IL303685B2

IL303685B2 - Ceramic catalyst, method of production and uses thereof

Info

Publication number: IL303685B2
Application number: IL303685A
Authority: IL
Original assignee: Electriq Global Energy Solutions Ltd
Priority date: 2023-06-13
Filing date: 2023-06-13
Publication date: 2025-02-01
Also published as: IL303685B1; IL303685A; WO2024257087A1

Description

0294883137- CERAMIC CATALYST, METHOD OF PRODUCTION AND USES THEREOF TECHNOLOGICAL FIELD The present disclosure relates to chemical catalysts.

BACKGROUND ART References considered to be relevant as background to the presently disclosed subject matter are listed below: - L. Wei, X. Dong, M. Ma, Y. Lu, D. Wang, S. Zhang, D. Zhao, Q. Wang. (2017). Co 3O 4 hollow fiber: an efficient catalyst precursor for hydrolysis of sodium borohydride to generate hydrogen. International Journal of Hydrogen Energy.

- T. Hung, H. Kuo, C. Tsai, H. Chen, R. Liu, B. Weng, J. Lee. (2011). An alternative cobalt oxide-supported platinum catalyst for efficient hydrolysis of sodium borohydride. Journal of Materials Chemistry(21), 11754-11759.

- Y. Huang, K. Wang, L. Cui, W. Zhu, A. M. Asiri, X. Sun. (2016). Effective hydrolysis of sodium borohydride driven by self-supported cobalt oxide nanorod array for on-demand hydrogen generation. Catalysis Communications, 87, 94-97.

Acknowledgement of the above references herein is not to be inferred as meaning that these are in any way relevant to the patentability of the presently disclosed subject matter.

BACKGROUND Although hydrogen has great potential as a clean and renewable energy source, its practical use as a fuel for transportation and power generation hinges on the development of safe and efficient methods for storage, distribution, and controlled release. One way to store hydrogen is by using borohydride compounds (e.g., KBH4, NaBH4), which can release hydrogen upon demand through a chemical reaction. 25 0294883137- For example, the dehydrogenation reaction of potassium borohydride dissolved in water is illustrated by the equation below: Borohydride compounds are stable and can store a high density of hydrogen, making these compounds attractive candidates for hydrogen storage.

Catalysts can improve the kinetics of borohydride dehydrogenation. Several types of catalysts have been explored for borohydride dehydrogenation, including noble metals (e.g., platinum (Pt) and palladium (Pd)) and non-noble metals (e.g., nickel (Ni) and cobalt (Co)).

L. Wei et al. describe the development of a catalyst for sodium borohydride hydrolysis to generate hydrogen. The catalyst precursor was a Co3O4 hollow fiber composed of a nanoparticles array, prepared by combustion method with a template of cotton absorbent. Cobalt oxide is reduced by NaBH 4, and the resulting active Co xB compounds further catalyze the hydrolysis of NaBH4 to generate hydrogen.

T. Hung et al, describe a Pt/Co3O4 catalyst for hydrogen generation in a sodium borohydride system.

Y. Huang et al, describe self-supported cobalt oxide nanorod arrays on a Ti sheet (Co 3O 4 NA/Ti) that can drive the dehydrogenation of NaBH 4 in alkaline solutions.

GENERAL DESCRIPTION The present disclosure provides, in accordance with its first aspect, a catalyst comprising -Al 2O 3 associated with cobalt oxide, including at least Co2+ and Co3+ oxidation states.

In accordance with a second aspect of the presently disclosed subject matter, there is provided a method of preparing a catalyst, the method comprises impregnating -Al2O3 with an aqueous solution comprising Co2+ to form impregnated -Al2O3; and subjecting said impregnated -Al 2O 3 to thermal treatment causing formation of cobalt oxide. 0294883137- In accordance with a third aspect of the presently disclosed subject matter, there is provided a catalyst, obtained or obtainable by the method of the presently disclosed second aspect.

Yet, in accordance with a fourth aspect of the presently disclosed subject matter, there is provided a process for hydrogen generation, the process comprises contacting a catalyst comprising -Al 2O 3 associated with cobalt oxide including at least Co2+ and Co3+ oxidation states with a solution comprising borohydride compound and proton donor solvent.

BRIEF DESCRIPTION OF THE DRAWINGS In order to better understand the subject matter that is disclosed herein and to exemplify how it may be carried out in practice, embodiments will now be described, by way of non-limiting example only, with reference to the accompanying drawings, in which: Figure 1 is a schematic illustration of possible phases of cobalt oxide as a function of oxygen content.

Figure 2 is a graph providing a time and temperature-dependent calcination profile during the formation of a catalyst in accordance with some examples of the presently disclosed subject matter.

Figure 3 is a graph showing the prediction of total hydrogen evolution after 1hours of using a catalyst according to some examples of the presently disclosed subject matter, as determined using a HOD system with 5M KBH 4.

Figure 4 is an -Al2O3, impregnated with 2.4%wt CoCl2·6H2O and calcinated at 450°C according to a non-limiting example of the presently disclosed subject matter.

Figure 5 is an -Al 2O 3, impregnated with 24%wt CoCl 2·6H 2O and calcinated at 450°C according to another non-limiting example of the presently disclosed subject matter.

Figure 6 is an -Al2O3, impregnated with 54%wt CoCl2·6H2O and calcinated at 450°C according to yet another non-limiting example of the presently disclosed subject matter. 30 0294883137- Figure 7 is an -Al2O3, impregnated with 64%wt Co(NO 3) 2·6H 2O and calcinated at 450°C according to a non-limiting example of the presently disclosed subject matter.

Figure 8 is an -Al2O3, impregnated with 54%wt CoCl2·6H2O using degassing methods and calcinated at 450°C, according to yet another non-limiting example of the presently disclosed subject matter.

Figure 9 is a graph showing catalytic activity as a function of cycles using two different catalysts of the presently disclosed subject matter.

Figure 10 is a cross-section SEM image (WD 6.13, Energy 15keV, magnification 10.00kx) -Al2O3, impregnated with 54%wt CoCl2·6H2O and calcinated at 450°C, without using degassing methods, showing that there is no visible cobalt oxide inside internal examined bead.

Figure 11 is a cross section SEM image (WD 6.13, Energy 20keV, magnification 10.00kx) -Al 2O 3, impregnated with 54%wt CoCl2·6H 2O using degassing methods and calcinated at 450°C, showing tetrahedral particles of the Co3O4 (circled).

Figure 12 is an -Al2O3, impregnated with 54%wt CoCl2·6H2O and calcinated at 250°C according to another non-limiting example of the presently disclosed subject matter.

Figure 13 is an -Al 2O 3, impregnated with 54%wt CoCl 2·6H 2O and calcinated at 650°C according to yet another non-limiting example of the presently disclosed subject matter.

Figure 14 is an -Al 2O 3, impregnated with 54%wt CoCl 2·6H 2O and calcinated at 850°C according to yet another non-limiting example of the presently disclosed subject matter.

Figure 15 is a graph showing the activity of a ceramic catalyst in a 3KW system (HOD system) using 5M KBH4 -Al2O3, impregnated with 54%wt CoCl2·6H2O and calcinated at 450°C. 0294883137- DETAILED DESCRIPTION Catalysts are employed in various applications both in laboratories and in industry to mediated chemical reactions. Catalysts operate by providing an alternative reaction route, wherein the activation energy is lower route is not mediated by the catalyst.

The present disclosure is based on the development of a catalyst using a ceramic porous material as a carrier for cobalt oxide.

It has been found that when selecting, as the ceramic carrier, -Al 2O 3 over other phases of Al 2O 3 phases or over other possible ceramic carriers (e.g., TiO 2 and SiO 2 ), the resulting catalyst has hydrogen gas generating activity that is improved over the other ceramic carriers, inter alia, in mechanical stability and/or durability. For example, it has been found that the catalyst based on -Al2O3 allows sufficient/effective hydrogen gas production even after numerous hydrogen gas production cycles (runs), while maintaining the catalyst's integrity and functionality (no mechanical degradation was observed or detected) and while not being affected by the mechanical stresses occurring during operation of a hydrogen-on-demand (HOD) system.

Thus, in accordance with a first aspect of the presently disclosed subject matter, there is provided a -Al 2O 3 associated with cobalt oxide including at least Co2+ and Co3+ oxidation states.

In the context of presently disclosed subject matter, when referring to cobalt oxide, it is to be understood to refer to any chemical entity comprising at least cobalt and oxygen. In some examples of the presently disclosed subject matter, the cobalt oxide is selected from the group consisting of Co 3O 4, Co 2O 3, CoO, Co 2AlO 4, CoAl 2O 4.

In some examples of the first aspect of the presently disclosed subject matter, the cobalt oxide comprises at least Co 3O 4.

Without being bound by theory, Figure 1 provides a schematic illustration of possible phases of cobalt oxide as a function of oxygen content.

The cobalt oxide is associated with the -Al2O3. In some examples of the first aspect of the presently disclosed subject matter, the -Al2O3 is porous and constitutes a porous carrier for the cobalt oxide. 0294883137- In some examples of the first aspect of the presently disclosed subject matter, the cobalt oxide is encaged within at least some of the pores of the porous -Al2O3. The encagment can be viewed, for example, by scanning electron microscope (SEM) as further exemplified hereinbelow.

In some examples of the first aspect of the presently disclosed subject matter, at least part of the -Al2O3 is in particulate form. Similarly, the particulate form can be viewed, e.g., by SEM.

In some examples of the first aspect of the presently disclosed subject matter, when the cobalt oxide is in particulate form, e.g., a crystalline form.

In some examples of the first aspect of the presently disclosed subject matter, when in crystalline form, the cobalt oxide may have a geometrical shape, such as a tetrahedron, pyramid, and octahedron.

In some examples of the presently disclosed subject matter, at least part of the cobalt oxide associated with the porous -Al 2O 3 has a tetrahedral shape.

In some examples of the presently disclosed subject matter, at least part of the cobalt oxide associated with the porous -Al2O3 has an octahedral shape.

In some examples of the presently disclosed subject matter, at least part of the cobalt oxide associated with the porous -Al 2O 3 has a combination of a tetrahedral and an octahedral shape.

In some examples of the first aspect of the presently disclosed subject matter, the cobalt oxide in particulate form has a particle size of at least 1nm.

In some examples of the first aspect of the presently disclosed subject matter, the cobalt oxide in particulate form has a particle size of at most 1mm.

In some examples of the first aspect of the presently disclosed subject matter, the cobalt oxide in particulate form has a particle size of between about 1nm to about 900 µm .

In some examples of the first aspect of the presently disclosed subject matter, the cobalt oxide in particulate form has a particle size of between about 1nm and about 500µm, at times between about 50nm and about 400µm, at times between about 100nm and about 600 µm, at times between about 500nm and about 250µm, at times, between about 1 µm and 250 µm, or any other range within the range of 1nm to about 900 µm. 30 0294883137- In some examples of the first aspect of the presently disclosed subject matter, the cobalt oxide is present in the catalyst in an amount that constitutes at least 0.1wt% out of the total weight of said catalyst. In some examples, the amount of the cobalt oxide present in the catalyst is at least about 0.5wt% out of the total weight of said catalyst; at times, at least about 5wt%; at times, at least about 10wt%; at times, at least about 15wt%; at times, at least about 20wt%; at times, at least about 25wt%; at times, at least about 30wt%; at times, at least about 35wt%.

In some examples of the first aspect of the presently disclosed subject matter, the cobalt oxide is present in the catalyst in an amount that constitutes not more than 40wt% out of the total weight of the catalyst.

In some examples, the amount of the cobalt oxide present in the catalyst is at most about 38wt% out of the total weight of said catalyst; at times, at most about 36wt%; at times, at most about 34wt%; at times, at most about 32wt%; at times, at most about 30wt%; at times, at most about 28wt%; at times, at most about 26wt%; at times, at most about 24wt%; at times, at most about 22wt%; at times, at most about 20wt%; at times, at most about 18wt%, at times, at most about 16wt%, at times, at most about 14wt%, at times, at most about 12wt%; at times, at most about 10wt%, out of the total weight of the catalyst.

In some examples of the first aspect of the presently disclosed subject matter, the cobalt oxide is present in the catalyst in an amount that constitutes between about 0.1wt% and about 40wt% out of the total weight of the catalyst.

In some examples, the amount of the cobalt oxide present in the catalyst is between any range falling between 0.1wt% and 40wt%, out of the total weight of the catalyst.

In some examples, the amount of the cobalt oxide present in the catalyst is at least 1wt% out of the total weight of said catalyst; at times, at least about 2wt% out of the total weight of said catalyst; at times, at least about 3wt% out of the total weight of said catalyst; at times, at least about 4wt% out of the total weight of said catalyst; at times, at least about 5wt% out of the total weight of said catalyst; at times, at least about 6wt% out of the total weight of said catalyst; at times, at least about 7wt% out of the total weight of said catalyst; at times, at least about 8wt% out of the total weight of said catalyst; at times, at least about 9wt% out of the total weight of said catalyst; at times, at least about 10wt% out of the total 30 0294883137- weight of said catalyst; at times, at least about 15wt% out of the total weight of said catalyst; at times, at least about 20wt% out of the total weight of said catalyst.

In some examples, the amount of the cobalt oxide present in the catalyst is at most 40wt% out of the total weight of said catalyst; at times, at most about 35wt% out of the total weight of said catalyst; at times, at most about 30wt% out of the total weight of said catalyst; at times, at most about 25wt% out of the total weight of said catalyst.

In some examples, the amount of the cobalt oxide present in the catalyst is between about 0.5wt% and about 38% out of the total weight of said catalyst; at times, between about 0.5wt% and about 30wt%, at times, between about 2wt% and about 25wt%, at times, between about 4wt% and about 35wt%, at times between about 2wt% and about 25wt%.In some examples of the first aspect of the presently disclosed subject matter, the particulate form of porous -Al 2O 3 has a particle size of between about 1mm and about 10mm.

In some examples of the first aspect of the presently disclosed subject matter, the porous -Al 2O 3 is also in particulate form, having a shape of particles, sheets, tubes, pellets etc. it is appreciated that due to its size, the porous -Al2O3 cannot be a free flowing powder. .

In some examples of the first aspect of the presently disclosed subject matter, the -Al 2O 3 has a surface area, in the absence of said cobalt oxide, of less than about 10 m/gr, between about 0.1 m/gr and about 10 m/g.

In some examples of the first aspect of the presently disclosed subject matter, the catalyst is essentially free of electrically conductive substances.

In the context of the present disclosure, when referring to "electrically conductive substances" it is to be understood to encompass any chemical substance that can participate in an electrochemical reaction and/or to conduct electrons. In some examples, the catalyst is essentially free of electrically conductive metals. In some examples, the catalyst is essentially free of noble metals.

In the context of the presently disclosed subject matter, the term "essentially free" is to be understood to mean that there is either no detectable amount of the substance being essentially absent from the catalyst or the amount is insufficient to participate in an electrochemical reaction or does not affect the performance of the catalyst. In some examples, the term "essentially free" can include the presence of trace amount of an 0294883137- electrically conductive substance, the amount being insignificant and/or insufficient to participate in an electrochemical reaction or to affect the performance of the catalyst.

In accordance with the presently disclosed first aspect, the catalyst exhibits catalytic activity, at least for the dehydrogenation of a target compound.

In some examples, the target compound is potassium borohydride.

In some examples, the target compound is lithium borohydride.

In some examples, the target compound is ammonium borohydride.

In some examples, the target compound is tetramethyl ammonium borohydride.

In some examples, the target compound is sodium borohydride.

In some examples, the target compound is a mixture of any of the above.

The catalyst disclosed herein demonstrated a beneficiary catalytic activity as determined using a Hydrogen-On-Demand (HOD) release system operated using 5M KBHin H 2O.

When referring to a catalytic activity it is to be understood as the capability of the catalyst to catalyze the production of hydrogen gas in an HOD release system, as compared to the production rate, under the same conditions, in the absence of the catalyst.

"Hydrogen-On-Demand" (HOD) release systems are well-known in the art and readily available. In some examples of the presently disclosed subject matter, the HOD release system employed by the present disclosure is as described in International Patent Application Publication No. WO 2019/202391, the content of which is incorporated herein, in its entirety, by reference.

In some examples of the presently disclosed subject matter, the catalytic activity is determined when the system is operated at elevated temperatures, e.g., above 50°C; at times, above 60°C; at times above 70°C.

In some examples of the presently disclosed subject matter, the catalytic activity is determined when the system is operated at elevated pressure, e.g., above 1bar; at times, above 2 bars; at times above 3 bars; at times, above 4 bars, at times, above 5 bars, at times even at about 6 bars. 0294883137- Thus, in the context of the presently disclosed subject matter, the catalyst can be defined as one having a statistically significant catalytic activity in generating hydrogen gas, as determined by a HOD release system in the presence of 5M KBH 4 in H 2O.

The presently disclosed catalyst exhibits beneficial mechanical stability and/or durability. Surprisingly, it has been found that even after numerous hydrogen gas production cycles (runs), the catalyst maintained its integrity and functionality (no mechanical degradation was observed or detected) and was not affected by the mechanical stresses occurring during the operation of a hydrogen-on-demand system.

Thus, in some examples of the presently disclosed subject matter, the catalyst is characterized by its ability to maintain its catalytic level, i.e. hydrogen activity (rate H2 production per gram catalyst). In some examples, the stability is characterized in that the catalyst does not substantially pulverize in time.

In accordance with a second aspect of the presently disclosed subject matter, there is provided a method of preparing a catalyst, the method comprising impregnating -Al 2O 3 with an aqueous solution comprising Co2+ to form impregnated -Al 2O 3; and subjecting the impregnated -Al2O3 to thermal treatment causing formation of cobalt oxide.

In some examples of the presently disclosed method, the aqueous solution comprises cobalt salt.

In some examples of the presently disclosed method, the cobalt salt within the aqueous solution is selected from the group consisting of cobalt acetate (Co(CH 3COO) 2), cobalt bromide (CoBr 2), cobalt chloride (CoCl 2), cobalt formate (Co(HCOO) 2), cobalt nitrate (Co(NO 3) 2), cobalt sulfate (CoSO 4), cobalt tartrate (CoC 4H 4O 6), and combinations thereof.

In some preferred example of the presently disclosed subject matter, the cobalt salt comprises at least cobalt chloride (CoCl2).

In some preferred example of the presently disclosed subject matter, the cobalt salt comprises at least cobalt nitrate (Co(NO 3) 2). 0294883137- In some preferred example of the presently disclosed subject matter, the cobalt salt comprises at least cobalt sulfate (CoSO 4).

In some preferred example of the presently disclosed subject matter, the cobalt salt comprises a combination of cobalt chloride, cobalt nitrate, and cobalt sulfate.

In some examples of the presently disclosed method, the cobalt salt(s) are at a total concentration of at least 2wt%, irrespective of whether there is a single type of salt or a combination of salts.

In some examples of the presently disclosed method, the cobalt salt(s) are at a concentration within a range of between about 2wt% and about 60wt% when determined at a temperature of 20ºC. In some examples of the presently disclosed method, the cobalt salt(s) are at a concentration close to their solubility limit, and in some examples it is around about 80gr/100ml as determined at 20ºC.

In some examples of the presently disclosed method, the -Al2O3 is subjected to negative pressure at least prior to its impregnation.

In some examples of the presently disclosed method, the -Al 2O 3 is subjected to negative pressure at least during said impregnation.

In the context of the presently disclosed subject matter, when referring to "negative pressure" it is to be understood as exposing the -Al2O3 to a pressure below 1 Atmosphere. It has been found that exposing the -Al2O3 to negative pressure improves the capacity of -Al 2O 3 to capture the cobalt to form the cobalt oxide particles inside the -Al 2O 3 pores and thus provides a higher yield in the presently disclosed method.

Without being bound by theory, it is believed that the exposure of the -Al 2O 3 to negative pressure results in removal of at least some impurities or otherwise undesired substances occupying the pores of -Al2O3 particles.

In some examples of the presently disclosed subject matter, the method comprises drying the impregnated -Al2O3 prior to applying the thermal treatment.

Drying of the impregnated -Al 2O 3 can be by any technique known in the art to allow water removal from the impregnated -Al 2O 3. For example, drying can be within an oven, or by applying hot air onto the impregnated -Al 2O 3, centrifugation of the 0294883137- impregnated -Al 2O 3, applying negative pressure on the impregnated -Al 2O 3, and any combination thereof.

In some examples, the drying of the impregnated -Al 2O 3 is by subjecting the impregnated -Al 2O 3 to temperatures between about 100ºC and about 250ºC; at times, between about 100ºC and about 200 ºC; at times, between about 100ºC and about 150 ºC.

In some examples of the presently disclosed subject matter, the drying of the impregnated -Al2O3 is by heating the same to a temperature of up to 200°C.

In some examples of the presently disclosed subject matter, the drying of the impregnated -Al2O3 comprises step-wise drying.

In the context of the presently disclosed subject matter, when referring to a "step- wise" process, e.g., step-wise heating, it is to be understood to mean the gradual increase of the temperature in a series of controlled, discrete increments or steps.

The impregnated -Al2O3 (either with or without the drying thereof after impregnation) is then subjected to thermal treatment.

In some examples of the presently disclosed subject matter, the thermal treatment comprises heating the impregnated -Al2O3 to a temperature between about 150°C and about 1000°C.

In some examples, the thermal treatment comprises heating the impregnated -Al 2O 3 to a temperature range of between about 200°C and about 900°C; at times, between about 250°C and about 1000°C; at times, between about 250°C and about 900°C.

In some examples of the presently disclosed subject matter, the thermal treatment is conducted under any one of oxygen environment, nitrogen environment, argon environment, hydrogen environment.

In some examples of the presently disclosed subject matter, the thermal treatment should take place for a time duration sufficient to effectively produce cobalt oxide particles associated with the -Al2O3. In the context of the presently disclosed subject matter, an effective association between the -Al2O3 and the cobalt oxide is one exhibiting a wt% of cobalt oxide out of a total weight of the catalyst of at least 0.2wt%; at times, at least 1wt%; at times, at least 2wt%; at times, at least 3wt%; at times, at least 4wt%; at times, at least 5wt%; at times, at least 6wt%; at times, at least 7wt%; at times, at least 8wt%. 30 0294883137- In some examples of the presently disclosed subject matter, the thermal treatment is applied for at least about 1hour; at times, for at least 1.5 hours; at times, for at least 2 hours; at times, for at least 2.5 hours; at times, for at least 3 hours; at times, for at least 3.5 hours; at times, for at least 4 hours.

In some examples of the presently disclosed subject matter, the thermal treatment is applied for about 4±1 hours.

In some examples of the presently disclosed subject matter, the thermal treatment comprises step-wise heating of said impregnated -Al2O3.

The presently disclosed subject matter also provides, in accordance with a further aspect thereof, a catalyst obtained or obtainable by the presently disclosed method.

The presently disclosed subject matter further provides, in accordance with a fourth of its aspects, a process for hydrogen generation making use of the presently disclosed catalyst. It is to be understood that all definitions of the catalyst provided with respect to the presently disclosed first, second and third aspects also apply to the process according to the presently disclosed fourth aspect.

In accordance with the presently disclosed fourth aspect, the presently disclosed process comprises contacting the presently disclosed catalyst (comprising -Al 2O associated with cobalt oxide including at least Co2+ and Co3+ oxidation states) with a solution comprising borohydride compound and proton donor solvent.

In the context of the presently disclosed subject matter, when referring to a "proton donor solvent" it is to be understood to mean any solvent capable of, in addition to dissolving borohydride salt, to release or donate protons (H+) in a chemical reaction. The proton donor solvent is also known by the term "protic solvent".

In some examples of the presently disclosed process for generating hydrogen, the proton donor solvent is selected from the group consisting of: water, ethanol, methanol, propanol, isopropanol, butanol, isobutanol, propanediol, ethylene glycol, glycerol, and mixtures thereof.

In some preferred examples, the proton donor solvent is water.

In accordance with the presently disclosed fourth aspect, the borohydride compound is selected from the group consisting of: potassium borohydride, sodium borohydride, 30 0294883137- lithium borohydride, ammonium borohydride, tetramethyl ammonium borohydride, and mixtures thereof.

In some preferred examples of the presently disclosed process for generating hydrogen, the borohydride compound comprises or is potassium borohydride.

Without being bound by theory, it is believed that in the presence of the presently disclosed catalyst, hydrogen generation occurs such that one proton (H+) is donated by water and the borohydride donates a hydride (hydrogen anion, H-), together forming H 2.

It has been found that the use of the presently disclosed catalyst allows its use in more than one hydrogen generation cycle, i.e., in two or more runs on the HOD system, without the need to replace the catalyst. In some examples, the catalyst can be used in more than 10 cycles, at times, in more than 20 cycles; at times, in more than 30 cycles; at times, in more than 40 cycles; at times, in more than even 45 cycles or even more than 50 cycles, while essentially maintaining the mechanical integrity and/or catalytic activity of the catalyst.

Thus, in accordance with the presently disclosed subject matter, the catalyst is one that maintains its mechanical integrity and/or catalytic activity for at least 40 hydrogen generation cycles.

All definitions, as defined and used herein, should be understood to control over dictionary definitions, definitions in documents incorporated by reference, and/or ordinary meanings of the defined terms.

As used herein, the indefinite articles "a", "an" and "the" include singular as well as plural references unless the context clearly dictates otherwise. In other words, unless clearly The term "about" as used herein indicates values that may deviate up to 1%, more specifically 5%, more specifically 10%, more specifically 15%, and in some cases up to 20% higher or lower than the value referred to, the deviation range including integer values, and, if applicable, non-integer values as well, constituting a continuous range. In some examples of the presently disclosed subject matter, the term "about" refers to ± 10 %. and/or claims, should are conjunctively present in some cases and disjunctively present in other cases. Multiple 0294883137- inclusive, i.e., the inclusion of at least one, but also including more than one, of a number or list of elements, and, optionally, additional unlisted items. Only terms clearly indicated elements.

Further, as used herein, the term "comprising" is intended to mean that a described product and/or process includes the recited element, but not excluding other elements. The term "consisting essentially of" is used to define a described product and/or process which includes the recited elements but exclude other elements that may have an essential significance on the described product and/or process. "Consisting of" shall thus mean excluding more than trace elements of other elements. Embodiments defined by each of these transition terms are within the scope of this invention.

The invention will now be exemplified in the following description of experiments that were carried out in accordance with the invention. It is to be understood that these examples are intended to be in the nature of illustration rather than of limitation. Obviously, many modifications and variations of these examples are possible in light of the above teaching. It is therefore, to be understood that within the scope of the present disclosure, the invention may be practiced otherwise, in a myriad of possible ways, than as specifically described hereinbelow.

DESCRIPTION OF NON-LIMITING EXAMPLES Materials And Methods Al 2O 3 (alpha and theta), TiO 2 and SiO 2 were purchased from Saint Gobain. CoCl 2·H 2O was purchased from Alfa Aesar. NaH 2PO 2 was purchased from Alfa Aesar. NaOH was purchased from SDFCL. KBH4 was purchased from Goldman.

Substrate Impregnation 0294883137- -15gr of the substrate in the form of beads were immersed in 100ml of cobalt solution and incubated for 12-24 hr. Following the incubation, the beads were filtered from the solution and washed 3 times. The beads were laid in a ceramic crucible and placed in an oven. Calcination The time-temperature profile of the calcination process is described in Figure 2 .

The calcination was performed by controlled heating of the sample in an ambient atmosphere using the following heating program: - 3°C/min until reaching 150°C (~35min). - 10.5 hours at 150°C. - 3°C /min until reaching the target calcination temperature. - 4 hours at target calcination temperature. - Non-controlled cooling to room temperature.

X-ray Diffraction (XRD) The phase amount of Co3O4 was calculated using Rietveld analysis.

Scanning Electron Microscopy (SEM) SEM imaging was performed at the acceleration voltage 10-20 KeV and Magnification range 1K-50K; Activity of ceramic catalyst in 3KW system The catalytic activity was determined using "Hydrogen-On-Demand" (HOD) release system as described in International Patent Application Publication No. WO 2019/202391, the content of which is incorporated herein, in its entirety, by reference.

Generally, activity (H 2 ml/sec/gr) was calculated in the following method: 50g of 2.3M KBH 4 and ceramics were placed in a 100ml flask. An upside-down measuring tube filled with water and placed in a bath was connected, using a hose, to the flask. The hydrogen generated flowed through the tube, pushing the water down the measuring tube. The amount of time it took to push a water volume (equivalent to the hydrogen volume generated) is the activity calculation. 0294883137- Example 1 Substrate selection The substrate must be stable under the fuel conditions, which are high pH, have minimal erosion from the hydrogen evolution.

The following substrates were examined: rutile-TiO 2, SiO 2, -Al 2O 3, -Al 2O 3 - Al2O3.

Table 1: Substrate weight loss (after 15 cycles in 5M KBH4) Substrate type Weight loss -Al2O3 Immediate dissolution -Al2O3 91.5% -Al2O3 4.2%TiO2 7.6%* SiO2 Immediate dissolution * based on 5 cycles and extrapolated to 15 cycles.

Figure 3 illustrates that the Co3O4 catalyst deposited on -alumina substrate exhibited a parabolic behavior, whereby the hydrogen production increased initially but then decreased over the cycles in fuel (5M KBH4 solution). This behavior was due to the high substrate dissolution rate during the process. Therefore, based on the catalytic behavior and the substrate's high dissolution -alumina substrate was not suitable as ceramic support for this application.

-Al2O3 had the lowest weight loss rate while providing the maximum hydrogen production ( Table 1 and Figure 3 ).

Example 2 Optimizing Co deposition solution Two types of cobalt solution were examined: - Solution A : 0.1M CoCl 2·6H 2O, 0.4M NaH 2PO 2·H 2O and pH=9.3.

- Solution B:CoCl2 dissolved in water: 2.4%wt [CoCl2·6H2O]. 20 0294883137- Table 2: Co deposition on a -Al2O3 substrate and resulting catalytic activity Solution Weight increase Activity [H2ml/sec/gr] Solution A 4% 0. Solution B 1% 0.

Table 2 demonstrates that the inclusion of sodium hypophosphite additive (Solution A) has a significant positive impact on both cobalt deposition (a 4% weight increase with Solution A) and catalytic activity (0.8 ml/sec/g). However, Solution B was preferable due to the solubility limit of CoCl2 in the presence of hypophosphite and the fact that hypophosphite provides no significant advantage over Solution B at the solubility limit.

The next step was to find the cobalt concentration that would yield the highest weight increase and activity. Due to the dissolution of -Al2O3, the work was continued -Al2O3.

Another way to increase the final amounts of cobalt oxide is by changing the concentration in the impregnation solution.

Three concentrations levels were used: 2.4wt%, 24wt% and 54wt% of CoCl2·6H2O ( Table 3 ). The samples were calcinated at 450 °C.

Based on the XRD analysis, as the percentage of CoCl2·6H2O increases from 2.4wt% to 24wt% and then to 54wt%, the resulting weight percentage of Co 3O 4 also increases from 0.2wt% ( Figure 4 ; See Table 6for ) to 2.6wt% ( Figure 5;See Table 6for ) and further to 5.1wt% ( Figure 6;See Table 6for ).

Table 3: Effect of CoCl2 concentration on the amount of Co3O4 and catalytic performance CoCl2 Concentration Weight increase Activity [H2ml/sec/gr] %Co3O4 (XRD) 2.4%wt CoCl 2 0% 0.2 0. 24%wt CoCl 2 3% 0.2 2. 0294883137- 54%wt CoCl2 6% 1.1 5.

Table 3 reveals a clear correlation between the concentration of cobalt salt and the resulting yield of cobalt oxide, with the latter increasing proportionally to the former. Notably, the solubility limit for cobalt chloride salt is 54%wt. By utilizing this concentration, cobalt oxide reached approximately 5.1%, a finding that was validated by XRD analysis ( Figure 6;See Table 6for ).

Utilizing a cobalt salt with higher solubility in water made it feasible to achieve a more significant final load of Co3O4. Specifically, XRD analysis ( Figure 7;See Table 6for ) shows that when a 64wt% solution of Co(NO3)2·6H2O was employed, a weight increase of about 8% Co 3O 4 was obtained.

Example 3 Degassing Degassing is a process that evacuates air or other substances (e.g., volatiles, humidity, etc.) trapped inside the pores of the porous ceramic support. To increase the cobalt oxide load inside the pores, a degassing procedure was employed on -Al2O3 beads that were placed in a flask under vacuum conditions for three hours. Then 54wt% CoCl 2 solution was injected into the flask and kept under vacuum for two more hours. The volume of the solution injected was equivalent of the volume of the pores according to the manufacturer's specification. Finally, the beads were calcinated at 450°C. Based on the XRD analysis, this procedure resulted in Co3O4 percentage reaching 9wt% ( Figure 8; See Table 6 for the values).

As further detailed in Table 4 , the degassing increased Co 3O 4 load from 5wt% to 9wt%.

Table 4: Effect of degassing on the amount of Co3O4 and catalytic performance Impregnation method Weight increase Activity [H2ml/sec/gr] %Co3O4 (XRD) 12-28 hours 5.8% 1.1 Degassing 11.5% 0.4 0294883137- It should be noted that while the initial activity was lower for higher Co3O4 loads, it is assumed that the short test duration prevented all the fuel from penetrating the internal pores, thus limiting the observation of the true impact of the degassing method on the initial activity.

As demonstrated in Figure 9 , the degassing procedure resulted in a higher Co3O4 load, which in turn yielded a ~20% increase in the total H 2 produced in each cycle.

Furthermore, SEM examination clearly indicates that the degassing procedure facilitates the incorporation of cobalt oxide particles inside the porous support: Figure 10 shows a cross-sectional -Al2O 3, impregnated for hours with 54wt% CoCl2·6H2O (without the degassing step) and calcinated at 450°C. There is no detectable cobalt oxide inside the examined ceramic bead (See Table 6 for the values).

Figure 11 shows a cross-sectional -Al 2O 3, impregnated with 54%wt CoCl 2·6H 2O using degassing method and calcinated at 450°C. The octahedral Co3O4 particles (circled) are abundantly present inside the examined ceramic bead (See Table 6 for the values).

Example 4 Optimizing calcination temperature The desired catalytic phase is controlled by the calcination temperature. Four different calcination temperatures were examined (i.e., 250°C, 450°C, 650°C and 850°C) using -Al2O3, impregnated with 54%wt CoCl2·6H2O.

At 250°C, the ceramic substrate retained purple color indicating that not all CoClwas converted into is cobalt oxide and most of the cobalt is in CoCl 2 form ( Figure 12;See Table 6 for the ). Therefore, while calcination at 250°c shows high weight increase and high activity it will not persist over time because the active CoCl2 will be quickly washed out from the ceramics.

As summarized in Table 5 below, at higher temperatures, (450°C, 650°C and 850°C) similar amounts of Co 3O 4, of ca. 5wt% were produced (as determined using XRD analysis (See Figure 6 , Figure 13and Figure 14 for calcination temperatures of 450°C, 650°C and 850°C respectively; See Table 6 ). 30 0294883137- Table 5: Effect of calcination temperature on the amount of Co3O4 and catalytic performance Calcination temp. Weight increase Activity [H2ml/sec/gr] %Co3O4 (XRD) 250°C 25% 3.3 0. 450°C 5.8% 1.1 650°C 6% 0.7 850°C 6.3% 0.1 5.

Table 6: values of XRD pattern Figure XRD pattern Figure Al 2O 3 25.5, 35, 37.7, 41.6, 43.2, 46.1, 52.4, 57.4, 59.6, 61, 61.2, 66.4, 68.1, 70.3, 74.2, 76.8, 77.1) Co3O4 31.2, 36.7, 59.3, 59.3, 65.1, 68.5, 69.6, 77.3) Figure Al 2O 59.7, 61, 61.2, 66.4, 68.1, 70.3, 74.2, 76.8, 77.2) Co 3O 68.5, 74, 77.3, 78.3) Figure Al2O3 25.5, 35.1, 37.7, 41.6, 43.3, 46.1, 52.5, 57.4, 59.7, 61.1, 61.2, 66.5, 68.1, 70.4, 74.2, 76.8, 77.2) Co 3O 4 31.2, 36.8, 38.5, 44.7, 55.6, 59.3, 59.3, 65.2, 68.6, 77.3) Figure Al 2O 3 25.4, 35, 37.6, 43.2, 46, 52.4, 57.3, 59.6, 61, 61.2, 66.4, 68.1, 74.2, 76.7, 77.1) Co3O4 31.1, 36.7, 38.4, 44.7, 55.5, 59.2, 59.2, 65.1, 68.5, 77.2, 78.3) Figure Al2O3 25.4, 35, 37.6, 43.2, 46, 52.4, 57.3, 59.6, 61, 61.1, 66.4, 68, 74.1, 76.7, 77.1) Co 3O 4 31.1, 36.7, 38.4, 44.6, 55.5, 59.2, 59.2, 65.1, 68.5, 74, 77.2, 78.2) 0294883137- Figure Al2O3 25.5, 35.1, 37.7, 43.3, 46.1, 52.5, 57.4, 59.7, 61.1, 61.2, 66.5, 68.2, 70.4, 74.2, 76.8, 77.2) CoCl 2·6H 2 25.1, 28.6, 29.8, 30.4, 31.7, 32.4, 32.7, 32.9, 34.9, 37.2, 40.6, 40.8, 40.8, 40.9, 41, 43.4, 43.5, 44.4, 45.5, 45.6, 46.5, 46.8, 47.7, 48.6, 48.7, 49.5, 50.3, 51.7, 53.6, 54.3, 55.2, 57, 57.1, 57.4, 57.6, 58.5, 59.4, 61.6, 62.6, 63.3, 63.9, 67.9, 68.5, 69, 69.6, 74.4, 74.8, 76.7) Figure Al 2O 3 25.5, 35, 37.7, 43.2, 46.1, 52.4, 57.4, 59.6, 61, 61.2, 66.4, 68.1, 70.3, 74.2, 76.8, 77.1) Co3O4 31.2, 36.7, 38.4, 44.7, 55.6, 59.3, 59.3, 65.1) Figure Al 2O 3 25.4, 35, 37.6, 41.5, 43.2, 46, 52.4, 57.4, 59.6, 61, 61.2, 66.4, 68.1, 70.3, 74.2, 76.8, 77.1) Co3O4 31.1, 36.7, 38.4, 44.7, 55.5, 59.2, 59.2, 65.1, 74, 77.2, 78.3) Example 5 Ceramic catalyst performance The performance of the ceramic catalyst ( -Al2O3, impregnated with 54wt% CoCl 2·6H 2O and calcinated at 450°C) was tested in the 3KW system using 5M KBH 4. The catalyst weight was adjusted to give the proper hydrogen flow. The results show stable performance after 40 cycles ( Figure 15 ).

Furthermore, throughout the process, no residues indicating the dissolution of the ceramic support were detected, suggesting a high level of durability for the ceramic catalyst.

Claims

23 303685/ 02948831104- CLAIMS:

1. A catalyst comprising -Al2O3 associated with cobalt oxide including at least Co2+ and Co3+ oxidation states.

2. The catalyst of claim 1, wherein at least part of said cobalt oxide is in particulate form.

3. The catalyst of claim 1 or 2, wherein said cobalt oxide is selected from the group consisting of Co3O4, Co2O3, CoO, Co2AlO4, CoAl2O4.

4. The catalyst of any one of claims 1 to 3, wherein said cobalt oxide comprises Co3O4.

5. The catalyst of any one of claims 1 to 4, wherein said -Al2O3 is porous and said cobalt oxide is at least within said pores of said -Al2O3.

6. The catalyst of any one of claims 1 to 5, comprising said cobalt oxide in an amount of between 0.1wt% and 40wt% out of the total weight of said catalyst.

7. The catalyst of any one of claims 2 to 6, wherein said particulate form of said cobalt oxide has a particle size of between 10nm to 10 micron.

8. The catalyst of any one of claims 1 to 7, being free of detectable amount of noble metals.

9. The catalyst of any one of claims 1 to 8, being free of detectable amount of electrically conductive substances.

10. The catalyst of any one of claims 1 to 9, exhibiting catalytic activity for dehydrogenation of a target compound selected from the group consisting of potassium borohydride, sodium borohydride, lithium borohydride, ammonium borohydride, tetramethyl ammonium borohydride, and mixtures thereof.

11. The catalyst of claim 10, wherein said target compound is potassium borohydride.

12. The catalyst according to claim 10 or 11, having catalytic activity when determined in a Hydrogen On Demand release system operated at 5M KBH4 in H2O.

13. A method of preparing a catalyst, the method comprises: 24 303685/ 02948831104- impregnating -Al2O3 with an aqueous solution comprising Co2+ to form impregnated -Al2O3; and subjecting said impregnated -Al2O3 to thermal treatment causing formation of cobalt oxide.

14. The method of claim 13, wherein said aqueous solution comprises cobalt salt.

15. The method of claims 14, wherein said cobalt salt is selected from the group consisting of cobalt acetate (Co(CH3COO)2), cobalt bromide (CoBr2), cobalt chloride (CoCl2), cobalt formate (Co(HCOO)2), cobalt nitrate (Co(NO3)2), cobalt sulfate (CoSO4), cobalt tartrate (CoC4H4O6), and combinations thereof.

16. The method of claim 14 or 15, wherein said cobalt salt comprises cobalt chloride (CoCl2).

17. The method of claim 14 or 15, wherein said cobalt salt comprises cobalt nitrate (Co(NO3)2).

18. The method of any one of claims 13 to 17, wherein said cobalt salt is at a concentration of at least 2wt%.

19. The method of any one of claims 14 to 18, wherein said cobalt salt is at a concentration within a range of between 2wt% and 60wt% when determined at a temperature of 20°C.

20. The method of any one of claims 13 to 19, comprising subjecting said -Al2Oto negative pressure at least prior to said impregnation.

21. The method of any one of claims 13 to 20, comprising subjecting said -Al2Oto negative pressure at least during said impregnation.

22. The method of any one of claims 13 to 21, wherein said thermal treatment comprises heating said impregnated -Al2O3 to a temperature between 150°C and 1000°C.

23. The method of any one of claims 13 to 22, wherein said thermal treatment is conducted under a gas selected from the group consisting of oxygen, hydrogen, nitrogen, argon and mixtures thereof.

24. The method of any one of claims 13 to 23, wherein said thermal treatment is applied for a time period of at least 1 hour. 25 303685/ 02948831104-

25. The method of any one of claims 13 to 24, wherein said thermal treatment comprises step-wise heating of said impregnated -Al2O3.

26. The method of any one of claims 13 to 25, comprising drying the impregnated -Al2O3 prior to said thermal treatment.

27. The method of claim 26, comprises heating said impregnated -Al2O3 to a temperature of up to 250°C.

28. The method of claim 26 or 27, wherein said drying comprises step-wise drying.

29. A catalyst obtained or obtainable by the method of any one of claims 13 to 29.

30. A process for hydrogen generation, the process comprises contacting a catalyst comprising -Al2O3 associated with cobalt oxide including at least Co2+ and Co3+ oxidation states with a solution comprising borohydride compound and proton donor solvent.

31. The process of claim 30, wherein said catalyst is as defined in any one of claims 1 to 11, or obtained by the method of any one of claims 13 to 28.

32. The process of claim 30 or 31, wherein said borohydride compound is selected from the group consisting of: potassium borohydride, sodium borohydride, lithium borohydride, ammonium borohydride, tetramethyl ammonium borohydride, and mixtures thereof.

33. The process of any one of claims 30 to 32, wherein said borohydride compound comprises potassium borohydride.

34. The process of any one of claims 30 to 33, wherein the proton donor solvent is selected from the group consisting of: water, ethanol, methanol, propanol, isopropanol, butanol, isobutanol, propanediol, ethylene glycol, glycerol, and mixtures thereof.

35. The process of any one of claims 30 to 34, wherein the proton donor solvent comprises water.

36. The process of any one of claims 30 to 35, comprising two or more hydrogen generation cycles. 26 303685/ 02948831104-

37. The process of claim 36, wherein said catalyst maintains its mechanical integrity and/or catalytic activity for at least 40 hydrogen generation cycles.