Abstract: The invention relates to a process for producing a hydrocarbon component of biological origin. The process comprises at least two steps, the first one of which is a HDO step and the second one is an isomerization step operated using the counter-current flow principle. A biological raw material containing fatty acids and/or fatty acid esters serves as the feed stock.

Abstract: The invention relates to a process for the manufacture of diesel range hydrocarbons wherein a feed is hydrotreated in a hydrotreating step and isomerised in an isomerisation step, and a feed comprising fresh feed containing more than 5 wt % of free fatty acids and at least one diluting agent is hydrotreated at a reaction temperature of 200-400° C., in a hydrotreating reactor in the presence of catalyst, and the ratio of the diluting agent/fresh feed is 5-30:1.

Abstract: A method for dimerizing isobutene, wherein, in dimerizing conditions, the isobutene is brought into contact with a porous cation exchange resin comprising a styrene polymer, which is cross-linked with divinyl benzene, and any sulphonic acid groups adhering to the polymer. The harmful deactivation of this catalyst, which is caused by the accumulation of the oligomers and polymers of isobutene and other C4-olefins in the cation exchange resin catalyst, is essentially decreased by selecting the cation exchange resin from a group including cation exchange resins, the acid,capacity of which is 4.7 equivalents/kg at a minimum, and the portion of divinyl benzene units of which is 5% by weight at a minimum and smaller than 20% by weight.

Abstract: The present invention relates to a process for the hydrogenation of olefins. The process comprises hydrogenation of a feed stock comprising more than 90 wt-% of olefins, carried out in a hydrogenation reactor comprising at least two reaction stages, wherein the feed stock is hydrogenated in the first reaction stage equipped with a cooling circuit and comprising a first and an optional second catalyst bed, and the effluent from the first reaction stage is hydrogenated in the final reaction stage comprising one or more catalyst beds and optionally equipped with a cooling circuit, the process is operated in trickling or pulse flow mode in a three phase reactor with a fixed catalyst bed and at least one catalyst of same or different type is used in each stage, the catalyst having different particle size and/or optionally different shape in at least two stages.

Abstract: The invention relates to a method for dimerizing isobutene, wherein, in dimerizing conditions, the isobutene is brought into contact with a porous cation exchange resin comprising a styrene polymer, which is cross-linked with divinyl benzene, and any sulphonic acid groups adhering to the polymer. The harmful deactivation of this catalyst, which is caused by the accumulation of the oligomers and polymers of isobutene and other C4-olefins in the cation exchange resin catalyst, is essentially decreased by selecting the cation exchange resin from a group including cation exchange resins, the acid capacity of which is 4.7 equivalents/kg at a minimum, and the portion of divinyl benzene units of which is 5% by weight at a minimum and smaller than 20% by weight.

Abstract: The invention relates to a process for producing a hydrocarbon component of biological origin. The process comprises at least two steps, the first one of which is a HDO step and the second one is an isomerization step operated using the counter-current flow principle. A biological raw material containing fatty acids and/or fatty acid esters serves as the feed stock.

Abstract: The invention relates to a method for dimerizing isobutene, wherein, in dimerizing conditions, the isobutene is brought into contact with a porous cation exchange resin comprising a styrene polymer, which is cross-linked with divinyl benzene, and any sulphonic acid groups adhering to the polymer. The harmful deactivation of this catalyst, which is caused by the accumulation of the oligomers and polymers of isobutene and other C4-olefins in the cation exchange resin catalyst, is essentially decreased by selecting the cation exchange resin from a group including cation exchange resins, the acid capacity of which is 4.7 equivalents/kg at a minimum, and the portion of divinyl benzene units of which is 5% by weight at a minimum and smaller than 20% by weight.