CN104745223A - Method for preparing low-carbon olefine and co-producing gasoline by methanol - Google Patents
Method for preparing low-carbon olefine and co-producing gasoline by methanol Download PDFInfo
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- CN104745223A CN104745223A CN201510128403.9A CN201510128403A CN104745223A CN 104745223 A CN104745223 A CN 104745223A CN 201510128403 A CN201510128403 A CN 201510128403A CN 104745223 A CN104745223 A CN 104745223A
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G3/00—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
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- 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
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
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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
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
- Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock
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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
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
- Y02P30/40—Ethylene production
Abstract
The invention discloses a method for preparing low-carbon olefine and co-producing gasoline by methanol. According to the method, an oligomerization reactor is introduced, a methanol aqueous solution is treated in a preheater and is dehydrated on the catalyst to generate dimethyl ether; then, balanced mixed gas of dimethyl ether, water and unreacted methanol is treated in a hydrocarbylation reactor and is transformed on ZSM-5 catalyst to generate a gaseous product I and a liquid product I; the gaseous product I is separated to obtain target products ethylene and propylene, and other gaseous products are subjected to oligomerization reaction to obtain a gaseous product II and a liquid product II; the gaseous product II is separated to obtain a small amount of LPG, the liquid product I and the liquid product II are mixed and separated to obtain a gasoline product. According to the process, ethylene and propylene having high additional values can be obtained, other gaseous products can be efficiently transformed into oligomerized gasoline, and more importantly, the ratio of ethylene and propylene to gasoline can be adjusted by changing the ZSM-5 catalyst in the hydrocarbylation reactor according to market requirement.
Description
Technical field
The invention belongs to chemical technology field, particularly relate to the technology of preparing low carbon olefinic hydrocarbon with methanol coproduction gasoline.
Background technology
Low-carbon alkene (ethene, propylene, butylene and their mixture) is the basic organic of important petrochemical complex.And wherein ethene is one of chemical that output is maximum in the world, be the core of petrochemical industry, ethylene product accounts for more than 70% of petroleum chemicals, and it also occupies critical role in national economy.The industrial scale of ethene and level have become the important symbol of a measurement national oil development of chemical industry level.
At present, the acquisition of China's low-carbon alkene still depends on petroleum resources.Wherein, ethene is mainly derived from naphtha steam cracking, and propylene is mainly derived from naphtha cracking by-product and refinery catalytic pyrolysis by-product.And this reduces the competitive power of China's low-carbon alkene to a certain extent.Because in recent years, the Middle East and north America region rely on natural gas source and price advantage, and extensive expansion ethene production capacity, thylene cost is with the obvious advantage, and the accounting in world's ethylene production obviously increases.2012, China's ethene production capacity reached 1,700 ten thousand tons/year, accounts for 11% of world's aggregated capacity.By resource limit, current China ethylene raw is based on petroleum naphtha, and be secondly solar oil, hydrogenation tail oil, the proportion such as ethane and propane is little.And wherein the ratio of petroleum naphtha in ethylene raw accounts for 65%, hydrogenation tail oil about about respectively accounts for 10% with solar oil, ethylene raw cost and the Middle East are compared with North America and is in a disadvantageous position [appoint really. the production technology of Non oil-based route preparing low-carbon olefins and industrial prospect [J]. body .2007 in fine chemistry industry, 37 (5): 6-9.].And this also causes China to the increase of Imported oil dependency degree further.The external dependence degree of China's oil also from 6% in 1993, soared all the way 2012 56.4%.Therefore, we are while enhancing your vigilance safely to the petroleum resources of China, also actively should seek the methods and direction of new preparing low-carbon olefins.
Preparing low-carbon olefins is except petroleum path, and Non oil-based route is also actively being sought in countries in the world.Wherein with Sweet natural gas or coal for raw material to have become the focus of research through preparing low carbon olefinic hydrocarbon with methanol technology.Rich coal resources in China, and adopt advanced coal chemical technology, greatly develop coal-based methanol alkene project, be conducive to the degree of self-sufficiency improving China's alkene and derived product, reduce the dependency degree to oil.
Certainly, now existing a lot of proven technique and some technology are applied by large-scale industrialization.As the FMTP technique of the fluidized-bed preparing propylene from methanol of the DMTO technique of the MTO technique of UOP, Dalian Chemiclophysics Inst., Chinese Academy of Sciences, the SMTO technique of Sinopec Group, the MTP technique of Lurgi company and Tsing-Hua University.But their object product is more single.And the preparing propylene by methanol transformation of Shanghai Petroleum Chemical Engineering Institute of China Petrochemical Industry exploitation and the method [CN201010116376.0] of aromatic hydrocarbons, the selectivity of the method propylene is greater than 32%, the yield of aromatic hydrocarbons is greater than 40%(methanol quality meter), therefore the utilization ratio of material benzenemethanol need to improve, and the kind of target product is too dull, cannot according to market requirement flexible.
Preparing low carbon olefinic hydrocarbon with methanol coproduction gasoline of the present invention solves the single problem of product equally, and while raising material benzenemethanol utilization ratio, the method can also realize the adjustment of product according to the market requirement.
Summary of the invention
Goal of the invention: for above-mentioned Problems existing and defect, the invention provides a kind of method of preparing low carbon olefinic hydrocarbon with methanol coproduction gasoline, and while raising material benzenemethanol utilization ratio, the method can also realize the adjustment of product according to the market requirement.
Technical scheme: for achieving the above object, the present invention by the following technical solutions: a kind of method of preparing low carbon olefinic hydrocarbon with methanol co-production gasoline, comprises the following steps:
(1) adopt continuous fixed reactor, first pre-reaction is carried out to methyl alcohol and obtains dme;
(2) by the dme of generation and unreacted methyl alcohol completely, and water is under the effect of ZSM-5 catalyzer, be obtained by reacting gas-phase product I and liquid product I, described gas-phase product I mainly comprises ethene and propylene, and the alkane of C1, C2, C3 and C4, C5, C6 hydrocarbon;
(3) gas-phase product I that step (2) obtains is carried out separation and obtain target product ethene and propylene, other gas-phase products are then sent into superposition reactor and are reacted, and obtain gas-phase product II and liquid product II;
(4) liquid product I then obtained respectively in step (2) and (3) and liquid product II are separated further and obtain LPG and gasoline.
As preferably, the operational condition of step (1) pre-reaction is as follows: catalyzer is Cu/Al
2o
3, temperature of reaction is 250 DEG C ~ 320 DEG C, and methanol quality air speed is 0.5h
-1~ 3h
-1, reaction pressure is normal pressure.
In such scheme, the reaction unit temperature of reaction of preparing low carbon olefinic hydrocarbon with methanol is 400 DEG C ~ 550 DEG C, and reaction pressure is 0 ~ 4MPa, catalyzer is modified zsm-5 zeolite, P charge capacity is 0 ~ 2%, and the silica alumina ratio of ZSM-5 molecular sieve is 10 ~ 400, and catalyzer is extruded moulding.And high-temperature water thermal treatment is carried out to preformed catalyst simultaneously, treatment temp is 450 DEG C ~ 650 DEG C.
As preferably, the reaction unit temperature of reaction of preparing low carbon olefinic hydrocarbon with methanol is 450 DEG C ~ 500 DEG C, and reaction pressure is 0.05 ~ 3MPa, and catalyzer is modified zsm-5 zeolite, and P charge capacity is the silica alumina ratio of 0.5 ~ 1.5%, ZSM-5 is 25 ~ 300, and catalyzer is extruded moulding.And high-temperature water thermal treatment is carried out to preformed catalyst simultaneously, treatment temp is 500 DEG C ~ 600 DEG C.
As preferably, the reaction unit catalyzer of building-up reactions is alumina silicate catalyst, and temperature of reaction is 50 DEG C ~ 180 DEG C, and reaction pressure is 0.1 ~ 4MPa.
As preferably, the reaction unit catalyzer of building-up reactions is alumina silicate catalyst, and temperature of reaction is 80 DEG C ~ 150 DEG C, and reaction pressure is 0.5 ~ 3MPa.
Beneficial effect: compared with prior art, the present invention not only solves current preparing low carbon olefinic hydrocarbon with methanol or the single problem of gasoline products, the adjustment of product can also be realized according to the market requirement, and further increase the utilization ratio of methyl alcohol, make methyl alcohol more change into the object product of high added value.Specifically: after the present invention isolates gas-phase product ethylene, propylene, other gas-phase product is carried out building-up reactions more further, mainly make C4, C5 change into polymer gasoline.Thus achieve preparing light olefins from methanol co-production gasoline.In the total reaction that the method provides, the transformation efficiency of methyl alcohol is greater than 99%, and the selectivity (molar selectivity) of product is best is greater than 17%, propylene about 53% for ethene, and ethene+propylene is about 70%; Yield of gasoline optimum data is 50%(mass yield).The most important thing is that the present invention can also regulate the ratio of ethylene, propylene and gasoline by the ZSM-5 catalyzer changed in alkylation reaction device according to the market requirement.
Accompanying drawing explanation
Fig. 1 is the process unit schematic diagram of preparing low carbon olefinic hydrocarbon with methanol coproduction gasoline method of the present invention.
Wherein, DME reaction 1, alkylation reaction device 2, first separator 3, superposition reactor 4, water cooler 5, second separator 6.
Embodiment
Below in conjunction with the drawings and specific embodiments, illustrate the present invention further, these embodiments should be understood only be not used in for illustration of the present invention and limit the scope of the invention, after having read the present invention, the amendment of those skilled in the art to the various equivalent form of value of the present invention has all fallen within the application's claims limited range.
Technological process of the present invention is as follows: first, and methyl alcohol reacts through DME reactor 1 and generates dme; Then, the dme that reaction generates, water and unreacted methyl alcohol are obtained by reacting gas-phase product and liquid product in alkylation reaction device 2, and gas-phase product is separated through the first separator 3 and obtains target product ethene+propylene; And other gas-phase product enters superposition reactor 4, the liquid product obtained with reactor 2 after building-up reactions through water cooler 5, and then obtains target product gasoline through the second separator 6 separation; And uncooled be LPG.Below by way of specific embodiment, the present invention is further described:
[embodiment 1]
According to the technical process shown in Fig. 1, methyl alcohol enters dimethyl ether reactor 1, and the temperature of reaction of reactor controls at 250 DEG C, and reaction pressure is normal pressure, and methanol quality air speed is 0.5h
-1, then water vapour, or the water obtained that circulates, dme, methanol vapor carries out alkylation reaction in alkylation reaction device 2, temperature of reaction controls at 450 DEG C, reaction pressure is 0.05MPa, loading catalyst is ZSM-5, its silica alumina ratio is 300, P charge capacity is 0.5%, hydrothermal treatment consists temperature is 600 DEG C, reaction gas-phase product is separated through the first separator 3, the selectivity of ethene is 21.47%, Propylene Selectivity is 42.77%, the selectivity of ethene+propylene is that 64.24%(is in volumn concentration), other gas-phase products enter superposition reactor 4 and react, temperature of reaction is 80 DEG C, reaction pressure is 0.5MPa, water cooler 5 is entered together with the liquid product that reactor 2 obtains, then the second separator 6 is entered, separation obtains gasoline, quality of gasoline yield is 20.11%.
[embodiment 2]
Technical process is as embodiment 1, and the temperature of reaction of 1 dimethyl ether reactor controls at 280 DEG C, and reaction pressure is normal pressure, and methanol quality air speed is 1h
-1, 2 alkylation reaction device temperature of reaction control at 480 DEG C, reaction pressure is 1MPa, loading catalyst is ZSM-5, its silica alumina ratio is 300, P charge capacity is 1.0 %, hydrothermal treatment consists temperature is 600 DEG C, after the first separator 3 is separated, the selectivity 15.88% of ethene, the selectivity of propylene is 49.30%, the selectivity of ethene+propylene is that 65.18%(is in volumn concentration), superposition reactor 4, controlling temperature of reaction is 120 DEG C, reaction pressure is 1.5MPa, liquid product enters water cooler 5, then the second separator 6 is entered, separation obtains gasoline, quality of gasoline yield is 19.42%.
[embodiment 3]
Technical process is as embodiment 1, and the temperature of reaction of dimethyl ether reactor 1 controls at 320 DEG C, and reaction pressure is normal pressure, and methanol quality air speed is 3h
-1, alkylation reaction device 2 temperature of reaction controls at 500 DEG C, reaction pressure is 0.5MPa, loading catalyst is ZSM-5, its silica alumina ratio is 300, P charge capacity is 1.5%, hydrothermal treatment consists temperature is 500 DEG C, after the first separator 3 is separated, the selectivity 17.22% of ethene, the selectivity of propylene is 45.86%, the selectivity of ethene+propylene is that 63.08%(is in volumn concentration), superposition reactor 4, controlling temperature of reaction is 150 DEG C, reaction pressure is 3MPa, liquid product enters water cooler 5, then the second separator 6 is entered, separation obtains gasoline, quality of gasoline yield is 21.15%.
[embodiment 4]
Technical process is as embodiment 1, and the temperature of reaction of dimethyl ether reactor 1 controls at 300 DEG C, and reaction pressure is normal pressure, and methanol quality air speed is 1h
-1, alkylation reaction device 2 temperature of reaction controls at 480 DEG C, reaction pressure is 0.05MPa, loading catalyst is ZSM-5, its silica alumina ratio is 300, P charge capacity is 1.0%, hydrothermal treatment consists temperature is 600 DEG C, after the first separator 3 is separated, the selectivity 16.92% of ethene, the selectivity of propylene is 53.40%, the selectivity of ethene+propylene is that 70.32%(is in volumn concentration), superposition reactor 4, controlling temperature of reaction is 120 DEG C, reaction pressure is 2MPa, liquid product enters water cooler 5, then the second separator 6 is entered, separation obtains gasoline, quality of gasoline yield is 18.31%.
[embodiment 5]
Technical process is as embodiment 1, and the temperature of reaction of dimethyl ether reactor 1 controls at 300 DEG C, and reaction pressure is normal pressure, and methanol quality air speed is 1h
-1, alkylation reaction device 2 temperature of reaction controls at 480 DEG C, reaction pressure is 0.05MPa, loading catalyst is ZSM-5, its silica alumina ratio is 150, P charge capacity is 1.0%, hydrothermal treatment consists temperature is 600 DEG C, after the first separator 3 is separated, the selectivity 22.18% of ethene, the selectivity of propylene is 37.70%, the selectivity of ethene+propylene is that 59.88%(is in volumn concentration), superposition reactor 4, controlling temperature of reaction is 100 DEG C, reaction pressure is 2MPa, liquid product enters water cooler 5, then the second separator 6 is entered, separation obtains gasoline, quality of gasoline yield is 30.86%.
[embodiment 6]
Technical process is as embodiment 1, and the temperature of reaction of dimethyl ether reactor 1 controls at 280 DEG C, and reaction pressure is normal pressure, and methanol quality air speed is 2h
-1, alkylation reaction device 2 temperature of reaction controls at 480 DEG C, reaction pressure is 0.05MPa, loading catalyst is ZSM-5, its silica alumina ratio is 150, P charge capacity is 1%, hydrothermal treatment consists temperature is 550 DEG C, after the first separator 3 is separated, the selectivity 20.64% of ethene, the selectivity of propylene is 42.51%, the selectivity of ethene+propylene is that 63.15%(is in volumn concentration), superposition reactor 4, controlling temperature of reaction is 150 DEG C, reaction pressure is 3MPa, liquid product enters water cooler 5, then the second separator 6 is entered, separation obtains gasoline, quality of gasoline yield is 25.46%.
[embodiment 7]
Technical process is as embodiment 1, and the temperature of reaction of dimethyl ether reactor 1 controls at 250 DEG C, and reaction pressure is normal pressure, and methanol quality air speed is 1.5h
-1, alkylation reaction device 2 temperature of reaction controls at 500 DEG C, reaction pressure is 0.1MPa, loading catalyst is ZSM-5, its silica alumina ratio is 150, P charge capacity is 0.5%, hydrothermal treatment consists temperature is 500 DEG C, after the first separator 3 is separated, the selectivity 23.98% of ethene, the selectivity of propylene is 32.74%, the selectivity of ethene+propylene is that 56.72%(is in volumn concentration), superposition reactor 4, controlling temperature of reaction is 120 DEG C, reaction pressure is 2MPa, liquid product enters water cooler 5, then the second separator 6 is entered, separation obtains gasoline, quality of gasoline yield is 27.88%.
[embodiment 8]
Technical process is as embodiment 1, and the temperature of reaction of dimethyl ether reactor 1 controls at 300 DEG C, and reaction pressure is normal pressure, and methanol quality air speed is 1h
-1, alkylation reaction device 2 temperature of reaction controls at 480 DEG C, reaction pressure is 1MPa, loading catalyst is ZSM-5, its silica alumina ratio is 25, P charge capacity is 1.0%, hydrothermal treatment consists temperature is 550 DEG C, after the first separator 3 is separated, the selectivity 17.13% of ethene, the selectivity of propylene is 15.26%, the selectivity of ethene+propylene is that 32.39%(is in volumn concentration), superposition reactor 4, controlling temperature of reaction is 80 DEG C, reaction pressure is 1MPa, liquid product enters water cooler 5, then the second separator 6 is entered, separation obtains gasoline, quality of gasoline yield is 46.49%.
[embodiment 9]
Technical process is as embodiment 1, and the temperature of reaction of dimethyl ether reactor 1 controls at 300 DEG C, and reaction pressure is normal pressure, and methanol quality air speed is 1.5h
-1, alkylation reaction device 2 temperature of reaction controls at 480 DEG C, reaction pressure is 2MPa, loading catalyst is ZSM-5, its silica alumina ratio is 25, P charge capacity is 1.5%, hydrothermal treatment consists temperature is 600 DEG C, after the first separator 3 is separated, the selectivity 16.65% of ethene, the selectivity of propylene is 14.77%, the selectivity of ethene+propylene is that 31.42%(is in volumn concentration), superposition reactor 4, controlling temperature of reaction is 80 DEG C, reaction pressure is 2MPa, liquid product enters water cooler 5, then the second separator 6 is entered, separation obtains gasoline, quality of gasoline yield is 50.03%.
[embodiment 10]
Technical process is as embodiment 1, and the temperature of reaction of dimethyl ether reactor 1 controls at 300 DEG C, and reaction pressure is normal pressure, and methanol quality air speed is 1h
-1; Alkylation reaction device 2 temperature of reaction controls at 500 DEG C, reaction pressure is 3MPa, loading catalyst is ZSM-5, its silica alumina ratio is 25, hydrothermal treatment consists temperature is 550 DEG C, after the first separator 3 is separated, the selectivity 16.35% of ethene, the selectivity of propylene is 15.89%, the selectivity of ethene+propylene is that 32.24%(is in volumn concentration), superposition reactor 4, controlling temperature of reaction is 150 DEG C, and reaction pressure is 3MPa, liquid product enters water cooler 5, then enter the second separator 6, be separated and obtain gasoline, quality of gasoline yield is 47.66%.
Claims (6)
1. a method for preparing low carbon olefinic hydrocarbon with methanol co-production gasoline, is characterized in that comprising the following steps:
(1) adopt continuous fixed reactor, first pre-reaction is carried out to methyl alcohol and obtains dme;
(2) by the dme of generation and unreacted methyl alcohol completely, and water is under the effect of ZSM-5 catalyzer, be obtained by reacting gas-phase product I and liquid product I, described gas-phase product I mainly comprises ethene and propylene, and the alkane of C1, C2, C3 and C4, C5, C6 hydrocarbon;
(3) gas-phase product I that step (2) obtains is carried out separation and obtain target product ethene and propylene, other gas-phase products are then sent into superposition reactor and are reacted, and obtain gas-phase product II and liquid product II;
(4) liquid product I then obtained respectively in step (2) and (3) and liquid product II are separated further and obtain LPG and gasoline.
2. the method for preparing low carbon olefinic hydrocarbon with methanol co-production gasoline according to claim 1, is characterized in that: the operational condition of step (1) pre-reaction is as follows: catalyzer is Cu/Al
2o
3, temperature of reaction is 250 DEG C ~ 320 DEG C, and methanol quality air speed is 0.5h
-1~ 3h
-1, reaction pressure is normal pressure.
3. the method for preparing low carbon olefinic hydrocarbon with methanol co-production gasoline according to claim 1, it is characterized in that: the reaction unit temperature of reaction of preparing low carbon olefinic hydrocarbon with methanol is 400 DEG C ~ 550 DEG C, reaction pressure is 0 ~ 4MPa, catalyzer is modified zsm-5 zeolite, P charge capacity is 0 ~ 2%, and the silica alumina ratio of ZSM-5 molecular sieve is 10 ~ 400, and catalyzer is extruded moulding, and high-temperature water thermal treatment is carried out to preformed catalyst simultaneously, treatment temp is 450 DEG C ~ 650 DEG C.
4. the method for preparing low carbon olefinic hydrocarbon with methanol co-production gasoline according to claim 1, it is characterized in that: the reaction unit temperature of reaction of preparing low carbon olefinic hydrocarbon with methanol is 450 DEG C ~ 500 DEG C, reaction pressure is 0.05 ~ 3MPa, catalyzer is modified zsm-5 zeolite, P charge capacity is the silica alumina ratio of 0.5 ~ 1.5%, ZSM-5 is 25 ~ 300, and catalyzer is extruded moulding, and high-temperature water thermal treatment is carried out to preformed catalyst simultaneously, treatment temp is 500 DEG C ~ 600 DEG C.
5. the method for preparing low carbon olefinic hydrocarbon with methanol co-production gasoline according to claim 1, it is characterized in that: the reaction unit catalyzer of building-up reactions is alumina silicate catalyst, temperature of reaction is 50 DEG C ~ 180 DEG C, and reaction pressure is 0.1 ~ 4MPa.
6. the method for preparing low carbon olefinic hydrocarbon with methanol co-production gasoline according to claim 1, it is characterized in that: the reaction unit catalyzer of building-up reactions is alumina silicate catalyst, temperature of reaction is 80 DEG C ~ 150 DEG C, and reaction pressure is 0.5 ~ 3MPa.
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Application publication date: 20150701 |