|Número de publicación||USRE28341 E|
|Tipo de publicación||Concesión|
|Fecha de publicación||18 Feb 1975|
|Fecha de presentación||4 Mar 1969|
|Fecha de prioridad||1 May 1964|
|Número de publicación||US RE28341 E, US RE28341E, US-E-RE28341, USRE28341 E, USRE28341E|
|Inventores||Robert L. Wadlinger|
|Exportar cita||BiBTeX, EndNote, RefMan|
|Citas de patentes (2), Citada por (146), Clasificaciones (17)|
|Enlaces externos: USPTO, Cesión de USPTO, Espacenet|
United States Patent Re. 28,341 Reissued Feb. 18, 1975 28,341 CATALYTIC COMPOSITION OF A CRYSTALLINE ZEOLITE Robert L. Wadlinger, Niagara, N.Y., and George T. Kerr,
Trenton, and Edward J. Rosinski, Deptford, N.J., assignors to Mobil Oil Corporation No Drawing. Original No. 3,308,069, dated Mar. 7, 1967, Ser. No. 364,316, May 1, 1964. Application for reissue Mar. 4, 1969, Ser. No. 806,753
Int. Cl. B01j 11/40; C10g 11/04 U.S. Cl. 208120 17 Claims Matter enclosed in heavy brackets appears in the original patent but forms no part of this reissue specification; matter printed in italics indicates the additions made by reissue.
ABSTRACT OF THE DISCLOSURE This invention relates to a new catalyst, zeolite beta. [XNa(1.0:0.I-X)TEA]Al .YSiO .WH 0 wherein X is less than I, Y is greater than but less than 100, W is up to about 4, and TEA represents tetraethylammonium ion, its process of manufacture, and its use in calcined form in catalytic hydrocarbon conversion processes.
This invention relates to a new synthetic zeolite and to a method for preparing the same. The invention also is concerned with a catalytic composition comprising said zeolite and with catalytic conversion in the presence thereof.
Crystalline aluminosilicate zeolite structurally consist basically of an open three-dimensional framework of SiO, and A10, tetrahedra. Such tetrahedra are crosslinked by the sharing of oxygen atoms, so that the ratio of oxygen atoms to the total of the aluminum and silicon atoms is equal to two. The negative electrovalence of tetrahedra containing aluminum is balanced by the inclusion within the crystal of cations, such as alkali or alkaline earth metal ions.
Many zeolites possess a crystal structure, having channels of molecular dimensions. The interstitial spaces are generally originally occupied by water of hydration. After at least partial dehydration, these zeolites may be utilized as efficient adsorbents whereby adsorbate molecules are retained within the interstitial spaces. The interstitial dimensions of openings in the crystal lattice limit the size and shape of the molecules that can be adsorbed. A separation of a mixture of various molecules, based upon molecular dimensions, wherein certain molecules are adsorbed by the zeolite while others are excluded from admission is therefore possible. It is such characteristic of many crystalline zeolites that has led to their designation as molecular sieves.
A number of synthetic crystalline zeolites have previously been prepared. They are distinguishable from each other and from naturally occurring zeolites on the basis of composition, crystal structure and adsorption properties. The existence of a number of zeolites having similar but distinguishable properties advantageously permits the selection of a particular member having optimum properties for a particular use.
Thus it has heretofore been known to prepare a synthetic zeolite known as zeolite A." Such material and preparation thereof has been described in U.S. 2,882,243. This zeolite is initially obtained in its sodium form, i.e. as a sodium aluminosilicate. Such material is capable of effectively sorbing water and straight chain compounds of three or less carbon atoms such as methane, ethane. npropane, methanol, ethanol, n-propanol and the like. Sodium zeolite A, however, is incapable of adsorbing, to an appreciable extent, straight chain compounds having more than three atoms in the chain. Thus, it is only after replacement, by ion exchange, of a substantial proportion of the sodium ions of the initially obtained sodium zeolite A with divalent ions. such as calcium or magnesium that the pore characteristics thereof are such as to effect separation of straight chain hydrocarbons of more than 3 carbon atoms from admixture with branch chain or cyclic compounds. Sodium zeolite A, known commercially as molecular sieve 4A, is thus incapable of admitting into its crystalline structure molecules for which the maximum dimension of the minimum projected crosssection is greater than about 4.9 Angstroms. In order to produce a zeolite A capable of effecting separation of mixtures of straight chain and branched chain molecules or for separation of straight chain molecules from cyclic compounds having four or more atoms. it has heretofore been necessary to first carry out exchange of the initially obtained sodium zeolite A with another ion, such as calcium or magnesium, and to thereby effect exchange of the sodium ion to the extent of at least about 40 percent with such substituting ion. The resulting product, in which calcium is the introduced ion, is known commercially as molecular sieve 5A. This zeolite has larger pore dimensions than does the 4A sieve and permits adsorption of molecules for which the maximum dimension of the minimum projected cross-section is about 5.5 Angstroms.
It has also been known prior to the present invention to synthesize a zeolite, known as zeolie ZK-4. more particularly described in co-pending application Serial No. 134,841, filed August 30, 1961. This zeolite, which essentially in its sodium form, i.e., the form in which the zeolite is obtained from the preparative reaction mixtures. is capable of accomplishing separation of straight chain molecules having more than three atoms in the chain from non-straight chain, i.e. from branched chain and/or cyclic, molecules of more than three atoms without the necessity of converting such form zeolite into another ionic form by prior base-exchange such as has heretofore been necessary in achieving a synthetic zeolite of the above requisite pore characteristics.
The composition of zeolite ZK-4 can stoichiometrically be expressed, in terms of mole ratios of oxides as follows:
0.1 to 0.3R:0.7 to IBM- 0: lAl O :2.5 to 4.0SiO -YH O where R is selected from the group consisting of a methyl ammonium oxide, hydrogen oxide and mixtures thereof with one another; M is a metal and n is the valence thereof and Y is any value from about 3.5 to about 5.5, said material being capable of selectively sorbing straight chain hydrocarbons of more than three carbon atoms from admixture of the same with non-straight chain hydrocarbons when M is sodium and capable of selectively sorbing water from admixture of the same with straight chain molecules having more than three atoms in the chain when M is potassium. Minor variations in the mole ratios of these oxides within the range indicated by the above formula do not significantly change the crystal structure or physical properties of the zeolite.
It has also been known prior to the present invention to synthesize a zeolite, known as zeolite alpha, more particularly described in co-pending application Ser. No. 237,289 filed November 13, 1962. This zeolite alpha has an A-type lattice and a silicon to aluminum content greater than that of zeolite ZK-4.
The composition of zeolite alpha can stoichiometrically be expressed, in terms of mole ratios of oxides as follows:
0.2 to (ism o: 0.5 to 0.8M O: 1Al O 4.0 to
Where R represents ions selected from those of the group consisting of metal, methyl ammonium, hydrogen and mixtures thereof with one another; m is the valence of R; M represents ions selected from those of the group consisting of hydrogen, metal and hydrogen-metal mixtures, n is the valence of M, and Y is any value up to about 8.0, said material being further characterized by the ability to selectively sorb straight chain hydrocarbons of more than three carbon atoms from admixture of the same with non-straight chain hydrocarbons when M is sodium and by an A type lattice as determined by X-ray diffraction.
In accordance with the present invention, there is provided a new zeolite having a novel structure as defined by X-ray crystallography and which has a novel combination of adsorption properties. This new zeolite will hereinafter be referred to as zeolite beta."
The present invention is directed to a crystalline synthetic material where composition has been calculated to be:
where X is less than 1, preferably less than 0.75; TEA represents tetraethylammonium ion; Y is greater than 5 but less than 100 and W is up to about 4 depending on the condition of dehydration and on the metal cation present. The TEA component is calculated by difference from the analyzed value of sodium and the ultimate theoretical cation of Al ratio of 1.0/1.
In another embodiment, the invention provides for a crystalline synthetic material which has catalytic properties having the composition:
where X, Y and W have the values listed above and n is the valence of the metal M which can be any metal, preferably a metal of groups la, 2a, 3a or one of the transition metals or mixtures thereof as shown in the Mendeleff periodic chart.
In still another embodiment, the invention provides for a crystalline synthetic material which has catalytic properties having the compositions:
where X, Y, W, n and M have the values listed above. This form of the catalyst is obtained from the initial sodium form of zeolite beta by ion exchange without calcining.
Thus, the zeolite beta is formed by crystallization from a reaction mixture containing the tetraethylammonium ion. Upon heating of the product, at a temperature in the approximate range of 400-1700 F. or higher, the tetraethylammonium ion undergoes degradation to the hydrogen ion. Further, in this case the value of W in the formula may be essentially 0.
It is a particular feature of the present invention, that zeolite beta is prepared from reaction mixtures containing tetraethylammonium hydroxide as the alkali and more specifically by heating in aqueous solution a mixture of the oxides or of materials whose chemical compositions can be completely represented as mixtures of the oxides N320, A1203, [(C2H5)4N]20, and H20 suitably at a temperature of about 75 C. to 200 C. until crystallization occurs. The composition of the reaction mixture, expressed in terms of mol ratios, preferably falls within the following ranges:
8103/ Aho -from about to about 200 Nap/tetraethylammonium hydroxide (TEAOH)from about 0.0 to 0.1
TEAOH/SiO -from about 0.1 to about 1.0
H O/TEAOHfrom about to about 75 The product which crystallizes from the hot reaction mixture is separated, suitably by centrifuging or filtration. washed with water and dried. The material so obtained may be calcined by heating in air or an inert atmosphere at a temperature in the approximate range of 400l700 F. or higher so long as the temperature is not sufficient to destroy the crystallinity.
In making zeolite beta, the method comprises reacting in aqueous media, amorphous silica solids or sols and a soluble aluminate along with aqueous solutions of tetraethylammonium hydroxide. The aluminate may be sodium aluminate or tetraethylammonium aluminate. Amorphous silica-alumina solids may be used as the source of the silica and alumina. The reaction mixture is initially continuously or periodically stirred to insure homogeneity. After this mixing, agitation may be stopped as it is unnecessary to agitate the reaction mass during the formation and crystallization of the zeolite, although mixing during such latter stages has not been found to be detrimental.
The crystallization procedures can be satisfactorily carried out at temperatures within the range from about C. to about 200 C. The pressure during crystallization is atmospheric or at least that which corresponds to the vapor pressure of water in equilibrium with the mixture of reactants. Heating is continued until desired crystalline zeolite product is formed. The zeolite crystals are then separated from the mother liquor and washed, preferably with distilled water.
In the synthesis of zeolite beta, it has been found that the composition of the reaction mixture is critical. Specifically, the presence of tetraethylammonium ions in such mixture has been found to be essential for the production of zeolite beta.
In the absence of such ions or even in the presence of quaternary ammonium ions other than tetraethyl, no zeolite beta was obtained.
Because of the use of tetraethylammonium hydroxide in its preparation, zeolite beta may contain occluded tetraethylammonium ions (e.g., as the hydroxide or silicate) within its pores in addition to that required by electro neutrality and indicated in the calculated formulas given heretofore. For example, there was found an additional 1.3 equivalent of tetraethylammonium ion in one preparation of zeolite beta beyond that required by the formulas given above. The formulas, of course, are calculated using the knowledge of all zeolite chemistry that one equivalent of cation is required per Al atom in tetrahedral coordination in the crystal lattice.
Sodium oxide present in the reaction mixture may be derived from sodium aluminate or an amorphous sodium aluminosilicate gel. The latter is characterized by the following composition:
Na (Alog where X is a number in the approximate range of 0.520. This material may be prepared by reaction of ethyl orthosilicate and sodium aluminate. Another suitable source of alumina and sodium oxide is a solution of aluminum turnings in an alkali. Tetraethylammonium aluminates can also be used. Silica present in the reaction mixture may be derived from a variety of sources, for example, silica gel, silica hydrosol, and silicate esters.
Zeolite beta is ditferent from any other known crystal line aluminosilicates in several ways. First of all, it has a novel structure as defined by X-ray crystallography. Some d-spacings of the crystal and their relative intensities as defined by X-ray powder pictures are given in Table 2 hereafter.
Secondly, zeolite beta has a novel combination of adsorption properties. The adsorptive capacities for cyclohexane, n-hexane and H 0 are approximately equal, or of the same order of magnitude. This is the first zeolite known to the inventors in which the H 0 adsorption capacity does not substantially exceed the cyclohexane adsorption. Further, the SiO /Al- O ratio is extremely high and extremely variable, going from 10 to and possibly as high as 150.
The following Table 1 summarizes the differences in water and cyclohexane adsorption for various zeolites:
In identification of zeolites, the X-ray powder diffraction pattern has been found useful. X-ray diffraction Catalytic materials can be prepared by calcining the original sodium form of zeolite beta and/or by replacing the major portion of the sodium in the zeolite with other metallic and/or ammoniacal ions. If the calcination is carried out prior to ion exchange, some or all of the re sulting hydrogen ions can be replaced by metal ions in the ion exchange process. For certain dehydrogenation and hydrogenation reactions such as hydrocracking the catalyst will preferably contain a metal of Groups 5b, 6b or 8 of the Periodic Table and such metal may either be in the cation of the zeolite or deposited on the surface of the zeolite when the later is characterized by a cracking activity. Thus, a Zeolite beta catalyst having a metal therein of Groups 1a, 2a, 3a or one of the transition metals may have deposited thereon a metal of Groups 5b, 6b or 8 of the Periodic Table.
Zeolite beta may be used as an adsorbent in any suitable form. For example, a column of powder crystalline material may afford excellent results as may a pelleted form obtained by pressing into pellets a mixture of zeolite beta and a suitable bonding agent, such as clay.
The compositions contemplated herein include not only the sodium form of zeolite beta as synthesized from a sodium-a1uminum-silicate-tetraethylammonium-water system with sodium as the exchangeable cation but also crystalline materials obtained from such a zeolite by partial or complete replacement of the sodium ion with other cations. The sodium cations can be replaced, at least in part, by other ions including those of metals below sodium in the electromotive series, calcium, ammonium, hydrogen and combinations of such ions with one another. Particularly preferred for such purpose are the alkaline earth metal ions; Group 2 metal ions, ions of the transition metals such as manganese and nickel, the rare earth metals such as cerium, lanthanum, praseodyminum, neodymium, samarium and mixtures thereof with each other and the other rare earth; and other ions, for example, hydrogen and ammonium which behave in zeolite beta as metals in that they can replace metal ions without causing any appreciable change in the basic structure of the zeolite crystal. The transition metals are those whose atomic numbers are from 21 to 28, from 39 to 46 and from 72 to 78 inclusive, namely scandium, titanium, vanadium. chromium, managese, iron, cobalt, nickel, yttrium. zirconium, niobium, molybdenum, ruthenium, rhodium, palladium, platinum, hafnium, tantalum, tungsten, rhenium, osmium and iridium.
Ion exchange of the sodium form of zeolite beta may be accomplished by conventional methods. A preferred continuous method is to pack zeolite beta into a series of vertical columns and successively pass through the beds a water solution of a soluble salt of the cation to be introduced into the zeolite; and change the flow from the first bed to the second bed as the zeolite in the first bed becomes ion exchanged to the desired extent. The spatial arrangement of the aluminum, silicon and oxygen atoms which make up the basic crystal lattice of the zeolite remains essentially unchanged by partial or complete substitution of the sodium ion by other cations.
powder patterns of zeolite beta were obtained utilizing standard techniques. The radiation was the K alpha doublet of copper and a Geiger counter spectrometer with a strip chart pen recorder was used. The peak heights, I, and the positions as a function of 24 where p is the Bragg angle, were read from the spectrometer chart. d (obs), the interplanar spacing in A, corresponding to the recorded lines were calculated. The cell constant for zeolite beta, i.e., the dimension of the edge of the cubic until cell was determined as 12.04 A.:0.14 A. X-ray powder diffraction data for typical zeolite beta samples are set forth in Table 2 hereinbelow.
The appearance of few minor lines and the disappearance of other lines can be attributed to compositional differences in silicon to aluminum ratios in the sodium form beta zeolites summarized in Table 2. In Table 3 the variation in intensities, and appearance and disappearance of some lines can be attributed to cation exchange.
Example A in Table 2 was dried at 212 F.; Examples B and C at 230 F. and Example D calcined ten hours at 1000 F. in air.
TABLE 2.SOD1U.\1ZEOL1TE BETA A B C D d d d (.1 (AJ Int. (A.) Int. (A.) Int. (9..) Int 14. 3 MW 11.5 S 11.5 S 11.8 S 11.55 S
10. 1 W 7. 56 7. 56 W 1. 59 W 7 5 MW 7. 44 VW 6. 97 6. 97 VW 7. 15 W 6. 86 MW 6. 615 6. 615 VW 6, 59 6. 54 W 6 59 .\1W 6. 165 VW 6. 10 6. 10 VW 6. 14 VW 6. 04 6. 02 W 6. 04 V W 5. 64 M 5. 51 W 5. 36 5. 36 VW 5. 29 5. 00 MW 4.91 4.91 \"W 4.955 VW 4. 81 4. 81 VW 4. W 4. 73 MW 4. N M 4. 25 M 4. 17 M 4. 16 M 4. 16 M 4. 15 M 3. 98 VS 3. 97 VS 3. J7 VS 3.1]? V5 3. 54 W 3. 53 W 3. 86 MW 3. 51 MW 3. 51 M 3. 42 W 3. 46 MW 3. 33 MW 3. 29 M 3. 31 MW 3. 21 3. 325 MW 3. 18 W 3. 21 VW 3. 12 W 3. 10 W 3. 095 MW 3 095 MW 3. 03 M 3. 03 MW 3. 01 M 3 015 M 2. 90 M 2. 93 2. 895 VW 2. J3 W 2. 74 VW 2. 76 VW 2. 69 W 2. 69 VW 2. 68 MW 2. 69 W 2. 58 W 2. 69 VW 2. .37 \'W 2. 49 W 2. 48 VW 2. 4115 VW 2. 4515 \'W 2. 41 VW 2. -10 VW 2. 13 VW 2. 40 V W 2. 34 W 2. 34 VW 2. 34 \W 2. 25 VW 2. 25 VW 2. 25 W 2. 21 2. 21 VW 2. 21 VW 2. 17 2. 17 VW 16 \'W 2. 13 2. 13 VW 2. 08 W 2. 08 VW 2. 08 MW 2. 08 W 2. 045 2. 05 VW 2 045 \'W 2. 03 VW 2. 03 VW 2. 03 W 2. 03 W l. 99 1. 99 VW TABLE 3 Ca Beta La Beta Mn Beta d M.) Int. ti t.) int. tltA.) Int.
ll. 4 5 ll. 5 S 11. 3 S
T. 4 VW 7. 5 W T. 22 7. W W 6. 8B 6. 33 W 6. 50 W 6. 50 MW 6. 57 MW 6. 10 VW 6. 0t 6. 04 W 6. 02 W 4. SB 4. 80 VW 4. 83 VW 4. 35 4. 35 M 4. M 4. 16 W 3. 07 VS 3. 97 VS 3. 97 VS 3.51 MW 3. 52 M 3. 52 MW 3. 31 MW 3. 31 MW 3. 31 MW 3. 23 3. 3 VW 3. 09 MW 3. 10 MW 3. 02 M 3. 01 M 3. 01 M 2. 93 W 2. 03 W 2. 90 W 2. 90 MW 2. 69 W 2. 69 W 2. 64 2. 64 W 2. 56 VW 2. 59 W 2. 48 \W 2. 49 VW 2. 47 \W 2. 41 Z. 41 VW 2. 40 VW 2. 34 VW 2 34 W 2. 34 VW 2. \'W 2 23 VW 2.19 VW 2. 17 2.]? VW 2. 08 W 2. 07 W 2.09 W 2. 03 VW 2. 03 YW 2.03 VW The more significant d values for exchanged beta zeolite are given in Table 4.
Table 4.d Values of Reflections in Exchanged Beta Highly active hydrocarbon conversion catalysts may be obtained by treating the above-described crystalline zeolite beta with a fluid medium containing a hydrogen ion or ion capable of conversion to a hydrogen ion in an amount sufiicient to impart catalytic properties thereto. The catalysts so obtained possess a wide spectrum in magnitude of catalytic activity; can be used in extremely small concentrations; and permit certain hydrocarbon conversion processes to be carried out under practicable and controllable rates at temperatures much lower than those previously employed. In the catal of hydrocarbon oils into hydrocarbon products of lower molecular weight, the reaction rates per unit volume of catalyst that are obtainable by (hydrogen treated) zeolite beta may vary up to several fold the rates achieved with siliceous catalysts heretofore proposed. These catalysts furthermore can be used directly as the sole catalytic constituent or as intermediates in the preparation of further modified contact masses having catalytic properties. Such modified contact masses may comprise the treated crystalline zeolite per se or a. dispersed mixture of the treated aluminosilicates with a predetermined amount of a low activity and/ or catalytically active material which serves as a binder or matrix for the catalyst constituent.
The high activity catalysts contemplated are obtained by contacting zeolite beta with a fluid medium containing hydrogen ions or ions capable of conversion thereto, washing the treated material free of soluble anions, and thereafter drying and thermally activating the product by heating at temperatures ranging from about 400 F. to 1700 F. or higher for a period between about one and forty-eight hours. The resulting product is an activated aluminosilicate, strongly acidic in character, which contains less than about 10 percent by weight metal and substantially corresponds to the hydrogen form of the zeolite beta precursor material. When subsequently used alone or combined in a state of particle size of less than about 40 microns, dispersed or otherwise intimately admixed with a suitable matrix, such as an inorganic oxide gel, the
resulting product has been found to be active as a catalyst for hydrocarbon conversion.
The compositions resulting from treatment of zeolite beta with fluid media containing hydrogen ions, ammonium ions or complex ammonium ions and metal ions. or mixtures thereof may be employed as catalysts in a wide variety of hydrocarbon conversion processes including isomerization, disproportionation, hydration of olefins, amination of olefins, oxidation, dehydrogenation, dehydration of alcohols, desulfurization, hydrogenation, re: f grming, hydrogmclging, polymerization and the like. The catalysts are exceptionally stable and are particularly useful in such of the above and related processes carried out at temperatures ranging from ambient temperatures of F. up to 1000 F., including such processes in which the catalyst is periodically regenerated by burning ofi combustible deposits. Because of their high catalytic activities, the catalysts are especially useful for elfecting various hydrocarbon conversion processes such as alkylntion, for example, at relatively low temperatures with small amounts of catalyst, thus providing a minimum of undesirable side reactions and operating costs.
The catalysts may be used as such or as intermediates in the preparation of further modified contact masses comprising low activity or catalytically active materials which serve as a support or matrix for the aluminosilicate. The catalyst may be used in powdered, granular or molded state formed into spheres or pellets of finely divided particles having a particle size of 2 to 500 mesh. In cases where the catalyst is molded, such as by extrusion, the aluminosilicate may be extruded before drying, or dried or partially dried and then extruded. The catalyst product is then preferably precalcined in an inert atmosphere or may undergo calcination initially during use in the conversion process. Generally, the composition is dried between 150 F. and 600 F. and thereafter calcined in air or steam or an inert atmosphere of nitrogen, hydrogen, helium, flue gas or other inert gas at temperatures ranging from 400 F. to 1700" F. for periods of time ranging from one to forty-eight hours or more. This heating step is known as thermal activation of the catalyst.
The catalyst of this invention may be prepared in any desired physical form. Preferably, it is used in the form of small fragments of a size best suited for operation under the specific conditions existing. Thus, the catalyst may be in the form of finely divided powder or may be in the form of pellets of A to 54;" size, for example, obtained upon pelleting, casting, or extruding in accordance with well known techniques.
The following examples will serve to illustrate the product and method of the present invention without limiting the same:
Example 1 2.3 g. of sodium aluminate were dissolved in 43.4 ml. water. This solution, hot, was added to 70 ml. of hot solution of 2.7 N tetraethylammonium hydroxide plus 18.6 g. silica gel (Davison) with rapid stirring which was continued for fifteen minutes. The mixture was held at 78 C. for about forty-two days. This process yielded crystals which were separated from the mother liquor by centrifugation. The wet solids, after decantation and subsequent water washing were dried at C. after which the crysatls showed the X-ray pattern of Table 2. The crystals then showed the properties:
Composition (dehydrated basis): Mol percent N320 A1 0 6.4 SiO; 89.0
Sorption properties: Wt. percent sorbed Cyclohexane 14.6 n-Hexane 13.8 11,0 20.1
The fact that the adsorption capacity for cyclohexane and n-hexane are relatively low in this case was found later to be due to incomplete crystallization in this particular case.
Example 2 A reaction mixture having the following composition, exclusive of water, was prepared:
Mol percent Na- O 0.3 A1 0.9 [(C2 )4N]2O 9. SiO 89.2
air at 550 C. was 0.7% Na O, 1.3% A1 0 and 98.0
mol percent SiO Thus the silica/alumina is almost 96/1.
Its absorption properties (calcined as above) were (ing. absorbed 100 g. sample) 19.4 cyclohexane, 16.6 nhexane and 18.1 water.
Example 3 The gelatinous material left in the flask in the above example was air-dried at room temperature. A portion of this material was added with 50 ml. of 2.65 N tetraethylammonium hydroxide (TEACH) to an autoclave and treated for three days at 150 C. The liquor obtained was centrifuged, yielding crystals which were washed and air dried. X-ray examination of the product showed the same crystalline structure as in the first two examples.
Example 4 The calcined product from Example 2 (1.5 cc.) was tested as a hydrocarbon conversion catalyst by passing a helium stream saturated at 73 F. with n-hexane over the catalyst at 700 F. and 0.4 LHSV. At the end of five minutes, chromatographic analysis of the product sample showed the catalyst to have a rate constant for the cracking of n-hexane 900 times as great as that of a standard silica-alumina cracking catalyst.
Example 5 A 6.6 g. sample of the product of Example 2 was base exchanged with a solution of 1.5 lb. RECl -6H O where RE is a rare earth and 0.6 lb. NH Cl dissolved in lbs. H 0 continuously for three days. The rare earth-acid aluminosilicate resulting from this exchange was also tested for its hydrocarbon conversion activity in the same manner used in Example 4 except that the temperature of the test was 600 F. In this case the relative rate constant (alpha) was 6400 times as great as the standard silica-alumina catalyst.
Example 6 A 1.63 g. sample of NaAlO was dissolved in 30.7 ml. H 0 and added to a mixture of 13.1 g. silica gel (Davison) and 49.5 ml. of 2.74 N tetraethylammonium hydroxide (TEAOI-I). The reaction mixture was charged to an autoclave and heated to 150 C. at which temperature it was held for six days. The crystalline product which formed had the following composition: N3g00.8%, Al O 3.25% and SO -96.0 mol percent, and X-ray examina tion showed the same crystalline pattern as in Examples 1 and 2. After calcination the adsorption capacity of the crystalline product was 17.2 g. cyclohexane/IOO g. beta and 18.3 g. H- -0/ 100 g. beta.
Example 7 An 11.6 g. sample of NaAlO was added to 116 ml. 2.58 N tetraethylammonium hydroxide (TEAOH). To this was added 290.7 g. silica sol (Ludox LS). A thick, smooth gel was formed immediately. This was placed into an autoclave, heated to 150 C. for six days at which time a large amount of crystalline material had formed. This was filtered and air dried. The X-ray pattern was again that of the beta-zeolite. The composition on a calcined sample was (mol percent): Na O-2.9%, Al O;,3.l% and SiOg94.0%.
Example 8 A 50 g. sample of the dried product from Example 7 was exchanged continuously for forty-eight hours with a 2 percent solution of NH Cl. After washing free of excess chloride ions the catalyst was dried, then calcined for three hours at 1000 F. The resulting material is an acid beta-aluminosilicate having only 0.07 percent Na content. This was tested at 600 F. by the hexane cracking test already described. Its relative rate constant for hexane cracking was 20,000.
Example 9 Another 50 g. portion of the dried product from Example 7 was exchanged continuously for forty-eight hours with a 2 percent solution of RECl -6H O. After washing, drying and air calcining the product contained 0.08 percent Na, 3.74 percent RE O, 5.2 percent A1 0 and percent SiO This was also tested at 600 F. as a hydrocarbon conversion catalyst by use of the hexane cracking test already described. Its relative reaction rate constant was 19,000.
It is to be understood that the above description is merely illustrative of preferred embodiments of the invention of which many variations may be made by those skilled in the art Within the scope of the following claims without departing from the spirit thereof.
What is claimed is:
1. A crystalline synthetic zeolite material having the calculated composition:
wherein X is less than 1, Y is greater than 5 but less than 100, W is up to about 4, and TEA represents tetraethylammonium ion, said material being characterized by an X-ray powder diffraction pattern essentially the same as that shown in Table 4.
2. A crystalline synthetic catalyst material having the composition:
[3M0 i 0.1 X)H]AlO2-YSiO2.wII2O where X is less than 1, Y is greater than 5 but less than 100. W is up to about 4, M is a metal, and n is the valence of M, said material being characterized by an X-ray powder diffraction pattern essentially the same as that shown in Table 4.
3. A crystalline synthetic catalyst material having the composition:
where X is less than 1, Y is greater than 5 but less than 100, M is a metal, and n is the valence of M, said material being characterized by an X-ray powder diffraction pattern essentially the same as that shown in Table 4.
4. A crystalline synthetic material having the composition:
where X is less than 1, Y is greater than 5 but less than 100, W is up to about 4, TEA represents tetraethylam' monium ion, M is a metal, and n is the valence of M, said material being characterized by an X-ray powder diffraction pattern essentially the same as that shown in Table 4.
5. A method for synthesizing a crystalline material which comprises preparing a reaction mixture whose composition expressed in terms of mo] ratios falls within the following ranges:
SiO /Al O from about 10 to about 200 Na O/tetraethylammOnium hydroxidefrom about 0.0
to about 0.1
Tetraethylammonium hydroxide/SiO from about 0.1 to
H o/tetraethylammonium hydroxide-from about 20 to about 75 and maintaining said mixture at a temperature within the range of 75 C. to 20 C. until said crystalline material is formed.
6. A method for synthesizing a crystalline material which comprises preparing a reaction mixture whose composition expressed in terms of mol ratios falls within the following ranges:
SiO /Al O -from about 10 to about 150 Na O/tetraethylammonium hydroxide-from about 0.0 to
Tetraethylammonium hydroxide/SiO from about 0.1 to
H OItetIaethyIammoniun-i hydroxidefrom about 20 to about 75 and maintaining said mixture at a temperature within the range of 75 C. to 150 C. until said crystalline material is formed.
7. A method in accordance with claim followed by separating the crystals from the mother liquor, and subjecting the separated crystals to a calcining treatment by heating at a temperature in the approximate range of 400- 1700 F.
8. A method in accordance with claim 5, followed by separating the crystals from the mother liquor and subjecting the crystals to ion exchange with a metal selected from the group consisting of the metals of Groups 1a, 2a, 3a, 3b, 4b, and 8 of the periodic classification of the elements.
9. A method for synthesizing a crystalline aluminosilicate in accordance with claim 7 followed by subjecting the crystals to ion exchange with a metal selected from the group consisting of the metals of Groups 1a, 2a, 3a, 3b, 4b, 5b, 6b, 7b and 8 of the periodic classification of the metals.
10. A method in accordance with claim 7 followed by depositing on the surface of the crystals a metal selected from the group consisting of metals of Groups, 5b, 6b and 8 of the periodic classification of the metals.
11. A method for synthesizing a crystalline aluminosilicate zeolite which comprises reacting sodium aluminate, silica and tetraethylammonium hydroxide, the resulting reaction mixture having a composition expressed in terms of mol ratios within the following ranges:
S102, Al,O -from about 10 to about 200 Na o/tetraethylammonium hydroxide-from about 0.0 to
Tetraethylammonium hydroxide/SiO- from about 0.1 to
fl o/tetraethylammonium hydroxide-from about to about 75 maintaining said mixture at a temperature within the approximate range of about 75 C. to 200 C. until crystals of said zeolite are formed, separating the crystals from the mother liquor and subjecting the separated crystals to an activation treatment by heating at a temperature in the approximate range of 400-1700 F.
12. A method for synthesizing a crystalline aluminosilicate zeolite which comprises reacting silica, tetraethylammonium aluminate and aqueous tetraethylammonium hydroxide, the resulting reaction mixture having a composition expressed in terms of mo] ratios within the followng ranges:
SiO /Al O from about 10 to about 200 Na o/tetraethylammonium hydroxidefrom about 0.0 to
Tetraethylammonium hydroxide/SiO from about 0.1 to
H o/tetraethylammonium hydroxide-from about 20 to about maintaining said mixture at a temperature within the approximate range of about 75 C. to 200 C. until crystals of said zeolite are formed, separating the crystals from the mother liquor and subjecting the separated crystals to an activation treatment by heating at a temperature in the approximate range of 400-1700 F.
13. A method for preparing a catalyst composition which comprises treating with an aqueous fluid medium containing a source of positive ions selected from the group consisting of acids and ammonium compounds, a crystalline synthetic aluminosilicate having the formula:
where X is less than 1, Y is greater than 5 but less than 100, W is up to about 4, and TEA represents tetraethylammonium ion; carrying out such treatment for a period of time sufficient to provide a hydrogen aluminosilicate composition, washing the treated material free of soluble anions, and thereafter drying and thermally activating the product by heating at temperatures ranging from about 400-l700 F.
14. A method for preparing a catalyst composition which comprises treating with an aqueous fluid medium containing a source of positive ions selected from the group consisting of rare earth metals and metals of Groups 2a and 3a of the Periodic Table, a crystalline synthetic aluminosilicate having the formula:
where X is less than 1, Y is greater than 5 but less than 100, W is up to about 4, and TEA represents tetraethyl ammonium ion; carrying out such treatment for a period of time sufficient to provide a hydrogen aluminosilicate composition, washing the treated material free of soluble anions, and thereafter drying and thermally activating the product by heating at temperatures ranging from about 4004700 F.
15. In a process for conducting in the presence of a solid porous catalyst a hydrocarbon conversion reaction characterized by a heat of reaction not less than zer the improvement which comprises contacting charge hydrocarbons for said reaction at conversion conditions with a crystalline aluminosilicate catalyst at least partially in the hydrogen form resulting from treatment of the zeolite defined in claim 2 with a fluid medium containing ions selected from the group consisting of hydrogen ions and ammonium ions.
16. The process of claim 15 wherein said fluid treating medium also contains metal cations.
17. The process of claim 15 wherein at least a portion of the ammonioum ions in said treating medium are complex ammonium ions.
References Cited UNITED STATES PATENTS 7/1964 Plank et al. 208-l20 7/1964 Plank et al. 208l20 DELBERT E. GANTZ, Primary Examiner US. Cl. X.R. 252455 Z UNITED STATES PATENT AND TRADEMARK OFFICE CERTIFICATE OF CORRECTION PATENT N0. Re. 28,341
DATED February 18, 1975 |NVENTOR(S) ROBERT L. WADLINGER, ET AL.
It is certified that error appears in the aboveAdentified patent and that said Letters Patent are hereby corrected as shown below:
Column 3, line 43, "n" at end of formula should be deleted.
Column ll, Claim 8, line 5, after e10" insert: To
Signed and Scaled this A lies 1:
RUTH C. MASON C. MARSHALL DANN Arresting Officer (nmmissr'mwr nj'lan'nrs and Trademarks
|Patente citada||Fecha de presentación||Fecha de publicación||Solicitante||Título|
|US3140251 *||21 Dic 1961||7 Jul 1964||Socony Mobil Oil Co Inc||Process for cracking hydrocarbons with a crystalline zeolite|
|US3140253 *||1 May 1964||7 Jul 1964||Socony Mobil Oil Co Inc||Catalytic hydrocarbon conversion with a crystalline zeolite composite catalyst|
|Patente citante||Fecha de presentación||Fecha de publicación||Solicitante||Título|
|US4820402||27 May 1987||11 Abr 1989||Mobil Oil Corporation||Hydrocracking process with improved distillate selectivity with high silica large pore zeolites|
|US4962269 *||5 Dic 1988||9 Oct 1990||Mobil Oil Corporation||Isomerization process|
|US5061466 *||16 Nov 1987||29 Oct 1991||Mobil Oil Corporation||Synthesis of large pore zeolites containing gallium|
|US5095169 *||11 Oct 1990||10 Mar 1992||Uop||Normal paraffin hydrocarbon isomerization process using activated zeolite beta|
|US5116794 *||21 Jun 1990||26 May 1992||Uop||Method for enhancing the activity of zeolite beta|
|US5128024 *||25 Mar 1991||7 Jul 1992||Mobil Oil Corporation||Simultaneous catalytic hydrocracking and hydrodewaxing of hydrocarbon oils with zeolite beta|
|US5132020 *||15 Oct 1991||21 Jul 1992||Mobil Oil Corp.||Sorption of alcohols using zeolite beta|
|US5157192 *||12 Nov 1991||20 Oct 1992||Mobil Oil Corporation||Conversion of tertiary alcohols to C8+ olefins|
|US5200168 *||31 Ene 1992||6 Abr 1993||Mobil Oil Corp.||Process for the dealumination of zeolite Beta|
|US5228979 *||5 Dic 1991||20 Jul 1993||Union Oil Company Of California||Hydrocracking with a catalyst containing a noble metal and zeolite beta|
|US5232579 *||14 Jun 1991||3 Ago 1993||Mobil Oil Corporation||Catalytic cracking process utilizing a zeolite beta catalyst synthesized with a chelating agent|
|US5258570 *||30 Sep 1991||2 Nov 1993||Uop||Activated zeolite beta and its use for hydrocarbon conversion|
|US5275720 *||30 Nov 1990||4 Ene 1994||Union Oil Company Of California||Gasoline hydrocracking catalyst and process|
|US5310714 *||8 Jul 1992||10 May 1994||Mobil Oil Corp.||Synthesis of zeolite films bonded to substrates, structures and uses thereof|
|US5316661 *||16 Abr 1993||31 May 1994||Mobil Oil Corporation||Processes for converting feedstock organic compounds|
|US5328590 *||27 Feb 1992||12 Jul 1994||Union Oil Company Of California||Hydrocracking process using a catalyst containing zeolite beta and a layered magnesium silicate|
|US5350501 *||28 Feb 1991||27 Sep 1994||Union Oil Company Of California||Hydrocracking catalyst and process|
|US5364997 *||6 Jul 1993||15 Nov 1994||Mobil Oil Corporation||Process for converting multi-branched heavy hydrocarbons to high octane gasoline|
|US5374349 *||11 Sep 1991||20 Dic 1994||Union Oil Company Of California||Hydrocracking process employing catalyst containing zeolite beta and a pillared clay|
|US5389358 *||16 Jul 1993||14 Feb 1995||W. R. Grace & Co.-Conn.||Zeolite GZS-11 and its dynamic preparation process|
|US5393407 *||26 Jun 1992||28 Feb 1995||Chevron Research Company||Hydrocarbon conversion utilizing a low-aluminum boron beta zeolite|
|US5393718 *||26 Jul 1993||28 Feb 1995||Uop||Activated zeolite beta and its use for hydrocarbon conversion|
|US5413977 *||23 Jun 1994||9 May 1995||Union Oil Company Of California||Catalyst containing zeolite beta and a layered magnesium silicate|
|US5427765 *||31 Mar 1994||27 Jun 1995||Tosoh Corporation||Method of producing zeolite β|
|US5447623 *||2 May 1994||5 Sep 1995||Uop||Hydrocracking catalyst and process|
|US5488193 *||25 Ene 1995||30 Ene 1996||Mobil Oil Corporation||Process for reducing polynuclear aromatic mutagenicity by alkylation|
|US5489719 *||6 Jun 1994||6 Feb 1996||Mobil Oil Corporation||Process for the production of tertiary alkyl ether rich FCC gasoline|
|US5522984 *||30 May 1995||4 Jun 1996||Uop||Modified zeolite beta, processes for preparation and use thereof|
|US5536687 *||31 May 1994||16 Jul 1996||Uop||Catalyst containing zeolite Beta|
|US5582713 *||6 Jun 1995||10 Dic 1996||W. R. Grace & Co.-Conn.||Catalytic cracking utilizing a catalyst comprising zeolite GZS-11|
|US5589153 *||2 Jun 1995||31 Dic 1996||The Dow Chemical Company||Synthesis of crystalline porous solids in ammonia|
|US5609654 *||31 May 1995||11 Mar 1997||Mobil Oil Corporation||Process for hydroisomerization and etherification of isoalkenes|
|US5614453 *||25 Oct 1994||25 Mar 1997||Uop||Catalyst containing zeolite beta and a pillared clay|
|US5626828 *||18 Oct 1994||6 May 1997||W. R. Grace & Co.-Conn.||Zeolite GZS-11 and its dynamic preparation process|
|US5659099 *||28 Feb 1995||19 Ago 1997||Uop||Activated zeolite beta and its use for hydrocarbon conversion|
|US5744673 *||20 Dic 1996||28 Abr 1998||Uop||Activated zeolite beta and its use for hydrocarbon conversion|
|US5763727 *||1 Feb 1993||9 Jun 1998||Mobil Oil Corporation||Fluidized bed paraffin disproportionation|
|US6294077||2 Feb 2000||25 Sep 2001||Mobil Oil Corporation||Production of high viscosity lubricating oil stock with improved ZSM-5 catalyst|
|US6306364 *||28 Sep 1999||23 Oct 2001||Uop Llc||Stannosilicate molecular sieves|
|US6392109||29 Feb 2000||21 May 2002||Chevron U.S.A. Inc.||Synthesis of alkybenzenes and synlubes from Fischer-Tropsch products|
|US6409986||18 Dic 1998||25 Jun 2002||Consejo Superior De Investigaciones Cientificas Universidad Politecnica De Valencia||Zeolite ITQ-5|
|US6440886||3 Nov 2000||27 Ago 2002||Uop Llc||Zeolite beta and its use in aromatic alkylation|
|US6441263||7 Jul 2000||27 Ago 2002||Chevrontexaco Corporation||Ethylene manufacture by use of molecular redistribution on feedstock C3-5 components|
|US6455595||24 Jul 2000||24 Sep 2002||Chevron U.S.A. Inc.||Methods for optimizing fischer-tropsch synthesis|
|US6472441||24 Jul 2000||29 Oct 2002||Chevron U.S.A. Inc.||Methods for optimizing Fischer-Tropsch synthesis of hydrocarbons in the distillate fuel and/or lube base oil ranges|
|US6521206 *||27 Jul 2000||18 Feb 2003||California Institute Of Technology||Molecular sieve CIT-6|
|US6566569||23 Jun 2000||20 May 2003||Chevron U.S.A. Inc.||Conversion of refinery C5 paraffins into C4 and C6 paraffins|
|US6649662||20 Jun 2002||18 Nov 2003||Chevron U.S.A. Inc.||Methods for optimizing fischer-tropsch synthesis of hydrocarbons in the distillate fuel and/or lube base oil ranges|
|US6670517||24 Ago 2000||30 Dic 2003||Exxon Mobil Chemical Patents Inc.||Process for alkylating aromatics|
|US6806087||28 May 2002||19 Oct 2004||Chevron U.S.A. Inc.||Use of microchannel reactors in combinatorial chemistry|
|US6846406||11 Abr 2003||25 Ene 2005||Consejo Superior De Investigaciones Cientificas||Process and catalysts for eliminating sulphur compounds from the gasoline fraction|
|US6891056||3 Oct 2003||10 May 2005||Shell Oil Company||Branched primary alcohol compositions and derivatives thereof|
|US6909020||3 Oct 2003||21 Jun 2005||Shell Oil Company||Branched primary alcohol compositions and derivatives thereof|
|US6916459||11 Abr 2003||12 Jul 2005||Consejo Superior De Investigaciones Cientificas||Zeolite ITQ-16|
|US6972348||24 Mar 2004||6 Dic 2005||Uop Llc||Catalytic conversion of polycyclic aromatics into xylenes|
|US6995295||23 Sep 2002||7 Feb 2006||Exxonmobil Chemical Patents Inc.||Alkylaromatics production|
|US7056489||1 Ago 2003||6 Jun 2006||Consejo Superior De Investigaciones Cientificas||Synthesis of zeolite ITQ-16 in an alkaline medium|
|US7071364||3 Oct 2003||4 Jul 2006||Shell Oil Company||Branched primary alcohol compositions and derivatives thereof|
|US7119042||10 Mar 2004||10 Oct 2006||Gifu University||Catalyst composition for the isomerization of n-paraffin and a process for isomerizing n-paraffin|
|US7148375||2 Abr 2004||12 Dic 2006||Shell Oil Company||Branched primary alcohol compositions and derivatives thereof|
|US7154014||22 Sep 2004||26 Dic 2006||Uop Llc||Alumina guard bed for aromatics transalkylation process|
|US7220885||27 May 2004||22 May 2007||Uop Llc||Catalyst treatment useful for aromatics conversion process|
|US7271303||22 Sep 2004||18 Sep 2007||Uop Llc||Multi-zone process for the production of diesel and aromatic compounds|
|US7273828||27 May 2004||25 Sep 2007||Uop Llc||Catalyst treatment useful for aromatics conversion process|
|US7307034||19 Oct 2006||11 Dic 2007||Uop Llc||Alumina guard bed for aromatics transalkylation process|
|US7348465||8 Feb 2005||25 Mar 2008||Shell Oil Company||Selective alkylation of aromatic hydrocarbons|
|US7393805||11 Abr 2007||1 Jul 2008||Uop Llc||Catalyst treatment useful for aromatics conversion process|
|US7411101||6 Feb 2002||12 Ago 2008||Exxonmobil Chemical Patents Inc.||Production of alkylaromatic compounds|
|US7420098||12 Ene 2007||2 Sep 2008||Uop Llc||Dual zone aromatic alkylation process|
|US7425659||31 Ene 2006||16 Sep 2008||Exxonmobil Chemical Patents Inc.||Alkylaromatics production|
|US7501547||10 May 2006||10 Mar 2009||Exxonmobil Chemical Patents Inc.||Alkylaromatics production|
|US7544849||22 May 2008||9 Jun 2009||Uop Llc||Catalyst treatment useful for aromatics conversion process|
|US7692052||14 Jun 2007||6 Abr 2010||Uop Llc||Multi-zone process for the production of xylene compounds|
|US7749373||13 Dic 2005||6 Jul 2010||Haldor Topsoe A/S||Hydrocracking process|
|US7772448||28 Ene 2009||10 Ago 2010||Badger Licensing Llc||Alkylaromatics production|
|US7868218||9 Jun 2010||11 Ene 2011||Exxonmobil Chemical Patents Inc.||Alkylaromatics production|
|US7923590||27 Jun 2008||12 Abr 2011||Exxonmobil Chemical Patents Inc||Production of alkylaromatic compounds|
|US8247627||16 Mar 2009||21 Ago 2012||Exxonmobil Chemical Patents Inc.||Process for producing phenol and/or cyclohexanone|
|US8247629||17 Abr 2007||21 Ago 2012||Exxonmobil Chemical Patents Inc.||Monoalkylated aromatic compound production|
|US8357830||29 Jun 2012||22 Ene 2013||Exxonmobil Chemical Patents Inc.||Monoalkylated aromatic compound production|
|US8445738||23 Sep 2009||21 May 2013||Badger Licensing Llc||Process for producing cumene|
|US8518242||26 May 2011||27 Ago 2013||Uop Llc||Fibrous substrate-based hydroprocessing catalysts and associated methods|
|US8524967||14 Nov 2012||3 Sep 2013||Exxonmobil Chemical Patents Inc.||Monoalkylated aromatic compound production|
|US8580228||20 Dic 2007||12 Nov 2013||Chevron U.S.A. Inc.||Treatment of cold start engine exhaust|
|US8586496||19 Jun 2009||19 Nov 2013||Exxonmobil Chemical Patents Inc.||Preparation of molecular sieve catalysts and their use in the production of alkylaromatic hydrocarbons|
|US8629311||10 Mar 2010||14 Ene 2014||Stone & Webster, Inc.||Alkylated aromatics production|
|US8633342||24 Sep 2009||21 Ene 2014||Badger Licensing Llc||Process for producing alkylaromatic compounds|
|US8802907||17 Dic 2010||12 Ago 2014||Exxonmobil Chemical Patents Inc.||Dehydrogenation process|
|US8877996||8 Nov 2013||4 Nov 2014||Exxonmobil Chemical Patents Inc.||Alkylated aromatics production|
|US8884088||17 Dic 2010||11 Nov 2014||Exxonmobil Chemical Patents Inc.||Dehydrogenation process|
|US8969639||17 Dic 2010||3 Mar 2015||Exxonmobil Chemical Patents Inc.||Dehydrogenation process|
|US9114362||26 Sep 2013||25 Ago 2015||Chevron U.S.A. Inc.||Treatment of cold start engine exhaust|
|US9382171||21 Jul 2014||5 Jul 2016||Exxonmobil Chemical Patents Inc.||Iridium-containing catalysts, their production and use|
|US20040042958 *||11 Abr 2003||4 Mar 2004||Canos Avelino Corma||Zeolite ITQ-16|
|US20040068133 *||3 Oct 2003||8 Abr 2004||Edwards Charles Lee||Branched primary alcohol compositions and derivatives thereof|
|US20040191144 *||8 Mar 2004||30 Sep 2004||California Institute Of Technology||Molecular sieve CIT-6|
|US20040198628 *||2 Abr 2004||7 Oct 2004||Edwards Charles Lee||Branched primary alcohol compositions and derivatives thereof|
|US20040220438 *||6 Feb 2002||4 Nov 2004||Shiou-Shan Chen||Production of alkylaromatic compounds|
|US20050266979 *||27 May 2004||1 Dic 2005||Boldingh Edwin P||Catalyst treatment useful for aromatics conversion process|
|US20050277800 *||10 Mar 2004||15 Dic 2005||Yoshihiro Sugi||Catalyst composition for the isomerization of n-paraffin and a process for isomerizing n-paraffin|
|US20060194279 *||7 Jul 2004||31 Ago 2006||Fujio Mizukami||Protein-refolding material|
|US20070042905 *||19 Oct 2006||22 Feb 2007||Antoine Negiz||Alumina Guard Bed for Aromatics Transalkylation Process|
|US20070086933 *||19 Oct 2006||19 Abr 2007||Antoine Negiz||Alumina Guard Bed for Aromatics Transalkylation Process|
|US20070179329 *||31 Ene 2006||2 Ago 2007||Clark Michael C||Alkylaromatics production|
|US20070185356 *||11 Abr 2007||9 Ago 2007||Boldingh Edwin P||Catalyst Treatment Useful for Aromatics Conversion Process|
|US20070265481 *||10 May 2006||15 Nov 2007||Clark Michael C||Alkylaromatics production|
|US20080128324 *||13 Dic 2005||5 Jun 2008||Hansen Jens A||Hydrocracking Process|
|US20080161622 *||14 Jun 2007||3 Jul 2008||Frey Stanley J||Multi-zone process for the production of xylene compounds|
|US20080171900 *||12 Ene 2007||17 Jul 2008||Schmidt Robert J||Dual zone aromatic alkylation process|
|US20080221375 *||22 May 2008||11 Sep 2008||Boldingh Edwin P||Catalyst Treatment Useful for Aromatics Conversion Process|
|US20080262279 *||27 Jun 2008||23 Oct 2008||Shiou-Shan Chen||Production of Alkylaromatic Compounds|
|US20090005543 *||4 Sep 2008||1 Ene 2009||National Inst Of Adv Industrial Science And Tech.||Protein-refolding material|
|US20090137855 *||28 Ene 2009||28 May 2009||Clark Michael C||Alkylaromatics Production|
|US20090306446 *||17 Abr 2007||10 Dic 2009||Exxonmobil Chemical Patents Inc.||Monoalkylated Aromatic Compound Production|
|US20100249472 *||9 Jun 2010||30 Sep 2010||Clark Michael C||Alkylaromatics Production|
|US20110037022 *||16 Mar 2009||17 Feb 2011||Exxonmobil Chemical Patents Inc.||Process for Producing Phenol and/or Cyclohexanone|
|US20110118521 *||19 Jun 2009||19 May 2011||Duncan Carolyn B||Preparation Of Molecular Sieve Catalysts And Their Use In The Production Of Alkylaromatic Hydrocarbons|
|US20110178342 *||23 Sep 2009||21 Jul 2011||Badger Licensing Llc||Process for producing cumene|
|US20110201858 *||23 Sep 2009||18 Ago 2011||Badger Licensing Llc||Process for producing cumene|
|US20110224468 *||24 Sep 2009||15 Sep 2011||Vincent Matthew J||Process for Producing Alkylaromatic Compounds|
|US20110224469 *||10 Mar 2010||15 Sep 2011||Vincent Matthew J||Alkylated Aromatics Production|
|EP0024948A2 *||3 Sep 1980||11 Mar 1981||Mobil Oil Corporation||A process for converting a high boiling hydrocarbon and catalyst for use in this process|
|EP0024948A3 *||3 Sep 1980||18 Mar 1981||Mobil Oil Corporation||A process for converting a high boiling hydrocarbon and catalyst for use in this process|
|EP0030784A1 *||3 Sep 1980||24 Jun 1981||Mobil Oil Corporation||A catalytic hydrocarbon-conversion process and a catalyst composition|
|EP0055046A1 *||4 Dic 1981||30 Jun 1982||Imperial Chemical Industries Plc||Zeolites|
|EP0095304A1 *||17 May 1983||30 Nov 1983||Mobil Oil Corporation||High silica zeolite beta and method for making it|
|EP0181096A1 *||10 Oct 1985||14 May 1986||Mobil Oil Corporation||Hydrocracking catalyst compostion and hydrocracking process using same|
|EP0186447A2 *||19 Dic 1985||2 Jul 1986||Mobil Oil Corporation||Catalytic cracking of paraffinic feedstocks with zeolite beta|
|EP0186447A3 *||19 Dic 1985||11 Nov 1987||Mobil Oil Corporation||Catalytic cracking of paraffinic feedstocks with zeolite beta|
|EP1894909A2||6 Feb 2002||5 Mar 2008||ExxonMobil Chemical Patents Inc.||Production of alkylaromatic compounds|
|EP1944075A2||6 Nov 2007||16 Jul 2008||GM Global Technology Operations, Inc.||Hybrid catalyst for NOx reduction using fuel hydrocarbons as reductant|
|WO2003093230A2||8 Abr 2003||13 Nov 2003||Chevron U.S.A., Inc.||Process for aromatics alkylation employing zeolite beta prepared by the in-extrudate method|
|WO2006107470A1||1 Mar 2006||12 Oct 2006||Exxonmobil Chemical Patents, Inc.||Multiphase alkylaromatics production|
|WO2006130248A2||18 Abr 2006||7 Dic 2006||Exxonmobil Chemical Patents Inc.||Process for reducing bromine index of hydrocarbon feedstocks|
|WO2007089381A2||3 Ene 2007||9 Ago 2007||Exxonmobil Chemical Patents Inc.||Alkylaromatics production|
|WO2008100658A1||10 Ene 2008||21 Ago 2008||Exxonmobil Chemical Patents Inc.||Production of high purity ethylbenzene from non-extracted feed and non-extracted reformate useful therein|
|WO2011071755A2||3 Dic 2010||16 Jun 2011||Exxonmobil Research And Engineering Company||Process and system to convert methanol to light olefin, gasoline and distillate|
|WO2011075523A2||15 Dic 2010||23 Jun 2011||Exxonmobil Research And Engineering Company||Process and system to convert olefins to diesel and other distillates|
|WO2011096991A1||17 Dic 2010||11 Ago 2011||Exxonmobil Chemical Patents Inc.||Dehydrogenation process|
|WO2011096995A1||17 Dic 2010||11 Ago 2011||Exxonmobil Chemical Patents Inc.||Dehydrogenation process|
|WO2013059172A1||16 Oct 2012||25 Abr 2013||Exxonmobil Research And Engineering Company||Process for producing phosphorus modified zeolite catalysts|
|WO2013119318A1||13 Dic 2012||15 Ago 2013||Exxonmobil Chemical Patents Inc.||Production of monoalkyl aromatic compounds|
|WO2014003732A1||27 Jun 2012||3 Ene 2014||Badger Licensing Llc||Process for producing cumene|
|WO2014008268A1||2 Jul 2013||9 Ene 2014||Badger Licensing Llc||Process for producing cumene|
|WO2014182294A1||8 May 2013||13 Nov 2014||Badger Licensing Llc||Aromatics alkylation process|
|WO2016085908A1||24 Nov 2015||2 Jun 2016||Badger Licensing Llc||Process for reducing the benzene content of gasoline|
|Clasificación de EE.UU.||208/120.15, 423/DIG.270, 502/86, 502/77, 208/120.1, 423/705, 502/60|
|Clasificación internacional||C01B39/48, C01B39/00, B01J29/00, B01J29/70|
|Clasificación cooperativa||B01J29/7007, C01B39/48, B01J29/7057|
|Clasificación europea||C01B39/48, B01J29/70B, B01J29/70Z4|