A reaction chamber for generating hydrogen gas using a hydrogen liquid carrier line may include a channel including a catalyst for causing the hydrogen gas to be produced from a hydrogen liquid carrier, the channel including an inlet end for the hydrogen liquid carrier and an outlet end for a spent carrier. The reaction chamber may also include a valve for controlling a rate of flow of the hydrogen liquid carrier flowing through the channel; a gas outlet for evacuating the hydrogen gas generated in the channel; and at least one processor configured to receive at least one indicator of a demand for the hydrogen gas and to control the valve to adjust the rate of flow of the hydrogen liquid carrier to meet the demand for the hydrogen gas.

A catalyst for preparing chlorine gas by hydrogen chloride oxidation, comprising the following components calculated according to mass content based on the total weight of the catalyst: 0.5-20 wt % copper; 2-10 wt % manganese; 0.05-2 wt % boron; 0.01-3 wt % chromium; 0.1-10 wt % rare earth metal; 0.1-10 wt % potassium; and 3-15 wt % titanium; also comprising 0.02-1.1 wt % phosphorus; and 0.03-1.9 wt % iron; the carrier content is 55-90 wt %. In the case of a fluidized bed reactor, the present catalyst can achieve a one-way hydrogen chloride conversion rate of 80-85%. Almost all of the 0-1000 mg/kg of chlorinated benzene contained in hydrogen chloride gas can be converted into CO.sub.2 and H.sub.2O without generating polychlorinated benzene.

A carbon catalyst has improved catalytic activity, and an electrode and a battery include the carbon catalyst. A carbon catalyst includes a metal and phosphorus atoms, wherein a ratio of a concentration (atomic %) of the phosphorus atoms exhibiting a peak having a peak top within a range of 132.50.3 eV and having a full width at half maximum of 2.00.5 eV, which is obtained by peak separation of a phosphorus atom P2p peak, with respect to a concentration (atomic %) of carbon atoms in X-ray photoelectron spectroscopic measurement is 0.0005 or more.

This present disclosure is directed to methods for the preparation of a hydrotreatment catalyst, such as nanoscale nickel phosphide (i.e., Ni.sub.2P) particles supported on high-surface area metal oxides (e.g., silica, alumina, amorphous silica-alumina), in a manner that is compatible with conditions employed in commercial hydrotreating units. The catalyst synthesis includes impregnation, drying, and in situ reduction, and can provide highly active catalysts for the removal of S and N impurities from crude oil fractions.

Disclosed are cathodes comprising a conductive support substrate having a catalyst coating including Ni.sub.5P.sub.4 nanocrystals. The conductive support substrate is capable of incorporating a material to be reduced, such as water or hydrogen cations. Also disclosed are methods for generating hydrogen gas from water via an electrolysis reaction or from the reduction of hydrogen cations, wherein the catalyst is part of a conductive support within a cathode, including (a) placing an anode and the inventive cathode in an electrolyte, (b) placing the anode and cathode in conductive contact with an external source of electricity, (c) providing a source of water to the cathode, and (d) using the external source of electricity to drive an electrolysis reaction at the cathode, whereby the hydrogen gas is generated from water. In certain embodiments, the reaction uses a free catalyst, wherein the catalyst is placed in proximity to the cathode.

A catalyst comprising a calcined oxide matrix which is mainly alumina and an active phase comprising nickel, said active phase being at least partially co-mixed within said calcined oxide matrix which is mainly alumina, the nickel content being in the range 5% to 65% by weight of said element with respect to the total mass of catalyst, said active phase not comprising any metal from group VIB, the nickel particles having a diameter of less than 15 nm, said catalyst having a median mesopore diameter in the range 12 nm to 25 nm, a median macropore diameter in the range 50 to 300 nm, a mesopore volume, measured by mercury porosimetry, of 0.40 mL/g or more and a total pore volume, measured by mercury porosimetry, of 0.45 mL/g or more. The process for the preparation of said catalyst, and its use in a hydrogenation process.

The process for obtaining M.sup.1BH.sub.4, the process comprising contacting M.sup.1-B0.sub.2 with a metal M.sup.2 in the presence of molecular hydrogen (H.sub.2) under conditions permitting the formation of M.sup.1-BH.sub.4 and M.sup.2-oxide, wherein the M.sup.1 is a metal selected from column I of the periodic table of elements or alloys of metals selected from column I of the periodic table of elements and M.sup.2 is a metal or an alloy of metals selected from column II of the periodic table of elements, provided that M.sup.2 is not Mg and M.sup.1 is different from M.sup.2.

The present disclosure relates to a method that includes heating a mixture that includes a metal phenylphosphine-containing precursor that includes at least one of Mo(PPh.sub.3).sub.2(CO).sub.4, Pd(PPh.sub.3).sub.4, Ru(PPh.sub.3).sub.3Cl.sub.2, Ru(PPh.sub.3).sub.2(CO).sub.2Cl.sub.2, Co(PPh.sub.3)(CO).sub.2(NO), and/or Rh(PPh.sub.3).sub.2(CO)Cl, a surfactant, and a solvent. The heating is to a target temperature to form a heated mixture containing a metal phosphide nanoparticle that includes at least one of MoP, Ru.sub.2P, Co.sub.2P, Rh.sub.2P, and/or Pd.sub.3P, and the metal phosphide nanoparticle is not hollow.

The present invention relates to a Fe-based hydrogenation catalyst having Fe as a primary active metal component, and zinc and potassium as a first co-active metal component. The molar ratio of the primary active metal component to the first co-active metal component is 0.5-200:1. The Fe-based hydrogenation catalyst in present invention overcomes the problem of limiting to the active metal components as used over decades for the conventional hydrogenation catalyst, and thus has long-term values for industrial application.

The present invention relates to a hydrotreating catalyst comprising at least one group VIB metal, at least one group VIII metal and an alumina support having a gamma alumina content greater than 50% by weight and less than 100% by weight with respect to the weight of the support, said support having a specific surface area comprised between 25 and 150 m.sup.2/g.