MULTIFUNCTIONAL CATALYST FOR THE CONVERSION OF CARBON DIOXIDE

Abstract

The present invention concerns a multifunctional catalyst for the conversion of CO.sub.2 into useful products, such as CO via the reverse water gas shift reaction. The catalyst according to the invention efficiently combined a water sorption functionality with at least one catalytic functionality into a single particle, by having a solid water sorbent impregnated with at least one metal capable of converting CO.sub.2 from a gaseous mixture comprising H.sub.2 and CO.sub.2. The catalyst according to the invention allows for higher selectivity in the conversion of CO.sub.2, at more lenient conditions in terms of temperature and pressure, and improved stability of the catalyst itself. The invention also concerns a process for converting CO.sub.2, utilizing the catalyst and the use of the catalyst in the conversion of CO.sub.2.

Claims

1.-15. (canceled)

16. A multifunctional catalyst, comprising a solid water sorbent impregnated with at least one metal capable of catalyzing the conversion of CO2 from a gaseous mixture comprising H2 and CO2, wherein the sorbent is a molecular sieve having a Si/Al molar ratio below 50 and containing pores having a diameter in the range of 3 to 20 Å and the metal content in the catalyst is not more than 40% based on total weight of the multifunctional catalyst.

17. The multifunctional catalyst according to claim 16, wherein the sorbent has a Si/Al molar ratio in the range of 1 and 2.

18. The multifunctional catalyst according to claim 17, wherein the sorbent has a Si/Al molar ratio is 1.

19. The multifunctional catalyst according to claim 16, wherein the sorbent is a zeolite selected from LTA zeolite, X-type zeolite and mixtures thereof.

20. The multifunctional catalyst according to claim 19, wherein the sorbent component comprises LTA-4A zeolite and/or zeolite 13×.

21. The multifunctional catalyst according to claim 16, wherein the pores have a diameter in the range of 4 to 8 Å.

22. The multifunctional catalyst according to claim 16, wherein the internal and external surfaces of the sorbent are impregnated with the at least one metal catalyst, and/or wherein the sorbent is impregnated with 0.1-40 wt %, based on total weight of the multifunctional catalyst.

23. The multifunctional catalyst according to claim 16, wherein the at least one metal is selected from the group consisting of Pt, Cs, Cu, Rh, Au, Zn, Co, Fe, Mo, Zn, Mn, Ru, Ir, Os, Ag, Al, Cr, Li, Na, K, Rb, Cs, Ce, Re, In, Zr, Ni, Mg, Al, Pd, Ga and mixtures thereof.

24. The multifunctional catalyst according to claim 23, wherein the at least one metal is selected from the group consisting of Pt, Zn, Fe, Cs, Cu and mixtures thereof.

25. The multifunctional catalyst according to claim 16, wherein the solid sorbent is further impregnated with a second metal capable of catalyzing the synthesis of dimethyl ether from methanol or diethyl ether from ethanol.

26. The multifunctional catalyst according to claim 16, wherein the solid sorbent is impregnated with the metal by wet impregnation.

27. A process for the conversion of CO2 from a gaseous feedstock comprising H2 and CO2, comprising the step of subjecting the gaseous feedstock to a multifunctional catalyst, comprising a solid water sorbent impregnated with at least one metal capable of converting CO2 from a gaseous mixture comprising H2 and CO2, wherein the sorbent is a molecular sieve having a Si/Al molar ratio below 50 and containing pores having a diameter in the range of 3 to 20 Å and the metal content in the catalyst is not more than 40% based on total weight of the multifunctional catalyst.

28. The process according to claim 27, wherein the conversion of CO2 involves a reverse water gas shift reaction (RWGS) to form CO, a hydrogenation reaction to form methanol or ethanol, or a Fisher-Tropsch reaction to form alkanes, a Fisher-Tropsch reaction to form alkenes, a Methanol to Olefins (MTO) reaction to form alkenes, an aromatization reaction to form aromatic hydrocarbons or a hydrogenation reaction to form methane, optionally wherein the hydrogenation reaction is accompanied with a dehydration reaction to convert methanol into dimethyl ether or ethanol into diethyl ether.

29. The process according to claim 28, wherein the conversion is a RWGS reaction.

30. The process according to claim 27, wherein the process takes place at a temperature in the range of 100-500° C., and/or wherein the reaction takes place at a pressure in the range of 0.5-20 MPa.

31. The process according to claim 27, wherein the molar ratio of H2 to CO2 in the feedstock is in the range of 10:1-1:5 and/or wherein the feedstock further comprises CO.

32. The process according to claim 27, further comprising a regeneration step of the catalyst wherein the pressure is reduced by at least 0.1×106 Pa and/or the temperature is increased by at least 20° C.

33. The process according to claim 27, wherein the sorbent component comprises LTA-4A zeolite and/or zeolite 13×.

34. The multifunctional catalyst according to claim 23, wherein the at least one metal is selected from the group consisting of Pt, Zn, Fe, Cs, Cu and mixtures thereof.

35. The multifunctional catalyst according to claim 16, wherein the solid sorbent is impregnated with the metal by wet impregnation.

Description

DETAILED DESCRIPTION

[0025] Accordingly, a first aspect of the present invention relates to a multifunctional catalyst for the conversion of CO.sub.2. The catalyst comprises a solid water sorbent impregnated with at least one metal capable of catalysing the conversion of CO.sub.2 from a gaseous mixture comprising H.sub.2 and CO.sub.2. The content of metal catalyst in the impregnated solid water sorbent is not more than 40% based on weight of the catalyst. The sorbent is a molecular sieve having a Si/Al molar ratio below 50 and contains pores (or cages) having a diameter in the range of 3 to 20 Å.

[0026] In a second aspect, the present invention concerns the use of the catalyst according to the invention as catalyst for the conversion of CO.sub.2. In a third aspect, the present invention concerns a process for the conversion of CO.sub.2 from a gaseous feedstock comprising H.sub.2 and CO.sub.2, comprising contacting the gaseous feedstock with the catalyst according to the invention.

[0027] Whenever reference is made to the catalyst according to the invention, or preferred embodiments thereof, this equally applies to the use and processes according to the invention. Also, whenever reference is made to the use according to the invention, this equally applies to the processes according to the invention.

The Catalyst

[0028] First and foremost, the present invention concerns a multifunctional catalyst for the conversion of CO.sub.2. The catalyst according to the invention is a multifunctional catalyst, comprising a solid water sorbent impregnated with at least one metal capable of converting CO.sub.2, wherein the sorbent is a molecular sieve having a Si/Al molar ratio below 50 and containing pores having a diameter in the range of 3 to 20 Å and the metal content in the catalyst is not more than 40% based on total weight of the multifunctional catalyst. The multifunctional nature of the catalyst resides in its sorption capacity of water and its catalytic capacity of converting CO.sub.2 and optionally the further conversion of the intermediate products from CO.sub.2. Hence, the catalyst according to the invention is at least bifunctional, but may have further functionalities. Preferably, the catalyst is bifunctional or trifunctional.

[0029] Catalytic particles that catalyse the conversion of CO.sub.2, typically by lowering the activation energy needed to perform the conversion reaction which increases the kinetics of the reaction. In the presence of a catalyst, the reaction would normally at best continue until the equilibrium at the process conditions is reached, and the product obtain is the equilibrium mixture, which will this contain substantial amounts of reactant(s). Sorbent particles shift the equilibrium be removing one the products, in the context of the present invention water, from the product mixture, such that the equilibrium will shift more and more towards the products. The product mixture obtained will thus mainly contain converted CO.sub.2 (e.g. CO in the context of the RWGS reaction), and significantly less reactant(s). Also, water will largely be absent from the product mixture, as it is sorbed on the sorbent. The uses and processes according to the invention can thus be referred to as “sorption-enhanced”. However, no shift of the equilibrium occurs if there is no reaction at all. Hence, the effect of the sorbent cannot occur in the absence of the catalyst. The present invention combines these two functionalities in a single catalytic particle, wherein catalysis of the conversion of CO.sub.2 occurs while at the same time, on the same particle, one of the reaction products, typically water, is sorbed and removed from the reaction mixture that is moving towards equilibrium. Thus, the multifunctional catalyst can only function in case the surface of the particles contains both catalytic sites, by virtue of the impregnated metal, and sorption sites, which are typically present in molecular sieves in their cationic form. Hence, the metal content in the catalyst should not be more than 40%, preferably not more than 30%, based on of total weight of the multifunctional catalyst. Alternatively, the amount of metal is defined as at most 75%, preferably at most 50%, of the surface of the sorbent is impregnated with metal.

[0030] The multifunctional catalyst according to the invention gives high selectivities towards the products of the conversion of CO.sub.2, even at high pressures of 15-200 bar and relatively low temperatures such as 225-335° C. For example, the conversion of CO.sub.2 into CO via the RWGS reaction ran smoothly at 300° C. at high pressures of 15-25 bar. Furthermore, the multifunctional catalyst according to the invention is homogenous, in that it contains one type of particles, while conventional multifunctional catalyst systems contain one type of particle with sorbent and other type(s) of particle(s) with catalyst. Such a heterogeneous particulate gives problems with uniformity, separation, scalability and instability of the system. Such problems are primarily caused by differences in hardness between the hard catalyst particles and soft sorbent particles as well as mass transfer limitations. For example, when such a convention system of sorbent particles and catalyst particles are mixed together in a fluidized bed reactor, the sorbent particles will quickly pulverize into a powder and lose their sorption capacity. This is avoided with the multifunctional catalyst according to the invention, which contains one type of particles, sorbent impregnated with metal catalyst.

[0031] The inventors have achieved these effects by using a multifunctional reactive sorbent, which is a material that both catalyses the conversion of CO.sub.2 and adsorbs water. The multifunctional reactive sorbent comprises a specific water sorbent and a metal impregnated on the surface of the sorbent, preferably in the pores thereof. The multifunctional catalyst thus contains both reactive pockets wherein CO.sub.2 is converted, as well as areas wherein H.sub.2O can be adsorbed. Since the sorbent and catalyst are thus integrated into one material, the conversion of CO.sub.2 can easily be scaled up.

[0032] The multifunctional catalyst is a solid material, preferably a granulate. The granules may be spherical, structured (e.g. composites, tandem, hybrid), pellets and the like. Advantageously, the granulate contains particles having a diameter of 150-600 μm, preferably in the range of 200-450 μm. The skilled person understands how to size the particulate based on internal and external mass transfer criteria. Thus, in a preferred embodiment, the catalyst according to the invention is a particle comprising a sorbent impregnated with at least one metal capable of catalyzing the conversion of CO.sub.2.

[0033] The sorbent part of the catalysts is a solid water sorbent. The sorbent is a molecular sieve. Even though any molecular sieve capable of sorbing water molecules is suitable in the context of the present invention, preferably a zeolite (microporous or mesoporous or mixtures thereof) is used as sorbent. Zeolites having a pore diameter in the range of 3 to 20 Å are known to the skilled person for the selective sorption of water molecules. Preferably, the pores have a diameter in the range of 4 to 9 Å. The pore structure of the zeolites may also contain cages, which could be beneficial in steering the product selectivity towards the desired product.

[0034] The skilled person understands that not all zeolites are water sorbents, and the zeolite that is used in the context of the present invention classifies as “solid water sorbent”, i.e. a zeolite capable of adsorbing water. Zeolites in their protonated (acidic) or ammonium form are normally not capable of adsorbing water, and thus are not considered in the context of the present invention. Protonated zeolites have protons associated to the negatively charged framework of the zeolite. In other words, the sites available for cations to be embedded in the zeolite framework are occupied by protons. This protonated form of a zeolite is well-known and correspond to zeolites in their acidic form, wherein the acidity refers to Brønsted acidity. Protonated zeolites are not to be confused with basic zeolites, which have cations, no protons, at these sorption sites. These cations, typically cations of group 1 and 2 metals, provide the sorbent with water adsorption capacity. These zeolites may also be referred to as being “exchanged”, which refers to the cation taken the place of the protein. As the skilled person will appreciate, water typically adsorbs to (metal) cations located at those sorption sites (see e.g. Ezzi and Ma, Equilibrium Adsorption Isotherm Mechanism of Water Vapor on Zeolites 3A, 4A, X, and Y, Proceedings of the ASME 2017 International Mechanical Engineering Congress & Exposition, Nov. 3-9, 2017, Tampa, Fla., USA). The form of zeolites wherein the cations, not protons, are present on the sorption sites is referred to as “cationic” or “basic”. Thus, in an especially preferred embodiment, the zeolite is in cationic form. In a preferred embodiment, the zeolite comprises Na.sup.+, Li.sup.+, K.sup.+, Ba.sup.2+, Mg.sup.2+, Ca.sup.2+ or mixtures thereof.

[0035] In a preferred embodiment, the solid water sorbent is a zeolite selected from LTA zeolite, FAU X-type, FAU Y-type including ultrastable Y (USY), EMT, BEA, CHA (ALPO, APSO, SAPO, SSZ-13), AFI (ALP04-5, SAPO-5, SSZ-24) zeolite, as well as and mixtures and derivatives (dealuminated, alkaline and acid treated, promoted and stabilized with rare earth metals, hybrids, partially exchanged etc.), and natural counterparts thereof. Preferred zeolites are selected from LTA zeolites, X-type zeolites and AFI, more preferably from USY, LTA zeolites and X-type zeolites. In an especially preferred embodiment, the zeolite is selected from USY, LTA-4A, EMT, AFI and 13×. Because of its larger pores, zeolite USY, EMT, AFI and 13× are especially suited for making larger molecules, such as methanol or olefins. Therefore, in one embodiment, the sorbent is USY, EMT, AFI and 13×when the conversion of CO.sub.2 is not into CO as the intended end-product, as in the RWGS reaction, preferably wherein the end product is methanol, ethanol, olefins or dimethyl ether.

[0036] Zeolite LTA (Linde Type A) belongs to the family of aluminosilicate molecular sieves. It is characterized by the formula [Na.sup.+.sub.12(H.sub.2O).sub.27].sub.8 [Al.sub.12Si.sub.12 O.sub.48].sub.8 (International Zeolite Association-IZA). Sodium ions in zeolite A can be exchanged with other cations such as lithium (Li-LTA), potassium (K-LTA), or calcium (Ca-LTA). When one ion is exchanged by the other, the size of the pore opening changes. Exchanging the potassium ions in zeolite LTA-3A with the smaller sodium ions results in zeolite LTA-4A having an increased diameter of the pores, which determines its accessibility for molecular permeation. When sodium is exchanged with Ca.sup.2+ in a 2:1 fashion, zeolite 5A is obtained.

[0037] Zeolite X belongs to the family of aluminosilicate molecular sieves with a faujasite-type structure (FAU). It is characterized by the formula [(Ca.sup.2+,Mg.sup.2+ Na.sup.+2).sub.29(H.sub.2O).sub.240] [Al.sub.58Si.sub.134 O.sub.384]—FAU (International zeolite association—IZA). Structurally, LTA zeolites and X-type are relatively similar. Both consist of p-cages, containing square and hexagon faces. In both types these cages are linked to create very hydrophilic supercages. The inventors obtained optimal results with LTA-4A zeolite and zeolite 13×.

[0038] The molecular sieve used as sorbent in the catalyst of the invention has a Si/Al molar ratio below 50, such as in the range 1-50. The preferred Si/Al molar ratio may depend on the specific product of the CO.sub.2 conversion reaction, as further specified below. Generally speaking, it is preferred that the Si/Al ratio is below 10, preferably below 5, more preferably in the range of 1-4.0, most preferably the Si/Al ratio is in the range of 1-2. In an alternative preferred embodiment, the Si/Al ratio is in the range of 10 50, more preferably in the range of 20-30. With higher Si/Al molar ratios, the hydrophilicity and water sorption capacity of the basic zeolite sorbent is reduced and the multifunctionality of the catalyst of the invention is impaired. Zeolites having a Si/Al ratio above 2 or even 10 are suitable. Their reduced Al content leads to a slightly lower water sorbent capacity.

[0039] In the protonated, acidic form of the zeolite, the reduced Al content increases the acid site strength of the remaining protonated sites to some extent, which is beneficial for (alcohol) dehydration to e.g. dimethyl ether or diethyl ether. Hence, especially for the trifunctional catalysts defined further below, the Si/Al ratio may be above 2.5, such as in the range of 2.5-50, preferably in the range 5-30. In case the conversion of CO.sub.2 involves dehydration, the zeolite is preferably in a partly exchanged state with both protonic acid sites (beneficial for dehydration) and basic sites (beneficial for adsorption). The ratio of acidic (protonated) sites to basic sites is at most 25/75, preferably at most 10/90, most preferably at most 5/95. Preferably, the zeolite is mostly in the cation (exchanged) state and the acidity may be present in the form of Lewis acid sites that relate to so-called extra-framework aluminium sites generated by dealumination or other structural defects. If needed, the Si/Al ratio could be increased by leaching of Al from the zeolite (dealumination). Such a procedure is known to the skilled person.

[0040] The sorbent is impregnated with at least one metal capable of catalysing the conversion of CO.sub.2 from a gaseous mixture comprising H.sub.2 and CO.sub.2. In the context of the present invention, it is not required that the entire surface of the sorbent is impregnated. Preferably, the sorbent is impregnated with 0.1-40 wt %, more preferably 1-30 wt % of metal, based on total weight of the catalyst. The optimal metal content may vary depending on the desired product and the specific metal or combination of metals used. In a preferred embodiment, at least the internal surface (the pores) are impregnated, more preferably both the internal surface (within the pores) and the external surface (the outside of the particles) are impregnated with the metal.

[0041] Several reactions are known to convert CO.sub.2 into useful products. Such useful products may be selected from such as CO, lower alcohols (e.g. methanol, ethanol), lower ethers (e.g. dimethyl ether, diethyl ether), alkanes. In a preferred embodiment, the conversion of CO.sub.2 involves the reverse water gas shift (RWGS) reaction, most preferably the conversion of CO.sub.2 is the RWGS reaction and the product is CO. A further suitable reaction is the hydrogenation of CO.sub.2 into alcohols, preferably methanol or ethanol, most preferably methanol. A further suitable conversion of CO.sub.2 involves the hydrogenation of CO.sub.2 into alcohols and the subsequent dehydration into ethers, preferably dimethyl ether or diethyl ether, most preferably dimethyl ether. A further suitable conversion of CO.sub.2 involves Fischer-Tropsch reaction to form hydrocarbons or alkanes.

[0042] The skilled person is capable of selecting a metal, or combination of metals, that is capable of catalysing the desired conversion of CO.sub.2. In a preferred embodiment, the sorbent is impregnated with at least one metal selected from the group consisting of Pt, Cs, Cu, Rh, Au, Zn, Co, Fe, Mo, Zn, Mn, Ru, Ir, Os, Ag, Al, Cr, Li, Na, K, Rb, Cs, Ce, Re, In, Zr, Ni, Mg, Al, Pd, Ga and mixtures thereof, preferably from the group consisting of Pt, Cu, Rh, Ir, Ru, Pd, Os, Cs, Fe and Zn. More preferably, the metal is selected from the group consisting of Pt, Cs, Cu, Fe, Zn, Rh and mixtures thereof. Even more preferably, the metal is selected from the group consisting of Pt, Cs, Cu, Fe and mixtures thereof. In a further preferred embodiment, the metal is Pt or a mixture comprising Pt, most preferably Pt or a mixture comprising Pt and Cs. Most preferably, the metal is Pt or a mixture of Pt, Cs and Cu or Fe.

[0043] In one especially preferred embodiment, the sorbent is impregnated with Pt. When Pt is present, the molecular sieve is preferably impregnated with 0.1-8 wt %, preferably 0.2-3 wt %, more preferably 0.5-2 wt % Pt, based on the total weight of the multifunctional catalyst. When Pt is present, the metal that is impregnated on the sorbent may contain one or more further metals, preferably selected from the group consisting of Rh, Ru, Ir, Pd, Os, Fe, Cs, Cu, Zn, or other transition metals.

[0044] In another especially preferred embodiment, the sorbent is impregnated with Cu, preferably a combination of Cu with Cs and/or Zn. When Cu is present, the molecular sieve is preferably impregnated with 1-40 wt %, preferably 2-30 wt %, more preferably 5-25 wt % Cu, based on the total weight of the multifunctional catalyst. The inventors have found that the impregnation of the solid water sorbent with a mixture of Cs and Cu or Pt is particularly advantageous for RWGS. Although the inventors do not wish to be bound by theory, it is believed that the presence of Cs blocks the side reactions that may lead to the formation of methanol or dimethyl ether, as such increasing the selectivity of the RWGS reaction to convert CO.sub.2 in CO. In case both Cu and Cs are present, it is preferred that the multifunctional catalyst comprises a molecular sieve impregnated with Cu and Cs in a molecular ratio of 47:1 to 1:1, preferably 6:1 to 2:1. In case both Cu and Zn are present, it is preferred that the multifunctional catalyst comprises a molecular sieve impregnated with Cu and Zn in a molecular ratio of 4:1 to 1:2, preferably 2:1 to 2:3.

[0045] The inventors have found that the formation of the desired product can be optimized by selecting the optimal combination of a metal (or combination of metals) and sorbent. In other words, the catalyst particle can be tuned to the formation of the desired product. Examples of such optimal combinations are provided below. As such, the present invention provides a versatile approach towards the conversion of CO.sub.2, wherein the metal (or combination of metals) and the sorbent may be selected to provide optimal conversion of CO.sub.2 into the desired product.

[0046] In an especially preferred embodiment, the conversion of CO.sub.2 involves the RWGS reaction. In the context of this embodiment, the metal is capable of catalysing the RWGS reaction. Preferably, the metal is selected from the group consisting of Pt, Cs, Cu, Rh, Au, Zn, Co, Fe, Mo and mixtures thereof, more preferably, the metal is selected from the group consisting of Pt, Cs, Cu, Fe and mixtures thereof. Most preferably, the metal is Pt, Pt or a mixture of Cs and Cu, or a mixture of Pt, Cs and Cu or Fe. In another preferred embodiment, the metal comprises at least Cs, which was found to be suitable to suppress hydrogenation of CO to produce methanol and as such increase the yield of CO. Preferably, the Cs content is in the range of 0.1-2.5 wt %, preferably 1-2 wt %, based on total weight of the catalyst.

[0047] In an especially preferred embodiment, the metal is Pt. This metal is optimally combined with a zeolites having a pore diameter in the range of 3 to 5 Å, preferably of about 4 Å, as sorbent. In another especially preferred embodiment, the metal is a mixture of Cu and Cs. This metal is optimally combined with a zeolites having a pore diameter in the range of 3 to 10 Å, preferably of about 4 Å, as sorbent. The Si/Al ratio for performing a RWGS reaction is preferably below 2.5, more preferably in the range of 1-2. Preferably, the sorbent in the multifunctional catalyst for the RWGS reaction is an LT-4A zeolite or 13×zeolite, most preferably an LT-4 Å zeolite. The inventors have obtained excellent results in catalysing the RWGS reaction with zeolite LTA-4 Å or 13×, impregnated with 1-4 wt % Pt, based on total weight of the catalyst.

[0048] In an alternative preferred embodiment, the conversion of CO.sub.2 involves hydrogenation to form methanol. In the context of this embodiment, the metal is capable of catalysing the hydrogenation of CO.sub.2. Preferably, the metal is selected from the group consisting of Cu, Au, Ag and mixtures thereof, more preferably from the group consisting of Cu, Au and mixtures thereof, most preferably the metal is Au. Preferably, the metal in the context of this embodiment does not comprise Cs. The metal is optimally combined with a zeolites having a pore diameter in the range of 5-10 Å, preferably in the range of 7-9 Å, as sorbent. Most preferably, the sorbent in the multifunctional catalyst for the hydrogenation of CO.sub.2 into methanol is a zeolite having a Si/Al ratio in the range of 1-2, more preferably in the range 1-1.5. The sorbent is preferably selected from the group consisting of faujasite, zeolite 13×, zeolite Y, BEA, AFI, EMT zeolites, more preferably from the group consisting of faujasite, zeolite 13×, zeolite Y, BEA, EMT zeolites.

[0049] In an alternative preferred embodiment, the conversion of CO.sub.2 involves hydrogenation to form ethanol. Herein, two molecules of methanol or one molecule of methanol and one molecule of CO couple to form a carbon-carbon bond. Zeolites with high acid site strength are preferred, such as dealuminated zeolites with Si/Al>2.5. In the context of this embodiment, the metal is capable of converting CO.sub.2, optionally together with CO, into ethanol. Preferably, the metal is selected from the group consisting of Cu, Zn, Mn, Rh, Ru, Pt, Ir, Os, Au, Ag, Al, Co, Cr, Fe, alkali metals and mixtures thereof, more preferably, the metal is selected from the group consisting of Cu, Zn, Cs, Li, K, Al, Fe, Rh and mixtures thereof. In a preferred embodiment, the metal is a mixture of (i) Cu and/or Zn, (ii) one or more of Cs, Li, K and Al and (iii) Fe and/or Rh. This metal is optimally combined with a zeolites having a pore diameter in the range of 5-10 Å, preferably in the range of 7-9 Å, as sorbent. Most preferably, the sorbent in the multifunctional catalyst is a zeolite having a Si/Al ratio in the range of 3-5. The sorbent is preferably selected from the group consisting of zeolite BEA, AFI, EMT and FAU (ultrastabilized Y (USY), dealuminated X), more preferably from the group consisting of zeolite BEA and FAU (ultrastabilized Y (USY), dealuminated X).

[0050] In an alternative preferred embodiment, the conversion of CO.sub.2, optionally together with CO, involves hydrogenation to form alkanes via Fischer-Tropsch synthesis. In the context of this embodiment, the metal is capable of converting CO.sub.2 into hydrocarbons. Preferably, the metal is selected from the group consisting of Co, Fe, Mo, Ru and mixtures thereof, and may further comprise K, Na, Li, Cs, Mn and mixtures thereof. These metals are optimally combined with a zeolite having a pore diameter in the range of 5-10 Å, preferably in the range of 7-9 Å, as sorbent. Most preferably, the sorbent in the multifunctional catalyst for Fischer-Tropsch synthesis is a zeolite having a Si/Al ratio above 5. The sorbent is preferably selected from the group consisting of zeolite BEA, AFI, EMT, FAU (Y including ultrastabilized Y (USY), 13×(including dealuminated 13×)), more preferably from the group consisting of zeolite BEA, FAU (Y including ultrastabilized Y (USY), 13×(including dealuminated 13×)).

[0051] In an alternative preferred embodiment, the conversion of CO.sub.2, optionally together with CO, involves hydrogenation to form alkenes via Fischer-Tropsch synthesis. In the context of this embodiment, the metal is capable of converting CO.sub.2 into hydrocarbons. Preferably, the metal is selected from the group consisting of Co, Fe, Mo, Ru and mixtures thereof, and may further comprise K, Ce, Na, Li, Zn, Cs, Mn or mixtures thereof, preferably comprise K, Ce, Na, Li, Cs, Mn or mixtures thereof, to promote the formation of olefins. The skilled person is capable to fine-tune the amount of the metals towards the formation of alkenes over alkanes. This metal is optimally combined with a zeolite having a pore diameter in the range of 5-13 Å, preferably in the range of 7-9 Å, as sorbent. Most preferably, the sorbent in the multifunctional catalyst is a zeolite having a Si/Al ratio above 5. The sorbent is preferably selected from the group consisting of zeolite CHA, BEA, AFI, EMT, FAU (Y including ultrastabilized Y (USY), 13×(including dealuminated 13×)), more preferably from the group consisting of zeolite CHA, BEA, FAU (Y including ultrastabilized Y (USY), 13×(including dealuminated 13×)).

[0052] In an alternative preferred embodiment, the conversion of CO.sub.2, optionally together with CO, involves hydrogenation to form alkenes via Methanol to Olefins (MTO) synthesis. In the context of this embodiment, the metal is capable of converting CO.sub.2 into C.sub.2-C.sub.4 olefins. Preferably the metal is selected from the group consisting of Cu, Re, In, Zr, Au, Co, Fe, Mo, Ru, Mg, Ca and mixtures thereof, preferably from the group consisting of Cu, Re, In, Zr, Au, Co, Fe, Mo, Ru and mixtures thereof, and may further comprise K, Ce, Na, Li, Cs, Mn and mixtures thereof to promote the formation of olefins. These metals are optimally combined with a zeolite having a pore diameter in the range of 4-13 Å, preferably in the range of 4-9 Å, as sorbent. Most preferably, the sorbent in the multifunctional catalyst is a zeolite having a Si/Al ratio above 5. The sorbent is preferably selected from the group consisting of zeolite CHA, BEA, EMT, AFI, FAU (Y including ultrastabilized Y (USY), 13×(including dealuminated 13×)), more preferably from the group consisting of zeolite CHA, BEA, EMT, FAU (Y including ultrastabilized Y (USY), 13×(including dealuminated 13×)).

[0053] In an alternative preferred embodiment, the conversion of CO.sub.2, optionally together with CO, involves hydrogenation to form methane. Preferably the metal is selected from the group consisting of Ni, Co, Mg, Al, Rh, Pt, Ru, Re, In, Zr, Fe, Mo, Mn and mixtures thereof, and may further comprise K, Ce, La, Na, Li, Cs, and mixtures thereof. These metals are optimally combined with a zeolite having a pore diameter in the range of 4-13 Å, preferably in the range of 4-9 Å, as sorbent. Most preferably, the sorbent in the multifunctional catalyst is a zeolite having a Si/Al ratio 1.5-4. The sorbent is preferably selected from the group consisting of zeolite CHA, BEA, EMT, AFI, FAU (Y including ultrastabilized Y (USY), 13×(including dealuminated 13×)), more preferably from the group consisting of zeolite CHA, BEA, EMT, FAU (Y including ultrastabilized Y (USY), 13×(including dealuminated 13×)).

[0054] In an alternative preferred embodiment, the conversion of CO.sub.2, optionally together with CO, involves hydrogenation to form aromatics. In the context of this embodiment, the metal is capable of converting CO.sub.2 into aromatic hydrocarbons. Preferably the metal is selected from the group consisting of Ga, Mo, Cu, Re, In, Zr, Au, Co, Fe, Mo, Ru and mixtures thereof, and may further comprise K, Na, Li, Cs, Mn and mixtures thereof. These metals are optimally combined with a zeolite having a pore diameter in the range of 4-13 Å, preferably in the range of 4-9 Å, as sorbent. Most preferably, the sorbent in the multifunctional catalyst is a zeolite having a Si/Al ratio above 5. The sorbent is preferably selected from the group consisting of zeolite CHA, BEA, EMT, AFI, FAU (ultrastabilized Y (USY), dealuminated X), more preferably from the group consisting of zeolite CHA, BEA, EMT, FAU (ultrastabilized Y (USY), dealuminated X).

[0055] The multifunctional catalyst according to the invention is at least bifunctional, wherein the two functionalities are the sorption capacity and the catalytic capacity. In an especially preferred embodiment, the catalyst contains more functionalities, and preferably is trifunctional. In this embodiment, the sorbent is impregnated with a mixture of at least two metal catalysts, each of which has a different functionality.

[0056] In an especially preferred embodiment, the conversion of CO.sub.2 involves hydrogenation to form methanol and the catalyst according to the invention contains a catalyst that is capable of catalysing the dehydration of methanol to form dimethyl ether. As such, the catalyst according to the invention is capable of efficiently converting CO.sub.2 and H.sub.2 into dimethyl ether in a single pass. One metal is capable of catalyzing the formation of methanol from a gaseous mixture comprising H.sub.2 and CO.sub.2, optionally together with CO, and another catalyst that is capable of catalysing the conversion of the thus formed methanol into dimethyl ether. The preferred catalyst for the formation of methanol is already defined above. In a preferred embodiment, the sorbent is optimized for catalyzing the dehydration of methanol. In this embodiment, the sorbent is preferably selected from faujasite (e.g. 13×, zeolite Y), BEA, EMT zeolites, LTA, which are preferably subjected to dealumination or desilication and stabilization treatments as known in the art. Additionally or alternatively, the bifunctional reactive sorbent is impregnated with a further metal (“promoted”), in order to enable or promote the catalysis of dehydrating methanol to form dimethyl ether. The dehydration catalyst can be promoted by depositions of Cu, Mn, Zn and rare earth metal (e.g. Ce, La), alkali metals (Li, K), phosphor (P) or mixtures thereof, e.g. Cu—Mn—Zn supported (Zr—)Y catalyst.

[0057] In an alternative preferred embodiment, the conversion of CO.sub.2 involves hydrogenation to form ethanol and the catalyst according to the invention further contains a catalyst that is capable of catalysing the dehydration of ethanol to form diethyl ether. As such, the catalyst according to the invention is capable of efficiently converting CO.sub.2, optionally together with CO, and H.sub.2 into diethyl ether in a single pass. One catalyst is capable of catalyzing the formation of ethanol from a gaseous mixture comprising H.sub.2 and CO.sub.2, and another catalyst is capable of converting the thus formed ethanol into diethyl ether. The preferred catalyst for the formation of ethanol is already defined above. In a preferred embodiment, the sorbent is optimized for catalyzing the dehydration of ethanol. In this embodiment, the sorbent is preferably selected from faujasite (e.g. 13×, zeolite Y), BEA, EMT zeolites, LTA, which are preferably subjected to dealumination and stabilization treatments as known in the art. Additionally or alternatively, the bifunctional reactive sorbent is impregnated with a further metal (“promoted”), in order to enable or promote the catalysis of dehydrating methanol to form dimethyl ether. Further deposition of precious and transition metals can prevent formation of ethylene and boost selectivity towards diethyl ether and improve stability.

[0058] The catalyst according to the invention may also be part of a catalyst system, comprising catalytic particles according to the invention and further catalytic particles which catalyse another reaction. Especially the bifunctional catalyst as defined above may be comprised in a catalyst system, wherein a second catalytic particulate is present. For example, the further catalytic particles may be methanol dehydration catalyst particles, that catalyse the dehydration of methanol to dimethyl ether, or ethanol dehydration catalyst particles, that catalyse the dehydration of ethanol to diethyl ether. Such methanol and ethanol dehydration catalytic particles are known in the art, e.g. from Ind. Eng. Chem. Res. 1992, 31, 4, 1035-1040. Typically, these catalyst particles contain a zeolite having a Si/Al ratio above 10, such as in the range of 20-50. Suitable zeolites include ZSM-5; MOR, SUZ-4, FER.

[0059] As such, a gaseous feed comprising CO.sub.2, optionally together with CO, and H.sub.2 can be fed to a reactor comprising the catalyst system according to the invention, and be converted into dimethyl ether in a single pass.

[0060] The multifunctional catalyst according to the invention can be prepared by methods known in the art, e.g. in Catalyst Preparation: Science and Engineering, Regalbuto (2007), CRC Press (ISBN 978-0-8493-7088-5), or in U.S. Pat. Nos. 3,226,339 and 3,527,836. In a preferred embodiment, the catalyst according to the invention is obtainable by, or obtained by, the following process: [0061] (i) contacting a solid water sorbent with a solution comprising at least one metal capable of catalysing the synthesis of CO from a gaseous mixture comprising H.sub.2 and CO.sub.2 via RWGS; [0062] (ii) drying at a temperature in the range of 90-150° C., preferably 95-115° C.; [0063] (iii) calcinating at a temperature in the range of 200-500° C., preferably 250-450° C., more preferably 300-400° C.; [0064] (iv) activating the catalyst under reducing atmosphere.

[0065] The sorbent subjected to step is typically in powder form. Preferably, the sorbent powder has an average particle size in the range of 50-200 μm, more preferably in the range of 100-150 μm.

[0066] In step (i), the sorbent is impregnated with the metal solution. Since the final catalyst should contain both sorption sites and catalytic sites, the impregnation step should take care that not all sorption steps are blocked by the metal. In other words, the impregnation of step (i) ensures that the metal content in the catalyst is not more than 40% based on of total weight of the multifunctional catalyst, preferably not more than 30% based on total weight of the catalyst. Alternatively, the amount of metal is defined as at most 75%, preferably at most 50%, of the surface of the sorbent being impregnated with metal.

[0067] An appropriate impregnation method should be selected to achieve such partial coverage of the sorbent surface with metal. Typically, incipient wetness impregnation is not suitable, as that provides the sorbent with the metal homogenously distributed over its surface, thereby blocking all water sorption sites (if any). Such a catalyst would have catalytic activity but no sorption capacity. A preferred impregnation technique is wet impregnation, wherein the metal is added to the sorbent in a volume that surpasses the total pore volume of the sorbent. As such, metal clusters will form on the surface of the sorbent during the drying of step (ii), when the solvent is removed, leaving parts of the surface free of metal and part of the surface covered by metal. Such wet impregnation is a technique known by the skilled person. Thus, in a preferred embodiment, the catalyst according to the invention is obtainable by or obtained by a wet impregnation method, most preferably involving steps (i)-(iv) defined above.

[0068] Thus, the volume of the solution is normally 1.1 to 10 times, preferably 1.5 to 5 times, the pore volume of sorbent. The pore volume of the material may be determined by N.sub.2 adsorption-desorption type of experiments or by a parallel wetting experiment to determine the level of dryness achieved by the event of capillary condensation as a function of the volume added. In a preferred embodiment, the volume of the solution is 1.1 to 4 times, more preferably 1.5 to 3.5 times, even more preferably 1.6-3, such as 2 to 3 times or 1.6 to 2 times, the pore volume of sorbent. Most preferably, the volume of the solution is 1.6 to 2 times the pore volume of sorbent. The metal is typically dissolved in water in salt form, such as Pt(NH.sub.3).sub.4(NO.sub.3).sub.2. This step is typically performed within a few minutes at room temperature and atmospheric pressure. The volume of the solution and the concentration of the metal therein should be chosen such that the final catalyst, obtained in step (iii), contains metal in an amount of at most 40 wt % based on total weight of the catalyst.

[0069] In step (ii), the solvent is removed, to obtain a dried layer of metal precursor on the surface of the sorbent. Drying is typically performed at a temperature in the range of 90-150° C. in an oven, preferably in the range of 95-105° C. This step is usually performed at atmospheric pressure under air atmosphere. The drying step (ii) ensures that the solvent is removed and metal salt clusters are formed on the surface of the sorbent, which is crucial for bi- or multifunctionality of the catalyst according to the invention.

[0070] In step (iii), the metal is converted into its oxide by calcination, which ensures dispersion of the metal over the surface of the sorbent. Any means for calcination known in the art may be sued. Calcination is typically performed at a temperature in the range of 200-500° C., preferably in the range of 250-450° C., more preferably in the range of 300-400° C. This step is usually performed in an oven under air atmosphere with a ramp rate of 5° C./min to the designated temperature, the temperature that was allowed to reduce after 6 hours to room temperature.

[0071] In step (iv), the metal precursor is converted into the catalytically active form of the metal. The skilled person is familiar with activation of metal catalysts. Activation is performed under a reducing atmosphere, typically an atmosphere comprising hydrogen gas. The samples are typically heated in-situ to 180° C. at 5° C./min under 10% hydrogen in N.sub.2, after which the heating rate was reduced to 2° C./min up to 325° C. followed by a 30 minute temperature hold and subsequently cooled down to reaction temperature.

[0072] During step (iv), the catalyst is activated, and is typically performed as last step shortly prior to the CO.sub.2 conversion reaction, such as the RWGS reaction, is carried out. Normally, the activation is performed within the RWGS reactor as first step of the RWGS process. The process may further comprise a step wherein the dried catalyst of step (ii) is loaded into a reactor, e.g. a RWGS reactor, wherein step (iii) is performed.

[0073] If needed, the dried catalyst of step (ii) may be converted into a granulate, before it is subjected to the reactor. This conversion may be performed by compressing the dried catalyst and broken into granules, e.g. by milling. The compression step may be performed using a hydraulic press and a compression force of for example 2-6 atm.

[0074] This process, comprising steps (i)-(iv), is particularly advantageous, because it enables the impregnation of the solid water sorbent with a metal catalyst without significant reduction of its water sorption capacity. In one aspect, the invention also concerns the process for preparing the catalyst as defined herein.

Process

[0075] The invention further concerns a process for the conversion of CO.sub.2 from a gaseous feedstock comprising H.sub.2 and CO.sub.2, comprising the step of subjecting the gaseous feedstock to the multifunctional catalyst according to the invention. The process may also be referred as being for the formation of a species selected from CO, methane, methanol, ethanol, dimethyl ether, diethyl ether, alkanes, alkenes or aromatics. The conversion of CO.sub.2 preferably involves a reverse water gas shift reaction (RWGS) to form CO, a hydrogenation reaction to form methanol or ethanol, a Fisher-Tropsch reaction to form alkanes, a Fisher-Tropsch reaction to form alkenes, a Methanol to Olefins (MTO) reaction to form alkenes, an aromatization reaction to form aromatic hydrocarbons or a hydrogenation reaction to form methane, optionally wherein the hydrogenation reaction is accompanied with a dehydration reaction to convert methanol into dimethyl ether or ethanol into diethyl ether. In an especially preferred embodiment, the process is for the formation of CO via the RWGS reaction.

[0076] The conversion of CO.sub.2 using catalytic particles is known in the art. The contacting between the gaseous feedstock with the catalyst is typically performed in a fixed bed or fluidized bed reactor. The skilled person is capable of determining the optimal conditions for the desired conversion, depending on the specific desired product. In general, the process is typically performed at a temperature in the range of 100-500° C., preferably in the range of 200-400° C., most preferably 200-350° C. Likewise, it is preferred that the process takes place at a pressure in the range of 0.5-20 MPa, preferably 1-10 MPa, more preferably 1.5-5 MPa.

[0077] In one embodiment, the process according to the invention is a RWGS reaction, and is thus performed under conditions suitable for conducting a RWGS reaction. In a preferred embodiment, the RWGS reaction takes place at a temperature in the range of 150-350° C., preferably in the range of 290-330° C. Likewise, it is preferred that the RWGS reaction takes place at a pressure in the range of 0.1-5.0 MPa, preferably 0.5-4.0 MPa, more preferably 1-2.5 MPa. These conditions have were found to be ideally suitable for performing the RWGS reaction with the catalyst according to the present invention. A preferred catalyst for the RWGS reaction is defined above, and is preferably used in the process according to the present embodiment.

[0078] In an alternative embodiment, the process according to the invention is a hydrogenation reaction to convert CO.sub.2 into methanol, and is performed under conditions suitable for conducting such a hydrogenation reaction. In a preferred embodiment, the reaction takes place at a temperature of 200-400° C., more preferably 230-320° C., most preferably at about 300° C. A preferred catalyst for the hydrogenation reaction is defined above, and is preferably used in the process according to the present embodiment.

[0079] In an alternative embodiment, the process according to the invention is a hydrogenation reaction to convert CO.sub.2 into ethanol, and is performed under conditions suitable for conducting such a hydrogenation reaction. In a preferred embodiment, the reaction takes place at a temperature of 200-400° C., more preferably 230-320° C., most preferably at about 300° C. A preferred catalyst for the hydrogenation reaction is defined above, and is preferably used in the process according to the present embodiment.

[0080] In an alternative embodiment, the process according to the invention is a Fischer-Tropsch reaction to convert CO.sub.2 into alkanes, and is performed under conditions suitable for conducting such a Fischer-Tropsch reaction. In a preferred embodiment, the reaction takes place at a temperature of 200-400° C., more preferably 250-350° C., most preferably at about 320° C. A preferred catalyst for the Fischer-Tropsch reaction for preparing alkanes is defined above, and is preferably used in the process according to the present embodiment.

[0081] In an alternative embodiment, the process according to the invention is a Fischer-Tropsch reaction to convert CO.sub.2 into alkenes, and is performed under conditions suitable for conducting such a Fischer-Tropsch reaction. In a preferred embodiment, the reaction takes place at a temperature of 200-400° C., more preferably 250-350° C., most preferably at about 320° C. A preferred catalyst for the Fischer-Tropsch reaction for preparing alkenes is defined above, and is preferably used in the process according to the present embodiment.

[0082] In an alternative embodiment, the process according to the invention is a Methanol to Olefin reaction to convert CO.sub.2 into alkenes, and is performed under conditions suitable for conducting such a MTO reaction. In a preferred embodiment, the reaction takes place at a temperature of 200-400° C., more preferably 250-350° C., most preferably at about 320° C. A preferred catalyst for the MTO reaction is defined above, and is preferably used in the process according to the present embodiment.

[0083] In an alternative embodiment, the process according to the invention is a methanation reaction to convert CO.sub.2 into methane, and is performed under conditions suitable for conducting such a methanation reaction. In a preferred embodiment, the reaction takes place at a temperature of 200-400° C., more preferably 250-350° C., most preferably at about 320° C. A preferred catalyst for the methanation reaction is defined above, and is preferably used in the process according to the present embodiment.

[0084] In an alternative embodiment, the process according to the invention is an aromatization reaction to convert CO.sub.2 into aromatic hydrocarbons, and is performed under conditions suitable for conducting such an aromatization reaction. In a preferred embodiment, the reaction takes place at a temperature of 200-400° C., more preferably 250-350° C., most preferably at about 320° C. A preferred catalyst for the aromatization reaction is defined above, and is preferably used in the process according to the present embodiment.

[0085] In an alternative embodiment, the process according to the invention is a hydrogenation reaction to convert CO.sub.2 into methanol and a dehydration reaction to convert methanol into dimethyl ether, and is performed under conditions suitable for conducting such a hydrogenation and dehydration reaction. In a preferred embodiment, the reaction takes place at a temperature of 200-400° C., more preferably 225-300° C., most preferably at about 275° C. Preferred catalysts for the combined hydrogenation and dehydration reaction is defined above, and is preferably used in the process according to the present embodiment. Herein, both the catalyst system comprising two distinct catalytic particles, one of which is the bifunctional catalyst according to the invention, and the trifunctional catalyst according to the invention is suitable.

[0086] In an alternative embodiment, the process according to the invention is a hydrogenation reaction to convert CO.sub.2 into ethanol and a dehydration reaction to convert ethanol into diethyl ether, and is performed under conditions suitable for conducting such a hydrogenation and dehydration reaction. In a preferred embodiment, the reaction takes place at a temperature of 200-400° C., more preferably 225-300° C., most preferably at about 275° C. A preferred catalyst for the combined hydrogenation and dehydration reaction is defined above, and is preferably used in the process according to the present embodiment. Herein, both the catalyst system comprising two distinct catalytic particles, one of which is the bifunctional catalyst according to the invention, and the trifunctional catalyst according to the invention is suitable.

[0087] The feedstock of the process according to the present invention is a gaseous feedstock comprising H.sub.2 and CO.sub.2. The feedstock may contain further gaseous components, such as CO, gaseous contaminants of a process gas (e.g. H.sub.2S, CH.sub.4) and inert gases (e.g. N.sub.2, Ar). The conversion of CO.sub.2 in CO and possibly downstream products is an important aspect of the present invention. For the process according to the invention, the presence of some CO in the feedstock has no negative impact. Also, the process according to the invention is capable of dealing with minor contaminants of CO.sub.2-containing process streams. In case the invention concerns the RWGS reaction, it is preferred that the feedstock does not comprise CO, as CO is efficiently formed in the RWGS reaction according to the present invention.

[0088] Preferably, the feedstock contains H.sub.2 and CO.sub.2, and optionally CO and inert gases such as N.sub.2 and Ar, and no other gaseous species. The molar ratio of H.sub.2 to CO.sub.2 in the feedstock may be in the range of 25:1-1:10, preferably 10:1-1:5, more preferably 5:1-1:1. The skilled person is capable of optimizing the molar ratio of in the feedstock for the desired product. For example, the optimal H.sub.2 to CO.sub.2 ratio for the RWGS reaction is about 1:1, while for alcohol, ether or alkanes, the feedstock preferably contains an excess of H.sub.2, such as an H.sub.2 to CO.sub.2 ratio of about 2:1-4:1.

[0089] The process according to the invention preferably comprises a step wherein the catalyst is regenerated. During the reaction, water molecules are sorbed onto the sorbent, in order to shift the equilibrium of the reaction towards the product, such as CO in case of the RWGS reaction. During regeneration, the sorbed water molecules are desorbed from the sorbent, such that the sorbent becomes available for a further reaction. Regeneration may be accomplished by any method known in the art. Typically, a temperature swing and/or pressure swing adsorption is employed. In one embodiment, the regeneration step involves a pressure reduction by at least 0.1×10.sup.6 Pa, preferably to a pressure in the range of 0.1×10.sup.6 Pa-0.3×10.sup.6 Pa, and/or a temperature increase by at least 20° C., preferably to a temperature in the range of 370° C.-500° C.

Use

[0090] A third aspect of the invention relates to the use of the catalyst according to the invention as catalyst for the RWGS reaction. The use according to the present aspect may also be worded as the use of the catalyst according to the invention as catalyst for the synthesis of CO via the RWGS reaction. The use according to the present aspect preferably employs the process according to the invention, and everything defined for the process according to the invention equally applies to the use according to the invention.

EXAMPLES

[0091] The invention is further illustrated by the following non-limiting examples.

Example 1: Preparation of Multifunctional Catalysts

[0092] A range of multifunctional catalysts according to the invention (1)-(6) was prepared. Selected solid water sorbents were contacted with a solution comprising a catalytic metal (see Table below for details per catalyst). The catalyst was dried at 105° C. under rigorous stirring. Subsequently, the catalysts were calcined at 400° C. (5° C./min, 6 h) to remove volatile components, depositing the metal oxide clusters on the catalyst surface. Next, the granulate was compressed using a pill press at 4 atm, then broken into granules. A sieve fraction of 212-450 μm was selected for the experiment. The last step in the preparation of the catalyst preparation is reduction in hydrogen flow (typically this step is carried out in-situ, the first step the catalysts in the reactor is subjected to).

[0093] Besides the multifunctional catalysts, a conventional catalyst typically used in RWGS reactions was prepared for comparison purposes.

TABLE-US-00001 Sorbent Metal Impregnation procedure (1) Zeolite 13X 10 wt % Cu >106 μm powder wet impregnated with 0.407 g Cu(NO.sub.3).sub.2•2.5H.sub.2O per gram of zeolite material by dissolving in the minimal amount of water. (2) Zeolite LTA-4A 10 wt % Cu >106 μm powder wet impregnated with 0.407 g  7 wt % Zn Cu(NO.sub.3).sub.2•2.5H.sub.2O and 0.176 g ZnCl.sub.2 per gram of zeolite material by dissolving in the minimal amount of water. (3) Zeolite 13X  7 wt % Cu >106 μm powder wet impregnated with 0.285 g  3 wt % Zn Cu(NO.sub.3).sub.2•2.5H.sub.2O and 0.123 g Zn(NO.sub.3).sub.2•3H.sub.2O per gram of zeolite material by dissolving in the minimal amount of water. (4) Zeolite 13X  2 wt % Pt >106 μm powder wet impregnated with 0.041 g Pt(NH.sub.3).sub.4(NO.sub.3).sub.2 per gram of zeolite material by dissolving in the minimal amount of water. (5) Zeolite LTA-4A  2 wt % Pt >106 μm powder wet impregnated with 0.041 g Pt(NH.sub.3).sub.4(NO.sub.3).sub.2 per gram of zeolite material by dissolving in the minimal amount of water. (6) Zeolite LTA-5A  2 wt % Pt >106 μm powder wet impregnated with 0.041 g Pt(NH.sub.3).sub.4(NO.sub.3).sub.2 per gram of zeolite material by dissolving in the minimal amount of water. (7) Zeolite 13X  7 wt % Co >106 μm powder wet impregnated with 0.372 g Co(NO.sub.3).sub.2•6H.sub.2O per gram of zeolite material by dissolving in the minimal amount of water.

Example 2: CO Selectivity During RWGS

[0094] Small-scale RWGS processes were conducted four of the catalysts of example 1, as well as with control catalyst (8), a low-temperature CuZnAl commercial water gas shift (LTS) mixed with molsieves 3A sorbent (ms). A feedstock of H.sub.2 and CO.sub.2 (4/1 mol/mol) and 5% of argon as tracer was fed to 26 g of the catalyst at 300° C. and 10 bar(a). Regeneration of the catalyst was performed by a combined temperature and pressure swing (TPSA), by lowering the pressure to 5 bar(a) and heating to 400° C., while feeding N.sub.2. The composition of the product gas was analysed by gas chromatography and mass spectroscopy. The composition (in mol %) is given in the table below.

TABLE-US-00002 CH.sub.4 CO CO.sub.2 C.sub.2H.sub.4 DME CH.sub.3OH (1) 1.9 73.3 23.4 0.9 0.6 0 (4) 13 72.3 13.7 0.2 0.4 0.4 (5) 5.9 85.1 7.8 0.9 0.2 0.1 (6) 69.2 1.5 29 0.3 0 0 (8) 4.6 57.2 15.8 0.7 21.2 0.5

[0095] All inventive catalysts outperformed the conventional catalyst (8), which is not selective for CO and forms substantial amounts of DME. Catalyst (5), a LTA-4A sorbent impregnated with 2 wt % Pt, gave especially good results, with over 90% conversion to CO and hardly any DME and CH.sub.4 formed.

Example 3: Stability

[0096] An extended RWGS process (>71 days) was conducted with catalyst (5) of example 1. A feedstock of H.sub.2 and CO.sub.2 (4/1 mol/mol) and 5% of argon as tracer was fed to 26 g of the catalyst at 300° C. and 10 bar(a). Regeneration of the catalyst was performed as part of each cycle after each reactive adsorption period of 2.5 hours by a combined temperature and pressure swing (TPSA), by lowering the pressure to 3 bar(a) and heating to 400° C., while feeding N.sub.2. The composition of the product gas was analysed periodically by gas chromatography and mass spectroscopy. The composition (in mol %) at certain points in time is given in the table below.

TABLE-US-00003 Time S_max S_max S_max S_max S_max (h) (CO) (CO.sub.2) (DME) (MeOH) (CH.sub.4) 432 85.7 7.9 0.3 0.2 6.0 672 82.5 13.1 0.0 0.0 4.4 1152 92.2 2.8 0.0 0.0 5.0 1704 97.8 2.2 0.0 0.0 0.0

[0097] Surprisingly, the catalyst was activated over time, while a (slight) deactivation normally occurs with conventional catalysts during such extended experiments. After 71 days, the catalyst according to the invention gave excellent conversions towards CO.

Example 4: Tuning the Design of Catalyst Toward Selective Formation of Dimethyl Ether

[0098] Zeolite 13×based catalysts (1) and (4) of Example 1 were compared using a feedstock of H.sub.2:CO:CO.sub.2=8:1:2 at 25 bar and 275° C. The Cu based catalyst (1) showed approximately 10 times higher dimethyl ether yield compared to the Pt analogue (4).

Example 5: Tuning the Design of Catalyst Toward Selective Formation of Methane

[0099] Zeolite 13×based reactive water sorbent (7) was tested using a feedstock of H.sub.2:CO.sub.2=1:4 at 10 bar and 275° C. The cobalt based reactive water sorbent reached CO.sub.2 conversion of 95% with product carbon selectivity towards CH.sub.4 of 91%, CO.sub.2 (5%) and ethane (4%).