CN103030515A - Alkylbenzene production method - Google Patents
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- CN103030515A CN103030515A CN2011102942418A CN201110294241A CN103030515A CN 103030515 A CN103030515 A CN 103030515A CN 2011102942418 A CN2011102942418 A CN 2011102942418A CN 201110294241 A CN201110294241 A CN 201110294241A CN 103030515 A CN103030515 A CN 103030515A
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Abstract
The present invention relates to an alkylbenzene production method, and is mainly to solve the problem of high energy consumption in the prior art. The present invention comprises the following steps: (1) feeding benzene and olefin into an alkylation reactor, and feeding an alkylation reaction liquid into a benzene column; (2) feeding benzene and polyalkylbenzene into a transalkylation reactor, feeding transalkylation reaction product into the benzene column; (3) feeding noncondensable gas-containing gas phase from the benzene column top into a non-aromatic hydrocarbon removing tower, and introducing tower bottom substances into an alkylbenzene tower; (4) discharging alkane-containing non-condensable gas from the non-aromatic hydrocarbon removing tower top, returning the benzene-containing material from the tower bottom to the benzene column; (5) obtaining the alkylbenzene product from the alkylbenzene tower top, feeding the material in the tower bottom to the polyalkylbenzene tower; and (6) recycling polyalkylbenzene obtained from the multi-alkylbenzene tower top or side line to the transalkylation reactor. The technical solution solves the problem well, and can be applied to the industrial production of alkylbenzene from benzene and olefin alkylation.
Description
Technical field
The present invention relates to a kind of production method of alkylbenzene, particularly produce the method for ethylbenzene and isopropyl benzene.
Background technology
Ethylbenzene in the alkylbenzene and isopropyl benzene are important Organic Chemicals, and wherein, mainly as the cinnamic raw material of preparation, isopropyl benzene is mainly for the production of phenol and acetone for ethylbenzene.
Industrial traditional preparation ethylbenzene and isopropyl benzene method all adopt solid phosphoric acid, aluminum chloride or hydrofluoric acid catalyst series, because it is serious to equipment corrosion, the three wastes are many, and along with the raising to environmental requirement, major part is replaced by novel sieve method.Produce at present alkylbenzene and turned to the molecular sieve catalyst that adopts highly selective, comprise the ZSM series of large pore molecular sieve Y, beta, MCM series and mesopore etc.
Most new ethylbenzene and the molecular sieve liquid-phase alkylation method of isopropyl benzene production equipment employing propylene and benzene.The method has the advantage of reaction conditions gentleness, olefin conversion height and good product selectivity, not only pollution-free and without corrosion, and the by product polyalkylbenzene can change ethylbenzene into or isopropyl benzene makes the alkylbenzene productive rate up to more than 99% by transalkylation, is in recent years each institute of large industrial group company common concern of the world, an and cleaner technology of development research competitively.
CN1037699 has announced a kind of manufacture method of alkylbenzene, the method proposes when producing isopropyl benzene, after the effluent of alkylation reactor and transalkylation reactor removes propane by depropanizing tower first, enter successively again benzene tower, isopropyl benzene tower and polyisopropylbenzene tower and separate, obtain the isopropyl benzene product.
Document WO 89/10910 has been announced a kind of technical process of producing isopropyl benzene, to be raw material propylene enter alkylation reactor after first by the interchanger preheating with new benzene feedstock of replenishing before adding reactor reacts, reacted material enters flash distillation plant, most of recycle benzene is separated, enter depropanizing tower, and the steam that is rich in isopropyl benzene enters the benzene tower, isolates residual benzene at this.Then with a small amount of heavies of clay treatment isopropyl benzene except by-product in the removal of alkylation reaction.From benzene Tata still higher aromatics out, be mainly diisopropylbenzene(DIPB) (DIPB), DIPB reacts the generation isopropyl benzene again in transalkylation workshop section.
More than two methods when producing isopropyl benzene, CN1037699 has adopted and depropanizing tower is set has removed propane, WO89/10910 then is first with after the reaction product vacuum flashing, the gaseous phase materials that contains propane and benzene enters depropanizing tower and removes propane.Although these two method technical process are different, equally all be provided with depropanizing tower, exist the shortcoming that knockout tower quantity is many, energy consumption is larger.
Summary of the invention
Technical problem to be solved by this invention is that conventional art exists technical process unreasonable when producing alkylbenzene, after the alkylation reaction product that only contains a small amount of alkane takes off the alkyl tower and separates by one first, just obtain the alkylbenzene product through benzene tower, alkylbenzene tower etc. again, the problem that the energy consumption that causes therefrom is high provides a kind of production method of new alkylbenzene.The method has the characteristics such as energy consumption is low, flow process is simple.
In order to solve the problems of the technologies described above, the technical solution used in the present invention is as follows: a kind of alkylbenzene production method may further comprise the steps:
A) in the presence of alkylation catalyst, comprise that the mixing raw material of fresh benzene, recycle benzene and alkene enters the alkylation reactor that contains at least two sections beds, enter the benzene tower through the reaction solution after the liquid phase alkylation reaction;
B) in the presence of transalkylation catalyst, the polyalkylbenzene that comprises fresh benzene, recycle benzene and recovery enters transalkylation reactor and carries out the liquid phase transalkylation reaction, and reaction product enters the benzene tower;
C) alkylated reaction liquid and transalkylation reaction liquid enter benzene tower middle part, fresh benzene enters from benzene tower middle and upper part, the top gaseous phase material enters return tank after entering the overhead condenser condensation, non-condensable gas enters d from the return tank of top of the tower discharging) step, the benzene of lateral line withdrawal function enters alkylation reactor and transalkylation reactor as raw material, and benzene tower tower bottoms enters e) step;
D) from c) step come contain alkane, gas non-aromatic and benzene enters the non-aromatic removal tower from the bottom, separate the liquid stream that rear cat head obtains containing the non-condensable gas logistics of alkane and non-aromatics and contains the components such as non-aromatic and benzene, tower reactor obtains the benzene logistics, and c is returned in the logistics of this strand benzene) benzene top of tower in the step;
E) from c) the benzene tower tower bottoms that comes of step enters alkylbenzene tower middle part, and cat head obtains the alkylbenzene product, tower bottoms enters f) step;
F) from e) the alkylbenzene tower tower bottoms that comes of step enters polyalkylbenzene tower middle part, and polyalkylbenzene is sent to transalkylation reactor from cat head or side line extraction, extraction heavy component at the bottom of the polyalkylbenzene tower.
In the technique scheme, alkene refers to ethene and propylene; Alkylbenzene then is ethylbenzene and isopropyl benzene; Non-condensable gas refers to ethane or propane; If fresh benzene contains certain moisture content and then enters the benzene tower and remove moisture content; The volumetric molar concentration of raw material ethene or propylene is 70～100%; The mass concentration of fresh benzene is 99.0～100%; Contain ethane or propane, benzene, ethylbenzene or isopropyl benzene component in the alkylated reaction liquid, wherein the volumetric molar concentration of ethane or propane is 0.001～20%; Alkylated reaction liquid directly enters the benzene tower to be separated without other separation facilities, benzene column overhead working pressure is 0.0～1.0MPa (g), preferable range is 0.1-0.6MPa (g), the cat head service temperature is 70～200 ℃, preferable range is 80～150 ℃, and the tower reactor temperature is 150～300 ℃, and preferable range is 200～250 ℃, theoretical plate number is 20～100, and preferable range is 30～60; The volumetric molar concentration of ethane or propane is 1-90% in the gaseous phase materials that benzene column overhead return tank is discharged, and preferable range is 10～70%; Benzene feedstock enters the benzene tower near the position on top, on benzene tower top but extract the benzene raw materials that is used for alkylation and transalkylation reaction out below the benzene feedstock entry position; The mass concentration of benzene is 70～100% in the benzene logistics of benzene tower side line extraction, and preferable range is 85～100%, and side line extraction position is several the 2nd～30 layer of tower tray from top to bottom, and preferable range is 5～15; The cat head working pressure of non-aromatic removal tower is 0.0～1.0MPa (g), and preferable range is 0.1～0.6MPa (g), and the cat head service temperature is 40～200 ℃, and preferable range is 40-100 ℃, and theoretical plate number is 2～30, and preferable range is 5～20; Alkylbenzene column overhead working pressure is-0.1～1.0MPa (g), preferable range is 0.0～0.5MPa (g), the cat head service temperature is 80～250 ℃, preferable range is 120～250 ℃, the tower reactor temperature is 150～300 ℃, preferable range is 180～250 ℃, and theoretical plate number is 10～100, and preferable range is 30～60; Polyalkylbenzene tower working pressure is-0.1～0.5MP (g), preferable range is-0.1～0.1MPa (g), service temperature is 80 ℃～250 ℃, preferable range is 100 ℃～200 ℃, the tower reactor temperature is 150～300 ℃, preferable range is 180～250 ℃, and theoretical plate number is 10～100, and preferable range is 30～60.
Among the present invention, the alkylation liquid that contains ethane or propane does not adopt Dealkylater to remove alkane but directly enters the benzene tower and separates, the benzene cat head arranges partial condenser, by the control condensing temperature, alkane is discharged from benzene column overhead return tank with the non-condensable gas form, then enters follow-up non-aromatic removal tower, in this tower, realize separating of alkane and benzene, while has also removed non-aromatic on a small quantity by what bring in the benzene feedstock, and the benzene that reclaims from this Tata still is back to the benzene tower, to reduce the unit consumption of benzene.Removed alkane and non-aromatic after benzene can be from the side line extraction of benzene tower, as the raw material of alkylation and transalkylation reaction.The logistics that contains alkylbenzene and the components such as polyalkylbenzene that tower reactor obtains enters the alkylbenzene tower and separates, and can obtain highly purified alkylbenzene product at the cat head of alkylbenzene tower.The material that contains polyalkylbenzene that obtains from alkylbenzene Tata still enters the polyalkylbenzene tower, the components such as the dialkyl benzene that reaction generates and trialkyl benzene are from this column overhead or near the side line extraction of the cat head raw material as transalkylation reaction, with the benzene one generation alkylbenzene that reacts, tower reactor is discharged a small amount of heavy component.Adopt the alkylbenzene production technique of the invention described above, cancelled and taken off alkyl tower and a series of equipment and the corresponding control devices such as corresponding overhead condenser, return tank, reflux pump and reboiler in traditional Alkylbenzene Unit, both reduced investment, reduced again energy consumption, be applicable to the benzene process flow process of different concns olefin feedstock, obtained preferably technique effect.
Description of drawings
Fig. 1 is traditional isopropyl benzene technological process of production synoptic diagram.
Fig. 2 is the isopropyl benzene technological process of production synoptic diagram of optimization of the present invention.
I is Alkylation benzene with propylene and benzene and polyisopropylbenzene transalkylation reaction unit among Fig. 1, and II is depropanizing tower, and III benzene tower, IV are the isopropyl benzene tower, and V is the polyisopropylbenzene tower, and VI is benzene tower return tank, and VII is the non-aromatic removal tower, and VIII is non-aromatic removal tower return tank.1 is propylene feedstocks, and 2 is the fresh benzene raw material, and 3 is dried benzene, and 4 is polyisopropylbenzene, and 5 is alkylated reaction liquid, and 6 is transalkylation reaction liquid, and 7 is propane, and 8 is dirty benzene, and 9 is the isopropyl benzene product, and 10 is heavy component.
In traditional isopropyl benzene technological process of production shown in Figure 1, propylene feedstocks 1 and recycle benzene raw material 3 enter alkylated reaction unit I, and fresh benzene raw material 2 is sent into reaction member I from the dried benzene raw materials 3 of lateral line withdrawal function after entering benzene tower III dehydration.The alkylated reaction liquid 5 that reaction generates enters depropanizing tower II from removed overhead propane gas 7, the transalkylation reaction liquid 6 that the depropanizing tower tower bottoms generates with reaction enters benzene tower III to be separated, dirty benzene 8 is discharged from cat head, dried benzene 3 enters alkylation and transalkylation reaction unit I from benzene tower lateral line withdrawal function, benzene tower tower bottoms enters isopropyl benzene tower IV to be separated, cat head obtains isopropyl benzene product 9, tower bottoms enters polyisopropylbenzene tower V to be separated, enter transalkylation and dried benzene carries out transalkylation reaction from the isolated polyisopropylbenzene 4 of polyisopropylbenzene tower, tower reactor is discharged heavy component 10.
Isopropyl benzene production technique of the present invention is seen Fig. 2.I is Alkylation benzene with propylene and benzene and polyisopropylbenzene transalkylation reaction unit among Fig. 2, and III benzene tower, IV are the isopropyl benzene tower, V is the polyisopropylbenzene tower, and VI is benzene column overhead condenser, and VII is benzene tower return tank, VIII is the non-aromatic removal tower, and IX is non-aromatic removal tower return tank.1 is propylene feedstocks, and 2 is the fresh benzene raw material, and 3 is dried benzene, and 4 is polyisopropylbenzene, and 5 is alkylated reaction liquid, and 6 is transalkylation reaction liquid, and 7 is propane, and 8 is dirty benzene, and 9 is the isopropyl benzene product, and 10 is heavy component.
Fig. 2 is in the isopropyl benzene technological process of production of the present invention, and propylene feedstocks 1 and recycle benzene raw material 3 enter alkylated reaction unit I, and fresh benzene raw material 2 is sent into reaction member I from side line extraction benzene raw materials 3 after entering benzene tower III dehydration.Compare with traditional flow process, the alkylated reaction liquid 5 that reaction generates directly enters benzene tower III with transalkylation reaction liquid 6 to be separated, benzene column overhead gas enters overhead condenser VI condensation, by control lime set temperature, the material that will contain propane and benzene is discharged from benzene column overhead return tank VII with the non-condensable gas form, deliver to non-aromatic removal tower VIII and carry out separating of propane and benzene, this tower is not established reboiler, method by control cat head condenser condenses temperature, allow propane discharge from non-aromatic removal tower return tank IX with the non-condensable gas form, one contains non-aromatic dirty benzene 8 simultaneously extraction, to prevent non-aromatic accumulation in system.Dried benzene 3 enters alkylation and transalkylation reaction unit I from benzene tower lateral line withdrawal function, benzene tower tower bottoms enters isopropyl benzene tower IV to be separated, cat head obtains isopropyl benzene product 9, tower bottoms enters polyisopropylbenzene tower V to be separated, enter transalkylation and dried benzene carries out transalkylation reaction from the isolated polyisopropylbenzene 4 of polyisopropylbenzene tower, polyisopropylbenzene Tata still is discharged a small amount of heavy component 10 that reaction generates.
The invention will be further elaborated below by embodiment, but be not limited only to following examples.
Embodiment
[embodiment 1]
Take volumetric molar concentration as 95% chemical grade propylene and the benzene of mass concentration as 99.8% as raw material, adopt Fig. 2 Technology to produce isopropyl benzene.Alkylation and transalkylation catalyst adopt the Beta zeolite as catalyzer.The molar content of propane is 2.5% in the reacted reaction product of Alkylation benzene with propylene.The benzene tower adopts 60 layers of valve tray, and the cat head working pressure is 0.25MPa (g), and dephlegmator of top of the tower control temperature is 110 ℃, discharge non-condensable gas from benzene tower return tank, wherein the propane volumetric molar concentration is 22.6%, and benzene mole concentration is 72.5%, other non-aromatic 4.9mol%.This strand material enters the non-aromatic removal tower bottom, the non-aromatic removal tower adopts 15 layers of valve tray, and the cat head working pressure is 0.2MPa (g), and dephlegmator of top of the tower control temperature is 40 ℃, the propane volumetric molar concentration is 88.2% from the non-condensable gas that discharge at the return tank top, and other is a small amount of benzene and other non-aromatics.The isopropyl benzene tower adopts 50 layers of valve tray, and the cat head working pressure is 0.02MPa (g), and the cat head service temperature is 158 ℃.The polyisopropylbenzene tower adopts 40 layers of valve tray, and the cat head working pressure is 20KPa (a), and tower top temperature is 130 ℃.After adopting this technical scheme, from the isopropyl benzene column overhead isopropyl benzene product that to obtain 25 tons of/hour purity be 99.97wt%.Benzene Tata still thermal load is 4.9MW, needs to consume 10.0 tons/hour of 4.0MPa (g) steam.Because the non-aromatic removal tower is without reboiler, so without steam consumption.In addition, the isopropyl benzene tower in present embodiment and the comparative example 1 is identical with the thermal load of polyisopropylbenzene tower, steam consumption too, so no longer list this two item numbers certificate.
[embodiment 2]
The production technique of isopropyl benzene is with embodiment 1, and the propylene take volumetric molar concentration as 99.5mol% and mass concentration are raw material as 99.8% benzene.Alkylation and transalkylation catalyst adopt the MCM-56 molecular sieve as catalyzer.The molar content of propane is 0.25% in the reacted reaction product of Alkylation benzene with propylene.The benzene tower adopts 65 layers of valve tray, the cat head working pressure is 0.25MPa (g), dephlegmator of top of the tower control temperature is 110 ℃, discharge the gas that contains propane from benzene tower return tank and enter the non-aromatic removal tower, propane content is 14.4mol% in this strand gaseous phase materials, benzene content is 64.9mol%, other non-aromatic 20.78mol%.This strand material enters the non-aromatic removal tower bottom, the non-aromatic removal tower adopts 15 layers of valve tray, the cat head working pressure is 0.2MPa (g), dephlegmator of top of the tower control temperature is 40 ℃, isolate the non-condensable gas that contains propane from the return tank top, wherein the propane molar content is 83.0%, and other is a small amount of benzene and other non-aromatics.The isopropyl benzene tower adopts 50 layers of valve tray, and the cat head working pressure is 0.02MPa (g), and the cat head service temperature is 158 ℃.The polyisopropylbenzene tower adopts 40 layers of valve tray, and the cat head working pressure is 20KPa (a), and tower top temperature is 130 ℃.After adopting this technical scheme, from the isopropyl benzene column overhead isopropyl benzene product that to obtain 50 tons of/hour purity be 99.97wt%.Benzene Tata still thermal load is 9.95MW, needs to consume 20.3 tons/hour of 4.0MPa (g) steam.Because the non-aromatic removal tower is without reboiler, so without steam consumption.In addition, the isopropyl benzene tower in present embodiment and the comparative example 2 is identical with the thermal load of polyisopropylbenzene tower, steam consumption too, so no longer list this two item numbers certificate.
[embodiment 3]
The production technique of isopropyl benzene is with embodiment 1, and the propylene take volumetric molar concentration as 80mol% and mass concentration are raw material as 99.8% benzene.Alkylation and transalkylation catalyst adopt the MCM-56 molecular sieve as catalyzer.The molar content of propane is 11.4% in the reacted reaction product of Alkylation benzene with propylene.The benzene tower adopts 60 layers of valve tray, the cat head working pressure is 0.22MPa (g), dephlegmator of top of the tower control temperature is 100 ℃, discharge the gas that contains propane from benzene tower return tank and enter the absorption tower, propane content is 41.1mol% in this strand gaseous phase materials, benzene content is 56.9mol%, other non-aromatic 2.0mol%.This strand material enters the non-aromatic removal tower, and non-aromatic removal column overhead working pressure is 0.15MPa (g), after absorbing from the non-condensable gas that cat head is discharged the volumetric molar concentration of propane be 91mol%.The isopropyl benzene tower adopts 50 layers of valve tray, and the cat head working pressure is 0.02MPa (g), and the cat head service temperature is 158 ℃.The polyisopropylbenzene tower adopts 40 layers of valve tray, and the cat head working pressure is 20KPa (a), and tower top temperature is 130 ℃.After adopting this technical scheme, from the isopropyl benzene column overhead isopropyl benzene product that to obtain 62.5 tons of/hour purity be 99.97wt%.Benzene Tata still thermal load is 12.4MW, needs to consume 25.4 tons/hour of 4.0MPa (g) steam.Because the non-aromatic removal tower is without reboiler, so without steam consumption.In addition, the isopropyl benzene tower in present embodiment and the comparative example 1 is identical with the thermal load of polyisopropylbenzene tower, steam consumption too, so no longer list this two item numbers certificate
[comparative example 1]
Adopt embodiment 1 identical raw material and catalyzer, adopt conventional process techniques as shown in Figure 1 to produce isopropyl benzene.The molar content of propane is 2.5% in the reacted reaction product of Alkylation benzene with propylene, and this material enters depropanizing tower and removes propane, and depropanizing tower is provided with 30 layers of valve tray, and the cat head working pressure is 1.52MPa (g).The benzene tower is provided with 60 layers of valve tray, and the cat head working pressure is 0.05MPa (g).The operational condition of isopropyl benzene tower and polyisopropylbenzene tower is identical with embodiment 1.The isopropyl benzene product that it is 99.97wt% that the isopropyl benzene column overhead obtains 25 tons of/hour purity.Depropanizing tower tower reactor thermal load is 2.2MW, and benzene Tata still thermal load is 5.1MW, needs altogether to consume 15.0 tons/hour of 4.0MPa (g) steam.Increased by 5.0 tons/hour steam consumption than embodiment 1.
[comparative example 2]
Adopt embodiment 2 identical raw material and catalyzer, adopt traditional technology as shown in Figure 1 to produce isopropyl benzene.The molar content of propane is 0.25% in the reacted reaction product of Alkylation benzene with propylene, and this material enters depropanizing tower and removes propane, and depropanizing tower is provided with 30 layers of valve tray, and the cat head working pressure is 1.52MPa (g).The benzene tower is provided with 60 layers of valve tray, and the cat head working pressure is 0.05MPa (g).The operational condition of isopropyl benzene tower and polyisopropylbenzene tower is identical with embodiment 2.The isopropyl benzene product that it is 99.97wt% that the isopropyl benzene column overhead obtains 50 tons of/hour purity.Depropanizing tower tower reactor thermal load is 4.5MW, and benzene Tata still thermal load is 10.2MW, needs altogether to consume 30.1 tons/hour of 4.0MPa (g) steam.Increased by 9.8 tons/hour steam consumption than embodiment 2.
[comparative example 3]
Adopt embodiment 3 identical raw material and catalyzer, adopt traditional technology as shown in Figure 1 to produce isopropyl benzene.The molar content of propane is 10.7% in the reacted reaction product of Alkylation benzene with propylene, and this material enters depropanizing tower and removes propane, and depropanizing tower is provided with 30 layers of valve tray, and the cat head working pressure is 1.52MPa (g).The benzene tower is provided with 60 layers of valve tray, and the cat head working pressure is 0.05MPa (g).The operational condition of isopropyl benzene tower and polyisopropylbenzene tower is identical with embodiment 3.The isopropyl benzene product that it is 99.97wt% that the isopropyl benzene column overhead obtains 60 tons of/hour purity.Depropanizing tower tower reactor thermal load is 5.5MW, and benzene Tata still thermal load is 12.7MW, needs altogether to consume 37.3 tons/hour of 4.0MPa (g) steam.Increased by 11.9 tons/hour steam consumption than embodiment 2.
Claims (10)
1. alkylbenzene production method may further comprise the steps:
A) in the presence of alkylation catalyst, comprise that the mixing raw material of fresh benzene, recycle benzene and alkene enters the alkylation reactor that contains at least two sections beds, enter the benzene tower through the reaction solution after the liquid phase alkylation reaction;
B) in the presence of transalkylation catalyst, the polyalkylbenzene that comprises fresh benzene, recycle benzene and recovery enters transalkylation reactor and carries out the liquid phase transalkylation reaction, and reaction product enters the benzene tower;
C) alkylated reaction liquid and transalkylation reaction liquid enter benzene tower middle part, fresh benzene enters from benzene tower middle and upper part, the top gaseous phase material enters return tank after entering the overhead condenser condensation, non-condensable gas enters d from the return tank of top of the tower discharging) step, the benzene of lateral line withdrawal function enters alkylation reactor and transalkylation reactor as raw material, and benzene tower tower bottoms enters e) step;
D) from c) step come contain alkane, gas non-aromatic and benzene enters the non-aromatic removal tower from the bottom, separate the liquid stream that rear cat head obtains containing the non-condensable gas logistics of alkane and non-aromatics and contains the components such as non-aromatic and benzene, tower reactor obtains the benzene logistics, and c is returned in the logistics of this strand benzene) benzene top of tower in the step;
E) from c) the benzene tower tower bottoms that comes of step enters alkylbenzene tower middle part, and cat head obtains the alkylbenzene product, tower bottoms enters f) step;
F) from e) the alkylbenzene tower tower bottoms that comes of step enters polyalkylbenzene tower middle part, and polyalkylbenzene is sent to transalkylation reactor from cat head or side line extraction, extraction heavy component at the bottom of the polyalkylbenzene tower.
2. alkylbenzene production method according to claim 1 is characterized in that alkene is ethene, propylene; Alkylbenzene is ethylbenzene and isopropyl benzene; Non-condensable gas is ethane or propane; Fresh benzene enters the benzene tower and removes moisture content; The volumetric molar concentration of raw material ethene or propylene is 70～100%; The mass concentration of benzene feedstock is 99.0～100%; Contain ethane or propane, benzene, ethylbenzene or isopropyl benzene component in the alkylated reaction liquid, wherein ethane or propane volumetric molar concentration be 0.001～20%.
3. alkylbenzene production method according to claim 1, it is characterized in that alkylated reaction liquid directly enters the benzene tower and separates without other separation facilities, the theoretical plate number of benzene tower is 20～100, benzene column overhead working pressure is 0.0～1.0MPa (g), the cat head service temperature is 70～200 ℃, and the tower reactor service temperature is 150～300 ℃.
4. alkylbenzene production method according to claim 2 is characterized in that benzene feedstock enters the benzene tower near the position on top, on benzene tower top but extract the benzene raw materials that is used for alkylation and transalkylation reaction out below the benzene feedstock entry position.
5. alkylbenzene production method according to claim 1 is characterized in that through the temperature after the benzene column overhead condenser condenses be 80～150 ℃.
6. alkylbenzene production method according to claim 1 is characterized in that the volumetric molar concentration of ethane in the gaseous phase materials that benzene column overhead return tank discharges or propane is 1～90%.
7. alkylbenzene production method according to claim 1 is characterized in that the mass concentration of benzene in the benzene logistics of benzene tower side line extraction is 70～100%, and side line extraction position is several the 2nd～30 layer of tower tray from top to bottom.
8. alkylbenzene production method according to claim 1, the cat head working pressure that it is characterized in that the non-aromatic removal tower is 0.0～1.0MPa (g), and the cat head service temperature is 40～200 ℃, and theoretical plate number is 2～30.
9. alkylbenzene production method according to claim 1 is characterized in that alkylbenzene column overhead working pressure is-0.1～1.0MPa (g), and the cat head service temperature is 80～250 ℃, and the tower reactor temperature is 150～300 ℃, and theoretical plate number is 10～100.
10. alkylbenzene production method according to claim 1, it is characterized in that polyalkylbenzene tower working pressure is-0.1～0.5MPa (g), the cat head service temperature is 80 ℃～250 ℃, and the tower reactor service temperature is 150～300 ℃, and theoretical plate number is 10～100.
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| CN106278794A (en) * | 2015-06-04 | 2017-01-04 | 常州瑞华化工工程技术有限公司 | The common liquid-phase alkylation of ethylene, propylene produces ethylbenzene and the method and apparatus of isopropylbenzene |
| CN108137433A (en) * | 2015-10-15 | 2018-06-08 | 巴杰许可有限责任公司 | Prepare Alkylaromatics |
| CN109721449A (en) * | 2017-10-31 | 2019-05-07 | 中国石油化工股份有限公司 | A kind of dilute ethylene reacts the method for producing ethylbenzene with benzene |
| CN109851466A (en) * | 2018-12-17 | 2019-06-07 | 实友化工（扬州）有限公司 | A kind of production method of isopropylbenzene |
| CN110093182A (en) * | 2019-04-18 | 2019-08-06 | 江苏中能化学科技股份有限公司 | A kind of alkyl benzene conduction oil and preparation method thereof |
| CN112028732A (en) * | 2020-05-13 | 2020-12-04 | 宁波科元精化股份有限公司 | Method for reducing non-aromatic hydrocarbon at side line of benzene tower |
| CN112250538A (en) * | 2020-11-13 | 2021-01-22 | 万华化学集团股份有限公司 | Cumene refining process flow |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN106278794A (en) * | 2015-06-04 | 2017-01-04 | 常州瑞华化工工程技术有限公司 | The common liquid-phase alkylation of ethylene, propylene produces ethylbenzene and the method and apparatus of isopropylbenzene |
| CN108137433A (en) * | 2015-10-15 | 2018-06-08 | 巴杰许可有限责任公司 | Prepare Alkylaromatics |
| CN109721449A (en) * | 2017-10-31 | 2019-05-07 | 中国石油化工股份有限公司 | A kind of dilute ethylene reacts the method for producing ethylbenzene with benzene |
| CN109851466A (en) * | 2018-12-17 | 2019-06-07 | 实友化工（扬州）有限公司 | A kind of production method of isopropylbenzene |
| CN110093182A (en) * | 2019-04-18 | 2019-08-06 | 江苏中能化学科技股份有限公司 | A kind of alkyl benzene conduction oil and preparation method thereof |
| CN112028732A (en) * | 2020-05-13 | 2020-12-04 | 宁波科元精化股份有限公司 | Method for reducing non-aromatic hydrocarbon at side line of benzene tower |
| CN112250538A (en) * | 2020-11-13 | 2021-01-22 | 万华化学集团股份有限公司 | Cumene refining process flow |
| CN112250538B (en) * | 2020-11-13 | 2023-01-13 | 万华化学集团股份有限公司 | Isopropyl benzene refining process flow |
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