Patent Application
20160296921
The present invention is directed to a process for the production of a catalyst composition, such catalyst composition and the use of such catalyst composition for the production of styrene.
Current major commercial process practiced globally for styrene production is through catalytic dehydrogenation of ethylbenzene. This is a very mature technology and a large part of the world's styrene capacity is produced through this route. The starting material ethylbenzene is produced through alkylation reaction between high purity benzene and ethylene and they make up a very large part of styrene's cost of production.
There are a few developing routes for styrene production, of which alkylation of toluene with methanol in presence of a basic catalyst seems to be attractive as both toluene and methanol are much cheaper than the usual feedstock benzene and ethylene. However, in this alternative route selectivity towards styrene was reported to be not so high and ethylbenzene was reported to be the major product.
The alkylation of the side chain of toluene with methanol or formaldehyde by contact of these reactants with X- or Y-type zeolites is described in Yashima et al in the Journal of Catalysis, Vol. 26, 303-312 (1972). More specifically, it is disclosed therein that alkylation of the methyl group of toluene to form styrene and ethylbenzene is effected by Na, K, Rb or Cs exchanged X- or Y-type zeolites, whereas Li exchanged zeolites of the same type effected predominantly alkylation of the benzene ring of toluene to form xylenes. Yashima et al interpret their results as suggesting that xylene formation is attributable to the acidity of the catalyst, whereas styrene and ethylbenzene formation is attributable to the basicity of the catalyst. The problem with this process is the low selectivity towards styrene.
JP57-68144 is directed to catalyst for styrene synthesis which comprises a zeolite of the faujasite class having at least 20% of the sodium cations present therein exchanged with cesium, potassium or rubidium and which has been treated to impregnate therein one or more divalent or trivalent metal salts of boric or phosphoric acid, the metal of said salt disclosed as being selected from magnesium, calcium, aluminum, manganese, iron, cobalt, nickel, copper and zinc.
U.S. Pat. No. 4,483,936 describes a catalyst composition capable of catalyzing the side chain alkylation of toluene with methanol comprising a crystalline aluminosilicate zeolite of the faujasite structure having present therein (1) at least one alkali metal selected from the group consisting of Cs, K, and Rb; (2) at least one metal selected from the Group of M metals consisting of Mn, Fe, Cu, and Zn; and (3) at least one member selected from the group consisting of boron and phosphorus.
It is an objective of the present invention to provide a catalyst composition for toluene production with an improved selectivity.
Accordingly, the present invention provides a process for the preparation of a catalyst composition comprising the steps of:
It was found that the production process of styrene from toluene using the catalyst composition obtained according to the process of the invention shows a surprisingly high selectivity towards styrene.
In step A), a salt of boric acid or phosphoric acid and a bivalent or trivalent metal is prepared.
The phosphoric acid and boric acid which forms the salt may be of any suitable form. As the phosphoric acid, orthophosphoric acid, pyrophosphoric acid, metaphosphoric acid, etc. may be used, orthophosphoric acid being most preferred. As the boric acid, orthoboric acid, metaboric etc. may be used, orthoboric acid being most preferred. The salt of step A) is preferably a borate of the bivalent or trivalent metal.
The bivalent or trivalent metal which forms the salt is preferably selected from the group consisting of magnesium, calcium, aluminum, chromium, manganese, iron, cobalt, nickel, copper, zinc, lanthanum, cerium and zirconium. Most preferably, the bivalent or trivalent metal is cobalt.
The following are preferred examples of the salt: magnesium borate, calcium borate, aluminum borate, chromium borate, manganese borate, iron borate, cobalt borate, nickel borate, copper borate, zinc borate, magnesium phosphate, calcium phosphate, aluminum phosphate, chromium phosphate, manganese phosphate, iron phosphate, cobalt phosphate, nickel phosphate, copper phosphate and zinc phosphate. These metal salts may also be used by mixing two or more types. Preferably, the metal salt is or comprises cobalt borate.
In sub-step A1), a borate or a phosphate of an alkali metal and a water soluble salt of the bivalent or trivalent metal are mixed to obtain a suspension. Preferably, the borate or the phosphate of the alkali metal of sub-step A1) comprises disodium tetraborate. The water soluble salt of the bivalent or trivalent metal may be any suitable salt, but preferably is an acetate.
The pH of the suspension obtained by sub-step A1) is adjusted to 7.0-11.5 by the addition of an alkaline solution. It was found that this range of pH resulted in a catalyst composition with a high selectivity towards styrene. More preferably, the pH is adjusted to 8.0-10.5, which results in an even higher selectivity towards styrene. Even more preferably, the pH is adjusted to 8.5-9.5 or 8.8-9.2.
The alkaline solution may be of any type, including alkali hydroxides such as sodium hydroxide.
The solution obtained by sub-step A2) is mixed until the salt is obtained, for example by stirring the solution for 5-6 hours. The obtained salt may be filtered, washed and dried.
The salt obtained by step A) is mixed with a crystalline aluminosilicate zeolite of the faujasite structure with SiO2/Al2O3 mole ratio in the range of about 2 to about 8 and including potassium, rubidium or cesium cations or combinations thereof.
The zeolite used in the present invention preferably has a molar ratio of SiO2/Al2O3 within the range of approximately 2:1 and approximately 8:1, exemplified by synthesized faujasite referred to as type X and type Y. An example of the type X and type Y faujasite is, respectively:
The zeolite is preferably type X, in particular 13X zeolite.
The method for replacing some or most sodium ions in zeolite with potassium, rubidium or cesium cations is well known, as described e.g. in U.S. Pat. No. 4,115,424. The following is given as one example:
Cesium hydroxide (CsOH) aqueous solution (125 g CsOH dissolved in 1650 ml water) is added to 75 g type X zeolite (for example, molecular sieve Na13X) in several batches and ion exchange is carried out for 10 to 48 hours while heating at 80 to 90° C. Subsequently, the zeolite treated with ion-exchange is washed well with water and dried for a day in a dryer at 130 to 150° C. The zeolite obtained in this manner generally has 10 to 50% of the sodium ions thereof replaced by cesium ions.
Preferably, the ion exchanged zeolite includes cesium cations.
The weight ratio between the metal salt obtained in step A) and the zeolite which are mixed in step B) is typically between 1:100 and 30:100, preferably between 5:100 and 25:100.
There are no particular restrictions with regards to the method for mixing the metal salt and the ion-exchanged zeolite. For example, the ion-exchanged zeolite may be mixed with a solution of the metal salt or a suspension of the metal salt. Preferably, the metal salt and the ion-exchanged zeolite are mixed in a dry state e.g. in a mortar. Subsequently, the mixture may be calcined at e.g. 400 to 550° C. for e.g. 2 to 4 hours prior to using this for a styrene synthesis reaction.
In particularly preferred embodiments, step A) comprises the sub-steps of
The present invention further provides the catalyst composition obtainable by the process according to the invention.
The present invention further provides a process for the production of styrene comprising reacting toluene and an agent selected from methanol and formaldehyde and mixtures thereof at an elevated reaction temperature in the presence of the catalyst composition according to the invention. Preferably, the agent is methanol.
The production of styrene is carried out by a gaseous mixture of toluene and methanol and/or formaldehyde passing through the catalyst zone under thermal conditions. The reaction is preferably conducted at gaseous hourly space velocity of 10-1500 hr−1, preferably 15-100 hr−1.
The reaction may be carried out at a molar ratio between toluene and methanol and/or formaldehyde of 1:1, but is preferably carried out at an excess of toluene over methanol and/or formaldehyde. The molar ratio between toluene and the agent selected from methanol and formaldehyde and mixtures thereof may preferably be 1:1 to 20:1, preferably 2:1 to 10:1.
The temperature at which the gaseous mixture contacts the catalyst is preferably within a range of 350 to 500° C., more preferably between 400 to 475° C. Other reaction conditions may be determined according to known methods.
According to a further aspect, the present invention provides use of the catalyst composition according to the invention for the production of styrene, preferably from toluene and methanol and/or formaldehyde.
Although the invention has been described in detail for purposes of illustration, it is understood that such detail is solely for that purpose and variations can be made therein by those skilled in the art without departing from the spirit and scope of the invention as defined in the claims.
It is further noted that the invention relates to all possible combinations of features described herein, preferred in particular are those combinations of features that are present in the claims.
It is further noted that the term ‘comprising’ does not exclude the presence of other elements. However, it is also to be understood that a description on a product comprising certain components also discloses a product consisting of these components. Similarly, it is also to be understood that a description on a process comprising certain steps also discloses a process consisting of these steps.
The invention is now elucidated by way of the following examples, without however being limited thereto.
Cesium exchanged 13X zeolite (Cs-13X) was prepared by multiple exchange of parent zeolite with cesium hydroxide solution. About 20 g of 13X zeolite in sodium form was suspended in a 300 mL solution (75 g cesium hydroxide/Liter water) and stirred at 100° C. for 2 hrs. The solid was filtered, dried and re-suspended again in 300 mL solution of cesium hydroxide and stirred for another 3 hrs. The process was repeated again with the remaining 400 mL of the solution and stirring continued overnight. Finally, the solid was filtered, washed and dried at 110° C.
Cobalt borate was prepared as follows: To a 500 mL 0.3M solution of di-sodium tetra-borate a solution of cobalt acetate (0.3M, 500 mL) was added drop-wise at room temperature with constant stirring to get a pink suspension. To this a solution of sodium hydroxide (15 g in 40 mL water) was added drop-wise till pH of the resultant solution reached 9. The mixture was stirred for 5-6 hours and the solid was filtered, washed and dried at 120° C. for overnight.
The final catalyst was prepared by grinding of 10 g Cs-13X zeolite and 2 g of Cobalt borate in dry state in a mortar. The mixture was calcined at 500° C. for 3 hours.
The reaction of toluene and methanol was carried out in a down flow fixed bed reactor. Typically 2 g of final catalyst was well mixed with alpha-alumina (1:1 w/w) and loaded in the reactor. The catalyst was pretreated for 2 hours at 375° C. in flowing nitrogen after which reactants (toluene and methanol 5:1 molar ratio) were introduced with a liquid feed pump. Typical liquid feed rate was 9.6 mL/h. Nitrogen flow was about 50 mL/min. The reaction temperature was varied from 375-425° C. The feed and reaction products were analyzed by on-line gas chromatograph. The result is given in Table 1.
Example 1 was repeated but cobalt borate was prepared at pH of 11 instead of 9. The result is given in Table 1.
Example 1 was repeated but Cs-13X was used as the catalyst in the reaction of toluene and methanol. The result is given in Table 1.
Example 1 was repeated but Cesium and boron exchanged 13X zeolite (Cs-B-13X) was used as the catalyst in the reaction of toluene and methanol. The result is given in Table 1.
Cs-B-13X was prepared by multiple exchange of parent zeolite with a solution of cesium hydroxide and boric acid. About 20 g of 13X zeolite in sodium form was suspended in a 300 mL solution (75 g cesium hydroxide +55 g boric acid/Liter water) and stirred at 100° C. for 2 hrs. The solid was filtered, dried and re-suspended again in 300 mL solution of cesium hydroxide and stirred for another 3 hrs. The process was repeated again with the remaining 400 mL of the solution and stirring continued overnight. Finally, the solid was filtered, washed, dried at 110° C. and then calcined at 500° C. for 3 hours.
In presence of all catalysts listed in Table 1 toluene reacts with methanol at 375° C. to give styrene and ethylbenzene. However, selectivity to styrene was different. While Cs-13X showed only 12% styrene selectivity (CEx A), this was improved to 41% with the incorporation of boron but about 30% C1-C2 light fractions were also produced (CEx B). On the other hand, incorporation of Co-borate improved styrene selectivity significantly to 54.2% (Ex 2) or 85% (Ex 1). No other by-products like benzene or xylenes were detected.
It can be seen from Table 1 that cobalt borate samples prepared at a pH 9 showed higher styrene selectivity than samples prepared at pH 11. Further, the ethylbenzene selectivity is also low at 14.6% at pH 9 compared to 37.0% at pH 11. This shows that incorporation of cobalt borate to Cs-13X improved styrene selectivity and styrene yield in a significant way with minimal formation of ethylbenzene by the use of appropriate pH during the preparation of cobalt borate. Formation of larger quantities of ethylbenzene requires further dehydrogenation at around 600-650° C. to obtain styrene. Thus, a catalyst which results in higher amounts of styrene with minimum ethylbenzene formation is most desirable.
Excess toluene and unreacted methanol can be recycled back to the reactor. The catalyst showed little deactivation and was found to be quite stable till 10-12 hours of time on stream.
| Number | Date | Country | Kind |
|---|---|---|---|
| 13195426.5 | Dec 2013 | EP | regional |
| Filing Document | Filing Date | Country | Kind |
|---|---|---|---|
| PCT/EP2014/076975 | 12/9/2014 | WO | 00 |
