Alkali continuous process

The recovery of fatty acids from soapstocks by a continuous process has been described soapstocks obtained from degumming and alkali refining operations are subjected to a saponification step followed by controlled acidification for cost efficiency and pollution control.Ila,b... 

Meade (26), who made use of an alkali metal alkoxide as a catalyst at 100°C at atmospheric and shghtly above atmospheric pressure. Further refinement was made by Tesoro (27), who conducted the reaction at 55-75°C and a vacuum of 4—8 kPa. Schurman (28) patented a continuous process for making alkanolamide, which makes use of a thin film reactor. It is claimed the short contact time in the reactor produces a high-purity alkanolamide (29). 

Many specially designed arc apparatus have been patented for the plasma treatment of petroleum fractions146- 151 Some of these permit cracking gas-liquid mixtures or gas-solid mixtures in continuous process with recycling of undecomposed petroleum. In one such device147 crude oil is mixed with an energy transfer medium (rare gas, alkali metal vapor) and the mixture formed into particles which are fed through the hollow cathode of an electrical arc sustained in the transfer medium. 

Hughes and coworkers have pnqxised a continuous process (Fig. 8-20) and have suggested its use for the production of aniline as well as methyl-anQine. The salient features pertain to the continuous partial elimination of the sodium chloride, stemming from the treatment of part of the aqueous portion of tiie reaction mass with alkali, for the recovery of methylamine without precipitation and filtration of the copper catalyst ... 

Out of the above mentioned methods, alkali treatment process (mercerization) has been adopted for the surface modification of Sisal Fiber (SF). The treatment of the fiber was carried out by immersing the fibers in IN sodium hydroxide (NaOH) solution for 1 hour at room temperature. Then, these fibers were washed with distilled water containing few drops of acetic add, followed by thorough washing imder continuous... 

Proteoivsis, protein degradation hydrolysis of proteins by the action of proteolytic enzymes, or nonenzymatically by acids (e.g. 6 M HCI at 110°C for 24 h or longer) or alkalis. Ultimate products of P. are amino aci Dietary proteins are hydrolysed to L-amino acids by P. in the intestine. After absorption, these amino acids are used in the synthesis of new proteins specific to the organism these, in turn, are eventually hydrolysed to amino acids by P. as part of the continual process of synthesis and degradation of cellular constituents (see Tiimover). A distinction is... 

The preparation of a synthetic latex is shown to be a very complex process that is affected by the monomers selected, surfactants, initiators and the polymerisation process. The semi-continuous process is the one most frequently used as it provides control of the polymerisation heat removal, as well as control of the composition of the copolymers comprising several types of monomer units. Some aspects of copolymerisation in emulsion and particle growth in the case of the semi-continuous process are discussed. The copolymers usually comprise 4 to 5 comonomers, some of them with functional groups. The functional groups serve as loci for crosslinking, improve colloid stability, increase polarity, improve adhesion and cause alkali-solubility and/or alkali swellability. High value polymer latices with special particle morphology, composition and other... 

The preceding epoxidation reaction can be performed in a batch, semibatch, or continuous process. Similar to that of the glyceryl ether process, a batch process is preferred for several reasons. One reason is that if the epoxidation does not achieve the desired conversion, it is a simple matter to add additional alkali metal hydroxide solution and continue the reaction. Sodium or potassium hydroxide is the preferred epoxidation reagent due to economic considerations. 

Af-chloroisocyanuric acid derivatives are produced in a continuous process involving the reaction of chlorine with cyanuric acid and a solution of alkali at 0-15°C. The reaction conditions should be carefully controlled to avoid the formation of the explosive NCI3 [8,9]. 

In the continuous process, which is more common today, the fat or oil is hydrolyzed by water at high temperatures and pressures in the presence of a catalyst, usually a zinc soap. The fat or oil and the water are introduced continuously into opposite ends of a larger reactor, and the fatty acids and glycerol are removed as formed, by distillation. The acids are then carefully neutralized with an appropriate amount of alkali to make soap. 

It was noted in the previous chapter (Section 1.4.2.1.) that the polymerization of isobutene could be accomplished only with cationic initiators. Aluminium chloride and boron trifluoride are the preferred initiators for commercial processes the separate addition of a co-catalyst is not generally necessary and adventitious substances possibly fulfil this role. At ordinary temperatures polymerization is extremely rapid and leads to low molecular weight polymers which are viscous oils or sticky solids. However, at low temperature (—80 to — 100°C) high molecular weight material is produced. Even at these low temperatures the reaction is complete in a few seconds and it is necessary to have particularly efficient means of dissipating the heat evolved. Conventional batch processes are unsuitable and continuous processes are used in which only small quantities of reactants are involved at any one moment. In one process (Badische Anilin- Soda-Fabrik A. G.), solutions of isobutene and boron trifluoride in liquid ethylene are mixed on a moving belt so that the polymerizing system is in the form of a thin film and heat is removed by the vaporization of the solvent. The polymer is then mixed with an alkali or ethanol to deactivate the initiator and treated with steam to remove water-soluble contaminants. Another process for polyisobutene (Standard Oil Co. (N.J.) (U.S.A.)) follows closely the procedure outlined in Section 2.10.2. for the manufacture of butyl rubber. 

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