Patent Application
20240279147
The present invention relates to processes for producing an ether compound; and more specifically, the present invention relates to processes for producing an ether compound directly from an alkyl ester using molecular hydrogen on a heterogeneous catalyst.
Ethers are used in various applications, including as a solvent. Ethers are particularly desirable for use as a solvent in applications because ethers possess excellent solvency, chemical stability and compatibility with other organic solvents and formulated products. Known routes of synthesizing ethers include the following three routes: (1) alkyl halides treated with alkoxides (so called the “Williamson ether synthesis”); (2) alcohol addition to an olefin; and (3) acid catalyzed coupling of alcohols. However, the above three routes have undesirable limitations including: (1) use of strongly acidic or basic conditions which can lead to competing elimination reactions that produce undesired olefins; (2) limited options of bio-sourced raw materials due to lack of reactivity with the above reactions which limit the structural variety of products; and (3) use of toxic raw materials and generation of waste streams in a manufacturing process. Therefore, what is desired is to provide a viable route for producing an ether that can be successfully scaled up commercially without the limitations of the above known routes.
For example, heretofore the known methods for producing an ether include the following: (1) a process using metal hydride/Lewis acid complexes, or hydrosilanes as stoichiometric hydride donors with precious metal catalysts as disclosed in J. Org. Chem., 2007, 72, 5920-5922; Tetrahedron Letters, 2017, 58, 3024-3027; (2) a process for producing a thionate (a salt or ester of thionic acid) such as a thioether (a sulfide which is a bonded compound of sulfur and two organic residues) as disclosed in J. Org. Chem., 1981, 46, 831-832; (3) a process for the catalytic reduction of α-monoglycerides with a 5 percent (%) Pd/C catalyst mixed with an acid cocatalyst at about 700 psi (4.8 megapascals [MPa]) and 120 degrees Celsius (° C.) as disclosed in U.S. Pat. No. 8,912,365; (4) a non-direct process for the hydrogenation of ethyl acetate into ethanol intermediates that subsequently couple to form a symmetrical ether by-product on Re/(gamma-Al2O3) or Re/(theta-Al2O3) at up to 4.6% conversion and 57% selectivity as disclosed in Russian Chemical Bulletin 1988, 37(1), 15-19 and Russian Chemical Bulletin 1986, 35, 280-283; and (5) a process for the hydrogenation of lactone to cyclic ethers, for example (e.g.), for production of tetrahydrofuran, in high selectivities such as greater than (>) 90% using various metal catalysts on various support carriers as disclosed in U.S. Pat. Nos. 3,370,067; 3,894,054; and 4,973,717. (6) a process using homogeneous metal complex catalysts (e.g. a ruthenium/triphos complex) which require impractical separation of catalyst from product. Angewandte Chemie, International Edition, 2015. 54, 5196-5200; ChemSusChem, 2016, 9, 1442-1448.
In a recently filed patent application, U.S. Pat. No. 63/107,739, a process to directly convert ester to ether with transition metals supported by metal oxide supports, such Nb2O5 and WO3 is described. The invention reported high direct selectivity of ether formation via hydrogenation, however, the ether product absolute selectivities from hydrogenation were generally low, typically in a range of 5 to 10% with a maximum value of 16%. Further improvement of the catalyst selectivity is required in order to make the process economically valuable.
It would therefore be desirable to have alternative processes for producing ethers that can be commercially manufactured and that provide advantages over existing processes, including improved absolute and/or direct selectivity.
The present invention is directed to new processes for producing an ether product from an ester starting raw material using transition metal catalysts on zeolite carriers.
In a broad embodiment, a process of the present invention includes producing an ether by hydrogenation of an ester in the presence of a heterogeneous catalyst.
In one embodiment, a process of the present invention includes direct selective reduction of carboxylic acid derivatives into ethers using molecular hydrogen and a proper catalyst formulation for achieving a high (e.g., >10%) absolute ether selectivity with a high (e.g., >80%) direct ether selectivity. Absolute ether selectivity is the percentage of the total products formed in the reaction, while the direct ether product selectivity is the percentage of direct ether product over the total ether products.
In another embodiment, a process of the present invention for producing an ether comprises mixing: (a) at least one ester with (b) hydrogen in the presence of (c) a heterogeneous catalyst to reduce the ester by hydrogenation to form an ether.
In still another embodiment, the present invention includes a solvent comprising the above ether product produced by the above process.
Some of the advantageous features that can be provided by one or more embodiments of the process of the present invention include, for example:
(1) An active catalyst is used in a one-step process. The catalyst is active for direct hydrogenation of an ester to reduce the ester to form an ether, rather than going through a known two-step ether formation process such as (i) ester hydrogenolysis to form alcohol followed by (ii) alcohol dehydration.
(2) A relatively inexpensive route is used. The process employs inexpensive molecular hydrogen as a reduction agent, rather than employing expensive hydrosilanes, metal hydrides, or metal hydride/Lewis acid complexes as a hydride donor. The highly reactive hydrosilanes or metal hydride employed in prior art processes also requires the design of a complicated and expensive process to ensure the safety of the operators running the prior art processes.
(3) A heterogeneous catalyst is used. The catalyst being heterogeneous rather than homogeneous, can contribute to lower manufacturing costs due to catalyst recyclability and separation.
(4) An efficient process is used.
(5) A flexible process is used. The process is applicable to a general ester compound (either cyclic or acyclic) as a feed material; and the process is not limited to a specified ester compound.
In one embodiment, the present invention includes a distinct and novel method for synthesizing ethers from esters with heterogeneous catalysts. The reactions of ester on heterogeneous catalysts include various chemical reaction routes or pathways, for example, hydrogenolysis, hydrolysis, dehydration, hydrogenation, and transesterification. In a general embodiment, the process of the present invention includes producing an ether by hydrogenation of an ester, such as a propyl acetate, in the presence of a heterogeneous catalyst. The present invention's novel hydrogenation reaction pathway or scheme, for example, the hydrogenation of propyl acetate reduction reaction scheme with R1 being —CH3 and R2 being —CH2CH3, is generally illustrated as Reaction Scheme (I) as follows:
In the above Reaction Scheme (I), water is generated by the reduction process; and the generated water can be separated by conventional processes such as distillation or other procedures known in the art. Functional groups R1 and R2 can be alkyl functional groups including straight or branched-chain alkyl groups, cyclic or non-cyclic alkyl groups; and mixtures thereof. Examples of the esters herein include but are not limited to ethyl acetate, propyl acetate, butyl acetate, ethyl propionate, butyl propionate and mixtures thereof. The desired ether product resulting from the above Reaction Scheme (I) can be a symmetric ether when Ri is equivalent to R2; or an unsymmetric ether when Ri is not equivalent to R2, for example, the unsymmetric ether can be ethyl propyl ether.
A “symmetric ether” herein means an ether that contains two identical functional groups, wherein R1 is identical to R2. An “unsymmetric ether” herein means an ether that contains two different functional groups, where R1 is not identical to R2.
In the present invention the desired reaction scheme, Reaction Scheme (I), is a direct hydrogenation route to obtain the desired ether product. By “direct hydrogenation” or “direct selective reduction” it is meant that carbonyl oxygen is removed from ester (R1COOCH2R2) by hydrogenation to form ether (R1CH2OCH2R2) while maintaining the alkoxyl group intact. The present invention process is different from known processes because the present invention process does not undergo a typical route for ester (R1COOCH2R2) hydrogenation, where ester first breaks into two alcohols (R1CH2OH+R2CH2OH molecules via hydrogenolysis and then subsequently forms a mixture of ethers (R1CH2OCH2R1+R1CH2OCH2R2+R2CH2OCH2R2) via dehydration. Direct hydrogenation can maintain the structure of the ether from ester by only eliminating the carbonyl oxygen. Thus, an unsymmetric ester provided to this process advantageously results in the direct production of an unsymmetric ether because this process does not break the ester into two alcohol molecules via hydrogenolysis. The selectivity of ethyl propyl ether in the reaction examples are listed in Table III and Table V described below in the Examples.
The term “direct ether product” herein means an ether that is formed by a one-step reduction process of ether from ester.
The term “indirect ether product” herein means an ether that is formed by a two-step reduction process of ether from ester including the steps of: (i) hydrogenolysis and (ii) dehydration.
The term “direct ether product selectivity” herein means the percentage of the direct ether product over the total ether products. E.g. for the reduction of propyl acetate, ethyl propyl ether is the direct ether product, and the direct ether product selectivity is the percentage of ethyl propyl ether over the total ether products (ethyl propyl ether+dipropyl ether+diethyl ether).
The term “ether product absolute selectivity” herein means the percentage of the ether product in the total products formed in the reaction (e.g., ethers, alcohols, and alkanes).
Advantageously, one unique factor of the present invention includes an increase in direct ether selectivity using the one-step process of the present invention versus the known two-step process.
In one embodiment, a process of the present invention for producing an ether comprises treating (a) an ester with (b) hydrogen in the presence of (c) a heterogeneous catalyst to reduce the ester by hydrogenation to form an ether.
In one desirable embodiment and as shown in Reaction Scheme (I) above, a process of the present invention for producing an ether comprises the steps of: (A) feeding into a reactor, an ester compound, component (a), such as propyl acetate; (B) feeding into the reactor, hydrogen, component (b), to form a hydrogen atmosphere in the reactor; and (C) charging the reactor with a heterogeneous catalyst system, component (c), comprising a transition metal on a zeolite support; sufficient to generate a hydrogenation reaction in the reactor; and (D) heating the contents of the reactor, components (a)-(c), at a temperature sufficient to reduce the ester compound to form an ether compound. For example, the heating step (D), can take place at a temperature of from 350 Kelvin (K) to 650 K. It will also be readily understood by those in the art that the order of the recited steps can be altered in certain circumstances, or steps may be done simultaneously
As is generally known in the art a “heterogeneous catalyst” refers to a catalyst whose phase (e.g., solid, liquid or gas) is different from the phase of the reactants. For example, the reactants (esters and hydrogen) and product (e.g., ether) can be in the liquid or gas phase while the catalyst is a solid.
In the present invention, the heterogeneous catalytic system of the present invention is a combination of a transition metal and a zeolite support. For instance, the catalyst used in some embodiments of the present invention can include from 0.1 weight percent (wt %) to 20 wt % of a transition metal supported on zeolite support member.
As is generally known in the art, zeolites are crystalline aluminosilicate materials composed of corner-sharing AlO4 and SiO4 tetrahedra joined into three-dimensional frameworks having pores of molecular dimensions. The presence of aluminum in the zeolite framework results in a negative charge that is balanced by cations. The zeolites in this invention have a framework type which may advantageously be selected from the group consisting of the following framework types FAU, MOR, BEA, CHA, FER, MFI, and combinations thereof, the framework types corresponding to the naming convention of the International Zeolite Association.
Atomic Si/Al ratios are often used in the practice of catalysis to characterize the zeolites and refers the number of silicon containing sites (typically SiO2) present per alumina containing site (typically HAlO2). The zeolites for use in the present invention can have an Si:Al ratio in the range of from 1 to 300. In some embodiments the ratio may be 2 to 250, or even 10 to 50.
The synergistic effect from both the transition metal component and the zeolite support component promotes the direct ether reduction route, as described in the reaction pathway Reaction Scheme (I). Without the combination of a transition metal and a zeolite support member as disclosed herein, an undesirable two-step ether formation route would take place. Steady-state rates and product selectivity for competing reaction pathways for a model ester compound are obtained in, for example, a packed-bed reactor and/or a trickle bed reactor as functions of reactant pressures, temperature, and ester conversion, which are controlled via the surface residence time.
The ester compound, component (a), to be reduced to an ether, can include one or more ester compounds, including, for example, a carboxylic acid derivative; an ester containing straight or branched-chain alkyl groups, and cyclic or non-cyclic alkyl groups; and mixtures thereof. In some embodiments, an unsymmetric ether includes a Reaction Scheme (I) wherein the R1 groups are not equal to the R2 groups. In some embodiments, the ester useful in the present invention can be, for example, propyl acetate (available from Sigma-Aldrich); butyl acetate (available from Sigma-Aldrich); butyl propionate, glycerin ester; and mixtures thereof.
The concentration of the ester, component (a), is not particularly critical. However, it may be advantageous, in some embodiments, for the ester to be present in an amount of at least 1 wt % so as to provide a desirable production rate and/or avoid an increase in separation costs. In some embodiments, the concentration of the ester is from 1 wt % to 100 wt %. The concentration of the ester is based on the total weight of ester compounds in the liquid feed raw material.
The concentration of the hydrogen, component (b), useful in the process of the present invention includes, for example, from 3 wt % to 100 wt % in one embodiment, from 10 wt % to 100 wt % in another embodiment, and from 50 wt % to 100 wt % in still another embodiment. Hydrogen with a low concentration of, for example less than (<) 3 wt % may decrease the reactivities or ether selectivities; and therefore, in such a case an undesirable increase of the reaction pressure would be required. The concentration of the hydrogen is based on the total weight of hydrogen in the gas feed raw material.
In a broad embodiment, the catalyst used in the process, component (c), of the present invention, can include one or more heterogeneous catalyst compounds. The catalysts used in the present invention process include, for example, a combination of (ci) a transition metal, supported on (cii) a zeolite support (carrier) member. For example, the transition metal (component (ci)) may include palladium (Pd); platinum (Pt); ruthenium (Ru); cobalt (Co); copper (Cu); Rhodium (Rh); Rhenium (Re); nickel (Ni); and mixtures thereof. The acidic zeolite carrier member (component (cii)) can be derived from any zeolite or mixture of zeolite includes, for example, faujasite zeolite (“FAU”): sodium Y zeolite (NaY) (A sodium ion exchanged Y zeolite); mordenite zeolite (“MOR”); beta zeolite (“BEA”); chabazite zeolite (“CHA”); ferrierite zeolite (“FER”); Mobil-five zeolite (“MFI”) and mixtures thereof. These zeolites can preferably have an Si to Al ratio in the range of from 2 to 250. In some preferred embodiments, the heterogeneous catalyst useful in the present invention can be Pd supported on a FAU support; Pt supported on a FAU, MOR, FER or CHA support; Rh supported on an FAU support, and mixtures thereof.
The heterogeneous catalyst of the present invention exhibits some advantageous properties. For example, the heterogeneous catalysts useful in the present invention provide a synergistic effect between the metallic compound (e.g., Pd or Pt) of the catalyst and the zeolite carriers of the catalyst in order to catalyze direct ester hydrogenation. Otherwise, ether selectivities may decrease.
The heterogeneous catalyst, component (c), includes, for example, from 0.01 wt % to 20 wt % of the metallic compound based on the total weight of the heterogeneous catalyst in one embodiment, from 0.1 wt % to 10 wt % of the metallic compound based on the total weight of the heterogeneous catalyst in another embodiment, and from 1 wt % to 5 wt % of the metallic compound based on the total weight of the heterogeneous catalyst in still another embodiment.
The process equipment used to carry out the reduction process can be any conventional reactor such as a packed-bed reactor or a trickle bed reactor. And, the ester conversion and ether selectivities can be controlled via the reactor pressure, temperature, and surface residence time.
For example, the pressure of the process of the present invention is from 0.1 MPa to 10 MPa in one embodiment, from 2 MPa to 6 MPa in another embodiment, and from 6 MPa to 10 MPa in still another embodiment. Below the aforementioned pressure range may lead to lower reactivities or lower ether selectivities than disclosed herein. A pressure higher than the aforementioned pressure range may be sufficient to use in the present invention; however, it may require a higher cost in reactor construction and operation.
For example, the temperature of the process of the present invention is from 350 K to 650 K in one embodiment, from 400 K to 500 K in another embodiment, and from 500 K to 650 K in still another embodiment. Below the aforementioned temperature range may lead to lower reactivities than disclosed herein. A temperature higher than the aforementioned temperature range may lead to unwanted alkane and alcohol by-products; and therefore, in such a case the selectivities of the ether may decrease.
For example, the ester conversion of the process of the present invention is from 1% to 100% in one embodiment, from 1% to 50% in another embodiment, and from 50% to 100% in still another embodiment. In some embodiments, ester conversions higher than the aforementioned conversion range may lead to more side reaction products.
The process of the present invention may be carried out as a batch process or a continuous process. When using a batch process, in some embodiments, the residence time of the process of the present invention is, for example, from 0.1 hour (hr) to 24 hr in one embodiment, from 0.1 hr to 8 hr in another embodiment, and from 1 hr to 24 hr in still another embodiment. In some embodiments, residence times below the aforementioned residence time range may lead to a lower ester conversion; and in some embodiments, residence times above the aforementioned residence time range may lead to unwanted side reaction products.
When using a continuous process, in some embodiments, the residence time of the process of the present invention is, for example, from 0.1 second (s) to 100 s in one embodiment, from 1 s to 10 s in another embodiment, and from 10 s to 100 s in still another embodiment. Residence times below the aforementioned residence time range may lead to a lower ester conversion; and in some embodiments, residence times above the aforementioned residence time range may lead to unwanted side reaction products.
Some advantageous properties and/or benefits of using the reduction process of the present invention include, for example, the process of the present invention can achieve steady-state rates; and the process can provide better selectivities of product for competing reaction pathways for an ester compound, even better than other heterogeneous catalysts that do no feature zeolite supports. Also, conventional processes for producing an ether also produces salt whereas the process of the present invention does not generate salt.
After an ester compound undergoes the reduction process, the resulting ether product is formed. The turnover rate of ester to the ether product can be from 10−8 moles of ether per gram catalyst per second (mol/gcat·S) to 10−5 mol/gcat·s in one general embodiment, from 5×10−8 mol/gcat·s to 5×10−6 mol/gcat·s. Ester turnover rates below the aforementioned rate range may lead to a lower ether production rate; and in some embodiments, ester turnover rate above the aforementioned residence time range may lead to unwanted side reaction products.
The selectivity of the ether product can depend on whether a vapor process or liquid process is used to form the ether and whether a batch process or continuous process is used. In general, the selectivity of the direct ether product is >10% in one embodiment, from 10% to 25% in another embodiment, and from 25% to 60% in still another embodiment.
While the ether product produced by the process of the present invention can be a symmetric ether or an unsymmetric ether, as an illustration of the present invention and not to be limited thereby, the present invention process is described with reference to an unsymmetric ether. It has been surprisingly discovered that the process of the present invention is selective for unsymmetric ether because in the present invention process the ester is directly converted to ether, without undergoing ester hydrogenolysis and alcohol dehydration. Ester hydrogenolysis and alcohol dehydration are two processes that are known to not be selective for a specific ether.
If an unsymmetric ether is desired for a specific process or end use, then use of the present invention process is more advantageous than conventional processes because:
(1) An ether product is more stable than the corresponding ester product under basic and acid conditions. Also, the ether products of the present invention do not typically undergo hydrolysis which can occur at high humidity and/or high temperatures.
(2) It is believed that the hydrogen reaction chemistry of the present invention process maintains the backbone of the ester product intact. During the hydrogenation, only the oxygen molecule is broken away from the backbone which leaves the carbon molecules and backbone oxygen intact. In conventional reaction processes, the reaction breaks the backbone and combines parts back together under different reaction conditions. Thus, no direct hydrogenation/reduction of the ester to an ether occurs.
(3) The process of the present invention, minimizes undesirable side reactions that may detrimentally affect the selectivities of the desired ether product.
The ether product of the present invention has a minimal impact on the environment, since the ether product is derived from organic and renewable sources. For example, the ether product advantageously can be used as a global green and bio-based solvent to address the stringent regulations imposed on chemical-based industrial solvents in relation to toxicity, non-biodegradability, volatile organic compound (VOC) emissions, and the like. Green and bio-based solvents are typically used in paints and coatings applications. Other applications include adhesives, pharmaceuticals, and printing inks. In some embodiments, the ether product can be used as a foam control agent and a flavor additive. In other embodiments, the ether product can be used in cosmetics and personal care applications.
The present invention provides biobased solvents at a cost and performance advantage to known solvents in the industry. In addition, the chemical transformation provided by the present invention process could be useful to produce, for example, bio-based surfactants, defoamers and lubricants with both an economically and environmentally favorable process.
The ether generation process of the present invention can also be used to develop: (1) a more robust capping process to overcome the issues of limited reactant alkyl chloride types and final product impurities; (2) new capped low viscosity-low volatility lubricants; and (3) new surfactants and new biobased defoamers for food and pharmacy applications, metalworking fluids applications, and other applications utilizing an ether solvent.
The following Inventive Examples (Inv. Ex.) and Comparative Examples (Comp. Ex.) (collectively, “the Examples”) are presented herein to further illustrate the present invention in detail but are not to be construed as limiting the scope of the claims. Unless otherwise stated all parts and percentages are by weight.
The catalyst (“Cat.”) formulations used in the Examples are described in Table I and Table II. The Examples using Cat. 1-Cat. 14 which follow (Table I), were tested in a vapor-phase reactor, while the Examples using Cat. 15-Cat. 28 (Table II) were tested in a liquid phase reactor.
Transition metal particles (Pd. Pt. Ru, Co, Ni, Cu, Rh) are deposited onto zeolites (FAU, Tosoh; NaY, ACS Materials; MOR, ACS Materials and Tosoh; BEA, Tosoh; MFI, Tosoh and Zeolyst; CHA, ACS Materials; FER, Zeolyst) using incipient wetness impregnation (IWI), weakly capping growth approach (WCGA), ion exchange (IE) or by modified NaBH4 reduction method, as indicated.
The IWI method involves preparing an aqueous solution with the precursor concentration adjusted to the indicated weight loading. An equivalent volume of the support pore volume was added dropwise to the support achieving incipient wetness. For Pd deposited zeolite catalysts prepared by IWI method, Cat. 4 used Pd(NH3)4Cl2·H2O as precursor, while Cat. 5, Cat.22-Cat. 25 used Pd(NH3)4(NO3)2 as precursor. For Pt. Rh, Ru, Ni, and Co deposited zeolite catalysts (Cat. 9-Cat.14, Cat. 16-Cat. 26), the precursors used were [Pt(NH3)4](NO3)2, Rh(NO3)3·xH2O, Ru(NO)(NO3)3, Ni(NO3)2·6H2O, Cu(NO3)2·2.5H2O, and Co(NO3)2·6H2O, respectively.
The WCGA method involves a synthesis procedure as published in the Journal of the American Chemical Society 2015, 137 (36), 11743-11748; Industrial & Engineering Chemistry Research 2021. 60, 2326-2336. First, palladium acetate (Pd(OAc)2 is dissolved in methanol to achieve a concentration of 170 mg Pd L−1 while stirring. After the precursor is dissolved, the zeolite support is added to the solution and left stirring for at least 18 hours. The initial yellow solution turns dark during the synthesis. Pd-zeolite solids were recovered by centrifugation and washed with methanol. After centrifugation, the solid has a dark grey-black color and the filtrate is clear. Cat. 1-Cat. 3, Cat. 6, Cat. 8, Cat. 15 were prepared by WCGA method.
The IE method involves a synthesis procedure as published in the Journal of Catalysis 1989, 118 (1), 266-274). Briefly catalysts are synthesized by preparing an aqueous solution of the metal precursor and adding the support while stirring. Samples are left stirring for at least 18 hours and then separated by centrifugation. Cat. 7 was prepared by IE method.
The modified NaBH4 reduction method is as described in the Journal of Molecular Catalysis A: Chemical 2013, 376, 63-70. Briefly, 5 grams of zeolites and 483 mg of ruthenium Chloride hydrate (RuCl3—xH2O) are placed together with 150 mL ethanol in a three neck 250 cm3 round flask. The mixture is vigorously stirred for at least 24 h under Ar atmosphere. After that, 0.3 M solution of NaBH4 in ethanol (40 cm3) was added drop wise to the mixture, and the resulting mixture is stirred for at least another 24 hours. The catalyst is collected by filtration and washed with ethanol.
Regardless of the method used to prepare them, the resulting wet solids are dried in a static oven at 353 K for more than 12 h. Subsequently, the samples are heated to the oxidative treatment temperature in flowing Air (Ultra Zero Grade Air) and held for 2 to 12 hours. Samples are then cooled to ambient temperature. The samples are then heated to the reduction temperature in flowing 20% H2/He (H2, Ultra High Purity 5.0) and (He, Ultra High Purity 5.0) and held for a 0.5 to 4 hours. Samples are cooled to ambient temperature and passivated in flowing Air/He (Ultra Zero Grade Air, 2 cm3 min−1) and (He, Ultra High Purity 5.0, 250 cm3 min−1) for 1 hour before exposure to ambient air.
Elemental analysis by energy dispersive X-ray fluorescence (EDXRF) and inductively coupled plasma (ICP) analysis gives the ratio of Pd to H+ (Al) and total weight loading.
The Examples using Cat. 1-Cat. 28 are representative Inventive Examples (Inv. Ex.) of the present invention, while the Examples using Cat. 29-Cat. 33 are Comparative Examples (Comp. Ex.). The catalysts 29-32 in Tables III and IV were prepared using the incipient wetness impregnation method as described in a recently filed patent application, U.S. 63/107,739 using the materials described in Tables III and IV. The catalyst 33 in Table IV was prepared via the incipient wetness impregnation method using aluminum silicate (Al2O3—SiO2) as support purchased from Sigma Aldrich.
The process of the present invention comprises a process that: (1) uses molecular hydrogen (H2) as a reducing agent; (2) is conducted in vapor phase or liquid; and (3) uses a heterogeneous catalyst for ester reduction to ether, where the heterogeneous catalyst includes a transition metal, for example a Pd-based catalyst, and where the catalyst support (carrier) is a zeolite for the inventive examples or an acid support, for example, a WO3-based catalyst carrier or a Nb2O5-based catalyst carrier, for the comparative examples.
Cat. 1-Cat. 14, and comparative Catalysts 29 and 30 were tested in a vapor-phase reactor. The vapor-phase reactor is a tubular packed bed reactor held within a stainless-steel tube (9.5 millimeters [mm] outer diameter [O. D.]) containing from 10 milligrams (mg) to 200 mg of catalyst. The catalyst is held at the center of the reactor using glass rods and packed glass wool. The tubular reactor is placed within a three-zone furnace (available from Applied Test Systems, 3210) that was controlled by an electronic temperature controller (available from
Watlow, EZ-Zone). The catalyst temperature is measured by a K-type thermocouple contained within a 1.6 mm stainless-steel sheath (available from Omega) that is coaxially aligned within the reactor and submerged within the catalyst bed. The volume of the catalyst bed is kept constant at 1.4 cubic centimeters (cm3) of material by mixing excess silicon carbide (SiC) (available from Washington Mills, Carborex green 36) with the desired amount of catalyst. The system is pressurized using a back-pressure regulator (BPR, an Equilibar LF Series available from Equilibar Precision Pressure Control) which is controlled by an electronic pressure regulator (EPR, an Equilibar GP1 available from Equilibar Precision Pressure). The reactor pressure is monitored upstream and downstream of the catalyst bed using a digital pressure gauge (available from Omega) and the EPR, respectively.
The gases used in the Examples are: H2 (available from Airgas Inc. as “Ultra High Purity 5.0”) and He (available from Airgas Inc. as “Ultra High Purity 5.0”). The gas flow rates are controlled using mass flow controllers (available from Bronkhorst as “EL-FLOW High Pressure”). The flow rate of liquid propyl acetate (C5H10O2, supplied by Sigma Aldrich, 537438, at greater than or equal to [≥]99.5%) is controlled using a stainless-steel syringe pump with a Hastelloy cylinder (100DX with D-series controller, available from Teledyne Isco) as the C5H1002 is fed through a polyether ether ketone (PEEK) polymer tube (1.6 mm O.D. and 0.25 mm inner diameter [I. D.]) the exit of which is positioned within a small bed of non-porous sand (SiO2 50-70 mesh particle size, supplied by Sigma Aldrich, 274739) within a cross flow of H2. The transfer lines surrounding the liquid inlet are kept at 373 K using heating tape (available from Omega) to avoid condensation. All transfer lines downstream of the liquid inlet are heated above 373 K using heating tape; and the line temperatures are monitored with K-type thermocouples (available from Omega) displayed on a digital reader (available from Omega).
Catalyst is pretreated in situ by heating the catalyst to the desired temperature at 0.08 Kelvin per second (K s−1) and holding the catalyst at that temperature for the desired time within 101 kilopascals (kPa) flowing H2 at 100 cubic centimeters per minute (cm3 min−1) prior to all catalytic measurements. The effluent of the reactor is characterized using on-line gas chromatography (HP 6890, available from Agilent). The gas chromatograph (GC) is equipped with a capillary column (DB-624 UI, 30 meters (m) length, 0.25 mm I. D., 1.40 micron [μm]) connected to a flame ionization detector to quantify the concentrations of combustible species. Sensitivity factors and retention times for all components are determined using gascous and liquid standards. Control of the reactor pressure and temperature, reactant flowrates, and the GC sampling are automated to allow for continuous measurements. Conversions are calculated on a carbon basis based on the amount of carbon that appears in the products. The carbon and oxygen balance closes within±20%. Reactor conditions during rate and selectivity measurements are varied by sequentially decreasing and then increasing the reactant pressure over the full range of 1 MPa to 10 MPa such that one or more of the conditions is measured at least twice throughout the experiment to ensure that measured trends were not a result of systematic deactivation.
Cat. 15-Cat. 28 and Comparative catalysts 31 and 32 are tested in a liquid-phase reactor. Rate and selectivity measurements are performed in a trickle bed reactor comprising a stainless-steel tube (1.6 mm OD) containing 1,000 mg to 4,000 mg of catalyst (30 mesh to 60 mesh), which is held at the center of the reactor using Pyrex glass rods and packed glass wool. The reactor is heated with an aluminum clamshell including two heat cartridges that was controlled by an electronic temperature controller (an EZ-Zone available from Watlow). The reaction temperature is measured by a K-type thermocouple contained within a 3.2 mm stainless-steel sheath (available from Omega) that is coaxially aligned within the reactor and submerged within the aluminum clamshell. The system is pressurized up to 6.6 MPa using a dome loaded back pressure regulator (BPR), an Equilibar LF Series, available from Equilibar Precision Pressure Control which is controlled by an electronic pressure regulator (EPR), an Equilibar GP1 available from Equilibar Precision Pressure Control. The reactor pressure is monitored using a digital pressure gauge (available from Omega) and the EPR.
The gas flow rates of H2 (available from Airgas); and He (available from Airgas); are controlled using mass flow controllers (EL-FLOW High Pressure controllers available from Bronkhorst). The flow rate of liquid propyl acetate (C5H10O2) supplied by Sigma Aldrich, 537438, at ≥99.5%, is controlled using a high performance liquid chromatography (HPLC) pump (P-LST40B available from Chromtech) as the C5H10O2 fed through a stainless-steel tube (1.6 mm O.D. and 0.15 mm I.D.) within a cross flow of H2 and He.
Catalysts are pretreated in situ by heating to 423 or 573 K at 0.08 K s−1 and holding for 2 hr within flowing He (20 kPa) and H2 (81 kPa) at 50 cm3 min−1 prior to all catalytic measurements. The effluent of the reactor passes through a stainless-steel cooling chamber including cold water (at a temperature of ˜377 K), and then gas and liquid products are separated in a gas-liquid separator (GLS). The liquid products collected in the GLS are delivered by an HPLC pump to a high-pressure liquid sampling valve (LSV, Transcendent Enterprise Inc., PLIS-6890, 1 μL of injection volume) which is attached to on-line gas chromatography (Agilent, HP 7890B). At outlet of LSV, manual BPR (Swagelok) is installed so that the pressure of the liquid is maintained at 1,380 kPa to prevent the products from evaporation in the sampling system. The gas and liquid products are characterized using on-line gas chromatography (Agilent, HP 7890B). The GC is equipped with two capillary columns (DB-Wax UI, 60 m length, 0.25 mm I.D., 0.25 μm, available from Agilent) for liquid product, and a GS-GASPRO (a GC column, 60 m length, 0.32 mm I. D., available from Agilent) is connected to a flame ionization detector to quantify the concentrations of species. Sensitivity factors and retention times for all gas products and liquid products are determined using gaseous standards and a methanizer (Polyarc System, PA-SYC-411, available from Activated Research Company), respectively. Control of the reaction pressure and temperature, reactant and product flowrates, and the GC samplings are automated to allow for continuous measurements. Conversions are calculated on a carbon basis based on the amount of carbon that appears in the products. The carbon balance closes within±10%.
A kinetic investigation of the catalysts (Cat. 1-Cat. 28) used in the Examples for the direct selective reduction of propyl acetate (an example of a representative ester) with molecular hydrogen is carried out to determine the reaction pathway for converting propyl acetate to an ether. There are several products observed in the product stream coming out of fixed bed reactor via GC analysis. The various products include, for example, light hydrocarbons such C2-C3 alkane and alkene, ethanol, propanol, dipropyl ether, diethyl ether, ethyl propyl ether, acetic acid, and ethyl acetate. Based on this observation, it can be concluded that the reaction took place via several routes in the reactor including for example: (1) hydrogenolysis of propyl acetate to one ethanol and one propanol; (2) hydrolysis of propyl acetate, to from propanol, and acetic acid; (3) the alcohols can then undergo dehydration to form light hydrocarbons, as well as dehydration to form ether products, like dipropyl ether, diethyl ether and ethyl propyl ether; (4) transesterification of propyl acetate with ethanol to form ethyl acetate; and (5) the route of the present invention, Reaction Scheme (I), i.c., direct hydrogenation of propyl acetate with hydrogen to form ethyl propyl ether. Since the desired product is the ethyl propyl ether via direct hydrogenation of propyl acetate, the route of Reaction Scheme (I) of the present invention is the desired reaction pathway. It should be noted that ethyl propyl ether could also be formed from the above route (3). However, the route (3) above is not desired since route (3) above includes alcohol dehydration reactions, and such alcohol dehydration reactions are not selective for the formation of unsymmetric ether over symmetric ethers such as dipropyl ether or diethyl ether. While the present invention process is not limited to producing either a symmetric ether or an unsymmetric ether; advantageously, the present invention process, selectively and in a direct pathway, provides an unsymmetric ether when desired or needed.
In Inv. Ex. 1-14 and Comp. Ex. 29 and 30, the ether selectivity results using Cat. 1-Cat. 14 and 29 and 30 in the vapor phase are described in Table V. The hydrogenation was 10 carried out under the following reaction conditions: at a temperature of 356-503 K, a H2 pressure of 6.2 MPa, and a propyl acetate pressure at 10 kPa.
In Inv. Ex. 14-28 and Comp. Ex. 31-33, the hydrogenation is carried out in a liquid-phase reactor using the indicated catalysts. The reactions for Inv. Ex. are carried out under a H2 pressure of 6293 kPa, and at an ester pressure of 119 kPa. The reactions for Comp. Ex. are carried out under a H2 pressure of 4977 kPa, and an ester pressure at 1573 kPa. In liquid-phase reactor, the molar concentration of the ester is higher in the feed stream compared to vapor-phase reactor, and the ester is maintained in liquid state. The ether product selectivities are described in Table VI.
In Inv. Ex. 1-9, the selectivities for formation of dipropyl ether and diethyl ether from propyl acetate are, in most cases, lower than 3%, while the relative selectivity for ethyl propyl ether among all the three ether products in most cases is higher than 80%. Such performance indicates that substantially all of the ethyl propyl ether is formed based on a direct hydrogenation reaction pathway of propyl acetate, since the alcohol dehydration has no preference in selectivities for symmetric or unsymmetric ether.
The results of Inv. Ex. 1-Inv. Ex. 3 indicate that Pd deposited on FAU with 50 Si/Al ratio provides a direct hydrogenation of ester to ether. Pd metal loading have minor effects on ether selectivities. 0.5˜4 wt % Pd loading on FAU with Si/Al ratio can be effective for direct ester reduction.
The results of Inv. Ex. 4-Inv. Ex. 5 indicate that the preparation method via IWI and the uses of different precursors has minor impact on direction hydrogenation of ester to ether. Pd deposited on FAU50 prepared by IWI with either Pd(NH3)4Cl2·H2O or Pd(NH3)4(NO3)2 precursors can be effective for direct ester reduction.
The results of Inv. Ex. 6-Inv. Ex. 7 indicate that Pd deposited on FAU with 250 Si/Al ratio and on Y zeolite with 2 Si/Al ratio can be effective for direct ester reduction.
The results of Inv. Ex. 8 indicate that while Pd deposited on BEA250 works to a degree, it is less effective in performing direct ester hydrogenation.
The results of Inv. Ex. 8-Inv. Ex. 9 indicate that Pt and Rh deposited FAU50 catalysts can be effective for direct ester hydrogenation.
The results of Inv. Ex. 11-Inv. Ex. 14 indicate that while transition metals such as Ru, Ni, Cu and Co on FAU50 supports work to a degree, they are less effective for direct ester hydrogenation.
The best direct ester reduction performance observed in vapor-phase reaction is from Inv. Ex. 2 using Cat. 2 (4.00 wt % Pd deposited on FAU with 50 Si/Al ratio), giving 48.4% absolute ethyl propyl ether selectivity with 90.0% direct ether selectivity.
In Inv. Ex. 15-19, the absolute selectivity for ethyl propyl ether and the direct ether selectivity obtained indicate that metal deposited zeolite catalyst (Pd deposited on FAU50, Pt deposited on MOR10, Pt deposited on MOR120, Pt deposited FER10 and Pt deposited on CHA10) can be applied for direct ester reduction in liquid-phase reaction.
The results of Inv. Ex. 20-28 indicate that while Pt deposited on zeolites supports, such as MFI11.5 and BEA14 and Pd deposited zeolites supports, such as BEA14, MOR10, MFI11.5 and CHA10 and Ru deposited zeolites supports, such as MOR10, BEA250, and MFI180 all work to a degree, they are less effective in performing direct ester hydrogenation.
The results of Comp. Ex. 31, 32, 33 show that catalysts on Al2O3, SiO2 or Al2O3-SiO2 supports are not effective in direct ester hydrogenation. It is indicating that the microstructure of zeolite supports is important to catalyze direct ester hydrogenation.
The best direct ester reduction performance observed in liquid-phase reaction is from Inv. Ex. 19 using Cat. 19 (2.46 wt % Pt deposited on FER with 10 Si/Al ratio), giving 58.0% absolute ethyl propyl ether selectivity with 93.7% direct ether selectivity.
This invention discloses a series of metal deposited zeolite catalysts (e.g., Pd deposited FAU, Pt deposited FAU, Rh deposited FAU, Pt deposited MOR, Pt deposited CHA, Pt deposited FER), which are highly effective for direct ester hydrogenation to ether in both vapor-phase and liquid-phase. The best performance obtained is 48.4% absolute ethyl propyl ether selectivity with 90.0% direct ether selectivity in vapor-phase reaction, and 58.0% absolute ethyl propyl ether selectivity with 93.7% direct ether selectivity in liquid-phase reaction. Such results significantly surpass the prior art performance on transition metal/metal oxide catalysts (“Processes for Producing an Ether”, 63/107,739), which claimed >5% in absolute ethyl propyl ether selectivity and >85% direct ether selectivity.
| Filing Document | Filing Date | Country | Kind |
|---|---|---|---|
| PCT/US22/48649 | 11/2/2022 | WO |
| Number | Date | Country | |
|---|---|---|---|
| 63276311 | Nov 2021 | US |
