A process for producing a diene, preferably a conjugated diene, more preferably 1,3-butadiene, includes the steps of dehydrating at least one alkenol in the presence of at least one catalytic material having at least one acid catalyst based on silica (SiO.sub.2) and alumina (Al.sub.2O.sub.3), preferably a silica-alumina (SiO.sub.2—Al.sub.2O.sub.3), the catalyst having an alumina content (Al.sub.2O.sub.3) lower than or equal to 12% by weight, preferably between 0.1% by weight and 10% by weight, with respect to the catalyst total weight. The alumina content is referred to the catalyst total weight without binder, and a pore modal diameter between 9 nm and 170 nm, preferably between 10 nm and 150 nm, still more preferably between 12 nm and 120 nm. Preferably, the alkenol is obtainable directly from biosynthetic processes, or catalytic dehydration processes of at least one diol, preferably a butanediol, more preferably 1,3-butanediol, still more preferably bio-1,3-butanediol, deriving from biosynthetic processes.

A process for producing a diene, preferably a conjugated diene, more preferably 1,3-butadiene, includes the steps of dehydrating at least one alkenol in the presence of at least one catalytic material having at least one acid catalyst based on silica (SiO.sub.2) and alumina (Al.sub.2O.sub.3), preferably a silica-alumina (SiO.sub.2—Al.sub.2O.sub.3), the catalyst having an alumina content (Al.sub.2O.sub.3) lower than or equal to 12% by weight, preferably between 0.1% by weight and 10% by weight, with respect to the catalyst total weight. The alumina content is referred to the catalyst total weight without binder, and a pore modal diameter between 9 nm and 170 nm, preferably between 10 nm and 150 nm, still more preferably between 12 nm and 120 nm. Preferably, the alkenol is obtainable directly from biosynthetic processes, or catalytic dehydration processes of at least one diol, preferably a butanediol, more preferably 1,3-butanediol, still more preferably bio-1,3-butanediol, deriving from biosynthetic processes.

A process for producing a diene, preferably a conjugated diene, more preferably 1,3-butadiene, includes the steps of dehydrating at least one alkenol in the presence of at least one catalytic material having at least one acid catalyst based on silica (SiO.sub.2) and alumina (Al.sub.2O.sub.3), preferably a silica-alumina (SiO.sub.2—Al.sub.2O.sub.3), the catalyst having an alumina content (Al.sub.2O.sub.3) lower than or equal to 12% by weight, preferably between 0.1% by weight and 10% by weight, with respect to the catalyst total weight. The alumina content is referred to the catalyst total weight without binder, and a pore modal diameter between 9 nm and 170 nm, preferably between 10 nm and 150 nm, still more preferably between 12 nm and 120 nm. Preferably, the alkenol is obtainable directly from biosynthetic processes, or catalytic dehydration processes of at least one diol, preferably a butanediol, more preferably 1,3-butanediol, still more preferably bio-1,3-butanediol, deriving from biosynthetic processes.

According to one or more embodiments of the present disclosure, chemical streams may be processed by a method which may comprise operating a first chemical process, stopping the first chemical process and removing the first catalyst from the reactor, and operating a second chemical process. The reaction of the first chemical process may be a dehydrogenation reaction, a cracking reaction, a dehydration reaction, or a methanol-to-olefin reaction. The reaction of the second chemical process may be a dehydrogenation reaction, a cracking reaction, a dehydration reaction, or a methanol-to-olefin reaction. The first reaction and the second reaction may be different types of reactions.

According to one or more embodiments of the present disclosure, chemical streams may be processed by a method which may comprise operating a first chemical process, stopping the first chemical process and removing the first catalyst from the reactor, and operating a second chemical process. The reaction of the first chemical process may be a dehydrogenation reaction, a cracking reaction, a dehydration reaction, or a methanol-to-olefin reaction. The reaction of the second chemical process may be a dehydrogenation reaction, a cracking reaction, a dehydration reaction, or a methanol-to-olefin reaction. The first reaction and the second reaction may be different types of reactions.

According to one or more embodiments of the present disclosure, chemical streams may be processed by a method which may comprise operating a first chemical process, stopping the first chemical process and removing the first catalyst from the reactor, and operating a second chemical process. The reaction of the first chemical process may be a dehydrogenation reaction, a cracking reaction, a dehydration reaction, or a methanol-to-olefin reaction. The reaction of the second chemical process may be a dehydrogenation reaction, a cracking reaction, a dehydration reaction, or a methanol-to-olefin reaction. The first reaction and the second reaction may be different types of reactions.

Methods for reducing or reusing emissions and waste from oil and gas processing facilities are described. Specifically, emission and waste streams can be partially oxidized before being treated in a modified syngas fermentation process with parallel bioreactors to produce commodity chemicals of commercial importance while lowering greenhouse gas emissions. At least one bioreactor is online at all times, offline reactors being emptied to collect product and recharged for use.

Methods for reducing or reusing emissions and waste from oil and gas processing facilities are described. Specifically, emission and waste streams can be partially oxidized before being treated in a modified syngas fermentation process with parallel bioreactors to produce commodity chemicals of commercial importance while lowering greenhouse gas emissions. At least one bioreactor is online at all times, offline reactors being emptied to collect product and recharged for use.

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.