Synthesis of alkyl tert-alkyl ethersusing clay catalysts

Abstract: Methyl tert-butyl ether is prepared from tertiary-butyl alcohol and methanol in one step by reaction of the TBA and methanol in the presence of a catalyst comprising a fluorosulfonic-acid modified montmorillonite clay at elevated temperature and moderate pressure.

Description: This invention concerns an improved process for preparing alkyl tertiary-alkyl ethers such as methyl tertiary-butyl ether (MTBE) by the reaction of tertiary alcohol such as tertiary-butanol and primary alcohol such as methanol in the presence of a catalyst comprising a fluorosulfonic acid-modified clay catalyst. The invention is particularly advantageous in that the reaction takes place in one-step and the catalyst exhibits no loss of activity even after up to 2000 hours of activity using crude methanol/t-butanol feedstocks. In addition this catalyst can accommodate higher temperatures than many of the other catalysts which have been proposed for MTBE production. Another desirable feature is that the product mix separates into an isobutylene-MTBE product-rich phase and a heavier aqueous methanol phase. Alkyl tertiary-alkyl ethers prepared by this invention, particularly MTBE, are useful as a blending component in high octane gasoline. It is known to those skilled in the art that ethers, including unsymmetrical ethers, may be prepared by reacting an alcohol with another alcohol to form the desired product. The reaction mixture, containing catalyst and/or condensing agent may be separated and further treated to permit attainment of the desired product. Such further treatment commonly includes one or more distillation operations. Methyl tert-butyl ether is finding increasing use as a blending component in high octane gasoline as the current gasoline additives based on lead and manganese are phased out. Currently all commercial processes for the manufacture of methyl tert-butyl ether are based upon the liquid-phase reaction of isobutylene and methanol (Eq. 1), catalyzed by a cationic ion-exchange resin (see, for example: Hydrocarbon Processing, Oct. 1984, p. 63; Oil and Gas J., Jan. 1, 1979, p. 76; Chem. Economics Handbook-SRI, Sept. 1986, p. 543-7051P). The cationic ion-exchange resins used in MTBE synthesis normally have the sulphonic acid functionality (see: J. Tejero, J. Mol. Catal., 42 (1987) 257; C. Subramamam et al., Can. J. Chem. Eng., 65 (1987) 613). With the expanding use of MTBE as an acceptable gasoline additive, a growing problem is the availability of raw materials. Historically, the critical raw material is isobutylene (Oil and Gas J., June 8, 1987, p. 55). It would be advantageous, therefore, to have a process to make MTBE that does not require isobutylene as a building block. It would be advantageous to have an efficient process for making MTBE by reaction of methanol with tertiary-butyl alcohol, since t-butanol (TBA) is readily available commercially through isobutane oxidation. In US-A-4,144,138 (1979) to Rao et al., there is disclosed a method for recovering methyl tertiary-butyl ether from etherification reaction effluent by azeotropic distillation to recover methanol-ether azeotrope overhead which is water-washed to give pure ether raffinate plus ether-methanol bottoms, the latter being azeotropically distilled to yield ether-methanol overhead which is recycled to water washing. The preparation of methyl tert-butyl ether from methyl and tert-butyl alcohols is discussed in S. V. Rozhkov et al., Prevrashch Uglevodorodov, Kislotno-Osnovn. Geterogennykh Katal. Tezisy Dokl. Vses Konf., 1977, 150 (C. A. 92:58165y). Here the TBA and methanol undergo etherification over KU-2 strongly acidic sulfopolystyrene cation-exchangers under mild conditions. This reference contains data on basic parameters of such a process. It is also pointed out that, although a plant for etherification over cation exchangers does not present any major problems, considerations include the fact that recycling large amounts of tert-butyl alcohol and methanol, as well as isobutylene, causes the scheme to be somewhat more expensive. Also, the progress of the reaction over cation exchangers is usually complicated by various adsorption and diffusion factors, by swelling phenomena, and by the variable distribution of the components between the solution and ion-exchanger phase. Furthermore, said acidic cation-exchangers with an organic (polystyrene or polymethacrylate) backbone generally have a very limited stability range with regard to operating temperatures, with temperatures above 120°C normally leading to irreversible destruction of the resin and loss of catalytic activity. In US-A-2,282,469 to Frolich there is disclosed a process for preparing methyl tertiary-butyl ether over a catalyst comprising Kieselguhr impregnated with phosphoric acid at a temperature of about 175°F to 350°F. . In an article titled "Catalysis: Selective Developments", Chem. Systems Report 84-3, 239-249, at section 3.4320, the unusual properties of smectite clays which make them of interest as catalysts are discussed. These compositions are layered and exhibit a 2:1 relationship between tetrahedral and octahedral sites. In addition the combination of cation exchange, intercalation and the fact that the distance between the layers can be adjusted provide interesting possibilities. There is a discussion of clay mineral catalysts, including "acid" montmorillonite clay catalysts in "Progress in Inorganic Chemistry", Vol. 35, p. 41 (1987). The process of pillaring this type of catalyst is discussed. Pillaring can convert a clay lamellar solid into a more heat resistant two dimensional zeolite material. GB-A-2,179,563 (1987) discloses the use of modified layered clay catalysts in reactions capable of catalysis by protons. Of particular interest in this invention were the three-layer sheet types, such as smectites, micas and vermiculites composed of successive layers of tetrahedral silica, octahedral alumina and tetrahedral silica which can exhibit swelling properties. US-A-4,590,294 discloses a process for the production of an ester comprising reacting an olefin from the group consisting of ethylene, hex-1-ene, hept-1-ene, oct-1-ene, 4-methylpent-1-ene, hex-2-ene, 1,5-hexadiene and cyclohexene with a carboxylic acid using as a catalyst component a hydrogen ion-exchanged layered clay. This reference would not seem to suggest a method for simultaneous dehydration of tert-butanol to isobutylene and the reaction with methanol to produce MTBE. In US-A-4,822,921, there is disclosed a method for producing MTBE by reacting tertiary-butyl alcohol and methanol in the presence of a catalyst comprising an inert support, such as titania, having a phosphoric acid impregnated thereon. US-A-4,827,048 discloses a method for producing MTBE by reacting tertiary-butyl alcohol and methanol in the presence of a catalyst comprising a heteropoly acid such as 12-tungstophosphoric acid or 12-molybdophosphoric acid on an inert support, such as titania. US-A-5081318 describes a one-step method for the synthesis of MTBE from t-butanol using a fluorosulfonic acid-modified zeolite catalyst. EP-A-0333078 discloses a method wherein t-butanol is reacted with methanol in a reaction zone in the presence of a catalyst to provide methy- tert -butyl ether in one-step which comprises using a catalyst selected from the group consisting of acidic aluminas, acidic silicas, or combinations thereof and zeolites containing alumina or silica, and acidic clay mineral catalysts. US-A-5059725 discloses a one-step synthesis for MTBE wherein t-butanol and methanol is reacted over a catalyst comprising ammonium sulfate or sulfuric acid deposited upon a Group IV oxide. In US-A-5300697 there is disclosed the use of a hydrogen fluoride-modified zeolite catalyst for the production of MTBE. Some of the catalysts described in the related art do not function well using higher temperatures. A number of these catalysts exhibit decreased performances when subject to crude feedstocks over extended periods of operation. It is an object of the present invention to selectively synthesize alkyl tertiary-alkyl ether such as methyl tertiary-butyl ether from tertiary alcohol, e.g. tertiary-butyl alcohol and primary alcohol, e.g. methanol in one step using a catalyst which can withstand high temperatures and which does not lose activity even after 2000 hours when subject to crude alcohol feedstocks. It has now been discovered that trifluoromethanesulfonic acid-modified montmorillonite clays can be used as catalysts for the selective synthesis of alkyl tertiary-alkyl ether from such alcohols. The accompanying examples demonstrate significantly higher isobutylene/MTBE yields using crude methanol/t-butanol feedstocks over extended periods than with other catalysts. In accordance with certain of its aspects, the present invention provides a method for preparing alkyl tertiary-alkyl ether from tertiary-alkyl alcohol and C 1 -C 6 primary alcohol in one-step which comprises reacting the tertiary-alkyl alcohol and primary alcohol in the presence of a catalyst comprising a trifluoromethanesulfonic acid-modified montmorillonite clay at an elevated temperature and moderate pressure. Most preferably, the invention provides a method for preparing methyl tert-butyl ether from tertiary-butyl alcohol and methanol by said process. The following description concentrates upon the reaction of methanol and tert-butyl alcohol to prepare MTBE. This important reaction does not restrict the scope of this invention. The preparation of MTBE can be represented by the following: Generally the methanol and t-butanol coreactants may be mixed in any proportion in order to generate the desired methyl t-butyl ether, but preferably the molar ratio of methanol to t-butanol in the feed mixture should be between 10:1 and 1:10, if the yield of desired MTBE is to be maximized. In order to achieve maximum selectivity to MTBE, and optimum conversion per pass, an excess of methanol in the liquid feed is desirable. The most preferred methanol-to-tertiary-butanol molar ratio is from 1:1 to 5:1. Optionally, said t-butanol plus methanol feed mixtures may be crude feedstocks containing other components, including water, ketones such as acetone, other alcohols such as 2-propanol, peroxides such as di-t-butyl peroxide, t-butyl hydroperoxide and allyl t-butyl peroxide, esters such as t-butyl formate, as well as methyl t-butyl ether product. In certain circumstances, it may be particularly desirable that the TBA conversion be high enough (e.g. >80% per pass), such that the crude product mix phase separates into an isobutylene-MTBE product-rich phase and a heavier aqueous methanol phase. Preferably such a product phase separation would be achieved at as low an etherification temperature as possible, but particularly in the range 160-200°C. The same process may also be applied to the preparation of other alkyl tertiary alkyl ethers. For example, said process may be applied to the reaction of a C 1 -C 6 primary alcohol such as methanol, ethanol, n-propanol and n-hexanol with a C 4 -C 10 tertiary alcohol such as, for example, tertiary-butanol and tertiary amyl alcohol. Reaction of methanol with tertiary amyl alcohol (2-methyl-2-butanol) would then yield methyl tertiary amyl ether (TAME). Alternatively a mixture of alcohols, e.g., a mixture of C 1 -C 5 alcohols, could be reacted to give a mixture of alkyl tert-alkyl ethers. Good results were realized using the trifluoromethanesulfonic acid-modified montmorillonite clays. Most preferred clays used to form this catalyst are silica-alumina clays. Chemically, clays are composed primarily of silicon, aluminum and oxygen, with minor amounts of magnesium and iron in some cases. Variations in the ratios of these constituents, and their crystal lattice configurations, result in some fifty separate clays, each with its own characteristic properties. Particularly effective in reaction (Eq. 2) are smectite clays. Smectite clays are discussed in the article cited in Chem. Systems Report, 84-3. These clays have small particle size and unusual intercalation properties which afford them high surface area. They are alumino silicates with a unique structure that permits modifications which provide useful catalysts. They comprise layered sheets of octahedral sites between sheets of tetrahedral sites, where the distance between the layers can be adjusted by swelling. This layering is illustrated in an article by F. Figueras, Catal. Rev.-Sci. Eng., 30 , 457 (1988). What renders the smectites of interest among the clay minerals is the combination of cation exchange, intercalation, and the fact that the distance between the layers can be adjusted by treatment with the appropriate solvent etc. The three layered sheet types include montmorillonite, vermiculite and some brittle mica. The idealized basic structure of clays of this type is that of a pyrophyllite which has the basic formula Si 8 Al 4 O 20 (OH) 4 . A general representation of the montmorillonite structure is: M x/n n+. yH 2 O(Al 4-x Mg x ) (Si 8 )O 20 (OH) 4 Where: M represents the interlamellar (balancing cations), normally sodium or lithium and x, y and n are integers. Said montmorillonite clays are best treated with fluorosulfonic acid as demonstrated in Example 1 or they can be pretreated with a mineral acid before the fluorosulfonic acid is added, as in Example 2. Mineral acids such as sulfuric acid and phosphoric acid activate montmorillonites by attacking and solubilizing structural cations in the octahedral layers. This opens up the clay structure and increases surface area. These acid-treated clays act as strong Bronsted acids. Where the montmorillonite clays are treated with a mineral acid, said clays should preferably have a residual acidity in the range 0.1 to 30 mg KOH/gm (titrated to phenolphthalein end point), a surface area of 10 to 1000 m 2 /gm, and a moisture content of up to 20 wt%. Illustrative examples include Engelhard Powdered Clay-113, having a residual acidity of 10 mg KOH/gm, surface area of 300 m 2 /gm and a moisture content of 4 wt%, Clay-13, having an acidity of 16 mg KOH/gm, a surface area of 300 m 2 /gm and a moisture content of 16 wt%, granular Clay-24, of particle size 20/60 mesh, having an acidity of 16 mg KOH/gm, a surface area of 300 m 2 /gm and a moisture content of 10 wt%, granular Clay-25, of particle size 10/20 mesh, having an acidity of 16 mg KOH/gm, a surface area of 400 m 2 /gm and a moisture content of 12 wt%, granular Clay-224, of particle size 20/60 mesh, having an acidity of 3.0 mg KOH/gm, a surface area of 350 m 2 /gm and a moisture content of <1 wt%, as well as extruded Clay-62, which may, for example, be in 0.15 or 0.5 cm diameter extrudates, and have acidity of about 3.0 mg KOH/gm, a surface area of 275 m 2 /gm and a moisture content of less than 1%. Most preferred are montmorillonite clays with a residual titratable acidity in the range of 1 to 20 mg KOH, a surface area of 100 to 500 m 2 /gm and a moisture content of <1%. Illustrative of such clays is Engelhard's Grade-224 clay in granular form. It has been discovered that fluorosulfonic acid-modified clays possess a number of improved properties for the production of MTBE. The acid useful for modifying the montmorillonite clay is trifluoromethanesulfonic acid (triflic acid). Examples 3, 4 and 5 demonstrate the effectiveness of trifluoromethanesulfonic acid. The performance of all such fluorosulfonic acid-modified clays in MTBE synthesis from t-butanol and methanol in one-step (Eq. 2) is illustrated by the accompanying examples. Said catalysts may be in the form of powders, pellets, granules, spheres, shapes and extrudates. The examples described herein demonstrate certain advantages using granules. The reaction may be carried out in either a stirred slurry reactor or in a fixed bed continuous flow reactor. The catalyst concentration should be sufficient to provide the desired catalytic effect. Etherification can generally be conducted at temperatures from 20° to 250°C; the preferred range is 80° to 200°C. The total operating pressure may be from 0 to 6895 kPa gauge pressure (gp) or higher. The preferred pressure range is 344 to 3440 kPa gp. Typically, MTBE is generated continuously in up to about 40 wt% concentration in the crude liquid product at total liquid hourly space velocities (LHSV) of up to 5 or higher and relatively mild conditions, where: LHSV = Volume Of Total Liquid Feed Run Through The Reactor Per Hour Volume of Catalyst In Reactor Conversions of t-butanol (TBA, wt%) are estimated in the following examples using the equation: (Wt% Conc. of TBA in Feed - Wt% Conc. of TBA in Product) Wt% Conc. of TBA in Feed x 100 Selectivities of methyl t-butyl ether (MTBE, mole %) and isobutylene (C 4 H 8 , mole%) are estimated from: Moles of MTBE (or C 4 H 8 ) in Product moles of TBA converted x 100 The examples which follow illustrate the one-step synthesis of MTBE from TBA and MeOH (Eq. 2) using fluorosulfonic acid-modified clays particularly in the form of granules. The following can be noted: a) In Example 3, the trifluoromethanesulfonic acid-modified montmorillonite clay of Example 1 gave MTBE in >40 wt% concentration when run at LHSV of 2 (e.g. Sample #1, Table 1) using a low MeOH/tBA molar feed ratio of 1.1:1. Under these conditions the tBA conversion is 68% at 120°C, but 91% at 160°C. At 160°C the crude product effluent is surprisingly separated into an isobutylene-MTBE rich phase and a heavier aqueous methanol phase. b) In Example 4, the trifluoromethanesulfonic acid-modified clay that had been previously treated with sulfuric acid (Example 2) gave tBA conversions of 89% and about 94% at 160° and 180°C operating temperature, respectively, and unexpected product phase separation at both temperatures (see Table 2). c) In Example 5, a 0.1% trifluoromethanesulfonic acid on montmorillonite clay catalyst provided excellent etherification activity over 84 days (+2000 hours) of operating time when using a crude tBA/MeOH feedstock also containing water, MTBE, isopropanol, acetone, di-t-butyl peroxide and t-butyl formate (see Table 3). d) The same catalyst as used in Example 5 gave good performance over a range of operating temperatures (see Example 6) and again product phase separation at 160°-180°C (Table 4) was observed. e) In comparative Example A, the unmodified montmorillonite clay gave low MTBE concentrations in the product effluent and only 25% tBA conversion per pass at 160°C (Sample #6, Table 5). EXAMPLE 1 This example illustrates the preparation of a trifluoromethanesulfonic acid-modified clay. To 85g of a neutral montmorillonite clay (Engelhard Grade 2C powder, dried at 175°C in vacuo) was added a solution of trifluoromethanesulfonic acid (10.0g) in dried acetone (100cc). The mixture was stirred for 24 hours under a nitrogen blanket, filtered and the solids washed first with acetone and water, then dried in vacuo at 40°C overnight and at 150°C for 4 hours. The recovered pale yellow powder was found to contain by analysis: H 2 O = 0.73% Acidity = 11 mg KOH/gm EXAMPLE 2 The example illustrates the preparation of another trifluoromethanesulfonic acid-modified montmorillonite clay. To 100g of a sulfuric acid-treated montmorillonite clay (Engelhard Grade 224 granules, dried at 175°C in vacuo) was added a solution of trifluoromethanesulfonic acid (10.0g) in dried acetone (100cc). The mixture was stirred for 24 hours under a nitrogen blanket, filtered and the solids washed first with acetone and water, then dried in vacuo at 40°C overnight and at 150°C for 4 hours. The recovered brown granules were found to contain by analysis. H 2 O = 1.76% Acidity = 3 mg KOH/gm EXAMPLE III This example illustrates the production of methyl t-butyl ether from t-butanol and methanol using a trifluoromethanesulfonic acid-modified montmorillonite clay. Synthesis was conducted in a tubular reactor 13mm int.diam. 304mm long), constructed of 316ss, operated upflow and mounted in a furnace controllable to ±1.0°C and fitted with pumps allowing flow control to <±1cc/hr. The reactor was also fitted with a pressure regulating device and equipment for monitoring temperature, pressure and flow rate (ss = stainless steel grade). The reactor was charged at the beginning of the experiment with 25cc triflic acid-modified clay powder prepared by the method of Example 1. A screen of glass wool was placed at the top and bottom of the reactor, to ensure the catalyst would remain in the middle portion. The catalyst bed was treated with a methanol/t-butanol (1.1:1 molar mix) upflow, at a flow rate of 50 cc/hr, while the reactor was held at 120°C, with a total pressure of 2070 kPa. Samples of crude product effluent were collected periodically on-stream, in 316 ss bombs and analyzed by glc and gc-ir. Typically analyses data for samples taken under these conditions are summarized in Table 1. Performance at a series of other temperatures (140°, 160° and 180°C) was determined using the same procedure. These results are also given in Table 1. Of note, conversion levels and isobutylene/MTBE selectivities at 120°C and 160°C are as follows: Sample Operating Temp(°C) TBA Conv.(%) Molar Selectivity (%) C 4 H 8 MTBE 1 120 68 21 77 5 160 91 EXAMPLE 4 This Example illustrates the performance of another trifluoromethanesulfonic acid-modified montmorillonite clay in the production of methyl t-butyl ether from t-butanol and methanol. Using the equipment and procedures of Example 3, 25 cc of the trifluoromethanesulfonic acid-modified clay of Example 2 was charged to the reactor system and performance was monitored over a series of operating temperatures (120°, 140°, 160° and 180°C) and tBA/MeOH (1.1:1) feed rates (LHSV = 2-5). The results are summarized in Table 2. Calculated tBA conversion and C 4 H 8 /MTBE selectivities for typical samples are as follows: Sample Operating Temp(°C) TBA Conv.(%) Molar Selectivity (%) C 4 H 8 MTBE 3 140 72 35 63 5 160 89 EXAMPLE 5 This example illustrates the performance of a ;, trifluoromethanesulfonic acid-modified clay in the production of methyl t-butyl ether from a crude t-butanol/methanol feedstock over an extended period. Using the equipment and procedures of Example 3, 25cc of a 0.1% triflic acid-modified montmorillonite clay was charged to the reactor system and performance was monitored over 84 days at 120°C using a crude feed mix comprising t-butanol, methanol, water, MTBE, acetone (Me 2 CO), isopropanol (2-PrOH), di-t-butyl peroxide (DTBP) and t-butyl formate (TBF). The tBA/MeOH molar feed ratio was 1:2, the feed rate was maintained at 50 cc/hr. The results are summarized in Table 3. Calculated tBA conversions and C 4 H 8 /MTBE selectivities for typical samples are as follows: Molar Selectivity (%) Sample Time On Stream (Days) TBA Conv.(%) C 4 H 8 MTBE 2 4 71 15 83 8 25 67 16 85 11 35 64 16 83 13 42 69 14 86 19 84 68 14 84 EXAMPLE 6 Using the equipment and procedures of Example 3, 25cc of a 0.1% triflic acid-modified montmorillonite clay was charged to the reactor system and performance was monitored over a series of operating temperatures (120°, 140°, 160° and 180°C). Results are summarized in Table 4. Calculated tBA conversion and C 4 H 8 /MTBE selectivities for typical samples are as follows: Molar Selectivity (%) Sample Operating Temp(°C) TBA Conv.(%) C 4 H 8 MTB 2 120 71 21 74 5 160 91 COMPARATIVE EXAMPLE A This comparative example illustrates the performance of unmodified montmorillonite clay in the production of methyl t-butyl ether from t-butanol and methanol. Using the equipment and procedures of Example 3, 25cc of untreated montmorillonite clay (Engelhard Grade 2C clay powder) was charged to this reactor system and performance was monitored over a series of temperatures (120°, 140°, 160° and 180°C). The tBA/MeOH (1:1.1) feed rate was maintained at 50 cc/hr. The results are summarized in Table 5. Calculated tBA conversion and C 4 H 8 /MTBE selectivities for Sample 2 and 6 are as follows: Molar Selectivity (%) Sample Operating Temp(°C) TBA Conv.(%) C 4 H 8 MTB 2 120 <1 - - 6 160 25 34 63

Claims: A process for the preparation of alkyl tertiary alkylether from tertiary alcohol and primary alcohol in the presence of a catalyst, characterized in that montmorillonite clay modified with trifluoromethanesulfonic acid is used as a catalyst. A process according to Claim 1 for the preparation of methyl tert-butyl ether from t-butanol and methanol. A method as claimed in Claim 2, wherein said t-butanol and methanol are present in a molar amount of 0.1 to 10 moles of methanol per mole of t-butanol. A method as claimed in Claim 2 or 3, wherein said t-butanol and methanol are continuously contacted with said catalyst at a temperature of 20°C to 250°C and a pressure of atmospheric to 6895 KPa gauge pressure to obtain methyl tert-butyl ether. A method as claimed in any one of Claims 1 to 4, wherein the montmorillonite clay is pre-treated with a sulfuric or phosphoric acid. A method as claimed in Claim 5, wherein the sulfuric acid or phosphoric acid-treated clay has a residual acidity in the range 0.1 to 30 mg KOH/gm. A method as claimed in any one of Claims 2 to 6, wherein the operating temperature is in the range 160°C to 200°C and the product comprises a two-phase mix of an isobutylene-MTBE product-rich phase and a heavier aqueous methanol-rich phase. A method as claimed in any one of Claims 1 to 7, wherein said montmorillonite clay has the structure: M x/n n+. yH 2 O(Al 4-x Mg x ) (Si 8 )O 20 (OH) 4 where: M represents the interlamellar balancing cations, and x, y and n are integers. The use of modified montmorillonite clay in a method of reacting t-butanol with methanol according to Claim 2.

Inventors: KNIFTON JOHN FREDERICK, SHEU Y-HWA EDWARD, KNIFTON, JOHN FREDERICK, SHEU, Y-HWA EDWARD
Applicants: HUNTSMAN SPEC CHEM CORP, HUNTSMAN SPECIALTY CHEMICALS CORPORATION
Application year: 1992
Main classification: C07C43
IPC codes: C07C43, C07C41, C07B61, B01J31