Liquor water-based

The iso-LSD salt can be converted back into the base by the addibon of methanolic KOH or potassium methoxide to the mother liquor. The resulting mixture should be added to a separatory funnel containing salt solution and ethylene dichloride. The LSD base is extracted into the ethylene dichloride layer (the lower layer). The lower layer is removed and fresh ethylene dichloride used to extract the last traces of LSD base from the salt water-base mixture. The ethylene dichloride extracts are combined, dried with MgSO, decolorized and filtered through diatomaceous earth as earlier. I he resulting ethylene dichloride solution may be combined with the chloroform solutions of iso-LSD which eluted from the chromatographic column. The combined solution may be evaporated to dryness under reduced pressure. 

Regeneration Options for Water-based Process Liquors... 

Transfer from Water-based to Ionic Liquid Based Liquors. In the case of water-based electrolytes, there are two economic incentives forthe above mentioned approaches the recovery of valuables and the avoidance of wastes and wastewaters. Despite the environmental attractiveness of such measures economic constraints may become an obstacle in industrial application. 

Product development in water-based paints must consider how paint residues are to be recycled in the user s painting facilities. In certain paint systems, such as auto body paint booths, overspray is caught in circulating aqueous liquors and reconcentrated by ultrafiltration (see Fig. 123). Concentrate solutions are added to the appropriate paint formulations. In a special stove-drying paint system, the material recycling rate is ca. 95%. The special membranes needed for the ultrafiltration step were developed by Hoechst subsidiaries Herberts and Hoechst Celanese Corporation, together with plant construction specialists. 

Chem. Descrip. 6-Acetoxy-2,4-dimethyl-m-dioxane CAS 828-00-2 EINECS/ELINCS 212-579-9 Uses Antimicrobial, presenrative, bacteriostat, tungistat, preservative for industrial water-based systems and emulsions incl. paints, coatings, textile finishes, adhesives, leather processing liquors, distillate fuels Features Patented broad-spectrum wide pH range usage Regulatory EPA reg. no. 824-7... 

Water-soluble emulsifiers for oils, solvents and waxes, pigment dispersants degreasers, emulsifiers and lubricants in fat liquoring, viscosity and emulsion stabilizers for PVA and water-based paints emulsifiers and dispersants for urethane foams and polyester resins coemulsifiers in fabric softener and dye carrier systems emulsifiers in synthetic fiber lubricants. 

The major application of electrochemical ozone cells is in the oxidation of water-based species (in order to provide sterilization) and the oxidation of industrial process liquors containing cyanides or organicSte.g. phenols, dyes and pesticides, In such applications it is environmentally more desirable than CI2 or OCl" treatment (Chapter 7) as the latter chemicals may leave a range of undesirable species. Ozone treatments may be advantageously coupled with ultraviolet treatments in order to remove certain persistent chemicals (such as certain pesticides or polychlorinated biphenyls). In the case of sterilization of potable water the cells are likely to remain small modular designs (Fig. 5,15(b)). While the O3 required is very dependent on inlet-water quality, a cell of 100 cm anode area may service up to KKK) m day of water at the 1 mg dm O3 dose level... 

This represents a specialty filler which contributes to paper brightness, ink receptivity and acts as a flame retardant. The effect on flame retardancy can be explained by the 35% of bound water based on material weight. The bound water is released at temperatures above 150 °C. The raw material source for the production of aluminum trihydrate (ATH) is bauxite. Bauxite is a blend of AI2O3, Fc203, Si02, H2O, Ti02 and other minerals. To produce ATH it is necessary to stabilize the alumina content and to separate out the other minerals. This is done by the so-called Bayer process. After final filtration, the clear liquor of sodium aluminate is seeded with specially prepared fine crystals of ATH. This seeding causes the sodium aluminate to decompose to ATH or Al(OH)3 which forms a precipitate. 

The free base tends to become oxidized in the air but may be preserved as the hydrochloride. This is prepared by transferring it as soon as possible to 1500 cc. of distilled water containing 100 cc. of concentrated hydrochloric acid. The sparingly soluble hydrochloride separates at once. It is recrystallized from the mixture with the use of a little decolorizing carbon, whereupon it separates as colorless needles. A further crop is obtained on concentrating the mother liquor under reduced pressure to about 200 cc. The yield is no g. (82.1 per cent of the theoretical amount). 

The reaction mixture is filtered with suction and the cake is washed thoroughly with two 200-ml. portions of glacial acetic acid (Note 4). The combined filtrate and washings are evaporated under reduced pressure on the steam bath until a thick oil, which generally partially crystallizes, remains. To purify the crude product, 100 ml. of water is added, and the flask is warmed on a steam bath until the solid melts. The mixture of water and oil is stirred rapidly in an ice bath, and diethyl acetamidomalonate crystallizes as a fine white product. After cooling in an ice bath for an additional hour, the product is collected by filtration, washed once with cold water, and dried in air at 50°. A second crop is obtained by concentrating the mother liquor under reduced pressure. The yield of diethyl acetamidomalonate, m.p. 95-97° (Note 5), is 52-53 g. (77-78%) based on malonic ester. 

The application of lignin as an adhesive is possible in principle. The first attempt needed very long press times due to the low reactivity (Pedersen process) [161]. This process was based on lignin polycondensation under strong acidic conditions, which led to considerable corrosion problems in the plant [161]. The particles had been sprayed with spent sulfite liquor (pH = 3-4) and pressed at 180°C. After this step, the boards were tempered in an autoclave under pressure at 170-200°C, whereby the sulfite liquor became insoluble after splitting off water and SO2. 

Thebaine, CjgHgiOgN. This base, which occurs in opium to the extent of 0-1 to 1 per cent., was first obtained by Pelletier and Thiboumery, who regarded it as isomeric with morphine, and named it paramorphine. It was examined by Kane, who first called it thebaine, and by Anderson, who described a method of isolation and provided the formula given above. It remains in the mother liquor after the removal of morphine and eodeine hydrochlorides in Gregory s process, and in Hesse s method of isolating it from this source is obtained as the acid tartrate. This is crystallised from hot water, and the alkaloid regenerated from it is reerystallised from dilute alcohol, from which it separates in leaflets, or from dry alcohol in prisms, m.p. 193°, — 218-6° (EtOH) or — 229-5°... 

The mixture of bases is best obtained by mixing solutions of sinomenine hydrochloride and potassium ferricyanide and adding solution of sodium carbonate. The precipitate is collected, washed with water and dissolved in dilute hydrochloric acid. The mixed hydrochlorides, which crystallise out, are separated by repeated crystallisation from water, the i/i-sinomenine hydrochloride remaining in the mother liquors. 

The process of isolation finally adopted by the former authors consists in precipitating as reineckates the water-soluble bases contained in a methyl alcoholic extract of the curare. The mixed reineckates are further purified, by solution in acetone and precipitation with water as often as may be necessary. The product so cleaned represents the bulk of the biological activity of the crude drug the mother liquors may contain curine (p. 374), which indicates a menisperm as one of the components of such curares. The mixed reineckates are then fractionated chromato-graphically over alumina and the components isolated as chlorides by the use of silver sulphate and barium chloride in succession. This process has been modified in detail by Schmid and Karrer, who have also found that with their curare, the more soluble reineckate fraction includes less potent quaternary alkaloids. 

After cooling, the reaction mixture is agitated (with a mixture of (water (40 cc) and a normal solution of methanesulfonic acid (70 cc), the xylene layer is removed and the acid liquors are (washed (with ether (200 cc). The aqueous phase is then made alkaline (with sodium hydroxide (d = 1.33 10 cc) and the liberated base Is extracted (with ether. The ethereal solution is dried over anhydrous potassium carbonate and concentrated at normal pressure. On distillation of the residue under reduced pressure 3-(3-methoxy-10-phenthi-azinyl)-2-methyl-1-dimethylaminopropane (11.3 g) is obtained, MP 103°C, BP 182° to 191°C/0.15 mm Hg. The hydrochloride prepared in isopropanol melts at about 90°C. 

The ether extracts are transferred to a 1-1. round-bottomed flask, the ether is removed by distillation, and the residue of crude mandelic acid is dried by warming it on a steam bath under the vacuum of a water pump. About 400 cc. of benzene is added, and the mixture is distilled until 100 cc. of distillate is collected. The acid in the residual mixture is brought completely into solution by the addition of 6-10 cc. of ethyl alcohol. The hot solution is then filtered through a warm Buchner funnel, and the filtrate is cooled overnight at 6°. The first crop of pure mandelic acid weighs 100-120 g. A second crop is obtained by evaporation of the mother liquor to about one-fourth its volume this weighs 20-40 g. The total yield is 136-144 g. (85-90 per cent of the theoretical amount based on the dichloroacetophenone, or 76-87 per cent based on the acetophenone). The white crystalline product melts at 115-117° (Note 6). 

Sulphur dioxide is recovered from a smelter gas containing 3.5 per cent by volume of SO2, by scrubbing it with water in a countercurrent absorption tower. The gas is fed into the bottom of the tower, and in the exit gas from the top the SO2 exerts a partial pressure of 1.14 kN/m2. The water fed to the top of the tower is free from SO2, and the exit liquor from the base contains 0.001145 kmol SC /kmol water. The process takes place at 293 K, at which the vapour pressure of water is 2.3 kN/m2. The water flow rate is 0.43 kmol/s. 

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