CN110183296A - A method of low-carbon alkene co-production gasoline is produced using Fischer-Tropsch synthesis oil - Google Patents
A method of low-carbon alkene co-production gasoline is produced using Fischer-Tropsch synthesis oil Download PDFInfo
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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
- 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
- C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
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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
- C10G50/00—Production of liquid hydrocarbon mixtures from lower carbon number hydrocarbons, e.g. by oligomerisation
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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
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1022—Fischer-Tropsch products
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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
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/02—Gasoline
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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
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/20—C2-C4 olefins
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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
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Abstract
The present invention provides a kind of method using Fischer-Tropsch synthesis oil production low-carbon alkene co-production gasoline, C5/C6 fraction in fischer-tropsch synthesis process products obtained therefrom is introduced into the methanol to olefins reaction device of MTO technology as raw material flow stock, reaction production low-carbon alkene and gasoline products in methanol to olefins reaction device；It is for replacing the recycle hydrocarbons for being partially or wholly used for being introduced in methanol to olefins reaction device that the C5/C6 fraction is wherein introduced into the methanol to olefins reaction device；The low-carbon alkene includes ethylene, propylene and/or butylene.Fischer-tropsch synthesis process and process for preparing propylene from methanol can effectively be coupled by method of the invention, can dramatically increase yield of light olefins, improve the added value of C5/C6 fraction in fischer-tropsch synthesis process, promote the income of process for preparing propylene from methanol.
Description
Technical field
The present invention relates to preparing light olefins from methanol technical field, in particular to one kind utilizes in MTO technology and takes
The method for holding in the palm synthetic oil production low-carbon alkene co-production gasoline.
Background technique
Coal in China reserves are more oily, gas reserves relative abundance, convert liquid on a large scale for coal with the technique of clean and effective
The industrialization of fluid fuel and chemicals advantageously reduces dependence of the China to Imported oil resource, improves China's oil product and chemistry
The basic self-supporting ability of product.Currently, product is mainly by alkane and alkene structure since Fiscber-Tropscb synthesis technology has raw material range wide
At and sulphur, nitrogen and the features such as arene content is low, clean and environmental protection, realize industrial applications in China, it is contemplated that 2020
China's Fischer-Tropsch synthesis oil industry will form about 31,000,000 tons/year of production capacity.
Currently, most F- T synthesis devices are in process of production using liquefied gas, naphtha and diesel component as major product.
And low value-added product therein such as C5/C6 fraction, still lack the solution for effectively improving its added value at present.
Low-carbon alkene (including ethylene, propylene and/or butylene) is important Elementary Chemical Industry raw material, with the increasing of national economy
Long, demand is continuously increased.The traditional processing technology of low-carbon alkene is petroleum path, but increasingly in short supply with petroleum resources
And heaviness, the economical significant attenuating of the alkene production technology of petroleum path, the low-carbon alkene production technology of Non oil-based route obtain
To tremendous development, wherein having realized the production scale of megaton by methanol/dimethyl ether production low-carbon alkene.Existing methanol alkene
In hydrocarbon technique, recycle hydrocarbons are recycled and introduce methanol to olefins reaction device as raw material participation reaction, and contained in recycle hydrocarbons therein
There are cyclic hydrocar-bons, be unfavorable for the generation of low-carbon alkene, and easily causes catalyst coking and deactivation.
Summary of the invention
In view of this, the present invention provides a kind of method using Fischer-Tropsch synthesis oil production low-carbon alkene co-production gasoline, it should
Fischer-tropsch synthesis process and MTO technology can effectively be coupled by method, will be low value-added in fischer-tropsch synthesis process
C5/C6 fraction is applied in methanol-to-olefins production process, and it is anti-to be all recycled to methanol-to-olefins with original use recycle hydrocarbons
The MTO technology of device is answered to compare, the improved technique of the present invention can dramatically increase yield of light olefins, improve Fischer-Tropsch and close
At the added value of C5/C6 fraction in technique, the income of process for preparing propylene from methanol is promoted.
The present invention is to reach its purpose, is adopted the following technical scheme that
The present invention provides a kind of method using Fischer-Tropsch synthesis oil production low-carbon alkene co-production gasoline, by F- T synthesis work
C5/C6 fraction in skill products obtained therefrom is introduced into the methanol to olefins reaction device of MTO technology as raw material flow stock,
Reaction production low-carbon alkene and gasoline products in methanol to olefins reaction device；Wherein introduced into the methanol to olefins reaction device
The C5/C6 fraction is for replacing the circulation in part or all of original process for being introduced in methanol to olefins reaction device
Hydrocarbon；The low-carbon alkene includes ethylene, propylene and/or butylene.Specifically, including the following steps:
1) first stage: methanol enters in DME reactor the reaction for carrying out methanol-fueled CLC dimethyl ether, obtains the first product
Stream, first product stream includes dimethyl ether, water and methanol；
2) second stage: first product stream, which enters in methanol to olefins reaction device, to react, and separates from products therefrom
Recycle hydrocarbons, low-carbon alkene and gasoline products are obtained, the low-carbon alkene includes ethylene, propylene and/or butylene；
Wherein, it in the second stage, is introduced into methanol to olefins reaction device and comes from fischer-tropsch synthesis process products obtained therefrom
In C5/C6 fraction and the second stage obtained in recycle hydrocarbons as raw material flow stock participate in react；And introduce the methanol
In the total amount of the C5/C6 fraction in olefin hydrocarbon reactor processed and the recycle hydrocarbons, the C5/C6 fraction proportion is
10wt%-100wt% (such as 10wt%, 20wt%, 30wt%, 40wt%, 50wt%, 60wt%, 70wt%, 80wt%,
90wt%, 100wt% etc.), more preferable ratio be 50wt%-100wt% (such as 50wt%, 60wt%, 70wt%, 80wt%,
90wt%, 100wt% etc.).
In the preferred embodiment of the invention, the C5/C6 fraction includes the ingredient of following mass percent: 15%-70%
The C5-C6 alkane of (such as 15%, 25%, 35%, 45%, 55%, 65%, 70% etc.), 15%-70% (such as 15%,
25%, C5-C6 alkene and 1%-20% (1%, 5%, 10%, 15%, 20% 35%, 45%, 55%, 65%, 70% etc.)
Deng) oxygenatedchemicals；Wherein, the oxygenatedchemicals is mainly alcohols, and the preferably described oxygenatedchemicals contains 80% or more
The alcohols of (such as 80%, 90%, 95% etc.) mass ratio, the alcohols are preferably methanol and/or ethyl alcohol；The oxygen-containing chemical combination
It is also possible in object containing components such as a small amount of ketone, aldehyde, acid.
In some specific embodiments, in the methanol to olefins reaction device, used catalyst is molecular sieve catalyst；
It is preferred that the catalyst is commercially available Clariant HZSM-5 catalyst, catalyst model MTPROP-1.
The present invention is the technical solution for making improvements and being formed on the basis of existing MTO technology, is improved
Point essentially consists in: in existing MTO technology, being all recycled to methanol to olefins reaction device using recycle hydrocarbons and participates in instead
It answers；And the present invention is partly or entirely replaced the recycle hydrocarbons, alternative is in fischer-tropsch synthesis process products obtained therefrom
C5/C6 fraction；Replacement ratio is controlled in 10wt%-100wt%.
It for MTO technology itself, has been well known to those skilled in the art, which mainly includes two
A stage, first stage are that methanol enters in DME reactor the reaction for carrying out methanol-fueled CLC dimethyl ether, obtain the first product stream,
Mainly contain dimethyl ether, water and methanol etc.；Second stage is that the first product stream is introduced into methanol to olefins reaction device, and is reacted
Catalyst contact in device, and react and generate gaseous products (low-carbon alkene) and product liquid containing low-carbon alkene；To liquid
Product separate and then obtains the downstream product such as C5/C6 recycle hydrocarbons and gasoline products, the isolated circulation from product liquid
The specific separating technology of hydrocarbon and gasoline products is state of the art, is not repeated.For example, known to a person skilled in the art
, it can C5/C6 recycle hydrocarbons therein isolated in this way: product liquid being entered into debutanizing tower, by the tower bottom of debutanizing tower
Obtained bottom product input dehexanizer is produced in the tower top output C5/C6 recycle hydrocarbons of dehexanizer in the tower bottom of dehexanizer
Gasoline products out；The concrete technology of C5/C6 recycle hydrocarbons and gasoline products is separated from the product liquid of methanol to olefins reaction device
Operation be state of the art, be it is well-known to those skilled in the art, this is not repeated.Wherein, recycle hydrocarbons (group subpackage
Positive isomeric olefine, positive isoparaffin and cyclic hydrocarbon containing C5-C6) the methanol to olefins reaction device of second stage can be recycled to
In.Specific technological operation can refer to this field prior art, not repeat one by one this.
Improvement of the invention essentially consists in second stage, i.e., is evaporated using the C5/C6 in fischer-tropsch synthesis process products obtained therefrom
Partly or entirely replacement is divided to be originally used for being recycled to the recycle hydrocarbons in methanol to olefins reaction device.
Preferably, in the step 2) of the method for the present invention, the C5/C6 that is introduced into the methanol to olefins reaction device
Fraction and the total mass flow rate of the recycle hydrocarbons be about the first product stream mass flow 60-80% (such as 60%, 70%,
80% etc.), wherein the first product stream mass flow also corresponds in step 1) the methanol quality stream for entering DME reactor
Amount.
In the present invention, the first stage is this field mature technology by the technique of methanol dimethyl ether synthesis in DME reactor,
Be it is well-known to those skilled in the art, this is not repeated.
In the present invention, in second stage, it is preferred that in step 2), in the methanol to olefins reaction device, reaction temperature control
It is made as 350-550 DEG C, reaction pressure is -0.1MPa to 0.3MPa.
Preferably, the methanol to olefins reaction device is fixed bed reactors.
The fischer-tropsch synthesis process, to be known in the art, such as patent document CN 1511188,
CN101297022B, CN104204141B etc. disclose the method that synthesis gas is converted into hydrocarbon through F- T synthesis.It is of the present invention
Fischer-tropsch synthesis process be not particularly limited, can be Low Temperature Fischer Tropsch synthesis technology or high temperature fischer-tropsch synthesis technology.Institute of the present invention
The C5/C6 fraction stated can come from the various specific fischer-tropsch synthesis process in this field.Document " ICL for Indirect Coal Liquefaction technology and its is ground
Study carefully progress " in, describe principle and typical process of the coal through synthesis gas indirect liquefaction synthetic liquid fuel in detail.Article points out,
ICL for Indirect Coal Liquefaction technique can be divided into low temperature ICL for Indirect Coal Liquefaction technique and high temperature ICL for Indirect Coal Liquefaction work by the reaction temperature of F- T synthesis
Reaction temperature is usually known as low temperature ICL for Indirect Coal Liquefaction technique lower than 280 DEG C by skill, and the referred to as high-temperature coal higher than 300 DEG C is indirect
Liquefaction process.Low temperature ICL for Indirect Coal Liquefaction uses fixed bed or paste state bed reactor；High temperature ICL for Indirect Coal Liquefaction is using fluidized bed (circulation
It is fluidized bed, fixed fluidized bed) reactor.In the present invention, used catalyst is not particularly limited in the fischer-tropsch synthesis process, this
The common catalyst in field, such as the main active component of common metal have the Fischer-Tropsch of the transition metal such as Fe, Co, Ni and Ru
Synthetic catalyst is preferably iron-based or cobalt-base catalyst, more preferable ferrum-based catalyst.
Technical solution provided by the invention has the following beneficial effects:
The present invention couples fischer-tropsch synthesis process and MTO technology, and Fischer-Tropsch is closed in present inventor's discovery
The methanol to olefins reaction device of MTO technology is introduced at the C5/C6 fraction (Fischer-Tropsch synthesis oil) of the low value-added product of technique
In, for partly or entirely replacing recycle hydrocarbons used in it, low-carbon alkene is can be improved in the introducing of one side C5/C6 fraction
Yield, yield can reach higher than 65%；On the one hand the gasoline products that octane number is greater than 92 can be also obtained, are increased economic efficiency；And
And in this way, also improve the added value of C5/C6 fraction obtained by fischer-tropsch synthesis process, while improving methanol-to-olefins work
The economic benefit of skill.
Specific embodiment
For a better understanding of the technical solution of the present invention, below with reference to the embodiment content that the present invention is further explained,
But the contents of the present invention are not limited to following embodiment.
In following embodiment or comparative example, the method for production low-carbon alkene co-production gasoline includes the following steps:
1) first stage: the methanol of 10g/hr enters in DME reactor the reaction for carrying out methanol-fueled CLC dimethyl ether, and DME is anti-
Answering device reaction temperature is 280 DEG C, reaction pressure 0.1MPa, with the CNM-3 type catalyst of Southwest Chemical Research and Design Institute, filling
Amount is 5g；The first product stream of reacted acquisition, which includes dimethyl ether, water and methanol.
2) second stage: the first product stream obtained above, which enters in methanol to olefins reaction device, to react, catalysis used
Agent is the HZSM-5 catalyst of Clariant MTPROP-1 specification, and reaction temperature is 480 DEG C, reaction pressure 0.1MPa, catalysis
Agent loadings are 10g；Isolated low-carbon alkene and product liquid from reaction product；Wherein, product liquid enters debutanization
Tower, bottom product enter dehexanizer, dehexanizer tower top output C5/C6 recycle hydrocarbons, tower bottom output gasoline products.
Wherein, in second stage, according to various embodiments or the concrete condition of comparative example, by the C5/C6 recycle hydrocarbons
And/or the C5/C6 fraction in fischer-tropsch synthesis process products obtained therefrom is introduced into methanol to olefins reaction device therein as raw material flow
Stock participates in reaction, and the C5/C6 fraction being introduced into methanol to olefins reaction device and the total mass flow rate of recycle hydrocarbons are 7g/hr.
Embodiment 1
In the C5/C6 fraction and recycle hydrocarbons total amount being introduced into methanol to olefins reaction device, the iron-based F- T synthesis C5/ of high temperature
Ratio shared by C6 product (i.e. C5/C6 fraction or Fischer-Tropsch synthesis oil) is that (the F- T synthesis C5/C6 i.e. in table 2 is produced 10wt%
Object substitution amount %, following embodiment is herewith), Fischer-Tropsch synthesis oil typical component is shown in Table the 1# in 1.Methanol to olefins reaction device goes out
Mouth product is analyzed through online gas-chromatography Agilent 7890A, and test result is shown in Table 2.
Embodiment 2
In the C5/C6 fraction and recycle hydrocarbons total amount being introduced into methanol to olefins reaction device, the iron-based F- T synthesis C5- of low temperature
Ratio shared by C6 product (i.e. C5/C6 fraction or Fischer-Tropsch synthesis oil) is 10wt%, and Fischer-Tropsch synthesis oil typical component is shown in Table 1
In 2#.Methanol to olefins reaction device outlets products are shown in Table 2 through online gas chromatographic analysis, test result.
Embodiment 3
In the C5/C6 fraction and recycle hydrocarbons total amount being introduced into methanol to olefins reaction device, the iron-based F- T synthesis C5- of high temperature
Ratio shared by C6 product (i.e. C5/C6 fraction or Fischer-Tropsch synthesis oil) is 20wt%, and Fischer-Tropsch synthesis oil typical component is shown in Table 1
In 1#.Methanol to olefins reaction device outlets products are shown in Table 2 through online gas chromatographic analysis, test result.
Embodiment 4
In the C5/C6 fraction and recycle hydrocarbons total amount being introduced into methanol to olefins reaction device, the iron-based F- T synthesis C5- of low temperature
Ratio shared by C6 product (i.e. C5/C6 fraction or Fischer-Tropsch synthesis oil) is 30wt%, and Fischer-Tropsch synthesis oil typical component is shown in Table 1
In 2#.Methanol to olefins reaction device outlets products are shown in Table 2 through online gas chromatographic analysis, test result.
Embodiment 5
In the C5/C6 fraction and recycle hydrocarbons total amount being introduced into methanol to olefins reaction device, the iron-based F- T synthesis C5- of high temperature
Ratio shared by C6 product (i.e. C5/C6 fraction or Fischer-Tropsch synthesis oil) is 30wt%, and Fischer-Tropsch synthesis oil typical component is shown in Table 1
In 3#.Methanol to olefins reaction device outlets products are shown in Table 2 through online gas chromatographic analysis, test result.
Embodiment 6
In the C5/C6 fraction and recycle hydrocarbons total amount being introduced into methanol to olefins reaction device, the iron-based F- T synthesis C5- of high temperature
Ratio shared by C6 product (i.e. C5/C6 fraction or Fischer-Tropsch synthesis oil) is 100% (not introducing recycle hydrocarbons), F- T synthesis
Oily typical component is shown in Table the 3# in 1.Methanol to olefins reaction device outlets products are shown in Table through online gas chromatographic analysis, test result
2。
Comparative example 1
The recycle hydrocarbons (i.e. substitution amount is 0wt%) that original technique is substituted without F- T synthesis C5/C6 product, i.e., only introduce and follow
Cyclic hydrocarbon, remaining condition are same as Example 1.Methanol to olefins reaction device outlets products are through online gas chromatographic analysis, test knot
Fruit is shown in Table 2.
1 F- T synthesis C5/C6 product of table composition
| Serial number | 1# | 2# | 3# |
| Component | Mass content % | Mass content % | Mass content % |
| Pentane | 2.98 | 24.01 | 11.22 |
| Amylene | 25.23 | 3.25 | 17.50 |
| Hexane | 12.81 | 45.21 | 24.05 |
| Hexene | 43.71 | 12.58 | 45.03 |
| Methanol | 5.11 | 3.47 | 0.04 |
| Ethyl alcohol | 9.68 | 10.50 | 1.16 |
Table 2
It will be understood by those skilled in the art that under the introduction of this specification, the present invention can be made some modifications or
Adjustment.These modifications or adjustment should also be as within the scope of the claims in the present invention.
Claims (10)
1. a kind of method using Fischer-Tropsch synthesis oil production low-carbon alkene co-production gasoline, which comprises the steps of:
1) first stage: methanol enters in DME reactor the reaction for carrying out methanol-fueled CLC dimethyl ether, obtains the first product stream；
2) second stage: first product stream, which enters in methanol to olefins reaction device, to react, isolated from products therefrom
Recycle hydrocarbons, low-carbon alkene and gasoline products, the low-carbon alkene include ethylene, propylene and/or butylene；
Wherein, it in the second stage, is introduced into methanol to olefins reaction device in fischer-tropsch synthesis process products obtained therefrom
Recycle hydrocarbons obtained in C5/C6 fraction and the second stage participate in reacting as raw material flow stock；And introduce the methanol alkene
In the total amount of the C5/C6 fraction in hydrocarbon reactor and the recycle hydrocarbons, the C5/C6 fraction proportion is 10wt%-
100wt%.
2. the method according to claim 1, wherein introducing the C5/C6 of the methanol to olefins reaction device
In the total amount of fraction and the recycle hydrocarbons, the C5/C6 fraction proportion is 50wt%-100wt%.
3. method according to claim 1 or 2, which is characterized in that the C5/C6 fraction includes following mass percent
Ingredient: C5-C6 alkane, the C5-C6 alkene of 15%-70% and the oxygenatedchemicals of 1%-20% of 15%-70%；Wherein, institute
Stating oxygenatedchemicals is mainly alcohols, and the preferably described oxygenatedchemicals contains the alcohols of 80% or more mass ratio, the alcohols
Preferably methanol and/or ethyl alcohol.
4. method according to claim 1-3, which is characterized in that in the methanol to olefins reaction device, institute
It is molecular sieve catalyst with catalyst；It is preferred that the catalyst is HZSM-5.
5. method according to claim 1-4, which is characterized in that the second stage, products therefrom include gas
The product liquid is inputted debutanizing tower by state product low-carbon alkene and product liquid, and tower bottom products obtained therefrom inputs de- hexane
Tower, obtains the recycle hydrocarbons in dehexanizer tower top, obtains the gasoline products in dehexanizer tower bottom.
6. method according to claim 1-5, which is characterized in that in the step 2), introduce the methanol system
The C5/C6 fraction in olefin hydrocarbon reactor and the total mass flow rate of the recycle hydrocarbons are the first product stream mass flow
60-80%.
7. method according to claim 1-6, which is characterized in that in step 2), the methanol to olefins reaction
In device, reaction temperature control is 350-550 DEG C, and reaction pressure is -0.1MPa to 0.3MPa.
8. method according to claim 1-7, which is characterized in that the methanol to olefins reaction device is fixed bed
Reactor.
9. method according to claim 1-8, which is characterized in that the fischer-tropsch synthesis process is Low Temperature Fischer Tropsch conjunction
At technique or high temperature fischer-tropsch synthesis technology.
10. -9 described in any item methods according to claim 1, which is characterized in that catalysis used in the fischer-tropsch synthesis process
Agent is iron-based or cobalt-base catalyst, preferably ferrum-based catalyst.
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| CN114409492A (en) * | 2021-12-15 | 2022-04-29 | 国家能源集团宁夏煤业有限责任公司 | Device and method for preparing low-carbon olefin from methanol |
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| CN114409492B (en) * | 2021-12-15 | 2023-12-22 | 国家能源集团宁夏煤业有限责任公司 | Device and method for preparing low-carbon olefin from methanol |
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