CN1043421C - Process for preparing p-methyl ethyl benzene by reaction of dilute ethylene and toluene - Google Patents
Process for preparing p-methyl ethyl benzene by reaction of dilute ethylene and toluene Download PDFInfo
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- CN1043421C CN1043421C CN93115961A CN93115961A CN1043421C CN 1043421 C CN1043421 C CN 1043421C CN 93115961 A CN93115961 A CN 93115961A CN 93115961 A CN93115961 A CN 93115961A CN 1043421 C CN1043421 C CN 1043421C
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- toluene
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- ethyl benzene
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- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 title claims abstract description 174
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 title claims abstract description 42
- 238000006243 chemical reaction Methods 0.000 title claims abstract description 36
- 239000005977 Ethylene Substances 0.000 title claims abstract description 17
- 238000004519 manufacturing process Methods 0.000 title abstract description 3
- JRLPEMVDPFPYPJ-UHFFFAOYSA-N 1-ethyl-4-methylbenzene Chemical compound CCC1=CC=C(C)C=C1 JRLPEMVDPFPYPJ-UHFFFAOYSA-N 0.000 title abstract 5
- HYFLWBNQFMXCPA-UHFFFAOYSA-N 1-ethyl-2-methylbenzene Chemical compound CCC1=CC=CC=C1C HYFLWBNQFMXCPA-UHFFFAOYSA-N 0.000 claims abstract description 33
- YNQLUTRBYVCPMQ-UHFFFAOYSA-N Ethylbenzene Chemical compound CCC1=CC=CC=C1 YNQLUTRBYVCPMQ-UHFFFAOYSA-N 0.000 claims abstract description 28
- CTQNGGLPUBDAKN-UHFFFAOYSA-N O-Xylene Chemical compound CC1=CC=CC=C1C CTQNGGLPUBDAKN-UHFFFAOYSA-N 0.000 claims abstract description 27
- 239000003795 chemical substances by application Substances 0.000 claims abstract description 26
- 150000004945 aromatic hydrocarbons Chemical class 0.000 claims abstract description 12
- 239000003054 catalyst Substances 0.000 claims abstract description 9
- 238000000034 method Methods 0.000 claims abstract description 9
- 230000008569 process Effects 0.000 claims abstract description 9
- 239000000203 mixture Substances 0.000 claims abstract description 7
- 239000002994 raw material Substances 0.000 claims abstract description 7
- 238000011084 recovery Methods 0.000 claims abstract description 6
- 230000009471 action Effects 0.000 claims abstract description 3
- 238000010521 absorption reaction Methods 0.000 claims description 37
- 239000000463 material Substances 0.000 claims description 22
- 238000005804 alkylation reaction Methods 0.000 claims description 18
- 238000003672 processing method Methods 0.000 claims description 17
- 230000029936 alkylation Effects 0.000 claims description 8
- 239000007788 liquid Substances 0.000 claims description 8
- 238000009835 boiling Methods 0.000 claims description 5
- 239000006227 byproduct Substances 0.000 claims description 5
- 239000003381 stabilizer Substances 0.000 claims description 4
- 238000000605 extraction Methods 0.000 claims description 3
- -1 methyl-ethyl Chemical group 0.000 claims description 3
- 238000002156 mixing Methods 0.000 claims description 3
- 239000000758 substrate Substances 0.000 claims description 3
- 241000282326 Felis catus Species 0.000 claims description 2
- 230000004888 barrier function Effects 0.000 claims description 2
- 230000003197 catalytic effect Effects 0.000 claims description 2
- 230000018044 dehydration Effects 0.000 claims description 2
- 238000006297 dehydration reaction Methods 0.000 claims description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 2
- 238000004523 catalytic cracking Methods 0.000 abstract description 3
- 239000012535 impurity Substances 0.000 abstract description 3
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 abstract description 2
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 abstract description 2
- 238000007670 refining Methods 0.000 abstract description 2
- 230000002745 absorbent Effects 0.000 abstract 1
- 239000002250 absorbent Substances 0.000 abstract 1
- 230000008020 evaporation Effects 0.000 abstract 1
- 238000001704 evaporation Methods 0.000 abstract 1
- 239000008096 xylene Substances 0.000 abstract 1
- 238000005516 engineering process Methods 0.000 description 4
- 150000001336 alkenes Chemical class 0.000 description 3
- 125000003118 aryl group Chemical group 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 230000009467 reduction Effects 0.000 description 3
- NLNPTKKKNZYFGY-UHFFFAOYSA-N 1-ethyl-2-methylbenzene Chemical compound CCC1=CC=CC=C1C.CCC1=CC=CC=C1C NLNPTKKKNZYFGY-UHFFFAOYSA-N 0.000 description 2
- 239000000284 extract Substances 0.000 description 2
- 230000009183 running Effects 0.000 description 2
- PRBXPAHXMGDVNQ-UHFFFAOYSA-N 2-[2-(2-hydroxyethoxy)ethoxy]acetic acid Chemical compound OCCOCCOCC(O)=O PRBXPAHXMGDVNQ-UHFFFAOYSA-N 0.000 description 1
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 1
- 229910021536 Zeolite Inorganic materials 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 239000012071 phase Substances 0.000 description 1
- 239000004033 plastic Substances 0.000 description 1
- 229920003023 plastic Polymers 0.000 description 1
- 229920000314 poly p-methyl styrene Polymers 0.000 description 1
- 230000002035 prolonged effect Effects 0.000 description 1
- 230000011218 segmentation Effects 0.000 description 1
- 230000035939 shock Effects 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- 150000003738 xylenes Chemical class 0.000 description 1
- 239000010457 zeolite Substances 0.000 description 1
Images
Classifications
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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
- 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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- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The present invention relates to a technological process for preparing p-methyl ethyl benzene by reaction of dilute ethylene and toluene, including hydrocarbonylation reaction, aromatic hydrocarbon recovery, p-methyl ethyl benzene evaporation, xylene removal and ethyl benzene several portions, and is characterized by that under the action of catalyst the dilute ethylene can directly adopt catalytic cracking dry gas of oil refinery as raw material, and has no need of pre-refining to remove H2S、O2、CO2CO and a small amount of propylene and other impurities directly enter a reactor to react with toluene, a mixture of polyalkylbenzene and the like in the reaction is used as an absorbent, aromatic hydrocarbon in tail gas is recovered, pressurization is not needed in the reaction process, raw material dilute ethylene is used as a condensing agent to enter the reactor in a segmented mode, reaction heat can be taken away in a segmented mode, and the reaction temperature is controlled.
The process has high ethylene conversion rate, the selectivity of the ethylene to generate the p-methyl ethylbenzene reaches 90-95%, the p-methyl ethylbenzene/(p + m) methyl ethylbenzene reaches 90%, and the recovery rate of the aromatic hydrocarbon in the tail gas reaches 99%.
Description
The present invention relates to a kind of use ethene and toluene reaction, particularly react the processing method of producing methyl-ethyl benzene with low-concentration ethane and toluene.
Methyl-ethyl benzene had in light weight, characteristics such as softening temperature is high, radiation-cross-linkable, it is the important source material of producing poly-p-methylstyrene series plastics, this technology is subjected to the extensive attention of various countries, at present, U.S. Mobil company is existing to produce the methyl-ethyl benzene Technology with ethene and toluene reaction, but purity height to the ethene requirement, must be more than 99%, required equipment is many, the technology more complicated, power consumption is high, and investment is big, does not find to react the processing method of producing methyl-ethyl benzene with rare ethene and toluene through international online retrieval.
The objective of the invention is to study rare ethene of a kind of usefulness and toluene and react the processing method of production methyl-ethyl benzene.
Accompanying drawing is that the process flow diagram to methyl-ethyl benzene is produced in rare ethene and toluene reaction.
The process to methyl-ethyl benzene is produced in the rare ethene of the present invention and toluene reaction, comprise alkylation reaction, aromatic recovery, methyl-ethyl benzene is steamed, take off dimethylbenzene, several parts of ethylbenzene form, the characteristics of this process are: alkene ethene enters stable can 35 by pipeline 16, behind tank 35 interior dehydration condensate drains, measure respectively through pipeline 16 ' minute three parts or four parts and to be sent to first of reactor 1, two, three or four sections entrance A, B, C or D, toluene is to steam the circulation toluene that tower 11 overhead line 30 send by the fresh toluene of pipeline 26 and toluene to mix, after pipeline 31 and heat exchanger 3 heat exchange, enter toluene heating furnace 5, be heated to 440---480 ℃, first paragraph entrance A from reactor 1 top adds again, the rare ethene that is added to reactor 1 first paragraph is mixed with the hot toluene of gas phase, rare ethene is heated to 330---and 370 ℃, under the effect of catalyst, rare ethene and toluene carry out alkylation reaction generate contain a methyl-ethyl benzene to methyl-ethyl benzene, reaction temperature is 290---450 ℃, pressure 0.4---2.5MPa, toluene is 2.5 with the ethylene molecule ratio---10, and weight ethylene air speed 0.2---1.5h-1。
Alkene and toluene reaction are thermopositive reaction, and after material came out from 1 first section beds of reactor, material and bed temperature just were upgraded to 390---430 ℃; Material mixed with rare ethene of second section inlet B before entering second section beds, and making the population temperature is 330---and 370 ℃, all the other each section reactions are the same.Through remaining ethene in the material of the 3rd section (or the 4th section) catalyst bed reaction four sections (or the 5th sections) almost with the toluene total overall reaction.
Reactor 1 outlet at bottom temperature is 390---430 ℃, the material of alkylation reaction is by pipeline 18 or 18 ' or 18 " ' or 18 ", successively through interchanger 4 and tower 10 bottom material heat exchange and interchanger 3 and the heat exchange of raw material toluene, temperature is by 390---and 430 ℃ drop to about 180 ℃, except that reaction end gas, all the other all are condensed and are liquid phase.Enter water cooler 2 then, temperature of charge drops to 40---and 60 ℃, enter first grade absorption tower 7 again from the bottom, alkylation liquid through oil-gas separator 7 ', the reaction end gas of separating from tower 7, with from contain a methyl-ethyl benzene methyl-ethyl benzene is steamed tower 13 bottom line 27 and contain raffinate etc. mixture be reverse by the absorption agent polyalkylbenzene that tower 7 tops enter and contact, after aromatic hydrocarbons such as toluene were absorbed, tail gas entered the high pressure gas pipe network from tower 7 overhead line 32; The absorption agent that has absorbed aromatic hydrocarbons such as toluene enters two-level absorption tower 8 from tower 7 bottom tube lines 19 together with alkylation liquid, be dissolved in the gas in alkylation liquid and the absorption agent, the absorption agent of going into tower 8 jackings in tower 8 (the same absorption tower of originating) carries out reverse the contact, light component from stabilizer tower 10 tops also contacts with absorption agent is reverse simultaneously, after trace toluene is absorbed once more, tail gas is sent as process furnace fuel from tower 8 napex pipelines 33, the temperature on absorption tower is 10---100 ℃, absorption pressure is 0.1---1.0MPa, and agent gas volume ratio (V) 0.0001---0.06.Absorption agent and alkylation liquid from tower 8 through pipeline 19 ' and interchanger 9 send into stabilizer tower 10, tower 10 top temperature 80---100 ℃, end temperature 140---200 ℃, pressure 0.1---0.6MPa, thermal source is made with thermal barrier in tower 10 bottoms, steam the light component of a part, return two-level absorption tower 8 bottoms through pipeline 34, tower 10 substrate material go toluene to steam tower 11 by self pressure through pipeline 20, steam the circulation toluene that tower 11 tops steam from toluene, it is part of raw materials, tower 11 top temperature 95---130 ℃, end temperature 150---185 ℃, pressure 0.1---0.4MPa, steam tower 11 middle and upper parts at toluene, offer a pipeline 21, extract 10 out---35% dimethylbenzene, the ethylbenzene fraction is sent into and is taken off dimethylbenzene, ethylbenzene tower 12, this cat head temperature 130---160 ℃, end temperature 230---250 ℃, pressure 0.1---0.4MPa.From by product carrying devices such as tower 12 top separating dimethyl benzenes, ethylbenzene; The bottoms material is through reboiler 12 ' steam light constituents such as dimethylbenzene, ethylbenzene, extracts the mixing of materials with 11 ends of tower out, through pipeline 23 send into contain a methyl-ethyl benzene methyl-ethyl benzene is steamed tower 13.What contain a methyl-ethyl benzene steams tower 13 top temperature 130 to methyl-ethyl benzene---and 180 ℃, end temperature 210---270 ℃, pressure 0.06---0.4MPa, 13 ends of tower,, all material was a part of through reboiler 13 ' extraction, enter one through pipeline 27, two-level absorption tower 7,8, recycle as absorption agent, another partly enters and takes off polyalkylbenzene tower 14, these tower 14 top temperature 140---180 ℃, end temperature 200---270 ℃, pressure 0.04---0.2MPa goes out device from the isolated polyalkylbenzene in tower 14 tops, at the bottom of tower, isolate high boiling mixture through pipeline 29 carrying devices, as fcc raw material or diesel component.
The used rare ethylene raw of processing method of the present invention can directly be used the refinery catalytic cracked dry gas, does not need to remove H
2S, O
2, CO
2, impurity such as CO and a small amount of propylene pre-refining processing.
Processing method of the present invention has adopted ET3228 zeolite catalyst (application number 89105098,1).
The alkylation reaction device of processing method of the present invention is the fixed bed that multistage changes, totally five sections, during entry into service with first section to the 4th section, when current four sections catalyst activity reduction arrive to a certain degree, again with in the 5th section incision system with preceding four sections runnings.
Process using of the present invention the reaction in by product polyalkylbenzene and high boiling material make absorption agent.
Processing method of the present invention has following advantage:
1, with rare ethene and toluene reaction, produce methyl-ethyl benzene, pressure is lower, as participating in reaction as rare ethylene raw with plant catalytic cracking dry gas, then need not pressurize, can save gas booster compressor and energy consumption, produce the process matched therewith that methyl-ethyl benzene is just become catalytic cracking.
2, in reaction process, rare ethene is again the cold shock agent, the heat of output when reacting for it is constantly taken away, rare ethene is that segmentation adds reactor, be that the thermal material that comes out of the preceding paragraph is before entering next section beds, first and rare ethene mixes, thereby reduction temperature of charge, sectional feeding is not only taken reaction heat away, temperature of reactor is evenly distributed, and the may command temperature rise has improved the molecular ratio of each section toluene and alkene simultaneously less than 60 ℃, and then the selectivity of the process of raising, ethene is generated methyl-ethyl benzene (containing a methyl-ethyl benzene) selectivity is reached 90---95%, methyl-ethyl benzene/(right+) methyl-ethyl benzene is reached about 90%, conversion of ethylene reaches 50---and 85%, prolonged catalyst life, the one way life-span reached more than 15 days.
3, the fixed reactor of alkylation reaction device for changing, totally five sections, during entry into service with first to fourth section, when current four sections catalyst activity reduction arrive to a certain degree, again with in the 5th section incision system with preceding four sections runnings, like this, can prolong the operational use time of catalyzer.
4, owing to adopted a part of by product polyalkylbenzene in the reaction and high boiling material, the aromatic hydrocarbons such as small amount of toluene in the tail gas can be reclaimed more than 98%, reduced the waste of aromatic hydrocarbons, reduce toluene consumption as absorption agent.
5, processing method of the present invention has adopted toluene to steam the tower middle and upper part and has offered a pipeline, extraction dimethylbenzene, ethylbenzene fraction enter and take off dimethylbenzene, ethylbenzene tower, separating dimethyl benzene, ethyl benzene mixtures, to reduce dimethylbenzene, ethylbenzene accumulation volume, can guarantee to contain the purity to methyl-ethyl benzene of a methyl-ethyl benzene, and reduce the impurity generation.
Lift several examples according to above-mentioned processing method:
Example 1, with the refinery catalysis drying gas through the metering average mark send into one, two, three sections hot toluene vapor mixing that enter with reactor head of reactor for three parts, under the ET3228 catalyst action, react 400 ℃ of temperature of reaction, pressure 0.5MPa, toluene and ethylene molecule be than 5/1, weight ethylene air speed 0.4h
-1, conversion of ethylene 72.42%, ethene generates the methyl-ethyl benzene selectivity 95.18% of (containing a methyl-ethyl benzene), and to methyl-ethyl benzene/(right+) methyl-ethyl benzene 91.74%.
Example 2, the alkylation reaction tail gas of this processing method enters from the bottom, absorption tower after coming out from oil-gas separator, 50 ℃ of population temperatures, absorption tower pressure 0.55MPa, the tower inner filling material, absorption agent adopts triethylene glycol ether, enter by tower top, fully contact with reaction end gas at Ta Nei, aromatic hydrocarbons such as the toluene in the tail gas are stayed in the absorption agent, when agent gas volume ratio 0.0018 (V), recycle ratio 0.136, gas space velocity 2.88h
-1The time, aromatic recovery rate 88.22% (W) such as toluene in the tail gas.
Example 3 in technology of the present invention, adopts polyalkylbenzene and height to boil mixture as absorption agent, reclaim in the tail gas aromatic hydrocarbons such as toluene, enter, fully contact with reaction end gas at Ta Nei by top, absorption tower, aromatic hydrocarbons such as the toluene in the tail gas are stayed in the absorption agent, and aromatic recovery rates such as toluene are more than 99%.
Claims (4)
1, the processing method to methyl-ethyl benzene is produced in the reaction of a kind of rare ethene and toluene, comprises alkylation reaction.Benzene-toluene-xylene recovery, methyl-ethyl benzene is steamed, takes off several parts of dimethylbenzene, ethylbenzene form, the feature of this processing method is:
A), rare ethene enters stable can (35) by pipeline (16), in jar (35) dehydration condensate drain after, divide three parts or four parts to measure respectively through pipeline (16 ') and be sent to first of reactor (1), two, three or four sections inlets (A), (B), (C) or (D), toluene is that the fresh toluene that come by pipeline (26) and toluene steam the circulation toluene that tower (11) overhead line (30) sends and mixes, after pipeline (31) and interchanger (3) heat exchange, enter toluene process furnace (5), be heated to 440---480 ℃, first section inlet (A) from reactor (1) top adds again, the rare ethene that is added to (1) first section of reactor is mixed with the hot toluene of gas phase, rare ethene is heated to 330---and 370 ℃, under catalyst action, rare ethene and toluene carry out alkylation reaction, generation contain a methyl-ethyl benzene to methyl-ethyl benzene, temperature of reaction is 290---450 ℃, pressure 0.4---2.5MPa, toluene and ethylene molecule are than 2.5---and 10, weight ethylene air speed 0.2---1.5h
-1
B), reactor (1) outlet at bottom temperature 390---430 ℃, the material of alkylation reaction is by pipeline (18) or (18 ') or (18 " ') or (18 "), successively through material heat exchange and the interchanger (3) and raw material toluene heat exchange of interchanger (4) with tower (10) bottom, temperature is by 390---and 430 ℃ drop to about 180 ℃, enter water cooler (2) then, temperature of charge drops to 40---and 60 ℃, enter first grade absorption tower (7) again from the bottom, alkylation liquid is through oil-gas separator (7 '), the reaction end gas of separating from tower (7), and methyl-ethyl benzene is steamed from what contain a methyl-ethyl benzene tower (13) bottom line (27) comes, and the absorption agent polyalkylbenzene that is entered by tower (7) top contains the reverse contacts of mixture such as raffinate, after aromatic hydrocarbons such as toluene were absorbed, tail gas entered the high pressure gas pipe network from tower (7) overhead line (32); The absorption agent that has absorbed aromatic hydrocarbons such as toluene enters two-level absorption tower (8) from tower (7) bottom tube line (19) together with alkylation liquid, be dissolved in the gas in alkylation liquid and the absorption agent, the absorption agent of going into tower (8) jacking in tower (8) carries out reverse the contact, light component from stabilizer tower (10) napex also contacts with absorption agent is reverse simultaneously, the temperature 10 on absorption tower---100 ℃, absorption pressure is 0.1---1.0MPa, and agent gas volume ratio (V) 0.0001---0.06;
C), absorption agent and alkylation liquid are sent into stabilizer tower (10) from tower (8) through pipeline (19 ') and interchanger (9), tower (10) top temperature 80---100 ℃, end temperature 140---200 ℃, pressure 0.1---0.6MPa, thermal source is made with thermal barrier in tower (10) bottom, steam the light component of a part, return two-level absorption tower (8) bottom through pipeline (34), tower (10) substrate material removes tower (11) through pipeline (20);
D), to steam the circulation toluene that tower (11) top steams from toluene be the part of raw material toluene, toluene steams tower (11) top temperature 95---130 ℃, end temperature 150---185 ℃, pressure 0.1---0.4MPa;
E), steam tower (11) middle and upper part at toluene and offer a pipeline (21),---35% dimethylbenzene, ethylbenzene fraction are sent into and are taken off 250 ℃ of dimethylbenzene, ethylbenzene tower (12), this cat head temperature 130---160 ℃, end temperature 230---to extract 10 out, pressure 0.1---0.4MPa pushes up by product carrying devices such as isolated dimethylbenzene, ethylbenzene from tower (12); Tower (12) substrate material steams light component such as dimethylbenzene, ethylbenzene through reboiler (12 '), and the mixing of materials at the extraction and tower (11) end is sent into methyl-ethyl benzene is steamed tower (13);
What f), contain a methyl-ethyl benzene steams the top temperature 130 of tower (13) to methyl-ethyl benzene---and 180 ℃, end temperature 210---270 ℃, pressure 0.06---0.4MPa, tower (13) bottom material is extracted a part out through reboiler (13 '), through pipeline (27) enter I and II absorption tower (7), (8) recycle as absorption agent, another part enters and takes off polyalkylbenzene tower (14);
G) take off the top temperature 140 of polyalkylbenzene tower (14)---180 ℃, end temperature 200---270 ℃, pressure 0.04---0.2MPa goes out device from the isolated polyalkylbenzene in tower (14) top, isolates high boiling mixture through pipeline (29) carrying device at the bottom of tower.
2, according to the described processing method of claim 1, it is characterized in that rare ethylene raw that this processing method is used, can directly use the refinery catalytic cracked dry gas.
3,, it is characterized in that the fixed bed that alkylation reaction device (1) changes for multistage according to the described processing method of claim 1.
4,, it is characterized in that adopting by product polyalkylbenzene and the high boiling material in the reaction to make absorption agent according to the described processing method of claim 1.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN93115961A CN1043421C (en) | 1993-12-12 | 1993-12-12 | Process for preparing p-methyl ethyl benzene by reaction of dilute ethylene and toluene |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN93115961A CN1043421C (en) | 1993-12-12 | 1993-12-12 | Process for preparing p-methyl ethyl benzene by reaction of dilute ethylene and toluene |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1103637A CN1103637A (en) | 1995-06-14 |
| CN1043421C true CN1043421C (en) | 1999-05-19 |
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| CN93115961A Expired - Fee Related CN1043421C (en) | 1993-12-12 | 1993-12-12 | Process for preparing p-methyl ethyl benzene by reaction of dilute ethylene and toluene |
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Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1057988C (en) * | 1996-11-25 | 2000-11-01 | 中国科学院大连化学物理研究所 | Process for preparing aromatic hydrocarbon from catalytic cracking tail gas in absence of oxygen |
| CN1986502B (en) * | 2005-12-21 | 2011-06-15 | 中国科学院大连化学物理研究所 | Ethylene and toluene catalytically separating process for preparing methyl ethyl benzene |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4107224A (en) * | 1977-02-11 | 1978-08-15 | Mobil Oil Corporation | Manufacture of ethyl benzene |
| CN1051166A (en) * | 1990-12-18 | 1991-05-08 | 中国石油化工总公司 | The process of producing ethylbenzene by reacting dilute ethylene and benzene |
-
1993
- 1993-12-12 CN CN93115961A patent/CN1043421C/en not_active Expired - Fee Related
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4107224A (en) * | 1977-02-11 | 1978-08-15 | Mobil Oil Corporation | Manufacture of ethyl benzene |
| CN1051166A (en) * | 1990-12-18 | 1991-05-08 | 中国石油化工总公司 | The process of producing ethylbenzene by reacting dilute ethylene and benzene |
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| CN1103637A (en) | 1995-06-14 |
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