CN100586910C - Method for producing propylene by conversion of carbinol or dimethyl ether - Google Patents
Method for producing propylene by conversion of carbinol or dimethyl ether Download PDFInfo
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- CN100586910C CN100586910C CN200710143259A CN200710143259A CN100586910C CN 100586910 C CN100586910 C CN 100586910C CN 200710143259 A CN200710143259 A CN 200710143259A CN 200710143259 A CN200710143259 A CN 200710143259A CN 100586910 C CN100586910 C CN 100586910C
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- propylene
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- methyl alcohol
- dimethyl ether
- catalyst
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- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 title claims abstract description 152
- 238000006243 chemical reaction Methods 0.000 title claims abstract description 69
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 title claims abstract description 58
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 title claims abstract description 56
- LCGLNKUTAGEVQW-UHFFFAOYSA-N Dimethyl ether Chemical compound COC LCGLNKUTAGEVQW-UHFFFAOYSA-N 0.000 title claims abstract description 36
- 238000004519 manufacturing process Methods 0.000 title description 4
- 239000003054 catalyst Substances 0.000 claims abstract description 26
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 claims abstract description 24
- 239000000203 mixture Substances 0.000 claims abstract description 20
- 238000000034 method Methods 0.000 claims abstract description 19
- 238000007323 disproportionation reaction Methods 0.000 claims abstract description 17
- 239000004215 Carbon black (E152) Substances 0.000 claims abstract description 12
- 229930195733 hydrocarbon Natural products 0.000 claims abstract description 12
- 150000002430 hydrocarbons Chemical class 0.000 claims abstract description 12
- 238000000926 separation method Methods 0.000 claims abstract description 10
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 8
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 claims abstract description 6
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 claims abstract description 3
- 239000001257 hydrogen Substances 0.000 claims abstract description 3
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 3
- 125000004435 hydrogen atom Chemical class [H]* 0.000 claims abstract description 3
- 239000001294 propane Substances 0.000 claims abstract description 3
- 238000005516 engineering process Methods 0.000 claims description 18
- 239000002994 raw material Substances 0.000 claims description 13
- IAQRGUVFOMOMEM-UHFFFAOYSA-N butene Natural products CC=CC IAQRGUVFOMOMEM-UHFFFAOYSA-N 0.000 claims description 12
- VXNZUUAINFGPBY-UHFFFAOYSA-N 1-Butene Chemical compound CCC=C VXNZUUAINFGPBY-UHFFFAOYSA-N 0.000 claims description 10
- 239000007864 aqueous solution Substances 0.000 claims description 6
- 229910004298 SiO 2 Inorganic materials 0.000 claims description 5
- 238000007233 catalytic pyrolysis Methods 0.000 claims description 5
- 239000002808 molecular sieve Substances 0.000 claims description 5
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims description 5
- 239000000470 constituent Substances 0.000 claims description 4
- 238000004523 catalytic cracking Methods 0.000 claims description 3
- 239000007809 chemical reaction catalyst Substances 0.000 claims description 2
- 150000001336 alkenes Chemical class 0.000 abstract description 5
- 239000005977 Ethylene Substances 0.000 abstract description 4
- 238000002360 preparation method Methods 0.000 abstract description 3
- 125000000383 tetramethylene group Chemical group [H]C([H])([*:1])C([H])([H])C([H])([H])C([H])([H])[*:2] 0.000 abstract description 3
- 238000010504 bond cleavage reaction Methods 0.000 abstract 1
- 238000006555 catalytic reaction Methods 0.000 abstract 1
- -1 ethylene, propylene Chemical group 0.000 abstract 1
- 125000002496 methyl group Chemical group [H]C([H])([H])* 0.000 abstract 1
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 abstract 1
- 230000007017 scission Effects 0.000 abstract 1
- 239000007789 gas Substances 0.000 description 7
- PNEYBMLMFCGWSK-UHFFFAOYSA-N Alumina Chemical compound [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 4
- 239000003208 petroleum Substances 0.000 description 4
- 239000000376 reactant Substances 0.000 description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 4
- 239000003245 coal Substances 0.000 description 3
- 230000008929 regeneration Effects 0.000 description 3
- 238000011069 regeneration method Methods 0.000 description 3
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 229910021536 Zeolite Inorganic materials 0.000 description 1
- 150000001335 aliphatic alkanes Chemical class 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000000571 coke Substances 0.000 description 1
- 235000009508 confectionery Nutrition 0.000 description 1
- 229910052593 corundum Inorganic materials 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000003502 gasoline Substances 0.000 description 1
- 238000007654 immersion Methods 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 238000002444 silanisation Methods 0.000 description 1
- 238000002791 soaking Methods 0.000 description 1
- 238000001694 spray drying Methods 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- 229910001845 yogo sapphire Inorganic materials 0.000 description 1
- 239000010457 zeolite Substances 0.000 description 1
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Classifications
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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
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
-
- 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
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
- Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock
-
- 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
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- 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
Abstract
The invention relates to a method for preparing olefin by methyl alcohol or dimethyl ether, in particular to the propylene preparation in high selectivity. The reaction method comprises methyl alcoholor dimethyl ether conversion reaction, ethylene and butylene anti-dismutation reaction and C4 over restructuring catalysis scission reaction: the methyl alcohol generates hydrocarbon mixture with rich propylene through a catalyst following reaction; when the hydrocarbon mixture is separated from the propylene via a separation system, the non-propylene components (comprising light component with hydrogen, methane, ethane, ethylene, propane and Cox, and heavy component with C4) are reacted through the anti-dismutation catalyst, so that the ethylene generates propylene with the butylene throughthe anti-dismutation reaction, and the generative hydrocarbon mixture returns to the separation system for being separated so as to get propylen. The unreacted C4 components and other heavy componentsare catalyzed and cracked so as to generate the hydrocarbon mixture with ethylene, propylene and other light components; the generative ydrocarbon mixture returns to the separation system for separation to get propylen.
Description
Technical field
The present invention relates to a kind of method, particularly highly-selective preparation of propylene by methyl alcohol or dimethyl ether production alkene.
Background technology
Propylene is the basic raw material of modern chemistry industry.Up to the present, most propylene all comes from petroleum processing engineering.Along with the exhausted day by day of petroleum resources and oil price constantly soaring in the recent period, develop new non-petroleum path and produce the growing propylene of demand and seem very urgent.By methyl alcohol or dme is that to produce propylene (MTP) be the novel process that is hopeful to replace petroleum path most to raw material.Coal or Sweet natural gas preparing synthetic gas are produced methyl alcohol by synthetic gas again and dme is sophisticated Technology.Therefore, be the gordian technique of coal system alkene route from methyl alcohol or dimethyl ether production propylene.
Preparing propylene from methanol process and methanol-to-olefins (ethene, propylene) (MTO) process are compared, because product is single propylene, in the subsequent separation process of product, can avoid the low temperature separation process step, therefore, can simplify flow process, reduce investment outlay greatly; Preparing propylene from methanol technology is worked in coordination with MTO technology as the part of coal system alkene, can test the changes in demand in market better.
In PCT patent WO2004/018089, a kind of device for preparing propylene from methyl alcohol has been described by Lurgi company, methyl alcohol is produced the mixed vapour of methyl alcohol, dme and water after by the pre-reactor that is filled with aluminium oxide catalyst, this mixture reacts in placed in-line fixed-bed reactor and generates the low-carbon alkene that is rich in propylene, in order to solve the heat-obtaining problem of reaction, device has designed many groups heat collector.It is reported, utilize this device, unite non-propylene product and loop back the technology that reactive system continues reaction, the propylene overall selectivity can reach 70%.In PCT patent WO01/92190, the method that propylene takes place to be prepared by methyl alcohol a kind of similar fixed bed reaction has also been described by MG TECHNOLOGIES company.
Summary of the invention
The purpose of this invention is to provide a kind of is raw material with methyl alcohol or dme, the reaction process of highly-selective preparation of propylene.
For improving the propylene selectivity, the present invention adopts three reacting phase bonded reaction process: comprise methanol conversion reaction, ethene and butene inverse disproportionation reaction and C
4Above heavy component catalytic cracking reaction.First reaction, fluidized-bed or moving bed reaction technology are adopted in the methanol conversion reaction, make the reaction of methyl alcohol or dme generate the hydrocarbon mixture (catalyzer 1) that is rich in propylene.Hydrocarbon mixture is through being separated into three parts: a part is purpose product propylene; A part is light component (containing hydrogen, methane, ethane, ethene, propane and COx); A part is C
4Above heavy component (contains C
4, C
5And C
6Above alkane and alkene, and aromatic hydrocarbons).Second reaction is ethene and butene inverse disproportionation reaction, will contain the light component and the C that contains butylene of ethene
4Above heavy component reacts by anti-disproportionation catalyst (catalyzer 2), adopts fixed bed reaction technology, and the hydrocarbon mixture of generation turns back to separation system to be separated, to obtain propylene.The 3rd reaction is the catalytic cracking reaction of heavy component, to carry out catalytic pyrolysis (catalyzer 3) through the component of isolating propylene after the anti-disproportionation, generation contains the hydrocarbon mixture of light component such as ethene, propylene, adopt ciculation fluidized bed reaction technique, the hydrocarbon mixture that generates turns back to separation system to be separated, to obtain propylene.
The raw material that is adopted among the present invention is methyl alcohol, dme, methanol aqueous solution, and the three is according to the mixture of arbitrary proportion composition.
Be the high conversion of realization methyl alcohol and the highly selective of propylene, first reaction of the present invention, promptly catalyst system therefor (catalyzer 1) is ZSM-5 catalyzer or SAPO-34 molecular sieve catalyst in methyl alcohol or the dimethyl ether conversion system olefine reaction.Second reaction, ethene and butene inverse disproportionation reaction catalyst system therefor (catalyzer 2) are loaded WO
3, Re
2O
7Perhaps MoO
3Catalyzer, support of the catalyst can be SiO
2, Al
2O
3And H-Beta, ZSM-5, HY and MCM-22 equimolecular sieve, also can be SiO
2, Al
2O
3Mixture with molecular sieve.The 3rd reaction, non-propylene component catalyst cracking catalyst system therefor (catalyzer 3) is ZSM-5 or SAPO-34.
Feature of the present invention is that fluidized-bed reaction technology is adopted in the reaction of methyl alcohol or dimethyl ether conversion, to solve the problem of fixed bed reaction mode heat-obtaining difficulty, simultaneously the fluidized-bed reaction mode have mass transfer good, do not stop up, react characteristics such as pressure reduction is little.Another feature of the present invention is to adopt ethene and butene inverse disproportionation to generate the propylene technology, has further improved the propylene selectivity, brings up to about 82% from 70% propylene selectivity of prior art.
Description of drawings
Fig. 1 be schematic diagram of the present invention as, produce propylene by methyl alcohol or dimethyl ether in high selectivity.
Embodiment
Ins and outs of the present invention are by the following example detailed description in addition.
Embodiment 1～3 is methyl alcohol reaction system olefine reaction technology.
Embodiment 1
With SiO
2/ Al
2O
3=200 ZSM-5 zeolite is an active constituent, and through soaking La, Mg, technologies such as spray drying forming, water treatment, online silanization are made methanol conversion catalyst.Adopt fluidized-bed reaction technology, 70% methanol aqueous solution is a raw material.The fluidized-bed reaction condition is: 502 ℃ of temperature, pressure (gauge pressure) 0.03MPa, methanol feeding/catalyst recirculation amount 1.0, air speed (in pure methyl alcohol) 5h
-1, catalyzer is residence time 90min in reactor, reactant gases residence time 5s, 620 ℃ of catalyst regeneration temperature.
Embodiment 2
Employing ZSM-5 is an active constituent, with Al
2O
3Be cakingagent, adopt oily injection formation technology to make movable bed catalyst, this catalyzer is made the movable bed catalyst of preparing propylene by methanol transformation after modification.Adopt moving bed reaction technology, 70% methanol aqueous solution is a raw material, and temperature of reaction is 480 ℃, pressure (gauge pressure) 0.1MPa, methanol feeding air speed (in pure methyl alcohol) 5h
-1, catalyzer is mean residence time 30h in reactor, reactant gases residence time 3s.
Embodiment 3
With SAPO-34 is active constituent, is cakingagent with SiO2-Al2O3, the spray-dried methanol conversion catalyst of making.Adopt fluidized-bed reaction technology, 70% methanol aqueous solution is a raw material.The fluidized-bed reaction condition is: 400 ℃ of temperature, pressure (gauge pressure) 0.05MPa, methanol feeding/catalyst recirculation amount 1.0, air speed (in pure methyl alcohol) 10h
-1, catalyzer is residence time 10min in reactor, reactant gases residence time 1.5s, 610 ℃ of catalyst regeneration temperature.
Table 1
Embodiment 4～8 raw materials are formed the influence to the methanol conversion reaction
Be raw material with pure methyl alcohol, 30% methanol aqueous solution, dme, dme+water (the two mol ratio is 1: 1) respectively, other is identical with embodiment 1.
Table 2
Embodiment 9
Ethene and butene inverse disproportionation reaction
With immersion process for preparing WO
3-Al
2O
3-HY catalyzer, and with this as ethene and butene inverse disproportionation catalyst.Adopt the fixed bed reaction mode, reaction conditions is: 160 ℃ of temperature, pressure 0.6MPa, air speed 1h
-1, ethene is 0.2 (mol ratio that is ethene and 2-butylene is 1: 1) with the ratio of hybrid C 4 (forming identical with hybrid C 4 among the embodiment 1).Conversion of ethylene 92%, propylene selectivity are 90%.By this reaction, ethene and 2-butylene among the embodiment 1 are converted into propylene, thereby make the total propylene selectivity of reaction reach 63%.
Embodiment 10
C
4Above heavy component catalytic pyrolysis
With the C after the anti-disproportionation
4Component with embodiment 1 in C
5 +Component mixes mutually, and is raw material with this mixture, adopts the fluidized-bed reaction mode, is the activity of such catalysts component with ZSM-5.510 ℃ of temperature of reaction, pressure (gauge pressure) 0.05MPa, air speed 3h
-1, water/oil ratio 0.15, catalyzer is residence time 42min in reactor, reactant gases residence time 2s, 650 ℃ of catalyst regeneration temperature.Propylene content 60.5% in the reacting rear material.
Three reaction process are taken all factors into consideration, and the material during molecular balance is formed light component (comprising ethene) 3.0%, propylene 81.8%, liquefied gas 3.2%, gasoline (containing aromatic hydrocarbons) 9.7%, coke 2.3%.
Claims (7)
1, the method for a kind of methyl alcohol or dimethyl ether conversion system propylene is characterized in that: this reaction process comprises reaction raw materials conversion reaction, ethene and butene inverse disproportionation reaction and C
4Above heavy component catalytic cracking reaction; Reaction raw materials generates the mixture that is rich in propylene by the catalyzer afterreaction, and non-propylene component is reacted by anti-disproportionation catalyst, makes ethene and butene inverse disproportionation generate propylene, and the hydrocarbon mixture of generation turns back to separation system to be separated, to obtain propylene; With unreacted C
4Component and other heavy component carry out catalytic pyrolysis, generate the hydrocarbon mixture that contains ethene, the light component of propylene, and the hydrocarbon mixture of generation turns back to separation system again to be separated, to obtain propylene; Ethene and butene inverse disproportionation reaction catalyst system therefor are loaded WO
3, Re
2O
7Perhaps MoO
3Catalyzer, support of the catalyst are SiO
2, Al
2O
3And H-Beta, ZSM-5, HY and MCM-22 molecular sieve, or SiO
2, Al
2O
3Mixture with molecular sieve; Methyl alcohol or dimethyl ether conversion system olefine reaction adopt fluidized-bed reaction technology.
2, according to the method for described methyl alcohol of claim 1 or dimethyl ether conversion system propylene, it is characterized in that: described reaction raw materials is methyl alcohol, dme or methanol aqueous solution.
3, according to the method for described methyl alcohol of claim 1 or dimethyl ether conversion system propylene, it is characterized in that: catalyst system therefor is ZSM-5 catalyzer or SAPO-34 molecular sieve catalyst in methyl alcohol or the dimethyl ether conversion system olefine reaction.
4, according to the method for described methyl alcohol of claim 1 or dimethyl ether conversion system propylene, it is characterized in that: C
4Above heavy component catalytic pyrolysis catalyst system therefor is that ZSM-5 or SAPO-34 are the microspherical catalyst of active constituent.
5, according to the method for described methyl alcohol of claim 1 or dimethyl ether conversion system propylene, it is characterized in that: described non-propylene component comprises the light component that contains hydrogen, methane, ethane, ethene, propane and COx and contains C
4Heavy component.
6, according to the method for described methyl alcohol of claim 1 or dimethyl ether conversion system propylene, it is characterized in that: ethene and butene inverse disproportionation reaction adopt fixed bed reaction technology.
7, according to the method for described methyl alcohol of claim 1 or dimethyl ether conversion system propylene, it is characterized in that: C
4Above heavy component catalytic pyrolysis adopts ciculation fluidized bed reaction technique.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN200710143259A CN100586910C (en) | 2006-11-07 | 2007-08-07 | Method for producing propylene by conversion of carbinol or dimethyl ether |
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN200610138098 | 2006-11-07 | ||
| CN200610138098.2 | 2006-11-07 | ||
| CN200710143259A CN100586910C (en) | 2006-11-07 | 2007-08-07 | Method for producing propylene by conversion of carbinol or dimethyl ether |
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| Publication Number | Publication Date |
|---|---|
| CN101177373A CN101177373A (en) | 2008-05-14 |
| CN100586910C true CN100586910C (en) | 2010-02-03 |
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|---|---|---|---|
| CN200710143259A Active CN100586910C (en) | 2006-11-07 | 2007-08-07 | Method for producing propylene by conversion of carbinol or dimethyl ether |
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Families Citing this family (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101747133A (en) * | 2008-12-11 | 2010-06-23 | 陕西煤化工技术工程中心有限公司 | Method of converting to propylene for methanol or dimethyl ether |
| CN101607858B (en) * | 2009-07-24 | 2013-07-24 | 中国海洋石油总公司 | Method for preparing aromatic hydrocarbons and propylene simultaneously employing methanol/dimethyl ether |
| CN101723778B (en) * | 2009-11-27 | 2013-10-16 | 清华大学 | Coupling process method for preparing alkene with alcohol or ether and dehydrogenating alkane |
| CN102190545A (en) * | 2010-03-03 | 2011-09-21 | 中国石油化工股份有限公司 | Method for utilizing byproducts in the process of preparing olefins from methanol |
| CN102190539B (en) * | 2010-03-03 | 2013-10-16 | 中国石油化工股份有限公司 | Method for increasing propylene yield |
| CN101823929B (en) * | 2010-04-14 | 2013-05-22 | 清华大学 | System and process for preparing aromatic hydrocarbon by converting methanol or dimethyl ether |
| CN109982990A (en) * | 2016-11-03 | 2019-07-05 | 沙特基础工业全球技术公司 | Integrated MTP/MTO process flow for production of propylene |
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