CN102276410B - Method for synthesizing ethylbenzene - Google Patents
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Abstract
The invention relates to a method for synthesizing ethylbenzene, and mainly solves the problems that ethylene must be taken as a raw material, the cost of the raw material is high and the content of dimethylbenzene is high in the product ethylbenzene in the conventional ethylbenzene production process. The method comprises the following steps that: a) benzene and ethanol enter an alkylation reactor loaded with a ZSM-5 nanoscale molecular sieve catalyst in a molar ratio of (2-8):1 under gas phase conditions and react to form a mixture 103 comprising benzene, ethylbenzene, diethylbenzene and water; b) the mixture 103 sequentially passes through a benzene recovery tower, an ethylbenzene recovery tower and a polyethylbenzene recovery tower so as to separate the water, the benzene, the ethylbenzene and the diethylbenzene from the mixture 103; and c) the partial benzene and diethylbenzene which are obtained through the separation enter a transalkylation reactor in a weight ratio of (2-10):1 under liquid phase conditions and are contacted with a Beta molecular sieve catalyst for a transalkylation reaction so as to generate the ethylbenzene. The technical scheme better solves the problems; in the scheme, the ethylbenzene is synthesized by using the ethanol as the raw material instead of the ethylene, the cost of the raw material is low, and the content of the dimethylbenzene in the product ethylbenzene is low; and the technical scheme can be used for the industrial production of the ethylbenzene.
Description
Technical field
The present invention relates to a kind of synthetic method of ethylbenzene, mainly solve in the past that ethylbenzene production technique must rely on that ethene is that raw material, raw materials cost are high, the high problem of xylene content in product ethylbenzene.
Background technology
Ethylbenzene is important industrial chemicals, is to produce the indispensable critical materials of vinylbenzene, and the object that most of ethylbenzene manufacturers produce ethylbenzene is to produce vinylbenzene for the styrene device of oneself, and about more than 90% ethylbenzene is for the production of vinylbenzene.And vinylbenzene is important basic organic chemical industry raw material, be mainly used in polymeric material field and produce polystyrene and multipolymer thereof, as ABS, AS, styrene-butadiene rubber(SBR) and unsaturated polyester thereof, in addition, vinylbenzene is also widely used in pharmacy, coating, pigment and textile industry as organic reaction intermediate.Along with automotive industry, isolator industry, packaging industry and daily necessities industry, along with the growing demand to styrene monomer, the ethylbenzene throughput in the world is also in continuous increase.
Industrial, absolutely large number ethylbenzene is that the alkylated reaction by benzene and ethene is synthesized into, normally at aluminum oxide, under the silica-alumina catalyst of silicon oxide-aluminum oxide and so on exists, benzene and ethylene reaction are manufactured to ethylbenzene, reaction be generally in 350～500 ℃ of temperature ranges and the pressure condition of 0.5～2MPaG under, in gas phase, carry out, the reaction product overwhelming majority is ethylbenzene, also has in addition the seldom light constituent of amount, propyl benzene, butylbenzene, diphenyl compounds and high-boiling-point impurity etc., benzene and many ethylbenzene are at the lower transalkylation reaction that carries out of transalkylation reactor gas phase condition, xylene content in product ethylbenzene is higher, conventionally more than 1000ppm, concrete document has Chinese patent ZL97106648.2, ZL02155114, ZL97106448.2.
Traditional benzene alkylation with ethylene process for preparing ethylbenzene must be take ethene as raw material, as the petroleum naphtha of ethylene raw from crude oil, along with the day by day soaring and day by day exhaustion of crude oil price, ethylene raw cost constantly increases thereupon, and the regional ethene source lacking at oil is just restricted.Industrial producing ethylene from dehydration of ethanol was once main ethylene industry production method, from eighties of last century since mid-term, petrochemical industry develops rapidly, ethylene industry transfers to take the thermo-cracking route that petroleum naphtha is raw material, along with the fast development of national economy, crude oil in China total quantity consumed increases year by year, a large amount of imported crude oils of having to, the energy security situation of China is more and more severeer, and we find new resource an urgent demand.
The develop rapidly of biochemical technology significantly reduces the production cost of biomass-making ethanol, for exploitation ethanol process for preparing ethylbenzene provides possibility.At present, bio-ethanol, except adopting farm crop corn, cassava etc., be fermentation raw material, also can be fermentation raw material with crop straw, be expected further to reduce alcohol production cost, biomass ethanol is clean renewable resources simultaneously, industrial at present, for reducing raw materials cost and expanding ethene source, conventionally with ethanol dehydration, obtain needed ethene, then with traditional ethene and benzene alkylation technique synthesizing ethyl benzene, concrete document there is Chinese patent ZL200810043303.6, ZL200610114032.X, ZL200610029972.9.
But ethanol dehydration technique needs lot of energy, in dehydration reaction process, also can there are some side reactions, ethanol utilization ratio is low, adds that the increase of investment and process cost has reduced ethanol raw material advantage cheap and easy to get.
Summary of the invention
Technical problem to be solved by this invention be technical problem to be solved by this invention be in the past ethylbenzene production technique must to rely on ethene be the high problem of xylene content in raw material, product ethylbenzene, a kind of synthetic method of new ethylbenzene is provided, and the method has advantages of can use that ethanol substitutes that ethene is low as raw material and benzene synthesizing ethyl benzene, raw materials cost, xylene content is low in product ethylbenzene.
For solving the problems of the technologies described above, the technical solution used in the present invention is as follows: a kind of synthetic method of ethylbenzene, comprise the following steps: a) ethanol and benzene, by entering alkylation reactor that ZSM-5 nanoscale molecular sieve catalyst be housed react at 2～8: 1 in molar ratio under gas phase condition, obtain comprising the mixture 103 of benzene, ethylbenzene, diethylbenzene and water; B) mixture 103, successively by benzene recovery tower, ethylbenzene recovery tower, many ethylbenzene recovery tower, is isolated water, benzene, ethylbenzene and diethylbenzene wherein; C) the part benzene that separation obtains enters transalkylation reactor by weight 2～10: 1 with diethylbenzene and contacts and carry out transalkylation reaction with Beta molecular sieve catalyst under liquid-phase condition, generates ethylbenzene.
In technique scheme, alkylated reaction temperature is 320 ℃～450 ℃, and reaction pressure is 0.5～2.0MPa, and ethanol weight space velocity is 0.6～2.5 hour
-1, benzene and ethanol mol ratio are 4.0～7.0: 1; Benzene recovery tower working pressure is 0.4～2.0MPaG, 125～200 ℃ of tower top temperatures, 200～300 ℃ of tower reactor temperature, reflux ratio 0.8～2; Ethylbenzene recovery tower working pressure is 0.0～0.5MPaG, 135～200 ℃ of tower top temperatures, 190～250 ℃ of tower reactor temperature, reflux ratio 2～6; Many ethylbenzene recovery tower working pressure is-0.1～0.2MPaG, 100～220 ℃ of tower top temperatures, 190～250 ℃ of tower reactor temperature, reflux ratio 0.1～2; Transalkylation reactor temperature of reaction is 150 ℃～280 ℃, and reaction pressure is 2.0～3.5MPaG, and liquid weight air speed is 1.0～3.0 hours
-1, benzene and many ethylbenzene weight ratio are 3～6: 1.
The present invention is mixed into by ethanol and benzene are pressed in high temperature the alkylation reactor that ZSM-5 nanoscale molecular sieve catalyst is housed under gas phase condition, in reactor, there is ethanol dehydration simultaneously and generate the reaction that ethene and ethene and benzene alkylation generate ethylbenzene, generate object product ethylbenzene, that technique of the present invention has advantages of is corrosion-free, pollution-free, flow process is simple and heat energy recovery rate is high.With respect to ethene, ethanol is renewable resources, and raw material is easy to get, and compares with the trend that current oil price rises steadily, and the advantage that ethanol is raw material will be day by day obvious.
The alkylation of ethanol dehydration reaction and ethene and benzene completes in a reactor simultaneously, the required heat of ethanol dehydration is supplied by the heat release of alkylated reaction, ethene and benzene that ethanol dehydration generates carry out alkylation under high temperature, middle pressure gas phase condition, 400 ℃ of left and right of temperature of reaction, pressure < 2.0MPaG, gas-phase reaction can make reactant mix; Reactor has been used and has met the ZSM-5 nanoscale molecular sieve catalyst that ethanol dehydration and ethylene alkylation carry out particular requirement simultaneously, and the selectivity of ethanol dehydration and transformation efficiency are very high, and ethene also can reach the level that ethylene process is identical with the transformation efficiency of benzene alkylation.Compare traditional ethanol substep Dehydration ethene, then make derived product by ethene, the technique that ethanol dehydration is carried out relatively separately in the side reaction of ethanol dehydration is few, technical process is simple, reduced investment, and process cost is low, there is obvious advantage, also better solved the difficult problem that alcohol dewatering apparatus maximizes.
In the present invention, benzene excessive in benzene and ethanol synthesis is recycled by the benzene tower arranging, in benzene column overhead phlegma except containing benzene, also has a certain amount of water (ethanol dehydration generation), benzene column overhead condenser is also oily water separating equipment simultaneously, by this equipment, divide and anhydrate, can be used as after treatment recirculated water or feedwater uses, reduced the energy consumption of device, divide the benzene after anhydrating partly to return to alkylation reactor, part is removed transalkylation reactor, arranging of divisor reduced the water-content in recycle benzene, extended the life-span of catalyzer, reduced side reaction simultaneously.
For improving ethylbenzene output, reduce the growing amount of many ethylbenzene, the present invention is provided with transalkylation reactor, in conventional art, transalkylation reaction is gas-phase reaction, temperature of reaction is higher, reach more than 400 ℃, in reactor, there is side reaction more, cause the difficulty of irreversible loss and the product separation of ethylbenzene, by product dimethylbenzene particularly, mainly by ethylbenzene isomerization reaction, be transformed, the generation of dimethylbenzene has not only reduced the yield of ethylbenzene, also can take in derived product vinylbenzene and go, and affects Quality of Styrene.The present invention adopts liquid phase transalkylation reaction technique, benzene contacts and carries out transalkylation reaction with Beta molecular sieve catalyst under high pressure low temperature liquid-phase condition with many ethylbenzene, reduction (250 ℃ following) due to temperature, effectively reduced ethylbenzene isomerization reaction, in ethylbenzene, xylene content obviously reduces, and reduces temperature of reaction simultaneously and also can reduce a large amount of energy consumptions.
Adopt technical solution of the present invention, ethanol can generate ethylbenzene with benzene direct reaction, can be with substituting ethylene raw, technical process is simple, produce under identical output ethylbenzene condition, ethanol raw material is than ethylene raw cost more than 20%, total raw material cost reduces approximately 10% than ethylene process, many ethylbenzene conversion that liquid-phase transalkylation reactor generates alkylated reaction are more ethylbenzene, reduced the generation of by product dimethylbenzene simultaneously, in product ethylbenzene, xylene content can be down to 600ppm by the 1000ppm of former technique, ethanol unit consumption is less than 450 kgs/tonne of ethylbenzene (by 100% straight alcohol) simultaneously, energy consumption is less than 1,000 million Jiao/ton ethylbenzene, product ethylbenzene purity is more than 99.8%, invest suitable with ethene route, there is obvious comprehensive advantage.
Accompanying drawing explanation
Fig. 1 is ethanol and the benzene one-step synthesis ethylbenzene schematic flow sheet that adopts technical solution of the present invention.
In Fig. 1,1 is ethanol evaporation device; 2 is alkylation reactor; 3 is benzene vaporizer; 4 is process furnace; 5 is transalkylation reactor; 6 is benzene tower; 7 is benzene overhead condenser; 8 is ethylbenzene tower; 9 is many ethylbenzene towers, 101 is feed ethanol, 102 is benzene feedstock, 103 is alkylation reactor outlet logistics, 104 divide water outlet logistics for benzene overhead condenser, 105 separate removal of alkylation reaction device benzene for benzene overhead condenser, 106 divide away transalkylation reactor benzene for benzene overhead condenser, 107 is the logistics of benzene tower reactor, 108 is ethylbenzene overhead product ethylbenzene stream, and 109 is the logistics of many ethylbenzene towers tower reactor Residual oil, and 110 is many ethylbenzene towers ethylbenzene stream at most, 111 is many ethylbenzene tower reactor logistics Residual oil, and 112 is transalkylation reactor outlet logistics.
In Fig. 1, feed ethanol 101 is after 1 evaporation of ethanol evaporation device, mix with benzene feedstock 102 through 4 heating of benzene vaporizer 3 and process furnace and the mixture of recycle benzene 105, in high temperature, press and under gas phase condition, enter alkylation reactor and react, generate ethylbenzene, many ethylbenzene and water, reaction product 103 enters benzene tower 6, overhead stream is after 7 condensations of benzene column overhead condenser, divide and anhydrate 104, part benzene 105 loops back alkylation reactor, part benzene 106 removes transalkylation reactor 5, benzene tower reactor logistics 107 is mainly ethylbenzene, many ethylbenzene and Residual oil, remove ethylbenzene tower 8, tower top separation obtains product ethylbenzene 108, tower reactor logistics 109 is after many ethylbenzene tower 9 separation, tower reactor is Residual oil 111, tower top is many ethylbenzene 110, after mixing with logistics 106, under cryogenic high pressure liquid-phase condition, enter transalkylation reactor 5 and carry out the more ethylbenzene product of transalkylation reaction generation, benzene tower 6 is returned in reactor outlet logistics 112.
Below by embodiment, the present invention is further elaborated.
Embodiment
[embodiment 1]
Certain 30,000 tons/year of ethanol and benzene one-step synthesis Benzene Device, adopt and press the synthetic technology of ethylbenzene shown in Fig. 1, the feed ethanol of 95% purity is after heating and gasifying, be mixed into benzene feedstock and recycle benzene after gasification heating the alkylation reactor that ZSM-5 nanoscale molecular sieve catalyst is housed, the mol ratio of benzene and ethanol is 6: 1,380 ℃ of alkylation reactor inlet temperatures, pressure 1.2MPaG, ethanol weight space velocity 1.5 hours
-1, after reaction, drop temperature is 400 ℃, wherein ethylbenzene weight percent is 16%, diethylbenzene is 1.6%, reaction product enters benzene tower, benzene column overhead working pressure 1.0MPaG, 160 ℃ of tower top temperatures, 250 ℃ of tower reactor temperature, reflux ratio 1 adopts 45 blocks of valve traies, overhead stream is after benzene column overhead condenser condenses, divide and anhydrate, dividing water content in the benzene after anhydrating is 0.1%, part loops back alkylation reactor, part is removed transalkylation reactor, Beta molecular sieve catalyst is housed in transalkylation reactor, temperature in is 180 ℃, pressure 2.8MPaG, the weight ratio of benzene and many ethylbenzene is 6: 1, liquid weight air speed is 2 hours
-1, many conversion of ethylbenzene are 70%, benzene tower tower bottoms removes ethylbenzene tower, ethylbenzene tower working pressure 0.1MPaG, 163 ℃ of tower top temperatures, 214 ℃ of tower reactor temperature, reflux ratio 3.2, tower top separation obtains product ethylbenzene, and many ethylbenzene recovery tower working pressure is-0.07MPaG, 100～220 ℃ of tower top temperatures, 190～250 ℃ of tower reactor temperature, reflux ratio 0.1～2, overhead condensation liquid is many ethylbenzene, deliver to transalkylation reactor, tower reactor logistics is Residual oil.
This device total raw material cost is 8800 yuan/ton of ethylbenzene, and ethylbenzene purity is 99.86%, and in ethylbenzene, xylene content is 580ppm, 440 kgs/tonne of ethylbenzene of ethanol unit consumption, and energy consumption is 860,000,000 Jiao/ton ethylbenzene.
[embodiment 2]
Certain 30,000 tons/year of ethanol and benzene one-step synthesis Benzene Device, in alkylation reactor, the mol ratio of benzene and ethanol is 5: 1, other technical process and operating parameters are identical with embodiment 1, and in alkylation reactor outlet material, ethylbenzene weight percent is 15%, and diethylbenzene is 2.0%.
This device total raw material cost is 8920 yuan/ton of ethylbenzene, and ethylbenzene purity is 99.8%, and in ethylbenzene, xylene content is 700ppm, 446 kgs/tonne of ethylbenzene of ethanol unit consumption, and energy consumption is 920,000,000 Jiao/ton ethylbenzene.
[embodiment 3]
Certain 60,000 tons/year of ethanol and benzene one-step synthesis Benzene Device, transalkylation reactor temperature in is 220 ℃, pressure 3.0MPaG, the weight ratio of benzene and many ethylbenzene is 7: 1, liquid weight air speed is 2 hours
-1, many conversion of ethylbenzene are 70%, other technical process and operating parameters are identical with embodiment 1.
This device total raw material cost is 8870 yuan/ton of ethylbenzene, and ethylbenzene purity is 99.82%, and in ethylbenzene, xylene content is 650ppm, 442 kgs/tonne of ethylbenzene of ethanol unit consumption, and energy consumption is 920,000,000 Jiao/ton ethylbenzene.
[comparative example 1]
Certain 30,000 tons/year of ethanol and benzene one-step synthesis Benzene Device, without transalkylation reactor, all the other technical process and operating parameters are identical with embodiment 1.
This device total raw material cost is 9710 yuan/ton of ethylbenzene, and ethylbenzene purity is 99.8%, and in ethylbenzene, xylene content is 700ppm, 486 kgs/tonne of ethylbenzene of ethanol unit consumption, and 3000 tons/year of diethylbenzene of by-product, diethylbenzene purity is 94%, energy consumption is 900,000,000 Jiao/ton ethylbenzene.
[comparative example 2]
Certain 60,000 tons/year of ethene and benzene alkylation synthesizing ethyl benzene device, employing pure ethylene is raw material, benzene feedstock and recycle benzene after the raw material ethene of 99.5% purity heats with gasification are mixed into the alkylation reactor that ZSM-5 molecular sieve alkylation catalyst is housed, the mol ratio of benzene and ethene is 6: 1,380 ℃ of alkylation reactor inlet temperatures, pressure 1.2MPaG, weight ethylene air speed 1.5 hours
-1after reaction, drop temperature is 405 ℃, wherein ethylbenzene weight percent is 16%, diethylbenzene is 1.6%, reaction product enters benzene tower, benzene column overhead working pressure 1.0MPaG, 160 ℃ of temperature, adopt 45 blocks of valve traies, and the phlegma of overhead stream after benzene column overhead condenser condenses partly loops back alkylation reactor, part is removed transalkylation reactor, transalkylation reactor adopts gas-phase process, in-built ZSM-5 molecular sieve catalyzer, and temperature in is 420 ℃, the mol ratio of benzene and many ethylbenzene is 4: 1, and total air speed is 20 hours
-1, many conversion of ethylbenzene are 60%, benzene tower, ethylbenzene tower and many ethylbenzene towers operational condition are identical with embodiment 1.
This device total raw material cost is 9850 yuan/ton of ethylbenzene, and ethylbenzene purity is 99.8%, and in ethylbenzene, xylene content is 1000ppm, 284 kgs/tonne of ethylbenzene of ethene unit consumption, and energy consumption is 910,000,000 Jiao/ton ethylbenzene.
[comparative example 3]
Certain 60,000 tons/year of Benzene Device, adopts the ethanol generation ethene that first dewaters, and then ethene and benzene alkylation is produced to ethylbenzene route, ethene and benzene alkylation produce ethylbenzene process flow process and operating parameters identical with comparative example 2.
This device total raw material cost is 9750 yuan/ton of ethylbenzene, and ethylbenzene purity is 99.75%, and in ethylbenzene, xylene content is 1000ppm, 540 kgs/tonne of ethylbenzene of ethanol unit consumption, and energy consumption is 19,500 million Jiao/ton ethylbenzene.
[comparative example 4]
Certain 30,000 tons/year of ethanol and benzene one-step synthesis Benzene Device, transalkylation reactor adopts gas phase reaction process, in-built ZSM-5 molecular sieve catalyzer, temperature in is 420 ℃, pressure 0.6MPaG, the mol ratio of benzene and many ethylbenzene is 4: 1, total air speed is 20 hours
-1, many conversion of ethylbenzene are 60%, other technical process and operating parameters are identical with embodiment 1.
This device total raw material cost is 8950 yuan/ton of ethylbenzene, and ethylbenzene purity is 99.82%, and in ethylbenzene, xylene content is 900ppm, 440 kgs/tonne of ethylbenzene of ethanol unit consumption, and energy consumption is 19,500 million Jiao/ton ethylbenzene.
Claims (5)
1. a synthetic method for ethylbenzene, comprises the following steps:
A) ethanol and benzene enter by 2～8:1 in molar ratio the alkylation reactor that ZSM-5 nanoscale molecular sieve catalyst is housed and react under gas phase condition, obtain comprising the mixture of benzene, ethylbenzene, diethylbenzene and water;
B) mixture, successively by benzene recovery tower, ethylbenzene recovery tower, many ethylbenzene recovery tower, is isolated water, benzene, ethylbenzene and diethylbenzene wherein;
C) the part benzene that separation obtains enters transalkylation reactor by weight 2～10:1 with diethylbenzene and contacts and carry out transalkylation reaction with Beta molecular sieve catalyst under liquid-phase condition, generates ethylbenzene;
Described transalkylation reactor temperature of reaction is 150 ℃～280 ℃, and reaction pressure is 2.0～3.5MPaG, and liquid weight air speed is 1.0～3.0 hours
-1, benzene and many ethylbenzene weight ratio are 3～6:1.
2. the synthetic method of ethylbenzene according to claim 1, is characterized in that alkylated reaction temperature is 320 ℃～450 ℃, and reaction pressure is 0.5～2.0MPa, and ethanol weight space velocity is 0.6～2.5 hour
-1, benzene and ethanol mol ratio are 4.0～7.0:1.
3. the synthetic method of ethylbenzene according to claim 1, is characterized in that benzene recovery tower working pressure is 0.4～2.0MPaG, 125～200 ℃ of tower top temperatures, 200～300 ℃ of tower reactor temperature, reflux ratio 0.8～2.
4. the synthetic method of ethylbenzene according to claim 1, is characterized in that ethylbenzene recovery tower working pressure is 0.0～0.5MPaG, 135～200 ℃ of tower top temperatures, 190～250 ℃ of tower reactor temperature, reflux ratio 2～6.
5. the synthetic method of ethylbenzene according to claim 1, is characterized in that many ethylbenzene recovery tower working pressure is-0.1～0.2MPaG, 100～220 ℃ of tower top temperatures, 190～250 ℃ of tower reactor temperature, reflux ratio 0.1～2.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201010200039.XA CN102276410B (en) | 2010-06-11 | 2010-06-11 | Method for synthesizing ethylbenzene |
| BRPI1103071-2A BRPI1103071B1 (en) | 2010-06-11 | 2011-06-13 | ETHYL BENZEN SYNTHESIS PROCESS FROM ETHANOL AND BENZENE |
| US13/158,709 US8519208B2 (en) | 2010-06-11 | 2011-06-13 | Processes for synthesizing ethylbenzene from ethanol and benzene |
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| CN201010200039.XA CN102276410B (en) | 2010-06-11 | 2010-06-11 | Method for synthesizing ethylbenzene |
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| CN102276410B true CN102276410B (en) | 2014-03-26 |
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| EP1775277A1 (en) * | 2004-05-28 | 2007-04-18 | Consejo Superior De Investigaciones Cientificas | Method and catalyst for the transalkylation/dealkylation of organic compounds |
| CN101085711A (en) * | 2007-07-13 | 2007-12-12 | 花尚元 | Method for synthesizing ethyl benzene and diethyl benzene |
| CN101450882A (en) * | 2007-12-06 | 2009-06-10 | 上海戊正工程技术有限公司 | Technique for producing ethyl benzene |
| CN101450888A (en) * | 2007-12-06 | 2009-06-10 | 上海戊正工程技术有限公司 | Method for preparing catalyst for synthesizing ethyl benzene |
| CN101618335A (en) * | 2009-08-06 | 2010-01-06 | 上海卓悦化工科技有限公司 | Method for preparing catalyst for compounding p-diethylbenzene by alkylation reaction of ethylbenzene and ethane or alcohol |
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Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP1775277A1 (en) * | 2004-05-28 | 2007-04-18 | Consejo Superior De Investigaciones Cientificas | Method and catalyst for the transalkylation/dealkylation of organic compounds |
| CN101085711A (en) * | 2007-07-13 | 2007-12-12 | 花尚元 | Method for synthesizing ethyl benzene and diethyl benzene |
| CN101450882A (en) * | 2007-12-06 | 2009-06-10 | 上海戊正工程技术有限公司 | Technique for producing ethyl benzene |
| CN101450888A (en) * | 2007-12-06 | 2009-06-10 | 上海戊正工程技术有限公司 | Method for preparing catalyst for synthesizing ethyl benzene |
| CN101618335A (en) * | 2009-08-06 | 2010-01-06 | 上海卓悦化工科技有限公司 | Method for preparing catalyst for compounding p-diethylbenzene by alkylation reaction of ethylbenzene and ethane or alcohol |
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