CN1377866A - Pre-treatment method for aromatic hydrocarbon - Google Patents
Pre-treatment method for aromatic hydrocarbon Download PDFInfo
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- CN1377866A CN1377866A CN01105848A CN01105848A CN1377866A CN 1377866 A CN1377866 A CN 1377866A CN 01105848 A CN01105848 A CN 01105848A CN 01105848 A CN01105848 A CN 01105848A CN 1377866 A CN1377866 A CN 1377866A
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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- 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
Abstract
The present invention relates to pre-treating method of arene and aims at solving the problem of poisoning deactivation of arene material to shorten the service life of catalyst during alkylation or transalkylation. In the arene pre-treatment technology, arene is pretreated with pre-treating agent containing hydrogen zeolite as main catalyst component and at temperature 0-300 deg.c and pressure 0-6.0 MPa so as to eliminate harmful components before its alkylation or transalkylation reaction. The said method may be used in industrial production.
Description
The present invention relates to a kind of pre-treatment method for aromatic hydrocarbon, particularly about the pretreated method of the aromatic hydrocarbons that is used for alkylation or transalkylation reaction.
Alkylbenzene is important basic Organic Chemicals such as ethylbenzene and isopropyl benzene.Ethylbenzene more than 98% comes from the alkylation of benzene and ethene, as cinnamic raw material.Isopropyl benzene is a raw material of producing phenol-acetone, and the phenol more than 90% is prepared by cumene method, and ratio is also increasing.At superseded alchlor process, after zeolite vapor-phase alkylation method, solid phosphoric acid vapor-phase alkylation method are competed respectively mutually, zeolite liquid-phase alkylation method becomes the main method of current production ethylbenzene, isopropyl benzene, is respectively the important component part of producing vinylbenzene, phenol process route.
Chinese patent CN1217310A " production technique of alkylbenzene ": a Recycle design part is returned alkylation reactor beyond the reaction solution, each section of alkylation reactor adopts intermediate heat segmentation heat-obtaining technology, and the liquid phase zeolite catalysis prepares ethylbenzene, isopropyl benzene and composition thereof.Chinese patent CN1175567A " alkylating method is carried out in the circulation by reactor effluent " uses conventional alkylation catalyst under gas phase or liquid-phase reaction condition, fresh aromatic hydrocarbons, alkylating agent and cycling stream are imported conversion zone, produce alkylated aromatic hydrocarbons (as ethylbenzene).These are compared with ordinary method by reactor effluent round-robin method, can reduce investment outlay and energy consumption, improve the benzene/olefin molar ratio in the reaction system simultaneously, thereby prolong catalyzer work-ing life.But monoalkylated benzenes content increases in the reactor feed, and is influential to the monoalkyl arenes selectivity.
U.S. Pat P4169111 " production of ethylbenzene " proposes benzene and ethene alkylation under the zeolite catalyst effect generates ethylbenzene and many ethylbenzene, at least a portion diethylbenzene returns alkylation reactor, and remaining diethylbenzene contains many ethylbenzene and benzene generates additional ethylbenzene in the transalkylation reactor that other establishes.At least a portion high purity diethylbenzene returns alkylation reactor, and under suitable operational condition, catalyzer work-ing life, and under the same terms, when not having many ethylbenzene and returning, catalyzer work-ing life was 93 days all more than 1 year in two different cycles of operation; When two, triethyl-benzene all returned, catalyzer work-ing life only was 55 days.A kind of alkylation catalyst method in work-ing life that prolongs of invention that Chinese patent CN1068809A " prolongs the method for life of alkylation catalysts ", for in the presence of alkylation catalyst with at least a aromatic hydrocarbons, for example benzene and at least a olefin alkylation reaction are produced at least a monoalkyl aromatic hydrocarbons, improvements are with a kind of additive that is selected from alcohol or water and at least a aromatic hydrocarbons, at least a olefin, cause catalyzer work-ing life to be improved, and can alkylation when aromatic hydrocarbons and alkene are in lower mol ratio.The addition of water exists with 200～1000PPm.Additive is an ethanol during synthesizing ethyl benzene.Additive is a Virahol during synthesizing iso-propylbenzene.U.S. Pat P5240889 " alkylation catalyst of hydration " is a kind of composition catalyzer that is used for alkylation and transalkylation, comprise a kind of molecular sieve, a kind of inorganic refractory oxide compound and surpass the moisture of 3.5wt% with alkylation and/or transalkylation activity.Benzene alkylation with ethylene and with the preparation ethylbenzene process integration of diethylbenzene transalkylation in, this catalyzer is found can keep long work-ing life.In preparation isopropyl benzene process integration, also like this.
Add some materials in the above-mentioned patent,, perhaps improve catalyst performance and suppress long-pending burnt side reaction, thereby prolong catalyzer work-ing life perhaps by adjusting reaction system.
No matter be process modification, or additive, all raw material aromatic hydrocarbons do not had enough attention to the influence of catalyst performance.Industrial, to being used for the pretreatment process of alkylation, transalkylation aromatic hydrocarbons, generally be to use such as ion exchange resin, acidic white earth, zeolite etc. and under normal temperature or lesser temps, handle, be purpose just often to reduce alkaline matter, perfect not to the utmost to the effect of prevention poisoning of catalyst and prevention catalyst deactivation.
The objective of the invention is to exist in the existing document owing to contain alkylation or the virulent impurity of transalkylation catalyst in the aroamtic hydrocarbon raw material in order to overcome, make the easy poisoning and deactivation of alkylation or transalkylation catalyst, thereby shorten the catalyzer shortcoming in work-ing life, a kind of pre-treatment method for aromatic hydrocarbon is provided.Raw material aromatic hydrocarbons has catalyzer and is difficult for poisoning and deactivation after this method is handled, thereby prolongs the catalyzer characteristics in work-ing life.
The objective of the invention is to realize by following technical scheme: a kind of pre-treatment method for aromatic hydrocarbon may further comprise the steps:
A) aroamtic hydrocarbon raw material is 0～300 ℃ by loading the bed of pretreating agent in temperature, is 0～6.0MPa in gauge pressure pressure, and the aroamtic hydrocarbon raw material air speed is 0.1～1000 hour
-1Handle under the condition;
B) used pretreating agent comprises following component by weight percentage: (1) 10～100% h-type zeolite, (2) 0～90% aluminium or the oxide compound of silicon.
In the technique scheme, the temperature preferable range is 60～270 ℃, is 0.3～5.2MPa in gauge pressure pressure preferable range, and aroamtic hydrocarbon raw material air speed preferable range is 1～500 hour
-1The preferable range that used by weight percentage pretreating agent comprises the amount of h-type zeolite is 30～95%.H-type zeolite is selected from ZSM-5, ZSM-8, ZSM-11, ZSM-12, ZSM-22, ZSM-33, L zeolite, β zeolite, MCM-22, MCM-36, MCM-49, MCM-51, MCM-56, chabazite, mordenite or faujusite and stray crystal mixture thereof.By weight percentage, used pretreating agent preferred version is that load is selected from least a metal or oxide compound in nickel, palladium or the platinum on the h-type zeolite, and its consumption is 0.001～5.0%, and its consumption preferable range is 0.1～4.1%.By weight percentage, used pretreating agent more preferably scheme is after load is selected from least a metal or oxide compound in nickel, palladium or the platinum on the h-type zeolite, also load be selected from least a metal or oxide compound in gallium, zinc, copper, silver, cobalt, rhodium or the iridium, its consumption is 0.01～5%, and its consumption more preferably scope is 0.1～1.0%.
The preparation method of aroamtic hydrocarbon raw material pretreating agent of the present invention is the preparation method of general zeolite catalyst, for example uses the former powder of silicon source, aluminium source and auxiliary agent (such as the organic amine template) synthetic zeolite, through aftershapings such as ion-exchange, modifications, obtains catalyzer.Can come into operation after the activation treatment.
The pretreated aromatic hydrocarbons of aroamtic hydrocarbon raw material pretreating agent of the present invention can be fresh feed, also can be recycle feed, such as benzene, many ethylbenzene, polyisopropylbenzene or the like, is used for alkylation, transalkylation reaction.
The suitable pretreatment condition of aroamtic hydrocarbon raw material pretreating agent of the present invention is to guarantee protective material Partial Liquid Phase system at least, and pretreatment condition preferably is to guarantee the protective material liquid-phase system.The pretreatment temperature general range is 0～300 ℃.Pre-treatment pressure general range is counted 0～6.0MPa with gauge pressure.Pre-treatment aromatic hydrocarbons LHSV general range is 0.1～1000 hour
-1
Why technology in the document can cause poisoning of catalyst in the past, mainly was because contain alkylation or the deleterious material of transalkylation catalyst in the raw material aromatic hydrocarbons, as nitrogenous compound, and sulphur, non-aromatic impurity such as alkene, alkynes.By adopting aroamtic hydrocarbon raw material pretreating agent pre-treatment aromatic hydrocarbons, alkaline matter content is reduced more among the present invention, in order to avoid reduce catalyzer effective acid amount; Also can remove micro-impurity such as desulfuration effectively, in order to avoid be deposited on the catalyzer; Also can remove non-aromatic impurity such as alkene, alkynes effectively, in order to avoid form the burnt precursor that grades of recombinating, therefore effectively prevented poisoning of catalyst, stoped catalyst deactivation, thereby prolonged the work-ing life of alkylation or transalkylation catalyst, catalyzer has been prolonged more than 40% work-ing life at least, obtained effect preferably.
The present invention is further elaborated below by embodiment, and still, scope of the present invention has more than and is limited to following explanation.[embodiment 1]
Get 20 gram aroamtic hydrocarbon raw material pretreating agents, h-type zeolite wherein is that silica alumina ratio is 16 ZSM-5, bar shaped with moulding is positioned in the fixed-bed reactor, guaranteeing that pretreatment system is that liquid phase is under 210 ℃ of pretreatment temperatures, the pre-treatment pressure 3.0MPa, pretreated fresh benzene was with liquid volume air speed LHSV 10 hours
-1, pre-treatment is 500 hours continuously, and the pretreating agent performance does not descend, and obtains 80 kilograms of qualified benzene.[embodiment 2]
Get 20 gram aroamtic hydrocarbon raw material pretreating agents, h-type zeolite wherein is that silica alumina ratio is 1.2 faujusite, bar shaped with moulding is positioned in the fixed-bed reactor, guaranteeing that pretreatment system is that liquid phase is under 120 ℃ of pretreatment temperatures, the pre-treatment pressure 1.5MPa, pretreated fresh benzene was with liquid volume air speed LHSV 10 hours
-1, pre-treatment is 1000 hours continuously, and the pretreating agent performance does not descend, and obtains 160 kilograms of qualified benzene.[embodiment 3]
Get 20 gram aroamtic hydrocarbon raw material pretreating agents, h-type zeolite wherein is that silica alumina ratio is 8.0 faujusite, bar shaped with moulding is positioned in the fixed-bed reactor, guaranteeing that pretreatment system is that liquid phase is under 250 ℃ of pretreatment temperatures, the pre-treatment pressure 4.0MPa, pretreated fresh benzene was with liquid volume air speed LHSV 25 hours
-1, pre-treatment is 1000 hours continuously, and the pretreating agent performance does not descend, and obtains 400 kilograms of qualified benzene.[embodiment 4]
Get 20 gram aroamtic hydrocarbon raw material pretreating agents, h-type zeolite wherein is that silica alumina ratio is 12 mordenite, bar shaped with moulding is positioned in the fixed-bed reactor, guaranteeing that pretreatment system is that liquid phase is under 130 ℃ of pretreatment temperatures, the pre-treatment pressure 1.5MPa, pretreated fresh benzene was with liquid volume air speed LHSV 10 hours
-1, pre-treatment is 1000 hours continuously, and the pretreating agent performance does not descend, and obtains 160 kilograms of qualified benzene.[embodiment 5]
Get 20 gram aroamtic hydrocarbon raw material pretreating agents, h-type zeolite wherein is that silica alumina ratio is that 6.0 faujusite, Pd element wt content are 0.2%, bar shaped with moulding is positioned in the fixed-bed reactor, guaranteeing that pretreatment system is that liquid phase is under 160 ℃ of pretreatment temperatures, the pre-treatment pressure 2.0MPa, pretreated fresh benzene was with liquid volume air speed LHSV 50 hours
-1, pre-treatment is 750 hours continuously, and the pretreating agent performance does not descend, and obtains 600 kilograms of qualified benzene.[embodiment 6]
Get 20 gram aroamtic hydrocarbon raw material pretreating agents, h-type zeolite wherein is that silica alumina ratio is that 18 mordenite, Pd element wt content are 0.1%, bar shaped with moulding is positioned in the fixed-bed reactor, guaranteeing that pretreatment system is that liquid phase is under 150 ℃ of pretreatment temperatures, the pre-treatment pressure 1.5MPa, pretreated fresh benzene was with liquid volume air speed LHSV 25 hours
-1, pre-treatment is 800 hours continuously, and the pretreating agent performance does not descend, and obtains 320 kilograms of qualified benzene.[embodiment 7]
Get 20 gram aroamtic hydrocarbon raw material pretreating agents, h-type zeolite wherein is that silica alumina ratio is that 22 ZSM-5, Pd element wt content are 0.04%, Ni element wt content is 4.0%, Co element wt content is 0.8%, bar shaped with moulding is positioned in the fixed-bed reactor, guaranteeing that pretreatment system is that liquid phase is under 200 ℃ of pretreatment temperatures, the pre-treatment pressure 3.0MPa, pretreated fresh benzene was with liquid volume air speed LHSV 100 hours
-1, pre-treatment is 300 hours continuously, and the pretreating agent performance does not descend, and obtains 480 kilograms of qualified benzene.[embodiment 8]
Get 20 gram aroamtic hydrocarbon raw material pretreating agents, h-type zeolite wherein is that silica alumina ratio is that 5 faujusite, Pd element wt content are 0.06%, Ni element wt content is 3.0%, Cu element wt content is 0.2%, bar shaped with moulding is positioned in the fixed-bed reactor, guaranteeing that pretreatment system is that liquid phase is under 190 ℃ of pretreatment temperatures, the pre-treatment pressure 3.0MPa, pretreated fresh benzene was with liquid volume air speed LHSV 200 hours
-1, pre-treatment is 200 hours continuously, and the pretreating agent performance does not descend, and obtains 640 kilograms of qualified benzene.[embodiment 9]
Get 20 gram aroamtic hydrocarbon raw material pretreating agents, h-type zeolite wherein is that silica alumina ratio is that 7.0 faujusite, Pd element wt content are 1.0%, Ni element wt content is 0.1%, Cu element wt content is 0.2%, bar shaped with moulding is positioned in the fixed-bed reactor, guaranteeing that pretreatment system is that liquid phase is under 100 ℃ of pretreatment temperatures, the pre-treatment pressure 1.5MPa, pretreated fresh benzene was with liquid volume air speed LHSV 5 hours
-1, pre-treatment is 1500 hours continuously, and the pretreating agent performance does not descend, and obtains 120 kilograms of qualified benzene.[embodiment 10]
Get 20 gram aroamtic hydrocarbon raw material pretreating agents, h-type zeolite wherein is that silica alumina ratio is that 10.0 mordenite, Pd element wt content are 0.7%, Pt element wt content is 0.1%, Cu element wt content is 0.6%, bar shaped with moulding is positioned in the fixed-bed reactor, guaranteeing that pretreatment system is that liquid phase is under 70 ℃ of pretreatment temperatures, the pre-treatment pressure 0.6MPa, pretreated fresh benzene was with liquid volume air speed LHSV 10 hours
-1, pre-treatment is 1500 hours continuously, and the pretreating agent performance does not descend, and obtains 240 kilograms of qualified benzene.[embodiment 11]
Appoint and to get embodiment 1,2,3,4,5 pretreated benzene, inlet amount is 4000 Grams Per Hours, and the ethylene feed amount is 150 Grams Per Hours, under 220 ℃ of temperature of reaction, reaction pressure 3.5MPa, in ethene WHSV 7.5 hours
-1Continuously by the alkylation reactor that 20 gram silica alumina ratios are 8 β zeolite alkylated catalyst is housed, investigated through 200 hours, do not detect ethene in the reaction product, the performance of alkylation catalyst does not descend, and its ethylbenzene selectivity (in ethyl) selectivity is more than 99.1%.[comparative example 1]
Get without pretreated fresh benzene, according to each step and the condition of the test of embodiment 11, after investigating through 120 hours, begin to detect ethene in the reaction product, the performance of alkylation catalyst descends to some extent, and its ethylbenzene selectivity (in ethyl) selectivity is 98.6%.[embodiment 12]
Appoint and to get embodiment 1,2,3,4,5,6,7,8,9,10 pretreated benzene, inlet amount is 300 Grams Per Hours, and the ethylene feed amount is 20 Grams Per Hours, under 220 ℃ of temperature of reaction, reaction pressure 3.5MPa, in ethene WHSV 1.0 hours
-1Continuously by the alkylation reactor that 20 gram silica alumina ratios are 28 β zeolite alkylated catalyst is housed, investigated through 2000 hours, do not detect ethene in the reaction product, the performance of alkylation catalyst does not descend, and its ethylbenzene selectivity (in ethyl) selectivity is 99.5%.[comparative example 2]
Get without pretreated fresh benzene, according to each step and the condition of the test of embodiment 12, after investigating through 1400 hours, begin to detect ethene in the reaction product, the performance of alkylation catalyst descends to some extent, and its ethylbenzene selectivity (in ethyl) selectivity is 98.8%.[embodiment 13]
Appoint and to get embodiment 1,2,3,4,5,6,7,8,9,10 pretreated benzene, inlet amount is 4000 Grams Per Hours, and the propylene feed amount is 200 Grams Per Hours, under 180 ℃ of temperature of reaction, reaction pressure 2.0MPa, in propylene WHSV 10 hours
-1Continuously by the alkylation reactor that 20 gram silica alumina ratios are 9 Y zeolite alkylation catalyst is housed, investigated through 200 hours, do not detect propylene in the reaction product, the performance of alkylation catalyst does not descend, and its isopropyl benzene selectivity (in propyl group) is 98.9%.[comparative example 3]
Get without pretreated fresh benzene, according to each step and the condition of the test of embodiment 13, after investigating through 140 hours, begin to detect propylene in the reaction product, the performance of alkylation catalyst descends to some extent, and its isopropyl benzene selectivity (in propyl group) is 98.2%.[embodiment 14]
Appoint and to get embodiment 1,2,3,4,5,6,7,8,9,10 pretreated benzene, inlet amount is 300 Grams Per Hours, and the propylene feed amount is 30 Grams Per Hours, under 180 ℃ of temperature of reaction, reaction pressure 2.0MPa, in propylene WHSV 1.5 hours
-1Continuously by the alkylation reactor that 20 gram silica alumina ratios are 27 β zeolite alkylated catalyst is housed, investigated through 2000 hours, do not detect propylene in the reaction product, the performance of alkylation catalyst does not descend, and its isopropyl benzene selectivity (in propyl group) is 99.3%.[comparative example 4]
Get without pretreated fresh benzene, according to each step and the condition of the test of embodiment 14, after investigating through 1200 hours, begin to detect propylene in the reaction product, the performance of alkylation catalyst descends to some extent, and its isopropyl benzene selectivity (in propyl group) is 98.4%.[embodiment 15]
Appoint and get embodiment 1,2,3,4,5,6,7,8,9,10 pretreated benzene, inlet amount is 60 Grams Per Hours, the diethylbenzene inlet amount is 6 Grams Per Hours, under 230 ℃ of temperature of reaction, reaction pressure 3.0MPa, continuously by the alkylation reactor that 20 gram silica alumina ratios are 28 β zeolite alkylated catalyst is housed, investigated through 1000 hours, the performance of alkylation catalyst does not descend, its diethylbenzene transformation efficiency maintains more than 92% always, ethylbenzene selectivity does not change about 99% substantially.[comparative example 5]
Get without pretreated fresh benzene, according to each step and the condition of the test of embodiment 15, after investigating through 800 hours, the performance of alkylation catalyst descends to some extent, its diethylbenzene transformation efficiency is since 92% decline, but ethylbenzene selectivity substantially changes about 99%.
Claims (10)
1, a kind of pre-treatment method for aromatic hydrocarbon may further comprise the steps:
A) aroamtic hydrocarbon raw material is 0～300 ℃ by loading the bed of pretreating agent in temperature, is 0～6.0MPa in gauge pressure pressure, and the aroamtic hydrocarbon raw material air speed is 0.1～1000 hour
-1Handle under the condition;
B) used pretreating agent comprises following component by weight percentage: (1) 10～100% h-type zeolite, (2) 0～90% aluminium or the oxide compound of silicon.
2,, it is characterized in that temperature is 60～270 ℃ according to the described pre-treatment method for aromatic hydrocarbon of claim 1.
3,, it is characterized in that in gauge pressure pressure be 0.3～5.2MPa according to the described pre-treatment method for aromatic hydrocarbon of claim 1.
4,, it is characterized in that the aroamtic hydrocarbon raw material air speed is 1～500 hour according to the described pre-treatment method for aromatic hydrocarbon of claim 1
-1
5,, it is characterized in that the amount that pretreating agent comprises h-type zeolite by weight percentage is 30～95% according to the described pre-treatment method for aromatic hydrocarbon of claim 1.
6,, it is characterized in that the h-type zeolite of used pretreating agent is selected from ZSM-5, ZSM-8, ZSM-11, ZSM-12, ZSM-22, ZSM-33, L zeolite, β zeolite, MCM-22, MCM-36, MCM-49, MCM-51, MCM-56, chabazite, mordenite or faujusite and stray crystal mixture thereof according to the described pre-treatment method for aromatic hydrocarbon of claim 1.
According to the described pre-treatment method for aromatic hydrocarbon of claim 1, it is characterized in that by weight percentage that 7, load is selected from least a metal or the oxide compound in nickel, palladium or the platinum on the h-type zeolite, its consumption is 0.001～5.0%.
According to the described pre-treatment method for aromatic hydrocarbon of claim 7, it is characterized in that by weight percentage that 8, load is selected from least a metal or the oxide compound in nickel, palladium or the platinum on the h-type zeolite, its consumption is 0.1～4.1%.
9, according to the described pre-treatment method for aromatic hydrocarbon of claim 7, it is characterized in that by weight percentage, on the h-type zeolite also load be selected from least a metal or oxide compound in gallium, zinc, copper, silver, cobalt, rhodium or the iridium, its consumption is 0.01～5%.
10, according to the described pre-treatment method for aromatic hydrocarbon of claim 9, it is characterized in that by weight percentage, on the h-type zeolite also load be selected from least a metal or oxide compound in gallium, zinc, copper, silver, cobalt, rhodium or the iridium, its consumption is 0.1～1.0%.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB01105848XA CN1166598C (en) | 2001-04-04 | 2001-04-04 | Pre-treatment method for aromatic hydrocarbon |
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| CNB01105848XA CN1166598C (en) | 2001-04-04 | 2001-04-04 | Pre-treatment method for aromatic hydrocarbon |
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| CN1377866A true CN1377866A (en) | 2002-11-06 |
| CN1166598C CN1166598C (en) | 2004-09-15 |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114436755A (en) * | 2020-10-19 | 2022-05-06 | 中国石油化工股份有限公司 | Optimization method of aromatic hydrocarbon transalkylation reaction raw material, aromatic hydrocarbon transalkylation reaction method and device |
| CN114456035A (en) * | 2020-10-21 | 2022-05-10 | 中国石油化工股份有限公司 | Aromatic hydrocarbon transalkylation method and system |
-
2001
- 2001-04-04 CN CNB01105848XA patent/CN1166598C/en not_active Expired - Lifetime
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114436755A (en) * | 2020-10-19 | 2022-05-06 | 中国石油化工股份有限公司 | Optimization method of aromatic hydrocarbon transalkylation reaction raw material, aromatic hydrocarbon transalkylation reaction method and device |
| CN114456035A (en) * | 2020-10-21 | 2022-05-10 | 中国石油化工股份有限公司 | Aromatic hydrocarbon transalkylation method and system |
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