Abstract: Systems and methods are provided for catalytic hydroprocessing to form lubricant base oils. The methods can include performing high pressure hydrofinishing after fractionating the hydrotreated and/or hydrocracked and/or dewaxed effluent. Performing hydrofinishing after fractionation can allow the high hydrogen pressure for hydrofinishing to be used on one or more lubricant base oil fractions that are desirable for high pressure hydrofinishing. This can allow for improved aromatic saturation of a lubricant base oil product while reducing or minimizing the hydrogen consumption. The high pressure hydrofinishing can be performed at a hydrogen partial pressure of at least about 2500 psig (˜17.2 Mpa), or at least about 2600 psig (˜18.0 Mpa), or at least about 3000 psig (˜20.6 MPa). The high pressure hydrofinishing can allow for formation of a lubricant base oil product with a reduced or minimized aromatics content, a reduced or minimized 3-ring aromatics content, or a combination thereof.

Abstract: Methods are provided for forming lubricant base stocks from feeds such as vacuum resid or other 510° C.+ feeds. A feed can be deasphalted and then catalytically and/or solvent processed to form lubricant base stocks, including bright stocks that are resistant to haze formation.

Abstract: Systems and methods are provided for catalytic hydroprocessing to form lubricant base oils. The methods can include performing high pressure hydrofinishing after fractionating the hydrotreated and/or hydrocracked and/or dewaxed effluent. Performing hydrofinishing after fractionation can allow the high hydrogen pressure for hydrofinishing to be used on one or more lubricant base oil fractions that are desirable for high pressure hydrofinishing. This can allow for improved aromatic saturation of a lubricant base oil product while reducing or minimizing the hydrogen consumption. The high pressure hydrofinishing can be performed at a hydrogen partial pressure of at least about 2500 psig (˜17.2 Mpa), or at least about 2600 psig (˜18.0 Mpa), or at least about 3000 psig (˜20.6 MPa). The high pressure hydrofinishing can allow for formation of a lubricant base oil product with a reduced or minimized aromatics content, a reduced or minimized 3-ring aromatics content, or a combination thereof.

Abstract: Systems and methods are provided for catalytic hydroprocessing to form lubricant base oils. The methods can include performing high pressure hydrofinishing after fractionating the hydrotreated and/or hydrocracked and/or dewaxed effluent. Performing hydrofinishing after fractionation can allow the high hydrogen pressure for hydrofinishing to be used on one or more lubricant base oil fractions that are desirable for high pressure hydrofinishing. This can allow for improved aromatic saturation of a lubricant base oil product while reducing or minimizing the hydrogen consumption. The high pressure hydrofinishing can be performed at a hydrogen partial pressure of at least about 2500 psig (˜17.2 Mpa), or at least about 2600 psig (˜18.0 Mpa), or at least about 3000 psig (˜20.6 MPa). The high pressure hydrofinishing can allow for formation of a lubricant base oil product with a reduced or minimized aromatics content, a reduced or minimized 3-ring aromatics content, or a combination thereof.

Abstract: Systems and methods are provided for producing lubricant basestocks having a reduced or minimized aromatics content. A first processing stage can perform an initial amount of hydrotreating and/or hydrocracking. A first separation stage can then be used to remove fuels boiling range (and lower boiling range) compounds. The remaining lubricant boiling range fraction can then be exposed under hydrocracking conditions to a USY catalyst including a supported noble metal, such as Pt and/or Pd. The USY catalyst can have a desirable combination of catalyst properties, such as a unit cell size of 24.30 or less (or 24.24 or less), a silica to alumina ratio of at least 50 (or at least 80), and an alpha value of 20 or less (or 10 or less). In some aspects, the effluent from the second (hydrocracking) stage can be dewaxed without further separation. In such aspects, a portion of the dewaxed effluent can be used as a recycle quench stream to cool the hydrocracking effluent prior to entering the dewaxing reactor.

Abstract: Systems and methods are provided for producing lubricant basestocks having a reduced or minimized aromatics content. A first processing stage can perform an initial amount of hydrotreating and/or hydrocracking. A first separation stage can then be used to remove fuels boiling range (and lower boiling range) compounds. The remaining lubricant boiling range fraction can then be exposed under hydrocracking conditions to a USY catalyst including a supported noble metal, such as Pt and/or Pd. The USY catalyst can have a desirable combination of catalyst properties, such as a unit cell size of 24.30 or less (or 24.24 or less), a silica to alumina ratio of at least 50 (or at least 80), and an alpha value of 20 or less (or 10 or less). In some aspects, the effluent from the second (hydrocracking) stage can be dewaxed without further separation. In such aspects, a portion of the dewaxed effluent can be used as a recycle quench stream to cool the hydrocracking effluent prior to entering the dewaxing reactor.

Abstract: Systems and methods are provided for producing lubricant basestocks having a reduced or minimized aromatics content. A first processing stage can perform an initial amount of hydrotreating and/or hydrocracking. A first separation stage can then be used to remove fuels boiling range (and lower boiling range) compounds. The remaining lubricant boiling range fraction can then be exposed under hydrocracking conditions to a USY catalyst including a supported noble metal, such as Pt and/or Pd. The USY catalyst can have a desirable combination of catalyst properties, such as a unit cell size of 24.30 or less (or 24.24 or less), a silica to alumina ratio of at least 50 (or at least 80), and an alpha value of 20 or less (or 10 or less). In some aspects, the effluent from the second (hydrocracking) stage can be dewaxed without further separation. In such aspects, a portion of the dewaxed effluent can be used as a recycle quench stream to cool the hydrocracking effluent prior to entering the dewaxing reactor.

Abstract: Systems and methods are provided for catalytic hydroprocessing to form lubricant base oils. The methods can include performing high pressure hydrofinishing after fractionating the hydrotreated and/or hydrocracked and/or dewaxed effluent. Performing hydrofinishing after fractionation can allow the high hydrogen pressure for hydrofinishing to be used on one or more lubricant base oil fractions that are desirable for high pressure hydrofinishing. This can allow for improved aromatic saturation of a lubricant base oil product while reducing or minimizing the hydrogen consumption. The high pressure hydrofinishing can be performed at a hydrogen partial pressure of at least about 2500 psig (˜17.2 Mpa), or at least about 2600 psig (˜18.0 Mpa), or at least about 3000 psig (˜20.6 MPa). The high pressure hydrofinishing can allow for formation of a lubricant base oil product with a reduced or minimized aromatics content, a reduced or minimized 3-ring aromatics content, or a combination thereof.

Abstract: Feeds containing triglycerides are processed to produce an olefinic diesel fuel product. The olefinic diesel can optionally be oligomerized to form a lubricant base oil product. The olefinic diesel is generated by deoxygenating the triglyceride-containing feed using processing conditions that enhance preservation of olefins that are present in the triglycerides. The triglyceride-containing feed is processed in the presence of a catalyst containing a Group VI metal or a Group VIII metal and optionally a physical promoter metal.

Abstract: Feeds containing triglycerides are processed to produce an olefinic diesel fuel product. The olefinic diesel can optionally be oligomerized to form a lubricant base oil product. The olefinic diesel is generated by deoxygenating the triglyceride-containing feed using processing conditions that enhance preservation of olefins that are present in the triglycerides. The triglyceride-containing feed is processed in the presence of a catalyst containing a Group VI metal or a Group VIII metal and optionally a physical promoter metal.

Abstract: Methods are provided for forming lubricant base stocks from feeds such as vacuum resid or other 510° C.+ feeds. A feed can be deasphalted and then catalytically and/or solvent processed to form lubricant base stocks, including bright stocks that are resistant to haze formation.

Abstract: Methods are provided for forming lubricant base stocks from feeds such as vacuum resid or other 510° C.+ feeds. A feed can be deasphalted and then catalytically and/or solvent processed to form lubricant base stocks, including bright stocks. The catalytic processing can correspond to processing in at least two stages. The amount of conversion performed in each stage can be varied to produce bright stocks with various properties.

Abstract: Methods are provided for forming lubricant base stocks from feeds such as vacuum resid or other 510° C.+ feeds. A feed can be deasphalted and then catalytically and/or solvent processed to form lubricant base stocks, including bright stocks that are resistant to haze formation.

Abstract: Feeds containing triglycerides are processed to produce a diesel fuel product and propylene. The diesel product and propylene are generated by deoxygenating the triglyceride-containing feed using processing conditions that enhance preservation of olefins that are present in the triglycerides. The triglyceride-containing feed is processed in the presence of a catalyst containing a Group VI metal and a Group VIII non-noble metal and in the presence of CO.

Abstract: Feedstocks containing biocomponent materials are coprocessed with mineral feeds using a Group VI metal catalyst prior to hydrodesulfurization of the feedstocks. The Group VI metal catalyst is optionally a physically promoted Group VI metal catalyst.

Abstract: An integrated process for producing naphtha fuel, diesel fuel and/or lubricant base oils from feedstocks under sour conditions is provided. The ability to process feedstocks under higher sulfur and/or nitrogen conditions allows for reduced cost processing and increases the flexibility in selecting a suitable feedstock. The sour feed can be delivered to a catalytic dewaxing step without any separation of sulfur and nitrogen contaminants. The integrated process includes an initial dewaxing of a feed under sour conditions, optional hydrocracking of the dewaxed feed, and a separation to form a first diesel product and a bottoms fraction. The bottoms fraction is then exposed to additional hydrocracking and dewaxing to form a second diesel product and optionally a lubricant base oil product. Alternatively, a feedstock can be hydrotreated, fractionated, dewaxed, and then hydrocracked to form a diesel fuel and a dewaxed, hydrocracked bottoms fraction that is optionally suitable for use as a lubricant base oil.

Abstract: Provided are processes for making hydrocarbons from renewable feed sources. In an embodiment, there is provided a method for co-producing lube basestock and transportation fuel from a feedstock of biological origin, the method including: a) converting a feedstock of biological origin to a ketone or a dimer acid in the presence of a first catalyst; and b) hydrogenating the ketone or the dimer acid to produce a hydrocarbon in the presence of a second catalyst comprising a hydrogenation catalyst and a hydrothermally stable binder.

Abstract: Methods are provided herein for co-processing of biocomponent feeds as well processing of mineral feeds in a reaction system at hydrogen partial pressures of about 500 psig (3.4 MPag) or less. The methods include using stacked beds of both CoMo and NiMo catalysts. The stacked catalyst beds provided unexpectedly high catalyst activity as the input feed to a reaction system was switched between a mineral feed and a feed containing both mineral and biocomponent portions. Additionally, use of stacked catalyst beds can allow for maintenance of the activity for the catalyst system in a reaction system while still achieving a desired activity for both types of feeds.

Abstract: Provided are high viscosity high quality Group II lube base stocks with improved properties produced by an integrated hydrocracking and dewaxing process. In one form, the Group II lube base stock includes greater than or equal to 90 wt. % saturates, and less than 10 wt. % aromatics, and has an aromatic performance ratio between 1.0 and 5.0. Also provided are lubricant formulations including the high viscosity high quality Group II lube base stock.

Abstract: Feeds containing triglycerides are processed to produce an olefinic diesel fuel product and propylene. The olefinic diesel can optionally be oligomerized to form a lubricant base oil product. The olefinic diesel and propylene are generated by deoxygenating the triglyceride-containing feed using processing conditions that enhance preservation of olefins that are present in the triglycerides. The triglyceride-containing feed is processed in the presence of a catalyst containing a Group VI metal or a Group VIII metal and optionally a physical promoter metal.