Abstract: Methods comprising contacting a residue comprising paraffinic, olefinic, and aromatic hydrocarbons with a polar solvent under conditions effective to extract at least a portion of the aromatic hydrocarbons from the residue into the polar solvent, thereby generating: an extract phase comprising the portion of aromatic hydrocarbons and the polar solvent; and, a raffinate phase comprising a majority of the paraffinic and olefinic hydrocarbons.

Abstract: Provided herein are molecular sieve membranes for separating hydrocarbons of a lube feed stock into a permeate and a retentate based on molecular shape. The molecular sieve membranes comprise one or more layers of size-selective catalyst and a porous support comprising a plurality of diffusing gaps. Each layer of size-selective catalyst has a plurality of perpendicular membrane channels and a plurality of opening pores. The porous support is in fluidic communication with the plurality of opening pores to provide a fluidic pathway between the perpendicular membrane channels and the diffusing gaps. Also provided are processes for separating n-paraffins from other hydrocarbons in a lube feed stock using the present molecular sieve membranes.

Abstract: Methods comprising contacting a residue comprising paraffinic, olefinic, and aromatic hydrocarbons with a polar solvent under conditions effective to extract at least a portion of the aromatic hydrocarbons from the residue into the polar solvent, thereby generating: an extract phase comprising the portion of aromatic hydrocarbons and the polar solvent; and, a raffinate phase comprising a majority of the paraffinic and olefinic hydrocarbons.

Abstract: Systems and methods are provided for performing solvent dewaxing using a dewaxing solvent that is not fully miscible with the feed being dewaxed. It has been unexpectedly discovered that by operating with a ketone solvent mixture that is beyond the miscibility limit by a small amount, the rate of solvent dewaxing can be substantially increased. Additionally, the difference between the filtration temperature during solvent dewaxing and the pour point of the resulting dewaxed product is unexpectedly reduced. The dewaxing solvent beyond the miscibility limit can correspond to, for example, a solvent mixture where the weight percent of methyl ethyl ketone is beyond the miscibility limit by 0.1 vol % to 5.0 vol %.

Abstract: Systems and methods are provided for producing upgraded raffinate and extract products from lubricant boiling range feeds and/or other feeds having a boiling range of 400° F. (204° C.) to 1500° F. (816° C.) or more. The upgraded raffinate and/or extract products can have a reduced or minimized concentration of sulfur, nitrogen, metals, or a combination thereof. The reduced or minimized concentration of sulfur, nitrogen, and/or metals can be achieved by hydrotreating a suitable feed under hydrotreatment conditions corresponding to relatively low levels of feed conversion. Optionally, the feed can also dewaxed, such as by catalytic dewaxing or by solvent dewaxing. Because excessive aromatic saturation is not desired, the pressure for hydrotreatment (and optional dewaxing) can be 500 psig (˜3.4 MPa) to 1200 psig (˜8.2 MPa).

Abstract: Systems and methods are provided for modifying or selecting processing conditions for bright stock formation based on compositional characterization of the feedstock and/or bright stock products. In some aspects, the compositional information can include Z-class characterization of the components of a feed and/or bright stock product, optionally in combination with carbon number and/or molecular weight for the components. The compositional information can be used to select processing conditions to allow for removal and/or modification of selected components within a bright stock in order to improve throughput and/or provide desirable cold flow properties.

Abstract: Systems and methods are provided for performing solvent dewaxing using a dewaxing solvent that is not fully miscible with the feed being dewaxed. It has been unexpectedly discovered that by operating with a ketone solvent mixture that is beyond the miscibility limit by a small amount, the rate of solvent dewaxing can be substantially increased. Additionally, the difference between the filtration temperature during solvent dewaxing and the pour point of the resulting dewaxed product is unexpectedly reduced. The dewaxing solvent beyond the miscibility limit can correspond to, for example, a solvent mixture where the weight percent of methyl ethyl ketone is beyond the miscibility limit by 0.1 vol % to 5.0 vol %.

Abstract: Systems and methods are provided for modifying or selecting processing conditions for bright stock formation based on compositional characterization of the feedstock and/or bright stock products. In some aspects, the compositional information can include Z-class characterization of the components of a feed and/or bright stock product, optionally in combination with carbon number and/or molecular weight for the components. The compositional information can be used to select processing conditions to allow for removal and/or modification of selected components within a bright stock in order to improve throughput and/or provide desirable cold flow properties.

Abstract: Systems and methods are provided for producing upgraded raffinate and extract products from lubricant boiling range feeds and/or other feeds having a boiling range of 400° F. (204° C.) to 1500° F. (816° C.) or more. The upgraded raffinate and/or extract products can have a reduced or minimized concentration of sulfur, nitrogen, metals, or a combination thereof. The reduced or minimized concentration of sulfur, nitrogen, and/or metals can be achieved by hydrotreating a suitable feed under hydrotreatment conditions corresponding to relatively low levels of feed conversion. Optionally, the feed can also dewaxed, such as by catalytic dewaxing or by solvent dewaxing. Because excessive aromatic saturation is not desired, the pressure for hydrotreatment (and optional dewaxing) can be 500 psig (˜3.4 MPa) to 1200 psig (˜8.2 MPa).

Abstract: Systems and methods are provided for producing upgraded raffinate and extract products from lubricant boiling range feeds and/or other feeds having a boiling range of 400° F. (204° C.) to 1500° F. (816° C.) or more. The upgraded raffinate and/or extract products can have a reduced or minimized concentration of sulfur, nitrogen, metals, or a combination thereof. The reduced or minimized concentration of sulfur, nitrogen, and/or metals can be achieved by hydrotreating a suitable feed under hydrotreatment conditions corresponding to relatively low levels of feed conversion. Optionally, the feed can also dewaxed, such as by catalytic dewaxing or by solvent dewaxing. Because excessive aromatic saturation is not desired, the pressure for hydrotreatment (and optional dewaxing) can be 500 psig (˜3.4 MPa) to 1200 psig (˜8.2 MPa).

Abstract: Systems and methods are provided for producing upgraded raffinate and extract products from lubricant boiling range feeds and/or other feeds having a boiling range of 400° F. (204° C.) to 1500° F. (816° C.) or more. The upgraded raffinate and/or extract products can have a reduced or minimized concentration of sulfur, nitrogen, metals, or a combination thereof. The reduced or minimized concentration of sulfur, nitrogen, and/or metals can be achieved by hydrotreating a suitable feed under hydrotreatment conditions corresponding to relatively low levels of feed conversion. Optionally, the feed can also dewaxed, such as by catalytic dewaxing or by solvent dewaxing. Because excessive aromatic saturation is not desired, the pressure for hydrotreatment (and optional dewaxing) can be 500 psig (˜3.4 MPa) to 1200 psig (˜8.2 MPa).

Abstract: A process for producing high yields of higher quality (API Group II, Group III?) lubricating oil basestock fractions which allows the production of two or more types of high quality lubes in continuous mode (no blocked operation mode) without transition times and feed or intermediate product tankage segregation. Two consecutive hydroprocessing steps are used: the first step processes a wide cut feed at a severity needed to match heavy oil lube properties. The second step hydroprocesses a light oil after fractionation of the liquid product from the first step at a severity higher than for the heavy oil fraction. The two hydroprocessing steps will normally be carried out in separate reactors but they may be combined in a single reactor which allows for the two fractions to be processed with different degrees of severity.

Abstract: A process for producing high yields of higher quality (API Group II, Group III?) lubricating oil basestock fractions which allows the production of two or more types of high quality lubes in continuous mode (no blocked operation mode) without transition times and feed or intermediate product tankage segregation. Two consecutive hydroprocessing steps are used: the first step processes a wide cut feed at a severity needed to match heavy oil lube properties. The second step hydroprocesses a light oil after fractionation of the liquid product from the first step at a severity higher than for the heavy oil fraction. The two hydroprocessing steps will normally be carried out in separate reactors but they may be combined in a single reactor which allows for the two fractions to be processed with different degrees of severity.

Abstract: Methods are provided for producing lubricant base oils using a combination of catalytic and solvent processing. By using a combination of catalytic processing for feed conversion and dewaxing while using solvent processing for removal of aromatics, Group II and Group III lubricant base oils can be produced using low pressure catalytic processes.

Abstract: The present invention is a process for removing waxy haze from and improving the filterability of base stocks including heavy mineral oil base stocks, gas-to-liquids (GTL) and hydrodewaxed or hydroisomerized waxy feed basestocks by filtering the waxy haze causing particles out of the base stock employing a filter characterized by a high surface area of pores accessible to the haze wax particles which have particles dimensions of no more than about 5 microns.

Abstract: An apparatus and method for determining at least one of the temperatures at which a petroleum product will manifest delayed haze and the temperature at which haze will not exist in the product is provided. The apparatus comprises a container for holding a sample of the product, a light source, light detector, heaters and coolers combined with microprocessor means for storing and analyzing at least one of light transmitted or scattered by the sample. Measurements are useful in determining the haze properties of the product and also for controlling a dehazing process to meet target haze properties.

Abstract: The present invention is a process for removing waxy haze from and improving the filterability of base stocks including heavy mineral oil base stocks, gas-to-liquids (GTL) and hydrodewaxed or hydroisomerized waxy feed basestocks by filtering the waxy haze causing particles out of the base stock employing a filter characterized by a high surface area of pores accessible to the haze wax particles which have particles dimensions of no more than about 5 microns.

Abstract: An apparatus and method for determining at least one of the temperatures at which a petroleum product will manifest delayed haze and the temperature at which haze will not exist in the product is provided. The apparatus comprises a container for holding a sample of the product, a light source, light detector, heaters and coolers combined with microprocessor means for storing and analyzing at least one of light transmitted or scattered by the sample. Measurements are useful in determining the haze properties of the product and also for controlling a dehazing process to meet target haze properties.