The present disclosure generally relates to methods for deoiling a hydrocarbon feed and to products formed therefrom. In an embodiment is provided a method of deoiling a feed that includes introducing a waxy feed and a deoiling solvent to a dilution chilling zone; mixing the waxy feed and the deoiling solvent in the dilution chilling zone at a temperature of from about 10° F. to about 30° F. to form a slurry; introducing the slurry to a filter zone, the filter zone comprising one or more filter stages, wherein a temperature of the slurry is from about 40° F. to about 75° F.; separating the wax from the oil and the deoiling solvent to form a wax cake in a first filter stage; and washing the wax cake in the first filter stage with the deoiling solvent to obtain a composition comprising a wax. In another embodiment is provided a composition comprising a wax.

Disclosed is an external circulating slurry reactive crystallizer, including a riser, a degassing zone and a downcomer. A lower end of the riser is communicated with a gas inlet pipe, a liquid inlet pipe and a solid feeding pipe, while an upper end of the riser is communicated with a lower end of the degassing zone. An upper end of the downcomer is integrally fixed to a sidewall of the degassing zone. At least one hydrocyclone is arranged at a lower end of the downcomer. The hydrocyclone is provided with an overflow port at an upper end thereof and an underflow port and a valve at a lower end thereof. The overflow port is communicated with the riser. The crystallizer can simultaneously realize reaction, crystallization and separation for continuous production with low cost, regulating and controlling the particle size distribution and morphology of crystals.

A method of forming lithium carbonate from a lithium-bearing solution including:

evaporating the lithium-bearing solution to precipitate a first group of impurities;
removing the first group of impurities to form a first purified solution; and
performing a flash crystallisation step within a predetermined temperature range to crystallise a second group of impurities from the first purified solution;
removing the second group of impurities from the first solution to form a second purified solution, wherein at least 90 wt % of lithium is recovered from the first purified solution; and
reacting the second purified solution with a metal carbonate to form lithium carbonate of at least 90 wt % purity.

Disclosed is an external circulating slurry reactive crystallizer, including a riser, a degassing zone and a downcomer. A lower end of the riser is communicated with a gas inlet pipe, a liquid inlet pipe and a solid feeding pipe, while an upper end of the riser is communicated with a lower end of the degassing zone. An upper end of the downcomer is integrally fixed to a sidewall of the degassing zone. At least one hydrocyclone is arranged at a lower end of the downcomer. The hydrocyclone is provided with an overflow port at an upper end thereof and an underflow port and a valve at a lower end thereof. The overflow port is communicated with the riser. The crystallizer can simultaneously realize reaction, crystallization and separation for continuous production with low cost, regulating and controlling the particle size distribution and morphology of crystals.

A method for preparing a purified styrene composition includes providing a crude hydrocarbon composition containing styrene, subjecting the crude hydrocarbon composition to a distillation in a divided-wall column to produce an overhead hydrocarbon stream, a bottom hydrocarbon stream and a side hydrocarbon stream and subjecting the side hydrocarbon stream to at least one crystallization step to obtain a purified styrene composition.

The present invention relates to process for separating p-phenylenediamine from a mixture containing o-phenylenediamine, aminobiphenyls and diphenylamine by means of distillation coupled with crystallization, wherein the distillation system consists of two divided wall columns and the crystallization comprises at least one stage suspension-based melt crystallization. A liquid fraction enriched in p-phenylenediamine obtained as the side-draw of the first divided wall column is sent to the subsequent suspension-based melt crystallization to produce substantially pure p-phenylenediamine. The overhead product of the first divided wall column is fed to the second divided wall column to produce highly pure o-phenylenediamine withdrawn from the side-draw of the second divided wall column.

A saline feed stream flows into a liquid-liquid extraction system; and a volatile organic solvent flows through a main compressor. The compressed volatile organic solvent then flows through a solvent regenerator, which can be a heat exchanger or a combination of a vaporization device and a condenser, to cool the volatile organic solvent. The cooled volatile organic solvent in liquid phase then flows into the liquid-liquid extraction system, where the saline feed stream contacts the volatile organic solvent to selectively extract water from the saline feed stream into the volatile organic solvent, producing a concentrated brine and an organic-rich mixture of water and the volatile organic solvent. The organic-rich mixture flows from the liquid-liquid extraction system into the solvent regenerator, where the organic-rich mixture is heated to produce an organic-rich vapor and desalinated water; and the organic-rich vapor is recycled as volatile organic solvent back into the liquid-liquid extraction system.

A system of concentrating and separating waste solvent liquid includes a distillation tower, an extracting distillation unit, an extract agent recovery unit, and a vapor permeation film unit. The scheme of centrifugal distillation is specifically employed to collocate with vapor permeation to effectively concentrate the content of isopropanol in the waste solvent liquid to generate a final produce with ultra high concentration of isopropanol, and constantly recovers the extract agent. The system is able to be quickly settled to a steady state of operation with low power consumption because the extracting distillation unit has smaller size. Since no liquid is left in the extract agent recovery unit, operation risk is greatly reduced. In addition, the input feed is almost processed, overall efficiency is thus improved. The vapor permeation film unit further removes considerably little content of water from the organic solvent to increase the content of isopropanol up to 99.9% or more.

A system of concentrating and separating waste solvent liquid includes a distillation tower, an extracting distillation unit, an extract agent recovery unit, and a vapor permeation film unit. The scheme of centrifugal distillation is specifically employed to collocate with vapor permeation to effectively concentrate the content of isopropanol in the waste solvent liquid to generate a final produce with ultra high concentration of isopropanol, and constantly recovers the extract agent. The system is able to be quickly settled to a steady state of operation with low power consumption because the extracting distillation unit has smaller size. Since no liquid is left in the extract agent recovery unit, operation risk is greatly reduced. In addition, the input feed is almost processed, overall efficiency is thus improved. The vapor permeation film unit further removes considerably little content of water from the organic solvent to increase the content of isopropanol up to 99.9% or more.

Metal compositions and processes for fractional crystallization of a molten crude tin mixture containing lead and silver are described. A process includes separating the molten crude tin mixture into a first silver-enriched liquid drain product at the liquid end of a crystallization step and a first tin-enriched product at the crystal end of the crystallization step whereby the first silver-enriched liquid drain product comprises on a dry weight basis 6.0-30.0% wt of lead, 70.0-91% wt of tin, 95.0-99.0% wt of lead and tin together, 0.75-5.00% wt of silver, and ≥0.24% wt of antimony. The first silver enriched liquid drain product also includes at least one of: 0.05-0.5% wt of arsenic; 0.05-0.6% wt of copper, 0.0030-0.0500% wt of nickel, at least 0.0010-0.40% wt of bismuth, at most 1.0% wt of iron, or at least 0.0005% wt of gold, the balance being impurities.