CN109694742A - A kind of method of Fischer Tropsch waxes comprehensive utilization production clean gasoline - Google Patents
A kind of method of Fischer Tropsch waxes comprehensive utilization production clean gasoline Download PDFInfo
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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
- C10G69/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process
- C10G69/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only
- C10G69/12—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only including at least one polymerisation or alkylation step
- C10G69/123—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only including at least one polymerisation or alkylation step alkylation
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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
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/20—Characteristics of the feedstock or the products
- C10G2300/201—Impurities
-
- 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
- C10G2300/20—Characteristics of the feedstock or the products
- C10G2300/201—Impurities
- C10G2300/202—Heteroatoms content, i.e. S, N, O, P
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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
- C10G2300/20—Characteristics of the feedstock or the products
- C10G2300/30—Physical properties of feedstocks or products
- C10G2300/305—Octane number, e.g. motor octane number [MON], research octane number [RON]
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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
- C10G2300/40—Characteristics of the process deviating from typical ways of processing
- C10G2300/4006—Temperature
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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
- C10G2300/40—Characteristics of the process deviating from typical ways of processing
- C10G2300/4012—Pressure
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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
- C10G2300/40—Characteristics of the process deviating from typical ways of processing
- C10G2300/4018—Spatial velocity, e.g. LHSV, WHSV
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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
- C10G2300/70—Catalyst aspects
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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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- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The present invention provides a kind of methods that Fischer Tropsch waxes comprehensively utilize production clean gasoline.Described method includes following steps: Fischer Tropsch waxes progress cracking reaction being obtained cracking oil gas, obtained oil gas obtains rich gas, light gasoline fraction, heavy naphtha, diesel oil distillate and recycle oil by fractionation；Light gasoline fraction therein obtains aromatisation gasoline fraction by aromatisation；Rich gas passes through isolated iso-butane, n-butene and isobutene, and obtained iso-butane and n-butene is alkylated to obtain gasoline alkylate fraction；Obtained isobutene carries out selective superposition-hydrotreating, obtains class gasoline alkylate fraction；Obtained heavy naphtha, aromatisation gasoline fraction, gasoline alkylate fraction and class gasoline alkylate fraction are carried out reconciling to obtain the clean gasoline.This method using the advantage of catalytic cracking process by F- T synthesis wax cracking fecund gasoline fraction, realize by the target of Fischer Tropsch waxes production six standard clean gasoline of high-octane rating state by this method.
Description
Technical field
The present invention relates to chemical fields, and specifically, the present invention relates to a kind of Fischer Tropsch waxes to comprehensively utilize production cleaning
The method of gasoline.
Background technique
The Fischer-Tropsch synthesis (F-T) of coal chemical technology is the reaction that CO adds hydrogen and carbochain to increase, and product is F-T synthesis
Oil, F-T synthetic oil can be divided into naphtha cut, diesel oil distillate, heavy oil fraction and synthetic wax according to boiling range division.F- T synthesis produces
Object has a very wide distribution, and can carry out different working processes according to the reapective features of Fischer-Tropsch synthetic, obtain high added value
Chemicals, to improve the economic value of product and the economic benefit of enterprise.
The density of F-T synthetic wax is 0.88g/cm3Left and right, the decompressed wax oil of a little higher than Daqing crude oil of hydrogen content, carbon number point
Cloth is concentrated mainly on C16~C45Between, normal paraffin content is higher, the total F-T synthesis of mass content Zhan in low temperature F-T synthetic method
50% or more of oil.Its main manufacturing process is that hydroisomerizing produces good base oil lubricating oil or is hydrocracked life at present
Produce aviation kerosine and the diesel oil etc. of high quality.In addition, F-T synthetic wax can be also used for producing various advanced special wax it is contour attached
Value-added product.
CN101173190 discloses a kind of processing flow of Fischer-Tropsch synthesis oil, and this method includes adding hydrogen, low temperature oil wash, taking off
Tetra- part of carbon and PSA, synthetic oil enters hydrofining reactor through heat exchange by filter and hydrogen mixing, using heating
300~380 DEG C of stove heating enter hydrofining reactor, and the oxygenatedchemicals, unsaturated hydrocarbons and metal in abjection raw material are miscellaneous
Matter；Hydrotreated product enters the high separator of heat after exchanging heat and carries out oil, gas two-phase laminated flow, is exchanged heat and to heat stove heating laggard
Enter hydrocracking reactor to be hydrocracked, fractionating system is gone in crackate and refined products mixing；Hydrofinishing plus hydrogen are split
Change reactor and use two sections of series connection combined process flows, shares a set of circulation hydrogen system；Hydrofinishing generates oil and is hydrocracked generation
Oil shares a set of fractionating system, and fractionating system uses three-column process flow；Low temperature oil wash technique steam consumption of the present invention is few, lighter hydrocarbons recovery
More, related investment is few, and decarbonization process reduces energy consumption, improves hydrogen recovery rate.
CN104711019A discloses a kind of system and method using Fischer-Tropsch synthesis oil production diesel oil and jet fuel, should
Method includes hydrofinishing and hydro-upgrading two parts, and Fischer-Tropsch synthesis oil enters hydrofining reaction with after hydrogen mixing first
Device, product enter fractionating column, and for the naphtha cut being cut into as ethylene cracking material, it is anti-that diesel oil distillate enters hydroisomerization
Device is answered, tail oil enters hydrocracking reactor, enters fractionating column after two reactor product mixing, aviation kerosine and bavin can be obtained
Oil product, tail oil then recycle and remove cracker.It can be produced relative to common purification-cracking tandem process this method
Fine-quality diesel oil, aviation kerosine and add hydrogen wax oil product, have simple process, process stablize, equipment investment is few, low in cost, fortune
The turn-week phase is long, and diesel oil and aviation kerosine high income simultaneously can be directly as fuel or high-quality blend components.
Since the process of current F-T synthetic wax is mostly invested, the hydrogenation process that operating cost is high, and synthetic wax adds
Although the aviation kerosine and diesel oil distillate of high quality can be obtained after hydrogen cracking, it is low that a great deal of economic value can be generated
C1~C4The naphtha cut of alkane and low octane rating.Compared with being hydrocracked, catalytic cracking process mainly produces gasoline fraction,
And the gas composition that catalytic cracking generates is mainly the high low-carbon alkene of economic value, and it is former to can be used as good chemical industry after separation
Material.Also, only contain a small amount of oxygen in Fischer Tropsch waxes, is clean catalytically cracked material without hetero atoms such as S, N, and
The gasoline products of production are also the clean fuel of no sulphur.But the hydro carbons of Fischer Tropsch waxes composition is mainly positive structure and isohydrocarbon
Class is free of aromatic hydrocarbon and cycloalkane, therefore the Aromatic Hydrocarbon in Gasoline content that cracking generates is lower, and n-alkane and olefin(e) centent are high,
It is not able to satisfy requirement of the six standard clean gasoline of state to research octane number (RON).
CN106609154A discloses a kind of method by Fischer-Tropsch synthesis oil production gasoline.It should be by the way that Fischer-Tropsch be arranged in parallel
Synthetic oil catalyst cracker and aromatization reactor split Fischer-Tropsch synthesis oil and catalytic cracking in first reactor
Change reaction, obtains the first reaction stream；It is anti-that aromatisation raw material and aromatized catalyst are carried out to aromatisation in second reactor
It answers, obtains the second reaction stream；First reaction stream and the second reaction stream injection settler are separated, isolated
Reclaimable catalyst regenerator coke burning regeneration is at least partially into after stripping, and obtained regenerated catalyst is at least partly returned
First reactor is returned to be recycled.This method can be improved the arene content in gasoline products, so that the octane number of gasoline is improved,
And gasoline yield can also be correspondinglyd increase.But it only uses catalytic cracking unit and is unable to reach yield of gasoline maximization, the party
65~66.18wt% of yield of gasoline in method, because there is quite a few Fischer-Tropsch synthesis oil to be converted into liquefied gas；And China horse
On to execute stringent six gasoline quality standard of state, it is desirable that olefin(e) centent in gasoline is less than 15v%, and arene content is less than
35v%, sulfur content are less than 10ug/g, and research octane number (RON) reaches 90 or more.It only uses catalyst cracker and aromatisation is anti-
Device is answered, the alkene in gasoline can not be fully converted into high-knock rating gasoline fraction, which does not illustrate produced gasoline yet
In olefin(e) centent.Therefore, the low alkene for meeting six quality standard of state, high-octane rating cleaning vapour are produced by Fischer-Tropsch synthesis oil
Oil, it is also necessary to new process.
CN104140847A discloses a kind of method by F- T synthesis naphtha production high-knock rating gasoline.This method master
It to be directed to F- T synthesis naphtha, carbon number distribution is concentrated mainly on C5~C12Between, boiling range range initial boiling point~200 DEG C use
The invention can be effectively by the F- T synthesis naphtha of low octane rating, i.e. the F- T synthesis gasoline fraction of low octane rating is converted into height
Octane rating gasoline fractions, the yield of F- T synthesis gasoline fraction are only 71~75wt%, and gasoline fraction loss is big, and after modification
Gasoline olefin, whether arene content meets six gasoline standard of state does not refer to.
From the point of view of existing publication, directly produced by Fischer Tropsch waxes meet the patent of six standard clean gasoline of state compared with
Few, Fischer Tropsch waxes carbon number distribution is concentrated mainly on C16~C45Between, normal paraffin content is high, and 300~800 DEG C of boiling range range,
Belonging to the heavy distillat in Fischer-Tropsch synthesis oil, this may be mainly to be influenced by raw material composition and property, and difficulty of processing is big, currently without
Suitable processing technology.
Summary of the invention
It is an object of the present invention to provide a kind of methods that Fischer Tropsch waxes comprehensively utilize production clean gasoline.The party
Method by F- T synthesis wax cracking fecund gasoline fraction, and uses aromatisation device solution first with the advantage of catalytic cracking process
The high problem of Fischer Tropsch waxes catalytically cracked gasoline distillate olefins content of having determined, while by iso-butane, the n-butene in cracked gas
By producing gasoline alkylate fraction, isobutene produces class gasoline alkylate fraction by selective superposition-hydrogenation technique, most
It is a large amount of to realize by the target of Fischer Tropsch waxes production six standard clean gasoline of high-octane rating state.
In order to achieve the above object, the present invention provides a kind of method that Fischer Tropsch waxes comprehensively utilize production clean gasoline, institute
The method of stating includes the following steps: that Fischer Tropsch waxes, which are carried out cracking reaction, obtains cracking oil gas, and obtained oil gas is by being fractionated
To rich gas, light gasoline fraction, heavy naphtha, diesel oil distillate and recycle oil；Light gasoline fraction therein is obtained by aromatisation
Aromatisation gasoline fraction；Rich gas pass through isolated iso-butane, n-butene and isobutene, obtained iso-butane and n-butene into
Row alkylation obtains gasoline alkylate fraction；Obtained isobutene carries out selective superposition-hydrotreating, obtains class alkylation vapour
Oil distillate；Obtained heavy naphtha, aromatisation gasoline fraction, gasoline alkylate fraction and class gasoline alkylate fraction are carried out
It reconciles to obtain the clean gasoline.
Some specific embodiments according to the present invention, wherein the density of Fischer Tropsch waxes is 0.80~0.98 (preferably 0.85
~0.95g/cm3)。
Some specific embodiments according to the present invention, wherein the light gasoline fraction be rich in light dydrocarbon, C 6 olefin it is light
Gasoline fraction；The heavy naphtha is the heavy naphtha rich in aromatic hydrocarbons.
Some specific embodiments according to the present invention, wherein the Fischer Tropsch waxes are to be split in the presence of a catalyst
Change reaction and obtains cracking oil gas；The catalyst is the Y type molecular sieve and ZSM-5 molecular sieve that content of rare earth is 0.5-2.5wt%
The composite catalyst being mixed into.
Some specific embodiments according to the present invention, wherein the ZSM-5 molecular sieve silica alumina ratio is 150-400.
Some specific embodiments according to the present invention, wherein Y type molecular sieve and ZSM-5 molecule in the composite catalyst
The mass ratio of sieve is (4-9): 1.
Rare earth in the composite catalyst is the rare earth element that this field is routinely added, and for example can be lanthanide series,
It specifically for example can be selected from La (lanthanum), Ce (cerium), Pr (praseodymium), Nd (neodymium), Pm (promethium), Sm (samarium) and Eu (europium)；And according to this hair
Bright some specific embodiments, wherein the rare earth in the composite catalyst is selected from lanthanum.
Some specific embodiments according to the present invention, wherein the Fischer Tropsch waxes first pass through preheating, are then being catalyzed again
Cracking reaction is carried out in the presence of agent obtains cracking oil gas.
Some specific embodiments according to the present invention, wherein the Fischer Tropsch waxes, which first pass through, is preheating to 180-260 DEG C,
Then it carries out cracking reaction in the presence of a catalyst again and obtains cracking oil gas.
Some specific embodiments according to the present invention, wherein the Fischer Tropsch waxes, which first pass through, is preheating to 200-220 DEG C,
Then it carries out cracking reaction in the presence of a catalyst again and obtains cracking oil gas.
Some specific embodiments according to the present invention, wherein the recycle oil is recycled back to fractionating step and continues to be fractionated.
Some specific embodiments according to the present invention, wherein the octane number of the aromatisation gasoline fraction is more than or equal to 92.
Some specific embodiments according to the present invention, wherein the octane number of the aromatisation gasoline fraction is 92-95.
Some specific embodiments according to the present invention, wherein the octane number of the gasoline alkylate fraction is more than or equal to 96.
Some specific embodiments according to the present invention, wherein the octane number of the gasoline alkylate fraction is 96-98.
Some specific embodiments according to the present invention, wherein the octane number of the class gasoline alkylate fraction is more than or equal to
96。
Some specific embodiments according to the present invention, wherein the octane number of the class gasoline alkylate fraction is 98-100.
Some specific embodiments according to the present invention, wherein the olefin(e) centent of the clean gasoline is less than 15v%, aromatic hydrocarbons
Content is less than 35v%, and sulfur content is more than or equal to 90 less than 10 μ g/g, research octane number (RON).
Some specific embodiments according to the present invention, wherein the research octane number (RON) of the clean gasoline is 90-95.
Some specific embodiments according to the present invention, wherein the cracking reaction is carried out in riser reactor, instead
Answer condition include outlet temperature of riser be 450-550 DEG C, oil ratio 4-15, reaction time 2-15s, reaction pressure is normal
Pressure.
Some specific embodiments according to the present invention, wherein outlet temperature of riser is 470-510 DEG C in cracking reaction.
Some specific embodiments according to the present invention, wherein oil ratio is 6-10 in cracking reaction.
Some specific embodiments according to the present invention, wherein the reaction time is 4-10s in cracking reaction.
Some specific embodiments according to the present invention, wherein the reaction condition of the aromatisation include: air speed be 0.1~
5h-1, reaction temperature is 250~560 DEG C, and reaction pressure is 0.1~3.0MPa.
Some specific embodiments according to the present invention, wherein air speed is 0.5~3h in aromatisation-1。
Some specific embodiments according to the present invention, wherein reaction temperature is 300~500 DEG C in aromatisation.
Some specific embodiments according to the present invention, wherein reaction pressure is 0.2~1.0MPa in aromatisation.
Some specific embodiments according to the present invention, wherein the alkylated reaction condition include: air speed be 1~
10h-1, reaction temperature is 0~100 DEG C, and reaction pressure is 0.4~3.5MPa, and alkane alkene molar ratio is 1~20.
Some specific embodiments according to the present invention, wherein air speed is 3~8h in alkylation-1。
Some specific embodiments according to the present invention, wherein reaction temperature is 5~40 DEG C in alkylation.
Some specific embodiments according to the present invention, wherein reaction pressure is 0.4~2.0MPa in alkylation.
Some specific embodiments according to the present invention, wherein alkane alkene molar ratio is 5~10 in alkylation.
Some specific embodiments according to the present invention, wherein the selective superposition of the selective superposition-hydrotreating
Reaction condition includes: 0.5~3h of air speed-1, 50~300 DEG C of reaction temperature, 0.4~3.5MPa of reaction pressure；Add the reaction item of hydrogen
Part includes: 0.5~3h of air speed-1, 50~300 DEG C of reaction temperature, 0.4~3.5MPa of reaction pressure, hydrogen/oil mol ratio 0.05~6.
Some specific embodiments according to the present invention, wherein the air speed in selective superposition is 0.5~1.5h-1。
Some specific embodiments according to the present invention, wherein the reaction temperature in selective superposition is 60~200 DEG C.
Some specific embodiments according to the present invention, wherein the reaction pressure in selective superposition is 0.5~2.0MPa.
Some specific embodiments according to the present invention, wherein adding the air speed in hydrogen is 0.5~1.5h-1。
Some specific embodiments according to the present invention, wherein adding the reaction temperature in hydrogen is 100~200 DEG C.
Some specific embodiments according to the present invention, wherein adding the reaction pressure in hydrogen is 1.0~2.0MPa.
Some specific embodiments according to the present invention, wherein adding the hydrogen/oil mol ratio in hydrogen is 0.2~2.
Some specific embodiments according to the present invention, wherein the Fischer Tropsch waxes, which first pass through, is preheating to 210 DEG C, then
It carries out cracking reaction in the presence of a catalyst again and obtains cracking oil gas；The cracking reaction is carried out in riser reactor,
Reaction condition includes that outlet temperature of riser is 490 DEG C, and oil ratio 8, reaction time 8s, reaction pressure is normal pressure；Aromatization
The reaction condition of change includes: that air speed is 1.5h-1, reaction temperature is 400 DEG C, reaction pressure 0.6MPa；It is described alkylated anti-
Answer condition include: air speed be 5h-1, reaction temperature is 24 DEG C, reaction pressure 1.2MPa, alkane alkene molar ratio 30；The selectivity
The reaction condition of overlapping-hydrotreating selective superposition includes: air speed 1.0h-1, 130 DEG C of reaction temperature, reaction pressure
1.25MPa；The reaction condition for adding hydrogen includes: air speed 1.0h-1, 150 DEG C of reaction temperature, reaction pressure 1.5MPa, hydrogen/oil mol ratio
1.1。
Some specific embodiments according to the present invention, wherein urged the described method includes: entering after Fischer Tropsch waxes are preheated
The riser reactor for changing cracking unit generates cracking oil gas with regenerated catalyst contact cracking, and oil gas is filled by catalytic cracking
The fractionating system set be separated into rich gas, rich in light dydrocarbon, the light petrol of C 6 olefin, rich in the heavy naphtha of aromatic hydrocarbons, diesel oil evaporates
Point and recycle oil.Wherein, recycle oil is recycled back to catalytic cracking unit and carries out freshening；Diesel oil distillate goes out catalytic cracking dress as product
It sets；Heavy naphtha rich in aromatic hydrocarbons enters gasoline attemperation apparatus；Light petrol rich in light dydrocarbon, C 6 olefin enters aromatization makeup
It sets, the aromatisation gasoline fraction that 95 or more octane number is rich in aromatic hydrocarbons is obtained after reaction, subsequently into gasoline attemperation apparatus；It urges
Change cracking rich gas iso-butane, n-butene are isolated after gas fractionation unit, into alkylation process produce octane number 96 with
On gasoline alkylate fraction, subsequently into gasoline attemperation apparatus.Catalytic cracking rich gas is isolated after gas fractionation unit
Isobutene, into selective superposition-hydrogenation technique 98 or more octane number of production class gasoline alkylate fraction, subsequently into vapour
Oily attemperation apparatus.It is reconciled by the gasoline fraction for producing four kinds of technique, olefin(e) centent can be obtained less than 15v%, virtue
Hydrocarbon content is less than 35v%, and sulfur content is less than 10ug/g, and research octane number (RON) reaches 90 or more six standard clean vapour of state
Oil.
Some specific embodiments according to the present invention, wherein the method specifically includes:
(1) after preheated to 180~260 DEG C of raw material (preferably 200~220 DEG C), into the riser of catalytic cracking unit
Reactor, reaction condition be 450~550 DEG C of outlet temperature of riser (preferably 470~510 DEG C), oil ratio 4~15 (preferably 6~
10), 2~15s of reaction time (preferably 4~10s), reaction pressure normal pressure generate cracked oil after contacting cracking with regenerated catalyst
Gas, oil gas by catalytic cracking unit fractionating system by routine operation be separated into rich gas, rich in light dydrocarbon, C 6 olefin it is light
Gasoline, the heavy naphtha rich in aromatic hydrocarbons, diesel oil distillate and recycle oil.
(2) recycle oil is recycled back to catalytic cracking unit and reenters riser reactor freshening；Diesel oil distillate is as product
Catalytic cracking unit out；
(3) heavy naphtha rich in aromatic hydrocarbons enters gasoline attemperation apparatus；
(4) light petrol rich in light dydrocarbon, C 6 olefin enters aromatisation device, in 0.1~5h of air speed-1(preferably 0.5~
3h-1), 250~560 DEG C of reaction temperature (preferably 300~500 DEG C), 0.1~3.0MPa of reaction pressure (preferably 0.2~1.0MPa)
Under the conditions of by reaction after obtain 92 or more octane number aromatisation gasoline fraction, subsequently into gasoline attemperation apparatus；
(5) catalytic cracking rich gas isolates iso-butane, n-butene after gas fractionation unit routine operation, into alkyl
Makeup is set, in 1~10h of air speed-1(preferably 3~8h-1), 0~100 DEG C of reaction temperature (preferably 5~40 DEG C), reaction pressure 0.4~
3.5MPa (preferably 0.4~2.0MPa), alkane alkene molar ratio 5~60 convert under the conditions of (preferably 20~40), produce octane number 96 with
On gasoline alkylate fraction, subsequently into gasoline attemperation apparatus.
(6) catalytic cracking rich gas isolates isobutene after gas fractionation unit routine operation, folded into selectivity
Conjunction-hydrogenation plant, in 0.5~3h of air speed-1(preferably 0.5~1.5h-1), 50~300 DEG C (preferably 60~200 of reaction temperature
DEG C), building-up reactions is carried out under the conditions of 0.4~3.5MPa of reaction pressure (preferably 0.5~2.0MPa), in 0.5~3h of air speed-1It is (excellent
Select 0.5~1.5h-1), 50~300 DEG C of reaction temperature (preferably 100~200 DEG C), 0.4~3.5MPa of reaction pressure (preferably 1.0~
2.0MPa), hydrogenation reaction is carried out under the conditions of hydrogen/oil mol ratio 0.05~6 (preferably 0.2~2), produces the class of 96 or more octane number
Gasoline alkylate fraction, subsequently into gasoline attemperation apparatus.
In conclusion the present invention provides a kind of methods that Fischer Tropsch waxes comprehensively utilize production clean gasoline.The present invention
Method have the advantages that
(1) catalytic cracking process is Non-adding hydrogen, and plant investment, operating cost are low, strong to adaptability to raw material, is heavy
The main technique of cracking hydrocarbon fecund gasoline is, it can be achieved that F- T synthesis wax cracking fecund gasoline fraction.
(2) light dydrocarbon, C 6 olefin are more in the gasoline fraction produced due to Fischer Tropsch waxes catalytic cracking, and direct hydrogenation can give birth to
Gasoline fraction at research octane number (RON) less than 50 can solve Fischer Tropsch waxes catalytically cracked gasoline using aromatisation device and evaporate
The problem for dividing olefin(e) centent high, and obtain the gasoline fraction rich in aromatic hydrocarbons of 92 or more research octane number (RON).
(3) using alkylation process by cracked gas iso-butane, normal butylenes be research octane number (RON) be up to 96 with
Upper gasoline alkylate fraction can increase by the yield of Fischer Tropsch waxes production six standard clean gasoline of high-octane rating state, and
Improve quality of gasoline.
It (4) is that research octane number (RON) is up to 98 by the isobutene conversion in cracked gas using selective superposition-hydrogenation technique
The above gasoline alkylate fraction can maximize and increase by the production of Fischer Tropsch waxes production six standard clean gasoline of high-octane rating state
Amount.
(5) four kinds of process combinations, are reconciled by gasoline fraction, can be produced olefin(e) centent with maximum and are less than 15v%, aromatic hydrocarbons
Content is less than 35v%, and sulfur content is more than or equal to 90 six quality standard clean gasoline of state less than 10 μ g/g, research octane number (RON).
Detailed description of the invention
Fig. 1 is the equipment schematic diagram of the embodiment of the present invention 1.
Specific embodiment
Below by way of the beneficial effect of the specific embodiment implementation process that the present invention will be described in detail and generation, it is intended to which help is read
Reader more fully understands essence and feature of the invention, does not limit the scope of the present invention.
Embodiment 1
Method flow is described as follows: into catalytic cracking riser reactor 2, (equipment is such as through pipeline 1 for the raw material after preheating
Shown in Fig. 1), the oil gas of generation enters catalytic cracking fractionating system 4 through pipeline 3.The catalysis that catalytic cracking fractionating system 4 is isolated
Cracking rich gas enters gas fractionation unit 10 through pipeline 5, and the isobutene isolated enters selective superposition-plus hydrogen through pipeline 11
Device 14, product type gasoline alkylate enter gasoline attemperation apparatus 20 through pipeline 15；Gas fractionation unit 10 isolates isobutyl
Through the entrance alkyl plant 16 of pipeline 12, product gasoline alkylate enters gasoline attemperation apparatus 20 through pipeline 17 for alkane and n-butene；
The remaining gas that gas fractionation unit 10 is isolated is through 13 ejector of pipeline.What catalytic cracking fractionating system 4 was isolated is rich in
Light dydrocarbon, C 6 olefin light petrol group lease making pipeline 6 enter aromatisation device 18, aromatisation gasoline after reaction through pipeline 19 into
Enter gasoline attemperation apparatus 20；The heavy naphtha rich in aromatic hydrocarbons that catalytic cracking fractionating system 4 is isolated enters gasoline through pipeline 7
Attemperation apparatus 20；The diesel oil distillate that catalytic cracking fractionating system 4 is isolated is as product through 8 ejector of pipeline；Catalytic cracking
The freshening oil distillate that fractionating system 4 is isolated is recycled back to catalytic cracking unit through pipeline 9 and reenters riser reactor freshening.
The blended gasoline of 20 product of gasoline attemperation apparatus is through 21 ejector of pipeline.
The raw material that the present embodiment uses is Fischer Tropsch waxes, and property is shown in Table 1, and table 2 is that Fischer Tropsch waxes catalytic cracking obtains
The product distribution obtained.
The catalyst of the present embodiment cracking reaction are as follows: the Y type molecular sieve and ZSM-5 molecular sieve mixing that lanthanum content is 1wt%
At composite catalyst；The mass ratio of Y type molecular sieve and ZSM-5 molecular sieve is 8:1, the ZSM-5 in the composite catalyst
Molecular sieve silica alumina ratio is 350.
Table 1
Table 2
Wherein catalytically cracked gasoline fraction yield is 62.06wt%, and wherein light FCC gasoline fraction yield is
34.57wt%, hydrocarbon composition and research octane number (RON) are shown in Table 3；Catalytic cracking heavy petrol reconciliation fraction yield is 27.49wt%,
Its hydrocarbon composition and research octane number (RON) are shown in Table 4.
Table 3
Table 4
Light FCC gasoline fraction is after aromatisation, the yield of gasoline of the gasoline reconciliation fraction rich in aromatic hydrocarbons of acquisition
For 29.73wt% (on the basis of F- T synthesis wax stock), hydrocarbon composition and research octane number (RON) are shown in Table 5.
Table 5
Iso-butane, n-butene yield in catalytic cracking liquefied gas are 4.0wt% and 9.2wt%, by alkylated reaction
Afterwards, the gasoline alkylate of acquisition reconciles fraction yield as 8.0wt%, and hydrocarbon composition and research octane number (RON) are shown in Table 6.
Table 6
Isobutene yield in catalytic cracking liquefied gas is 8.4wt%, after selective superposition-hydrogenation technique reaction,
The class gasoline alkylate of acquisition reconciles fraction yield as 8.4wt%, and hydrocarbon composition and research octane number (RON) are shown in Table 7.
Table 7
The catalytic cracking heavy petrol of 27.49wt% is reconciled into fraction, the isomerization gasoline of 34.57wt% reconciles fraction,
The gasoline alkylate reconciliation fraction of 8.0wt% is reconciled, and the state six that can obtain the research octane number (RON) 91 of 70.06wt% is clear
Clean gasoline, hydrocarbon composition and research octane number (RON) are shown in Table 8.
Table 8
Method flow is described as follows: the raw material after preheating enters catalytic cracking riser reactor 2 through pipeline 1, generation
Oil gas enters catalytic cracking fractionating system 4 through pipeline 3.The 4 catalytic cracking rich gases isolated enter gas fractionation unit through pipeline 5
10, the isobutene that gas fractionation unit 10 is isolated enters selective superposition-hydrogenation plant 14 through pipeline 11, and selectivity is folded
The product type gasoline alkylate of conjunction-hydrogenation plant 14 enters gasoline attemperation apparatus 20 through pipeline 15；Gas fractionation unit 10 separates
Through the entrance alkyl plant 16 of pipeline 12, product gasoline alkylate enters gasoline through pipeline 17 and reconciles for iso-butane and n-butene out
Device 20；The remaining gas that gas fractionation unit 10 is isolated is through 13 ejector of pipeline.Catalytic cracking fractionating system 4 is isolated
Rich in light dydrocarbon, C 6 olefin light petrol group lease making pipeline 6 enter hysomer device 18, the isomerization gasoline after reaction
Enter gasoline attemperation apparatus 20 through pipeline 19；The heavy naphtha rich in aromatic hydrocarbons that catalytic cracking fractionating system 4 is isolated is through pipe
Line 7 enters gasoline attemperation apparatus 20；The diesel oil distillate that catalytic cracking fractionating system 4 is isolated is drawn through pipeline 8 as product and is filled
It sets；The 4 freshening oil distillates isolated are recycled back to catalytic cracking unit through pipeline 9 and reenter riser reactor freshening.Gasoline
The product blended gasoline of attemperation apparatus 20 is through 21 ejector of pipeline.
The raw material that the present embodiment uses is Fischer Tropsch waxes, and property is shown in Table 1.1, and table 1.2 is the operation of each group technology
Condition, table 1.3 are the product distribution that Fischer Tropsch waxes catalytic cracking obtains.
1.1 feedstock property of table
1.2 group technology operating condition of table
The distribution of 1.3 catalytic cracking product of table
1.4 light FCC gasoline fraction property of table and heavy naphtha property
Wherein catalytically cracked gasoline fraction yield is 62.06wt%, and wherein light FCC gasoline fraction yield is
34.57wt%, catalytic cracking heavy petrol reconcile fraction yield as 27.49wt% (being shown in Table 1.3)；Its hydrocarbon composition and is ground at sulfur content
The method octane number of studying carefully is shown in Table 1.4.
Light FCC gasoline fraction is after aromatisation, the aromatisation gasoline reconciliation fraction hydrocarbon composition of acquisition, sulfur content
1.5 are shown in Table with research octane number (RON).Iso-butane, n-butene in catalytic cracking liquefied gas after alkylated reaction, acquisition
Gasoline alkylate hydrocarbon composition, sulfur content and research octane number (RON) are shown in Table 1.5.It is anti-that isobutene carries out selective superposition-hydrotreating
Class gasoline alkylate hydrocarbon composition, sulfur content and the research octane number (RON) that should be obtained are shown in Table 1.5.
1.5 aromatisation gasoline fraction property of table, alkylation and class gasoline alkylate fraction property
On the basis of the conversion of Fischer Tropsch waxes, the catalytic cracking heavy petrol reconciliation that catalytic cracking obtains 27.49wt% evaporates
Point, light petrol aromatisation obtains the aromatisation gasoline reconciliation fraction of 25.92wt%, and the iso-butane of 4.0wt% is reacted with n-butene
The gasoline alkylate reconciliation fraction of 8.0wt% is obtained, the isobutene of 10.1wt% carries out selective superposition-hydrotreating reaction
The class gasoline alkylate reconciliation fraction of 10.1wt% is obtained, the gasoline component that four group technologies obtain reconcile and can obtain
Six clean gasoline of state of the research octane number (RON) 93.2 of 71.15wt%, hydrocarbon composition and research octane number (RON) are shown in Table 1.6.
Each group technology blended gasoline yield of table 1.6 and the clean gasoline property that reconciles
Embodiment 2
Method flow brief introduction and embodiment 1 are consistent.
The raw material that the present embodiment uses is Fischer Tropsch waxes, and property is shown in Table 2.1, and table 2.2 is the operation of each group technology
Condition, table 2.3 are the product distribution that Fischer Tropsch waxes catalytic cracking obtains.
The catalyst of the present embodiment cracking reaction are as follows: the Y type molecular sieve and ZSM-5 molecular sieve mixing that lanthanum content is 2wt%
At composite catalyst；The mass ratio of Y type molecular sieve and ZSM-5 molecular sieve is 5:1, the ZSM-5 in the composite catalyst
Molecular sieve silica alumina ratio is 180.
2.1 feedstock property of table
2.2 group technology operating condition of table
The distribution of 2.3 catalytic cracking product of table
2.4 light FCC gasoline fraction property of table and heavy naphtha property
Wherein catalytically cracked gasoline fraction yield is 57.49wt%, and wherein light FCC gasoline fraction yield is
28.21wt%, catalytic cracking heavy petrol reconcile fraction yield as 29.28wt% (being shown in Table 2.3)；Its hydrocarbon composition and is ground at sulfur content
The method octane number of studying carefully is shown in Table 2.4.
Light FCC gasoline fraction is after aromatisation, the aromatisation gasoline reconciliation fraction hydrocarbon composition of acquisition, sulfur content
2.5 are shown in Table with research octane number (RON).Iso-butane, n-butene in catalytic cracking liquefied gas after alkylated reaction, acquisition
Gasoline alkylate hydrocarbon composition, sulfur content and research octane number (RON) are shown in Table 2.5.It is anti-that isobutene carries out selective superposition-hydrotreating
Class gasoline alkylate hydrocarbon composition, sulfur content and the research octane number (RON) that should be obtained are shown in Table 2.5.
2.5 aromatisation gasoline fraction property of table, alkylation and class gasoline alkylate fraction property
On the basis of the conversion of Fischer Tropsch waxes, the catalytic cracking heavy petrol reconciliation that catalytic cracking obtains 29.28wt% evaporates
Point, light petrol aromatisation obtains 19.75% isomerization gasoline reconciliation fraction, and the isobutane and butene of 6.5wt%, which reacts, to be obtained
The gasoline alkylate reconciliation fraction of 13.0wt%, the isobutene of 9.7wt% carry out selective superposition-hydrotreating reaction and obtain
The class gasoline alkylate reconciliation fraction of 9.7wt%, the gasoline component that four group technologies obtain reconcile and can obtain
Six clean gasoline of state of the research octane number (RON) 94.7 of 71.73wt%, hydrocarbon composition and research octane number (RON) are shown in Table 2.6.
Each group technology blended gasoline yield of table 2.6 and the clean gasoline property that reconciles
Embodiment 3
Method flow brief introduction and embodiment 1 are consistent.
The raw material that the present embodiment uses is Fischer Tropsch waxes, and property is shown in Table 3.1, and table 3.2 is the operation of each group technology
Condition, table 3.3 are the product distribution that Fischer Tropsch waxes catalytic cracking obtains.
The catalyst of the present embodiment cracking reaction are as follows: the Y type molecular sieve and ZSM-5 molecular sieve that lanthanum content is 1.5wt% are mixed
The composite catalyst of synthesis；The mass ratio of Y type molecular sieve and ZSM-5 molecular sieve is 7:1, the ZSM- in the composite catalyst
5 molecular sieve silica alumina ratios are 200.
3.1 feedstock property of table
3.2 group technology operating condition of table
The distribution of 3.3 catalytic cracking product of table
3.4 light FCC gasoline fraction property of table and heavy naphtha property
Wherein catalytically cracked gasoline fraction yield is 59.78wt%, and wherein light FCC gasoline fraction yield is
31.39wt%, catalytic cracking heavy petrol reconcile fraction yield as 28.39wt% (being shown in Table 3.3)；Its hydrocarbon composition and is ground at sulfur content
The method octane number of studying carefully is shown in Table 3.4.
Light FCC gasoline fraction is after aromatisation, the aromatisation gasoline reconciliation fraction hydrocarbon composition of acquisition, sulfur content
3.5 are shown in Table with research octane number (RON).Iso-butane, n-butene in catalytic cracking liquefied gas after alkylated reaction, acquisition
Gasoline alkylate hydrocarbon composition, sulfur content and research octane number (RON) are shown in Table 3.5.It is anti-that isobutene carries out selective superposition-hydrotreating
Class gasoline alkylate hydrocarbon composition, sulfur content and the research octane number (RON) that should be obtained are shown in Table 3.5.
3.5 aromatisation gasoline fraction property of table, alkylation and class gasoline alkylate fraction property
On the basis of Fischer Tropsch waxes, catalytic cracking obtains the catalytic cracking heavy petrol reconciliation fraction of 28.39wt%, light vapour
Oily aromatisation obtains 25.11% aromatisation gasoline reconciliation fraction, and the iso-butane of 6.7wt% reacts acquisition with n-butene
The gasoline alkylate reconciliation fraction of 13.4wt%, the isobutene of 11.0wt% carry out selective superposition-hydrotreating reaction and obtain
The class gasoline alkylate reconciliation fraction of 11.0wt%, the gasoline component that four group technologies obtain reconcile and can obtain
Six clean gasoline of state of the research octane number (RON) 94.5 of 77.90wt%, hydrocarbon composition and research octane number (RON) are shown in Table 3.6.
Each group technology blended gasoline yield of table 3.6 and the clean gasoline property that reconciles
According to the regulation of national correlation department, six B standard of motor petrol state rises from January 1st, 2023 and executes.Three implementations
The blended gasoline quality of example is above six B standard of motor petrol state, and due to oxide-free, for national next step ethanol vapor
The production of oil leaves reconciliation space.
Claims (10)
1. a kind of method of Fischer Tropsch waxes comprehensive utilization production clean gasoline, wherein described method includes following steps: will take
Support synthetic wax carries out cracking reaction and obtains cracking oil gas, and obtained oil gas obtains rich gas, light gasoline fraction, heavy petrol by fractionation
Fraction, diesel oil distillate and recycle oil；Light gasoline fraction therein obtains aromatisation gasoline fraction by aromatisation；Rich gas is through excessive
From iso-butane, n-butene and isobutene is obtained, obtained iso-butane and n-butene, which is alkylated to obtain gasoline alkylate, to be evaporated
Point；Obtained isobutene carries out selective superposition-hydrotreating, obtains class gasoline alkylate fraction；Obtained heavy petrol is evaporated
Divide, aromatisation gasoline fraction, gasoline alkylate fraction and class gasoline alkylate fraction carry out reconciling to obtain the cleaning vapour
Oil.
2. according to the method described in claim 1, wherein, the light gasoline fraction is the light petrol rich in light dydrocarbon, C 6 olefin
Fraction；The heavy naphtha is the heavy naphtha rich in aromatic hydrocarbons.
3. according to the method described in claim 1, wherein, the Fischer Tropsch waxes are to carry out cracking reaction in the presence of a catalyst
Obtaining cracking oil gas, (the preferably described Fischer Tropsch waxes first pass through preheating and (are preferably preheating to 180-260 DEG C (to be more preferably preheating to
200-220 DEG C)), then carry out cracking reaction in the presence of a catalyst again and obtain cracking oil gas)；The catalyst contains for rare earth
The Y type molecular sieve that amount is 0.5-2.5wt% and composite catalyst (the preferably ZSM-5 molecular sieve sial that ZSM-5 molecular sieve is mixed into
Molar ratio is 150-400) (mass ratio of Y type molecular sieve and ZSM-5 molecular sieve is (4-9) in the preferably described composite catalyst:
1)。
4. according to the method described in claim 1, wherein, the recycle oil is recycled back to fractionating step and continues to be fractionated.
5. according to the method described in claim 1, wherein, the octane number of the aromatisation gasoline fraction is more than or equal to 92 (preferably
For 92-95)；The octane number of the gasoline alkylate fraction is more than or equal to 96 (preferably 96-98)；The class gasoline alkylate evaporates
The octane number divided is more than or equal to 98 (preferably 98-100).
6. according to the method described in claim 1, wherein, the olefin(e) centent of the clean gasoline is less than 15v%, and arene content is small
In 35v%, sulfur content is more than or equal to 90 (preferably 90-95) less than 10 μ g/g, research octane number (RON).
7. reacting item according to the method described in claim 1, wherein, the cracking reaction is carried out in riser reactor
Part includes that outlet temperature of riser is 450-550 DEG C (preferably 470-510 DEG C), and oil ratio is 4-15 (preferably 6-10), instead
It is 2-15s (preferably 4-10s) between seasonable, reaction pressure is normal pressure.
8. according to the method described in claim 1, wherein, the reaction condition of the aromatisation includes: that air speed is 0.1~5h-1It is (excellent
Select 0.5~3h-1), reaction temperature be 250~560 DEG C (preferably 300~500 DEG C), reaction pressure be 0.1~3.0MPa (preferably
0.2~1.0MPa).
9. according to the method described in claim 1, wherein, the alkylated reaction condition includes: that air speed is 1~10h-1It is (excellent
It is selected as 3~8h-1), reaction temperature is 0~100 DEG C (preferably 5~40 DEG C), and reaction pressure is 0.4~3.5MPa (preferably 0.4
~2.0MPa), alkane alkene molar ratio is 1~20 (preferably 5~10).
10. according to the method described in claim 1, wherein, the reaction of the selective superposition of the selective superposition-hydrotreating
Condition includes: 0.5~3h of air speed-1(preferably 0.5~1.5h-1), 50~300 DEG C of reaction temperature (preferably 60~200 DEG C), reaction
0.4~3.5MPa of pressure (preferably 0.5~2.0MPa)；The reaction condition for adding hydrogen includes: 0.5~3h of air speed-1(preferably 0.5~
1.5h-1), 50~300 DEG C of reaction temperature (preferably 100~200 DEG C), 0.4~3.5MPa of reaction pressure (preferably 1.0~
2.0MPa), hydrogen/oil mol ratio 0.05~6 (preferably 0.2~2).
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| CN111925822A (en) * | 2020-07-17 | 2020-11-13 | 中科合成油工程有限公司 | Method for preparing high-octane gasoline and device for implementing method |
| CN112725004A (en) * | 2020-12-14 | 2021-04-30 | 中科合成油内蒙古有限公司 | Method and device for producing high-octane gasoline from Fischer-Tropsch synthesis intermediate product |
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| CN106609154A (en) * | 2015-10-21 | 2017-05-03 | 中国石油化工股份有限公司 | Method or producing gasoline from Fischer-Tropsch synthetic oil |
| CN109705908A (en) * | 2017-10-26 | 2019-05-03 | 中国石油化工股份有限公司 | A kind of catalytic cracking combination method and system of fecund clean gasoline with high octane |
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