CN106367116A - Method for producing aromatic hydrocarbons by using reforming raffinate oil - Google Patents
Method for producing aromatic hydrocarbons by using reforming raffinate oil Download PDFInfo
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Abstract
The present invention discloses a method for producing aromatic hydrocarbons by using reforming raffinate oil. The method specifically comprises that reforming raffinate oil is dewatered with a drying tower, the dewatered reforming raffinate oil is heated with the pre-heater to achieve a reaction temperature, the heated reforming raffinate oil enters an aromatization reactor and an aromatization reaction is performed, the aromatization reaction products pass through a separation tower and an extraction tower so as to be divided into hydrogen, dry gas, liquefied gas, C5<+> non-aromatic hydrocarbon and light aromatic hydrocarbon, the C5<+> non-aromatic hydrocarbon enters a fractionation tower and is subjected to fractionation cutting to obtain C5-C6 distillates and C6-C7 distillates, and the C6-C7 distillates return to the aromatization reactor so as to be continuously aromatized. According to the present invention, the reforming raffinate oil can be effectively converted into the light aromatic hydrocarbons, the light aromatic hydrocarbon yield can achieve 50-60%, and the high octane number gasoline blending component having the research octane numbers (RON) of 87-90 is by-produced; and with the application of the method in the blending of the catalytic cracking gasoline, the olefin content can be substantially reduced, the processing utilization channel of the reforming raffinate oil is expanded, and the utilization value of the reforming raffinate oil is improved.
Description
Technical field
The invention belongs to technical field of petrochemical industry, it is a kind of catalysis conversion method of reforming raffinate oil, specifically, be a kind of
The method producing aromatic hydrocarbons and high-knock rating gasoline blend component using reforming raffinate oil.
Background technology
With the rapid growth of China's economy, the fast development of polyester industrial, growing to the demand of aromatic hydrocarbons, make urging of China
Change reformer production capacity, there has also been very big growth, catalytic reforming also from produce high-knock rating gasoline based on turn to
Produce based on aromatic hydrocarbons.In addition to obtaining most of aromatic hydrocarbons, also substantial portion of non-aromatic component is reforming raffinate oil to reformer, weight
Whole raffinating oil accounts for the 30～40% of reformed oil, and the yield of reforming raffinate oil increases with the enlarging of reformer.
At present, reforming raffinate oil is mainly used as gasoline blend component or produces all kinds of solvent naphthas, is used as ethylene cracking material on a small quantity.
Due to reforming raffinate oil octane number (ron) only 60～70, limited as gasoline blend component addition, added value is relatively low；
On the other hand, reforming raffinate oil mainly containing c5～c7 hydrocarbon increasingly strict with the environmental protection requirement of China, boiling range≤90 DEG C, its
Range as solvent naphtha is also limited；And reforming raffinate oil isoparaffin content is high, as ethylene cracking material, with directly
Evaporate Petroleum to compare, ethylene yield is relatively low.
Reforming raffinate oil main component is c5～c7 isomery, n-alkane, a small amount of cycloalkane, alkene, aromatic hydrocarbons, and octane number is low,
But the not objectionable impurities such as Nitrogen or sulfur-compounds and heavy metal, are corresponding lightweight such as by c6～c7 alkane transformations of reforming raffinate oil
Aromatic hydrocarbons, has very big appreciation potential.
But due to the reforming raffinate oil mainly isoparaffin containing c5～c7, isoparaffin content ＞ 70%, using conventional reforming catalyst
Carry out aromatisation, aromatics yield is low.
Chemical Engineer (2013) 3:62-64 is reported and is mixed, using reforming raffinate oil, the feelings reformed with catalytic reforming raw material
Condition.But raffinate oil and be added to the aromatisation depth leading to Reformed Gasoline in reformer feed and octane number decline.
Catalytic reforming communicates the catalytic aromatization that (1991) 4:41-43 reports reforming raffinate oil, and reforming raffinate oil is directly made
For raw material, reformed with platinum stannum reforming catalyst, but result is shown, the reforming raffinate oil containing c5～c7 hydrocarbon is urged in traditional platinum stannum
Aromatisation effect in agent is extremely difficult and selectivity is low.
Content of the invention
It is an object of the invention to provide a kind of method preparing light aromatics using reforming raffinate oil, this Guttae Phacosylini reforming raffinate oil
Prepare light aromatics, and by-product research octane number (RON) (ron) 87～90 high-knock rating gasoline blend component.
For reaching above-mentioned purpose, the present invention adopts the following technical scheme that
A kind of method preparing light aromatics using reforming raffinate oil, comprises the following steps:
After reforming raffinate oil drying tower 1 dehydration is mixed with hydrogen, through heat exchanger 4, with aromatization reactor 3 out anti-
Answer product heat exchange, enter heating furnace 2, be heated to reaction temperature, from top enter aromatization reactor 3 contact with catalyst into
Row aromatization, product through supercooling, enters knockout tower 5 after heat exchanger 4 with drying tower 1 raw material heat exchange out
Isolate fuel gas, materials at bottom of tower enters extraction tower 6, the light aromatics isolated from extraction tower 6 is from bottom of towe discharge system, tower
Push up the c obtaining5 +Non-aromatics enters fractionating column 7 fractional distillation, fractionating column 7 tower top obtain evaporating point < 60 DEG C of c5～c6 fraction, bottom of towe
Evaporate a little > 60 DEG C of c6～c7 fraction converge with drying tower 1 raw material out after through heat exchanger 4 heat exchange, enter back into heating furnace 2 plus
Heat, returns aromatization reactor 3 and proceeds aromatization.
In said method, reforming raffinate oil is dehydrated through molecular sieve drying tower, makes the water content in reforming raffinate oil be less than 2 μ g/g.
Hydrogen to oil volume ratio 400～1200:1 in said method, raw material volume air speed is 1.5～3.5h-1.
Aromatisation temperature described in said method is 440～500 DEG C, and pressure is 0.2～1.0mpa.
Catalyst described in said method be metal-modified pt/k l molecular sieve catalyst, modified metal be sn, zn, ba,
One or more of fe, metal total load amount is 2.0～3.0wt%.
Specifically by al (oh)3It is added in koh solution, heating for dissolving obtains Alumina gel, by sncl4·5h2O is dissolved in distilled water
In, then it is mixed to form mixed solution with Alumina gel, under stirring, mixed solution is added in Ludox, stirring forms white gels,
Again white gels are moved into crystallization in crystallizing kettle, then cool down rapidly, product is centrifuged, washs, gained solid is through overdrying
Dry, obtain stanniferous kl molecular screen primary powder；Stanniferous kl molecular sieve is soaked in the saline solution of one or more of zn, ba, fe
Stain, drying, roasting, then in pt (nh3)2cl2Dipping, dry, roasting in solution, or directly in pt (nh3)2cl2Solution
Middle dipping, drying, roasting.
Preferably by 43.5gal (oh)3It is added in the solution that 500ml contains 129gkoh, heating for dissolving obtains Alumina gel, will
15.0gsncl4·5h2O is dissolved in 200ml distilled water, then is mixed to form mixed solution with Alumina gel, by mixed solution under stirring
It is added in the Ludox of 783ml, stirring forms white gels, then white gels are moved into 150 DEG C of crystallization in the crystallizing kettle of 3l
2 days, then it is rapidly cooled to 40 DEG C, product is centrifuged, washs to liquid phase ph value is 10～11, gained solid is in 120
DEG C drying 10 hours, obtains stanniferous kl molecular screen primary powder；
pt(nh3)2cl2During solution impregnation, concentration is 16mg/ml, and during dipping, liquid/solid volume ratio is 4: 1,30 DEG C of dipping temperature, leaching
6 hours stain time；After impregnating, solid is in 120 DEG C of dryings 10 hours, 350 DEG C of roastings 4 hours；
When the saline solution of one or more of zn, ba, fe impregnates, impregnate 24 hours at 30 DEG C, solid after impregnating
In 120 DEG C of dryings 10 hours, 350 DEG C of roastings 4 hours.
In said method, fuel gas includes hydrogen, dry gas and liquefied gas.
In said method, fractionating column 7 tower top obtains evaporating point that < 60 DEG C of c5～c6 fraction is including isopentane, pentane, 2,2- bis-
Methybutane and the mixture of 2,3- dimethylbutane, research octane number (RON) 90～92, evaporate < 60 DEG C of point.
In said method, reforming raffinate oil contains c5<9.0wt%, c8<1.0wt, c6～c7>90%, boiling range≤90 DEG C.
The present invention devises rational technological process first, with the use of metal-modified pt/k l molecular sieve catalyst, makes reformation
Raffinate oil and carry out aromatization under certain condition, effectively reforming raffinate oil is converted into light aromatics, light aromatics yield can
Reach 55～70%, simultaneously by-product research octane number (RON) (ron) 87～90 high-knock rating gasoline blend component, be catalyzed for being in harmonious proportion
Cracking gasoline can be greatly lowered its olefin(e) centent, expanded the processing and utilization channel of reforming raffinate oil, improve reforming raffinate oil
Value.
Brief description
Fig. 1 is the process flow diagram of the present invention；
In figure: 1- drying tower；2- heating furnace；3- aromatization reactor；4- heat exchanger；5- separator；6- extraction tower；7- fractional distillation
Tower.
Specific embodiment
The invention will be further described with specific embodiment below in conjunction with the accompanying drawings, but the present invention is not limited to this.
In Fig. 1, reforming raffinate oil is dehydrated through molecular sieve drying tower 1, makes the water content in reforming raffinate oil be less than 2 μ g/g, warp
Cross heat exchanger 4, with aromatization reactor 3 product heat exchange out, enter heating furnace 2, be heated to reaction temperature, from top
End is entered aromatization reactor 3 and is contacted with catalyst and carries out aromatization, product warp after heat exchanger 4 with raw material heat exchange
Supercooling, enters knockout tower 5 and separates, isolate hydrogen, dry gas, liquefied gas, materials at bottom of tower enters extraction tower 6 and separates, gently
Matter aromatic hydrocarbons from bottom of towe discharge system, the c that tower top obtains5 +Non-aromatics enters fractionating column 7 fractional distillation, tower top obtain evaporating point < 60 DEG C of c5～
C6 fraction, mainly isopentane, the mixture of pentane, 2,2- dimethylbutane and 2,3- dimethylbutane, organon octane
Value (ron) 90～92, as high octane gasoline component discharge system, the evaporating a little of bottom of towe > 60 DEG C of c6～c7 fraction is through heat exchange
Device 4, heating furnace 2 return aromatization reactor 3 and proceed aromatization.
Embodiment 1
By 43.5gal (oh)3It is added in the solution that 500ml contains 129gkoh, heating for dissolving obtains Alumina gel, will
15.0gsncl4·5h2O is dissolved in 200ml distilled water, then is mixed to form mixed solution with Alumina gel, by mixed solution under stirring
It is added in the Ludox of 783ml, stirring forms white gels.Again white gels are moved into 150 DEG C of crystallization in the crystallizing kettle of 3l
2 days, then it is rapidly cooled to 40 DEG C, product is centrifuged, washs to liquid phase ph value is 10～11, gained solid is in 120
DEG C drying 10 hours, obtains stanniferous kl molecular screen primary powder.
Embodiment 2
The stanniferous kl molecular sieve of Example 1 preparation is as carrier, the pt (nh with concentration as 16mg/ml3)2cl2Solution is satiated
And dipping, during dipping, liquid/solid volume ratio is 4: 1,30 DEG C of temperature, dip time 6 hours, and after impregnating, solid is dry in 120 DEG C
Dry 10 hours, 350 DEG C of roastings 4 hours, make the catalyst sl-1 of 1.0wt% containing pt, sn1.0wt%.
Embodiment 3
The stanniferous kl molecular sieve of Example 1 preparation is as carrier, the fecl with concentration as 5wt%3Solution impregnates 24 at 30 DEG C
Hour, after impregnating solid in 120 DEG C of dryings 10 hours, 350 DEG C of roastings 4 hours, then solid concentration is 16mg/ml
Pt (nh3)2cl2Solution supersaturation impregnates, and during dipping, liquid/solid volume ratio is 4: 1,30 DEG C of temperature, dip time 6 hours, will
After dipping, solid is in 120 DEG C of dryings 10 hours, 350 DEG C of roastings 4 hours, makes 1.0wt% containing pt, sn1.0wt%, fe0.5wt%
Catalyst sl-2.
Embodiment 4
The stanniferous kl molecular sieve of Example 1 preparation is as carrier, the bacl with concentration as 5wt%2Solution impregnates 24 at 30 DEG C
Hour, after impregnating solid in 120 DEG C of dryings 10 hours, 350 DEG C of roastings 4 hours, then solid concentration is 16mg/ml
Pt (nh3)2cl2Solution supersaturation impregnates, and during dipping, liquid/solid volume ratio is 4: 1,30 DEG C of temperature, dip time 6 hours, will
After dipping, solid is in 120 DEG C of dryings 10 hours, 350 DEG C of roastings 4 hours, makes 1.0wt% containing pt, sn1.0wt%, ba0.5wt%
Catalyst sl-3.
Embodiment 5
Example 1 preparation stanniferous kl molecular sieve as carrier, with the bacl containing 5wt%2, the fecl of 5wt%3Solution is 30
DEG C dipping 24 hours, after impregnating solid in 120 DEG C of dryings 10 hours, 350 DEG C of roastings 4 hours, then solid concentration is
Pt (the nh of 16mg/ml3)2cl2Solution supersaturation impregnates, and during dipping, liquid/solid volume ratio is 4: 1,30 DEG C of temperature, dip time 6
Hour, after impregnating solid in 120 DEG C of dryings 10 hours, 350 DEG C of roastings 4 hours, make 1.0wt% containing pt, sn1.0wt%,
The catalyst sl-4 of ba0.5wt%, fe0.5wt%.
Embodiment 6
Example 1 preparation stanniferous kl molecular sieve as carrier, with the bacl containing 5wt%2, the zncl of 5wt%2Solution is 30
DEG C dipping 24 hours, after impregnating solid in 120 DEG C of dryings 10 hours, 350 DEG C of roastings 4 hours, then solid concentration is
Pt (the nh of 16mg/ml3)2cl2Solution supersaturation impregnates, and during dipping, liquid/solid volume ratio is 4: 1,30 DEG C of temperature, dip time 6
Hour, after impregnating solid in 120 DEG C of dryings 10 hours, 350 DEG C of roastings 4 hours, make 1.0wt% containing pt, sn1.0wt%,
The catalyst sl-5 of zn0.5wt%, fe0.5wt%.
Embodiment 7
Reforming raffinate oil (its pona composition analysis is shown in Table 1) molecular sieve drying tower is dehydrated, and makes the water content in reforming raffinate oil low
In 2 μ g/g, the preheated rear aromatization reactor that enters is reacted, and reaction condition is: 480 DEG C of reaction temperature, pressure 1.0mpa,
Hydrogen to oil volume ratio 600:1, raw material volume air speed is 2.5h-1.Used catalyst is the catalyst sl-1 of embodiment 2 preparation.Virtue
Hydrogen isolated by the separated tower of structure product, dry gas, liquefied gas enter back into extraction tower and extract light aromatics, c5 +Non-aromatics
Enter fractionating column and fractionate out and evaporate c6～c7 fraction of 60 DEG C of point<60 DEG C of c5～c6 fraction, bottom of towe evaporate a little>to return aromatisation anti-
Device is answered to proceed aromatization.With it, total reaction result such as table 2.
Embodiment 8
Reforming raffinate oil (its pona composition analysis is shown in Table 1) molecular sieve drying tower is dehydrated, and makes the water content in reforming raffinate oil low
In 2 μ g/g, the preheated rear aromatization reactor that enters is reacted, and reaction condition is: 460 DEG C of reaction temperature, pressure 0.35mpa,
Hydrogen to oil volume ratio 800:1, raw material volume air speed is 2.0h-1.Used catalyst is the catalyst sl-2 of embodiment 3 preparation.Virtue
Hydrogen isolated by the separated tower of structure product, dry gas, liquefied gas enter back into extraction tower and extract light aromatics, c5 +Non-aromatics
Enter fractionating column and fractionate out and evaporate c6～c7 fraction of 60 DEG C of point<60 DEG C of c5～c6 fraction, bottom of towe evaporate a little>to return aromatisation anti-
Device is answered to proceed aromatization.With it, total reaction result such as table 2.
Embodiment 9
Reforming raffinate oil (its pona composition analysis is shown in Table 1) molecular sieve drying tower is dehydrated, and makes the water content in reforming raffinate oil low
In 2 μ g/g, the preheated rear aromatization reactor that enters is reacted, and reaction condition is: 440 DEG C of reaction temperature, pressure 0.5mpa,
Hydrogen to oil volume ratio 400:1, raw material volume air speed is 1.5h-1.Used catalyst is the catalyst sl-3 of embodiment 4 preparation.Virtue
Hydrogen isolated by the separated tower of structure product, dry gas, liquefied gas enter back into extraction tower and extract light aromatics, c5 +Non-aromatics
Enter fractionating column and fractionate out and evaporate c6～c7 fraction of 60 DEG C of point<60 DEG C of c5～c6 fraction, bottom of towe evaporate a little>to return aromatisation anti-
Device is answered to proceed aromatization.With it, total reaction result such as table 2.
Embodiment 10
Reforming raffinate oil (its pona composition analysis is shown in Table 1) molecular sieve drying tower is dehydrated, and makes the water content in reforming raffinate oil low
In 2 μ g/g, the preheated rear aromatization reactor that enters is reacted, and reaction condition is: 500 DEG C of reaction temperature, pressure 0.2mpa,
Hydrogen to oil volume ratio 800:1, raw material volume air speed is 3.5h-1.Used catalyst is the catalyst sl-4 of embodiment 5 preparation.Virtue
Hydrogen isolated by the separated tower of structure product, dry gas, liquefied gas enter back into extraction tower and extract light aromatics, c5 +Non-aromatics
Enter fractionating column and fractionate out and evaporate c6～c7 fraction of 60 DEG C of point<60 DEG C of c5～c6 fraction, bottom of towe evaporate a little>to return aromatisation anti-
Device is answered to proceed aromatization.With it, total reaction result such as table 2.
Embodiment 11
Reforming raffinate oil (its pona composition analysis is shown in Table 1) molecular sieve drying tower is dehydrated, and makes the water content in reforming raffinate oil low
In 2 μ g/g, the preheated rear aromatization reactor that enters is reacted, and reaction condition is: 460 DEG C of reaction temperature, pressure 0.4mpa,
Hydrogen to oil volume ratio 1200:1, raw material volume air speed is 2.5h-1.Used catalyst is the catalyst sl-5 of embodiment 6 preparation.Virtue
Hydrogen isolated by the separated tower of structure product, dry gas, liquefied gas enter back into extraction tower and extract light aromatics, c5 +Non-aromatics
Enter fractionating column and fractionate out and evaporate c6～c7 fraction of 60 DEG C of point<60 DEG C of c5～c6 fraction, bottom of towe evaporate a little>to return aromatisation anti-
Device is answered to proceed aromatization.With it, total reaction result such as table 2.
Comparative example 1
Reforming raffinate oil (its pona composition analysis is shown in Table 1) is preprocessed to enter aromatization reactor and platinum stannum reforming catalyst
Ps-6 (sinopec Chang Ling catalyst branch company) contact carries out aromatization, and reaction condition is: 470 DEG C of reaction temperature, pressure
Power 1.8mpa, hydrogen to oil volume ratio 1000:1, raw material volume air speed is 3h-1.With it, total reaction result such as table 2.
Comparative example 1
Reforming raffinate oil (its pona composition analysis is shown in Table 1) is preprocessed to enter aromatization reactor and platinum stannum reforming catalyst
Ps-6 (sinopec Chang Ling catalyst branch company) contact carries out aromatization, and reaction condition is: 500 DEG C of reaction temperature, pressure
Power 1.0mpa, hydrogen to oil volume ratio 800:1, raw material volume air speed is 2h-1.With it, total reaction result such as table 2.
Table 1 reforming raffinate oil pona forms
| Carbon number | N-alkane | Isoparaffin | Alkene | Cycloalkane | Aromatic hydrocarbons | Amount to |
| 3 | 0.35 | 0.00 | 0.00 | 0.00 | 0.00 | 0.35 |
| 4 | 0.19 | 0.24 | 0.00 | 0.00 | 0.00 | 0.43 |
| 5 | 5.25 | 3.45 | 0.00 | 0.00 | 0.00 | 8.70 |
| 6 | 16.13 | 69.46 | 0.00 | 1.77 | 0.02 | 87.38 |
| 7 | 1.08 | 1.96 | 0.00 | 0.00 | 0.00 | 3.04 |
| 8 | 0.00 | 0.00 | 0.00 | 0.01 | 0.00 | 0.01 |
| Total | 23.00 | 75.11 | 0.00 | 1.78 | 0.02 | 99.91 |
Table 2 embodiment reaction result
Claims (10)
1. a kind of prepare the method for light aromatics it is characterised in that comprising the following steps using reforming raffinate oil:
After reforming raffinate oil drying tower 1 dehydration is mixed with hydrogen, through heat exchanger 4, produce with aromatization reactor 3 reaction out
Thing heat exchange, enters heating furnace 2, is heated to reaction temperature, contacts with catalyst from top entrance aromatization reactor 3 and carries out virtue
Structureization is reacted, and product through supercooling, enters knockout tower 5 and separates after heat exchanger 4 with drying tower 1 raw material heat exchange out
Go out fuel gas, materials at bottom of tower enters extraction tower 6, from bottom of towe discharge system, tower top obtains the light aromatics isolated from extraction tower 6
The c arriving5 +Non-aromatics enters fractionating column 7 fractional distillation, and fractionating column 7 tower top obtains evaporating point < 60 DEG C of c5～c6 fraction, the evaporating a little of bottom of towe
> 60 DEG C of c6～c7 fraction after raw material out converges with drying tower 1 through heat exchanger 4 heat exchange, enter back into heating furnace 2 and heat,
Return aromatization reactor 3 and proceed aromatization.
2. according to claim 1 prepare the method for light aromatics it is characterised in that reformation raffinate using reforming raffinate oil
Oil, through the dehydration of molecular sieve drying tower, makes the water content in reforming raffinate oil be less than 2 μ g/g.
3. according to claim 1 prepare the method for light aromatics it is characterised in that hydrogen oil volume using reforming raffinate oil
Ratio 400～1200:1, raw material volume air speed is 1.5～3.5h-1.
4. according to claim 3 prepare the method for light aromatics it is characterised in that described virtue using reforming raffinate oil
Structure temperature is 440～500 DEG C, and pressure is 0.2～1.0mpa.
5. the method that the utilization reforming raffinate oil according to claim 1 or 2 or 3 or 4 prepares light aromatics, its feature exists
In described catalyst is metal-modified pt/k l molecular sieve catalyst, and modified metal is in sn, zn, ba, fe
Plant or several, metal total load amount is 2.0～3.0wt%.
6. according to claim 5 prepare the method for light aromatics using reforming raffinate oil it is characterised in that by al (oh)3
It is added in koh solution, heating for dissolving obtains Alumina gel, by sncl4·5h2O is dissolved in distilled water, then mixes shape with Alumina gel
Become mixed solution, under stirring, mixed solution is added in Ludox, stirring forms white gels, then white gels are moved into brilliant
Change crystallization in kettle, then cool down rapidly, product is centrifuged, washs, gained solid, through drying, obtains stanniferous kl molecule
Sieve former powder；Stanniferous kl molecular sieve is impregnated in the saline solution of one or more of zn, ba, fe, is dried, roasting, so
Afterwards in pt (nh3)2cl2Dipping, dry, roasting in solution, or directly in pt (nh3)2cl2Dipping, dry, roasting in solution.
7. according to claim 6 using reforming raffinate oil prepare light aromatics method it is characterised in that will
43.5gal(oh)3It is added in the solution that 500ml contains 129gkoh, heating for dissolving obtains Alumina gel, by 15.0gsncl4·5h2o
It is dissolved in 200ml distilled water, then is mixed to form mixed solution with Alumina gel, under stirring, mixed solution is added to the silicon of 783ml
In colloidal sol, stirring forms white gels, then white gels are moved into 150 DEG C of crystallization 2 days in the crystallizing kettle of 3l, then cold rapidly
But to 40 DEG C, product is centrifuged, washs to liquid phase ph value is 10～11, gained solid in 120 DEG C of dryings 10 hours,
Obtain stanniferous kl molecular screen primary powder；
pt(nh3)2cl2During solution impregnation, concentration is 16mg/ml, and during dipping, liquid/solid volume ratio is 4: 1,30 DEG C of dipping temperature, leaching
6 hours stain time；After impregnating, solid is in 120 DEG C of dryings 10 hours, 350 DEG C of roastings 4 hours；
When the saline solution of one or more of zn, ba, fe impregnates, impregnate 24 hours at 30 DEG C, solid after impregnating
In 120 DEG C of dryings 10 hours, 350 DEG C of roastings 4 hours.
8. according to claim 1 prepare the method for light aromatics it is characterised in that fuel gas bag using reforming raffinate oil
Include hydrogen, dry gas and liquefied gas.
9. according to claim 1 prepare the method for light aromatics it is characterised in that fractionating column 7 using reforming raffinate oil
Tower top obtains evaporating point that < 60 DEG C of c5～c6 fraction is including isopentane, pentane, 2,2- dimethylbutane and 2,3- dimethyl butyrate
The mixture of alkane, research octane number (RON) 90～92, evaporate < 60 DEG C of point.
10. according to claim 1 prepare the method for light aromatics using reforming raffinate oil it is characterised in that described
Reforming raffinate oil contains c5<9.0wt%, c8<1.0wt, c6～c7>90%, boiling range≤90 DEG C.
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| CN112080320A (en) * | 2019-06-12 | 2020-12-15 | 中国石油化工股份有限公司 | Method for producing aromatic hydrocarbon and hydrogen with high yield from C6-C7 alkane |
| CN114426871A (en) * | 2020-09-18 | 2022-05-03 | 中国石油化工股份有限公司 | Catalytic reforming method for naphtha |
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| US5609751A (en) * | 1994-07-26 | 1997-03-11 | Chevron Chemical Company | Para-xylene selective reforming/aromatization |
| CN101746774B (en) * | 2008-11-28 | 2012-05-23 | 中国石油化工股份有限公司 | Tin-containing L zeolite and preparation method thereof |
| CN102382678B (en) * | 2010-08-25 | 2014-02-26 | 中国石油化工股份有限公司 | Method for producing aromatic hydrocarbon from coked gasoline |
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| CN112080320B (en) * | 2019-06-12 | 2023-07-18 | 中国石油化工股份有限公司 | Method for high-yield aromatic hydrocarbon and hydrogen from C6-C7 alkane |
| CN114426871A (en) * | 2020-09-18 | 2022-05-03 | 中国石油化工股份有限公司 | Catalytic reforming method for naphtha |
| CN114763493A (en) * | 2021-01-13 | 2022-07-19 | 中国石油化工股份有限公司 | Method and system for producing gasoline blend oil by using carbon five raffinate oil |
| CN114763493B (en) * | 2021-01-13 | 2024-01-12 | 中国石油化工股份有限公司 | Method and system for producing gasoline blend oil by using carbon five raffinate oil |
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