CN102464566B - 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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- CN102464566B CN102464566B CN201010552132.7A CN201010552132A CN102464566B CN 102464566 B CN102464566 B CN 102464566B CN 201010552132 A CN201010552132 A CN 201010552132A CN 102464566 B CN102464566 B CN 102464566B
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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 material flow 19 comprising 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 alkyl group transfer reaction zone for carrying out alkyl group transfer reaction to obtain a material flow 20; the material flow 20, 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 the material flow 21 enters the follow-up refining process, thereby the isopropylbenzene product is obtained.
Description
Technical field
The present invention relates to a kind of method of 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.As far back as UOP in 1945, just announced under an acidic catalyst exists, the method (SPA method) of preparing isopropyl benzene with the reaction of propylene and benzene (USP2382318), SPA method be take 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 take micro-pore zeolite as catalyzer, has 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 separation, and polysubstituted isopropyl benzene enters the transalkylation reaction zone of a single bed and carries out transalkylation reaction after mixing with benzene again.
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 the mol ratio of benzene and polyisopropylbenzene, raw material air speed and polyisopropylbenzene raw material 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 method of new 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 of 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 is successively by depropanizing tower, benzene rectifying tower and isopropyl benzene rectifying tower, and separation obtains propane logistics 15, benzene logistics 9, isopropyl benzene logistics 16 and contains the logistics 23 of 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 reaction zone, contact and carry out transalkylation reaction with catalyzer, obtain logistics 20 after reaction; Logistics 20, the 3rd burst of benzene logistics 11 and logistics 14 enter the second transalkylation reaction zone, contact and carry out transalkylation reaction with catalyzer, obtain logistics 21 after reaction; Logistics 21 enters follow-up rectification flow, obtains 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 ℃, 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 reaction zone temperature of reaction preferable range is 130～190 ℃; 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, PSH-3, MCM-22, MCM-56 or MCM-49.
In technique scheme, the second transalkylation reaction zone temperature of reaction preferable range is 150～210 ℃; 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, PSH-3, MCM-22, MCM-56 or MCM-49.
In the inventive method, the first transalkylation reaction zone and the second transalkylation reaction zone are all fixed-bed reactor, and wherein the catalyzer of filling is selected from Y zeolite, Beta zeolite, mordenite, SHY-1, SHY-2, PSH-3, MCM-22, MCM-56 or MCM-49.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, and PSH-3 can be according to disclosed method preparation in US4439409.
In the inventive method, the operational condition of depropanizing tower is: 40～80 ℃ of tower top temperatures, 210～280 ℃ of tower reactor temperature, working pressure 1.3～1.8MPa.The operational condition of benzene rectifying tower is: 80～120 ℃ of tower top temperatures, 170～220 ℃ of tower reactor temperature, working pressure 0～0.3MPa.The operational condition of isopropyl benzene rectifying tower is: 150～160 ℃ of tower top temperatures, 200～250 ℃ of tower reactor temperature, working pressure 0～0.03MPa.Polysubstituted isopropyl benzene tower operational condition is: tower top temperature is 120～160 ℃, and tower reactor temperature is 190～250 ℃, 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 after transalkylation reaction (logistics 21) enters successively follow-up benzene rectifying tower, isopropyl benzene rectifying tower and polyisopropylbenzene rectifying tower and refines, and obtains product isopropyl benzene.
In the inventive method, described pressure refers to gauge pressure.
In the inventive method, the first transalkylation reaction zone and the second transalkylation reaction zone can be independently, the fixed-bed reactor of two series connection, can be also complete fixed-bed reactor that contain two beds.
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.
Accompanying drawing explanation
Fig. 1 and Fig. 2 are process flow diagram of the present invention.
In Fig. 1, the first transalkylation reaction zone and the second transalkylation reaction zone be independently, the fixed-bed reactor of two series connection.
In Fig. 2, the first transalkylation reaction zone and the second transalkylation reaction zone are included in fixed-bed reactor.
In Fig. 1 and Fig. 2, 1 is alkylation reactor, 2 is the first transalkylation reaction zone, 3 is the second transalkylation reaction zone, 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 reaction zone, 11 is the benzene (the 3rd strand of benzene) to the second transalkylation reaction zone, 12 is the benzene (first strand of benzene) to alkylation reactor, 13 is the polyisopropylbenzene to the first transalkylation reaction zone, 14 is the polyisopropylbenzene to the second transalkylation reaction zone, 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 the first transalkylation reaction zone product stream, 21 is the second transalkylation reaction zone product stream, 22 is depropanizing tower tower bottoms.
In Fig. 1 and in Fig. 2, 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 reaction zone.First burst of 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 is successively by depropanizing tower, benzene rectifying tower and isopropyl benzene rectifying tower, and separation obtains propane logistics 15, benzene logistics 9, isopropyl benzene logistics 16 and contains the logistics 23 of 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 reaction zone, contact and carry out transalkylation reaction with catalyzer, obtain logistics 20 after reaction; The 3rd burst of benzene logistics 11 and logistics 14 enter the second transalkylation reaction zone, contact and carry out transalkylation reaction with catalyzer, obtain logistics 21 after reaction; Logistics 21 enters follow-up rectification flow, obtains 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 170 grams containing the preformed catalyst of 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: 130 ℃ of temperature of reaction, reaction pressure 2.5MPa, enter benzene intake (logistics 12) 550 Grams Per Hours of alkylation reactor, propylene intake 110 Grams Per Hours, four sections of amounts that pass into successively propylene are 20,25,30,35 Grams Per Hours.
Transalkylation reactor adopts the fixed-bed reactor of two series connection.The first transalkylation reaction zone is loaded 40 grams containing the preformed catalyst of Beta zeolite, and the second transalkylation reaction zone is loaded 50 grams containing the preformed catalyst of PSH-3 zeolite.The reaction conditions of first transalkylation reactor is: 150 ℃ of temperature of reaction, polyisopropylbenzene inlet amount (logistics 13) 40 Grams Per Hours, benzene input (logistics 10) 100 Grams Per Hours, reactor outlet pressure 1.5MPa.Wherein, diisopropylbenzene(DIPB) content 98% in logistics 13.Second transalkylation reactor condition is: 175 ℃ of temperature of reaction, reaction pressure 1.4MPa, polyisopropylbenzene inlet amount (logistics 14) 70 Grams Per Hours, benzene input (logistics 11) 90 Grams Per Hours, reactor outlet pressure 1.5MPa.Wherein, tri-isopropyl benzene content 6% in logistics 14.
The operational condition of depropanizing tower is: 45 ℃ of tower top temperatures, 230 ℃ of tower reactor temperature, working pressure 2.50MPa.
The operational condition of benzene rectifying tower is: 87 ℃ of tower top temperatures, 185 ℃ of tower reactor temperature, working pressure 0.02MPa.
The operational condition of isopropyl benzene rectifying tower is: 154 ℃ of tower top temperatures, 220 ℃ of tower reactor temperature, working pressure 0.02MPa.
Polyisopropylbenzene rectifying tower operational condition is: 134 ℃ of tower top temperatures, 215 ℃ of tower reactor temperature, working pressure-80MPa.
Reaction result: isopropyl benzene productive rate 99.7%, isopropyl benzene purity 99.97%, n-proplbenzene content 170ppm in isopropyl benzene.
[embodiment 2]
With [embodiment 1], just alkylation reactor beds is divided into four sections, is mounted with 200 grams containing the preformed catalyst of MCM-22 zeolite, and four sections are equipped with 45,50,50,55 grams successively, and propylene divides four section feedings.Alkylation reactor reaction conditions is: 1 50 ℃ of temperature of reaction, reaction pressure 2.5MPa, enter benzene intake (logistics 12) 550 Grams Per Hours of alkylation reactor, propylene intake 160 Grams Per Hours, four sections of amounts that pass into successively propylene are 35,40,40,45 Grams Per Hours.
Transalkylation reactor adopts the fixed-bed reactor of two series connection.Wherein first transalkylation reactor loads 80 grams containing the preformed catalyst of Beta zeolite, and second transalkylation reactor loads 30 grams containing the preformed catalyst of PSH-3 zeolite.The reaction conditions of first transalkylation reactor is: 150 ℃ of temperature of reaction, polyisopropylbenzene inlet amount (logistics 13) 40 Grams Per Hours, benzene input (logistics 10) 100 Grams Per Hours, reactor outlet pressure 1.5MPa.Wherein, diisopropylbenzene(DIPB) content 99% in logistics 13.Second transalkylation reactor condition is: 175 ℃ of temperature of reaction, reaction pressure 1.4MPa, polyisopropylbenzene inlet amount (logistics 14) 70 Grams Per Hours, benzene input (logistics 11) 90 Grams Per Hours, reactor outlet pressure 1.5MPa.Wherein, tri-isopropyl benzene content 10% in logistics 14.
The operational condition of depropanizing tower is: 45 ℃ of tower top temperatures, 230 ℃ of tower reactor temperature, working pressure 2.50MPa.
The operational condition of benzene rectifying tower is: 87 ℃ of tower top temperatures, 185 ℃ of tower reactor temperature, working pressure 0.02MPa.
The operational condition of isopropyl benzene rectifying tower is: 154 ℃ of tower top temperatures, 220 ℃ of tower reactor temperature, working pressure 0.02MPa.
Polyisopropylbenzene rectifying tower operational condition is: 130 ℃ of tower top temperatures, 214 ℃ of tower reactor temperature, working pressure-90MPa.
Reaction result: isopropyl benzene productive rate 99.7%, isopropyl benzene purity 99.97%, n-proplbenzene content 205ppm in isopropyl benzene.
[embodiment 3]
With [embodiment 1], just alkylation reactor beds is divided into four sections, is mounted with 170 grams containing the preformed catalyst of SHY-1 zeolite, and four sections are equipped with 45,50,50,55 grams successively, and propylene divides four section feedings.Alkylation reactor reaction conditions is: 130 ℃ of temperature of reaction, reaction pressure 2.5MPa, enter benzene intake (logistics 12) 550 Grams Per Hours of alkylation reactor, propylene intake 160 Grams Per Hours, four sections of amounts that pass into successively propylene are 35,40,40,45 Grams Per Hours.
Transalkylation reactor adopts the fixed-bed reactor of two series connection.Wherein first transalkylation reactor loads 80 grams containing the preformed catalyst of Beta zeolite, and second transalkylation reactor loads 30 grams containing the preformed catalyst of SHY-2 zeolite.The reaction conditions of first transalkylation reactor is: 150 ℃ of temperature of reaction, polyisopropylbenzene inlet amount (logistics 13) 40 Grams Per Hours, benzene input (logistics 10) 100 Grams Per Hours, reactor outlet pressure 1.5MPa.Wherein, diisopropylbenzene(DIPB) content 99% in logistics 13.Second transalkylation reactor condition is: 180 ℃ of temperature of reaction, reaction pressure 1.5MPa, polyisopropylbenzene inlet amount (logistics 14) 60 Grams Per Hours, benzene input (logistics 11) 60 Grams Per Hours, reactor outlet pressure 1.5MPa.Wherein, tri-isopropyl benzene content 12% in logistics 14.
The operational condition of depropanizing tower is: 43 ℃ of tower top temperatures, 228 ℃ of tower reactor temperature, working pressure 2.50MPa.
The operational condition of benzene rectifying tower is: 85 ℃ of tower top temperatures, 182 ℃ of tower reactor temperature, working pressure 0.02MPa.
The operational condition of isopropyl benzene rectifying tower is: 155 ℃ of tower top temperatures, 220 ℃ of tower reactor temperature, working pressure 0.02MPa.
Polyisopropylbenzene rectifying tower operational condition is: 129 ℃ of tower top temperatures, 214 ℃ of tower reactor temperature, working pressure-85MPa.
Reaction result: isopropyl benzene productive rate 99.7%, isopropyl benzene purity 99.97%, n-proplbenzene content 215ppm in isopropyl benzene.
[embodiment 4]
Press the technical process of Fig. 2, alkylation reactor beds is divided into four sections, be mounted with 170 grams containing the preformed catalyst of MCM-22 zeolite, four sections are equipped with 35,40,45,50 grams successively, and propylene divides four section feedings, and alkylation reactor reaction conditions is: 135 ℃ of temperature of reaction, reaction pressure 2.5MPa, enter benzene intake 600 Grams Per Hours of alkylation reactor, propylene intake 120 Grams Per Hours, four sections of amounts that pass into successively propylene are 25,28,32,35 Grams Per Hours.
Transalkylation reactor adopts two sections of fixed-bed reactor of a laminar.Wherein transalkylation reactor epimere loads 50 grams containing the preformed catalyst of Beta zeolite, and transalkylation reactor hypomere loads 90 grams containing the preformed catalyst of MCM-56 zeolite.The reaction conditions of epimere transalkylation reactor is: 150 ℃ of temperature of reaction, polyisopropylbenzene inlet amount 70 Grams Per Hours, benzene input 200 Grams Per Hours.Hypomere reaction conditions is: 170 ℃ of temperature of reaction, polyisopropylbenzene inlet amount 100 Grams Per Hours, benzene input 50 Grams Per Hours, reactor outlet pressure 1.5MPa.Wherein, diisopropylbenzene(DIPB) content 99% in logistics 13.Tri-isopropyl benzene content 10% in logistics 14.
The operational condition of depropanizing tower is: 42 ℃ of tower top temperatures, 225 ℃ of tower reactor temperature, working pressure 2.45MPa.
The operational condition of benzene rectifying tower is: 85 ℃ of tower top temperatures, 180 ℃ of tower reactor temperature, working pressure 0.01MPa.
The operational condition of isopropyl benzene rectifying tower is: 153 ℃ of tower top temperatures, 218 ℃ of tower reactor temperature, working pressure 0.02MPa.
Polyisopropylbenzene rectifying tower operational condition is: 131 ℃ of tower top temperatures, 215 ℃ of tower reactor temperature, working pressure-80MPa.
Reaction result: isopropyl benzene productive rate 99.7%, isopropyl benzene purity 99.97%, n-proplbenzene content 250ppm in isopropyl benzene.
[embodiment 5]
Press the technical process of Fig. 2, alkylation reactor beds is divided into four sections, be mounted with 1 80 grams containing the preformed catalyst of SHY-2 zeolite, four sections are equipped with 35,40,45,50 grams successively, and propylene divides four section feedings, and alkylation reactor reaction conditions is: 130 ℃ of temperature of reaction, reaction pressure 2.4MPa, enter benzene intake 600 Grams Per Hours of alkylation reactor, propylene intake 120 Grams Per Hours, four sections of amounts that pass into successively propylene are 25,28,32,35 Grams Per Hours.
Transalkylation reactor adopts two sections of fixed-bed reactor of a laminar.Wherein transalkylation reactor epimere loads 50 grams containing the preformed catalyst of Beta zeolite, and transalkylation reactor hypomere loads 90 grams containing the preformed catalyst of SHY-1 zeolite.The reaction conditions of epimere transalkylation reactor is: 150 ℃ of temperature of reaction, polyisopropylbenzene inlet amount 70 Grams Per Hours, benzene input 200 Grams Per Hours.Hypomere reaction conditions is: 170 ℃ of temperature of reaction, polyisopropylbenzene inlet amount 100 Grams Per Hours, benzene input 50 Grams Per Hours, reactor outlet pressure 1.5MPa.Wherein, diisopropylbenzene(DIPB) content 99% in logistics 13.Tri-isopropyl benzene content 10% in logistics 14.
The operational condition of depropanizing tower is: 55 ℃ of tower top temperatures, 235 ℃ of tower reactor temperature, working pressure 2.55MPa.
The operational condition of benzene rectifying tower is: 115 ℃ of tower top temperatures, 216 ℃ of tower reactor temperature, working pressure 0.2MPa.
The operational condition of isopropyl benzene rectifying tower is: 153 ℃ of tower top temperatures, 218 ℃ of tower reactor temperature, working pressure 0.02MPa.
Polyisopropylbenzene rectifying tower operational condition is: 125 ℃ of tower top temperatures, 206 ℃ of tower reactor temperature, working pressure-150MPa.
Reaction result: isopropyl benzene productive rate 99.7%, isopropyl benzene purity 99.97%, n-proplbenzene content 250ppm in isopropyl benzene.
[comparative example 1]
With [embodiment 1], just transalkylation partly only has a reactor, and only from polyisopropylbenzene rectifying tower tower top, draws logistics, and this logistics all enters transalkylation reaction zone.Transalkylation reaction zone is mounted with the preformed catalyst of 50 grams of Beta zeolites, 153 ℃ 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 ℃ 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 ℃ 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. a method for benzene and production of propylene isopropyl benzene, comprises 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 is successively by depropanizing tower, benzene rectifying tower and isopropyl benzene rectifying tower, and separation obtains propane logistics, benzene logistics, isopropyl benzene logistics and contains the logistics of 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, and the heavy constituent logistics that contains tar enters follow-up flow process; 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 second transalkylation reaction zone product stream enters follow-up rectification flow, obtains product isopropyl benzene;
Described alkylation reactor beds is divided into four sections, is mounted with 170 grams containing the preformed catalyst of 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: 130 ℃ of temperature of reaction, reaction pressure 2.5MPa, enter first strand of benzene intake 550 Grams Per Hour of alkylation reactor, propylene intake 110 Grams Per Hours, four sections of amounts that pass into successively propylene are 20,25,30,35 Grams Per Hours;
Transalkylation reactor adopts the fixed-bed reactor of two series connection; The first transalkylation reaction zone is loaded 40 grams containing the preformed catalyst of Beta zeolite, and the second transalkylation reaction zone is loaded 50 grams containing the preformed catalyst of PSH-3 zeolite; The reaction conditions of first transalkylation reactor is: 150 ℃ of temperature of reaction, polyisopropylbenzene logistics inlet amount 40 Grams Per Hours of the first transalkylation reaction zone, second strand of benzene logistics inlet amount 100 Grams Per Hour, reactor outlet pressure 1.5MPa; Wherein, diisopropylbenzene(DIPB) content 98% in the polyisopropylbenzene logistics of the first transalkylation reaction zone; Second transalkylation reactor condition is: 175 ℃ of temperature of reaction, reaction pressure 1.4MPa, polyisopropylbenzene logistics inlet amount 70 Grams Per Hours of the second transalkylation reaction zone, the 3rd strand of benzene logistics inlet amount 90 Grams Per Hours, reactor outlet pressure 1.5MPa; Wherein, tri-isopropyl benzene content 6% in the polyisopropylbenzene logistics of the second transalkylation reaction zone;
The operational condition of depropanizing tower is: 45 ℃ of tower top temperatures, 230 ℃ of tower reactor temperature, working pressure 2.50MPa;
The operational condition of benzene rectifying tower is: 87 ℃ of tower top temperatures, 185 ℃ of tower reactor temperature, working pressure 0.02MPa;
The operational condition of isopropyl benzene rectifying tower is: 154 ℃ of tower top temperatures, 220 ℃ of tower reactor temperature, working pressure 0.02MPa;
Polyisopropylbenzene rectifying tower operational condition is: 134 ℃ of tower top temperatures, 215 ℃ of tower reactor temperature, working pressure-80MPa;
Reaction result: isopropyl benzene productive rate 99.7%, isopropyl benzene purity 99.97%, n-proplbenzene content 170ppm in isopropyl benzene.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| EP2865660B1 (en) | 2013-10-28 | 2016-05-04 | China Petroleum & Chemical Corporation | Method for producing isopropyl benzene from benzene and propylene |
| CN104557438B (en) * | 2013-10-28 | 2017-06-20 | 中国石油化工股份有限公司 | The method of benzene and production of propylene isopropylbenzene |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1037669A (en) * | 1988-04-28 | 1989-12-06 | 唐化学原料公司 | Be used for separating the ferrous disulfide depressant of ferrous disulfide from coal |
| 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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Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1037669A (en) * | 1988-04-28 | 1989-12-06 | 唐化学原料公司 | Be used for separating the ferrous disulfide depressant of ferrous disulfide from coal |
| 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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