A method for preparing diphenol compounds includes adding a hydroxyphenyl carboxylic acid, a tyrosine ethyl ester, hydroxybenzotriazole hydrate and a solvent and stirring to produce a first solution. EDCI HCl is added to the first solution to produce a first mixture. Ethyl acetate is added to the first mixture to produce a second mixture. The second mixture is added to sodium chloride to produce a third mixture having layer separation. An aqueous layer is removed from the third mixture. The third mixture is extracted with reagents after the aqueous layer has been removed from the third mixture to produce a fourth mixture. Magnesium sulfate is added to the fourth mixture to produce a fifth mixture. The fifth mixture is filtered to produce filtrate. The filtrate is concentrated. Crystallization of the concentrated filtrate is induced. Methylene chloride is added to the crystallized filtrate to produce a solid product.

Provided is nickel powder obtained by adding seed crystals to a nickel ammine complex solution and performing hydrogen reduction reaction under high temperatures and high pressures, wherein the nickel powder does not produce dust during handling, and a container can be efficiently filled with the nickel powder. The method for producing nickel powder includes: adding seed crystals and a surfactant having a nonionic or anionic functional group to a solution containing a nickel ammine complex to forma mixed slurry; and subjecting the mixed slurry to hydrogen reduction under high temperature and high pressure conditions in a pressure vessel to obtain nickel powder from the mixed slurry.

Provided is a fluid processing apparatus using a crystallization promoting medium (CPM) as a fluid processing medium. The apparatus comprises one or more column bed units in parallel connection, wherein the column bed units may be connected in parallel with a bypass flow path having a check valve, and except the first column bed unit, each of the column bed units is provided with a check valve upstream thereof. Also provided is a method for improving the efficiency of a CPM-based fluid processing apparatus having only one column bed unit. The method comprises: replacing the column bed unit of the CPM-based fluid processing apparatus having only one fluid processing column bed unit with: (i) a plurality of secondary column bed units in parallel connection, wherein the secondary column bed units may be connected in parallel with a bypass flow path having a check valve; and except the first secondary column bed unit, each of the secondary column bed units is provided with a check valve upstream thereof; or (ii) one column bed unit and a bypass flow path that is connected in parallel with the column bed unit and has a check valve. Also provided is a proportional check valve that opens proportionally as the pressure increases.

The present invention relates to a process for the solidification of hexyl 2-[4-(diethylamino)-2-hydroxybenzoyl]benzoate (INCI diethylamino hydroxybenzoyl hexyl benzoate, DHHB), wherein the process comprises the step of (a) applying a shear rate of less than 800 s.sup.?1 to liquid hexyl 2-[4-(diethylamino)-2-hydroxybenzoyl]benzoate and (b) adding seed crystals of hexyl 2-[4-(diethylamino)-2-hydroxybenzoyl]benzoate.

A method for producing a nickel-containing hydroxide is provided that includes a particle growth step of promoting growth of nickel-containing hydroxide particles by neutralization crystallization in an aqueous solution accommodated in an agitation tank. In the particle growth step, an averaged value of the maximum accelerations of the flows of streamlines for the aqueous solution is greater than 600 m/s.sup.2.

The present invention addresses the problem of providing a crystallization method having excellent separation performance between a crystal fraction and a liquid fraction after crystallization in a dry-mode separation method employing stirring crystallization and compression filtration, whereby it becomes possible to produce an SUS-rich oil/fat from an SUS-containing oil/fat. In the dry-mode oil/fat separation for producing an SUS-rich oil/fat having an SUS content of 60% by weight or more from an SUS-containing oil/fat having an SUS content of 30% by weight or more, a crystalline S3 component is added to the SUS-containing oil/fat in an amount of 5 to 200 ppm by weight relative to the amount of the SUS-containing oil/fat at a temperature that is higher by 0 to 2 C. than a cloud point of the SUS-containing oil/fat so as to be mixed, and performing stirring crystallization. When the SUS contains StOSt as the main component, the S3 component is preferably one derived from an extremely hydrogenated oil of an oil/fat that is in a liquid form at ambient temperature.

The present invention relates to the extraction of lithium from liquid resources, such as natural and synthetic brines, leachate solutions from clays and minerals, and recycled products.

Certain aspects of the present disclosure relate to a fluid treatment reactor. Separate input ports for influent and recycled effluent serve to eliminate the need for pH adjustment or carbonate stripping of the influent and recycled effluent flows. The fluid treatment reactor may include a media, a vessel including a top portion and a bottom portion, a solid discharge port, an effluent discharge port, an influent input in fluid communication with the media, and a recycled effluent port in fluid communication with the media.

It is an object of the present disclosure to provide a method for producing a reduced coenzyme Q10 Form II crystal or a crystalline solid thereof, which is capable of stably producing a reduced coenzyme Q10 Form II crystal or a crystalline solid thereof.

The present embodiment is a method for producing a reduced coenzyme Q10 Form II crystal or a crystalline solid thereof, the method using a crystallizer provided with a crystallization unit, a turbidity detection unit capable of detecting a turbidity in the crystallization unit, and a temperature adjustment unit capable of adjusting a temperature in the crystallization unit, and the method including: accommodating a mixed solution containing an alcohol and a reduced coenzyme Q10 in the crystallization unit; adding a reduced coenzyme Q10 Form II crystal as a seed crystal to the mixed solution; and precipitating a reduced coenzyme Q10 Form II crystal in the mixed solution after adding the seed crystal, wherein the precipitation includes controlling a temperature with the temperature adjustment unit based on a turbidity change rate obtained by the turbidity detection unit.

The invention relates to a continuous method for obtaining a crystalline monosaccharide, comprising: continuous crystallization of the monosaccharide in a main crystallizer (10), wherein crystallization by evaporation and/or crystallization by cooling is carried out continuously on a crystal suspension in the main crystallizer in order to allow crystals of the monosaccharide to grow in the crystal suspension; separation of crystals of the monosaccharide out of the crystal suspension to obtain crystalline monosaccharide; continuous formation of a mass of crystallization magma for the main crystallizer (10) in a cascade, wherein the cascade comprises at least one first stage (13) and a final stage (15) connected in series and each stage comprises at least one pre-crystallizer (13A, 15A), wherein, in the at least one pre-crystallizer (13A) of the first stage (13), a solution is seeded with monosaccharide by means of monosaccharide seed crystals in order to obtain a pre-crystallization magma, and a mass of crystallization magma for the downstream stage (14, 15) is formed from the pre-crystallization magma by means of crystallization by cooling and/or crystallization by evaporation, and wherein a solution containing monosaccharide and a mass of crystallization magma from the upstream stage is supplied to the at least one pre-crystallizer (15A, 15B, 15C) of the final stage (15) to obtain a pre-crystallization magma, and in the at least one pre-crystallizer (15A, 15B, 15C) of the final stage (15) a mass of crystallization magma for the main crystallizer (10) is formed from the pre-crystallisation magma by means of crystallization by cooling and/or crystallization by evaporation; the continuous supply of a solution containing the monosaccharide and a mass of crystallization magma from the at least one pre-crystallizer (15A, 15B, 15C) of the final stage (15) of the cascade to the main crystallizer (10) to provide the crystal suspension.