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.

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.

A process for the treatment of a light naphtha feedstock that comprises normal paraffins and iso-paraffins may include separating the feedstock into a first iso-paraffin stream and a normal paraffin stream. The separating may be performed with 5A molecular sieves, a pressure of about 1-3 bars, and a temperature of 100-260° C. A product stream may be provided by subjecting the normal paraffin stream to at least one of steam cracking, isomerizing, and aromatizing.

A process for the treatment of a light naphtha feedstock that comprises normal paraffins and iso-paraffins may include separating the feedstock into a first iso-paraffin stream and a normal paraffin stream. The separating may be performed with 5A molecular sieves, a pressure of about 1-3 bars, and a temperature of 100-260° C. A product stream may be provided by subjecting the normal paraffin stream to at least one of steam cracking, isomerizing, and aromatizing.

A process to produce 1-octene and 1-decene includes (a) separating a composition containing an oligomer product—which contains from 15 to 80 mol % C.sub.6 olefins, from 20 to 80 mol % C.sub.8 olefins, and from 5 to 20 mol % C.sub.10+ olefins—into a first oligomer composition containing C.sub.6 alkanes and at least 85 mol % C.sub.6 olefins (e.g., 1-hexene), a second oligomer composition containing at least 85 mol % C.sub.8 olefins (e.g., 1-octene), and a heavies stream containing C.sub.10+ olefins, then (b) contacting a metathesis catalyst system with the first oligomer composition to form a first composition comprising C.sub.10 linear internal olefins, (c) contacting the C.sub.10 linear internal olefins with an isomerization hydrofunctionalization catalyst system to form a second composition containing a functionalized alkane, (d) retro-hydrofunctionalizing the functionalized alkane to form a third composition containing 1-decene, and (e) purifying the third composition to isolate a fourth composition containing at least 90 mol % 1-decene. Processes to produce 1-hexene and 1-decene also are described, as well as related manufacturing systems.

A process to produce 1-octene and 1-decene includes (a) separating a composition containing an oligomer product—which contains from 15 to 80 mol % C.sub.6 olefins, from 20 to 80 mol % C.sub.8 olefins, and from 5 to 20 mol % C.sub.10+ olefins—into a first oligomer composition containing C.sub.6 alkanes and at least 85 mol % C.sub.6 olefins (e.g., 1-hexene), a second oligomer composition containing at least 85 mol % C.sub.8 olefins (e.g., 1-octene), and a heavies stream containing C.sub.10+ olefins, then (b) contacting a metathesis catalyst system with the first oligomer composition to form a first composition comprising C.sub.10 linear internal olefins, (c) contacting the C.sub.10 linear internal olefins with an isomerization hydrofunctionalization catalyst system to form a second composition containing a functionalized alkane, (d) retro-hydrofunctionalizing the functionalized alkane to form a third composition containing 1-decene, and (e) purifying the third composition to isolate a fourth composition containing at least 90 mol % 1-decene. Processes to produce 1-hexene and 1-decene also are described, as well as related manufacturing systems.

A process for combined renewable 1-decene and renewable carboxylic diacid production from a fatty acid ester containing feedstock, wherein the feedstock is first subjected to metathesis reaction conditions, recovery of 1-decene and then to microbial oxidation to yield diacids in a fermentation broth. Diacids of unusual carbon chains lengths are thereby obtainable.

A process for combined renewable 1-decene and renewable carboxylic diacid production from a fatty acid ester containing feedstock, wherein the feedstock is first subjected to metathesis reaction conditions, recovery of 1-decene and then to microbial oxidation to yield diacids in a fermentation broth. Diacids of unusual carbon chains lengths are thereby obtainable.

A molecular sieve has a silica/alumina molar ratio of 100-300, and has a mesopore structure. One closed hysteresis loop appears in the range of P/P.sub.0=0.4-0.99 in the low temperature nitrogen gas adsorption-desorption curve, and the starting location of the closed hysteresis loop is in the range of P/P.sub.0=0.4-0.7. The catalyst formed from the molecular sieve as a solid acid not only has a good capacity of isomerization to reduce the freezing point, but also can produce a high yield of the product with a lower pour point. The process for preparing the catalyst involves steps including crystallization, filtration, calcination, and hydrothermal treatment.

A molecular sieve has a silica/alumina molar ratio of 100-300, and has a mesopore structure. One closed hysteresis loop appears in the range of P/P.sub.0=0.4-0.99 in the low temperature nitrogen gas adsorption-desorption curve, and the starting location of the closed hysteresis loop is in the range of P/P.sub.0=0.4-0.7. The catalyst formed from the molecular sieve as a solid acid not only has a good capacity of isomerization to reduce the freezing point, but also can produce a high yield of the product with a lower pour point. The process for preparing the catalyst involves steps including crystallization, filtration, calcination, and hydrothermal treatment.