Patent Application
20090030239
The present invention relates to a process for making butenes using aqueous isobutanol as a reactant.
Butenes are useful intermediates for the production of linear low density polyethylene (LLDPE) and high density polyethylene (HDPE), as well as for the production of transportation fuels and fuel additives. The production of butenes from butanol is known, however the dehydration of butanol to butenes results in the formation of water, and thus these reactions have historically been carried out in the absence of water. Aiouache, F., and Goto, S. (J. Chem. Engr. of Japan (2002) 35:443-449 discuss the dehydration of 2-methyl-1-butanol to isoamylenes, and the strong inhibition thereof by water.
Efforts directed at improving air quality and increasing energy production from renewable resources have resulted in renewed interest in alternative fuels, such as ethanol and butanol, that might replace gasoline and diesel fuel. Efforts are currently underway to increase the efficiency of isobutanol production by fermentative microorganisms with the expectation that renewable feedstocks, such as corn waste and sugar cane bagasse, could be used as carbon sources. It would be desirable to be able to utilize such isobutanol streams for the production of butenes, and for the further production of fuel additives from said butenes.
The present invention relates to a process for making at least one butene comprising contacting a reactant comprising isobutanol and at least about 5% water (by weight relative to the weight of the water plus isobutanol) with at least one acid catalyst at a temperature of about 50 degrees C. to about 450 degrees C. and a pressure from about 0.1 MPa to about 20.7 MPa to produce a reaction product comprising said at least one butene, and recovering said at least one butene from said reaction product to obtain at least one recovered butene. In one embodiment, the reactant is obtained from fermentation broth.
The at least one recovered butene is useful as an intermediate for the production of transportation fuels and fuel additives. In particular, the at least one recovered butene can be converted to isoalkanes, C10 to C13 alkyl substituted aromatic compounds, and butyl alkyl ethers. In addition, the at least one recovered butene can be converted to isooctenes, which can further be converted to additional useful fuel additives, such as isooctanes, isooctanols or isooctyl alkyl ethers.
The Drawing consists of seven figures.
The present invention relates to a process for making at least one butene from a reactant comprising water and isobutanol. The at least one butene so produced is useful as an intermediate for the production of transportation fuels, wherein transportation fuels include, but are not limited to, gasoline, diesel fuel and jet fuel. The present invention further relates to the production of transportation fuel additives using butenes produced by the process of the invention.
In its broadest embodiment, the process of the invention comprises contacting a reactant comprising isobutanol and water with at least one acid catalyst to produce a reaction product comprising at least one butene, and recovering said at least one butene from said reaction product to obtain at least one recovered butene. The term “butene” includes 1-butene, isobutene, and/or cis and trans 2-butene.
Although the reactant could comprise less than about 5% water by weight relative to the weight of the water plus isobutanol, it is preferred that the reactant comprise at least about 5% water. In a more specific embodiment, the reactant comprises from about 5% to about 80% water by weight relative to the weight of the water plus isobutanol.
In one preferred embodiment, the reactant is derived from fermentation broth, and comprises at least about 50% isobutanol (by weight relative to the weight of the isobutanol plus water) (sometimes referred to herein as “aqueous isobutanol”). One advantage to the microbial (fermentative) production of isobutanol is the ability to utilize feedstocks derived from renewable sources, such as corn stalks, corn cobs, sugar cane, sugar beets or wheat, for the fermentation process. Efforts are currently underway to engineer (through recombinant means) or select for organisms that produce isobutanol with greater efficiency than is obtained with current microorganisms. Such efforts are expected to be successful, and the process of the present invention will be applicable to any fermentation process that produces isobutanol at levels currently seen with wild-type microorganisms, or with genetically modified microorganisms from which enhanced production of isobutanol is obtained.
Isobutanol can be fermentatively produced by recombinant microorganisms as described in copending and commonly owned U.S. Patent Application No. 60/730,290, page 5, line 9 through page 45, line 20, including the sequence listing. The biosynthetic pathway enables recombinant organisms to produce a fermentation product comprising isobutanol from a substrate such as glucose; in addition to isobutanol, ethanol is formed. The biosynthetic pathway enables recombinant organisms to produce isobutanol from a substrate such as glucose. The biosynthetic pathway to isobutanol comprises the following substrate to product conversions:
The biological production of butanol by microorganisms is believed to be limited by butanol toxicity to the host organism. Copending and commonly owned application docket number CL-3423, page 5, line 1 through page 36, Table 5, and including the sequence listing (filed 4 May 2006) enables a method for selecting for microorganisms having enhanced tolerance to butanol, wherein “butanol” refers to 1-butanol, 2-butanol, isobutanol or combinations thereof. A method is provided for the isolation of a butanol tolerant microorganism comprising:
Fermentation methodology is well known in the art, and can be carried out in a batch-wise, continuous or semi-continuous manner. As is well known to those skilled in the art, the concentration of isobutanol in the fermentation broth produced by any process will depend on the microbial strain and the conditions, such as temperature, growth medium, mixing and substrate, under which the microorganism is grown.
Following fermentation, the fermentation broth from the fermentor can be used for the process of the invention. In one preferred embodiment the fermentation broth is subjected to a refining process to produce an aqueous stream comprising an enriched concentration of isobutanol. By “refining process” is meant a process comprising one unit operation or a series of unit operations that allows for the purification of an impure aqueous stream comprising isobutanol to yield an aqueous stream comprising substantially pure isobutanol. For example, in one embodiment, the refining process yields a stream that comprises at least about 5% water and isobutanol, but is substantially free of ethanol that may have been present in the fermentation broth.
Refining processes typically utilize one or more distillation steps as a means for recovering a fermentation product. It is expected, however, that fermentative processes will produce isobutanol at very low concentrations relative to the concentration of water in the fermentation broth. This can lead to large capital and energy expenditures to recover the isobutanol by distillation alone. As such, other techniques can be used either alone or in combination with distillation as a means of concentrating the dilute isobutanol product. In such processes where separation techniques are integrated with the fermentation step, cells are often removed from the stream to be refined by centrifugation or membrane separation techniques, yielding a clarified fermentation broth. These cells are then returned to the fermentor to improve the productivity of the isobutanol fermentation process. The clarified fermentation broth is then subjected to such techniques as pervaporation, gas stripping, liquid-liquid extraction, perstraction, adsorption, distillation, or combinations thereof. Depending on product mix, these techniques can provide a stream comprising water and isobutanol suitable for use in the process of the invention. If further purification is necessary, the stream can be treated further by distillation to yield an aqueous isobutanol stream.
1-Butanol and isobutanol share many common features that allow the separation schemes devised for the separation of 1-butanol and water to be applicable to the isobutanol and water system. For instance both 1-butanol and isobutanol are equally hydrophobic molecules possessing log Kow coefficients of 0.88 and 0.83, respectively. Kow is the partition coefficient of a species at equilibrium in an octanol-water system. Based on the similarities of the hydrophobic nature of the two molecules one would expect both molecules to partition in largely the same manner when exposed to various solvent systems such as decanol or when adsorbed onto various solid phases such as silicone or silicalite. In addition, both 1-butanol and isobutanol share similar K values, or vapor-liquid partition coefficients, when in solution with water. Another useful thermodynamic term is α which is the ratio of partition coefficients, K values, for a given binary system. For a given concentration and temperature up to 100° C. the values for K and α are nearly identical for 1-butanol and isobutanol in their respective butanol-water systems, indicating that in evaporation type separation schemes such as gas stripping, pervaporation, and distillation, both molecules should perform equivalently.
The separation of 1-butanol from water, and the separation of 1-butanol from a mixture of acetone, ethanol, 1-butanol and water as part of the ABE fermentation process by distillation have been described. In particular, in a butanol and water system, 1-butanol forms a low boiling heterogeneous azeotrope in equilibrium with 2 liquid phases comprised of 1-butanol and water. This azeotrope is formed at a vapor phase composition of approximately 58% by weight 1-butanol (relative to the weight of water plus 1-butanol) when the system is at atmospheric pressure (as described by Doherty, M. F. and Malone, M. F. in Conceptual Design of Distillation Systems (2001), Chapter 8, pages 365-366, McGraw-Hill, New York). The liquid phases are roughly 6% by weight 1-butanol (relative to the weight of water plus 1-butanol) and 80% by weight 1-butanol (relative to the weight of water plus 1-butanol), respectively. In similar fashion, isobutanol also forms a minimum boiling heterogeneous azeotrope with water that is in equilibrium with two liquid phases. The azeotrope is formed at a vapor phase composition of 67% by weight isobutanol (relative to the weight of water plus isobutanol) (as described by Doherty, M. F. and Malone, M. F. in Conceptual Design of Distillation Systems (2001), Chapter 8, pages 365-366, McGraw-Hill, New York). The two liquid phases are roughly 6% by weight isobutanol (relative to the weight of water plus isobutanol) and 80% by weight isobutanol (relative to the weight of water plus isobutanol), respectively. Thus, in the process of distillative separation of a dilute 1-butanol and water or isobutanol and water system, a simple procedure of sub-cooling the azeotrope composition into the two phase region allows one to cross the distillation boundary formed by the azeotrope.
For fermentation processes in which isobutanol is the predominant alcohol of the fermentation broth, the aqueous isobutanol can be recovered by azeotropic distillation, as described generally in Ramey, D. and Yang, S.-T. (Production of butyric acid and butanol from biomass, Final Report of work performed under U.S. Department of Energy DE-F-G02-00ER86106, pages 57-58) for the production of 1-butanol. An aqueous isobutanol stream from the fermentation broth is fed to a distillation column, from which an isobutanol-water azeotrope is removed as a vapor phase. The vapor phase from the distillation column (comprising at least about 33% water (by weight relative to the weight of water plus isobutanol)) can then be used directly as the reactant for the process of the present invention, or can be fed to a condenser. Upon cooling, an isobutanol-rich phase (comprising at least about 16% water (by weight relative to the weight of water plus isobutanol)) will separate from a water-rich phase in the condenser. One skilled in the art will know that solubility is a function of temperature, and that the actual concentration of water in the aqueous isobutanol stream will vary with temperature. The isobutanol-rich phase can be decanted and used for the process of the invention, and the water-rich phase preferably is returned to the distillation column.
For fermentation processes in which an aqueous stream comprising isobutanol and ethanol are produced, the aqueous isobutanol/ethanol stream is fed to a distillation column, from which a ternary isobutanol/ethanol/water azeotrope is removed. The azeotrope of isobutanol, ethanol and water is fed to a second distillation column from which an ethanol/water azeotrope is removed as an overhead stream. A stream comprising isobutanol, water and some ethanol is then cooled and fed to a decanter to form an isobutanol-rich phase and a water-rich phase. The isobutanol-rich phase is fed to a third distillation column to separate an isobutanol/water stream from an ethanol/water stream. The isobutanol/water stream can be used for the process of the invention.
Generally, there are two steps involved in the removal of volatile components by pervaporation. One is the sorption of the volatile component into the membrane, and the other is the diffusion of the volatile component through the membrane due to a concentration gradient. The concentration gradient is created either by a vacuum applied to the opposite side of the membrane or through the use of a sweep gas, such as air or carbon dioxide, also applied along the backside of the membrane. Pervaporation for the separation of 1-butanol from a fermentation broth has been described by Meagher, M. M., et al in U.S. Pat. No. 5,755,967 (Column 5, line 20 through Column 20, line 59) and by Liu, F., et al (Separation and Purification Technology (2005) 42:273-282). According to U.S. Pat. No. 5,755,967, acetone and/or 1-butanol were selectively removed from an ABE fermentation broth using a pervaporation membrane comprising silicalite particles embedded in a polymer matrix. Examples of polymers include polydimethylsiloxane and cellulose acetate, and vacuum was used as the means to create the concentration gradient. The method of U.S. Pat. No. 5,755,967 can similarly be used to recover a stream comprising isobutanol and water from fermentation broth, and this stream can be used directly as the reactant of the present invention, or can be further treated by distillation to produce an aqueous isobutanol stream that can be used as the reactant of the present invention.
In general, gas stripping refers to the removal of volatile compounds, such as butanol, from fermentation broth by passing a flow of stripping gas, such as carbon dioxide, helium, hydrogen, nitrogen, or mixtures thereof, through the fermentor culture or through an external stripping column to form an enriched stripping gas. Gas stripping to remove 1-butanol from an ABE fermentation has been exemplified by Ezeji, T., et al (U.S. Patent Application No. 2005/0089979, paragraphs 16 through 84). According to U.S. 2005/0089979, a stripping gas (carbon dioxide and hydrogen) was fed into a fermentor via a sparger. The flow rate of the stripping gas through the fermentor was controlled to give the desired level of solvent removal. The flow rate of the stripping gas is dependent on such factors as configuration of the system, cell concentration and solvent concentration in the fermentor. This process can also be used to produce an enriched stripping gas comprising isobutanol and water, and this stream can be used directly as the reactant of the present invention, or can be further treated by distillation to produce an aqueous isobutanol stream that can be used as the reactant of the present invention.
Using adsorption, organic compounds of interest are removed from dilute aqueous solutions by selective sorption of the organic compound by a sorbant, such as a resin. Feldman, J. in U.S. Pat. No. 4,450,294 (Column 3, line 45 through Column 9, line 40 (Example 6)) describes the recovery of an oxygenated organic compound from a dilute aqueous solution with a cross-linked polyvinylpyridine resin or nuclear substituted derivative thereof. Suitable oxygenated organic compounds included ethanol, acetone, acetic acid, butyric acid, n-propanol and n-butanol. The adsorbed compound was desorbed using a hot inert gas such as carbon dioxide. This process can also be used to recover an aqueous stream comprising desorbed isobutanol, and this stream can be used directly as the reactant of the present invention, or can be further treated by distillation to produce an aqueous isobutanol stream that can be used as the reactant of the present invention.
Liquid-liquid extraction is a mass transfer operation in which a liquid solution (the feed) is contacted with an immiscible or nearly immiscible liquid (solvent) that exhibits preferential affinity or selectivity towards one or more of the components in the feed, allowing selective separation of said one or more components from the feed. The solvent comprising the one or more feed components can then be separated, if necessary, from the components by standard techniques, such as distillation or evaporation. One example of the use of liquid-liquid extraction for the separation of butyric acid and butanol from microbial fermentation broth has been described by Cenedella, R. J. in U.S. Pat. No. 4,628,116 (Column 2, line 28 through Column 8, line 57). According to U.S. Pat. No. 4,628,116, fermentation broth containing butyric acid and/or butanol was acidified to a pH from about 4 to about 3.5, and the acidified fermentation broth was then introduced into the bottom of a series of extraction columns containing vinyl bromide as the solvent. The aqueous fermentation broth, being less dense than the vinyl bromide, floated to the top of the column and was drawn off. Any butyric acid and/or butanol present in the fermentation broth was extracted into the vinyl bromide in the column. The column was then drawn down, the vinyl bromide was evaporated, resulting in purified butyric acid and/or butanol.
Other solvent systems for liquid-liquid extraction, such as decanol, have been described by Roffler, S. R., et al. (Bioprocess Eng. (1987) 1:1-12) and Taya, M., et al (J. Ferment. Technol. (1985) 63:181). In these systems, two phases were formed after the extraction: an upper less dense phase comprising decanol, 1-butanol and water, and a more dense phase comprising mainly decanol and water. Aqueous 1-butanol was recovered from the less dense phase by distillation.
These processes can also be used to obtain an aqueous stream comprising isobutanol that can be used directly as the reactant of the present invention, or can be further treated by distillation to produce an aqueous isobutanol that can be used as the reactant of the present invention.
Aqueous streams comprising isobutanol, as obtained by any of the methods above, can be the reactant for the process of the present invention. The reaction to form at least one butene is performed at a temperature of from about 50 degrees Centigrade to about 450 degrees Centigrade. In a more specific embodiment, the temperature is from about 100 degrees Centigrade to about 250 degrees Centigrade.
The reaction can be carried out under an inert atmosphere at a pressure of from about atmospheric pressure (about 0.1 MPa) to about 20.7 MPa. In a more specific embodiment, the pressure is from about 0.1 MPa to about 3.45 MPa. Suitable inert gases include nitrogen, argon and helium.
The reaction can be carried out in liquid or vapor phase and can be run in either batch or continuous mode as described, for example, in H. Scott Fogler, (Elements of Chemical Reaction Engineering, 2nd Edition, (1992) Prentice-Hall Inc, CA).
The at least one acid catalyst can be a homogeneous or heterogeneous catalyst. Homogeneous catalysis is catalysis in which all reactants and the catalyst are molecularly dispersed in one phase. Homogeneous acid catalysts include, but are not limited to inorganic acids, organic sulfonic acids, heteropolyacids, fluoroalkyl sulfonic acids, metal sulfonates, metal trifluoroacetates, compounds thereof and combinations thereof. Examples of homogeneous acid catalysts include sulfuric acid, fluorosulfonic acid, phosphoric acid, p-toluenesulfonic acid, benzenesulfonic acid, hydrogen fluoride, phosphotungstic acid, phosphomolybdic acid, and trifluoromethanesulfonic acid.
Heterogeneous catalysis refers to catalysis in which the catalyst constitutes a separate phase from the reactants and products. Heterogeneous acid catalysts include, but are not limited to 1) heterogeneous heteropolyacids (HPAs), 2) natural clay minerals, such as those containing alumina or silica, 3) cation exchange resins, 4) metal oxides, 5) mixed metal oxides, 6) metal salts such as metal sulfides, metal sulfates, metal sulfonates, metal nitrates, metal phosphates, metal phosphonates, metal molybdates, metal tungstates, metal borates, 7) zeolites, and 8) combinations of groups 1-7. See, for example, Solid Acid and Base Catalysts, pages 231-273 (Tanabe, K., in Catalysis: Science and Technology, Anderson, J. and Boudart, M (eds.) 1981 Springer-Verlag, New York) for a description of solid catalysts.
The heterogeneous acid catalyst may also be supported on a catalyst support. A support is a material on which the acid catalyst is dispersed. Catalyst supports are well known in the art and are described, for example, in Satterfield, C. N. (Heterogeneous Catalysis in Industrial Practice, 2nd Edition, Chapter 4 (1991) McGraw-Hill, New York).
In one embodiment of the invention, the reaction is carried out using a heterogeneous catalyst, and the temperature and pressure are chosen so as to maintain the reactant and reaction product in the vapor phase. In a more specific embodiment, the reactant is obtained from a fermentation broth that is subjected to distillation to produce a vapor phase having at least about 33% water. The vapor phase is directly used as a reactant in a vapor phase reaction in which the acid catalyst is a heterogeneous catalyst, and the temperature and pressure are chosen so as to maintain the reactant and reaction product in the vapor phase. It is believed that this vapor phase reaction would be economically desirable because the vapor phase is not first cooled to a liquid prior to performing the reaction.
One skilled in the art will know that conditions, such as temperature, catalytic metal, support, reactor configuration and time can affect the reaction kinetics, product yield and product selectivity. Depending on the reaction conditions, such as the particular catalyst used, products other than butenes may be produced when isobutanol is contacted with an acid catalyst. Additional products comprise dibutyl ethers (such as di-1-butyl ether) and isooctenes. Standard experimentation, performed as described in the Examples herein, can be used to optimize the yield of butenes from the reaction.
Following the reaction, if necessary, the catalyst can be separated from the reaction product by any suitable technique known to those skilled in the art, such as decantation, filtration, extraction or membrane separation (see Perry, R. H. and Green, D. W. (eds), Perry's Chemical Engineer's Handbook, 7th Edition, Section 13, 1997, McGraw-Hill, New York, Sections 18 and 22).
The at least one butene can be recovered from the reaction product by distillation as described in Seader, J. D., et al (Distillation, in Perry, R. H. and Green, D. W. (eds), Perry's Chemical Engineer's Handbook, 7th Edition, Section 13, 1997, McGraw-Hill, New York). Alternatively, the at least one butene can be recovered by phase separation, or extraction with a suitable solvent, such as trimethylpentane or octane, as is well known in the art. Unreacted isobutanol can be recovered following separation of the at least one butene and used in subsequent reactions.
The present process and certain embodiments for accomplishing it are shown in greater detail in the Drawing figures.
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The at least one recovered butene is useful as an intermediate for the production of linear, low density polyethylene (LLDPE) or high density polyethylene (HDPE), as well as for the production of transportation fuels and fuel additives. For example, butenes can be used to produce alkylate, a mixture of highly branched alkanes, mainly isooctane, having octane numbers between 92 and 96 RON (research octane number) (Kumar, P., et al (Energy & Fuels (2006) 20:481-487). In some refineries, isobutene is converted to methyl t-butyl ether (MTBE). In addition, butenes are useful for the production of alkyl aromatic compounds. Butenes can also be dimerized to isooctenes and further converted to isooctanes, isooctanols and isooctyl alkyl ethers that can be used as fuel additives to enhance the octane number of the fuel.
In one embodiment of the invention, the at least one recovered butene is contacted with at least one straight-chain, branched or cyclic C3 to C5 alkane in the presence of at least one acid catalyst to produce a reaction product comprising at least one isoalkane. Methods for the alkylation of olefins are well known in the art and process descriptions can be found in Kumar, P., et al (supra) for the alkylation of isobutane and raffinate II (a mixture comprising primarily butanes and butenes); and U.S. Pat. No. 6,600,081 (Column 3, lines 42 through 63) for the reaction of isobutane and isobutylene to produce trimethylpentanes (TMPs). Generally, the acid catalysts useful for these reactions have been homogeneous catalysts, such as sulfuric acid or hydrogen fluoride, or heterogeneous catalysts, such as zeolites, heteropolyacids, metal halides, Bronsted and Lewis acids on various supports, and supported or unsupported organic resins. The reaction conditions and product selectivity are dependent on the catalyst. Generally, the reactions are carried out at a temperature between about −20 degrees C. and about 300 degrees C., and at a pressure of about 0.1 MPa to about 10 MPa.
The at least one isoalkane produced by the reaction can be recovered by distillation (see Seader, J. D., supra) and added to a transportation fuel. Unreacted butenes or alkanes can be recycled and used in subsequent reactions to produce isoalkanes.
In another embodiment, the at least one recovered butene is contacted with benzene, a C1 to C3 alkyl-substituted benzene, or combination thereof, in the presence of at least one acid catalyst or at least one basic catalyst to produce a reaction product comprising at least one C10 to C13 substituted aromatic compound. C1 to C3 alkyl-substituted benzenes include toluene, xylenes, ethylbenzene and trimethyl benzene.
Methods for the alkylation of aromatic compounds are well known in the art; discussions of such reactions can be found in Handbook of Heterogeneous Catalysis, Volume 5, Chapter 4 (Ertl, G., Knözinger, H., and Weitkamp, J. (eds), 1997, VCH Verlagsgesellschaft mbH, Weinheim, Germany) and Vora, B. V., et al (Alkylation, in Kirk-Othmer Encyclopedia of Chemical Technology, Volume 2, pages 169-203, John Wiley & Sons, Inc., New York).
In the alkylation of aromatic compounds, acid catalysts promote the addition of butenes to the aromatic ring itself. Typical acid catalysts are homogenous catalysts, such as sulfuric acid, hydrogen fluoride, phosphoric acid, AlCl3 and boron fluoride, or heterogeneous catalysts, such as alumino-silicates, clays, ion-exchange resins, mixed oxides, and supported acids. Examples of heterogeneous catalysts include ZSM-5, Amberlyst® (Rohm and Haas, Philadelphia, Pa.) and Nafion®-silica (DuPont, Wilmington, Del.).
In base-catalyzed reactions, the butenes are added to the alkyl group of an aromatic compound. Typical basic catalysts are basic oxides, alkali-loaded zeolites, organometallic compounds such as alkyl sodium, and metallic sodium or potassium. Examples include alkali-cation-exchanged X- and Y-type zeolites, magnesium oxide, titanium oxide, and mixtures of either magnesium oxide or calcium oxide with titanium dioxide.
The at least one C10 to C13 substituted aromatic compound produced by the reaction can be recovered by distillation (see Seader, J. D., supra) and added to a transportation fuel. Unreacted butenes, benzene or alkyl-substituted benzene can be recycled and used in subsequent reactions to produce substituted aromatic compounds.
In yet another embodiment, the at least one recovered butene is contacted with methanol, ethanol, a C3 to C15 straight-chain, branched or cyclic alcohol, or a combination thereof, in the presence of at least one acid catalyst, to produce a reaction product comprising at least one butyl alkyl ether. The “butyl” group can be 1-butyl, 2-butyl or isobutyl, and the “alkyl” group can be straight-chain, branched or cyclic. The reaction of alcohols with butenes is well known and is described in detail by Stüwe, A. et al (Handbook of Heterogeneous Catalysis, Volume 4, Section 3.11, pages 1986-1998 (Ertl, G., Knözinger, H., and Weitkamp, J. (eds), 1997, VCH Verlagsgesellschaft mbH, Weinheim, Germany)) for the production of methyl-t-butyl ether (MTBE) and methyl-t-amyl ether (TAME). In general, butenes are reacted with alcohols in the presence of an acid catalyst, such as an ion exchange resin. The etherification reaction can be carried out at pressures of about 0.1 to about 20.7 MPa, and at temperatures between 50 and 200 degrees Centigrade.
The at least one butyl alkyl ether produced by the reaction can be recovered by distillation (see Seader, J. D., supra) and added to a transportation fuel. Unreacted butenes or alcohols can be recycled and used in subsequent reactions to produce butyl alkyl ethers.
In another embodiment, the at least one recovered butene can be dimerized to isooctenes, and further converted to isooctanes, isooctanols or isooctyl alkyl ethers, which are useful fuel additives. The terms isooctenes, isooctanes and isooctanols are all meant to denote eight-carbon compounds having at least one secondary or tertiary carbon. The term isooctyl alkyl ether is meant to denote a compound, the isooctyl moiety of which contains eight carbons, at least one carbon of which is a secondary or tertiary carbon.
The dimerization reaction can be carried out as described in U.S. Pat. No. 6,600,081 (Column 3, lines 42 through 63) for the reaction of isobutane and isobutylene to produce trimethylpentanes (TMPs). The at least one recovered butene is contacted with at least one dimerization catalyst (for example, silica-alumina) at moderate temperatures and pressures and high throughputs to produce a reaction product comprising at least one isooctene. Typical operations for a silica-alumina catalyst involve temperatures of about 150 degrees Centigrade to about 200 degrees Centigrade, pressures of about 2200 kPa to about 5600 kPa, and liquid hourly space velocities of about 3 to 10. Other known dimerization processes use either hydrogen fluoride or sulfuric acid catalysts. With the use of the latter two catalysts, reaction temperatures are kept low (generally from about 15 degrees Centigrade to about 50 degrees Centigrade with hydrogen fluoride and from about 5 degrees Centigrade to about 15 degrees Centigrade with sulfuric acid) to ensure high levels of conversion. Following the reaction, the at least one isooctene can be separated from a solid dimerization catalyst, such as silica-alumina, by any suitable method, including decantation. The at least one isooctene can optionally be recovered from the reaction product by distillation (see Seader, J. D., supra) to produce at least one recovered isooctene. Unreacted butenes can be recycled and used in subsequent reactions to produce isooctenes.
The at least one recovered isooctene produced by the dimerization reaction can then be contacted with at least one hydrogenation catalyst in the presence of hydrogen to produce a reaction product comprising at least one isooctane. Suitable solvents, catalysts, apparatus, and procedures for hydrogenation in general can be found in Augustine, R. L. (Heterogeneous Catalysis for the Synthetic Chemist, Marcel Decker, New York, 1996, Section 3); the hydrogenation can be performed as exemplified in U.S. Patent Application No. 2005/0054861, paragraphs 17-36). In general, the reaction is performed at a temperature of from about 50 degrees Centigrade to about 300 degrees Centigrade, and at a pressure of from about 0.1 MPa to about 20 MPa. The principal component of the hydrogenation catalyst may be selected from metals from the group consisting of palladium, ruthenium, rhenium, rhodium, iridium, platinum, nickel, cobalt, copper, iron, osmium; compounds thereof; and combinations thereof. The catalyst may be supported or unsupported. The at least one isooctane can be separated from the hydrogenation catalyst by any suitable method, including decantation The at least one isooctane can then be recovered (for example, if the reaction does not go to completion or if a homogeneous catalyst is used) from the reaction product by distillation (see Seader, J. D., supra) to obtain a recovered isooctane, and added to a transportation fuel. Alternatively, the reaction product itself can be added to a transportation fuel. If present, unreacted isooctenes can be used in subsequent reactions to produce isooctanes.
In another embodiment, the at least one recovered isooctene produced by the dimerization reaction is contacted with water in the presence of at least one acidic catalyst to produce a reaction product comprising at least one isooctanol. The hydration of olefins is well known, and a method to carry out the hydration using a zeolite catalyst is described in U.S. Pat. No. 5,288,924 (Column 3, line 48 to Column 7, line 66), wherein a temperature of from about 60 degrees Centigrade to about 450 degrees Centigrade and a pressure of from about 700 kPa to about 24,500 kPa are used. The water to olefin ratio is from about 0.05 to about 30. Where a solid acid catalyst is used, such as a zeolite, the at least one isooctanol can be separated from the at least one acid catalyst by any suitable method, including decantation. The at least one isooctanol can then optionally be recovered from the reaction product by distillation (see Seader, J. D., supra), and added to a transportation fuel. Alternatively, the reaction product itself can be added to a transportation fuel. Unreacted isooctenes, if present, can be used in subsequent reactions to produce isooctanols.
In still another embodiment, the at least one recovered isooctene produced by the dimerization reaction is contacted with at least one acid catalyst in the presence of at least one straight-chain or branched C1 to C5 alcohol to produce a reaction product comprising at least one isooctyl alkyl ether. One skilled in the art will recognize that C1 and C2 alcohols cannot be branched. The etherification reaction is described by Stüwe, A., et al (Synthesis of MTBE and TAME and related reactions, Section 3.11, in Handbook of Heterogeneous Catalysis, Volume 4, (Ertl, G., Knözinger, H., and Weitkamp, J. (eds), 1997, VCH Verlagsgesellschaft mbH, Weinheim, Germany)) for the production of methyl-t-butyl ether. The etherification reaction is generally carried out at temperature of from about 50 degrees Centigrade to about 200 degrees Centigrade at a pressure of from about 0.1 to about 20.7 MPa. Suitable acid catalysts include, but are not limited to, acidic ion exchange resins. Where a solid acid catalyst is used, such as an ion-exchange resin, the at least one isooctyl alkyl ether can be separated from the at least one acid catalyst by any suitable method, including decantation. The at least one isooctyl alkyl ether can then be recovered from the reaction product by distillation (see Seader, J. D., supra) to obtain a recovered isooctyl alkyl ether, and added to a transportation fuel. Alternatively, the reaction product itself can be added to a transportation fuel. If present, unreacted isooctenes can be used in subsequent reactions to produce isooctyl alkyl ethers.
According to embodiments described above, butenes produced by the reaction of aqueous isobutanol with at least one acid catalyst are first recovered from the reaction product prior to being converted to compounds useful in transportation fuels. However, as described in the following embodiments, the reaction product comprising butenes can also be used in subsequent reactions without first recovering said butenes.
Thus, one alternative embodiment of the invention is a process for making at least one C10 to C13 substituted aromatic compound comprising:
(a) contacting a reactant comprising isobutanol and at least about 5% water (by weight relative to the weight of the water plus isobutanol) with at least one acid catalyst at a temperature of about 50 degrees C. to about 450 degrees C. and a pressure from about 0.1 MPa to about 20.7 MPa to produce a first reaction product comprising at least one butene;
(b) contacting said first reaction product with benzene, a C1 to C3 alkyl-substituted benzene, or a combination thereof, in the presence of at least one acid catalyst or at least one basic catalyst at a temperature of about 100 degrees C. to about 450 degrees C., and at a pressure of about 0.1 MPa to about 10 MPa to produce a second reaction product comprising at least one C10 to C13 substituted aromatic compound; and
(c) recovering the at least one C10 to C13 substituted aromatic compound from the second reaction product to obtain at least one recovered C10 to C13 substituted aromatic compound.
The at least one recovered C10 to C13 substituted aromatic compound can then be added to a transportation fuel.
Another embodiment of the invention is a process for making at least one butyl alkyl ether comprising:
(a) contacting a reactant comprising isobutanol and at least about 5% water (by weight relative to the weight of the water plus isobutanol) with at least one acid catalyst at a temperature of about 50 degrees C. to about 450 degrees C. and a pressure from about 0.1 MPa to about 20.7 MPa to produce a first reaction product comprising at least one butene;
(b) contacting said first reaction product with methanol, ethanol, a C3 to C15 straight-chain, branched or cyclic alcohol, or a combination thereof, in the presence of at least one acid catalyst at a temperature of about 50 degrees C. to about 200 degrees C., and at a pressure of about 0.1 MPa to about 20.7 MPa to produce a second reaction product comprising at least one butyl alkyl ether; and
(c) recovering the at least one butyl alkyl ether from the second reaction product to obtain at least one recovered butyl alkyl ether.
The at least one recovered butyl alkyl ether can be added to a transportation fuel.
An alternative process for making at least one butyl alkyl ether comprises:
(a) contacting a reactant comprising isobutanol and at least about 5% water (by weight relative to the weight of the water plus isobutanol) with at least one acid catalyst at a temperature of about 50 degrees C. to about 450 degrees C. and a pressure from about 0.1 MPa to about 20.7 MPa to produce a first reaction product comprising at least one butene and at least some unreacted isobutanol;
(b) contacting said first reaction product with at least one acid catalyst, and optionally with methanol, ethanol, a C3 to C15 straight-chain, branched or cyclic alcohol, or a combination thereof, at a temperature of about 50 degrees C. to about 200 degrees C., and at a pressure of about 0.1 MPa to about 20.7 MPa to produce a second reaction product comprising at least one butyl alkyl ether; and
(c) recovering the at least one butyl alkyl ether from the second reaction product to obtain a recovered butyl alkyl ether.
The at least one recovered butyl alkyl ether can then also be added to a transportation fuel.
Another embodiment of the invention is a process for making a reaction product comprising at least one isooctane comprising:
(a) contacting a reactant comprising isobutanol and at least about 5% water (by weight relative to the weight of the water plus isobutanol) with at least one acid catalyst at a temperature of about 50 degrees C. to about 450 degrees C. and a pressure from about 0.1 MPa to about 20.7 MPa to produce a first reaction product comprising at least one butene;
(b) recovering said at least one butene from said first reaction product to obtain at least one recovered butene;
(c) contacting said at least one recovered butene with at least one acid catalyst to produce a second reaction product comprising at least one isooctene;
(d) contacting said second reaction product with hydrogen in the presence of at least one hydrogenation catalyst to produce said reaction product comprising at least one isooctane; and
(e) optionally recovering the at least one isooctane from the reaction product to obtain at least one recovered isooctane.
Another embodiment of the invention is a process for making a reaction product comprising at least one isooctanol comprising:
(a) contacting a reactant comprising isobutanol and at least about 5% water (by weight relative to the weight of the water plus isobutanol) with at least one acid catalyst at a temperature of about 50 degrees C. to about 450 degrees C. and a pressure from about 0.1 MPa to about 20.7 MPa to produce a first reaction product comprising at least one butene;
(b) recovering said at least one butene from said first reaction product to obtain at least one recovered butene;
(c) contacting said at least one recovered butene with at least one acid catalyst to produce a second reaction product comprising at least one isooctene;
(d) contacting said second reaction product with water and at least one acid catalyst to produce said reaction product comprising at least one isooctanol; and
(e) optionally recovering the at least one isooctanol from the reaction product to obtain at least one recovered isooctanol.
In the following examples, “C” is degrees Centigrade, “mg” is milligram; “ml” is milliliter; “MPa” is mega Pascal; “wt. %” is weight percent; “GC/MS” is gas chromatography/mass spectrometry.
Amberlyst® (manufactured by Rohm and Haas, Philadelphia, Pa.), tungstic acid, isobutanol and H2SO4 were obtained from Alfa Aesar (Ward Hill, Mass.); CBV-3020E was obtained from PQ Corporation (Berwyn, Pa.); Sulfated Zirconia was obtained from Engelhard Corporation (Iselin, N.J.); 13% Nafion®/SiO2 can be obtained from Engelhard; and H-Mordenite can be obtained from Zeolyst Intl. (Valley Forge, Pa.).
A mixture of isobutanol, water, and catalyst was contained in a 2 ml vial equipped with a magnetic stir bar. The vial was sealed with a serum cap perforated with a needle to facilitate gas exchange. The vial was placed in a block heater enclosed in a pressure vessel. The vessel was purged with nitrogen and the pressure was set at 6.9 MPa. The block was brought to the indicated temperature and controlled at that temperature for the time indicated. After cooling and venting, the contents of the vial were analyzed by GC/MS using a capillary column (either (a) CP-Wax 58 [Varian; Palo Alto, Calif.], 25 m×0.25 mm, 45 C/6 min, 10 C/min up to 200 C, 200 C/10 min, or (b) DB-1701 [J&W (available through Agilent; Palo Alto, Calif.)], 30 m×0.25 mm, 50 C/10 min, 10 C/min up to 250 C, 250 C/2 min).
The examples below were performed according to this procedure under the conditions indicated for each example.
The feedstock was 85 wt. % isobutanol/15 wt. % water.
This application claims priority under 35 U.S.C. §119 from U.S. Provisional Application Ser. No. 60/814,682 (filed Jun. 16, 2006), the disclosure of which is incorporated by reference herein for all purposes as if fully set forth.
| Number | Date | Country | |
|---|---|---|---|
| 60814682 | Jun 2006 | US |
