CN114716292B - Process system and process method for producing paraxylene in high yield - Google Patents
Process system and process method for producing paraxylene in high yield Download PDFInfo
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- CN114716292B CN114716292B CN202011526470.3A CN202011526470A CN114716292B CN 114716292 B CN114716292 B CN 114716292B CN 202011526470 A CN202011526470 A CN 202011526470A CN 114716292 B CN114716292 B CN 114716292B
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- URLKBWYHVLBVBO-UHFFFAOYSA-N Para-Xylene Chemical group CC1=CC=C(C)C=C1 URLKBWYHVLBVBO-UHFFFAOYSA-N 0.000 title claims abstract description 130
- 238000000034 method Methods 0.000 title claims abstract description 47
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 23
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 claims abstract description 182
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 claims abstract description 174
- 238000010555 transalkylation reaction Methods 0.000 claims abstract description 67
- CTQNGGLPUBDAKN-UHFFFAOYSA-N O-Xylene Chemical compound CC1=CC=CC=C1C CTQNGGLPUBDAKN-UHFFFAOYSA-N 0.000 claims abstract description 58
- 239000008096 xylene Substances 0.000 claims abstract description 54
- 238000007323 disproportionation reaction Methods 0.000 claims abstract description 40
- 238000005804 alkylation reaction Methods 0.000 claims abstract description 38
- 238000006317 isomerization reaction Methods 0.000 claims abstract description 37
- 230000029936 alkylation Effects 0.000 claims abstract description 35
- 238000000926 separation method Methods 0.000 claims abstract description 31
- 239000000047 product Substances 0.000 claims abstract description 29
- 238000001179 sorption measurement Methods 0.000 claims abstract description 27
- 238000006243 chemical reaction Methods 0.000 claims abstract description 20
- 238000005194 fractionation Methods 0.000 claims abstract description 18
- 239000000376 reactant Substances 0.000 claims abstract description 12
- 239000007795 chemical reaction product Substances 0.000 claims abstract description 10
- 150000004945 aromatic hydrocarbons Chemical class 0.000 claims description 110
- 239000000463 material Substances 0.000 claims description 79
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims description 63
- 238000000605 extraction Methods 0.000 claims description 28
- 239000002808 molecular sieve Substances 0.000 claims description 23
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims description 23
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 23
- 239000002994 raw material Substances 0.000 claims description 20
- 125000003118 aryl group Chemical group 0.000 claims description 15
- 239000004927 clay Substances 0.000 claims description 15
- 239000007788 liquid Substances 0.000 claims description 13
- 239000012071 phase Substances 0.000 claims description 13
- 239000000203 mixture Substances 0.000 claims description 12
- 238000011084 recovery Methods 0.000 claims description 11
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 claims description 10
- 239000003463 adsorbent Substances 0.000 claims description 9
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 8
- 239000003054 catalyst Substances 0.000 claims description 8
- 238000007599 discharging Methods 0.000 claims description 8
- 229910021536 Zeolite Inorganic materials 0.000 claims description 7
- 239000010457 zeolite Substances 0.000 claims description 7
- 239000004215 Carbon black (E152) Substances 0.000 claims description 6
- 229930195733 hydrocarbon Natural products 0.000 claims description 6
- 150000002430 hydrocarbons Chemical class 0.000 claims description 5
- 239000007791 liquid phase Substances 0.000 claims description 5
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 claims description 4
- ZOKXTWBITQBERF-UHFFFAOYSA-N Molybdenum Chemical compound [Mo] ZOKXTWBITQBERF-UHFFFAOYSA-N 0.000 claims description 4
- BQCADISMDOOEFD-UHFFFAOYSA-N Silver Chemical compound [Ag] BQCADISMDOOEFD-UHFFFAOYSA-N 0.000 claims description 4
- QCWXUUIWCKQGHC-UHFFFAOYSA-N Zirconium Chemical compound [Zr] QCWXUUIWCKQGHC-UHFFFAOYSA-N 0.000 claims description 4
- 150000001336 alkenes Chemical class 0.000 claims description 4
- 229910052797 bismuth Inorganic materials 0.000 claims description 4
- JCXGWMGPZLAOME-UHFFFAOYSA-N bismuth atom Chemical compound [Bi] JCXGWMGPZLAOME-UHFFFAOYSA-N 0.000 claims description 4
- 229910052802 copper Inorganic materials 0.000 claims description 4
- 239000010949 copper Substances 0.000 claims description 4
- 239000007789 gas Substances 0.000 claims description 4
- 239000012535 impurity Substances 0.000 claims description 4
- 229910052809 inorganic oxide Inorganic materials 0.000 claims description 4
- 229910052746 lanthanum Inorganic materials 0.000 claims description 4
- FZLIPJUXYLNCLC-UHFFFAOYSA-N lanthanum atom Chemical compound [La] FZLIPJUXYLNCLC-UHFFFAOYSA-N 0.000 claims description 4
- 229910052751 metal Inorganic materials 0.000 claims description 4
- 239000002184 metal Substances 0.000 claims description 4
- 150000002739 metals Chemical class 0.000 claims description 4
- 229910052750 molybdenum Inorganic materials 0.000 claims description 4
- 239000011733 molybdenum Substances 0.000 claims description 4
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 claims description 4
- 229910052702 rhenium Inorganic materials 0.000 claims description 4
- WUAPFZMCVAUBPE-UHFFFAOYSA-N rhenium atom Chemical compound [Re] WUAPFZMCVAUBPE-UHFFFAOYSA-N 0.000 claims description 4
- 239000000377 silicon dioxide Substances 0.000 claims description 4
- 229910052709 silver Inorganic materials 0.000 claims description 4
- 239000004332 silver Substances 0.000 claims description 4
- 229910052726 zirconium Inorganic materials 0.000 claims description 4
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims description 3
- 229910052680 mordenite Inorganic materials 0.000 claims description 3
- 239000005995 Aluminium silicate Substances 0.000 claims description 2
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 2
- 235000012211 aluminium silicate Nutrition 0.000 claims description 2
- 239000011230 binding agent Substances 0.000 claims description 2
- 229910052739 hydrogen Inorganic materials 0.000 claims description 2
- 239000001257 hydrogen Substances 0.000 claims description 2
- NLYAJNPCOHFWQQ-UHFFFAOYSA-N kaolin Chemical group O.O.O=[Al]O[Si](=O)O[Si](=O)O[Al]=O NLYAJNPCOHFWQQ-UHFFFAOYSA-N 0.000 claims description 2
- 229910052697 platinum Inorganic materials 0.000 claims description 2
- 229910052761 rare earth metal Inorganic materials 0.000 claims description 2
- 150000002910 rare earth metals Chemical class 0.000 claims description 2
- 239000007787 solid Substances 0.000 claims description 2
- 229910052721 tungsten Inorganic materials 0.000 claims description 2
- 229910052720 vanadium Inorganic materials 0.000 claims description 2
- 238000005192 partition Methods 0.000 claims 4
- 238000005265 energy consumption Methods 0.000 abstract description 10
- 230000008901 benefit Effects 0.000 abstract description 4
- 238000005516 engineering process Methods 0.000 abstract description 2
- YNQLUTRBYVCPMQ-UHFFFAOYSA-N Ethylbenzene Chemical compound CCC1=CC=CC=C1 YNQLUTRBYVCPMQ-UHFFFAOYSA-N 0.000 description 4
- 230000000052 comparative effect Effects 0.000 description 4
- WOZVHXUHUFLZGK-UHFFFAOYSA-N dimethyl terephthalate Chemical compound COC(=O)C1=CC=C(C(=O)OC)C=C1 WOZVHXUHUFLZGK-UHFFFAOYSA-N 0.000 description 4
- IVSZLXZYQVIEFR-UHFFFAOYSA-N m-xylene Chemical group CC1=CC=CC(C)=C1 IVSZLXZYQVIEFR-UHFFFAOYSA-N 0.000 description 4
- KKEYFWRCBNTPAC-UHFFFAOYSA-N Terephthalic acid Chemical compound OC(=O)C1=CC=C(C(O)=O)C=C1 KKEYFWRCBNTPAC-UHFFFAOYSA-N 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- DSNHSQKRULAAEI-UHFFFAOYSA-N 1,4-Diethylbenzene Chemical compound CCC1=CC=C(CC)C=C1 DSNHSQKRULAAEI-UHFFFAOYSA-N 0.000 description 2
- 125000000217 alkyl group Chemical group 0.000 description 2
- -1 naphthene hydrocarbon Chemical class 0.000 description 2
- 239000003921 oil Substances 0.000 description 2
- 230000001105 regulatory effect Effects 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 230000000274 adsorptive effect Effects 0.000 description 1
- 150000001335 aliphatic alkanes Chemical class 0.000 description 1
- 230000002152 alkylating effect Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 238000004364 calculation method Methods 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000002425 crystallisation Methods 0.000 description 1
- 230000008025 crystallization Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 229940079593 drug Drugs 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000000835 fiber Substances 0.000 description 1
- 229940078552 o-xylene Drugs 0.000 description 1
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 description 1
- 239000000575 pesticide Substances 0.000 description 1
- 125000001997 phenyl group Chemical group [H]C1=C([H])C([H])=C(*)C([H])=C1[H] 0.000 description 1
- 230000000704 physical effect Effects 0.000 description 1
- 239000004033 plastic Substances 0.000 description 1
- 229920003023 plastic Polymers 0.000 description 1
- 235000012239 silicon dioxide Nutrition 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- 229920003002 synthetic resin Polymers 0.000 description 1
- 239000000057 synthetic resin Substances 0.000 description 1
Classifications
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/04—Purification; Separation; Use of additives by distillation
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2/00—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms
- C07C2/86—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by condensation between a hydrocarbon and a non-hydrocarbon
- C07C2/862—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by condensation between a hydrocarbon and a non-hydrocarbon the non-hydrocarbon contains only oxygen as hetero-atoms
- C07C2/864—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by condensation between a hydrocarbon and a non-hydrocarbon the non-hydrocarbon contains only oxygen as hetero-atoms the non-hydrocarbon is an alcohol
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C5/00—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms
- C07C5/22—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by isomerisation
- C07C5/27—Rearrangement of carbon atoms in the hydrocarbon skeleton
- C07C5/2767—Changing the number of side-chains
- C07C5/277—Catalytic processes
- C07C5/2791—Catalytic processes with metals
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C6/00—Preparation of hydrocarbons from hydrocarbons containing a different number of carbon atoms by redistribution reactions
- C07C6/08—Preparation of hydrocarbons from hydrocarbons containing a different number of carbon atoms by redistribution reactions by conversion at a saturated carbon-to-carbon bond
- C07C6/12—Preparation of hydrocarbons from hydrocarbons containing a different number of carbon atoms by redistribution reactions by conversion at a saturated carbon-to-carbon bond of exclusively hydrocarbons containing a six-membered aromatic ring
- C07C6/126—Preparation of hydrocarbons from hydrocarbons containing a different number of carbon atoms by redistribution reactions by conversion at a saturated carbon-to-carbon bond of exclusively hydrocarbons containing a six-membered aromatic ring of more than one hydrocarbon
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/12—Purification; Separation; Use of additives by adsorption, i.e. purification or separation of hydrocarbons with the aid of solids, e.g. with ion-exchangers
- C07C7/13—Purification; Separation; Use of additives by adsorption, i.e. purification or separation of hydrocarbons with the aid of solids, e.g. with ion-exchangers by molecular-sieve technique
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Water Supply & Treatment (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
A process system and a process method for producing more para-xylene comprise a xylene fractionation unit, an adsorption separation unit, an isomerization reaction unit, a disproportionation and transalkylation unit and an alkylation unit; the process system and the process method of the invention improve the conversion rate of toluene, fully utilize the conversion of benzene to paraxylene, and simultaneously adopt a dividing wall column technology to realize the purpose of separating reactants from reaction products in one column, thereby reducing the energy consumption of the device, improving the paraxylene yield of high added value products and improving the economic and social benefits.
Description
Technical Field
The invention relates to a production method of paraxylene, in particular to a process system and a process method for producing paraxylene in a more yield mode.
Background
Para-xylene is one of the important basic organic raw materials in the petrochemical industry, is mainly used for Preparing Terephthalic Acid (PTA) and dimethyl terephthalate (DMT), and is widely applied to the production fields of chemical fibers, synthetic resins, pesticides, medicines, plastics and the like. According to statistics, in 2019, the capacity of PX in China is greatly increased by 1190 ten thousand tons, the total capacity reaches 2503 ten thousand tons, and the capacity is increased by 70.4%, so that the PX capacity is the highest increased in recent years.
The C 8 aromatics include ortho-xylene, para-xylene, meta-xylene, and ethylbenzene four isomers, with the para-xylene market being greatest, so it is generally more desirable in industry to enhance or even maximize the production of para-xylene from a particular C 8 aromatic feedstock. Because of their similar chemical structures and physical properties and identical molecular weights, para-xylene-poor C 8 aromatics are generally converted into a mixture of C 8 aromatics with equilibrium concentration through isomerization reaction, and meanwhile, the para-xylene products with high purity are obtained through disproportionation and transalkylation reactions of toluene and C 9 aromatics, and then through technical means such as rectification, adsorption separation and the like, the para-xylene-poor C 8 aromatics are subjected to isomerization reaction again in a system cycle, and the toluene and the C 9 aromatics are subjected to disproportionation and transalkylation reactions.
The separation of paraxylene is generally carried out industrially by crystallization and adsorption separation, and the adsorption separation is used more. The raw materials for adsorption separation are mixed C 8 aromatic hydrocarbons, the para-xylene is preferentially adsorbed by utilizing the different selectivities of four isomers of the C 8 aromatic hydrocarbons, and then the para-xylene on the adsorbent is desorbed by using a desorber. The extracted liquid is a paraxylene-rich material, and a high-purity paraxylene product is obtained through rectification; the raffinate is a paraxylene-lean material, the resolving agent is separated from the raffinate tower, and the equilibrium concentration C8 aromatic hydrocarbon mixture is obtained through isomerization reaction, and then the paraxylene is recycled for fractionation.
In the process, the selectivity of para-xylene in the disproportionation and transalkylation reaction of toluene and C 9 aromatic hydrocarbon is less than 30%, so that the circulation amount of a disproportionation and transalkylation unit is large, and the energy consumption of the device is increased; meanwhile, the product benzene is taken as a product outlet device and is not fully utilized, so that the total yield of the paraxylene is further reduced.
Disclosure of Invention
Aiming at the defects of the prior art, the invention aims to provide a method for producing more paraxylene, which improves the selectivity of paraxylene, fully utilizes the conversion of benzene and toluene products into paraxylene, reduces the energy consumption of a device and improves the total yield of paraxylene which is a high value-added product.
In order to achieve the above purpose, the technical scheme adopted by the invention is as follows:
The technical object of the first aspect of the present invention is to provide a process system for producing paraxylene in high yield, comprising a xylene fractionation unit, an adsorption separation unit, an isomerization reaction unit, a disproportionation and transalkylation unit and an alkylation unit;
The xylene fractionation unit comprises a xylene tower, a heavy aromatic hydrocarbon tower and a C 8 + mixed aromatic hydrocarbon raw material feeding pipeline connected with the xylene tower, wherein a tower bottom discharging pipeline of the xylene tower is connected with an inlet of the heavy aromatic hydrocarbon tower, a tower top discharging pipeline of the xylene tower is connected with an adsorption separation unit, the heavy aromatic hydrocarbon tower is a dividing wall tower, a tower top discharging pipeline of the heavy aromatic hydrocarbon tower is connected with a disproportionation and transalkylation reactor, and a side line discharging pipeline is connected with the transalkylation reactor;
The adsorption separation unit comprises an adsorption separation tower, and is used for separating a paraxylene stream and a paraxylene-lean stream, and the paraxylene-lean stream pipeline is connected with the isomerization reaction unit;
The isomerization reaction unit comprises an isomerization reactor and a deheptanizer connected with the isomerization reactor, wherein a tower top material pipeline of the deheptanizer is connected with a benzene tower I, and a tower bottom material pipeline is connected with a xylene tower;
the disproportionation and transalkylation unit comprises a disproportionation and transalkylation reactor, a transalkylation reactor and a clay tower, wherein the discharge pipelines of the disproportionation and transalkylation reactor and the transalkylation reactor are connected with the feed pipeline of the clay tower, and the discharge pipeline of the clay tower is connected with the benzene tower I;
The alkylation unit comprises a benzene tower I, a toluene tower I and an alkylation reactor, wherein a top discharge pipeline of the benzene tower I is connected with the transalkylation reactor, a bottom discharge pipeline is connected with the toluene tower I, a top discharge pipeline of the toluene tower I is connected with the alkylation reactor, a bottom discharge pipeline is connected with the xylene tower, the alkylation reactor comprises a reactant feed pipeline, a product discharge pipeline of the alkylation reactor is connected with a gas-liquid separator after passing through a cooler, a gas-phase material outlet pipeline of the gas-liquid separator is connected with a reactant feed pipeline of the alkylation reactor after passing through a compressor, a liquid-phase material outlet pipeline of the gas-liquid separator is connected with an oil-water separator, a water-phase product outlet pipeline of the oil-water separator is connected with a methanol recovery tower, a top discharge pipeline of the methanol recovery tower is connected with a reactant feed pipeline of the alkylation reactor, and bottom discharge is water; the top discharge pipeline of the benzene tower II is connected with the transalkylation reactor, the bottom discharge pipeline of the benzene tower II is connected with the toluene tower II, the top discharge pipeline of the toluene tower II is connected with the disproportionation and transalkylation reactor, and the bottom discharge pipeline of the toluene tower II is connected with the xylene tower.
Further, the feed line to the transalkylation reactor is also connected to a benzene feed line from an aromatic extraction unit.
Further, the feed line to the disproportionation and transalkylation reactor is also connected to the toluene feed line from the aromatic extraction unit.
Further, the heavy aromatic hydrocarbon tower is a dividing wall tower, a vertical baffle plate is arranged in the middle of the traditional rectifying tower, and the rectifying tower is divided into an upper public rectifying section, a lower public stripping section, a rectifying feeding section and a side line extraction section which are separated by the baffle plate.
The technical purpose of the second aspect of the invention is to provide a process method for producing more para-xylene by using the system, which comprises the following steps: the method comprises the steps that C 8 + mixed aromatic hydrocarbon raw materials from an aromatic hydrocarbon extraction unit enter a xylene tower of a xylene fractionation unit, the bottom materials are C 9 + mixed aromatic hydrocarbons, the mixed aromatic hydrocarbon raw materials enter a heavy aromatic hydrocarbon tower, the top materials are C 8 aromatic hydrocarbons, the mixed aromatic hydrocarbon raw materials enter an adsorption separation unit, high-purity paraxylene is separated, a low-paraxylene material flow enters an isomerization reactor of an isomerization reaction unit, reaction products of the isomerization reactor enter a deheptanizer, the top materials of the deheptanizer are C 7 - mixed aromatic hydrocarbons, the benzene tower I of an alkylation unit, the bottom materials of the benzene tower I are C 8 + mixed aromatic hydrocarbons, and the mixed aromatic hydrocarbon raw materials return to the xylene tower of the xylene fractionation unit; the bottom material of the heavy aromatic hydrocarbon tower is C 11 + mixed aromatic hydrocarbon, the top material is C 9 aromatic hydrocarbon, the mixed aromatic hydrocarbon enters a disproportionation and transalkylation reactor, the side material is C 10 aromatic hydrocarbon, and the mixed aromatic hydrocarbon enters the transalkylation reactor; the products of the disproportionation and alkyl transfer reactor and the products of the alkyl transfer reactor enter a clay tower to remove impurities such as olefin and the like, and the discharged materials of the clay tower enter a benzene tower I;
Benzene is taken as the top material of the benzene tower I, enters a transalkylation reactor, and the bottom material of the benzene tower I is C 7 + mixed aromatic hydrocarbon and enters a toluene tower I; the tower bottom material of the toluene tower I is C 8 + mixed aromatic hydrocarbon, the mixed aromatic hydrocarbon enters the xylene tower, the tower top material and the methanol enter an alkylation reactor together, an alkylation reaction product is cooled by a cooler and then enters a gas-liquid separator, a separated gas phase is boosted by a compressor and then returns to the alkylation reactor, a separated liquid phase enters an oil-water separator, a water phase product separated by the oil-water separator enters a methanol recovery tower, the tower top material of the methanol recovery tower is methanol and returns to the alkylation reactor, and the tower bottom material is water; the oil phase product separated by the oil-water separator enters a benzene tower II, the top product of the benzene tower II is benzene, the benzene enters a transalkylation reactor, and the bottom material is C 7 + mixed aromatic hydrocarbon and enters a toluene tower II; toluene is taken as the top material of the toluene tower II, the toluene enters a disproportionation and transalkylation reactor, and the bottom material is C 8 + mixed aromatic hydrocarbon and enters a xylene tower.
Further, the feed to the transalkylation reactor also includes benzene from the aromatic extraction unit.
Further, the feed to the disproportionation and transalkylation reactor also includes toluene from the aromatic extraction unit.
The mixed aromatic hydrocarbon mixture raw material of C 8 + from the aromatic hydrocarbon extraction unit mainly comprises mixed aromatic hydrocarbon containing ethylbenzene, paraxylene, o-xylene and m-xylene, and also comprises heavy hydrocarbon with a content of more than C 9. Wherein the heavy hydrocarbon above C 9 is hydrocarbon such as aromatic hydrocarbon, alkane, naphthene hydrocarbon with carbon number above 9.
In the xylene fractionation unit, the top pressure of the xylene column is 0.3-2.5 mpa, preferably 0.5-1.8 mpa, and the top temperature is 50-300 ℃, preferably 110-280 ℃. The xylene tower is preferably a plate tower, and the number of the plates is 150-200.
In the xylene fractionating unit, a heavy aromatic hydrocarbon tower is a dividing wall tower, a vertical baffle plate is arranged in the middle of a traditional rectifying tower, and the rectifying tower is divided into an upper public rectifying section, a lower public stripping section, a rectifying feeding section and a side line extraction section which are separated by the baffle plate; the tower top material is C 9 aromatic hydrocarbon, the tower bottom material is C 11 + mixed aromatic hydrocarbon, and the lateral line material is C 10 aromatic hydrocarbon.
In the adsorption separation unit, a simulated moving bed process of countercurrent contact of liquid and solid is adopted, the selectivity of the adsorbent to four isomers of C 8 aromatic hydrocarbon is utilized to preferentially adsorb paraxylene, and then the desorber is used for desorbing the paraxylene on the adsorbent. The inside of the adsorption separation tower is filled with an adsorbent with high selectivity for paraxylene. The active component of the adsorbent is an X-type zeolite or a Y-type molecular sieve of Ba or BaK, and the binder is selected from kaolin, silicon dioxide or aluminum oxide. The desorbent is not only mutually soluble with each component in the raw materials, but also has larger boiling point difference with each component in the C 8 aromatic hydrocarbon, is easy to recycle and is preferably p-diethylbenzene or toluene.
The operation conditions of the adsorption separation unit are as follows: the temperature is 100 to 300 ℃, preferably 150 to 200 ℃, and the pressure is 0.2 to 1.5MPa, preferably 0.6 to 1.0MPa.
The operating conditions of the isomerization reaction unit are as follows: the reaction temperature is 300-450 ℃, preferably 330-400 ℃, the pressure is 0.1-2.0 MPa, preferably 0.4-1.5 MPa, the mass airspeed is 2-10 hours -1, preferably 3-6 hours -1, and the molar ratio of reaction hydrogen to hydrocarbon is 2-8, preferably 3-6.
In the isomerization reaction unit, an isomerization catalyst is filled in the isomerization reactor, and the isomerization catalyst is a molecular sieve or an inorganic oxide carrier and is loaded with one or more active components of Pt, sn, mg, bi, pb, pd, re, mo, W, V and rare earth metals. The molecular sieve is one or a mixture of a plurality of five-membered ring molecular sieve, mordenite, EUO type molecular sieve and MFI molecular sieve. The inorganic oxide is alumina and/or silica.
The alkylating reagent adopted in the alkylation reactor is CH 3 Br, synthesis gas, methanol and the like, preferably methanol, and meanwhile toluene generates disproportionation reaction to generate benzene and C 8 aromatic hydrocarbon. Zeolite molecular sieves, mainly X zeolite, Y zeolite, mordenite, MOR, ZSM-5, MCM-22, SAPO-5, SAPO-11, SAPO-34, etc., are filled in the alkylation reactor. The operating conditions are as follows: the reaction temperature is 300-700 ℃, preferably 400-600 ℃, the pressure is 0.1-2.0 MPa, preferably 0.1-0.5 MPa, and the mass airspeed is 1-10 h -1, preferably 2-4 h -1.
In the disproportionation and transalkylation reactor, reactants are toluene and C 9 aromatic hydrocarbon, and toluene from an aromatic hydrocarbon extraction unit is used as a supplementary reactant and is regulated according to the amount of C 9 aromatic hydrocarbon. The disproportionation and transalkylation reactor is filled with a catalyst of molecular sieve loaded with active components, wherein the molecular sieve is selected from beta-zeolite, mordenite, MCM-22 and other molecular sieves, the active components are selected from at least one of metals of bismuth, molybdenum, silver, copper, zirconium, lanthanum and rhenium or oxides thereof, and the operation conditions are as follows: the reaction temperature is 250-650 ℃, preferably 300-550 ℃, the pressure is 1-8 MPa, preferably 2-5 MPa, and the weight space velocity is 0.2-3 h -1, preferably 0.5-2 h -1.
In the transalkylation reactor, reactants are benzene and C 10 arene, benzene from an arene extraction unit is a supplementary reactant, and the reaction is regulated according to the amount of C 10 arene. The catalyst of active components loaded by molecular sieves is filled in the transalkylation reactor, the molecular sieves are selected from beta-zeolite, mordenite, MCM-22 and other molecular sieves, the active components are selected from at least one of metals of bismuth, molybdenum, silver, copper, zirconium, lanthanum and rhenium or oxides thereof, and the operation conditions are as follows: the reaction temperature is 200-650 ℃, preferably 320-550 ℃, the pressure is 1-8 MPa, preferably 2.5-5.5 MPa, and the weight space velocity is 0.2-3 h -1, preferably 0.5-2.7 h -1.
Compared with the prior art, the production process of the high-yield paraxylene has the following beneficial effects: the conversion rate of toluene is improved, the conversion of benzene to paraxylene is fully utilized, and meanwhile, the separation wall tower technology is adopted, so that the aim of separating reactants from reaction products in one tower is fulfilled, the energy consumption of the device is reduced, the paraxylene yield of a high value-added product is improved, and the economic benefit and the social benefit are improved.
Drawings
The accompanying drawings are included to provide a further understanding of the invention, and are incorporated in and constitute a part of this specification, illustrate the invention and together with the description serve to explain, without limitation, the invention. In the drawings:
FIG. 1 is a schematic diagram of a conventional para-xylene production process flow;
FIG. 2 is a schematic diagram of the process flow for the production of para-xylene in accordance with the present invention.
Wherein, 101. C 8 + mixed aromatic hydrocarbon raw material from aromatic hydrocarbon extraction unit, 102. Xylene column, 103. Adsorption separation unit, 104. Para-xylene, 105. Isomerization reaction unit, 106. Deheptanizer, 107.C 7 -aromatic hydrocarbon, 108. Heavy aromatic hydrocarbon column, 109.C 10 + mixed aromatic hydrocarbon, 110. Toluene from aromatic hydrocarbon extraction unit, 111. Disproportionation and transalkylation reactor, 112. Clay column, 113. Benzene column, 114. Benzene, 115. Toluene column.
201. C 8 + mixed aromatics feed from the aromatics extraction unit, 202. Xylene column, 203. Adsorption separation unit, 204. Para-xylene, 205. Isomerization reactor, 206. Deheptanizer, 207. Heavy aromatics column, 208.C 10 + mixed aromatics, 209. Disproportionation and transalkylation reactor, 210. Clay column, 211. Benzene column I, 212. Transalkylation reactor, 213. Toluene column I, 214. Toluene from the aromatics extraction unit, 215. Methanol, 216. Alkylation reactor, 217. Cooler, 218. Gas-liquid separation tank, 219. Compressor, 220. Oil-water separator, 221. Methanol recovery column, 222. Water, 223. Benzene column II, 224. Toluene column II, 225. Benzene from the aromatics extraction unit.
Detailed Description
The production process of paraxylene according to the present invention will be described in more detail with reference to the accompanying drawings.
In the following examples and comparative examples, the following formulas were used for calculation of each parameter:
FIG. 1 is a schematic diagram of a conventional process for producing para-xylene from C 8 + mixed aromatics, the process including a xylene fractionation unit, an adsorptive separation unit, an isomerization unit, and a disproportionation and transalkylation unit. The specific process flow is as follows: the C 8 + mixed aromatic hydrocarbon raw material 101 from the aromatic hydrocarbon extraction unit is fed into a xylene tower 102, the tower top material is used as raw material of an adsorption separation unit 103, and the tower bottom material is fed into a heavy aromatic hydrocarbon tower 108. The high-purity paraxylene 104 is separated by the adsorption separation unit 103, the paraxylene-lean material flow enters the isomerization reaction unit 105, the reaction product enters the deheptanizer column 106, the top material is C 7 -aromatic hydrocarbon 107, and the bottom material returns to the paraxylene column 102. The bottom material of the heavy aromatic column 108 is C 10 + mixed aromatic 109, and the top material and toluene 110 from the aromatic extraction unit enter a disproportionation and transalkylation reactor 111. The reaction product is sent to benzene tower 113 after the impurities such as olefin are removed by clay tower 112, the top product is benzene 114, and the bottom material is sent to toluene tower 115. The toluene overhead enters the disproportionation and transalkylation reactor and the bottoms enters the xylene column 102.
FIG. 2 is a schematic flow chart of the para-xylene production process of the present invention, wherein the process flow comprises a xylene fractionation unit, an adsorption separation unit, an isomerization unit, a disproportionation and transalkylation unit, and an alkylation unit. The process flow for producing paraxylene is as follows: the mixed C 8 + aromatic hydrocarbon raw material 201 from the aromatic hydrocarbon extraction unit enters a xylene tower 202 of a xylene fractionation unit, the bottom material is mixed C 9 + aromatic hydrocarbon, the mixed C 9 + aromatic hydrocarbon raw material enters a heavy aromatic hydrocarbon tower 207, the top material is C 8 aromatic hydrocarbon, the mixed C 9 + aromatic hydrocarbon raw material enters an adsorption separation unit 203, high-purity para-xylene 204 is separated, a para-xylene-poor material enters an isomerization reactor 205 of an isomerization reaction unit, the reaction product of the isomerization reactor 205 enters a deheptanizer 206, the top material of the deheptanizer 206 is mixed C 7 - aromatic hydrocarbon, the mixed C 8 + aromatic hydrocarbon is introduced into a benzene tower I of an alkylation unit, and the bottom material is mixed C 8 + aromatic hydrocarbon, and the mixed C3934 aromatic hydrocarbon is returned to the xylene tower 202 of the xylene fractionation unit; the bottom material of the heavy aromatic column 207 is C 11 + mixed aromatic hydrocarbon, the top material is C 9 aromatic hydrocarbon, the mixture enters the disproportionation and transalkylation reactor 209, the side material is C 10 aromatic hydrocarbon, and benzene 225 from the aromatic hydrocarbon extraction unit enters the transalkylation reactor 212; the products of the disproportionation and transalkylation reactor and the products of the transalkylation reactor enter a clay tower 210 to remove impurities such as olefin and the like, and the discharged materials of the clay tower 210 enter a benzene tower I211;
Benzene is taken as the top material of the benzene tower I211, enters the transalkylation reactor 210, and the bottom material is C 7 + mixed aromatic hydrocarbon, enters the toluene tower I213; the bottom material of the toluene tower I213 is C 8 + mixed aromatic hydrocarbon, the mixed aromatic hydrocarbon enters the xylene tower 202, the top material, toluene 214 from an aromatic hydrocarbon extraction unit and methanol 215 enter an alkylation reactor 216 together, an alkylation reaction product is cooled by a cooler 217 and then enters a gas-liquid separator 218, the separated gas phase is boosted by a compressor 219 and then returns to the alkylation reactor 216, the separated liquid phase enters an oil-water separator 220, the water phase product separated by the oil-water separator 220 enters a methanol recovery tower 221, the top material of the methanol recovery tower 221 is methanol, the methanol returns to the alkylation reactor 216, and the bottom material is water 222; the oil phase product separated by the oil-water separator 220 enters a benzene tower II 223, the top product of the benzene tower II 223 is benzene, the benzene enters a transalkylation reactor 212, and the bottom material is C 7 + mixed aromatic hydrocarbon and enters a toluene tower II 224; toluene column II 224 has toluene as the top material and a disproportionation and transalkylation reactor 209, and aromatic hydrocarbon mixture as the bottom material and C 8 + as the bottom material and a xylene column 202.
The effect of the productive p-xylene production process provided by the present invention is specifically described below by way of examples.
Comparative example 1
Comparative example 1 illustrates the process and energy consumption of conventional para-xylene production. The composition of the C 8 + aromatic hydrocarbon mixture feed from the aromatic hydrocarbon extraction unit is shown in Table 1, and the toluene purity from the aromatic hydrocarbon extraction unit is >95%.
TABLE 1C 8 + composition of aromatic hydrocarbon mixture feedstock
The result of paraxylene production by using the process system shown in fig. 1 shows that in the conventional paraxylene production process, the toluene conversion rate is 21%, the paraxylene yield is 61.8%, and the device energy consumption is 332 kgEO/(t.px).
Example 1
Example 1 illustrates the process and energy consumption of the multi-product para-xylene production provided by the present invention. The feed composition was consistent with comparative example 1, with benzene and toluene purities >95% from the aromatic extraction unit.
The production of paraxylene by the process system shown in fig. 2 shows that the toluene conversion is 26.5%, the paraxylene yield is 67.4%, and the device energy consumption is 310 kgEO/(t.px).
Compared with the conventional xylene production process, the method for producing the paraxylene provided by the invention has the advantages that the toluene conversion rate is increased by 26.2%, the paraxylene yield is increased by 9.1%, and the device energy consumption is reduced by 6.6%. Therefore, the invention improves the conversion rate of toluene and the yield of paraxylene, and simultaneously utilizes benzene to generate paraxylene with high added value, thereby reducing the energy consumption of the device.
Claims (18)
1. The process system for producing the paraxylene is characterized by comprising a xylene fractionation unit, an adsorption separation unit, an isomerization reaction unit, a disproportionation and transalkylation unit and an alkylation unit;
The xylene fractionation unit comprises a xylene tower, a heavy aromatic hydrocarbon tower and a C 8 + mixed aromatic hydrocarbon raw material feeding pipeline connected with the xylene tower, wherein a tower bottom discharging pipeline of the xylene tower is connected with an inlet of the heavy aromatic hydrocarbon tower, a tower top discharging pipeline of the xylene tower is connected with an adsorption separation unit, the heavy aromatic hydrocarbon tower is a dividing wall tower, a tower top discharging pipeline of the heavy aromatic hydrocarbon tower is connected with a disproportionation and transalkylation reactor, and a side line discharging pipeline is connected with the transalkylation reactor;
The adsorption separation unit comprises an adsorption separation tower, and is used for separating a paraxylene stream and a paraxylene-lean stream, and the paraxylene-lean stream pipeline is connected with the isomerization reaction unit;
The isomerization reaction unit comprises an isomerization reactor and a deheptanizer connected with the isomerization reactor, wherein a tower top material pipeline of the deheptanizer is connected with a benzene tower I, and a tower bottom material pipeline is connected with a xylene tower;
the disproportionation and transalkylation unit comprises a disproportionation and transalkylation reactor, a transalkylation reactor and a clay tower, wherein the discharge pipelines of the disproportionation and transalkylation reactor and the transalkylation reactor are connected with the feed pipeline of the clay tower, and the discharge pipeline of the clay tower is connected with the benzene tower I;
The alkylation unit comprises a benzene tower I, a toluene tower I and an alkylation reactor, wherein a top discharge pipeline of the benzene tower I is connected with the transalkylation reactor, a bottom discharge pipeline is connected with the toluene tower I, a top discharge pipeline of the toluene tower I is connected with the alkylation reactor, a bottom discharge pipeline is connected with the xylene tower, the alkylation reactor comprises a reactant feed pipeline, a product discharge pipeline of the alkylation reactor is connected with a gas-liquid separator after passing through a cooler, a gas-phase material outlet pipeline of the gas-liquid separator is connected with a reactant feed pipeline of the alkylation reactor after passing through a compressor, a liquid-phase material outlet pipeline of the gas-liquid separator is connected with an oil-water separator, a water-phase product outlet pipeline of the oil-water separator is connected with a methanol recovery tower, a top discharge pipeline of the methanol recovery tower is connected with a reactant feed pipeline of the alkylation reactor, and bottom discharge is water; the top discharge pipeline of the benzene tower II is connected with the transalkylation reactor, the bottom discharge pipeline of the benzene tower II is connected with the toluene tower II, the top discharge pipeline of the toluene tower II is connected with the disproportionation and transalkylation reactor, and the bottom discharge pipeline of the toluene tower II is connected with the xylene tower.
2. The process system of claim 1, wherein the feed line to the transalkylation reactor is further connected to a benzene feed line from an aromatics extraction unit.
3. The process system of claim 1, wherein the feed line to the disproportionation and transalkylation reactor is further connected to a toluene feed line from an aromatic extraction unit.
4. The process system of claim 1, wherein the heavy aromatic column is a dividing wall column, and a vertical partition plate is placed in the middle of the conventional rectifying column to divide the rectifying column into four parts, namely an upper public rectifying section, a lower public stripping section, and a rectifying feeding section and a side-draw section which are separated by the partition plate.
5. A process for the production of para-xylene using the process system according to any one of the claims 1 to 4, comprising: the method comprises the steps that C 8 + mixed aromatic hydrocarbon raw materials from an aromatic hydrocarbon extraction unit enter a xylene tower of a xylene fractionation unit, the bottom materials are C 9 + mixed aromatic hydrocarbons, the mixed aromatic hydrocarbon raw materials enter a heavy aromatic hydrocarbon tower, the top materials are C 8 aromatic hydrocarbons, the mixed aromatic hydrocarbon raw materials enter an adsorption separation unit, high-purity paraxylene is separated, a low-paraxylene material flow enters an isomerization reactor of an isomerization reaction unit, reaction products of the isomerization reactor enter a deheptanizer, the top materials of the deheptanizer are C 7 - mixed aromatic hydrocarbons, the benzene tower I of an alkylation unit, the bottom materials of the benzene tower I are C 8 + mixed aromatic hydrocarbons, and the mixed aromatic hydrocarbon raw materials return to the xylene tower of the xylene fractionation unit; the bottom material of the heavy aromatic hydrocarbon tower is C 11 + mixed aromatic hydrocarbon, the top material is C 9 aromatic hydrocarbon, the mixed aromatic hydrocarbon enters a disproportionation and transalkylation reactor, the side material is C 10 aromatic hydrocarbon, and the mixed aromatic hydrocarbon enters the transalkylation reactor; the product of the disproportionation and transalkylation reactor and the product of the transalkylation reactor enter a clay tower to remove olefin impurities, and the discharged material of the clay tower enters a benzene tower I;
Benzene is taken as the top material of the benzene tower I, enters a transalkylation reactor, and the bottom material of the benzene tower I is C 7 + mixed aromatic hydrocarbon and enters a toluene tower I; the tower bottom material of the toluene tower I is C 8 + mixed aromatic hydrocarbon, the mixed aromatic hydrocarbon enters the xylene tower, the tower top material and the methanol enter an alkylation reactor together, an alkylation reaction product is cooled by a cooler and then enters a gas-liquid separator, a separated gas phase is boosted by a compressor and then returns to the alkylation reactor, a separated liquid phase enters an oil-water separator, a water phase product separated by the oil-water separator enters a methanol recovery tower, the tower top material of the methanol recovery tower is methanol and returns to the alkylation reactor, and the tower bottom material is water; the oil phase product separated by the oil-water separator enters a benzene tower II, the top product of the benzene tower II is benzene, the benzene enters a transalkylation reactor, and the bottom material is C 7 + mixed aromatic hydrocarbon and enters a toluene tower II; toluene is taken as the top material of the toluene tower II, the toluene enters a disproportionation and transalkylation reactor, and the bottom material is C 8 + mixed aromatic hydrocarbon and enters a xylene tower.
6. The process of claim 5 wherein the feed to the transalkylation reactor further comprises benzene from an aromatic extraction unit and the feed to the disproportionation and transalkylation reactor further comprises toluene from the aromatic extraction unit.
7. The process according to claim 5, wherein in the xylene fractionation unit, the top pressure of the xylene column is 0.3 to 2.5mpa, and the top temperature is 50 to 300 ℃; the xylene tower is a plate tower, and the number of the plates is 150-200.
8. The process according to claim 7, wherein in the xylene fractionation unit, the top pressure of the xylene column is 0.5 to 1.8mpa and the top temperature is 110 to 280 ℃.
9. The process according to claim 5, wherein in the xylene fractionation unit, the heavy aromatic column is a dividing wall column, a vertical partition plate is placed in the middle of the conventional rectifying column, and the rectifying column is divided into an upper common rectifying section, a lower common stripping section, and a rectifying feed section and a side draw section separated by the partition plate; the tower top material is C 9 aromatic hydrocarbon, the tower bottom material is C 11 + mixed aromatic hydrocarbon, and the lateral line material is C 10 aromatic hydrocarbon.
10. The process according to claim 5, wherein the adsorption separation unit adopts a simulated moving bed process of countercurrent contact of liquid and solid, uses different selectivities of the adsorbent to four isomers of C 8 aromatic hydrocarbon to preferentially adsorb paraxylene, and then desorbs paraxylene on the adsorbent by using a desorber.
11. The process according to claim 10, wherein the adsorption separation column is internally filled with an adsorbent having high selectivity for para-xylene, the active component of the adsorbent is an X-type zeolite or a Y-type molecular sieve of Ba or BaK, and the binder is selected from kaolin, silica or alumina.
12. The process of claim 5, wherein the adsorption separation unit is operated under the following conditions: the temperature is 100-300 ℃ and the pressure is 0.2-1.5 MPa.
13. The process of claim 5, wherein the isomerization unit is operated under the following conditions: the reaction temperature is 300-450 ℃, the pressure is 0.1-2.0 MPa, the mass airspeed is 2-10 hours -1, and the molar ratio of reaction hydrogen to hydrocarbon is 2-8.
14. The process according to claim 5, wherein the isomerization reactor is filled with an isomerization catalyst, and the isomerization catalyst is a molecular sieve or an inorganic oxide carrier loaded with one or more active components selected from Pt, sn, mg, bi, pb, pd, re, mo, W, V and rare earth metals; the molecular sieve is one or a mixture of a plurality of five-membered ring molecular sieve, mordenite, EUO type molecular sieve and MFI molecular sieve; the inorganic oxide is alumina and/or silica.
15. The process of claim 5 wherein the alkylation reactor contains a zeolite molecular sieve selected from at least one of zeolite X, zeolite Y, mordenite, MOR, ZSM-5, MCM-22, SAPO-5, SAPO-11, and SAPO-34.
16. The process of claim 5 wherein the alkylation reactor operating conditions are: the reaction temperature is 300-700 ℃, the pressure is 0.1-2.0 MPa, and the mass airspeed is 1-10 h -1.
17. The process of claim 5 wherein the disproportionation and transalkylation reactor contains a catalyst having an active component supported thereon, the molecular sieve being selected from the group consisting of beta zeolite, mordenite, MCM-22 molecular sieves, the active component being selected from at least one of the metals bismuth, molybdenum, silver, copper, zirconium, lanthanum and rhenium or oxides thereof, operating under the following conditions: the reaction temperature is 250-650 ℃, the pressure is 1-8 MPa, and the weight airspeed is 0.2-3 h -1.
18. The process of claim 5 wherein the transalkylation reactor is charged with a catalyst having an active component selected from the group consisting of beta zeolite, mordenite, MCM-22 molecular sieves, and at least one of the metals or oxides thereof selected from the group consisting of bismuth, molybdenum, silver, copper, zirconium, lanthanum and rhenium, operating conditions being as follows: the reaction temperature is 200-650 ℃, the pressure is 1-8 MPa, and the weight airspeed is 0.2-3 h -1.
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