CN102464565B - Method for producing isopropylbenzene by using benzene and propylene - Google Patents
Method for producing isopropylbenzene by using benzene and propylene Download PDFInfo
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- CN102464565B CN102464565B CN201010551968.5A CN201010551968A CN102464565B CN 102464565 B CN102464565 B CN 102464565B CN 201010551968 A CN201010551968 A CN 201010551968A CN 102464565 B CN102464565 B CN 102464565B
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Abstract
The invention relates to a method for producing isopropylbenzene by using benzene and propylene and mainly solves the problem of high content of n-propylbenzene existing in an isopropylbenzene product of the prior art. The method better solves the problem and can be applied to the industrial production of isopropylbenzene by adopting the technical scheme which comprises the following steps of: (1) a first stream of benzene material flow 12 and propylene enter an alkylation reactor to react, thereby a material flow 19 comprising the benzene, propylene, isopropylbenzene and polyisopropylbenzene is obtained; (b) the material flow 19 is separated to obtain material flow 23 containing polyisopropylbenzene; (c) after the material flow 23 is separated by a rectifying tower, material flow 13 is obtained at the tower top, and material flow 14 is obtained in the middle part of the tower; (d) a second stream of material flow 10 and the material flow 13 enter a first a first alkyl group transfer reaction zone for carrying out alkyl group transfer reaction to obtain material flow 21; and a third stream of material flow 11 and the material flow 14 enter a second alkyl group transfer reaction zone for carrying out alkyl group transfer reaction to obtain material flow 22; and (e) the material flow 21 and the material flow 22 enter the follow-up refining process, thereby the isopropylbenzene product is obtained.
Description
Technical field
The present invention relates to a kind of method by benzene and production of propylene isopropyl benzene.
Background technology
Isopropyl benzene is a kind of important Organic Chemicals, is the main intermediate compound of producing phenol, acetone and alpha-methyl styrene.Industrial isopropyl benzene be by propylene and benzene alkylated reaction prepare, its by product is mainly polyisopropylbenzene.Just announce under an acidic catalyst exists as far back as UOP in 1945, the method (SPA method) of preparing isopropyl benzene with the reaction of propylene and benzene (USP2382318), SPA method is taking solid phosphoric acid as alkylation catalyst, because solid phosphoric acid can not catalysis transalkylation reaction, so there is no transalkylation part in technical process.Therefore, SPA method can only be moved under high benzene alkene mol ratio (5～7) condition, and the yield of its isopropyl benzene is only 95% left and right.Last century the eighties, Monsanto company develops with AlCl
3for the isopropyl benzene production technique of alkylation catalyst, and realize industrial application.Due to AlCl
3equally can not catalysis transalkylation reaction, therefore, with AlCl
3it is still lower aspect the yield of isopropyl benzene that method is produced isopropyl benzene, also has serious pollution problem and corrosion of equipment problem simultaneously.
In the nineties in last century, (US4992606, US5362697, US5453554, US5522984, US5672799, US6162416, the US6051521) companies such as Dow, CD Tech, Mobil-Badger, Enichem and UOP have announced in succession taking micro-pore zeolite as catalyzer, have the fixed-bed process flow process of transalkylation ability.In the prior art, first benzene and propylene carry out alkylated reaction in alkylation reaction device, the polysubstituted isopropyl benzene that alkylated reaction generates is after distillation system separates, and polysubstituted isopropyl benzene enters single bed transalkylation reactor after mixing with benzene again carries out transalkylation reaction.
In the alkylation process of benzene and propylene, the activity of acidic zeolite catalyst, stability and foreign matter content depend on operational condition to a great extent, as benzene alkene ratio, air speed and temperature of reaction.The impact of benzene alkene comparison catalyst stability is particularly serious, in order to improve the reaction stability of catalyzer, should reduce as far as possible the content of alkylation reactor inner propene.Therefore, in actual industrial production, propylene has all adopted the method for sectional feeding, and the pattern of sectional feeding is also conducive to control bed temperature and carries out in suitable interval.
In the transalkylation reaction of benzene and polyisopropylbenzene, the composition of mol ratio, raw material air speed and the polyisopropylbenzene raw material of benzene and polyisopropylbenzene all can have a strong impact on the transformation efficiency of polyisopropylbenzene and the growing amount of impurity n-proplbenzene, the transalkylation reaction of polyisopropylbenzene tends to produce more impurity n-proplbenzene, and this can the serious quality that reduces product isopropyl benzene.Therefore, by process optimization, improve polyisopropylbenzene transformation efficiency, reduce the n-proplbenzene that transalkylation generates, significant to enhancing productivity, improving the quality of products.
Summary of the invention
Technical problem to be solved by this invention is that prior art exists the higher problem of n-proplbenzene content in transalkylated product, and a kind of new method by benzene and production of propylene isopropyl benzene is provided.The method has significantly reduced n-proplbenzene content, has improved the quality of product isopropyl benzene.
For solving the problems of the technologies described above, the technical solution used in the present invention is as follows: a kind of method by benzene and production of propylene isopropyl benzene, comprises the following steps:
A) first burst of benzene logistics 12 and propylene enter alkylation reactor and react, and obtain comprising the logistics 19 of benzene, propane, isopropyl benzene and polyisopropylbenzene;
B) logistics 19, successively by depropanizing tower, benzene rectifying tower and isopropyl benzene rectifying tower, separates and obtains propane logistics 15, benzene logistics 9, isopropyl benzene logistics 16 and the logistics 23 containing polyisopropylbenzene;
C) logistics 23 enters polyisopropylbenzene rectifying tower, and after rectifying separation, tower top obtains logistics 13, and tower middle part obtains logistics 14, and tower reactor obtains the heavy constituent logistics 17 containing tar, and logistics 17 enters follow-up flow process; In logistics 13, diisopropylbenzene(DIPB) content is at least greater than 95 % by weight; In logistics 14, tri-isopropyl benzene content is at least greater than 0.5 % by weight;
D) second burst of benzene logistics 10 and logistics 13 enter the first transalkylation reactor, contact and carry out transalkylation reaction with catalyzer, obtain logistics 21; The 3rd burst of benzene logistics 11 and logistics 14 enter the second transalkylation reactor, contact and carry out transalkylation reaction with catalyzer, obtain logistics 22;
E) logistics 21 and logistics 22 enter follow-up rectification flow, obtain product isopropyl benzene.
In technique scheme, in logistics 13, diisopropylbenzene(DIPB) content preferable range is 96～100 % by weight.In logistics 14, tri-isopropyl benzene content preferable range is 1～50 % by weight.
In technique scheme, alkylation reactor reaction conditions preferable range is: the mol ratio of first burst of benzene logistics and propylene is 1～10, and temperature of reaction is 110～190 DEG C, and reaction pressure is 1.0～4.0MPa, and liquid phase air speed is 1～10 hour-1.Alkylation catalyst preferred version is for being selected from Y zeolite, Beta zeolite, mordenite or MCM-22.
In technique scheme, the first transalkylation reactor temperature of reaction preferable range is 130～190 DEG C; Reaction pressure preferable range is 1.0～3.0MPa; Second burst of benzene logistics 10 is 0.3～5 with the weight ratio preferable range of logistics 13, and more preferably scope is 0.7～3; Liquid phase air speed preferable range is 0.5～10 hour
-1, more preferably scope is 1～6 hour
-1.Transalkylation catalyst preferred version is for being selected from Y zeolite, Beta zeolite, mordenite, SHY-1, SHY-2 or MCM-22.
In technique scheme, the second transalkylation reactor temperature of reaction preferable range is 150～210 DEG C; Reaction pressure preferable range is 1.0～3.0MPa; The 3rd burst of benzene logistics 11 is 0.3～5 with the weight ratio preferable range of logistics 14, and more preferably scope is 0.7～3; Liquid phase air speed preferable range is 0.5～10 hour
-1, more preferably scope is 1～6 hour
-1.Transalkylation catalyst preferred version is for being selected from Y zeolite, Beta zeolite, mordenite, SHY-1, SHY-2 or MCM-22.
In the inventive method, the first transalkylation reactor and the second transalkylation reactor are all fixed-bed reactor, and wherein the catalyzer of filling is selected from Y zeolite, Beta zeolite, mordenite, SHY-1, SHY-2 or MCM-22.Wherein SHY-1 can be according to disclosed method preparation in CN200410066636.2, and SHY-2 can be according to disclosed method preparation in CN200610029979.0.
In the inventive method, the operational condition of depropanizing tower is: 40～80 DEG C of tower top temperatures, 210～280 DEG C of tower reactor temperature, working pressure 1.3～1.8MPa.The operational condition of benzene rectifying tower is: 80～120 DEG C of tower top temperatures, 170～220 DEG C of tower reactor temperature, working pressure 0～0.3MPa.The operational condition of isopropyl benzene rectifying tower is: 150～160 DEG C of tower top temperatures, 200～250 DEG C of tower reactor temperature, working pressure 0～0.03MPa.Polysubstituted isopropyl benzene tower operational condition is: tower top temperature is 120～160 DEG C, and tower reactor temperature is 190～250 DEG C, working pressure-300～0kPa.
In the inventive method, participating in the benzene of reaction, comprise first burst of benzene logistics 12, second burst of benzene logistics 10 and the 3rd burst of benzene logistics 11, can be benzene or its mixture that fresh benzene, benzene rectifying tower reclaim.
In the inventive method, the product (logistics 24 and logistics 25) after transalkylation reaction enters successively follow-up benzene rectifying tower, isopropyl benzene rectifying tower and polyisopropylbenzene rectifying tower and refines, and obtains product isopropyl benzene.
The inventive method is cut polysubstituted isopropyl benzene through suitable rectifying, be separated into two lighter and heavier logistics of component, control diisopropylbenzene(DIPB) content in the logistics that component is lighter and be at least greater than 95 % by weight, control tri-isopropyl benzene content in the heavier logistics of component and be at least greater than 0.5 % by weight.Transalkylation reaction is carried out respectively in these two bursts of logistics, has significantly reduced the content of n-proplbenzene, in isopropyl benzene n-proplbenzene content minimum be only 360ppm, improved isopropyl benzene quality product, obtained good technique effect.
Brief description of the drawings
Fig. 1 is process flow diagram of the present invention.
In Fig. 1, 1 is alkylation reactor, 2 is the first transalkylation reactor, 3 is the second transalkylation reactor, 4 is depropanizing tower, 5 is benzene rectifying tower, 6 is isopropyl benzene rectifying tower, 7 is polyisopropylbenzene rectifying tower, 8 is fresh benzene, 9 heat up in a steamer column overhead logistics for benzin, 10 is the benzene (second strand of benzene) to the first transalkylation reactor, 11 is the benzene (the 3rd strand of benzene) to the second transalkylation reactor, 12 is the benzene (first strand of benzene) to alkylation reactor, 13 is the polyisopropylbenzene to the first transalkylation reactor, 14 is the polyisopropylbenzene to the second transalkylation reactor, 15 is propane, 16 is isopropyl benzene, 17 is polyisopropylbenzene tower bottom of rectifying tower liquid, 18 is propylene, 19 is alkylation reactor product, 20 is depropanizing tower tower bottoms, 21 is the first transalkylation reactor product stream, 22 is the second transalkylation reactor product stream.
In Fig. 1, fresh benzene 8 enters benzene rectifying tower 4, and after recycle benzene Hybrid Heating, is divided into three strands, is sent to respectively alkylation reactor and first, second transalkylation reactor.Benzene logistics 12 and propylene 18 enter alkylation reactor and react, and obtain comprising the logistics 19 of benzene, propane, isopropyl benzene and polyisopropylbenzene; Wherein propylene is that segmentation enters.Logistics 19, successively by depropanizing tower, benzene rectifying tower and isopropyl benzene rectifying tower, separates and obtains propane logistics 15, benzene logistics 9, isopropyl benzene logistics 16 and the logistics 23 containing polyisopropylbenzene.Logistics 23 enters polyisopropylbenzene rectifying tower, and after rectifying separation, tower top obtains logistics 13, and tower middle part obtains logistics 14, and tower reactor obtains the heavy constituent logistics 17 containing tar, and logistics 17 enters follow-up flow process.Second burst of benzene logistics 10 and logistics 13 enter the first transalkylation reactor, contact and carry out transalkylation reaction with catalyzer, obtain logistics 21.The 3rd burst of benzene logistics 11 and logistics 14 enter the second transalkylation reactor, contact and carry out transalkylation reaction with catalyzer, obtain logistics 22.Logistics 21 and logistics 22 enter benzene rectifying tower, isopropyl benzene rectifying tower and polyisopropylbenzene rectifying tower successively, after refining, obtain product isopropyl benzene.
Below by embodiment, the present invention is further elaborated.
Embodiment
[embodiment 1]
Press the technical process of Fig. 1, alkylation reactor beds is divided into four sections, is mounted with 200 grams of preformed catalysts containing MCM-22 zeolite, and every section is equipped with 50 grams, and propylene divides four section feedings.Alkylation reactor reaction conditions is: 135 DEG C of temperature of reaction, and reaction pressure 2.3MPa, enters benzene intake 780 Grams Per Hours of alkylation reactor, propylene intake 200 Grams Per Hours, every section is 50 Grams Per Hours.
The first transalkylation reactor loads 100 grams of preformed catalysts containing Beta zeolite, and second transalkylation reactor loads 50 grams of preformed catalysts containing MCM-22 zeolite.The reaction conditions of the first transalkylation reactor is: 150 DEG C of temperature of reaction, reaction pressure 1.2MPa, polyisopropylbenzene inlet amount (logistics 13) 100 Grams Per Hours, benzene input (logistics 10) 150 Grams Per Hours.Wherein, diisopropylbenzene(DIPB) content 98% in logistics 13.The reaction conditions of the second transalkylation reactor is: 185 DEG C of temperature of reaction, reaction pressure 1.4MPa, polyisopropylbenzene inlet amount (logistics 14) 80 Grams Per Hours, benzene input (logistics 11) 100 Grams Per Hours.Wherein, tri-isopropyl benzene content 10% in logistics 14.
The operational condition of depropanizing tower is: 45 DEG C of tower top temperatures, 230 DEG C of tower reactor temperature, working pressure 2.50MPa.
The operational condition of benzene rectifying tower is: 87 DEG C of tower top temperatures, 185 DEG C of tower reactor temperature, working pressure 0.02MPa.
The operational condition of isopropyl benzene rectifying tower is: 154 DEG C of tower top temperatures, 220 DEG C of tower reactor temperature, working pressure 0.02MPa.
Polyisopropylbenzene rectifying tower operational condition is: 130 DEG C of tower top temperatures, 214 DEG C of tower reactor temperature, working pressure-90MPa.
Reaction result: isopropyl benzene productive rate 99.7%, isopropyl benzene purity 99.97%, n-proplbenzene content 210ppm in isopropyl benzene.
[embodiment 2]
With [embodiment 1], just alkylation reactor beds is divided into four sections, is mounted with 170 grams of preformed catalysts containing MCM-22 zeolite, and four sections are equipped with 35,40,45,50 grams successively, and propylene divides four section feedings.Alkylation reactor reaction conditions is: 140 DEG C of temperature of reaction, and reaction pressure 2.5MPa, enters benzene intake 600 Grams Per Hours of alkylation reactor, propylene intake 170 Grams Per Hours, four sections of amounts that pass into successively propylene are 35,40,45,50 Grams Per Hours.
The first transalkylation reactor loads 50 grams of preformed catalysts containing Beta zeolite, and the second transalkylation reactor loads 50 grams of preformed catalysts containing MCM-22 zeolite.The reaction conditions of the first transalkylation reactor is: 150 DEG C of temperature of reaction, reaction pressure 1.2MPa, polyisopropylbenzene inlet amount 70 Grams Per Hours, benzene input 140 Grams Per Hours.Wherein, diisopropylbenzene(DIPB) content 99% in logistics 13.The reaction conditions of the second transalkylation reactor is: 185 DEG C of temperature of reaction, reaction pressure 1.5MPa, polyisopropylbenzene inlet amount 100 Grams Per Hours, benzene input 100 Grams Per Hours.Wherein, tri-isopropyl benzene content 8% in logistics 14.
The operational condition of depropanizing tower is: 45 DEG C of tower top temperatures, 230 DEG C of tower reactor temperature, working pressure 2.50MPa.
The operational condition of benzene rectifying tower is: 87 DEG C of tower top temperatures, 185 DEG C of tower reactor temperature, working pressure 0.02MPa.
The operational condition of isopropyl benzene rectifying tower is: 154 DEG C of tower top temperatures, 220 DEG C of tower reactor temperature, working pressure 0.02MPa.
Polyisopropylbenzene rectifying tower operational condition is: 128 DEG C of tower top temperatures, 210 DEG C of tower reactor temperature, working pressure-120MPa.
Reaction result: isopropyl benzene productive rate 99.7%, isopropyl benzene purity 99.97%, n-proplbenzene content 240ppm in isopropyl benzene.
[embodiment 3]
With [embodiment 2], just alkylation reactor reaction conditions is: 135 DEG C of temperature of reaction, reaction pressure 2.5MPa, enters benzene intake 600 Grams Per Hours of alkylation reactor, propylene intake 120 Grams Per Hours.
The first transalkylation reactor loads 50 grams of preformed catalysts containing Beta zeolite, and second transalkylation reactor loads 50 grams of preformed catalysts containing MCM-56 zeolite.The reaction conditions of the first transalkylation reactor is: 148 DEG C of temperature of reaction, reaction pressure 1.1MPa, polyisopropylbenzene inlet amount 70 Grams Per Hours, benzene input 140 Grams Per Hours.Wherein, diisopropylbenzene(DIPB) content 98% in logistics 13.The reaction conditions of the second transalkylation reactor is: 170 DEG C of temperature of reaction, reaction pressure 1.5MPa, polyisopropylbenzene inlet amount 100 Grams Per Hours, benzene input 100 Grams Per Hours.Wherein, tri-isopropyl benzene content 5% in logistics 14.
Reaction result: isopropyl benzene productive rate 99.7%, isopropyl benzene purity 99.97%, n-proplbenzene content 200ppm in isopropyl benzene.
[embodiment 4]
With [embodiment 1], just alkylation reactor beds is divided into four sections, be mounted with 160 grams of preformed catalysts containing SHY-1 zeolite (SHY-1 is according to disclosed method preparation in CN200410066636.2), four sections are equipped with 35,40,45,50 grams successively, and propylene divides four section feedings.Alkylation reactor reaction conditions is: 132 DEG C of temperature of reaction, and reaction pressure 2.5MPa, enters benzene intake 600 Grams Per Hours of alkylation reactor, propylene intake 150 Grams Per Hours, four sections of amounts that pass into successively propylene are 30,35,40,45 Grams Per Hours.
The first transalkylation reactor loads 50 grams of preformed catalysts containing Beta zeolite, and the second transalkylation reactor loads 50 grams of preformed catalysts containing SHY-2 zeolite.The reaction conditions of the first transalkylation reactor is: 150 DEG C of temperature of reaction, reaction pressure 1.2MPa, polyisopropylbenzene inlet amount 70 Grams Per Hours, benzene input 140 Grams Per Hours.Wherein, diisopropylbenzene(DIPB) content 99% in logistics 13.The reaction conditions of the second transalkylation reactor is: 180 DEG C of temperature of reaction, reaction pressure 1.5MPa, polyisopropylbenzene inlet amount 100 Grams Per Hours, benzene input 110 Grams Per Hours.Wherein, tri-isopropyl benzene content 12% in logistics 14.
The operational condition of depropanizing tower is: 43 DEG C of tower top temperatures, 225 DEG C of tower reactor temperature, working pressure 2.45MPa.
The operational condition of benzene rectifying tower is: 85 DEG C of tower top temperatures, 185 DEG C of tower reactor temperature, working pressure 0.02MPa.
The operational condition of isopropyl benzene rectifying tower is: 154 DEG C of tower top temperatures, 220 DEG C of tower reactor temperature, working pressure 0.02MPa.
Polyisopropylbenzene rectifying tower operational condition is: 130 DEG C of tower top temperatures, 213 DEG C of tower reactor temperature, working pressure-100MPa.
Reaction result: isopropyl benzene productive rate 99.7%, isopropyl benzene purity 99.97%, n-proplbenzene content 210ppm in isopropyl benzene.
[comparative example 1]
With [embodiment 1], just transalkylation part only has a reactor, and only draws logistics from polyisopropylbenzene rectifying tower tower top, and this logistics all enters transalkylation reactor.Transalkylation reaction zone is mounted with the preformed catalyst of 50 grams of Beta zeolites, 153 DEG C of temperature of reaction, reaction pressure 1.1MPa, benzene flow 100 Grams Per Hours, polysubstituted isopropyl benzene flow 80 Grams Per Hours, diisopropylbenzene(DIPB) content 96% in polysubstituted isopropyl benzene, successive reaction 5 days.
Reaction result: polyisopropylbenzene transformation efficiency only has 35%, n-proplbenzene content 560ppm in isopropyl benzene.
[comparative example 2]
With [comparative example 1], just transalkylation reaction zone is mounted with the preformed catalyst of 60 grams of MCM-22 zeolites, 185 DEG C of temperature of reaction, reaction pressure 1.5MPa, benzene flow 80 Grams Per Hours, polysubstituted isopropyl benzene flow 80 Grams Per Hours, diisopropylbenzene(DIPB) content 96% in polysubstituted isopropyl benzene, successive reaction 5 days.
Reaction result: polyisopropylbenzene transformation efficiency 55%, n-proplbenzene content 800ppm in isopropyl benzene.
[comparative example 3]
With [comparative example 1], just transalkylation reaction zone is mounted with the preformed catalyst of 60 grams of MCM-22 zeolites, 172 DEG C of temperature of reaction, reaction pressure 1.5MPa, benzene flow 100 Grams Per Hours, polysubstituted isopropyl benzene flow 80 Grams Per Hours, diisopropylbenzene(DIPB) content 96% in polysubstituted isopropyl benzene, successive reaction 5 days.
Reaction result: polyisopropylbenzene transformation efficiency 40%, n-proplbenzene content 630ppm in isopropyl benzene.
Claims (1)
1. by a method for benzene and production of propylene isopropyl benzene, comprise the following steps:
Fresh benzene enters benzene rectifying tower, and after recycle benzene Hybrid Heating, is divided into three strands, is sent to respectively alkylation reactor and first, second transalkylation reaction zone; First burst of benzene logistics and propylene enter alkylation reactor and react, and obtain comprising the logistics of benzene, propane, isopropyl benzene and polyisopropylbenzene, and wherein propylene is that segmentation enters; The above-mentioned logistics that comprises benzene, propane, isopropyl benzene and polyisopropylbenzene, successively by depropanizing tower, benzene rectifying tower and isopropyl benzene rectifying tower, separates and obtains propane logistics, benzene logistics, isopropyl benzene logistics and the logistics containing polyisopropylbenzene; Logistics containing polyisopropylbenzene enters polyisopropylbenzene rectifying tower, after rectifying separation, tower top obtains the polyisopropylbenzene logistics of the first transalkylation reaction zone, tower middle part obtains the polyisopropylbenzene of the second transalkylation reaction zone, tower reactor obtains the heavy constituent logistics containing tar, enters follow-up flow process containing the heavy constituent logistics of tar; The polyisopropylbenzene logistics of second burst of benzene logistics and the first transalkylation reaction zone enters the first transalkylation reaction zone, contacts and carries out transalkylation reaction with catalyzer, obtains the first transalkylation reaction zone product stream after reaction; The polyisopropylbenzene logistics of the 3rd burst of benzene logistics and the second transalkylation reaction zone enters the second transalkylation reaction zone, contacts and carries out transalkylation reaction with catalyzer, obtains the second transalkylation reaction zone product stream after reaction; Described the first transalkylation reaction zone product stream and the second transalkylation reaction zone product stream enter benzene rectifying tower, isopropyl benzene rectifying tower and polyisopropylbenzene rectifying tower successively, after refining, obtain product isopropyl benzene;
Described alkylation reactor beds is divided into four sections, is mounted with 170 grams of preformed catalysts containing MCM-22 zeolite, and four sections are equipped with 35,40,45,50 grams successively, and propylene divides four section feedings; Alkylation reactor reaction conditions is: 135 DEG C of temperature of reaction, reaction pressure 2.5MPa, enter first burst of benzene intake 600/ hour of alkylation reactor, propylene intake 120 Grams Per Hours, four sections of amounts that pass into successively propylene are 35,40,45,50 Grams Per Hours;
The first transalkylation reactor loads 50 grams of preformed catalysts containing Beta zeolite, and second transalkylation reactor loads 50 grams of preformed catalysts containing MCM-56 zeolite; The reaction conditions of the first transalkylation reactor is: 148 DEG C of temperature of reaction, reaction pressure 1.1MPa, polyisopropylbenzene inlet amount 70 Grams Per Hours, benzene input 140 Grams Per Hours; Wherein, diisopropylbenzene(DIPB) content 98% in logistics 13; The reaction conditions of the second transalkylation reactor is: 170 DEG C of temperature of reaction, reaction pressure 1.5MPa, polyisopropylbenzene inlet amount 100 Grams Per Hours, benzene input 100 Grams Per Hours; Wherein, tri-isopropyl benzene content 5% in logistics 14;
The operational condition of depropanizing tower is: 45 DEG C of tower top temperatures, 230 DEG C of tower reactor temperature, working pressure 2.50MPa;
The operational condition of benzene rectifying tower is: 87 DEG C of tower top temperatures, 185 DEG C of tower reactor temperature, working pressure 0.02MPa;
The operational condition of isopropyl benzene rectifying tower is: 154 DEG C of tower top temperatures, 220 DEG C of tower reactor temperature, working pressure 0.02MPa;
Polyisopropylbenzene rectifying tower operational condition is: 128 DEG C of tower top temperatures, 210 DEG C of tower reactor temperature, working pressure-120MPa;
Reaction result: isopropyl benzene productive rate 99.7%, isopropyl benzene purity 99.97%, n-proplbenzene content 200ppm in isopropyl benzene.
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| CN103739438B (en) * | 2012-10-17 | 2015-08-12 | 中国石油化工股份有限公司 | The method of benzene and propylene liquid phase hydrocarbonylation preparing isopropylbenzene |
| CN114478171B (en) * | 2020-10-26 | 2024-06-28 | 中国石油化工股份有限公司 | Method and system for refining cumene |
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|---|---|---|---|---|
| CN1037699A (en) * | 1988-05-09 | 1989-12-06 | 鲁姆斯克雷斯特公司 | The manufacturing of alkylbenzene |
| US5177285A (en) * | 1991-12-23 | 1993-01-05 | Uop | Process for wet aromatic alkylation and dry aromatic transalkylation |
| CN1235146A (en) * | 1999-04-09 | 1999-11-17 | 中国石油天然气集团公司 | Method for preparing ethylbenzene and/or isopropylbenzene from thin ethylene and/or propylene |
| CN1884239A (en) * | 2005-06-22 | 2006-12-27 | 中国石油化工股份有限公司 | Method for producing isopropyl benzene |
-
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- 2010-11-17 CN CN201010551968.5A patent/CN102464565B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1037699A (en) * | 1988-05-09 | 1989-12-06 | 鲁姆斯克雷斯特公司 | The manufacturing of alkylbenzene |
| US5177285A (en) * | 1991-12-23 | 1993-01-05 | Uop | Process for wet aromatic alkylation and dry aromatic transalkylation |
| CN1235146A (en) * | 1999-04-09 | 1999-11-17 | 中国石油天然气集团公司 | Method for preparing ethylbenzene and/or isopropylbenzene from thin ethylene and/or propylene |
| CN1884239A (en) * | 2005-06-22 | 2006-12-27 | 中国石油化工股份有限公司 | Method for producing isopropyl benzene |
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