CN1068809A - Prolong the method for life of alkylation catalysts - Google Patents
Prolong the method for life of alkylation catalysts Download PDFInfo
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- CN1068809A CN1068809A CN 92105748 CN92105748A CN1068809A CN 1068809 A CN1068809 A CN 1068809A CN 92105748 CN92105748 CN 92105748 CN 92105748 A CN92105748 A CN 92105748A CN 1068809 A CN1068809 A CN 1068809A
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- aromatic hydrocarbon
- alkene
- benzene
- alcohol
- catalyst
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- 239000003054 catalyst Substances 0.000 title claims abstract description 50
- 238000000034 method Methods 0.000 title claims abstract description 38
- 238000005804 alkylation reaction Methods 0.000 title claims abstract description 23
- 230000029936 alkylation Effects 0.000 title claims abstract description 22
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 claims abstract description 96
- 238000006243 chemical reaction Methods 0.000 claims abstract description 39
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 claims abstract description 37
- 150000001336 alkenes Chemical class 0.000 claims abstract description 31
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 24
- 150000004945 aromatic hydrocarbons Chemical class 0.000 claims abstract description 22
- 239000000654 additive Substances 0.000 claims abstract description 9
- 230000000996 additive effect Effects 0.000 claims abstract description 9
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 claims abstract description 5
- 125000003158 alcohol group Chemical group 0.000 claims abstract 2
- YNQLUTRBYVCPMQ-UHFFFAOYSA-N Ethylbenzene Chemical compound CCC1=CC=CC=C1 YNQLUTRBYVCPMQ-UHFFFAOYSA-N 0.000 claims description 30
- 239000010457 zeolite Substances 0.000 claims description 27
- 229910021536 Zeolite Inorganic materials 0.000 claims description 25
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical group O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 claims description 23
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical group C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 claims description 15
- RWGFKTVRMDUZSP-UHFFFAOYSA-N cumene Chemical compound CC(C)C1=CC=CC=C1 RWGFKTVRMDUZSP-UHFFFAOYSA-N 0.000 claims description 10
- 230000008569 process Effects 0.000 claims description 10
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 claims description 6
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 claims description 6
- KFZMGEQAYNKOFK-UHFFFAOYSA-N Isopropanol Chemical compound CC(C)O KFZMGEQAYNKOFK-UHFFFAOYSA-N 0.000 claims description 2
- 150000001298 alcohols Chemical class 0.000 claims 1
- 230000009849 deactivation Effects 0.000 description 11
- 230000008929 regeneration Effects 0.000 description 10
- 238000011069 regeneration method Methods 0.000 description 10
- 230000000694 effects Effects 0.000 description 8
- 230000002779 inactivation Effects 0.000 description 7
- UFWIBTONFRDIAS-UHFFFAOYSA-N Naphthalene Chemical compound C1=CC=CC2=CC=CC=C21 UFWIBTONFRDIAS-UHFFFAOYSA-N 0.000 description 4
- 239000002253 acid Substances 0.000 description 4
- 150000004996 alkyl benzenes Chemical class 0.000 description 4
- 239000012071 phase Substances 0.000 description 4
- 239000005977 Ethylene Substances 0.000 description 3
- 125000000217 alkyl group Chemical group 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- 230000009257 reactivity Effects 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- 230000001476 alcoholic effect Effects 0.000 description 2
- -1 alkyl hydrocarbon Chemical class 0.000 description 2
- 239000006227 byproduct Substances 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 238000006073 displacement reaction Methods 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 239000007791 liquid phase Substances 0.000 description 2
- 239000011541 reaction mixture Substances 0.000 description 2
- CXWXQJXEFPUFDZ-UHFFFAOYSA-N tetralin Substances C1=CC=C2CCCCC2=C1 CXWXQJXEFPUFDZ-UHFFFAOYSA-N 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
- 239000012190 activator Substances 0.000 description 1
- 239000004480 active ingredient Substances 0.000 description 1
- 230000002152 alkylating effect Effects 0.000 description 1
- 125000003118 aryl group Chemical group 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- VEFXTGTZJOWDOF-UHFFFAOYSA-N benzene;hydrate Chemical compound O.C1=CC=CC=C1 VEFXTGTZJOWDOF-UHFFFAOYSA-N 0.000 description 1
- UNYSKUBLZGJSLV-UHFFFAOYSA-L calcium;1,3,5,2,4,6$l^{2}-trioxadisilaluminane 2,4-dioxide;dihydroxide;hexahydrate Chemical compound O.O.O.O.O.O.[OH-].[OH-].[Ca+2].O=[Si]1O[Al]O[Si](=O)O1.O=[Si]1O[Al]O[Si](=O)O1 UNYSKUBLZGJSLV-UHFFFAOYSA-L 0.000 description 1
- 229910052676 chabazite Inorganic materials 0.000 description 1
- 238000004581 coalescence Methods 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 238000003795 desorption Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 238000005984 hydrogenation reaction Methods 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000005259 measurement Methods 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 238000003541 multi-stage reaction Methods 0.000 description 1
- 150000002989 phenols Chemical class 0.000 description 1
- 125000001997 phenyl group Chemical group [H]C1=C([H])C([H])=C(*)C([H])=C1[H] 0.000 description 1
- 238000006116 polymerization reaction Methods 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- 125000000383 tetramethylene group Chemical group [H]C([H])([*:1])C([H])([H])C([H])([H])C([H])([H])[*:2] 0.000 description 1
Images
Classifications
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2/00—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms
- C07C2/54—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by addition of unsaturated hydrocarbons to saturated hydrocarbons or to hydrocarbons containing a six-membered aromatic ring with no unsaturation outside the aromatic ring
- C07C2/64—Addition to a carbon atom of a six-membered aromatic ring
- C07C2/66—Catalytic processes
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2529/00—Catalysts comprising molecular sieves
- C07C2529/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites, pillared clays
- C07C2529/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
A kind of about the improving one's methods of alkylated reaction, in reaction zone, at least a aromatic hydrocarbon (for example, benzene) and at least a alkene are carried out alkylated reaction to produce at least a monoalkyl aromatic hydrocarbon in the presence of alkylation catalyst.The improvement of this method comprises, with a kind of additive and at least a aromatic hydrocarbon and at least a olefin that is selected from alcohol or water.Alcohol or water added to causing life of catalyst to improve in the charging, and can when aromatic hydrocarbon and alkene are in lower mol ratio, carry out alkylated reaction.
Description
The present invention relates to prolong the life-span of alkylation catalyst, such as zeolite alkylated catalyst.Further say, the present invention relates to prolong and be used for aromatic hydrocarbon and olefin alkylation reaction method with the life of alkylation catalysts of producing alkyl aromatics.
Alkylated reaction is in alkylation reactor, with aromatic substance such as benzene, naphthalene or 1,2,3,4-tetralin and alkene such as ethene, propylene or butylene in reaction in the presence of the alkylation catalyst and under catalyticing conversioning condition to produce alkyl aromatics.For example benzene can be produced ethylbenzene or isopropyl benzene respectively with ethene or propylene reaction.Be provided with one or more alkylation catalyst bed layers in the reactor.Catalyzer can be the alkylation catalyst of zeolite catalyst or other type.
Alkylated reaction can carry out in liquid phase, vapour phase or vapour-liquid mixed phase.Because these alkylated reactions are strong heat releases, preferably provide heat-removal capability so keep service temperature in beds, or carry out the stepwise process reaction, and in each intersegmental cooling that appropriateness is provided.Such adiabatic operation method is desirable.For the temperature that limits in each conversion zone raises, it is excessive aromatic hydrocarbon that people adopt with respect to alkene, and when adopting the multistage reactor, can limit the amount of alkene that feeds in each section reaction mixture.In addition, will reduce the amount of the undesirable more alkyl aromatic that in each conversion zone, is generated with excessive aromatic hydrocarbon.For example, it is about 5: 1 to about 6: 1 that production alkylbenzene (for example ethylbenzene or isopropyl benzene) can adopt total mol ratio of benzene and alkene, if adopt the multistage reaction, the ethene portioning can be added in each conversion zone.In the back of each section, can after each part conversion of olefines, apply cooling.Preferably the alkene div in par aeq is added each section.Under catalyticing conversioning condition, this reaction is very fast, and only needs just converted olefin fully of a thin layer catalyst bed.
Along with the time growth of each bed of operation catalyzer, catalyzer is inactivation gradually.The inactivation of catalyzer is accompanied by the zone that reacts and is shifted along beds.After reaction zone shifts out the whole length of catalyst bed fully, just with catalyst regeneration.The peak temperature walk rate is fast more, and the needs of catalyzer are just frequent more in regeneration or the reduction bed.Under the constant condition of others, the speed of catalyst deactivation is proportional with the alkylbenzene production rate.The speed of catalyst deactivation is also along with the ratio of benzene and alkene reduces and increases.Benzene and alkene are in when hanging down ratio, and some alkene is assembled coalescence and generated other high-molecular weight alkene.These alkene can have the phenyl ring alkylation alkyl hydrocarbon of long side chain with generation.In addition, be that ratio along with benzene and alkene reduces and increases to the selectivity of polyalkylbenzene such as dialkyl group, trialkyl and tetraalkyl benzene.In general, the speed of catalyst deactivation is along with the concentration of heavy alkylbenzene and polyalkylbenzene increases and increases.These heavy products are preferentially adsorbed on and carry out polymerization on the activity of such catalysts position, and desorption from the catalyzer no longer.Therefore, catalyzer is with regard to inactivation.
Temperature is also influential to activity of such catalysts.Temperature is lower than optimum range, can cause the selectivity of polyalkylbenzene is increased, so produce bigger deactivation rate.Temperature is higher than optimum range, and cracking can take place polyalkylbenzene, can produce the active ingredient of polymkeric substance and the speed of other high boiler material meeting accelerator activator inactivation.
Deactivation rate energy enough " reactivity parameter ", or AP comes quantificational expression.Calculate this reactivity parameter and be by certain period with process in the catalyst quality of inactivation divided by the quality of the alkylbenzene that in same long time, generates.Catalyzer with quite high AP value has the long life-span in needs regeneration or before changing.Catalyzer with quite low AP value needs the regenerated frequency just higher, this situation be accompanied by usually production loss and (or) the increasing of extra charge.Be also noted that fresh catalyzer has high AP value, and its AP value is just very little after regeneration, that is, behind catalyst regeneration, its inactivation is preceding more faster than regeneration.Such phenomenon is that people are undesirable, because increased process cost thus and subtracted the ability of having fallen the prediction catalyst performance.
Therefore, the purpose of this invention is to provide a method of improving alkylated reaction by the prolongation catalyst life.
According to one embodiment of the invention, improving one's methods of a kind of alkylated reaction is provided, be used in reaction zone in the presence of alkylation catalyst, at least a aromatic hydrocarbon and at least a alkene being carried out alkylated reaction to produce at least a monoalkyl aromatic hydrocarbon at reaction zone.This is improved one's methods and comprises and will be selected from additive and at least a aromatic hydrocarbon and at least a olefin of alcohol or water.
Can comprise benzene, naphthalene and 1,2,3,4-tetralin by alkylating aromatic hydrocarbon, but have more than be limited to as above several.Can be used for alkene with aromatics alkylationization comprise ethene, propylene, butylene with and composition thereof, but have more than be limited to above several.In one embodiment, at least a aromatic hydrocarbon is benzene.Can comprise that benzene alkylation with ethylene produces ethylbenzene by the representative example that the present invention carries out alkylated reaction, and isopropyl benzene is produced in the benzene alkylation with propylene reaction.
In one embodiment, alkylated reaction can be to carry out to about 30: 1 condition in about 3: 1 in the mol ratio of aromatic hydrocarbon and alkene, and preferably its mol ratio is about 5: 1 to about 6: 1.
In one embodiment, additive is a water.The consumption of water is advisable with 100ppm at least by the benzene feed charging meter, and approximately 200ppm is to about 1, and 500ppm is better, selects about 300ppm to about 1, and 000ppm is better, and preferably selects for use about 400ppm to about 800ppm.Water consumption depends on the ratio of used aromatic hydrocarbon and alkene and the character and the state of alkylation catalyst accurately.
In another embodiment, additive can be an alcohol, although can use any kind alcohol (for example, single-or two-hydroxyl alcohols, phenols, ethanol class), preferably use the alcohol that can in reactor effluent, not increase impurity or by product quantity.If for example benzene alkylation with ethylene reaction is generated ethylbenzene, be added to the alcohol ethanol preferably in the charging.If the benzene alkylation with propylene reaction is generated isopropyl benzene, add preferably Virahol of alcohol, if desired alkyl thing needn't be a kind of pure compound, the mixture that so also can use alcohol is as additive.
Alcohol should exist with the significant quantity that prolongs catalyst life; , the alcohol amount of adding in the charging should not form the water as byproduct of reaction of amount of interference, or the alcohol amount can suppress the speed of alkylated reaction.
The consumption of alcohol is in used amount of alkene about 1%(mole preferably) to about 10%(mole), perhaps preferably approximately 0.2%(is heavy in the weight of benzene) to approximately 0.5%(is heavy).
Alkylated reaction can carry out in liquid phase, vapour phase or liquid-vapour mixed phase.Alkylated reaction can carry out under following condition, and temperature is about 250 °F to about 900 °F, and preferably about 350 °F to about 600 °F, pressure is about 150 pounds/inch
2(gauge pressure) is to about 2000 pounds/inch
2(gauge pressure) and preferably about 250 pounds/inch
2(gauge pressure) is to about 1000 pounds/inch
2(gauge pressure), and total weight hourly space velocity (WHSV) is about 2 hours
-1To about 1000 hours
-1, preferably about 4 to about 100 hours
-1WHSV is meant weight hourly space velocity, and represents with the charging quality of per unit catalyst quality, promptly hour
-1
Adoptable alkylation catalyst is zeolite catalyst preferably.In one embodiment, zeolite catalyst does not contain the hydrogenation metal.Adoptable zeolite catalyst comprises X zeolite, Y zeolite, L zeolite, beta-zeolite, ZSM-5, ω-zeolite, mordenite and chabazite.In one embodiment, zeolite can be Y zeolite or beta-zeolite.These zeolites are acid type preferably.
Further describe the present invention with reference to following example, still, scope of the present invention has more than the following explanation of limit.
About following example, removing has other explanation, adopts following condition.
The steel pipe that the alkylation reactor that is adopted is 1 inch by an internal diameter constitutes, and 20 inch catalyzer how long wherein is housed and the mobile hot galvanic couple of axial location is housed.Reactor is placed in the isolator of a bed thickness, so that reactor is operated under adiabatic method.With the benzene charging,, enter the lower end of reactor again with volume pump earlier by preheater.Ethene measures with the mass flow control device, and mixes with benzene before benzene enters preheater.The reaction mixture of discharging by reactor head is collected with storage tank then through supercooler and back pressure regulator.In two of reactor equal conversion zones, benzene and ethene all react with (B/E) mol ratio of 12/1.Therefore, total B/E mol ratio is 6/1.Regulate preheating temperature and make that the peak temperature in each reactor region is about 475 °F to about 485 °F.Pressure in this system maintains about 550 pounds/inch
2(gauge pressure) is to about 600 pounds/inch
2(gauge pressure) by axial thermocouple measurement, draws temperature profile, to determine the position of peak temperature.
Example 1
Catalyzer is made of a kind of commodity zeolite that is called zeolite " A ", and it is molded into about 1/4 inch is long, diameter is the extrudate of 1/16 inch.In the time of 840 hours, the displacement that records peak temperature is 1.35 inches at this reactive system of operation.
With the ethene flow velocity is benchmark, can calculate ethylbenzene (EB) amount that makes.Be included in the catalyst deactivation of that part of weight in the constant volume in the reactor, the peak temperature position when this volume was begun by the identical timed interval when finishing limits.The reactivity parameter that utilizes these numerical value to calculate decaying catalyst is 14,000 kilograms of EB/ kilograms.Position for this catalyzer peak temperature is plotted on the accompanying drawing 1 over time.
Example 2
Under condition mentioned above, the another kind of commodity zeolite that will be called zeolite " B " is tested in adiabatic experimental installation.Obtaining the activity of such catalysts parameter is 6,000 kilograms of EB/ kilograms.The position of this catalyzer peak temperature is plotted on the accompanying drawing 2 over time.
Example 3
Zeolite " A " generates in the ethylbenzene process behind the inactivation at benzene alkylation, and with the regeneration techniques of knowing in the present technique field, the heavy organic substance of burnt deposit on zeolite selectively is with this zeolite regeneration.Under condition mentioned above, the catalyzer after the regeneration is used for the adiabatic alkylated reaction.Obtaining the activity of such catalysts parameter is 1,100 kilogram of EB/ kilogram.The position of peak temperature is plotted on the accompanying drawing 3 over time.
Example 4
Except 0.2%(is heavy) ethanol be dissolved in the benzene, handle zeolites " A " according to example 3.This amount of alcohol is equivalent to be fed to 5% of ethene in the reactor, and remaining desired ethene is with gas feed, as mentioned above it is dissolved in the benzene.The position that Fig. 4 represents peak temperature over time.In view of the above, calculating the catalyst activity parameter is 32,700 kilograms of EB/ kilograms.If stop to add ethanol, surpass 168 hours in the operating time, the deactivation rate of this catalyzer just increases at once, as the curve of Fig. 4 the time surpass 168 hours shown.This example shows if stop to add ethanol, will lose and add the alcoholic acid beneficial effect.
Example 5
The container that liquid-liquid contact is provided in the benzene feeding line is so that benzene vapor and water reach capacity, and except that this difference, this example still adopts same catalyst described in the example 1 and reaction conditions.This container fills one deck water, and allow benzene feed with the form of droplet from wherein passing through.The benzene that gathers at the water layer top is by water saturation.It further mixes with ethene, and preheating also is fed in the reactor mentioned above, and the sample of reactor effluent shows moisture 500-650ppm, it be equivalent to the contact temperature when (20～25 ℃) saturation concentration about 80～90%.In 540 hours process of the test, moving of the peak temperature position in the bed represented with Fig. 5.Test in view of the above, calculating activity of such catalysts parameter (AP) is 39,800 kilograms of EB/ kilograms.This test shows, water is fed in the reactor with specified amount, can increase the stability of catalyzer significantly, and the AP value that shows as catalyzer increases.In another experiment, except the water yield that is fed in the reactor is about 200ppm, repeat condition mentioned above.Consequently minimum to the influence of catalyst deactivation speed.
Example 6
Adopt example 2 described reactor assembly and working method.Use a kind of different zeolite catalyst that is called zeolite " C ", the shape of it and zeolite " A " and size are basic identical.But, the acid height of zeolite " C ".The position of the curve representation peak temperature of Fig. 6 is with the variation of operating time.The time reach 100 hours, do not allow water feed this system.After this, use-case 5 described water-benzene contactors, the curve of being drawn with the displacement of operating time by the position of peak temperature is lower angle of inclination, i.e. and proof interpolation water has direct influence to the stability of zeolite catalyst.
Example 7
Adopt example 1 described same reactor system and operational condition.This example is to measure, when B/E value is lower than when implementing the employed value of previous examples, and the performance whether interpolation water and/or ethanol can rugged catalysts.In each stage, the ratio of B/E adopts 10/1, that is, total ratio of B/E is 5/1.The position of peak temperature in the variations of various operating times as shown in Figure 7.Be used for initial example of benzene.At initial 90 hours, the activity of such catalysts parameter was 350 kilograms of EB/ kilograms.Operate after 90 hours, benzene feed and 0.4%(is heavy) ethanol mix.The water that contains 1000ppm in the effluent of alkylation reactor, in during the interpolation alcoholic acid, calculating the activity of such catalysts parameter is 13,700 kilograms of EB/ kilograms.This example shows that when the ethylene concentration in the charging was higher than the example of front, the water that ethanol and/or ethanol and benzene reaction produce still can be kept the useful influence of catalyst deactivation speed.
Advantage of the present invention comprises that because catalyst deactivation speed reduces, reactive system can have the long operating time between twice regeneration of catalyzer.Can also reach same throughput with the catalyzer of smaller size smaller.In addition, reduce catalyst deactivation speed under the concentration by alkene in increasing charging, reactor can be worked when effluent is in higher concentration, therefore, can use less reactor and reaches given throughput.
Yet, should be appreciated that scope of the present invention has more than and is limited to each embodiment as described above.The present invention can implement to be different from the mode that mask body describes, but still falls within the scope of the appended claims.
Claims (19)
1, a kind of method of alkylated reaction, in reaction zone with at least a aromatic hydrocarbon and at least a alkene in the presence of alkylation catalyst, carry out alkylated reaction and produce at least a monoalkyl aromatic hydrocarbon, the improvement of this method comprises: additive and at least a described aromatic hydrocarbon and at least a described olefin that will be selected from alcohol or water.
2, according to the process of claim 1 wherein that described additive is a water.
3, according to the method for claim 2, wherein said water exists with the amount of 100ppm at least.
4, according to the method for claim 3, wherein said water exists with the amount of 200ppm to 1000ppm.
5, according to the method for claim 4, wherein said water exists with the amount of 300ppm to 900ppm.
6, according to the method for claim 5, wherein said water exists with the amount of 400ppm to 800ppm.
7, according to the process of claim 1 wherein that described additive is alcohol.
8, according to the process of claim 1 wherein that described at least a aromatic hydrocarbon is benzene.
9, according to the process of claim 1 wherein that described at least a aromatic hydrocarbon and at least a alkene carry out alkylated reaction with 3: 1 to 30: 1 mol ratio.
10, according to the method for claim 9, wherein said at least a aromatic hydrocarbon and at least a alkene carry out alkylated reaction with 5: 1 to 6: 1 mol ratio.
11, method according to Claim 8, wherein said at least a alkene is ethene.
12, according to the method for claim 11, wherein said at least a alkene is propylene.
13, according to the method for claim 11, wherein said at least a monoalkyl aromatic hydrocarbon is an ethylbenzene.
14, method according to Claim 8, wherein said at least a monoalkyl aromatic hydrocarbon is an isopropyl benzene.
15, method according to Claim 8, wherein said additive are alcohol.
16, according to the method for claim 15, wherein by the weight of benzene, this alcohol is heavy with 0.2%() heavy to 0.5%() amount exist.
17, according to the method for claim 15, wherein alkene is that ethene and alcohol are ethanol.
18, according to the method for claim 15, alkene is propylene in the base, and alcohol is Virahol.
19, according to the process of claim 1 wherein that described alkylation catalyst is a zeolite catalyst.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US73209091A | 1991-07-18 | 1991-07-18 | |
| US732,090 | 1991-07-18 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN1068809A true CN1068809A (en) | 1993-02-10 |
Family
ID=24942149
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 92105748 Pending CN1068809A (en) | 1991-07-18 | 1992-07-15 | Prolong the method for life of alkylation catalysts |
Country Status (4)
| Country | Link |
|---|---|
| CN (1) | CN1068809A (en) |
| AU (1) | AU2002292A (en) |
| MX (1) | MX9202524A (en) |
| WO (1) | WO1993002027A1 (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102652121A (en) * | 2009-12-16 | 2012-08-29 | 环球油品公司 | Detergent Alkylation Using Rare Earth Exchange Catalysts |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5877384A (en) * | 1996-02-12 | 1999-03-02 | The M. W. Kellogg Company | Apparatus and process for separating reaction effluent in the manufacture of cumene |
| IT1397885B1 (en) | 2009-12-23 | 2013-02-04 | Polimeri Europa Spa | PROCESS FOR PREPARING ETHYLBENZENE. |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4387260A (en) * | 1981-04-20 | 1983-06-07 | Cosden Technology, Inc. | Alkylation of aromatic compounds with silicalite catalysts in the presence of steam |
| US4400570A (en) * | 1982-05-21 | 1983-08-23 | Cosden Technology, Inc. | Ethylbenzene production employing tea-silicate catalysts |
-
1992
- 1992-04-06 WO PCT/US1992/002877 patent/WO1993002027A1/en not_active Ceased
- 1992-04-06 AU AU20022/92A patent/AU2002292A/en not_active Abandoned
- 1992-05-28 MX MX9202524A patent/MX9202524A/en unknown
- 1992-07-15 CN CN 92105748 patent/CN1068809A/en active Pending
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102652121A (en) * | 2009-12-16 | 2012-08-29 | 环球油品公司 | Detergent Alkylation Using Rare Earth Exchange Catalysts |
| CN102652121B (en) * | 2009-12-16 | 2016-01-13 | 环球油品公司 | Detergent Alkylation Using Rare Earth Exchange Catalysts |
Also Published As
| Publication number | Publication date |
|---|---|
| MX9202524A (en) | 1993-01-01 |
| WO1993002027A1 (en) | 1993-02-04 |
| AU2002292A (en) | 1993-02-23 |
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