CN104557431B - The paraxylene production method of diversification of feedstock - Google Patents
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Abstract
The present invention relates to the paraxylene production method of a kind of diversification of feedstock, mainly solve conventional art exists the problem that raw material sources are single, raw material adjusts very flexible.The light cycle oil that the present invention carrys out catalytic cracking by employing enters selective hydrogenation open loop unit generation mixture I；C3 C6 lighter hydrocarbons in described mixture I are concomitantly introduced into light-hydrocarbon aromatized unit as reaction raw materials and fresh light hydrocarbon feedstocks, and reaction generates mixture II；In described mixture I, C7 C10 introduces transalkylation reaction and generates mixture III；Mixture II enters product separative element together with III, isolates C3 C6 component and returns light-hydrocarbon aromatized unit, and C7 component returns transalkylation, C8 and above component and enters benzenol hydrorefining；Dimethylbenzene tower top C8 aronmatic enters p-xylene separation unit and obtains para-xylene product, component at the bottom of tower enters heavy aromatics tower, heavy aromatics tower is isolated C9 C10 component and is returned the technical scheme of transalkylation, preferably solves this problem, can be used for paraxylene industrial production.
Description
Technical field
The present invention relates to a kind of method that diversification of feedstock produces paraxylene, be by by light cycle oil in particular
Selective hydrogenation open loop unit, light-hydrocarbon aromatized unit, transalkylation, paraxylene adsorption separation unit and C8 aronmatic
The associating of isomerization unit, produces the method obtaining high-purity para-xylene product.
Background technology
Utilize toluene and carbon nine and above heavy aromatics (C thereof9 +A) transalkylation reaction increasing production of xylol is effectively to utilize weight virtue
Hydrocarbon carrys out the method for increasing production of xylol, is widely used.Industrial paraxylene (PX) product is mainly entered by Aromatic Hydrocarbon United Plant
Row produces.Tradition Aromatic Hydrocarbon United Plant relates to the unit such as reformation, transalkylation, isomerization, PX separation, and PX is as product extraction.
Wherein reforming process is aromatic hydrocarbons reaction of formation, and its primary raw material is naphtha, is reacted by many and completes, specifically includes that ring
Dehydrating alkanes becomes aromatic hydrocarbons, and paraffin dehydrogenation is cyclized, alkane and the isomerization of cycloalkane, the dealkylation of alkylaromatic hydrocarbon, alkane
Hydrocarbon is hydrocracking into light hydrocarbon.Generate in product rich in benzene,toluene,xylene and the product of heavy aromatics, produce associating as PX
The reaction raw materials of other unit in device.In recent years, along with the fast development of alkene industry, splitting with naphtha as raw material equally
Solve olefin production quickly to increase.Alkene produces and the competition to the demand composition of feed naphtha of aromatics production process, causes
Feed naphtha shortage becomes increasingly conspicuous.
On the other hand, China's catalytic cracking unit by-product gently to circulate cracked oil (LCO) output huge, annual output is about
Reach 10,000,000 tons.Its composition mainly contains monocycle, dicyclo and thrcylic aromatic hydrocarbon, and aromatics quality mark is up to 75%-85%, can conduct
Produce aromatization chemical product effectively supplements raw material.LCO selective hydrogenation ring opening process mainly generates C3-C10 non-aromatics, BTX
And heavy arene.Uop Inc., Kawasaki, Japan catalyst chemical conversion industrial group and Canada's Nova companies develop and with LCO are
Raw material produces the Aromatics Production Technology of BTX.Sinopec Shanghai Petroleum Chemical Engineering Institute (SRIPT) also gently follows in catalytic cracking
Ring oil produces aromatic hydrocarbons technical field and is studied, and bears first fruit.It is former with LCO that CN102365349A discloses a kind of
Material produces the method for aromatic hydrocarbons, patent with the product after LCO hydrotreating and naphtha or straight run light oil together as reformer unit
Reaction raw materials produces aromatic compound.
Additionally, the lighter hydrocarbons utilization rate of China's refinery gas weight is the lowest, being mainly used for producing alkylate oil, overall utilization is not
Foot 20%.Along with the raising of China's oil refining working ability, in particular with the application of heavy-oil catalytic agent process technology so that
Lighter hydrocarbons productivity increases year by year, and its olefin(e) centent is higher, causes combustion quality poor, and also results in the wasting of resources.Therefore, utilize now
The aromatization technology having lighter hydrocarbons resource to produce aromatic hydrocarbons opens new aromatics production approach, has good application prospect.
CN101596461 discloses a kind of aromatizing catalyst for light hydrocarbon and preparation method, and catalyst contains MFI structure acidic molecular
Sieve and aluminum phosphate and zinc oxide component, it is possible to decrease catalyst carbon deposit speed.CN101759511A discloses a kind of light-hydrocarbon aromatized
Fixed bed double-reactor method, catalyst life can be extended, CN101538184A discloses a kind of moving bed reaction-regeneration work
Skill is used and light dydrocarbon aromatization reaction, has high liquid yield and stability.
LCO selective hydrogenation open loop and light-hydrocarbon aromatized technology is used to substitute traditional reformation with naphtha as raw material
Technology, had both opened up aromatic hydrocarbons and had generated raw material, it is possible to made two kinds of technology realize resource complementation, add the flexibility of raw material.
Summary of the invention
The technical problem to be solved is that the Aromatic Hydrocarbon United Plant of existing production paraxylene exists raw material sources
The problem that single, raw material adjusts very flexible, it is provided that a kind of diversification of feedstock produces the method for paraxylene, the method is passed through will
Light cycle oil selective hydrogenation open loop unit, light-hydrocarbon aromatized unit, transalkylation, paraxylene adsorption separation unit and
The associating of isomerization of C-8 aromatics unit, produces and obtains high-purity para-xylene product, has raw material sources variation, raw material group
Become to adjust advantage flexibly.
For solving above-mentioned technical problem, the present invention uses technical scheme as follows, and a kind of diversification of feedstock produces paraxylene
Method, comprise the following steps successively:
A) light cycle oil carrying out catalytic cracking enters selective hydrogenation open loop unit, generates with catalyst haptoreaction and contains
The mixture I of lighter hydrocarbons, benzene,toluene,xylene, carbon nine and above aromatic hydrocarbons；
B) described mixture I isolates C2 and following components, C3-C6 component, C7-C10 component and C11+ component successively, its
Middle C3-C6 component enters light-hydrocarbon aromatized unit as reaction raw materials together with fresh light hydrocarbon feedstocks, and reaction generates mixture II,
C7-C10 component enters transalkylation reaction and generates mixture III；
C) described mixture II enters product separative element together with mixture III, isolates C2 and following components, C3-C6
Component, C7 and above component.Wherein C3-C6 component returns the light-hydrocarbon aromatized unit of b) step, C7 and above component and enters first
Benzene column, tower top obtains C7 component and returns the transalkylation of b) step, obtains C8 and above component enters benzenol hydrorefining at the bottom of tower；
D) benzenol hydrorefining isolates C8 aronmatic, C9-C10 component, C11 and above component, and wherein C9-C10 component returns
B) transalkylation of step；
E) C8 aronmatic from d) step enters p-xylene separation unit, obtains para-xylene product and containing to diformazan
The C8 aronmatic of benzene；
F) C8 aronmatic containing paraxylene from e) step enters isomerization of C-8 aromatics unit, and the product obtained returns
Return the product separative element of c) step.
In technique scheme, preferred technical scheme is, from selective hydrogenation open loop unit, transalkylation and
The C3-C6 lighter hydrocarbons product of isomerization unit enters light-hydrocarbon aromatized unit as reaction raw materials, from selective hydrogenation open loop list
The C7-C10 component of unit enters transalkylation as reaction raw materials；In step a), light circulation cracked oil chosen property hydrogenation is opened
Ring generates containing aromatic hydrocarbons and non-aromatic component；In step a), in light circulation cracked oil, nitrogen content is not more than 1000ppm, sulfur content
It is not more than 1000ppm；Fresh light hydrocarbon feedstocks is alkane or the alkene of C1-C8, and prioritization scheme is alkane or the alkene of C3-C6；Step
Rapid b) in mixture III C8 aronmatic content than C8 aronmatic content high at least 30% in transalkylation reactant.
In technique scheme, preferred technical scheme is, selective hydrogenation open loop unit uses molecular sieve catalyst, urges
Agent contains at least one molecular sieve in beta-zeolite, modenite, ZSM-5, NU-87, ZSM-12 or MCM-22, catalysis
Agent possibly together with II A in the periodic table of elements, III A, IV A, V A, VI A, VII A, I B, II B, III B, IV B, V B, VI B, VII B, VIII
At least one element in B race or its compound, its consumption is calculated as 0.001 ~ 5% with catalyst weight percent；Light-hydrocarbon aromatized
The catalyst that unit uses contains at least one Si-Al molecular sieve with MFI, MOR, BETA structure, and catalyst is possibly together with being selected from
At least one element in I B, II B, III B, IV B, V B, VI B, VII B, VIII B race or its compound, its consumption is with catalyst weight
Percentages is 0.01 ~ 10%；Transalkylation uses molecular sieve catalyst, and catalyst contains selected from beta-zeolite, mercerising boiling
At least one molecular sieve in stone, ZSM-5, NU-87, ZSM-12 or MCM-22, catalyst is possibly together with in platinum, molybdenum, rhenium, nickel
At least one metal or its oxide；
In technique scheme, preferred technical scheme is, the operating condition of selective hydrogenation open loop unit is as follows: reaction
Pressure is 0.5 ~ 6MPa, and reaction temperature is 100 ~ 600 DEG C, hydrogen hydrocarbon mol ratio 0.1 ~ 10, and liquid weight air speed is 0.5 ~ 10h-1；Alkane
The operating condition of group-transfer unit is as follows: reaction pressure is 0.5 ~ 5MPa, and reaction temperature is 200 ~ 600 DEG C, hydrogen hydrocarbon mol ratio 0.5
~ 10, liquid weight air speed is 0.8 ~ 10h-1；Light-hydrocarbon aromatized unit operating condition is as follows: reaction pressure is 0.1 ~ 5MPa, reaction
Temperature is 200 ~ 700 DEG C, hydrogen hydrocarbon mol ratio 0.1 ~ 10, and liquid weight air speed is 0.5 ~ 8h-1；The behaviour of isomerization of C-8 aromatics unit
Making condition as follows: reaction pressure is 0.5 ~ 6MPa, reaction temperature is 300 ~ 500 DEG C, hydrogen hydrocarbon mol ratio 0.5 ~ 25, and liquid weight is empty
Speed is 0.5 ~ 10h-1；P-xylene separation unit uses paraxylene adsorbing separation；P-xylene separation unit obtain to two
Toluene product design is more than 99.8 %(weight).
The aromatics production process of Aromatic Hydrocarbon United Plant is widened by the present invention and selects into light-hydrocarbon aromatized unit and light cycle oil
Selecting property hydrogenation unit, the unit of light cycle oil selective hydrogenation simultaneously provides reaction raw materials for light-hydrocarbon aromatized unit.The virtue produced
Hydrocarbon products is through transalkylation increasing production of xylol, and obtains high-purity to two through p-xylene separation and isomerization unit
Toluene product.Present invention process is simple, can originate and ratio by modulation aroamtic hydrocarbon raw material flexibly, can be used for paraxylene industrial production mistake
Journey.
Accompanying drawing explanation
Fig. 1 is the method process flow diagram of the diversification of feedstock production paraxylene of the present invention.
In Fig. 1, I is selective hydrogenation open loop unit, and II is dethanizer, and III is raw material pre-separation unit, and IV is lighter hydrocarbons virtues
Structure unit, V is disproportionation and transalkylation, and VI is product separative element, and VII is toluene tower, and VIII is benzenol hydrorefining, and Ⅸ is
Paraxylene adsorption separation unit, Ⅺ is isomerization of C-8 aromatics unit.1 for gently circulating cracked oil, and 2 for selecting hydrogenation open loop product
Thing, 3 is C1-C2 hydrocarbon component, and 4 is dethanizer substrate, and 5 is C3-C6 hydrocarbon component, and 6 is light hydrocarbon feedstocks, and 7 is C7-C10 hydrocarbon component,
8 is C11+ component, and 9 is light dydrocarbon aromatization reaction product, and 10 is disproportionation and transalkylation product, and 11 is C1-C2 hydrocarbon component,
12 is C3-C6 hydrocarbon component, and 13 is C7 and above hydrocarbon component, and 14 is C7 hydrocarbon component, and 15 is C8 and above component, and 16 is C8 component,
17 is C9-C10 component, and 18 is C11 and above component, and 19 is paraxylene, and 20 feed for isomerization unit, and 21 is isomerization list
Unit's product.
In the technological process producing paraxylene shown in Fig. 1, fresh material 1 enters selective hydrogenation open loop unit I, reaction
Product 2 enters dethanizer II, and tower top obtains C1-C2 component 3, and tower bottom product 4 enters raw material pre-separation unit III, isolated
C3-C6 component 5 enters light-hydrocarbon aromatized unit IV together with light hydrocarbon feedstocks 6.Isolated C7-C10 component with from toluene tower
The C7 component 14 of VII and the C9-C10 component 17 from benzenol hydrorefining VIII enter disproportionation and transalkylation V together.Unit IV
Enter product separative element VI together with 10 with unit V product 9, isolate light component 11, C3-C6 component 12, C7 and above group
Divide 13；Component 12 returns unit III, and component 13 enters toluene tower VII, and tower top obtains C7 component 14 and returns unit V, component at the bottom of tower
15 enter benzenol hydrorefining VIII, isolate C8 component 16, C9-C10 component 17 and C11+ component 18 successively；Component 16 enters diformazan
Benzene adsorption separation unit Ⅸ, component 17 returns disproportionation and transalkylation V.Paraxylene adsorption separation unit Ⅸ obtains height
Pure paraxylene 19, ortho-xylene and meta-xylene 20 send into isomerization of C-8 aromatics unit Ⅺ, and Mixed XYLENE 21 returns product
Separative element VI.
Below by the description to embodiment, further illustrate but be not intended to the present invention.
Detailed description of the invention
[embodiment 1]
With light cycle oil and lighter hydrocarbons as raw material, raw material composition is as shown in table 1.
Technological process selects hydrocracking unit process as it is shown in figure 1, fresh light circulation cracked oil raw material 60t/h enters,
Product enters raw material pre-separation unit after isolating the light component of C1-C2, isolates C3-C6 component, C7-C10 component and C11
+ component.Wherein C3-C6 component enters light-hydrocarbon aromatized unit, C7-as reaction raw materials together with fresh light hydrocarbon feedstocks 40t/h
C10 component enters transalkylation together with toluene tower top circulation C7 component and heavy aromatics tower side take-off C9-C10 component.
Light-hydrocarbon aromatized unit and transalkylation product enter product separative element together, isolate the light component of C1-C2, C3-C6
Component and C7+ component.Wherein C3-C6 component returns lighter hydrocarbons aromatization unit, and C7+ component enters toluene tower, and tower top isolates C7
Component returns transalkylation, and C8+ component at the bottom of tower enters benzenol hydrorefining.Benzenol hydrorefining isolates carbon eight component, C9-C10 group
Point and C11+ component, wherein carbon eight component enter paraxylene adsorption separation unit, it is thus achieved that purity higher than 99.8wt% to diformazan
Benzaldehyde product, C9-C10 component returns disproportionation and transalkylation.
Each unit reaction condition is as shown in table 2, and combined unit product yield is as shown in table 3.
Table 1
| LCO feedstock oil forms | |
| Sulfur content, ppm | 600 |
| Nitrogen content, ppm | 300 |
| Aromatic hydrocarbons, wt% | 64 |
| Lighter hydrocarbons form, wt% | |
| Propane | 1.1 |
| Propylene | 1.6 |
| Butane | 20.2 |
| Butylene | 75.9 |
| C5+ | 1.2 |
| LCO/ lighter hydrocarbons, wt% | 3:2 |
Table 2
| Reaction member | Parameter |
| LCO selective hydrogenation unit | |
| Temperature, DEG C | 450 |
| Pressure, MPa | 4.0 |
| Mass space velocity, h-1 | 2 |
| Hydrogen hydrocarbon mol ratio | 6 |
| Light-hydrocarbon aromatized unit | |
| Temperature, DEG C | 500 |
| Pressure, MPa | 0.4 |
| Mass space velocity, h-1 | 1.2 |
| Transalkylation | |
| Temperature, DEG C | 400 |
| Pressure, MPa | 2.8 |
| Mass space velocity, h-1 | 3.0 |
| Hydrogen hydrocarbon mol ratio | 5 |
| Isomerization of C-8 aromatics unit | |
| Temperature, DEG C | 420 |
| Pressure, MPa | 2.5 |
| Mass space velocity, h-1 | 4.0 |
| Hydrogen hydrocarbon mol ratio | 4 |
Table 3
| Product | Yield, t/h |
| C1-C2 | 19 |
| PX | 67 |
| C11 +A | 14 |
[embodiment 2]
With light cycle oil and lighter hydrocarbons as raw material, raw material composition is as shown in table 1.
Technological process selects hydrocracking unit process as it is shown in figure 1, fresh light circulation cracked oil raw material 70t/h enters,
Product enters raw material pre-separation unit after isolating the light component of C1-C2, isolates C3-C6 component, C7-C10 component and C11
+ component.Wherein C3-C6 component enters light-hydrocarbon aromatized unit, C7-as reaction raw materials together with fresh light hydrocarbon feedstocks 50t/h
C10 component enters transalkylation together with toluene tower top circulation C7 component and heavy aromatics tower side take-off C9-C10 component.
Light-hydrocarbon aromatized unit and transalkylation product enter product separative element together, isolate the light component of C1-C2, C3-C6
Component and C7+ component.Wherein C3-C6 component returns lighter hydrocarbons aromatization unit, and C7+ component enters toluene tower, and tower top isolates C7
Component returns transalkylation, and C8+ component at the bottom of tower enters benzenol hydrorefining.Benzenol hydrorefining isolates carbon eight component, C9-C10 group
Point and C11+ component, wherein carbon eight component enter paraxylene adsorption separation unit, it is thus achieved that purity higher than 99.9wt% to diformazan
Benzaldehyde product, C9-C10 component returns disproportionation and transalkylation.
Each unit reaction condition is as shown in table 4, and combined unit product yield is as shown in table 5.
Table 4
| Reaction member | Parameter |
| LCO selective hydrogenation unit | |
| Temperature, DEG C | 460 |
| Pressure, MPa | 4.5 |
| Mass space velocity, h-1 | 2.5 |
| Hydrogen hydrocarbon mol ratio | 6.5 |
| Light-hydrocarbon aromatized unit | |
| Temperature, DEG C | 510 |
| Pressure, MPa | 0.5 |
| Mass space velocity, h-1 | 1.4 |
| Transalkylation | |
| Temperature, DEG C | 410 |
| Pressure, MPa | 2.9 |
| Mass space velocity, h-1 | 3.2 |
| Hydrogen hydrocarbon mol ratio | 5.1 |
| Isomerization of C-8 aromatics unit | |
| Temperature, DEG C | 430 |
| Pressure, MPa | 2.6 |
| Mass space velocity, h-1 | 4.2 |
| Hydrogen hydrocarbon mol ratio | 4.5 |
Table 5
| Product | Yield, t/h |
| C1-C2 | 18 |
| PX | 69 |
| C11 +A | 13 |
Claims (10)
1. a paraxylene production method for diversification of feedstock, comprises the following steps successively:
A) light cycle oil carrying out catalytic cracking enters selective hydrogenation open loop unit, generates containing light with catalyst haptoreaction
The mixture I of hydrocarbon, benzene,toluene,xylene, carbon nine and above aromatic hydrocarbons；
B) described mixture I isolates C2 and following components, C3～C6 component, C7～C10 component and C11 successively+Component, wherein
C3～C6 component enters light-hydrocarbon aromatized unit as reaction raw materials together with fresh light hydrocarbon feedstocks, and reaction generates mixture II,
C7～C10 component enters transalkylation reaction and generates mixture III；
C) described mixture II enters product separative element together with mixture III, isolates C2 and following components, C3～C6 group
Point, C7 and above component, wherein C3～C6 component returns the light-hydrocarbon aromatized unit of b) step, C7 and above component and enters toluene
Tower, tower top obtains C7 component and returns the transalkylation of b) step, obtains C8 and above component enters benzenol hydrorefining at the bottom of tower；
D) benzenol hydrorefining isolates C8 aronmatic, C9～C10 component, C11 and above component, and wherein C9～C10 component returns b)
The transalkylation of step；
E) C8 aronmatic from d) step enters p-xylene separation unit, obtains para-xylene product and containing paraxylene
C8 aronmatic；
F) C8 aronmatic containing paraxylene from e) step enters isomerization of C-8 aromatics unit, and the product obtained returns c)
The product separative element of step.
Diversification of feedstock the most according to claim 1 produces the method for paraxylene, it is characterised in that carrys out self-selectively and adds
Hydrogen open loop unit, the C3-C6 lighter hydrocarbons product of transalkylation and isomerization unit enters light-hydrocarbon aromatized as reaction raw materials
Unit；C7-C10 component from selective hydrogenation open loop unit enters transalkylation as reaction raw materials；Fresh lighter hydrocarbons
Raw material is alkane or the alkene of C1～C8 of C1～C8.
Diversification of feedstock the most according to claim 2 produces the method for paraxylene, it is characterised in that gently follow in step a)
The chosen property hydrogenation open loop of ring oil generates containing aromatic hydrocarbons and non-aromatic component；In light cycle oil, nitrogen content is not more than 1000ppm, sulphur
Content is not more than 1000ppm；Fresh light hydrocarbon feedstocks is alkane or the alkene of C1～C8 of C3～C6.
Diversification of feedstock the most according to claim 1 produces the method for paraxylene, it is characterised in that mixing in step b)
In thing III, C8 aronmatic content is than C8 aronmatic content high at least 30% in transalkylation reactant.
Diversification of feedstock the most according to claim 1 produces the method for paraxylene, it is characterised in that selective hydrogenation is opened
Ring element use molecular sieve catalyst, catalyst contain selected from beta-zeolite, modenite, ZSM-5, NU-87, ZSM-12 or
At least one molecular sieve in MCM-22, catalyst possibly together with II A in the periodic table of elements, III A, IV A, V A, VI A, VII A,
At least one element in I B, II B, III B, IV B, V B, VI B, VII B, VIII race or its compound, its consumption is with catalyst weight
Percentages is 0.001～5%.
Diversification of feedstock the most according to claim 1 produces the method for paraxylene, it is characterised in that light-hydrocarbon aromatized list
The catalyst that unit uses contains at least one Si-Al molecular sieve with MFI, MOR, BETA structure, and catalyst is possibly together with selected from I
At least one element in B, II B, III B, IV B, V B, VI B, VII B, VIII race or its compound, its consumption is with catalyst weight hundred
Proportion by subtraction is calculated as 0.01～10%.
Diversification of feedstock the most according to claim 1 produces the method for paraxylene, it is characterised in that transalkylation
Using molecular sieve catalyst, catalyst contains in beta-zeolite, modenite, ZSM-5, NU-87, ZSM-12 or MCM-22
At least one molecular sieve, catalyst is possibly together with at least one metal in platinum, molybdenum, rhenium, nickel or its oxide.
Diversification of feedstock the most according to claim 1 produces the method for paraxylene, it is characterised in that selective hydrogenation is opened
The operating condition of ring element is as follows: reaction pressure is 0.5～6MPa, and reaction temperature is 100～600 DEG C, hydrogen hydrocarbon mol ratio 0.1～
10, liquid weight air speed is 0.5～10h-1；The operating condition of transalkylation is as follows: reaction pressure is 0.5～5MPa, instead
Answering temperature is 200～600 DEG C, hydrogen hydrocarbon mol ratio 0.5～10, and liquid weight air speed is 0.8～10h-1；Light-hydrocarbon aromatized unit is grasped
Making condition as follows: reaction pressure is 0.1～5MPa, reaction temperature is 200～700 DEG C, hydrogen hydrocarbon mol ratio 0.1～10, liquid weight
Amount air speed is 0.5～8h-1；The operating condition of isomerization of C-8 aromatics unit is as follows: reaction pressure is 0.5～6MPa, reaction temperature
Degree is 300～500 DEG C, hydrogen hydrocarbon mol ratio 0.5～25, and liquid weight air speed is 0.5～10h-1。
Diversification of feedstock the most according to claim 1 produces the method for paraxylene, it is characterised in that p-xylene separation
Unit uses paraxylene adsorbing separation.
Diversification of feedstock the most according to claim 1 produces the method for paraxylene, it is characterised in that paraxylene divides
The para-xylene product concentration obtained from unit is more than 99.8 weight %.
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| CN114426879B (en) * | 2020-10-15 | 2023-08-08 | 中国石油化工股份有限公司 | System and method for utilizing hydrocarbon-containing mixture |
| CN114426886B (en) * | 2020-10-15 | 2023-04-07 | 中国石油化工股份有限公司 | Integral processing method for hydrocarbon mixture |
| CN114456036B (en) * | 2020-10-22 | 2024-03-26 | 中国石油化工股份有限公司 | Method for producing aromatic hydrocarbon and olefin |
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| CN102190553A (en) * | 2010-03-03 | 2011-09-21 | 中国石油化工股份有限公司 | Aromatic hydrocarbon alkyl transfer method for producing benzene and p-xylene |
| CN102365349A (en) * | 2009-03-27 | 2012-02-29 | 千代田化工建设株式会社 | Method for producing aromatic hydrocarbon |
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| US8524961B2 (en) * | 2011-10-07 | 2013-09-03 | Uop Llc | Integrated catalytic cracking and reforming processes to improve p-xylene production |
| US8617384B2 (en) * | 2011-10-07 | 2013-12-31 | Uop Llc | Integrated catalytic cracking gasoline and light cycle oil hydroprocessing to maximize p-xylene production |
| US8608941B2 (en) * | 2011-10-07 | 2013-12-17 | Uop Llc | Reforming process with integrated fluid catalytic cracker gasoline and hydroprocessed cycle oil |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN102365349A (en) * | 2009-03-27 | 2012-02-29 | 千代田化工建设株式会社 | Method for producing aromatic hydrocarbon |
| CN102190553A (en) * | 2010-03-03 | 2011-09-21 | 中国石油化工股份有限公司 | Aromatic hydrocarbon alkyl transfer method for producing benzene and p-xylene |
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