Abstract: A particulate desulfurization material includes one or more copper compounds supported on a zinc oxide support material, wherein the desulfurization material has a copper content in the range 0.1 to 5.0% by weight and a tapped bulk density ?1.55 kg/l. The material is obtained by (i) mixing a powdered copper compound with a particulate zinc support material comprising zinc oxide and one or more precursors that form zinc oxide upon calcination, and one or more binders to form a copper-containing composition, (ii) shaping the copper-containing composition by granulation, and (iii) drying and calcining the resulting granulated material.

Abstract: A particulate desulfurization material includes one or more copper compounds supported on a zinc oxide support material, wherein the desulfurization material has a copper content in the range 0.1 to 5.0% by weight and a tapped bulk density ?1.55 kg/l. The material is obtained by (i) mixing a powdered copper compound with a particulate zinc support material comprising zinc oxide and one or more precursors that form zinc oxide upon calcination, and one or more binders to form a copper-containing composition, (ii) shaping the copper-containing composition by granulation, and (iii) drying and calcining the resulting granulated material.

Abstract: A particulate desulphurization material includes one or more copper compounds supported on a zinc oxide support material, wherein the desulphurization material has a copper content in the range 0.1 to 5.0% by weight and a tapped bulk density ?1.55 kg/l. The material is obtained by (i) mixing a powdered copper compound with a particulate zinc support material comprising zinc oxide and one or more precursors that form zinc oxide upon calcination, and one or more binders to form a copper-containing composition, (ii) shaping the copper-containing composition by granulation, and (iii) drying and calcining the resulting granulated material.

Abstract: A process for reducing the thiophene content in a synthesis gas mixture, comprises the steps of (i) passing a synthesis gas mixture comprising hydrogen and carbon oxides and containing thiophene over a copper-containing sorbent disposed in a sorbent vessel at an inlet temperature in the range 200-280° C., (ii) withdrawing a thiophene depleted synthesis gas containing methanol from the sorbent vessel, and (iii) adjusting the temperature of the methanol-containing thiophene-depleted synthesis gas mixture. The resulting gas mixture may be used for production of chemicals, e.g. methanol production or for the Fischer-Tropsch synthesis of liquid hydrocarbons, for hydrogen production by using water gas shift, or for the production of synthetic natural gas.

Abstract: A particulate desulphurisation material is described including one or more copper compounds supported on a zinc oxide support material, wherein the desulphurisation material has a copper content in the range 0.1 to 5.0% by weight and a tapped bulk density?1.55 kg/l.

Abstract: A process for desulphurizing hydrocarbons includes passing a mixture of hydrocarbon and hydrogen over a hydrodesulphurization catalyst to convert organosulphur compounds present in the hydrocarbon to hydrogen sulphide, passing the resulting mixture over a hydrogen sulphide sorbent including zinc oxide to reduce the hydrogen sulphide content of the mixture, and passing the hydrogen sulphide-depleted mixture over a further desulphurization material. The further desulphurization material includes one or more nickel compounds, a zinc oxide support material, and optionally one or more promoter metal compounds of iron, cobalt, copper and precious metals. The desulphurization material has a nickel content in the range 0.3 to 20% by weight and a promoter metal compound content in the range 0 to 10% by weight.

Abstract: A process for hydrogenating olefins is disclosed. The olefins are present in a feed gas which includes H2 and one or more sulfur compounds. The sulfur compounds may include H2S and organic sulfur compounds. The feed gas is passed through a reactor at an inlet temperature from 100° C. to 250° C. The reactor contains a catalyst which is active at the inlet temperature. The reactor may be adiabatic. Saturated hydrocarbons are formed from the olefins. A temperature gradient may be formed in the reactor due to the exothermic nature of the hydrogenation reaction, causing the temperature to increase downstream in the reactor. At temperatures higher than the inlet temperature, H2S may be formed from organic sulfur compounds. A gas mixture including saturated hydrocarbons, H2S and H2 exits the reactor and may be brought into contact with a chemical adsorbent which removes the H2S. The gas stream may then be passed to a steam methane reformer.

Abstract: A process is described for reducing the thiophene content in a synthesis gas mixture, comprising comprises the steps of (i) passing a synthesis gas mixture comprising hydrogen and carbon oxides and containing thiophene over a copper-containing sorbent disposed in a sorbent vessel at an inlet temperature in the range 200-280 oC, (ii) withdrawing a thiophene depleted synthesis gas containing methanol from the sorbent vessel, and (iii) adjusting the temperature of the methanol-containing thiophene-depleted synthesis gas mixture. The resulting gas mixture may be used for production of chemicals, e.g. methanol production or for the Fischer-Tropsch synthesis of liquid hydrocarbons, for hydrogen production by using water gas shift, or for the production of synthetic natural gas.

Abstract: A process for desulphurising hydrocarbons includes the steps of (i) passing a mixture of hydrocarbon and hydrogen over a hydrodesulphurisation catalyst to convert organosulphur compounds present in the hydrocarbon to hydrogen sulphide, (ii) passing the resulting mixture over a hydrogen sulphide sorbent including zinc oxide to reduce the hydrogen sulphide content of the mixture and (iii) passing the hydrogen sulphide-depleted mixture over a further desulphurisation material, where the further desulphurisation material includes one or more nickel compounds, a zinc oxide support material, and optionally one or more promoter metal compounds selected from one or more compounds of iron, cobalt, copper and precious metals, the desulphurisation material having a nickel content in the range 0.3 to 20% by weight and a promoter metal content in the range 0 to 10% by weight.

Abstract: A particulate desulfurization material includes one or more nickel compounds, a zinc oxide support material, and one or more alkali metal compounds wherein the nickel content of the material is in the range 0.3 to 10% by weight and the alkali metal content of the material is in the range 0.2 to 10% by weight. A method of making the desulfurization material includes the steps: (i) contacting a nickel compound with a particulate zinc support material and an alkali metal compound to form an alkali-doped composition, (ii) shaping the alkali-doped composition, and (iii) drying, calcining, and optionally reducing the resulting material. The desulfurization material may be used to desulfurize hydrocarbon gas streams with reduced levels of hydrocarbon hydrogenolysis.

Abstract: A particulate desulphurisation material includes one or more nickel compounds, a zinc oxide support material, and one or more alkali metal compounds wherein the nickel content of the material is in the range 0.3 to 10% by weight and the alkali metal content of the material is in the range 0.2 to 10% by weight. A method of making the desulphurisation material includes the steps: (i) contacting a nickel compound with a particulate zinc support material and an alkali metal compound to form an alkali-doped composition, (ii) shaping the alkali-doped composition, and (iii) drying, calcining, and optionally reducing the resulting material. The desulphurisation material may be used to desulphurise hydrocarbon gas streams with reduced levels of hydrocarbon hydrogenolysis.

Abstract: A process for hydrogenating olefins is disclosed. The olefins are present in a feed gas which includes H2 and one or more sulfur compounds. The sulfur compounds may include H2S and organic sulfur compounds. The feed gas is passed through a reactor at an inlet temperature from 100° C. to 250° C. The reactor contains a catalyst which is active at the inlet temperature. The reactor may be adiabatic. Saturated hydrocarbons are formed from the olefins. A temperature gradient may be formed in the reactor due to the exothermic nature of the hydrogenation reaction, causing the temperature to increase downstream in the reactor. At temperatures higher than the inlet temperature, H2S may be formed from organic sulfur compounds. A gas mixture including saturated hydrocarbons, H2S and H2 exits the reactor and may be brought into contact with a chemical adsorbent which removes the H2S. The gas stream may then be passed to a steam methane reformer.