Systems are provided that permit temperature control of a catalyst bed for conversion of alcohols to fuel hydrocarbons by modulating the water content of the alcohol feed stream provided to the catalyst bed. In some embodiments a secondary catalyst bed is provided for the conversion of light hydrocarbons found in the initial hydrocarbon product to fuel hydrocarbons that are liquid at ambient temperature and pressure.

Methods of catalytic hydrogenation, including methods that may be used to hydrogenate an unsaturated reactant to produce an at least partially saturated product that may be a solid at 20° C. Systems for catalytic hydrogenation that may include a reactor bed containing one or more activated carbon monolith catalysts. At least 97% of unsaturated bonds may be saturated by the methods and systems.

The present invention relates to a method for producing mixtures of hydrocarbons and aromatic compounds, for use as fuel components (preferably in the range C5-C16), by means of catalytic conversion of the oxygenated organic compounds contained in aqueous fractions derived from biomass treatments, wherein said method can comprise at least the following steps: (i) bringing the aqueous mixture containing the oxygenated organic compounds derived from biomass in contact with a catalyst comprising at least Sn and Nb, Sn and Ti, and combinations of Sn, Ti and Nb; (ii) reacting the mixture with the catalyst in a catalytic reactor at temperatures between 100 and 350° C. and under pressures from 1 to 80 bar in the absence of hydrogen; and (iii) recovering the products obtained by means of the liquid/liquid separation of the aqueous and organic phases.

Systems and methods are provided that permit temperature control of a catalyst bed for conversion of alcohols to fuel hydrocarbons by modulating the water content of the alcohol feed stream provided to the catalyst bed. Heat generated by exothermic reactions in the catalyst bed can be utilized to pre-heat the alcohol feed stream. In some embodiments a secondary catalyst bed is provided for the conversion of light hydrocarbons found in the initial hydrocarbon product to fuel hydrocarbons that are liquid at ambient temperature and pressure.

Pyrolysis methods and apparatuses that allow effective heat removal, for example when necessary to achieve a desired throughput or process a desired type of biomass, are disclosed. According to representative methods, the use of a quench medium (e.g., water), either as a primary or a secondary type of heat removal, allows greater control of process temperatures, particularly in the reheater where char, as a solid byproduct of pyrolysis, is combusted. Quench medium may be distributed to one or more locations within the reheater vessel, such as above and/or within a dense phase bed of fluidized particles of a solid heat carrier (e.g., sand) to better control heat removal.

The present invention relates to a method for processing a renewable bio-based material comprising the step of reacting the bio-based material with hydrogen in the presence of a catalyst on a support in a reactor to form a treated oil; (i) passing the treated oil through a distillation unit and an adsorption unit to form green diesel; and/or (ii) passing the treated oil through at least one distillation column to separate the treated oil into at least one component and passing the at least one component through an adsorption column; and wherein the reactor comprises a cooling function for controlling the temperature of the reactor, wherein the cooling function is at least one of an internal cooling function and an external cooling function.

Process for the conversion of oxygenates to C.sub.5+ hydrocarbons boiling in the gasoline boiling range, comprising the steps of continuously a) providing one or more feed streams of one or more oxygenate compounds; b) heating the one or more feed streams to an inlet temperature of one or more downstream conversion reactors; c) introducing the one or more heated feed stream into inlet of the one or more conversion reactors; d) converting in the one or more conversion reactors the one or more heated feed stream in presence of catalyst to a converted oxygenate product comprising C.sub.5+ hydrocarbons; e) withdrawing from the one or more conversion reactors the converted oxygenate product; f) determining at outlet of the one or more conversion reactors amount of the one or more unconverted oxygenate compounds in the withdrawn converted oxygenate product; g) separating the converted oxygenate product into a C.sub.4 hydrocarbon fraction, a fraction with the C.sub.5+ hydrocarbons boiling in the gasoline boiling range and a fraction comprising water and the one or more unconverted oxygenate compounds, wherein the inlet temperature of the one or more feed streams in step b is continuously adjusted to maintain a constant amount of the one or more unconverted oxygenate compounds as determined in step f.

The present invention relates to a process for the conversion of a feedstock comprising at least 50 wt % related to the total weight of the feedstock of triglycerides, fatty acid esters and/or fatty acids having at least 10 carbon atoms into hydrogen, olefins, dienes, aromatics, gasoline, diesel fuel, jet fuel, naphtha and liquefied petroleum gas comprising: a) introducing of said feedstock in a first reactor to produce linear paraffins in presence of a hydrodesulfurization catalyst and hydrogen, b) separating the effluent of said first reactor in at least three parts to produce at least a first stream comprising part of said linear paraffins and at least a second stream comprising part of said linear paraffins, and at least a third stream comprising part of said linear paraffins c) sending said first stream to a steam cracker to produce hydrogen, olefins, dienes, aromatics and gasoline, diesel fuel being further fractionated; d) introducing said second stream into a second reactor in presence of a hydrocracking or hydroisomerization catalyst to produce a mixture comprising diesel fuel, jet fuel, naphtha and liquefied petroleum gas being further fractionated e) blending said third stream with the diesel fuel obtained at said step d)
wherein said feedstock of said first reactor is diluted in order to limit the temperature increase within said first reactor; and wherein before entering the first reactor said dilution is performed with a weight ratio diluent:feedstock being 1:1, and wherein said diluent comprises at least part of said paraffins obtained at step b).

An integrated system for the conversion of biomass to renewable natural gas and then to methanol and other value-added products is provided. The integrated system includes a compressor that receives biomass gases from a biomass source and a series of purification stations that produce purified gas from the biomass gases. Characteristically, the purified gas has an enhanced amount of methane. A gas-to-liquids plant converts the purified gas to a product blend that includes methanol.

Process for the conversion of oxygenates to C.sub.5+ hydrocarbons boiling in the gasoline boiling range, comprising the steps of continuously a) providing one or more feed streams of one or more oxygenate compounds; b) heating the one or more feed streams to an inlet temperature of one or more downstream conversion reactors; c) introducing the one or more heated feed stream into inlet of the one or more conversion reactors; d) converting in the one or more conversion reactors the one or more heated feed stream in presence of catalyst to a converted oxygenate product comprising C.sub.5+ hydrocarbons; e) withdrawing from the one or more conversion reactors the converted oxygenate product; f) determining at outlet of the one or more conversion reactors amount of the one or more unconverted oxygenate compounds in the withdrawn converted oxygenate product; g) separating the converted oxygenate product into a C.sub.4 hydrocarbon fraction, a fraction with the C.sub.5+ hydrocarbons boiling in the gasoline boiling range and a fraction comprising water and the one or more unconverted oxygenate compounds, wherein the inlet temperature of the one or more feed streams in step b is continuously adjusted to maintain a constant amount of the one or more unconverted oxygenate compounds as determined in step f.