US2904607A - Alkylation of aromatics - Google Patents
Alkylation of aromatics Download PDFInfo
- Publication number
- US2904607A US2904607A US636909A US63690957A US2904607A US 2904607 A US2904607 A US 2904607A US 636909 A US636909 A US 636909A US 63690957 A US63690957 A US 63690957A US 2904607 A US2904607 A US 2904607A
- Authority
- US
- United States
- Prior art keywords
- aromatics
- silicate
- sodium
- catalyst
- alumino
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Lifetime
Links
Images
Classifications
-
- 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
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B33/00—Silicon; Compounds thereof
- C01B33/20—Silicates
- C01B33/26—Aluminium-containing silicates, i.e. silico-aluminates
- C01B33/28—Base exchange silicates, e.g. zeolites
- C01B33/2807—Zeolitic silicoaluminates with a tridimensional crystalline structure possessing molecular sieve properties; Isomorphous compounds wherein a part of the aluminium ore of the silicon present may be replaced by other elements such as gallium, germanium, phosphorus; Preparation of zeolitic molecular sieves from molecular sieves of another type or from preformed reacting mixtures
-
- 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
Definitions
- the present invention relates to the production of alkyl aromatic compounds by reacting aromatic and olefinic hydrocarbons. More particularly, the present invention relates to a process for the production of alkyl aromatic hydrocarbon compounds of high anti-knock value, which are of suitable boiling range for use as motor fuels. Still more particularly, the present invention relates to a novel catalytic composition peculiarly adapted to produce high yields of alkylated aromatics.
- Alkylated aromatics boiling in the naphtha range are known to be capable, when added to naphthas boiling in the gasoline fraction, of imparting a high degree of anti-knock capability.
- the alkylating agent is most frequently an alkyl halide, an alcohol, or an alkene; the essential requirement is that the alkylating agent be capable of inter acting with the catalyst to produce a carbonium ion.
- the catalyst is a powerful electrophilic reagent, in the Lewis sense, such as AlC1 FeCl SbCl BF ZnCl TiCl HF, H2804, H3PO4, SiO Al O P205 and the like. These reactions are generally carried out at low temperatures and in particular when a Friedel-Crafts catalyst is employed, in the presence of a hydrogen halide such as HCl.
- Alumino-silicates of high alkylation activity may be prepared by mixing and heating sodium aluminate and sodium silicate, preferably metasilicate, under carefully controlled conditions to produce a crystalline product which is subsequently dehydrated under condition to preserve the crystalline structure.
- the sodium content of the crystalline aluminosilicate may be replaced by effecting ion exchange with an appropriate metal salt such as a group II, 111 or IV metal.
- the metal ion influences the size of the pore openings, as does the ratio of the reagents and the reaction conditions.
- the alkylation catalyst is prepared from a sodium silicate having a high ratio of soda to silica.
- the ratio is at least 0.8/1, and may be as high as 2/1.
- the ratio is 1/ 1
- the desired reagent is sodium metasilicate.
- Water glass or sodium silicates having lower Na O/siO ratios do not form the adsorbent crystals unless subjected to extended heat soaking or crystallization periods.
- the composition of the sodium aluminate is less critical than that of the sodium silicate.
- Sodium aluminates having any ratio of soda to alumina in the range of 1/1 to 3/1 may be employed; however, a sodium aluminate having a high ratio of soda to alumina is preferred, and a sodium aluminate having the ratio 1.5/1 Na O/Al O is particularly desirable.
- the amounts of sodium silicate solution and sodium aluminate solutions are such that the ratio of silica to alumina in the final mixture is at least 3/1 and preferably about 4/ 1l0/1.
- the method of mixing the sodium metasilicate and sodium aluminate solutions must be carried out in a manner allowing formation of a precipitate having a uniform composition.
- a preferred method is to add the sodium aluminate to the sodium metasilicate at ambient temperatures using rapid and efficient agitation to make a homogeneous paste. Thereafter the mixture is heated to about 180-215 F. for a period as long as 200 hours or more to ensure crystallization in the crystal form necessary to adsorb aromatic molecules. It has been found that the heat soaking period is essential to produce the desired product, which has a pore opening of about 13 Angstroms.
- a solution of sodium metasilicate is prepared in vessel 2 and of sodium aluminate in vessel 4.
- the concentration of the silicate may be in the range of about 30-300 grams of SiO per liter, preferably in the range of about 200 grams per liter.
- the solution of aluminate has a concentration in the range of 40400 grams A1 0 per liter, preferably about 200-300 grams per liter.
- the amounts of metasilicate and aluminate solutions employed are such that the ratio of silica to alumina in the final mixture is in the range of 3/ 1-10/ 1. A ratio of about 4/ l-8/ 1 is particularly desirable.
- Sodium aluminate solution comprising 5-25 A1 0 is passed via line 1 into a mixing zone 5 where it is contacted with a sodium silicate solution comprising -25% SiO as solid, introduced through line 3.
- the mixing zone is preferably maintained at ambient temperatures. Mixing should be rapid and efiicient, e.g., the impeller zone of a centrifugal pump.
- the relative amounts of silicate and aluminate introduced to the mixing zone is about 3.5/1 ratio SiO /Al O
- the resulting mixture, or slurry is then fed via line 7 through a heat exchanger 9 which is maintained at about 180 F. to 250 F. or higher.
- the heat exchanger may comprise water, or superheated steam, or high boiling organic materials, or heated fluid solids, at controlled temperature.
- the flow rate of the material through line 7 is adjusted so that the time interval spent in the heated zone 9 is sulficient to complete crystal formation. At about 210 F., this is about 3 to 24 hours; at higher temperatures, shorter times are required, while at lower temperatures, somewhat longer time is required.
- the effluent crystalline product is then taken via line 11 to a filter and subsequent finishing operations. If desired, a portion of the efiluent stream from the heated zone may be recycled via line 13 by a pump (not shown) to slurry line 7 to serve as seed material and possibly catalyst for the crystallization process.
- the precipitated sodium-aluminosilicate after the heatsoaking period, is withdrawn through line 11, passed to filtration and water-washing zone 17, and then dried and activated in calcination zone 15.
- Activation temperature may be in the range of 4001000 F., preferably about 700900 F.
- the process of manufacture may be modified in various ways, providing the critical features of the high ratio of Na O/SiO in the sodium silicate and of the high ratio of SiO /Al O and the heat soaking period are maintained.
- it may be desirable to base-exchange the recovered zeolite with another ion, such as calcium, to form a calcium sodium alumino-silicate.
- This baseexchange modifies the size of the pore openings.
- the filter cake of sodium alumino-silicate may be base-exchanged with a solution of a calcium salt or other salt solutions before drying, though this is not essential.
- the crystalline precipitate of sodium alumino-silicate may be dried, activated by heating to about 700 to 900 F. and used as such, or if desired, the dried alumino-silicate may be base-exchanged with a salt solution.
- the exchange reaction may be carried out in several stages if desired using a column contacting technique, countercurrent flow, or other known methods of carrying out base exchange reactions.
- very dilute solutions of calcium salt for example 0.01 to 0.1 molar, may be employed for the base exchange reaction; however, it is preferred to use more concentrated solutions, for example, in the range of about 0.5 to 3.0 molar.
- a solution of calcium chloride having a concentration in the range of about 5 to 20 percent by weight is particularly preferred.
- Base exchanging may be carried out by treating the wet precipitate in the filter with a salt solution, or by reslurrying the precipitate in a salt solution.
- a salt solution Besides sodium, other alkali aluminates and metasilicates such as potassium, lithium and the like may be employed.
- other water soluble salts may be employed in the base exchange reaction in place of calcium salts.
- salts of potassium, lithium, strontium, magnesium, zinc, cadmium, and the like may be employed. Magnesium is particularly desirable.
- the alkylation reaction is carried out in equipment of conventional type, one arrangement of which is illustrated in Figure 2.
- An aromatic, such as benzene or an aromatic concentrate is fed through line 2 along with .a gaseous olefin to a reactor 6 packed with the aluminosilicate catalyst and maintained at a temperature within the approximate range of 300 to 850 F., preferably 400 to 750 F., and at a pressure which may vary up to about 1000 p.s.i.g.
- the reaction product is passed through line 8 to gas separator 10 for recovery of unconverted olefins which are recycled via 12 to the alkylation reactor.
- Liquid product from this separator is transferred to a distillation column 16 for separation of unconverted aromatics, mono-alkyl aromatics, and any poly-alkyl aromatics formed.
- the unconverted aromatics fraction is recycled via 18 to the alkylation reactor while the mono-alkylated'aromatics are recovered as product.
- Poly-alkyl aromatics, such as the di-alkyl aromatics, will be recycled to the alkylation reaction if the yield of mono-alkyl aromatics is to be maximized, since these more highly alkylated products react with benzene in the presence of the alumino-silicate catalyst to form additional quantities of the mono-alkyl aromatic.
- the alumino-silicate catalyst is the formation, under normal operating conditions, of a high proportion of the mono-alkyl derivative. If, however, it is desired to maximize poly-alkyl aromatics production, the monoalkyl aromatic may be recycled to the reactor along with the unconverted aromatic while the poly-alkyl aromatics are recovered as product.
- the aromatic/ olefin mol ratio will preferably be about 1/1 to 10/1. If poly-alkyl aromatics are desired, the ratio is preferably about 0.5/1 or less.
- the adaptability of this catalytic material to various modes of contacting is outstanding in comparison with previously known catalysts.
- the alumino-sil-icate may be used in fixedbed or moving-bed reactors, as pellets or various shaped forms, as a fluidized powder, or as a powder dispersed or suspended in the liquid hydrocarbon or in some suitable fluid.
- the alumino-silicate not only is characterized by long life but is completely restored in activity after prolonged use by simple oxidation treatments with air or other oxygen-containing gas. The usual high catalyst losses and/or expense resulting from reworking of conventional acid type catalysts is avoided.
- the sodium aluminosilicate was prepared in aqueous medium at a final pH of 1012, and even after drying and calcining at 850 F. an aqueous suspension showed a pH .of 10-11, indicating the basic nature of this catalyst.
- Alkylate Isopropylbenzene, Vol. percent Polyisopropylbenzene, Vol. percent"
- EXAMPLE 2 A 500 gram sample of the 13 Angstrom pore diameter sodium zeolite was slurried in a liter of water and 1500 cc. of magnesium chloride solution added. The base exchange operation was repeated twice with fresh 12% magnesium chloride solution each time. The wet pellets were dried in an oven at 250 F. and calcined for 4 hours at 850 F. This material when analyzed showed that about 76% of the original soda content was replaced with magnesia.
- the magnesium zeolite thus formed was tested for alkylation activity by contacting with propylene and toluene mixtures at 850 F. at atmospheric pressure. Feed rates were about 0.64 v./v./hr. for the toluene and about 5 mol propylene per mol of toluene feed. The results were as follows:
- magnesium form of this zeolite is also an active alkylating agent for aromatics with olefins.
- isobutane and isopentane may be alkylated with propylene or isobutylene.
- the alumino-silicate may be used to concentrate the aromatic reactant from such materials as straight run, thermal or catalytic naphthas in which the aromatic content is usually quite low, and hence these streams could not normally be used as alkylation feeds.
- Aromatics for the alkylation can similarly be adsorbed from hydroformates or aromatized naphthas.
- Olefinic reactants may likewise be concentrated from a variety of feed sources.
- a process for alkylating an aromatic hydrocarbon with an olefin which comprises contacting the same in the presence of a crystalline metallic alumino-silicate having a uniform pore opening of about 6 to 15 Angstrom units at a temperature of from about 300 to 850 F.
- An improved process for alkylating aromatic hydrocarbons with olefins which comprises passing an olefinic stream to an alkylation zone, contacting said reactants with a crystalline metallic alumino-silicate having uniform pore openings of 13 Angstroms at about 400 to 750 F., and recovering good yields of alkylated aromatics from said zone.
- An improved process for preparing a high octane motor fuel which comprises passing an aromatic hydrocarbon having from C to C carbon atoms and a low boiling olefin to an alkylation zone, contacting said mixture at a temperature of from about 400 to 750 F., with a metallic crystalline alumino-silicate catalyst having uniform pore openings of 13 Angstroms, forming a reaction product comprising monoalkylated and poly-alkylated aromatics, separating a high octane gasoline comprising substantial amounts of monoalkylated aromatics, and recycling poly-alkylated aromatics to said alkylation zone.
Description
ALKYLATION OF AROMATICS William Judson Mattox and William Floyd Arey, Jr.,
Baton Rouge, La., assignors to Esso Research and Engineering Company, a corporation of Delaware Application January 29, 1957, Serial No. 636,909 6 Claims. (Cl. 260-671) The present invention relates to the production of alkyl aromatic compounds by reacting aromatic and olefinic hydrocarbons. More particularly, the present invention relates to a process for the production of alkyl aromatic hydrocarbon compounds of high anti-knock value, which are of suitable boiling range for use as motor fuels. Still more particularly, the present invention relates to a novel catalytic composition peculiarly adapted to produce high yields of alkylated aromatics.
Processes for the cracking of gas oil and similar petroleum fractions to gasoline result in the production of normally gaseous hydrocarbons such as ethylene, propylene, the butylenes and higher. Appreciable quantities of naphtha fraction product are also olefinic, and have relatively high octane values. However, with the increasing development of high compression engines, these fuels are not satisfactory from an anti-detonation viewpoint.
Alkylated aromatics boiling in the naphtha range are known to be capable, when added to naphthas boiling in the gasoline fraction, of imparting a high degree of anti-knock capability. Various methods for the production of alkylated aromatics by combining olefinic or similar unsaturated material, either from products of a conventional thermal or catalytic cracking process or from other sources, with aromatic compounds such as benzene or its homologues, have been proposed.
The prior art processes in general employ an acidic catalyst. The alkylating agent is most frequently an alkyl halide, an alcohol, or an alkene; the essential requirement is that the alkylating agent be capable of inter acting with the catalyst to produce a carbonium ion. The catalyst is a powerful electrophilic reagent, in the Lewis sense, such as AlC1 FeCl SbCl BF ZnCl TiCl HF, H2804, H3PO4, SiO Al O P205 and the like. These reactions are generally carried out at low temperatures and in particular when a Friedel-Crafts catalyst is employed, in the presence of a hydrogen halide such as HCl.
The prior art processes carried out with acidic catalysts are open to many objections. Beside the corrosive nature of the catalyst, the catalyst consumption is high as are regeneration costs, and yields of alkylate boiling in the gasoline range are low, and complicated separations and recycle of feed are required. Furthermore, these catalysts tend to polymerize the olefinic reagents and thus minimize available starting materials. 7
It is an object of the present invention to provide a highly eflicient process for the production of alkyl aromatic compounds.
It is a still further object of this invention to employ a non-acidic catalyst for alkylating aromatics with olefins which provides optimum yields of alkylated aromatics boiling within the naphtha boiling range and minimizes the formation of higher boiling compositions.
Other and further objects and advantages of the present invention will become more clear hereinafter.
nited States Patent 0 2,904,607; Fatented Sept. 15, 1959 It has now been found that aromatic may be particularly readily alkylated with olefins by contacting the reagents at moderately elevated temperatures with a crystalline alumino-silicate catalyst having pore openings adequate to admit freely the individual aromatic and olefinic molecule, and which catalysts have a basic rather than the hitherto desired acidic reaction. The pore opening will therefore be about 6 to 15 Angstroms. Too large an opening, however, does not permit the high activity because of the concomitant decrease in available surface area.
Alumino-silicates of high alkylation activity may be prepared by mixing and heating sodium aluminate and sodium silicate, preferably metasilicate, under carefully controlled conditions to produce a crystalline product which is subsequently dehydrated under condition to preserve the crystalline structure. The sodium content of the crystalline aluminosilicate may be replaced by effecting ion exchange with an appropriate metal salt such as a group II, 111 or IV metal. The metal ion influences the size of the pore openings, as does the ratio of the reagents and the reaction conditions.
In accordance with the present invention, the alkylation catalyst is prepared from a sodium silicate having a high ratio of soda to silica. The ratio is at least 0.8/1, and may be as high as 2/1. Preferably, however, the ratio is 1/ 1, and the desired reagent is sodium metasilicate. Water glass or sodium silicates having lower Na O/siO ratios do not form the adsorbent crystals unless subjected to extended heat soaking or crystallization periods.
The composition of the sodium aluminate is less critical than that of the sodium silicate. Sodium aluminates having any ratio of soda to alumina in the range of 1/1 to 3/1 may be employed; however, a sodium aluminate having a high ratio of soda to alumina is preferred, and a sodium aluminate having the ratio 1.5/1 Na O/Al O is particularly desirable. The amounts of sodium silicate solution and sodium aluminate solutions are such that the ratio of silica to alumina in the final mixture is at least 3/1 and preferably about 4/ 1l0/1. The method of mixing the sodium metasilicate and sodium aluminate solutions must be carried out in a manner allowing formation of a precipitate having a uniform composition. A preferred method is to add the sodium aluminate to the sodium metasilicate at ambient temperatures using rapid and efficient agitation to make a homogeneous paste. Thereafter the mixture is heated to about 180-215 F. for a period as long as 200 hours or more to ensure crystallization in the crystal form necessary to adsorb aromatic molecules. It has been found that the heat soaking period is essential to produce the desired product, which has a pore opening of about 13 Angstroms.
The process of preparing the catalyst may be more clearly understood when read in conjunction with Figure 1, which is a diagrammatic representation of a preferred method of manufacturing the large pore material. Turning now to that figure, a solution of sodium metasilicate is prepared in vessel 2 and of sodium aluminate in vessel 4. The concentration of the silicate may be in the range of about 30-300 grams of SiO per liter, preferably in the range of about 200 grams per liter. The solution of aluminate has a concentration in the range of 40400 grams A1 0 per liter, preferably about 200-300 grams per liter. The amounts of metasilicate and aluminate solutions employed are such that the ratio of silica to alumina in the final mixture is in the range of 3/ 1-10/ 1. A ratio of about 4/ l-8/ 1 is particularly desirable.
Sodium aluminate solution comprising 5-25 A1 0 is passed via line 1 into a mixing zone 5 where it is contacted with a sodium silicate solution comprising -25% SiO as solid, introduced through line 3. The mixing zone is preferably maintained at ambient temperatures. Mixing should be rapid and efiicient, e.g., the impeller zone of a centrifugal pump. The relative amounts of silicate and aluminate introduced to the mixing zone is about 3.5/1 ratio SiO /Al O The resulting mixture, or slurry, is then fed via line 7 through a heat exchanger 9 which is maintained at about 180 F. to 250 F. or higher. The heat exchanger may comprise water, or superheated steam, or high boiling organic materials, or heated fluid solids, at controlled temperature. During the time of passage through the heated zone, the slurry undergoes crystallization to give the desired adsorbent structure. The flow rate of the material through line 7 is adjusted so that the time interval spent in the heated zone 9 is sulficient to complete crystal formation. At about 210 F., this is about 3 to 24 hours; at higher temperatures, shorter times are required, while at lower temperatures, somewhat longer time is required. The effluent crystalline product is then taken via line 11 to a filter and subsequent finishing operations. If desired, a portion of the efiluent stream from the heated zone may be recycled via line 13 by a pump (not shown) to slurry line 7 to serve as seed material and possibly catalyst for the crystallization process.
The precipitated sodium-aluminosilicate, after the heatsoaking period, is withdrawn through line 11, passed to filtration and water-washing zone 17, and then dried and activated in calcination zone 15. Activation temperature may be in the range of 4001000 F., preferably about 700900 F.
The process of manufacture may be modified in various ways, providing the critical features of the high ratio of Na O/SiO in the sodium silicate and of the high ratio of SiO /Al O and the heat soaking period are maintained. Thus, it may be desirable to base-exchange the recovered zeolite with another ion, such as calcium, to form a calcium sodium alumino-silicate. This baseexchange modifies the size of the pore openings. Where this is done, the filter cake of sodium alumino-silicate may be base-exchanged with a solution of a calcium salt or other salt solutions before drying, though this is not essential. The crystalline precipitate of sodium alumino-silicate may be dried, activated by heating to about 700 to 900 F. and used as such, or if desired, the dried alumino-silicate may be base-exchanged with a salt solution.
The exchange reaction may be carried out in several stages if desired using a column contacting technique, countercurrent flow, or other known methods of carrying out base exchange reactions. If desired, very dilute solutions of calcium salt, for example 0.01 to 0.1 molar, may be employed for the base exchange reaction; however, it is preferred to use more concentrated solutions, for example, in the range of about 0.5 to 3.0 molar. A solution of calcium chloride having a concentration in the range of about 5 to 20 percent by weight is particularly preferred.
Base exchanging may be carried out by treating the wet precipitate in the filter with a salt solution, or by reslurrying the precipitate in a salt solution. Besides sodium, other alkali aluminates and metasilicates such as potassium, lithium and the like may be employed. Similarly, other water soluble salts may be employed in the base exchange reaction in place of calcium salts. For example, salts of potassium, lithium, strontium, magnesium, zinc, cadmium, and the like may be employed. Magnesium is particularly desirable.
The alkylation reaction is carried out in equipment of conventional type, one arrangement of which is illustrated in Figure 2. An aromatic, such as benzene or an aromatic concentrate is fed through line 2 along with .a gaseous olefin to a reactor 6 packed with the aluminosilicate catalyst and maintained at a temperature within the approximate range of 300 to 850 F., preferably 400 to 750 F., and at a pressure which may vary up to about 1000 p.s.i.g. The reaction product is passed through line 8 to gas separator 10 for recovery of unconverted olefins which are recycled via 12 to the alkylation reactor. Liquid product from this separator is transferred to a distillation column 16 for separation of unconverted aromatics, mono-alkyl aromatics, and any poly-alkyl aromatics formed. The unconverted aromatics fraction is recycled via 18 to the alkylation reactor while the mono-alkylated'aromatics are recovered as product. Poly-alkyl aromatics, such as the di-alkyl aromatics, will be recycled to the alkylation reaction if the yield of mono-alkyl aromatics is to be maximized, since these more highly alkylated products react with benzene in the presence of the alumino-silicate catalyst to form additional quantities of the mono-alkyl aromatic. One of the distinct advantages, therefore, to the use of the alumino-silicate catalyst is the formation, under normal operating conditions, of a high proportion of the mono-alkyl derivative. If, however, it is desired to maximize poly-alkyl aromatics production, the monoalkyl aromatic may be recycled to the reactor along with the unconverted aromatic while the poly-alkyl aromatics are recovered as product. When producing monoalkyl benzenes, the aromatic/ olefin mol ratio will preferably be about 1/1 to 10/1. If poly-alkyl aromatics are desired, the ratio is preferably about 0.5/1 or less.
In addition to the advantages already mentioned for the alumino-silicate catalyst, the adaptability of this catalytic material to various modes of contacting is outstanding in comparison with previously known catalysts. For example, the alumino-sil-icate may be used in fixedbed or moving-bed reactors, as pellets or various shaped forms, as a fluidized powder, or as a powder dispersed or suspended in the liquid hydrocarbon or in some suitable fluid. Further, the alumino-silicate not only is characterized by long life but is completely restored in activity after prolonged use by simple oxidation treatments with air or other oxygen-containing gas. The usual high catalyst losses and/or expense resulting from reworking of conventional acid type catalysts is avoided.
The process of the present invention may be further illustrated by the following example.
A crystalline sodium alumino-silicate having a pore opening of about 13 Angstroms, and prepared in a manner similar to that described heretofore was employed as an aromatic alkylation catalyst. The sodium aluminosilicate was prepared in aqueous medium at a final pH of 1012, and even after drying and calcining at 850 F. an aqueous suspension showed a pH .of 10-11, indicating the basic nature of this catalyst.
EXAMPLE 1 Alkylation of benzene with propylene sodium alumina-silicate catalysts [Temp-400 F.; pressure-atm.; CuHG/CaHo mo1ratio1.5/1]
Test N0 1 2 Alumino-Silicate Catalyst:
Pore Opening, A Composition Reaction Product:
Isopropylbenzene, Vol. percent Polyisopropylbenzene, Vol. percenL.
Alkylate: Isopropylbenzene, Vol. percent Polyisopropylbenzene, Vol. percent" These data show clearly that it is not enough to employ a zeolite for the alkylation catalyst, but a zeolite having pore openings large enough to admit the reactants. A 4 Angstrom pore opening is too small for this purpose and thus no product was obtained. On the other hand, with the 13 Angstrom pore openings, 83% of the alkylation product that was obtained was mono-alkyl aromatic. To produce alkylated product containing this high a percentage of cumene with phosphoric activated-kieselguhr catalyst (900 p.s.i., and 525 F.) requires a benzene to propylene mol ratio of 4/ l and a correspondingly high recycle of benzene.
EXAMPLE 2 A 500 gram sample of the 13 Angstrom pore diameter sodium zeolite was slurried in a liter of water and 1500 cc. of magnesium chloride solution added. The base exchange operation was repeated twice with fresh 12% magnesium chloride solution each time. The wet pellets were dried in an oven at 250 F. and calcined for 4 hours at 850 F. This material when analyzed showed that about 76% of the original soda content was replaced with magnesia.
The magnesium zeolite thus formed was tested for alkylation activity by contacting with propylene and toluene mixtures at 850 F. at atmospheric pressure. Feed rates were about 0.64 v./v./hr. for the toluene and about 5 mol propylene per mol of toluene feed. The results were as follows:
Liquid product, C 4- Mol percent toluene 69.3 Mol percent C C C aromatics 17.7
These data show that the magnesium form of this zeolite is also an active alkylating agent for aromatics with olefins.
Not only may aromatics be alkylated in accordance with the present invention, but also isoparaflins and alicyclic compounds. Thus, isobutane and isopentane may be alkylated with propylene or isobutylene.
It is also advantageous to employ these 13 Angstrom pore alumino-silicates for concentrating aromatics or isoparaifins from hydrocarbon streams. For example, the alumino-silicate may be used to concentrate the aromatic reactant from such materials as straight run, thermal or catalytic naphthas in which the aromatic content is usually quite low, and hence these streams could not normally be used as alkylation feeds. Aromatics for the alkylation can similarly be adsorbed from hydroformates or aromatized naphthas. Olefinic reactants may likewise be concentrated from a variety of feed sources.
What is claimed is:
1. A process for alkylating an aromatic hydrocarbon with an olefin which comprises contacting the same in the presence of a crystalline metallic alumino-silicate having a uniform pore opening of about 6 to 15 Angstrom units at a temperature of from about 300 to 850 F.
2. An improved process for alkylating aromatic hydrocarbons with olefins which comprises passing an olefinic stream to an alkylation zone, contacting said reactants with a crystalline metallic alumino-silicate having uniform pore openings of 13 Angstroms at about 400 to 750 F., and recovering good yields of alkylated aromatics from said zone.
3. An improved process for preparing a high octane motor fuel which comprises passing an aromatic hydrocarbon having from C to C carbon atoms and a low boiling olefin to an alkylation zone, contacting said mixture at a temperature of from about 400 to 750 F., with a metallic crystalline alumino-silicate catalyst having uniform pore openings of 13 Angstroms, forming a reaction product comprising monoalkylated and poly-alkylated aromatics, separating a high octane gasoline comprising substantial amounts of monoalkylated aromatics, and recycling poly-alkylated aromatics to said alkylation zone.
4. The process of claim 3 wherein said catalyst is a sodium alumino-silicate.
5. The process of claim 3 wherein said catalyst is a magnesium alumino-silicate.
6. The process of claim 3 wherein said aromatics are concentrated from a dilute aromatics comprising stream by contacting said stream with said alumino-silicates.
References Cited in the file of this patent UNITED STATES PATENTS 1,728,732 Jaeger Sept. 17, 1929 2,197,862 Hyman Apr. 23, 1940 2,253,285 Connolly Aug. 19, 1941 2,294,779 Hyman 'Sept. 1, 1942 2,317,803 Reeves et al Apr. 27, 1943 2,698,305 Plank et a1. Dec. 28, 1954
Claims (1)
1. A PROCESS FOR ALKYLATING AN AROMATIC HYDROCARBON WITH AN OLEFIN WHICH COMPRISE CONTACTING THE SAME IN THE PRESENCE OF A CRYSTALLINE METALLIC ALUMINO-SILICATE HAVING A UNIFORM PORE OPENING OF ABOUT 6 TO 15 ANGSTROM UNITS AT A TEMPERATURE OF FROM ABOUT 300* TO 850*F.
Priority Applications (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US636909A US2904607A (en) | 1957-01-29 | 1957-01-29 | Alkylation of aromatics |
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US636909A US2904607A (en) | 1957-01-29 | 1957-01-29 | Alkylation of aromatics |
Publications (1)
Publication Number | Publication Date |
---|---|
US2904607A true US2904607A (en) | 1959-09-15 |
Family
ID=24553848
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
US636909A Expired - Lifetime US2904607A (en) | 1957-01-29 | 1957-01-29 | Alkylation of aromatics |
Country Status (1)
Country | Link |
---|---|
US (1) | US2904607A (en) |
Cited By (69)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US2971824A (en) * | 1958-08-11 | 1961-02-14 | Socony Mobil Oil Co Inc | Process for recovering sulfur from hydrogen sulfide-containing gases |
US2971904A (en) * | 1957-02-12 | 1961-02-14 | Exxon Research Engineering Co | Petroleum process catalyst supported on a molecular sieve zeolite |
US2992283A (en) * | 1959-07-30 | 1961-07-11 | Exxon Research Engineering Co | Preparation of aromatic and saturated hydrocarbons |
US3018264A (en) * | 1957-11-25 | 1962-01-23 | Union Carbide Corp | Polyepoxide compositions |
US3033778A (en) * | 1958-11-07 | 1962-05-08 | Socony Mobil Oil Co Inc | Catalytic conversion in the presence of carbon dioxide promoted crystalline metal aluminosilicates |
US3054657A (en) * | 1958-03-31 | 1962-09-18 | Union Carbide Corp | Crystalline zeolite s |
US3071434A (en) * | 1960-01-20 | 1963-01-01 | Socony Mobil Oil Co Inc | Process for makling crystalline zeolites |
US3119660A (en) * | 1960-09-26 | 1964-01-28 | Union Carbide Corp | Process for producing molecular sieve bodies |
US3119659A (en) * | 1960-09-26 | 1964-01-28 | Union Carbide Corp | Process for producing molecular sieve bodies |
US3121754A (en) * | 1958-06-13 | 1964-02-18 | Exxon Research Engineering Co | Catalytic process |
US3140322A (en) * | 1958-08-14 | 1964-07-07 | Socony Mobil Oil Co Inc | Selective catalytic conversion |
US3140249A (en) * | 1960-07-12 | 1964-07-07 | Socony Mobil Oil Co Inc | Catalytic cracking of hydrocarbons with a crystalline zeolite catalyst composite |
US3151174A (en) * | 1961-05-02 | 1964-09-29 | Givaudan Corp | 1, 1-dimethyl tetrahydronaphthindans and process for preparing same |
US3152192A (en) * | 1961-05-02 | 1964-10-06 | Givandan Corp | Process for preparing trialkyl-1, 1-dimethylindans |
US3251897A (en) * | 1962-12-20 | 1966-05-17 | Socony Mobil Oil Co Inc | Alkylation of aromatic compounds in the presence of an alumino-silicate catalyst |
US3321272A (en) * | 1962-12-27 | 1967-05-23 | Mobil Oil Corp | Process for making crystalline zeolites |
US3417148A (en) * | 1967-06-30 | 1968-12-17 | Universal Oil Prod Co | Alkylation process |
US3425800A (en) * | 1967-10-05 | 1969-02-04 | Aluminum Co Of America | Production of crystalline zeolites |
US3499941A (en) * | 1965-12-10 | 1970-03-10 | Socony Mobil Oil Co | Production of organic halides |
US3518317A (en) * | 1966-04-21 | 1970-06-30 | Ici Ltd | Production of substituted phenols |
US3541180A (en) * | 1968-06-25 | 1970-11-17 | Sun Oil Co | Alkylation of isobutene with ethylene or propylene and with an alumino-silicate catalyst |
US3720756A (en) * | 1970-01-22 | 1973-03-13 | Bayer Ag | Production of synthetic zeolites of faujasite structure |
DE2321399A1 (en) * | 1972-04-28 | 1973-11-15 | Mobil Oil Corp | METHOD OF VAPOR PHASE ALKYLATION IN THE PRESENCE OF A CRYSTALLINE ALUMINOSILICATE CATALYST |
DE2321471A1 (en) * | 1972-05-12 | 1973-11-29 | Mobil Oil Corp | PROCESS FOR STEAM PHASE ALKYLATION OF AROMATIC HYDROCARBONS |
USB366861I5 (en) * | 1973-06-04 | 1975-01-28 | ||
JPS507062B1 (en) * | 1964-07-07 | 1975-03-20 | ||
DE2624097A1 (en) * | 1975-05-29 | 1976-12-09 | Mobil Oil Corp | PROCESS FOR THE ALKYLATION OF AROMATIC HYDROCARBONS |
US4016246A (en) * | 1965-04-09 | 1977-04-05 | Laporte Industries Limited | Manufacture of synthetic zeolites |
US4049737A (en) * | 1975-09-18 | 1977-09-20 | Mobil Oil Corporation | Propylation of toluene |
US4072729A (en) * | 1975-06-16 | 1978-02-07 | Uop Inc. | Simulated moving bed reaction process |
US4085156A (en) * | 1968-01-15 | 1978-04-18 | Mobil Oil Corporation | Conversion of hydrocarbons |
US4150100A (en) * | 1978-06-13 | 1979-04-17 | Pq Corporation | Preparing zeolite NaA |
US4157950A (en) * | 1961-10-04 | 1979-06-12 | Mobil Oil Corporation | Conversion of hydrocarbons |
US4248847A (en) * | 1977-02-08 | 1981-02-03 | Kali-Chemie Ag | Process for preparing a substantially crystalline sodium aluminosilicate |
US4267158A (en) * | 1979-03-15 | 1981-05-12 | Henkel Kommanditgesellschaft Auf Aktien | Continuous process for the production of amorphouse sodium aluminosilicate |
US4278649A (en) * | 1979-03-15 | 1981-07-14 | Henkel Kommanditgesellschaft Auf Aktien | Continuous process for the production of amorphous sodium aluminosilicate in an elongated reaction zone |
US4291185A (en) * | 1978-12-14 | 1981-09-22 | Mobil Oil Corporation | Alkylation of benzene in petroleum |
US4306106A (en) * | 1978-06-05 | 1981-12-15 | Mobil Oil Corporation | Conversion of polar compounds using a ZSM-5 zeolite catalyst |
US4314979A (en) * | 1977-07-29 | 1982-02-09 | Pcuk Produits Chimiques Ugine Kuhlmann | Industrial process for continuous production of zeolite A |
US4371510A (en) * | 1979-10-13 | 1983-02-01 | Henkel Kommanditgesellschaft Auf Aktien | Process for the continuous crystallization of zeolitic sodium aluminosilicates of smallest particle size |
US4374093A (en) * | 1981-02-20 | 1983-02-15 | Mobil Oil Corporation | Continuous-stream upflow zeolite crystallization apparatus |
US4379761A (en) * | 1981-01-08 | 1983-04-12 | Mobil Oil Corporation | Catalyst and process for making said catalyst |
US4385042A (en) * | 1979-08-06 | 1983-05-24 | Mobil Oil Corporation | Continuous reaction/separation method for nucleated growth reactions |
US4393262A (en) * | 1978-12-14 | 1983-07-12 | Mobil Oil Corporation | Production of isopropylbenzene |
US4421941A (en) * | 1981-01-08 | 1983-12-20 | Mobil Oil Corporation | Catalyst and process for selective production of para-dialkysubstituted benzenes |
EP0308097A1 (en) | 1987-09-02 | 1989-03-22 | Mobil Oil Corporation | Transalkylation of polyalkylaromatic hydrocarbons |
US4885426A (en) * | 1987-09-02 | 1989-12-05 | Mobil Oil Corporation | Transalkylation of polyaromatics |
US4922053A (en) * | 1989-05-24 | 1990-05-01 | Fina Technology, Inc. | Process for ethylbenzene production |
US4962256A (en) * | 1988-10-06 | 1990-10-09 | Mobil Oil Corp. | Process for preparing long chain alkyl aromatic compounds |
FR2650273A1 (en) * | 1989-07-26 | 1991-02-01 | Michelin Rech Tech | CYCLOALKYLATION OF AROMATIC COMPOUNDS ON ZEOLITHES |
US4992606A (en) * | 1988-10-06 | 1991-02-12 | Mobil Oil Corp. | Process for preparing short chain alkyl aromatic compounds |
US5019670A (en) * | 1986-07-29 | 1991-05-28 | Mobil Oil Corporation | Process for producing alkylaromatic lubricant fluids |
US5026943A (en) * | 1988-05-09 | 1991-06-25 | Mobil Oil Corp | Catalytic conversion over catalyst comprising synthetic crystal MCM-35 |
US5030785A (en) * | 1988-10-06 | 1991-07-09 | Mobil Oil Corp. | Process for preparing long chain alkyl aromatic compounds employing Lewis acid-promoted zeolite catalysts |
US5043503A (en) * | 1990-08-14 | 1991-08-27 | Mobil Oil Corporation | Production of lubricant stocks from polycyclic paraffins |
US5105042A (en) * | 1989-05-30 | 1992-04-14 | Mobil Oil Corp. | Sulfated layered titanium oxide catalysts in process for preparing long chain alkyl aromatic compounds |
US5107049A (en) * | 1986-07-29 | 1992-04-21 | Mobil Oil Corporation | Stabilization of polyalpha-olefins |
US5145817A (en) * | 1991-05-24 | 1992-09-08 | The Dow Chemical Company | Alkylation process using dual metal ultrastable Y zeolite |
US5157185A (en) * | 1989-09-01 | 1992-10-20 | Mobil Oil Corporation | Alkylation of aromatics |
US5252197A (en) * | 1992-09-28 | 1993-10-12 | Abb Lummus Crest Inc. | Process for upgrading gasolines and other hydrocarbon mixtures |
US5334795A (en) * | 1990-06-28 | 1994-08-02 | Mobil Oil Corp. | Production of ethylbenzene |
US5434325A (en) * | 1993-06-21 | 1995-07-18 | Deltech Corporation | Process for the production of tertiary butylethylbenzene |
US5488194A (en) * | 1994-05-16 | 1996-01-30 | Mobil Oil Corp. | Selective production of para-dialkyl substituted benzenes and catalyst therefor |
US5569805A (en) * | 1993-10-18 | 1996-10-29 | Mobil Oil Corporation | Catalytic conversion of aromatic compounds |
US5900520A (en) * | 1995-01-23 | 1999-05-04 | Mobil Oil Corporation | Aromatics alkylation |
US5939597A (en) * | 1994-11-10 | 1999-08-17 | Mobil Oil Corporation | Fluid bed process for para-xylene production |
US6010617A (en) * | 1992-11-13 | 2000-01-04 | Mobil Oil Corporation | Process for producing non-carcinogenic coal-tar-derived products |
EP1456154A1 (en) | 2001-12-20 | 2004-09-15 | Polimeri Europa S.p.A. | Process for the alkylation of aromatic compounds |
US7954254B2 (en) * | 2002-05-15 | 2011-06-07 | Nederlandse Organisatie Voor Toegepast-Natuurwetenschappelijk Onderzoek Tno | Method for drying a product using a regenerative adsorbent |
Citations (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US1728732A (en) * | 1926-10-19 | 1929-09-17 | Selden Co | Base-exchange body |
US2197862A (en) * | 1938-03-21 | 1940-04-23 | Velsicol Corp | Process for polymerizing unsaturated gases |
US2253285A (en) * | 1938-03-29 | 1941-08-19 | Standard Oil Dev Co | Cracking oil by leached zeolites |
US2294779A (en) * | 1939-11-22 | 1942-09-01 | Velsicol Corp | Contact decolorization |
US2317803A (en) * | 1939-12-30 | 1943-04-27 | Standard Oil Dev Co | Catalytic process |
US2698305A (en) * | 1951-03-23 | 1954-12-28 | Socony Vacuum Oil Co Inc | Process for controlling pore size |
-
1957
- 1957-01-29 US US636909A patent/US2904607A/en not_active Expired - Lifetime
Patent Citations (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US1728732A (en) * | 1926-10-19 | 1929-09-17 | Selden Co | Base-exchange body |
US2197862A (en) * | 1938-03-21 | 1940-04-23 | Velsicol Corp | Process for polymerizing unsaturated gases |
US2253285A (en) * | 1938-03-29 | 1941-08-19 | Standard Oil Dev Co | Cracking oil by leached zeolites |
US2294779A (en) * | 1939-11-22 | 1942-09-01 | Velsicol Corp | Contact decolorization |
US2317803A (en) * | 1939-12-30 | 1943-04-27 | Standard Oil Dev Co | Catalytic process |
US2698305A (en) * | 1951-03-23 | 1954-12-28 | Socony Vacuum Oil Co Inc | Process for controlling pore size |
Cited By (75)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US2971904A (en) * | 1957-02-12 | 1961-02-14 | Exxon Research Engineering Co | Petroleum process catalyst supported on a molecular sieve zeolite |
US3018264A (en) * | 1957-11-25 | 1962-01-23 | Union Carbide Corp | Polyepoxide compositions |
US3054657A (en) * | 1958-03-31 | 1962-09-18 | Union Carbide Corp | Crystalline zeolite s |
US3121754A (en) * | 1958-06-13 | 1964-02-18 | Exxon Research Engineering Co | Catalytic process |
US2971824A (en) * | 1958-08-11 | 1961-02-14 | Socony Mobil Oil Co Inc | Process for recovering sulfur from hydrogen sulfide-containing gases |
US3140322A (en) * | 1958-08-14 | 1964-07-07 | Socony Mobil Oil Co Inc | Selective catalytic conversion |
US3033778A (en) * | 1958-11-07 | 1962-05-08 | Socony Mobil Oil Co Inc | Catalytic conversion in the presence of carbon dioxide promoted crystalline metal aluminosilicates |
US2992283A (en) * | 1959-07-30 | 1961-07-11 | Exxon Research Engineering Co | Preparation of aromatic and saturated hydrocarbons |
US3071434A (en) * | 1960-01-20 | 1963-01-01 | Socony Mobil Oil Co Inc | Process for makling crystalline zeolites |
US3140249A (en) * | 1960-07-12 | 1964-07-07 | Socony Mobil Oil Co Inc | Catalytic cracking of hydrocarbons with a crystalline zeolite catalyst composite |
US3119659A (en) * | 1960-09-26 | 1964-01-28 | Union Carbide Corp | Process for producing molecular sieve bodies |
US3119660A (en) * | 1960-09-26 | 1964-01-28 | Union Carbide Corp | Process for producing molecular sieve bodies |
US3151174A (en) * | 1961-05-02 | 1964-09-29 | Givaudan Corp | 1, 1-dimethyl tetrahydronaphthindans and process for preparing same |
US3152192A (en) * | 1961-05-02 | 1964-10-06 | Givandan Corp | Process for preparing trialkyl-1, 1-dimethylindans |
US4157950A (en) * | 1961-10-04 | 1979-06-12 | Mobil Oil Corporation | Conversion of hydrocarbons |
US3251897A (en) * | 1962-12-20 | 1966-05-17 | Socony Mobil Oil Co Inc | Alkylation of aromatic compounds in the presence of an alumino-silicate catalyst |
US3321272A (en) * | 1962-12-27 | 1967-05-23 | Mobil Oil Corp | Process for making crystalline zeolites |
JPS507062B1 (en) * | 1964-07-07 | 1975-03-20 | ||
US4016246A (en) * | 1965-04-09 | 1977-04-05 | Laporte Industries Limited | Manufacture of synthetic zeolites |
US3499941A (en) * | 1965-12-10 | 1970-03-10 | Socony Mobil Oil Co | Production of organic halides |
US3518317A (en) * | 1966-04-21 | 1970-06-30 | Ici Ltd | Production of substituted phenols |
US3417148A (en) * | 1967-06-30 | 1968-12-17 | Universal Oil Prod Co | Alkylation process |
US3425800A (en) * | 1967-10-05 | 1969-02-04 | Aluminum Co Of America | Production of crystalline zeolites |
US4085156A (en) * | 1968-01-15 | 1978-04-18 | Mobil Oil Corporation | Conversion of hydrocarbons |
US3541180A (en) * | 1968-06-25 | 1970-11-17 | Sun Oil Co | Alkylation of isobutene with ethylene or propylene and with an alumino-silicate catalyst |
US3720756A (en) * | 1970-01-22 | 1973-03-13 | Bayer Ag | Production of synthetic zeolites of faujasite structure |
DE2321399A1 (en) * | 1972-04-28 | 1973-11-15 | Mobil Oil Corp | METHOD OF VAPOR PHASE ALKYLATION IN THE PRESENCE OF A CRYSTALLINE ALUMINOSILICATE CATALYST |
FR2181940A1 (en) * | 1972-04-28 | 1973-12-07 | Mobil Oil | |
DE2321471A1 (en) * | 1972-05-12 | 1973-11-29 | Mobil Oil Corp | PROCESS FOR STEAM PHASE ALKYLATION OF AROMATIC HYDROCARBONS |
USB366861I5 (en) * | 1973-06-04 | 1975-01-28 | ||
DE2624097A1 (en) * | 1975-05-29 | 1976-12-09 | Mobil Oil Corp | PROCESS FOR THE ALKYLATION OF AROMATIC HYDROCARBONS |
US4072729A (en) * | 1975-06-16 | 1978-02-07 | Uop Inc. | Simulated moving bed reaction process |
US4049737A (en) * | 1975-09-18 | 1977-09-20 | Mobil Oil Corporation | Propylation of toluene |
US4248847A (en) * | 1977-02-08 | 1981-02-03 | Kali-Chemie Ag | Process for preparing a substantially crystalline sodium aluminosilicate |
US4314979A (en) * | 1977-07-29 | 1982-02-09 | Pcuk Produits Chimiques Ugine Kuhlmann | Industrial process for continuous production of zeolite A |
US4306106A (en) * | 1978-06-05 | 1981-12-15 | Mobil Oil Corporation | Conversion of polar compounds using a ZSM-5 zeolite catalyst |
US4150100A (en) * | 1978-06-13 | 1979-04-17 | Pq Corporation | Preparing zeolite NaA |
US4393262A (en) * | 1978-12-14 | 1983-07-12 | Mobil Oil Corporation | Production of isopropylbenzene |
US4291185A (en) * | 1978-12-14 | 1981-09-22 | Mobil Oil Corporation | Alkylation of benzene in petroleum |
US4267158A (en) * | 1979-03-15 | 1981-05-12 | Henkel Kommanditgesellschaft Auf Aktien | Continuous process for the production of amorphouse sodium aluminosilicate |
US4278649A (en) * | 1979-03-15 | 1981-07-14 | Henkel Kommanditgesellschaft Auf Aktien | Continuous process for the production of amorphous sodium aluminosilicate in an elongated reaction zone |
US4385042A (en) * | 1979-08-06 | 1983-05-24 | Mobil Oil Corporation | Continuous reaction/separation method for nucleated growth reactions |
US4371510A (en) * | 1979-10-13 | 1983-02-01 | Henkel Kommanditgesellschaft Auf Aktien | Process for the continuous crystallization of zeolitic sodium aluminosilicates of smallest particle size |
US4379761A (en) * | 1981-01-08 | 1983-04-12 | Mobil Oil Corporation | Catalyst and process for making said catalyst |
US4421941A (en) * | 1981-01-08 | 1983-12-20 | Mobil Oil Corporation | Catalyst and process for selective production of para-dialkysubstituted benzenes |
US4374093A (en) * | 1981-02-20 | 1983-02-15 | Mobil Oil Corporation | Continuous-stream upflow zeolite crystallization apparatus |
US5019670A (en) * | 1986-07-29 | 1991-05-28 | Mobil Oil Corporation | Process for producing alkylaromatic lubricant fluids |
US5107049A (en) * | 1986-07-29 | 1992-04-21 | Mobil Oil Corporation | Stabilization of polyalpha-olefins |
EP0308097A1 (en) | 1987-09-02 | 1989-03-22 | Mobil Oil Corporation | Transalkylation of polyalkylaromatic hydrocarbons |
US4885426A (en) * | 1987-09-02 | 1989-12-05 | Mobil Oil Corporation | Transalkylation of polyaromatics |
US5026943A (en) * | 1988-05-09 | 1991-06-25 | Mobil Oil Corp | Catalytic conversion over catalyst comprising synthetic crystal MCM-35 |
US5030785A (en) * | 1988-10-06 | 1991-07-09 | Mobil Oil Corp. | Process for preparing long chain alkyl aromatic compounds employing Lewis acid-promoted zeolite catalysts |
US4992606A (en) * | 1988-10-06 | 1991-02-12 | Mobil Oil Corp. | Process for preparing short chain alkyl aromatic compounds |
US4962256A (en) * | 1988-10-06 | 1990-10-09 | Mobil Oil Corp. | Process for preparing long chain alkyl aromatic compounds |
US4922053A (en) * | 1989-05-24 | 1990-05-01 | Fina Technology, Inc. | Process for ethylbenzene production |
US5105042A (en) * | 1989-05-30 | 1992-04-14 | Mobil Oil Corp. | Sulfated layered titanium oxide catalysts in process for preparing long chain alkyl aromatic compounds |
WO1991001959A1 (en) * | 1989-07-26 | 1991-02-21 | Michelin Recherche Et Technique S.A. | Selectively cycloalkylating naphtalene on zeolites |
FR2650273A1 (en) * | 1989-07-26 | 1991-02-01 | Michelin Rech Tech | CYCLOALKYLATION OF AROMATIC COMPOUNDS ON ZEOLITHES |
US5292978A (en) * | 1989-07-26 | 1994-03-08 | Michelin Recherche Et Technique | Selective cycloalkylation of naphthalene on zeolites |
US5157185A (en) * | 1989-09-01 | 1992-10-20 | Mobil Oil Corporation | Alkylation of aromatics |
US5334795A (en) * | 1990-06-28 | 1994-08-02 | Mobil Oil Corp. | Production of ethylbenzene |
US5043503A (en) * | 1990-08-14 | 1991-08-27 | Mobil Oil Corporation | Production of lubricant stocks from polycyclic paraffins |
US5145817A (en) * | 1991-05-24 | 1992-09-08 | The Dow Chemical Company | Alkylation process using dual metal ultrastable Y zeolite |
US5252197A (en) * | 1992-09-28 | 1993-10-12 | Abb Lummus Crest Inc. | Process for upgrading gasolines and other hydrocarbon mixtures |
US6010617A (en) * | 1992-11-13 | 2000-01-04 | Mobil Oil Corporation | Process for producing non-carcinogenic coal-tar-derived products |
US5434325A (en) * | 1993-06-21 | 1995-07-18 | Deltech Corporation | Process for the production of tertiary butylethylbenzene |
US5569805A (en) * | 1993-10-18 | 1996-10-29 | Mobil Oil Corporation | Catalytic conversion of aromatic compounds |
US5488194A (en) * | 1994-05-16 | 1996-01-30 | Mobil Oil Corp. | Selective production of para-dialkyl substituted benzenes and catalyst therefor |
US5939597A (en) * | 1994-11-10 | 1999-08-17 | Mobil Oil Corporation | Fluid bed process for para-xylene production |
US5900520A (en) * | 1995-01-23 | 1999-05-04 | Mobil Oil Corporation | Aromatics alkylation |
EP1456154A1 (en) | 2001-12-20 | 2004-09-15 | Polimeri Europa S.p.A. | Process for the alkylation of aromatic compounds |
US20050075239A1 (en) * | 2001-12-20 | 2005-04-07 | Gianni Girotti | Process for the alkylation of aromatic compounds |
US7524788B2 (en) | 2001-12-20 | 2009-04-28 | Polimeri Europa S.P.A. | Process for the alkylation of aromatic compounds |
EP1456154B1 (en) * | 2001-12-20 | 2014-04-23 | versalis S.p.A. | Process for the alkylation of benzene |
US7954254B2 (en) * | 2002-05-15 | 2011-06-07 | Nederlandse Organisatie Voor Toegepast-Natuurwetenschappelijk Onderzoek Tno | Method for drying a product using a regenerative adsorbent |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
US2904607A (en) | Alkylation of aromatics | |
AU652190B2 (en) | Isoparaffin alkylation processes using alumina catalysts | |
US3549557A (en) | Isoparaffin alkylation process and catalyst for use therein | |
RU2094418C1 (en) | Method of producing cumene or ethyl benzene | |
US3033778A (en) | Catalytic conversion in the presence of carbon dioxide promoted crystalline metal aluminosilicates | |
KR920002241B1 (en) | Process for preparation of lower aliphatic hydrocarbons | |
US3647916A (en) | Isoparaffin-olefin alkylation with crystalline zeolite catalysts at low isoparaffin to olefin ratios | |
US3641177A (en) | Alkylation of aromatic hydrocarbons | |
US4599470A (en) | Process for the transalkylation or dealkylation of alkyl aromatic hydrocarbons | |
US3669903A (en) | Catalytic cracking process | |
US4579831A (en) | Method of zeolitic catalyst manufacture | |
US2410111A (en) | Treatment of hydrocarbons | |
US3840613A (en) | Paraffin alkylation with olefin using highly active crystalline zeolite catalyst | |
US2407918A (en) | Catalytic conversion of carbonaceous materials | |
US3121754A (en) | Catalytic process | |
US2346657A (en) | Treatment of butane | |
US2419599A (en) | Alkylation of aromatic hydrocarbons | |
US2382318A (en) | Alkylation of benzene | |
JPS6158112B2 (en) | ||
US4119676A (en) | Process for isomerization of alkylaromatic hydrocarbon | |
RU2031900C1 (en) | Method of alkylation of isoparaffin with olefin | |
US2897246A (en) | Alkylation process with treated silica-alumina catalyst | |
US3533939A (en) | Reforming with a crystalline aluminosilicate free of hydrogenation activity | |
US2389406A (en) | Production of olefinic hydrocarbons | |
US3193493A (en) | Catalytic cracking process with a catalyst composition comprising an aluminosilicate containing beryllium |