This disclosure relates to new processes to produce high paraffinic diesel from crude oil, such as tight oil from the Permian basin. This disclosure also relates to high paraffinic diesel compositions and high paraffinic diesel blends.

This disclosure relates to new processes to produce high paraffinic diesel from crude oil, such as tight oil from the Permian basin. This disclosure also relates to high paraffinic diesel compositions and high paraffinic diesel blends.

Processes herein may be used to thermally crack various hydrocarbon feeds, and may eliminate the refinery altogether while making the crude to chemicals process very flexible in terms of crude. In embodiments herein, crude is progressively separated into at least light and heavy fractions. Depending on the quality of the light and heavy fractions, these are routed to one of three upgrading operations, including a fixed bed hydroconversion unit, a fluidized catalytic conversion unit, or a residue hydrocracking unit that may utilize an ebullated bed reactor. Products from the upgrading operations may be used as feed to a steam cracker.

A process for augmenting energy in a dryer used in processing is disclosed. The process includes providing a source of syrup having concentrated solids. They syrup is then directed through a syrup line to a recirculation pump where it is recirculated to a heat exchanger having a source of heat delivered thereto. The syrup is heated to a temperature above a flash point of the syrup. The heated syrup is delivered to a flash tank and water vapor is flashed off and then directed through a vent and into a dryer. Cooled syrup remaining in the flash tank is delivered through a cooled liquid line to the syrup line to repeat the process. The delivery of water vapor to the dryer results in an additional source of energy being transferred to the dryer.

A process for augmenting energy in a dryer used in processing is disclosed. The process includes providing a source of syrup having concentrated solids. They syrup is then directed through a syrup line to a recirculation pump where it is recirculated to a heat exchanger having a source of heat delivered thereto. The syrup is heated to a temperature above a flash point of the syrup. The heated syrup is delivered to a flash tank and water vapor is flashed off and then directed through a vent and into a dryer. Cooled syrup remaining in the flash tank is delivered through a cooled liquid line to the syrup line to repeat the process. The delivery of water vapor to the dryer results in an additional source of energy being transferred to the dryer.

A direct-contact, spray-assisted, evaporation and condensation, DCSEC system includes a heating block configured to receive and heat up seawater; plural evaporation and condensation stages, wherein n is a natural number, each stage being configured to generate water vapors through flash evaporation; an evaporation only stage connected to a last stage of the plural evaporation and condensation stages, the evaporation only stage configured to receive a brine from the last stage n of the plural evaporation and condensation stages; an input/output block configured to receive the brine from the evaporation only stage and to discharge it outside the system, and also to receive cooling water; and a pressure-swing regeneration block fluidly connected to the evaporation only stage to receive the water vapors and to generate a hot vapor, which is provided to the heating block for heating the seawater.

The present invention relates to a process for treating an effluent obtained from an oligomerization step in a vaporization step. In particular, the oligomerization step is a step for dimerization of ethylene to 1-butene with a nickel-based catalytic system.

The present invention relates to a process for treating an effluent obtained from an oligomerization step in a vaporization step. In particular, the oligomerization step is a step for dimerization of ethylene to 1-butene with a nickel-based catalytic system.

Monoethylene glycol (MEG) may be reclaimed by a process that includes contacting a MEG-water-salt stream with a heat transfer fluid and then flash separating the MEG and water in the flash separator vessel where the pressure is higher than 0.3 barA (0.03 MPa), the temperature is in the range of above 120° C. to about 250° C., and the residence time of the MEG and water ranges from about 1 second to about 10 minutes, and then removing the MEG and water in an overhead of the flash separator vessel and removing the salt from the flash separator vessel. In some embodiments it is expected that the temperature of the process may range from above 165° C. to about 250° C. and/or that the pressure may be atmospheric.

Monoethylene glycol (MEG) may be reclaimed by a process that includes contacting a MEG-water-salt stream with a heat transfer fluid and then flash separating the MEG and water in the flash separator vessel where the pressure is higher than 0.3 barA (0.03 MPa), the temperature is in the range of above 120° C. to about 250° C., and the residence time of the MEG and water ranges from about 1 second to about 10 minutes, and then removing the MEG and water in an overhead of the flash separator vessel and removing the salt from the flash separator vessel. In some embodiments it is expected that the temperature of the process may range from above 165° C. to about 250° C. and/or that the pressure may be atmospheric.