| CN113788735A (en) * | 2021-09-30 | 2021-12-14 | 中安联合煤化有限责任公司 | Light hydrocarbon recovery and start-up method suitable for methanol-to-olefin reaction short-time shutdown period |
| CN113788735B (en) * | 2021-09-30 | 2024-05-10 | 中安联合煤化有限责任公司 | Light hydrocarbon recovery start-up method suitable for short-time shutdown period of methanol-to-olefin reaction |
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