The process removes hydrogen sulfide from hydrotreated gas by TSA. Hydrogen sulfide adsorbs on the adsorbent while allowing hydrogen in the hydrotreated gas to pass the adsorbent to provide a desulfided hydrogen gas stream and a sulfided adsorbent. A regenerant gas stream can be contacted with the sulfided adsorbent at a swing temperature to desorb hydrogen sulfide from the adsorbent into the regenerant gas stream. The regenerant gas stream can then be recycled to a hydrotreating reactor for processing biorenewable feed to provide hydrogen sulfide to the reactor. The desulfided gas stream can be purified to remove impurities such as carbon oxides and recycled to the hydrotreating reactor and/or used as the regenerant gas stream.

The process removes hydrogen sulfide from hydrotreated gas by TSA. Hydrogen sulfide adsorbs on the adsorbent while allowing hydrogen in the hydrotreated gas to pass the adsorbent to provide a desulfided hydrogen gas stream and a sulfided adsorbent. A regenerant gas stream can be contacted with the sulfided adsorbent at a swing temperature to desorb hydrogen sulfide from the adsorbent into the regenerant gas stream. The regenerant gas stream can then be recycled to a hydrotreating reactor for processing biorenewable feed to provide hydrogen sulfide to the reactor. The desulfided gas stream can be purified to remove impurities such as carbon oxides and recycled to the hydrotreating reactor and/or used as the regenerant gas stream.

Systems and methods are provided for catalytically dewaxing a diesel boiling range feed. In some aspects, catalytic dewaxing can be performed at low hydrogen treat gas rates and/or low hydrogen purity conditions. In other aspects, the systems and methods can allow for distillate dewaxing while reducing or minimizing the amount of equipment required.

The present invention relates to new crystalline zeolite SSZ-52x prepared using a quaternary ammonium cation templating agent, for example, having the structure:

##STR00001##

wherein X.sup.− is an anion which is not detrimental to the formation of the SSZ-52x. SSZ-52x is useful as a catalyst and shows improved durability, particularly with regard to NO.sub.x conversion.

The present invention provides a process to prepare middle distillates and base oils from a Fischer-Tropsch product, by (a) subjecting the Fischer-Tropsch product to a hydroprocessing step in the presence of a catalyst comprising a molecular sieve with a pore size between 5 and 7 angstrom and a SiO.sub.2/AlO.sub.3 ratio of at least 25, preferably from 50 to 180 and a group VIII metal to obtain a mixture comprising one or more middle distillate fractions and a first residual fraction and a naphtha fraction; (b) separating the mixture as obtained in step (a) by means of atmospheric distillation into one or more middle distillate fractions, a first residual fraction and a naphtha fraction; (c) separating the first residual fraction by means of vacuum distillation into at least a distillate base oil fraction and a second residual fraction.

A production plant and a method for production of a synthetized gasoline product from a synthetic hydrocarbon mixture produced from a mixture of reactive oxygenates, the method including a. separating the synthetic hydrocarbon mixture in at least a light hydrocarbon fraction, and a higher boiling hydrocarbon fraction, wherein the higher boiling fraction comprises at least 70% of the molecules including 10 or more carbon atoms and less than 20% of the molecules comprising exactly 9 carbon atoms, b. directing at least an amount of said higher boiling hydrocarbon fraction as a hydrocracking feedstock to contact a material catalytically active in hydrocracking under effective hydrocracking conditions providing a hydrocracked hydrocarbon stream, wherein at least an amount of said hydrocracked hydrocarbon stream is combined with at least an amount of said light hydrocarbon fraction, to provide said synthetized gasoline product having a T.sub.90 being below T.sub.90 of said synthetic hydrocarbon mixture.

Process for isomerization of paraffinic feedstocks operating at a temperature of between 200° C. and 500° C., at a total pressure of between 0.45 MPa and 7 MPa, at a partial pressure of hydrogen of between 0.3 and 5.5 MPa, at an hourly space velocity of between 0.1 and 10 kg of feedstock introduced per kg of catalyst and per hour, using a catalyst having at least one group VIII metal, at least one matrix and at least one IZM-2 zeolite, the total weight content of alkali metal and/or alkaline-earth metal elements is less than 200 ppm by weight relative to the total mass of said catalyst.

Process for isomerization of paraffinic feedstocks operating at a temperature of between 200° C. and 500° C., at a total pressure of between 0.45 MPa and 7 MPa, at a partial pressure of hydrogen of between 0.3 and 5.5 MPa, at an hourly space velocity of between 0.1 and 10 kg of feedstock introduced per kg of catalyst and per hour, using a catalyst having at least one group VIII metal, at least one matrix and at least one IZM-2 zeolite, the total weight content of alkali metal and/or alkaline-earth metal elements is less than 200 ppm by weight relative to the total mass of said catalyst.

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.