HIGH-SILICA MORDENITE AND PROCESS FOR PREPARATION THEREOF

Abstract: A high-silica mordenite is provided, which is a synthetic mordenite prepared without performing the dealuminization treatment, and is characterized in that the silica/alumina molar ratio is in the range of from 12 to 30 and the amount of benzene adsorption is 7 to 10% by weight as determined at a temperature of 25°C under a vapor pressure of 35 mmHg. The high-silica mordenite is prepared by a process wherein a reaction mixture having a composition represented by the following oxide molar ratios: Na₂/SiO₂ = 0.08 - 0.2 SiO₂/Al₂O = 14 - 55 H₂O/Na₂O = 100 - 300 and H₂O/SiO₂ = 10 - 40 is formed using synthetic amorphous silicic acid having an apparent specific gravity of from 0.05 to 0.45 g/ml as a silica source, and the reaction mixture is heated at a temperature of 140 to 180°C with stirring to effect crystallization.

Description: HIGH-SILICA MORDENITE AND PROCESS FOR PREPARATION THEREOF BACKGROUND OF THE INVENTION (1) Field of the Invention This invention relates to a high-silica mordenite having a high benzene adsorption capacity and a process for the preparation thereof. (2) Description of the Prior Art As is seen from the fact that the term "zeolite" is derived from the Greek word "vein" (boiling stone), the zeolite is a crystalline aluminosilicate containing zeolitic water. The basic structure of the zeolite comprises SiO4 tetrahedrons having four oxygen atoms at apexes with the silicon atom being as the center and A104 tetrahedrons having four oxygen atoms at apexes with the aluminum atom being as the center, where these SiO4 tetrahedrons and A104 tetrahedrons are regularly and three-dimensionally connected to one another while owning oxygen atoms jointly so that the O/(Al + Si) atomic ratio is 2. Negative charges of the A104 tetrahedrons are electrically neutralized by coupling with cations of an alkali metal or alkaline earth metal. Various pores are formed, which sizes differ depending upon the particular manner of arrangement of the tetrahedrons. Ordinarily, water molecules and exchangeable cations are present in these pores. Products obtained by exchanging cations in zeolite with other appropriate cations are widely used as a molecular sieve having a function of selectively occluding a specific molecule in the pores thereof, a catalyst capable of advancing a certain reaction only in the pores thereof, an ion exchanger or a catalyst carrier. various zeolites differing in the crystal structure and chemical composition are known, and in these zeolites, the adsorbing properties, catalytic properties and ion exchanging properties are different according to the differences of the crystal structure and chemical composition. Different zeolite names are given to the respective zeolites. Zeolites are naturally produced, and at the present, those which are the same as the natural zeolites can be syntheiszed. Furthermore, even zeolites which do not naturally occur can be synthesized. As the zeolite of the former type, that is, naturally occurring zeolites, there can be mentioned mordenite, offretite, erionite, clinoptilolite and chabazite, and as the zeolite of the latter type, that is, the synthetic zeolite, there are known many products such as zeolite A, zeolite X, zeolite Y, ZK-4 and ZSM-5. These zeolites can be discriminated from one another by X-ray powder diffraction patterns. The mordenite intended in the present invention is distinguished from a natural mordenite and ordinarily called nsynthetic mordenite" or "large port mordenite". The crystal of the mordenite is of the orthorhombic system and is characterized by the lattice constants a, b and c of 18.1 angstroms, 20.4 angstroms and 7.5 anstroms, respectively. The pores have a channel of the 12-membered rings of oxygen atoms having a pore diameter of 6.7 x 7.0 angstroms and a channel of the 8-membered rings of oxygen atoms having a pore diameter of 2.9 x 5.7 angstroms. A typical X-ray diffraction pattern of mordenite powder is characterized by lattice spacings (d ) shown in Table 1, by which the mordenite is clearly distinguishable over other zeolites. Table 1 Spacing 26 (degrees) by Relative Peak (aA) Ka Doublet of Cu Intensity (I) 13.52 6.53 42 10.19 8.67 7 9.03 9.79 100 6.77 13.1 4 6.57 13.5 8 6.38 13.9 37 6.06 14.6 3 5.78 15.3 28 4.51 19.7 42 4.26 20.8 6 4.133 21.5 9 3.980 22.3 100 3.830 23.2 5 3.757 23.7 8 3.563 25.0 14 3.528 25.2 3 3.471 25.6 24 3.410 26.1 23 3.386 26.3 44 3.218 27.7 24 3.198 27.9 35 2.939 30.4 3 2.891 30.9 11 2.710 33.0 2 2.697 33.2 33 2.556 35.1 18 2.519 35.6 4 2.460 36.5 4 The source of Table 1 is "Zeolite Molecular Sieves", page 231, by Donald W. Breck, and the values for 26 have been supplemented by us. The value of 26 and the relative intensity of mordenite differ more or less according to the synthesis process, but all of zeolites obtained according to the present invention are included in the synthetic mordenite. Mordenite is ordinarily represented by the following chemical formula: Na2OAl2O3l0SiO26H2O Namely, mordenite is characteristic over other zeolites in that the SiO2/A1203 molar ratio is 10 and higher than those of other zeolites. Mordenite is excellent in the heat resistance and acid resistance, and therefore, mordenite is widely used as an adsorbent or a catalyst in various industries. It has been found that in zeolites, increase of the SiO2/A1203 molar ratio results in improvements of not only the heat resistance and acid resistance but also the catalytic properties as a solid acid, and therefore, high-silica zeolites represented by ZSM-5 developed by Mobil Oil Co. have recently attracted attention in the art. However, an organic mineralizer such as a quaternary ammonium salt is used in the process for preparing a zeolite of the ZSM-5 type, and hence, this process is not advantageous. Furthermore, since the pore size of ZSM-5 is 5 to 6 angstroms and smaller than those of synthetic mordenite, uses of ZSM-5 are considerably limited. Accordingly, development of an industrial process for preparing a mordenite having a high Six2/ Al 203 ratio is eagerly desired. Various processes for increasing the SiO2/ A1203 molar ratio of mordenite above 10 have been proposed. For example, the following processes can be mentioned. (1) Japanese Examined Patent Publication No. 51-15000 discloses a process in which after contact of mordenite with water vapor at high temperatures, a mineral acid treatment is repeated for removal of alumina by dissolution. However, since the SiO2/A1203 molar ratio is increased over 10 by treating once -prepared mordenite, the process is complicated. Moreover, pores of high-silica mordenite obtained by the dealuminization treatment crumble owing to the repetition of the mineral acid treatment, resulting in reduction of the heat resistance. Accordingly, the increase of the SiO2/A1203 is practically limited, and other properties are not so improved as expected even if the SiO2/A1203 molar ratio is increased. (2) The report of O.J. Whittemore, Jr., American Mineralogist, Volume 57, 1146-1151, 1972 discloses a process for preparing mordenite in which an alumina-silica gel having an SiO2/A1203 molar ratio of 10.1 to 15.5 is prepared from a dilute aqueous solution of sodium silicate, a dilute aqueous solution of aluminum chloride and hydrochloric acid; and the alumina-silica gel is crystallized by heating the gel at 1840C for 16 hours, whereby a mordenite having an SiO2/A1203 molar ratio of 12 to 19.5 is obtained. This process requires complicated steps of forming an alumina-silica gel in advance, adding this gel to an aqueous solution of sodium silicate after filtration, water washing and drying and subjecting the so-prepared starting composition to crystallization. (3) Japanese Unexamined Patent Publication No. 56-160316 discloses a process for preparing a high-silica mordenite having an SiO2/A1203 molar ratio of 15 to 25.8 from sodium silicate, aluminum sulfate, sulfuric acid and sodium chloride. From the industrial viewpoint, this process is not preferred because aluminum sulfate and sulfuric acid both having a highly corrosive action are used and a large amount of sodium chloride should be used as a mineralizer. Furthermore, from the results of the tracing experiments made by us, it has been confirmed that a high-silica mordenite having a high benzene adsorption cannot be obtained according to this process. SUMMARY OF THE INVENTION It is a primary object of the present invention to provide a high-silica mordenite having a high purity, an SiO2/A1203 molar ratio of 12 to 30 and a high benzene adsorption capacity, which can be obtained without using an organic mineralizer or inorganic mineralizer. Other objects and advantages of the present invention will be apparent from the following description. In one aspect of the present invention, there is provided a high-silica mordenite which is a synthetic mordenite prepared without performing the dealuminization treatment, said mordenite being characterized in that the silica/alumina molar ratio is in the range of from 12 to 30 and the amount of benzene adsorption is 7 to 10% by weight as determined at a temperature of 250C under a vapor pressure of 35 mmHg. In another aspect of the present invention, there is provided a process for the preparation of a synthetic mordenite having a silica/alumina molar ratio of from 12 to 30, which comprises preparing a reaction mixture having a composition represented by the following oxide molar ratios: Na2O/Sio2 = 0.08 - 0.2 SiO2/A12O3 = 14 - 55 H2O/Na2O = 100 - 300 and H2O/SiO2 2 10 - 40 by using synthetic amorphous silicic acid having an apparent specific gravity of from 0.05 to 0.45 g/ml as a silica source, and heating the reaction mixture at a temperature of 140 to 1800C with stirring to effect crystallization. BRIEF DESCRIPTION OF THE DRAWING Figs. 1 through 3 are X-ray powder X-ray diffraction patterns (Ka doublet of copper) of the high-silica mordenites obtained in Example 1, 2 and 4, respectively; and Fig. 4 is an X-ray powder X-ray diffraction pattern of the product obtained in Comparative Example 2. DESCRIPTION OF THE PREFERRED EMBODIMENTS The preparation process of the present invention is characterized in that a specific silica source is used. Namely, the silica source used in the present invention is limited to synthetic amorphous silicic acid having an apparent specific gravity of from 0.05 to 0.45 g/ml, especially from 0.10 to 0.35 g/ml, as determined according to a method described hereinafter, that is, so -called white carbon. The process for the preparation of white carbon is not particularly critical, but, for example,. a customary process for forming white carbon from water glass and sulfuric acid may be adopted. The apparent specific gravity of white carbon differs according to the particle size, the size of secondary particles and the specific surface area. Any white carbon can be used in the present invention if the above-mentioned requirement of the apparent specific gravity is satisfied. When ordinary silica sources such as sodium silicate, silica sol, silica gel and siliceous natural products are used, a high-silica mordenite free of impurities cannot be obtained unless an organic or inorganic mineralizer is used. Furthermore, in this case, even if'a mineralizer is used, a high-silica mordenite having a high benzene adsorption cannot be obtained. The kind of the alumina source is not particularly critical. For example, there can be used aluminum oxide, aluminum hydroxide, sodium aluminate, aluminum sulfate and aluminum nitrate. An aqueous solution of sodium aluminate is most preferred as the alumina source. Sodium hydroxide is preferably used as an alkaline adjusting agent. In the present invention, it is indispensable that a reaction mixture having a composition represented by the following oxide molar ratios should be prepared from the silica source, the alumina source, the alkaline adjusting agent and water and subjected to the crystallization: Na2O/SiO2 = 0.08 - 0.20 SiO2/A1203 = 14 - 55 H20/Na2O = 100 - 300 H20/SiO2 = 10 - 40 The process for forming this reaction mixture from the above-mentioned starting materials is not particularly critical. However, according to a preferred embodiment of the present invention, the alumina source and soidum hydroxide are dissolved in water, the silica source is incorporated into the solution with stirring, and then the resulting reaction mixture is charged in an autoclave where the reaction mixture is heated at 140 to 1800C with stirring to effect crystallization. The time required for the crystallization is 20 to 150 hours, though the crystallization time differs according to the heating temperature. In the present inventin, stirring during the crystallization is important. More specifically, it is preferred that the peripheral speed defined by the following formula: (n) (d) (v) 60 wherein d stands for a maximum diameter (m) of a stirring vane during rotation and v stands for the stirring speed (rpm), by at least 0.1 m/sec. If the peripheral speed is lower than 0.1 m/sec and thus the stirring is weak, a temperature unevenness is caused in the reaction mixture. Consequently, the crystallization of the product is insufficient and the crystallization degree is low or impurities such as analcime are readily formed. It is especially preferred that the stirring speed be at least 0.5 m/sec. A preferred crystallization temperature is 150 to 1700C. In this case, the crystallization time is 40 to 80 hours. The composition of the high-silica mordenite prepared according to the present invention can be expressed by the following formula: xNa2OAl2O3. (12-30)SiO2.yH2O In the above formula, the value of x differs according to the degree of water washing, but the value of x is ordinarily about 1, and y is 0 or a positive number and also this value differs according to the degree of drying or dehydration. The SiO2/A1203 molar ratio of the product can be adjusted by the following methods. If a starting mixture having a higher SiO2/A12O3 molar ratio or a lower Na2O/SiO2 molar ratio is used, the SiO2/A1203 molar ratio of the product is increased. If the SiO2/A1203 molar ratio of the starting mixture is reduced or the Na2O/SiO2 molar ratio of the starting mixture is increased, the SiO2/A1203 molar ratio of the product is reduced. In order to increase the ratio of SiO2 recovered as the crystal to SiO2 used as the starting material, that is, the yield of SiO2 , it is preferred that the Na2O/SiO2 molar ratio of the starting mixture be low. If the composition of the starting mixture is outside the range specified in the present inventin, impurities are formed, an amorphous product is present in the product and the crystallization degree is not increased, and in an extreme case, the crystallization is not advanced at all. From the viewpoint of the reaction operation, an amount of water used for the reaction is important. If the amount of water is too small, the stirring is impossible. In contrast, if the amount of water is too large, the amount of the obtained product per unit volume of the reaction vessel is reduced. It is preferred that the H2O/SiO2 molar ratio in the starting mixture be in the range of from 15 to 30. In the present invention, it is not necessary to use an organic mineralizer such as a quaternary ammonium salt or an inorganic mineralizer such as sodium chloride in addition to the above-mentioned silica source, alumina source, alkaline adjusting agent and water. This is one of important features of the process of the present invention. After completion of the crystallization, solid -liquid separation is carried out according to customary procedures, and the recovered solid is sufficiently washed with water and dried to obtain a product. The amount of benzene adsorption of the high-silica mordenite prepared according to the process of the present invention is in the range of from 7 to 10% by weight as determined at a temperature of 250C under a benzene vapor pressure of 35 mmHg, which is much higher than the amount of benzene adsorption of commercially available mordenite Zeolon 100Na, that is, 5.8% by weight. The reason why the high-silica mordenite of the present invention has a high benzene adsorption capacity has not been elucidated completely, but it is presumed that this effect is attained by the increased affinity of the mordenite with benzene, more specifically, not only by the high silica/alumina molar ratio, but also, by the increased purity and uniform and regular crystal structure obtained under the specific reaction conditions of the present invention, as well as by the fact that no mineralizing agent is used. The high-silica mordenite prepared according to the process of the present invention is ion-exchanged with an appropriate cation by a known method in the powdery state or after molding. The high-silica mordenite is used in various fields, for example, as a dehydrating agent, an adsorptive separating agent or a catalyst. Furthermore, since the high-silica mordenite of the present invention has a very high benzene adsorption capacity, it can effectively be used as an adsorbent for benzene and other aromatic compounds, and it can also be used effectively as an alkylation or disproportionation catalysts. The present invention will now be described in detail with reference to the following examples. In the examples, the apparent specific gravity and the amount of benzene adsorption were determined as follows. Apparent Specific Gravity 1 g of a sample is charged in a cylinder of an apparent specific gravity measuring apparatus, and a piston is inserted into the cylinder and quietly brought down into the sample while holding the piston lightly with fingers. The piston is allowed to stand still in this state for 30 minutes, and the height difference H (cm) between the piston and cylinder is measured and the apparent specific gravity is calculated according to the following formula: Apparent specific gravity = (H - 2*) x Note: The apparent specific gravity measuring apparatus comprises a metallic cylinder and a piston to be adapted to the cylinder. The cylinder has an inner diameter of 2.2 cm and a depth of 11.5 cm, and the piston has a length of 12.7 cm and a weight of 190 g. The apparent specific gravity measured by this method is expressed by the weight (g) of 1 ml of the sample compressed under a pressure of 50 g/cm2. *: 1.2 = 12.7 - 11.5 **: 3.8 = area of cylinder = 1.1 x 1.1 x 3.14 Amount of Benzene Adsorption McBain-Baker type adsorption apparatus is used for the measurement. After about 1 g of a sample is activated at 3500C in vacuo for 2 hours, the sample is maintained at 250C and benzene vapor is introduced under a pressure of 35 mmHg. The amount adsorbed of benzene is measured after passage of 3 hours. Example 1 A vessel was charged with 7.16 liters of pure water, and 44.2 g of solid sodium hydroxide and 540 g of an aqueous solution of sodium aluminate (Na2O = 19.4% by weight, A1203 = 20.1% by weight, H2O = 60.5% by weight) were added. Then, 1.45 kg of white carbon (Nipsil supplied by Nippon Silica Industrial Co., Ltd. and having an apparent specific gravity of 0.14) was added to the mixture with stirring to obtain a reaction mixture having the following composition: 2.1Na2O A1203 20SiO2 '400H20 This reaction mixture was charged in an autoclave having a capacity of 10 liters and was heated at 1650C for 48 hours with stirring at a peripheral speed of 1 m/sec to effect crystallization. Solid-liquid separation was carried out, and the recovered solid was sufficiently washed with water and then dried at 1100C to obtain a product having the following composition: 1.06Na2O A1203O17.4SiO2*0.2H2O - The crystallization degree and the presence or absence of impurities are shown in Table 2. The X-ray diffraction pattern of the product is shown in Fig. 1. Examples 2 through 5 and Comparative Examples I through 4 The procedures of Example 1 were repeated in the same manner except that the composition of the starting material, silica source and temperature and other conditions were changed as indicated in Table 2. Incidentally, an autoclave having a capacity of 1 liter was used for the crystallization. The obtained results are shown in Table 2. The X-ray diffraction patterns of the products obtained in Examples 2 and 4 and Comparative Example 2 are shown in Figs. 2, 3 and 4, respectively. The silica sources in Table 2 are as follows: A: Nipsil VN-3 supplied by Nippon Silica Industrial Co., Ltd. (apparent specific gravity = 0.14) B: Carplex X67 supplied by Shionogi Seiyaku (apparent specific gravity = 0.17) C: Silica Gel 70A supplied by Dokai Kagaku Kogyo (apparent specific gravity = 0.5) Table 2 Composition of Crystallization Conditions Product Starting Mixture Na2O/ SiO2/ H2O/ H2O/ Temper- Time Stirring SiO2/ Crystal- Impurities Silica Benzene ature Speed lization source Adsorption SiO2 Al2O3 Na2O SiO2 ( C) (hours) (m/sec) Al2O3 Degree (% by weight) Example 1 0.105 20 190 20 165 48 1 17.4 Good None A 9.8 Example 2 0.140 15 140 20 165 48 1 12.1 Good None A 8.5 Example 3 0.123 30 160 20 165 48 1 22.7 Good None A 9.3 Example 4 0.100 30 200 20 165 48 0.5 26.5 Good None A 7.7 Example 5 0.180 50 110 20 165 48 1 27.8 Good None B 8.1 Comparative " " " " " " 0 - Poor - B Example 1 Comparative 0.105 20 190 20 165 48 1 - Amorphous - C Example 2 Comparative 0.220 50 90 20 165 48 1 - Fairy Observed A Example 3 Comparative 0.070 15 290 20 165 48 1 - Amorphous - A Example 4 Referential Tracing experiment of Example 1 of Japanese 17.0 Good None 4.6 Example 1 Unexamined Patent Publication No. 56-160316 Referential Commercially available Zeolon 100Na 11.2 Good None 5.8 Example 2

Claims: CLAIMS 1. A high-silica mordenite which is a synthetic mordenite prepared without performing the dealuminization treatment, said mordenite being characterized in that the silica/alumina molar ratio is in the range of from 12 to 30 and the amount of benzene adsorption is 7 to 10% by weight as determined at a temperature of 250C under a vapor pressure of 35 mmHg. 2. A high-silica mordenite according to claim 1, wherein said mordenite has a composition expressed by the formula: xNa20 A1203 (12-30) SiO2 yH20 wherein x is about 1, y is 0 or a positive number. 3. A process for the preparation of a synthetic mordenite having a-silica/alumina molar ratio of from 12 to 30, which comprises preparing a reaction mixture having a composition represented by the following oxide molar ratios: Na2O/SiO2 = 0.08 - 0.2 SiO2/A1203 = 14 - 55 H20/Na2O = 100 - 300 and H2O/SiO2 = 10 - 40 by using synthetic amorphous silicic acid having an apparent specific gravity of from 0.05 to 0.45 g/ml as a silica source, and heating the reaction mixture at a temperature of 140 to 1800C with stirring to effect crystallization. 4. A process according to claim 3, wherein said synthetic amorphous silicic acid has an apparent specific gravity of from 0.10 to 0.35 g/ml. 5. A process according to claim 3 or 4, wherein an alumina source used for the preparation of said reaction mixture is at least one compound selected from the group consisting of aluminum oxide, aluminum hydroxide, sodium aluminate, aluminum sulfate and aluminum nitrate. 6. A process according to any one of claims 3 to 5, wherein said reaction mixture is prepared by incorporating the silica source into an aqueous solution of an alumina source and sodium hydroxide while the aqueous solution is stirred. 7. A process according to any one of claims 3 to 6, wherein said heating of the reaction mixture is carried out for a period of 20 to 150 hours. 8. A process according to any one of claims 3 to 6, wherein said heating of the reaction mixture is carried out at a temperature of 150 to 1700C for a period of 40 to 80 hours. 9. A process according to any one of claims 3 to 8, wherein said stirring of the reaction mixture carried out during heating for effecting crystallization is conducted under conditions such that the peripheral speed of a stirring vane defined by the formula: (n) (d) (v) 60 be at least 0.1 m/sec, wherein d is a maximum diameter (m) of the stirring vane during rotation and v is a stirring speed (rpm). 10. A process according to any one of claims 3 to 9, wherein the amount of water used for the preparation of the reaction mixture is such that the H2O/SiO2 molar ratio in the starting mixture be in the range of from 15 to 30.

Inventors: FUKUSHIMA, TOSHIHISA, IGAWA, KAZUSHIGE, ITABASHI, KEIJI
Applicants: TOYO SODA MANUFACTURING CO., LTD.
Application year: 1983
Main classification: C01B33
IPC codes: C01B39, B01J29, B01J20