Abstract: This light illumination unit comprises: a heat sink that has a plate-shaped heat sink body and fins protruding from a first main surface of the heat sink body; an electronic substrate that is laminated on a second main surface of the heat sink body on the reverse side thereof from the first main surface; and a light illumination element that is mounted on a first surface of the electronic substrate on the side thereof where the heat sink is provided. As a result of said configuration, it is possible to save space as well as power.

Abstract: The present invention is directed at obtaining a high yield of a target substance and simultaneously securing high productivity. A reaction apparatus 10 has: a main flow channel 12 having an inner diameter of 3 mm, in which a raw material M1 flows; an introduction flow channel 14 in which a raw material M2 that causes a chemical reaction with the raw material M1 flows; and five branch introduction flow channels 16a to 16e which are branched from the introduction flow channel 14 and introduce the raw material M2 to the main flow channel 12, at predetermined introduction points 12o to 12s in the main flow channel 12. Here, in the main flow channel 12, the flow channel lengths of the flow channels 12b to 12d between adjacent introduction points 12p to 12s are not longer than those of the flow channels 12a to 12c between the next previous adjacent introduction points 12o to 12r in a flow direction of the raw material M1.

Abstract: Catalyst particles are contacted with a liquid and a gas in a vertically extending cylindrical vessel. The particles and liquid are placed in the vessel into which the gas and liquid are continuously fed from the bottom thereof so that an upwardly flowing mixture comprising the particles, liquid and gas is formed. The mixture is introduced into a gas separating zone disposed adjacent to an upper portion of the vessel to separate the mixture by gravity into a gas phase, a supernatant liquid phase and a phase rich in the catalyst particles. The gas and supernatant phases are continuously withdrawn from the separating zone while the catalyst particles-rich phase is continuously recycled to the bottom of the vessel by gravity.

Abstract: A process for the production of a carbonyl compound such as acetic acid by reacting a carbonylatable compound such as methanol with a carbon monoxide in the presence of a carbonylation catalyst containing a noble metal complex supported on a porous, cross-linked vinylpyridine resin at a temperature of 140-250.degree. C., a carbon monoxide partial pressure of 7-30 kg/cm.sup.2 and a hydrogen partial pressure of 0.1-5 kg/cm.sup.2 to obtain a liquid product containing the carbonyl compound and an unreacted CO-containing gas product. The water content and the carbonylation degree of the liquid product within the reactor are maintained at 0.5-10% by weight and 0.5-0.9, respectively, The carbonyl compound is separated from the liquid product in a flasher and/or a distillation tower formed of titanium or a titanium-palladium alloy. The liquid product is introduced into a pressure reducing valve and then mixed with the CO-containing gas product before being fed to the flasher and/or distillation tower.

Abstract: Catalyst particles are contacted with a liquid and a gas in a vertically extending cylindrical vessel. The particles and liquid are placed in the vessel into which the gas and liquid are continuously fed from the bottom thereof so that an upwardly flowing mixture comprising the particles, liquid and gas is formed. The mixture is introduced into a gas separating zone disposed adjacent to an upper portion of the vessel to separate the mixture by gravity into a gas phase, a supernatant liquid phase and a phase rich in the catalyst particles. The gas and supernatant phases are continuously withdrawn from the separating zone while the catalyst particles-rich phase is continuously recycled to the bottom of the vessel by gravity.

Abstract: A process for the production of a carbonic diester, wherein an alcohol is reacted in a reaction zone with carbon monoxide and oxygen in the presence of (a) metallic copper or a copper compound, (b) a heterocyclic compound containing one or more nitrogen atoms in the cyclic skeleton and (c) a glycol ether represented by the following formula (I):R.sup.1 O--(CHR.sup.2 --CH.sub.2 O).sub.n --R.sup.3 (I)wherein R.sup.1 stands for an alkyl group having from 1 to 6 carbon atoms, R.sup.2 stands for a hydrogen atom or an alkyl group having 1 or 2 carbon atoms, R.sup.3 stands for a hydrogen atom or an alkyl group having from 1 to 6 carbon atoms and n is an integer of from 1 to 12.

Abstract: A high quality bisphenol A with a high purity and an excellent hue is produced from a crystalline adduct of bisphenol A and phenol by washing the adduct with specifically purified phenol, followed by decomposition of the washed adduct to separate bisphenol A. The purification is performed by a method including contacting raw material phenol with a strong-acid ion exchange resin to obtain treated phenol, and distilling the treated phenol.

Abstract: High quality bisphenol A is produced from a neutral crystalline adduct of bisphenol A and phenol by fusing the adduct in an atmosphere having a maximum oxygen content of 0.005 % by volume, followed by evaporation of liberated phenol. The crystalline adduct may be mixed with an aliphatic carboxylic acid before the fusion to reduce the coloring of the product. When an acidic crystalline adduct is used, the use of a strong alkali salt of an aliphatic carboxylic acid is suitably used. Interior surfaces of the apparatuses for carrying out the fusion and evaporation are desirably washed with an organic solvent to remove oxygen therefrom. The evaporation of phenol is suitably performed by two stage steam stripping wherein a used stripping gas obtained in the second stage is employed as a stripping gas in the first stage while steam is used as the stripping gas in the second stage.

Abstract: High quality bisphenol A is produced from a neutral crystalline adduct of bisphenol A and phenol by fusing the adduct in an atmosphere having a maximum oxygen content of 0.005% by volume, followed by evaporation of liberated phenol. The crystalline adduct may be mixed with an aliphatic carboxylic acid before the fusion to reduce the coloring of the product. When an acidic crystalline adduct is used, the use of a strong alkali salt of an aliphatic carboxylic acid is suitably used. Interior surfaces of the apparatuses for carrying out the fusion and evaporation are desirably washed with an organic solvent to remove oxygen therefrom. The evaporation of phenol is suitably performed by two stage steam stripping wherein a used stripping gas obtained in the second stage is employed as a stripping gas in the first stage while steam is used as the stripping gas in the second stage.

Abstract: High quality bisphenol A is produced from a neutral crystalline adduct of bisphenol A and phenol by fusing the adduct in an atmosphere having a maximum oxygen content of 0.005% by volume, followed by evaporation of liberated phenol. The crystalline adduct may be mixed with an aliphatic carboxylic acid before the fusion to reduce the coloring of the product. When an acidic crystalline adduct is used, the use of a strong alkali salt of an aliphatic carboxylic acid is suitably used. Interior surfaces of the apparatuses for carrying out the fusion and evaporation are desirably washed with an organic solvent to remove oxygen therefrom. The evaporation of phenol is suitably performed by two stage steam stripping wherein a used stripping gas obtained in the second stage is employed as a stripping gas in the first stage while steam is used as the stripping gas in the second stage.

Abstract: A methanol carbonylation catalyst includes a rhodium complex supported on a porous, cross-linked vinylpyridine resin, wherein the vinylpyridine resin has a cross-linking degree of 30-60%, a pore volume of 0.1-0.4 ml/g and an average pore diameter of 20-100 nm. The catalyst may be prepared by contacting the pyridine ring-containing resin with an aqueous solution containing rhodium ion and then contacting the resulting rhodium ion-carrying resin with carbon monoxide and an alkyl iodide in an organic solvent to convert the rhodium ion to a rhodium complex bound to the resin. Acetic acid is produced by reacting carbon monoxide with methanol at a temperature of 140.degree.-250.degree. C. and a partial pressure of carbon monoxide of 7-30 kg/cm.sup.2 in the presence of an alkyl iodide and the above catalyst.

Abstract: A liquid feed containing methanol, carbon monoxide, an alkyl iodide and a solvent is contacted with a supported rhodium catalyst to produce acetic acid at a temperature of 140.degree.-250.degree. C. and a pressure of 15-60 kg/cm.sup.2 G with a partial pressure of carbon monoxide of 7-30 kg/cm.sup.2 while maintaining (a) the water concentration of the product solution in the range of 0.5-10% by weight and (b) the carbonylation degree C.sub.r, defined in the specification, of the solution within the reactor at 0.15 or more. The solvent may be a carboxylic acid or a carboxylic acid ester.

Abstract: High quality bisphenol A is produced from a neutral crystalline adduct of bisphenol A and phenol by fusing the adduct in an atmosphere having a maximum oxygen content of 0.005% by volume, followed by evaporation of liberated phenol. The crystalline adduct may be mixed with an aliphatic carboxylic acid before the fusion to reduce the coloring of the product. When an acidic crystalline adduct is used, the use of a strong alkali salt of an aliphatic carboxylic acid is suitably used. Interior surfaces of the apparatuses for carrying out the fusion and evaporation are desirably washed with an organic solvent to remove oxygen therefrom. The evaporation of phenol is suitably performed by two stage steam stripping wherein a used stripping gas obtained in the second stage is employed as a stripping gas in the first stage while steam is used as the stripping gas in the second stage.

Abstract: A method and apparatus for the combustion treatment of a toxic gas which forms microparticles by combustion are disclosed wherein the toxic gas is subjected to a combustion treatment in a specific combustion furnace where the combustion gas formed is brought into contact with an aqueous film flowing downwards on the inner wall of the furnace from the upper end portion thereof to the lower end portion thereof or with a cooled surface, and then optionally with aqueous droplets dispersed in the interior space of the furnace. The water captures the microparticles formed by combustion of the toxic gas and is discharged out of the furnace as a mixed flow with the combustion gas thus treated, and optionally the mixed flow is successively treated in a gas-liquid separator.

Abstract: A catalyst for dehalogenation of a halide comprising a corrosion-resistant ceramic or graphite having a surface area of 5.0 m.sup.2 /g or less and, supported thereon, at least one of a platinum group metal and a silicide thereof, and a method of dehalogenation of a halide using this catalyst.

Abstract: A method for the hydrogenation of coal tar pitch which comprises subjecting said coal tar pitch containing toluene insolubles to slight hydrogenation in the presence of a hydrogenation catalyst having carried on a refractory inorganic oxide carrier at least one member selected from the class consisting of elemental metals, belonging to Groups VI B and VIII in the Periodic Table and oxides and sulfides thereof, under the conditions of 280.degree. to 400.degree. C. of reaction temperature, 20 to 200 kg/cm.sup.2. G of hydrogen pressure, 0.1 to 10 hr.sup.-1 of LHSV, and 500 to 2,000 Nl/liter of hydrogen to liquid ratio, and a catalyst therefor. The "slight" hydrogenation is hydrogenation to a degree such that the difference of hydrogen to carbon atomic ratio between the untreated coal tar pitch and the hydrogenated coal tar pitch falls in the range of 0.03 to 0.5.