CN1266040A - Catalytic distillation method for production of alkylbenzene - Google Patents
Catalytic distillation method for production of alkylbenzene Download PDFInfo
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Abstract
The catalytic distillation for producing alkylbenzene is implmented in a catalytic distillation tower formed from four sections or five sections, and said catalytic distillation tower possesses from upper to lower in sequence first rectifying section, first reaction section, second rectifying section, second reaction section and stripping section, in which the first rectifying section may not be setup, the benzene and olefine can implement alkylation reaction in the above-mentioned reaction section, and its by-product polyalkylbenzene can implement transalkylation reaction in the second reaction section. Said invention can simultaneously implement alkylation reaction and transalkylation reaction in the same catalytic distillation tower, raise the conversion rate of olefine and selectivity of alkylbenzene, and simplify technological process.
Description
The invention belongs to the method for producing alkylbenzene, more particularly, is the catalytic distillation method of producing alkylbenzene.
Alkylbenzene is the organic industry product with significant application value, and for example isopropyl benzene is an important chemical intermediate of producing phenol, acetone, and ethylbenzene is to produce the cinnamic main raw material of synthetic materials important monomer.Traditional alkylbenzene production method is to be catalyzer with solid phosphoric acid or aluminum chloride, makes benzene and alkene carry out alkylated reaction.But when being catalyzer with the solid phosphoric acid, the polyalkylbenzene that side reaction generates can not further carry out transalkylation, thereby has reduced the yield of purpose product alkylbenzene.With the aluminum chloride is the still formula recirculation reactor of catalyzer, and corrosion and seriously polluted needs with expensive specific equipment.Kai Fa molecular sieve liquid phase fixed bed alkylation process in recent years, catalyzer is free from environmental pollution and renewable, but benzene alkylation is a strong exothermal reaction, traditional fixed-bed process flow process complexity, unit temp is difficult to control, energy consumption is big, and requires high benzene alkene ratio and low-speed.
USP4,849,569 have proposed a kind of catalytic distillation technology, promptly in reaction, finish separating of reactant and resultant, and utilize reaction heat to carry out fractionation by distillation, made full use of the process energy, and owing to reaction product is successively removed, destroy chemical equilibrium, improved the transformation efficiency of reactant and the yield of purpose product.But the member of its filling is catalyzer to be added the Stainless Steel Cloth parcel with woven fiber glass form, and labour intensity is big and mass-transfer efficiency is low, and reaction effect is undesirable.
CN1064475A has proposed a kind of cartridge type catalytic reaction distillation technology in bulk, is characterized in that fixed-bed reactor are put into distillation tower forms conversion zone, and with each bed temperature of Quench Material control between bed, this technology does not make full use of the reaction liberated heat.
USP5,476,978 catalytic distillation technologies that propose are applied to alkylation process, but many alkyl thing content height in its product, reaction conversion ratio, selectivity are not high, need complicated follow-up transalkylation and separating technology.
The method that provides two kinds of high conversions, highly selective, technology simply to produce alkylbenzene on the basis of existing technology is provided.
One of method provided by the invention mainly is to carry out in by first rectifying section, first conversion zone, second rectifying section, second conversion zone, five sections catalytic distillation towers that constitute of stripping section at one, alkene and benzene carry out alkylated reaction at first conversion zone, the by product polyalkylbenzene carries out transalkylation reaction at second conversion zone, and the overhead condensation material all refluxes.
This method is so concrete enforcement: alkene enters in the tower from the first conversion zone bottom, 70～90% benzene feedstock from the first rectifying section top or the first conversion zone top or return tank enter in the tower, the main resultant of first conversion zone is alkylbenzene, polyalkylbenzene, the reaction liberated heat is absorbed by the partial material gasification, gaseous phase materials benzene and unreacted alkene upwards flow through first rectifying section, come out to reflux after condenser condenses from cat head; The alkylbenzene that reaction generates, polyalkylbenzene etc. are carried dense back through second rectifying section and are mixed with the mixture of the benzene feedstock of the polyalkylbenzene that obtains at the bottom of the alkylbenzene separation column and 10～30% downwards and then enter in the tower from second conversion zone.Mainly carry out transalkylation reaction at the above-mentioned material of second conversion zone, reaction product mainly is an alkylbenzene.Product separates through stripping section with the unreacted reactant of part, and unreacted benzene upwards enters second conversion zone; Obtain alkylbenzene at the bottom of the tower and enter reboiler with a small amount of polyalkylbenzene, return in the tower after the gasification of part product, another part enters the alkylbenzene separation column to be separated, and the polyalkylbenzene that alkylbenzene separation column bottom obtains is back to catalytic distillation tower, and the alkylbenzene of cat head then goes out device as product.
The height of catalytic distillation tower and diameter ratio are 5～100: 1, the height of first rectifying section is 0.5～10% of a tower height, the height of first conversion zone is 20～50% of a tower height, the height of second rectifying section is 15～30% of a tower height, the height of second conversion zone is 10～30% of a tower height, and the height of stripping section is 0.5～50% of a tower height.
First rectifying section can be common packing tower section, also can be the tray column section.If packing tower section, wherein filling can be random filler, also can be regular packing.If tray column, its inside can be any one column plates that is suitable for.
Mainly carry out the alkylated reaction of benzene in first conversion zone.The heap catalyzer that looses can be loaded in this conversion zone, also the catalytic distillation structure that includes catalyzer can be loaded.The catalyzer of filling is selected from a kind of in molecular sieve catalyst, storng-acid cation exchange resin, carried heteropoly acid or the heteropolyacid salt.The reaction pressure of first conversion zone is 0.1～5.0 MPa, and temperature is 50～300 ℃.
Second rectifying section can be common packing tower section, also can be the tray column section.If packing tower section, wherein filling can be random filler, also can be regular packing.If tray column, its inside can be any one column plates that is suitable for.The effect of this section is to isolate alkene, guarantees that second conversion zone does not contain alkene.
Mainly carry out the transalkylation reaction of polyalkylbenzene in second conversion zone.Can load the heap catalyzer that looses in this conversion zone, also can load the catalytic distillation structure that includes catalyzer, the catalyzer of filling is selected from a kind of in molecular sieve catalyst, storng-acid cation exchange resin, carried heteropoly acid or the heteropolyacid salt.The catalyzer of this conversion zone filling can be identical with first conversion zone, also can be different.The reaction pressure of second conversion zone is 0.1～5.0 MPa, and temperature is 50～300 ℃.
Stripping section can be common packing tower section, also can be the tray column section.If packing tower section, wherein filling can be random filler, also can be regular packing.If tray column, its inside can be any one column plates that is suitable for.The effect of this section is the benzene of separating residual.
In method provided by the invention, when catalyst for alkylation reaction is identical with the transalkylation reaction catalyzer, disclosed molecular sieve catalyst among the preferred CN1096470A, it has, and transformation efficiency height, selectivity are good, the advantage of activity and good stability.When this catalyzer was used for alkylated reaction and transalkylation reaction, the reaction pressure of first conversion zone was 0.4～2.0 MPa, and temperature is 100～250 ℃; The reaction pressure of second conversion zone is 0.4～2.0 MPa, and temperature is 200～300 ℃.
Can load the heap catalyzer that looses in the present invention's first conversion zone and second conversion zone, also can load the catalytic distillation structure that includes catalyzer, preferred catalytic distillation member.Two sections fills can be identical, also can be different.The composite component that catalytic distillation structure is made up of filler and catalyzer, the top of member is the distribution disengaging zone, can be random filler such as Raschig ring, Pall ring, saddle packing etc. in the district, also can be regular packing such as corrugated plate type, grid type, honeycomb type etc.; The bottom of member is a reaction zone, filling solid acid catalyst in the reaction zone.The relative dimension in two districts, member upper and lower can specifically be determined according to practical situation by those skilled in the art.Member can huddle, and also can put in order block.The voidage of member is 30～95%, so member has good gas-liquid distribution performance, low pressure drop, competent place of carrying out chemical reaction can be provided, and activity of such catalysts is given full play to.
When the heap catalyzer is loose in filling in first conversion zone or second conversion zone, must place the inertia support at the orlop of this section, this support should have enough spaces to guarantee that material passes through smoothly.
The total amount of benzene and olefin molar ratio are 1～8: 1 in the inventive method.In order to obtain high benzene alkylation reaction selectivity, usually need excessive benzene and olefine reaction, but owing to adopt the catalytic distillation structure of low pressure drop among the present invention, make the quantity of reflux of overhead benzene higher, therefore total amount and the olefin molar ratio at benzene is 1～8: 1 o'clock high conversion and highly selective with regard to guaranteeing to react.
It is the process that raw material carries out alkylated reaction synthesis of alkyl benzene that the present invention is suitable for low-molecular olefine and benzene, and the raw material low-molecular olefine one of is selected from ethene, propylene, n-butene, iso-butylene or the 2-butylene, or the mixture of above-mentioned two or more alkene.
Another kind of method provided by the invention mainly is to carry out in by first conversion zone, rectifying section, second conversion zone, four sections catalytic distillation towers that constitute of stripping section at one, alkene and benzene carry out alkylated reaction at first conversion zone, the by product polyalkylbenzene carries out transalkylation reaction at second conversion zone, and the overhead condensation material all refluxes.
This method is so concrete enforcement: alkene enters in the tower from the first conversion zone bottom, 70～90% benzene feedstock enters in the tower from the first conversion zone top or return tank, the main resultant of first conversion zone is alkylbenzene, polyalkylbenzene, the reaction liberated heat is absorbed by the partial material gasification, and gaseous phase materials benzene and unreacted alkene come out to reflux after condenser condenses from cat head; The alkylbenzene that reaction generates, polyalkylbenzene etc. are carried dense back through rectifying section and are mixed with the mixture of the benzene feedstock of the polyalkylbenzene that obtains at the bottom of the alkylbenzene separation column and 10～30% downwards and then enter in the tower from second conversion zone.Mainly carry out transalkylation reaction at the above-mentioned material of second conversion zone, reaction product mainly is an alkylbenzene.Product separates through stripping section with the unreacted reactant of part, and unreacted benzene upwards enters second conversion zone; Obtain alkylbenzene at the bottom of the tower and enter reboiler with a small amount of polyalkylbenzene, return in the tower after the gasification of part product, another part enters the alkylbenzene separation column to be separated, and the polyalkylbenzene that alkylbenzene separation column bottom obtains is back to catalytic distillation tower, and the alkylbenzene of cat head then goes out device as product.
The height of catalytic distillation tower and diameter ratio are 5～100: 1, the height of first conversion zone is 20～50% of a tower height, the height of rectifying section is that the height of 15～30%, second conversion zone of tower height is 10～30% of a tower height, and the height of stripping section is 0.5～50% of a tower height.
Mainly carry out the alkylated reaction of benzene in first conversion zone.The heap catalyzer that looses can be loaded in this conversion zone, also the catalytic distillation structure that includes catalyzer can be loaded.The catalyzer of filling is selected from a kind of in molecular sieve catalyst, storng-acid cation exchange resin, carried heteropoly acid or the heteropolyacid salt.The reaction pressure of first conversion zone is 0.1～5.0 MPa, and temperature is 50～300 ℃.
Rectifying section can be common packing tower section, also can be the tray column section.If packing tower section, wherein filling can be random filler, also can be regular packing.If tray column, its inside can be any one column plates that is suitable for.The effect of this section is to isolate alkene, guarantees that second conversion zone does not contain alkene.
Mainly carry out the transalkylation reaction of polyalkylbenzene in second conversion zone.Can load the heap catalyzer that looses in this conversion zone, also can load the catalytic distillation structure that includes catalyzer, the catalyzer of filling is selected from a kind of in molecular sieve catalyst, storng-acid cation exchange resin, carried heteropoly acid or the heteropolyacid salt.The catalyzer of this conversion zone filling can be identical with first conversion zone, also can be different.The reaction pressure of second conversion zone is 0.1～5.0 MPa, and temperature is 50～300 ℃.
Stripping section can be common packing tower section, also can be the tray column section.If packing tower section, wherein filling can be random filler, also can be regular packing.If tray column, its inside can be any one column plates that is suitable for.The effect of this section is the benzene of separating residual.
In method provided by the invention, when catalyst for alkylation reaction is identical with the transalkylation reaction catalyzer, disclosed molecular sieve catalyst among the preferred CN1096470A, it has, and transformation efficiency height, selectivity are good, the advantage of activity and good stability.When this catalyzer was used for alkylated reaction and transalkylation reaction, the reaction pressure of first conversion zone was 0.4～2.0 MPa, and temperature is 100～250 ℃; The reaction pressure of second conversion zone is 0.4～2.0 MPa, and temperature is 200～300 ℃.
Can load the heap catalyzer that looses in the present invention's first conversion zone and second conversion zone, also can load the catalytic distillation structure that includes catalyzer, preferred catalytic distillation member.Two sections fills can be identical, also can be different.The composite component that catalytic distillation structure is made up of filler and catalyzer, the top of member is the distribution disengaging zone, can be random filler such as Raschig ring, Pall ring, saddle packing etc. in the district, also can be regular packing such as corrugated plate type, grid type, honeycomb type etc.; The bottom of member is a reaction zone, filling solid acid catalyst in the reaction zone.The relative dimension in two districts, member upper and lower can specifically be determined according to practical situation by those skilled in the art.Member can huddle, and also can put in order block.The voidage of member is 30～95%, so member has good gas-liquid distribution performance, low pressure drop, competent place of carrying out chemical reaction can be provided, and activity of such catalysts is given full play to.
When the heap catalyzer is loose in filling in first conversion zone or second conversion zone, must place the inertia support at the orlop of this section, this support should have enough spaces to guarantee that material passes through smoothly.
The total amount of benzene and olefin molar ratio are 1～8: 1 in the inventive method.In order to obtain high benzene alkylation reaction selectivity, usually need excessive benzene and olefine reaction, but owing to adopt the catalytic distillation structure of low pressure drop among the present invention, make the quantity of reflux of overhead benzene higher, therefore total amount and the olefin molar ratio at benzene is 1～8: 1 o'clock high conversion and highly selective with regard to guaranteeing to react.
It is the process that raw material carries out alkylated reaction synthesis of alkyl benzene that the present invention is suitable for low-molecular olefine and benzene, and the raw material low-molecular olefine one of is selected from ethene, propylene, n-butene, iso-butylene or the 2-butylene, or the mixture of above-mentioned two or more alkene.
Below in conjunction with accompanying drawing method provided by the present invention is given further instruction.
Accompanying drawing 1 is a method flow synoptic diagram of producing alkylbenzene on five sections catalytic distillation towers provided by the invention.
The used catalytic distillation tower of this method is divided into five sections, is followed successively by from top to bottom: the first rectifying section I, the first conversion zone II, the second rectifying section III, the second conversion zone IV, stripping section V.
The technical process of this method is as follows: alkene enters catalytic distillation tower 2 through pipeline 1 from the first conversion zone II bottom, benzene feedstock 70～90% through pipeline 3 from the first rectifying section I top or the first conversion zone top or return tank 4 enter in the tower, 10～30% of benzene feedstock enters in the tower from the second conversion zone IV top through pipeline 5.Alkene and benzene mainly generate alkylbenzene, polyalkylbenzene at the first conversion zone internal reaction.The reaction liberated heat is absorbed by the partial material gasification.Liquid phase materials such as the alkylbenzene that reaction generates, polyalkylbenzene flow downward through the second rectifying section III.Enter in the tower from the second conversion zone top through pipeline 7 from alkylbenzene separation column 6 isolating polyalkylbenzene, and mix with the liquid phase stream that flows downward.The above-mentioned liquid phase stream of second conversion zone with carry out transalkylation reaction from the excessive benzene of pipeline 5, reaction product mainly is an alkylbenzene.Reaction product through stripping section V carry dense after, obtain an alkylbenzene and an a small amount of polyalkylbenzene part at the bottom of the tower and enter reboiler 9 gasifications after pipeline 10 returns in the tower through pipeline 8, another part enters the alkylbenzene separation column through pipeline 11, the polyalkylbenzene that alkylbenzene separation column bottom obtains enters catalytic distillation tower through pipeline 7 from the second conversion zone top, and the alkylbenzene that alkylbenzene separation column top obtains is through pipeline 12 caterpillars.The gaseous stream that first conversion zone generates separates through the first rectifying section I, and lower boiling benzene and unreacted alkene enter condenser 14 condensations through pipeline 13, enter return tank 4 through pipeline 15 again, and in tower, alkene is through pipeline 17 caterpillars through pipeline 16 total refluxs for benzene.
Accompanying drawing 2 is a method flow synoptic diagram of producing alkylbenzene on four sections catalytic distillation towers provided by the invention.
The used catalytic distillation tower of this method is divided into four sections, is followed successively by from top to bottom: the first conversion zone I, rectifying section II, the second conversion zone III, stripping section IV.
The technical process of this method is as follows: alkene enters catalytic distillation tower 2 through pipeline 1 from the first conversion zone I bottom, 70～90% of benzene feedstock enters in the tower from the first conversion zone top or return tank 4 through pipeline 3, and 10～30% of benzene feedstock enters in the tower from the second conversion zone III top through pipeline 5.Alkene and benzene mainly generate alkylbenzene, polyalkylbenzene at the first conversion zone internal reaction.The reaction liberated heat is absorbed by the partial material gasification.Liquid phase materials such as the alkylbenzene that reaction generates, polyalkylbenzene flow downward through rectifying section II.Enter in the tower from the second conversion zone top through pipeline 7 from alkylbenzene separation column 6 isolating polyalkylbenzene, and mix with the liquid phase stream that flows downward.The above-mentioned liquid phase stream of second conversion zone with carry out transalkylation reaction from the excessive benzene of pipeline 5, reaction product mainly is an alkylbenzene.Reaction product through stripping section IV carry dense after, obtain an alkylbenzene and an a small amount of polyalkylbenzene part at the bottom of the tower and enter reboiler 9 gasifications after pipeline 10 returns in the tower through pipeline 8, another part enters the alkylbenzene separation column through pipeline 11, the polyalkylbenzene that alkylbenzene separation column bottom obtains enters catalytic distillation tower through pipeline 7 from the second conversion zone IV top, and the alkylbenzene that alkylbenzene separation column top obtains is through pipeline 12 caterpillars.The gaseous stream that first conversion zone generates enters condenser 14 condensations through pipeline 13, enters return tank 4 through pipeline 15 again, and in tower, alkene is through pipeline 17 caterpillars through pipeline 16 total refluxs for benzene.
Method provided by the invention compared with prior art, can guarantee that alkylated reaction, transalkylation reaction carry out simultaneously in same catalytic distillation tower, realization response section product separates simultaneously with reactant, the selectivity of conversion of olefines rate height, alkylbenzene is good, reaction space-time yield height, the mol ratio of benzene feedstock and alkene is low, and benzene and alkene raw materials components mole ratio then can be up to more than 10 in the prior art.
Accompanying drawing 1 is a method flow synoptic diagram of producing alkylbenzene on five sections catalytic distillation towers provided by the invention.
Accompanying drawing 2 is a method flow synoptic diagram of producing alkylbenzene on four sections catalytic distillation towers provided by the invention.
The following examples will give further instruction to method provided by the invention, but not thereby limiting the invention.
Employed alkylation catalyst is identical with transalkylation catalyst among the embodiment, and its trade names are AEB, is the catalyst plant production of Qilu Petrochemical company.
At an ethene and a benzene preparing ethylbenzene by reaction that carries out on by five sections catalytic distillation towers that constitute.
32 millimeters of the internal diameters of this catalytic distillation tower, high 2600 millimeters, wherein first rectifying section is high 250 millimeters, and first conversion zone is high 900 millimeters, and second rectifying section is high 550 millimeters, and second conversion zone is high 700 millimeters, and stripping section is high 200 millimeters.
Ethene enters in the tower from the first conversion zone bottom, and 90% of benzene feedstock enters in the tower from the first rectifying section top, and 10% of benzene feedstock enters in the tower from the second conversion zone top.Ethene and benzene react at first conversion zone, mainly generate ethylbenzene, diethylbenzene.The heat that reaction is emitted is absorbed by the partial material gasification.The material that ethylbenzene, diethylbenzene and other boiling points that reaction generates is higher than benzene flows downward through second rectifying section, and diethylbenzene is wherein carried in this section enters second conversion zone after dense.Carry out transalkylation reaction in second conversion zone and the excessive benzene of introducing from this section top, reaction product mainly is an ethylbenzene.Reaction product is after stripping section separates, after entering the reboiler gasification, an ethylbenzene that obtains at the bottom of the tower and an a small amount of diethylbenzene part return in the tower, another part enters the ethylbenzene separation column, and the diethylbenzene at the bottom of the tower returns catalytic distillation tower from the second conversion zone top, the ethylbenzene caterpillar of cat head.The gaseous stream that first conversion zone generates, after first rectifying section separated, lower boiling benzene entered the return tank total reflux in tower through condenser, and the unreacted ethene of minute quantity is from return tank emptying.
The mol ratio of benzene feed and ethene is 1: 1, and reaction conditions and result are as shown in table 1.The result shows that the transformation efficiency of ethene is greater than 95%, and the selectivity of ethylbenzene can reach more than 90%.
At a propylene that carries out on by four sections catalytic distillation towers that constitute and benzene reaction preparing isopropylbenzene.
32 millimeters of the internal diameters of this catalytic distillation tower, high 2600 millimeters, wherein first conversion zone is high 900 millimeters, and rectifying section is high 500 millimeters, and second conversion zone is high 700 millimeters, and stripping section is high 500 millimeters.
Propylene enters in the tower from the first conversion zone bottom, and 80% of benzene feedstock enters in the tower from the first conversion zone top respectively, and 20% of benzene feedstock enters in the tower from the second conversion zone top.Propylene and benzene react at first conversion zone, mainly generate isopropyl benzene, polyisopropylbenzene (mainly being diisopropylbenzene(DIPB)).The heat that reaction is emitted is absorbed by the partial material gasification.Isopropyl benzene, polyisopropylbenzene and other boiling points that reaction generates is higher than the material of benzene and carried dense back inflow second conversion zone downwards through rectifying section.Carry out transalkylation reaction in second conversion zone and the excessive benzene that enters from this section top, reaction product mainly is an isopropyl benzene.Reaction product is separated purification through stripping section, obtain at the bottom of the tower returning in the tower after an isopropyl benzene and an a small amount of polyisopropylbenzene part enter the reboiler gasification, another part enters the isopropyl benzene separation column, and the polyisopropylbenzene at the bottom of the tower returns catalytic distillation tower from the second conversion zone top, the isopropyl benzene caterpillar of cat head.The material that first conversion zone generates enters the return tank total reflux in tower through condenser, and the unreacted propylene of minute quantity is from return tank emptying.
The mol ratio of benzene and propylene is 1: 1, and reaction conditions and result are as shown in table 2.The result shows that propylene conversion reaches more than 99%, and the isopropyl benzene selectivity is greater than 90%.
Table 1
| The test sequence number | ????1 | ????2 | ????3 |
| The ethene mass space velocity, hour -1 | ??0.33 | ??0.20 | ??0.24 |
| Reaction pressure (gauge pressure), MPa | ??0.75 | ??0.8 | ??1.05 |
| The first conversion zone temperature, ℃ | ??168 | ??172 | ??186 |
| The second conversion zone temperature, ℃ | ??209 | ??210 | ??218 |
| Column bottom temperature, ℃ | ??244 | ??251 | ??261 |
| Discharging at the bottom of the tower, Grams Per Hour | ??78.6 | ??48 | ??58.6 |
| Tower still material is formed, heavy % | |||
| Benzene | ??2.04 | ??0.19 | ??0.24 |
| Ethylbenzene | ??95.75 | ??96.97 | ??96.95 |
| Diethylbenzene | ??2.21 | ??2.84 | ??2.81 |
| Ethylbenzene/diethylbenzene | ??43 | ??34 | ??34 |
| The ethylbenzene space-time yield, gram/gram catalyzer hour | ??1.16 | ??0.72 | ??0.87 |
Table 2
| The test sequence number | ??1 | ????2 | ????3 | ????4 | ????5 |
| Reaction pressure (gauge pressure), MPa | 0.65 | ?1.08 | ?1.10 | ?1.11 | ?1.10 |
| The first conversion zone temperature, ℃ | 160 | ?192 | ?193 | ?194 | ?194 |
| The second conversion zone temperature, ℃ | 201 | ?220 | ?220 | ?221 | ?225 |
| Inlet amount, Grams Per Hour | |||||
| Benzene | 61 | ?122 | ?106 | ?300 | ?444 |
| Propylene | 34 | ?67 | ?58 | ?164 | ?239 |
| Air speed (in the propylene quality), hour -1 | 0.45 | ?0.89 | ?0.77 | ?2.19 | ?3.19 |
| Tower still material is formed, heavy % | |||||
| Benzene | Trace | Trace | Trace | Trace | ?0.05 |
| Isopropyl benzene | 94.04 | ?96.42 | ?95.74 | ?91.36 | ?91.04 |
| Polyisopropylbenzene | 5.96 | ?3.58 | ?4.26 | ?8.64 | ?8.91 |
| Isopropyl benzene/polyisopropylbenzene | 15.8 | ?26.9 | ?22.5 | ?10.6 | ?10.2 |
| The isopropyl benzene space-time yield, gram/gram catalyzer hour | 1.18 | ?2.41 | ?2.08 | ?5.63 | ?8.29 |
Claims (18)
1, a kind of catalytic distillation method of producing alkylbenzene, be included in catalytic distillation tower internal olefin and benzene and carry out alkylated reaction, obtain reaction product at the bottom of the tower, the overhead condensation material all refluxes, it is characterized in that using one by first rectifying section, first conversion zone, second rectifying section, second conversion zone, five sections catalytic distillation towers of forming of stripping section, alkene and benzene carry out alkylated reaction at first conversion zone, and the by product polyalkylbenzene carries out transalkylation reaction at second conversion zone.
2, press the method for claim 1, the height and the diameter ratio that it is characterized in that described catalytic distillation tower are 5～100: 1, the height of first rectifying section is 0.5～10% of a tower height, the height of first conversion zone is 20～50% of a tower height, the height of second rectifying section is 15～30% of a tower height, the height of second conversion zone is 10～30% of a tower height, and the height of stripping section is 0.5～50% of a tower height.
3, by the method for claim 1, it is characterized in that 70～90% benzene feedstock from the first rectifying section top or the first conversion zone top or return tank enter in the tower, 10～30% benzene feedstock enters in the tower from the second conversion zone top.
4, by the method for claim 1, it is characterized in that described alkene is selected from ethene, propylene, n-butene, iso-butylene or the 2-butylene, or the mixture of above-mentioned two or more alkene.
5,, it is characterized in that entering the benzene total amount of catalytic distillation tower and the mol ratio of alkene is 1～8: 1 by the method for claim 1.
6, by the method for claim 1, it is characterized in that the reaction conditions of first conversion zone and second conversion zone is: pressure 0.1～5.0 MPa, 50～300 ℃ of temperature.
7, by the method for claim 1, a part that it is characterized in that polyalkylbenzene is that the reaction product separation obtains at the bottom of tower, returns from the top of catalytic distillation tower second conversion zone; Another part is the by product of first conversion zone, carries through second rectifying section and enters second conversion zone after dense.
8, by the method for claim 1, it is characterized in that can loading in first conversion zone and second conversion zone heap catalyzer that looses, also can load the catalytic distillation structure that includes catalyzer, two sections fills can be identical, also can be different.
9,, it is characterized in that described catalyzer is selected from a kind of in molecular sieve catalyst, storng-acid cation exchange resin, carried heteropoly acid or the heteropolyacid salt by the method for claim 1.
10, a kind of catalytic distillation method of producing alkylbenzene, be included in catalytic distillation tower internal olefin and benzene and carry out alkylated reaction, obtain reaction product at the bottom of the tower, the overhead condensation material all refluxes, it is characterized in that using one by first conversion zone, rectifying section, second conversion zone, four sections catalytic distillation towers of forming of stripping section, alkene and benzene carry out alkylated reaction at first conversion zone, and the by product polyalkylbenzene carries out transalkylation reaction at second conversion zone.
11, press the method for claim 10, the height and the diameter ratio that it is characterized in that described catalytic distillation tower are 5～100: 1, the height of first conversion zone is 20～50% of a tower height, the height of rectifying section is 15～30% of a tower height, the height of second conversion zone is 10～30% of a tower height, and the height of stripping section is 0.5～50% of a tower height.
12, by the method for claim 10, it is characterized in that 70～90% benzene feedstock enters in the tower from the first conversion zone top or return tank, 10～30% benzene feedstock enters in the tower from the second conversion zone top.
13, by the method for claim 10, it is characterized in that described alkene is selected from ethene, propylene, n-butene, iso-butylene or the 2-butylene, or the mixture of above-mentioned two or more alkene.
14,, it is characterized in that entering the benzene total amount of catalytic distillation tower and the mol ratio of alkene is 1～8: 1 by the method for claim 10.
15, by the method for claim 10, it is characterized in that the reaction conditions of first conversion zone and second conversion zone is: pressure 0.1～5.0 MPa, 50～300 ℃ of temperature.
16, by the method for claim 10, a part that it is characterized in that polyalkylbenzene is that the reaction product separation obtains at the bottom of tower, returns from the second conversion zone top of catalytic distillation tower; Another part is the by product of first conversion zone, carries through rectifying section and enters second conversion zone after dense.
17, by the method for claim 10, it is characterized in that can loading in first conversion zone and second conversion zone heap catalyzer that looses, also can load the catalytic distillation structure that includes catalyzer, two sections fills can be identical, also can be different.
18,, it is characterized in that described catalyzer is selected from a kind of in molecular sieve catalyst, storng-acid cation exchange resin, carried heteropoly acid or the heteropolyacid salt by the method for claim 10.
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| Application Number | Priority Date | Filing Date | Title |
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| CN99102801A CN1085644C (en) | 1999-03-05 | 1999-03-05 | Catalytic distillation method for production of alkylbenzene |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN99102801A CN1085644C (en) | 1999-03-05 | 1999-03-05 | Catalytic distillation method for production of alkylbenzene |
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| CN1266040A true CN1266040A (en) | 2000-09-13 |
| CN1085644C CN1085644C (en) | 2002-05-29 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN99102801A Expired - Fee Related CN1085644C (en) | 1999-03-05 | 1999-03-05 | Catalytic distillation method for production of alkylbenzene |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1834075B (en) * | 2005-03-17 | 2012-09-05 | 催化蒸馏技术公司 | Process for the co-production of cumene and secondary butyl benzene |
| CN110002937A (en) * | 2019-04-29 | 2019-07-12 | 南京克米斯璀新能源科技有限公司 | Linear alkylbenzene (LAB) production technology and linear alkylbenzene (LAB) production equipment |
| CN112316856A (en) * | 2020-09-01 | 2021-02-05 | 河北工业大学 | Equipment and method for producing ethylbenzene by catalytic reaction distillation with concentrated ethylene as raw material |
| CN113019265A (en) * | 2021-03-16 | 2021-06-25 | 中国恩菲工程技术有限公司 | Reaction device and method for preparing final product by using same |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5476978A (en) * | 1989-09-05 | 1995-12-19 | Chemical Research & Licensing Company | Process for the preparation of ethyl benzene |
| CN1029309C (en) * | 1991-12-04 | 1995-07-12 | 齐鲁石油化工公司研究院 | Process for alkylating aromatic hydrocarbon |
| FR2684893A1 (en) * | 1991-12-16 | 1993-06-18 | Inst Francais Du Petrole | CATALYTIC REACTIVE DISTILLATION METHOD AND APPARATUS FOR ITS IMPLEMENTATION. |
-
1999
- 1999-03-05 CN CN99102801A patent/CN1085644C/en not_active Expired - Fee Related
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1834075B (en) * | 2005-03-17 | 2012-09-05 | 催化蒸馏技术公司 | Process for the co-production of cumene and secondary butyl benzene |
| CN110002937A (en) * | 2019-04-29 | 2019-07-12 | 南京克米斯璀新能源科技有限公司 | Linear alkylbenzene (LAB) production technology and linear alkylbenzene (LAB) production equipment |
| CN112316856A (en) * | 2020-09-01 | 2021-02-05 | 河北工业大学 | Equipment and method for producing ethylbenzene by catalytic reaction distillation with concentrated ethylene as raw material |
| CN113019265A (en) * | 2021-03-16 | 2021-06-25 | 中国恩菲工程技术有限公司 | Reaction device and method for preparing final product by using same |
| CN113019265B (en) * | 2021-03-16 | 2022-09-20 | 中国恩菲工程技术有限公司 | Reaction device and method for preparing final product by using same |
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| Publication number | Publication date |
|---|---|
| CN1085644C (en) | 2002-05-29 |
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