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    • 42. 发明授权
      US5395994A Method for recovering methanol solvent 失效
    • Method for recovering methanol solvent
    • 甲醇溶剂回收方法
    • US5395994A
    • 1995-03-07
    • US245949
    • 1994-05-19
    • Robert E. Williams , William J. Cranston, III
    • Robert E. Williams , William J. Cranston, III
    • C07C29/80 , C07C37/62 , C07C39/367 , C07C27/26 , C07C29/74 , C07C37/68
    • C07C29/80 , C07C37/62
    • This invention provides an environmentally acceptable method for recovery of phenolic and brominated phenolic compounds, alcohol solvent, and bromide values from the a reaction medium liquid mixture formed in the production of a tetrabromobisphenol-A predominant product. The process comprises (a) separating the tetrabromobisphenol-A predominant product and alkyl bromide from the reaction medium thereby forming a liquid mixture containing alcohol, phenolic and brominated phenolic compounds, HBr, and water; (b) treating the liquid mixture with a sufficient amount of alkaline or alkaline earth metal hydroxide so as to form a treated aqueous mixture having a pH in the range of from about 9.5 to about 14.0, and containing MBr.sub.n, water, alcohol, and soluble salts of the phenolic and brominated phenolic compounds, wherein M is an alkaline or alkaline earth metal ion, and n is the valence of M; (c) distilling alcohol from the treated aqueous mixture of (b); (d) acidifying the treated aqueous mixture from (c) subsequent to distillation with a sufficient amount of acid to precipitate the phenolic and brominated phenolic compounds therefrom; and (e) separating the precipitated phenolic and brominated phenolic compounds from the acidified aqueous mixture of (d).
    • 本发明提供了一种用于从生产四溴双酚A主要产物中形成的反应介质液体混合物回收酚类和溴化酚类化合物，醇溶剂和溴化物值的环境可接受的方法。 该方法包括（a）从反应介质中分离出四溴双酚A主要产物和烷基溴，从而形成含有醇，酚和溴化酚化合物HBr和水的液体混合物; （b）用足量的碱金属或碱土金属氢氧化物处理液体混合物，以形成pH在约9.5至约14.0范围内的处理过的水性混合物，并含有MBrn，水，醇和可溶的 酚类和溴化酚类化合物的盐，其中M是碱金属或碱土金属离子，n是M的化合价; （c）从经处理的（b）水混合物中蒸馏出醇; （d）用（c）在蒸馏后用足够量的酸酸化经处理的含水混合物以从其中沉淀酚类和溴化酚类化合物; 和（e）从（d）的酸化含水混合物中分离出沉淀的酚类和溴化酚类化合物。
    • 基本信息 添加关注 加入工作空间 PDF全文 PDF下载 全文下载 相似专利 双屏查看 权利要求书 说明书全文 Global Dossier Espacenet 法律信息 同族专利 专利引用
    • 44. 发明授权
      US4556728A Separation of methanol from mixtures containing it 失效
    • Separation of methanol from mixtures containing it
    • 从含有它的混合物中分离甲醇
    • US4556728A
    • 1985-12-03
    • US675501
    • 1984-11-28
    • David Farrar , Gerald P. Benn
    • David Farrar , Gerald P. Benn
    • B01D11/04 , C07C27/00 , C07C29/74 , C07C29/88 , C07C31/04 , C07C67/00 , C07C67/03 , C07C29/92
    • C07C29/88
    • A substantially anhydrous mixture of methanol with an organic compound with which it forms an azeotrope can be separated by dissolving into the mixture lithium chloride or other suitable salt that forms a complex with methanol so as to form a homogeneous mixture, adding an organic solvent that is miscible with the organic compound but immiscible with the complex and thereby forming a heterogeneous mixture, and separating the phases. The methanol can be recovered from one phase and the organic compound from the other. The organic compound may typically be methyl acrylate or methacrylate, the blend being, for instance, obtainable during the transesterification of methyl (meth)acrylate with an alcohol to form a higher boiling ester such as dimethylaminoethyl (meth)acrylate or 2-ethylhexyl acrylate.
    • 甲醇与其形成共沸物的有机化合物的基本上无水的混合物可以通过将与甲醇形成络合物的氯化锂或其它合适的盐溶解在混合物中来分离，从而形成均匀的混合物，加入有机溶剂， 与有机化合物混溶，但与配合物不混溶，从而形成非均相混合物，并分离相。 甲醇可以从一相回收，有机化合物可从另一相回收。 有机化合物通常可以是丙烯酸甲酯或甲基丙烯酸甲酯，所述共混物例如可以在（甲基）丙烯酸甲酯与醇的酯交换反应中获得，以形成较高沸点的酯，如（甲基）丙烯酸二乙基氨基乙酯或丙烯酸2-乙基己酯。
    • 基本信息 添加关注 加入工作空间 PDF全文 PDF下载 全文下载 相似专利 双屏查看 权利要求书 说明书全文 Global Dossier Espacenet 法律信息 同族专利 专利引用
    • 45. 发明授权
      US4405343A Methanol dehydration 失效
    • Methanol dehydration
    • 甲醇脱水
    • US4405343A
    • 1983-09-20
    • US413744
    • 1982-09-01
    • Donald F. Othmer
    • Donald F. Othmer
    • B01D53/04 , B01D53/26 , C07C29/74
    • B01D53/0423 , B01D53/04 , B01D53/261 , C07C29/74 , B01D2257/7022 , B01D2259/402
    • Methanol is converted from syngas at high temperatures and pressures. The gas stream leaving the converter, at 300.degree. to 500.degree. C., above atmospheric pressure--usually between 750 to 7000 pounds per square inch, has besides the unreacted permanent gases of the syngas and others, methanol and water as well as other liquid impurities. Based on the weight of methanol, water may be present in from 0.5 to 20%, also small amounts of higher alcohols, dimethyl ether, etc. Condensation gives an aqueous liquid, from which the water must be separated if the methanol is to be used as a motor fuel. When this amount of water is low e.g. 0.5 to 12% this may be separated by adsorption most economically from the gas before condensation of the methanol. The energy in this gas stream at a high temperature and pressure above the ambient may be used to dehydrate completely the methanol, by the use of a conventional desiccant.
    • 甲醇在高温和高压下由合成气转化而成。 在300〜500℃，高于大气压（通常为750〜7000磅/平方英寸）的气流中除了合成气等未反应的永久性气体外，还有甲醇和水以及其他液体 杂质。 基于甲醇的重量，水可以以0.5至20％存在，少量的高级醇，二甲醚等。冷凝得到水性液体，如果要使用甲醇，则必须从其中分离水 作为汽油。 当该水量低时，例如 0.5至12％，这可以通过甲烷冷凝前的气体最经济地吸附分离。 在高于环境的高温和高压下，该气流中的能量可以通过使用常规的干燥剂来完全脱水甲醇。
    • 基本信息 添加关注 加入工作空间 PDF全文 PDF下载 全文下载 相似专利 双屏查看 权利要求书 说明书全文 Global Dossier Espacenet 法律信息 同族专利 专利引用
    • 46. 发明授权
      US4302222A Methods and apparatus for continuous preparative chromatographic separation of fluid mixtures 失效
    • Methods and apparatus for continuous preparative chromatographic separation of fluid mixtures
    • 液体混合物连续制备色谱分离的方法和设备
    • US4302222A
    • 1981-11-24
    • US121775
    • 1980-02-14
    • Bernard Miller , Henry L. Friedman , Charles H. Meiser, Jr.
    • Bernard Miller , Henry L. Friedman , Charles H. Meiser, Jr.
    • B01D53/02 , C07C29/74 , G01N30/40 , G01N30/58 , B01D15/08
    • G01N30/58 , B01D53/025 , C07C29/74 , G01N30/40
    • Two processes and apparatus for chromatographically separating components of a volatilizable mixture on a continuous basis are described herein as specific examples of the continuous preparative chromotographic separation of unwanted volatile species from volatile product by passage through a continuous fibrous textile solid. The volatilized mixture is fed by means of a flowing carrier gas through a column or conduit containing continuous polymeric solid therein such as a fibrous textile solid like yarn wherein one unwanted component of the mixture is significantly retarded in its passage by adsorption processes as compared to the other components of the mixture. The retarded component is that which one wishes to remove from the mixture. The desired product is gathered at the outlet of the conduit. The polymeric solid separating medium is regenerated by removal of the adsorbed component in either of two ways. In one method the adsorbing material is arranged in a continuously moving closed loop so that the adsorbed species can be stripped from it at a different location without interfering with continuous separation. The regenerated adsorbent is then returned to the point where it can serve to separate more of the mixture. In an alternate procedure, the adsorbed species is removed from a stationary adsorbing material by backflushing with carrier gas once the desired product has cleared. The column is then ready to receive a new charge of feed mixture. The conduit is preferably heated to control the movement of the various species so as to optimize the efficiency of separation. The major case to which these methods have been applied is the removal of water from a mixture with ethanol.
    • 作为连续制备色谱分离挥发性混合物的组分的两种方法和装置在本文中作为通过连续的纤维织物固体连续制备色谱分离挥发性物质的挥发性物质的具体实例。 挥发的混合物通过流动的载体气体通过其中含有连续聚合物固体的柱或导管进料，例如纤维织物固体如纱，其中混合物的一种不需要的组分在吸附过程中通过吸附过程显着延迟 混合物的其他组分。 延迟部件是希望从混​​合物中去除的部件。 所需产品聚集在导管的出口处。 通过以两种方式之一去除吸附组分来再生聚合物固体分离介质。 在一种方法中，吸附材料被布置在连续移动的闭环中，使得吸附的物质可以在不同的位置从其剥离，而不会干扰连续分离。 然后将再生的吸附剂返回到其可用于分离更多混合物的点。 在另一种方法中，一旦所需的产品清除，吸附的物质就会从固定的吸附材料中去除。 然后该柱准备好接收新的饲料混合物。 导管优选被加热以控制各种物质的运动，以便优化分离效率。 使用这些方法的主要情况是用乙醇从混合物中除去水。
    • 基本信息 添加关注 加入工作空间 PDF全文 PDF下载 全文下载 相似专利 双屏查看 权利要求书 说明书全文 Global Dossier Espacenet 法律信息 同族专利 专利引用
    • 49. 发明授权
      US3950371A Method of separating mixtures of fatty substances 失效
    • Method of separating mixtures of fatty substances
    • 分离脂肪物质混合物的方法
    • US3950371A
    • 1976-04-13
    • US458684
    • 1974-04-08
    • Lutz Jeromin , Norbert Bremus , Georg Friederici , Peter Peiffer
    • Lutz Jeromin , Norbert Bremus , Georg Friederici , Peter Peiffer
    • C07C51/42 , B01D9/02 , C07C29/74 , C07C67/48 , C11B7/00 , C11C1/08 , B01D9/00 , C11B3/00
    • C11B7/0091
    • A method for separating fatty substance mixtures into components of different melting points by the "Rewetting or Hydrophilization Process," with the heat removal necessary for cooling and crystallizing higher melting fatty substance fractions being obtained essentially by vacuum evaporation of an aqueous, non-surface-active electrolyte solution in direct contact with the fatty substance mixture.THE PRIOR ARTThe separation of fatty acid mixtures or of fatty acid ester mixtures into components of different melting points by a wetting agent process is known from U.S. Pat. No. 2,800,493, July 23, 1957, Stein et al. This process has become known as the "Rewetting or Hydrophilization Process." According to this patent, a mixture of solid and oily fatty substance particles is transformed by means of a wetting agent solution, optionally containing non-surface-active electrolyte, into a dispersion of separate solid and oily fatty substance particles. This dispersion is separated by means of solid jacket centrifuges into an oily phase and an aqueous phase containing the solid fatty substance particles in dispersion. The heat removal necessary for the crystallization of the solid fatty substance particles is obtained by cooling devices, in particular scraping condensers. After termination of the separating process, the recovered wetting agent solution is recycled. German Pat. No. 1,010,062, or U.S. Pat. No. 2,972,636, Stein et al, describes a corresponding process for the separation of fatty alcohols.The essential disadvantages of the above mentioned processes are the high investment and operating costs for cooling equipment and cooling devices. In particular the required scraping condensers are costly and require continual servicing.From U.S. Pat. No. 3,541,122 a method is further known for the separation of mixtures of fat-like materials into fractions of different melting points, which is also carried out by the rewetting process. Here, however, the cooling of the molten fatty substance mixture required for crystallization is obtained by vacuum evaporation of water. After completion dispersion of the fatty substance mixture consisting of liquid and solid particles in a wetting agent solution, the crystallized solid phase is separated by filtration, and the oily dispersion passes through the filter. In this procedure the separation of the oily fraction and the solid particles is not complete, so that the latter have a relatively high iodine number and hence a comparatively poor quality.Published German Patent Application (DOS) No. 1,915,298, discloses a method of separating fatty acid, fatty alcohol, or fatty acid ester mixtures into components of different melting points by mixing the molten mixture with an aqueous wetting agent solution. The crystallization of the solid fractions to be separated is obtained by evaporating a part of the aqueous wetting agent solution under reduced pressure. Because the fatty substances used can be degased only with difficulty and incompletely on being fed into the crystallizer vessel, intense foaming takes place upon addition of the wetting agent solution, whereby the progress of the process is greatly disturbed. Moreover, the wetting agent hinders crystal growth, which in turn leads to difficulties in the further separation of oily and solid phase.OBJECTS OF THE INVENTIONIt is an object of the present invention, in carrying out the rewetting process to avoid the high investment costs for the installation and servicing of refrigeration equipment and cooling devices, in particular scraping condensers, and, furthermore, to improve the effectiveness of the separation method and hence to improve the quality of the products obtained.It is another object of the present invention to provide a method of separating fatty substance mixtures into components of different melting points by the rewetting process, with the heat removal necessary for cooling and crystallizing higher melting fatty substance fractions being obtained essentially by vacuum evaporation of an aqueous, non-surface-active electrolyte solution in direct contact with the fatty substance mixture.These and further objects of the present invention will become apparent as the description thereof proceeds.DESCRIPTION OF THE INVENTIONThe present invention relates to a method of separating fatty substance mixtures into components of different melting points.Generally speaking, the present invention concerns a method of separating fatty substance mixtures into components of different melting points by the rewetting process, with the heat removal necessary for cooling and crystallizing higher melting fatty substance fractions being obtained essentially by vacuum evaporation of an aqueous, non-surface-active electrolyte solution in direct contact with the fatty substance mixture.More particularly, the present invention provides a method of separating fatty substance mixtures into components of different melting points by the rewetting process, where the heat removal required for the cooling and crystallization of higher melting fatty substance fractions is obtained by vacuum evaporation of an aqueous phase in direct contact with the fatty substance mixture, characterized by the following steps:a. partial or complete melting of the fatty substance mixture;b. addition of an aqueous non-surface-active electrolyte solution to the molten fatty substance mixture and evaporation of a part of the water of the electrolyte solution by means of a vacuum simultaneously with intensive mixing to produce partial or complete crystallization of the higher melting fraction;c. addition of wetting agent solution with dispersing of the liquid and solid fatty substance therein, preferably while maintaining the vacuum and continuing the water evaporation until the separation temperature is reached;d. separation of the dispersion by means of centrifuge into an oily phase containing the lower melting fatty substance fractions, and an aqueous phase containing the crystallized fatty substance fractions in dispersed form;e. separation of the higher melting fatty substance fractions from the aqueous phase by filtration or by melting and subsequent separation of oily from aqueous phase by centrifuging or allowing to settle.The present invention is preferrably directed to an improvement in the method for the separation of mixtures of fatty substances into components of different melting points by the rewetting process which comprises the steps of (a) at least partial melting of a fatty substance mixture, (b) cooling and crystallizing said fatty substance mixture into a mixture of liquid and solid particles, (c) dispersing said mixture of liquid and solid particles in an aqueous wetting agent solution containing electrolyte at a temperature whereby a dispersion of liquid and solid fatty substance is obtained, (d) separation said dispersion into a lighter phase consisting substantially of the liquid, lower-melting fatty substance fractions and a heavier phase consisting substantially of solid, higher-melting fatty substance fractions dispersed in said aqueous wetting agent solution, (e) separating the solid higher-melting fatty substance fractions from said aqueous wetting agent solution, and (f) recovering said separated fatty components of different melting points; the improvement which comprises in step (b) adding an aqueous non-surface-active electrolyte solution to said at least partially melted fatty substance mixture and cooling to substantially the separation temperature by evaporation under vacuum of a part of the water of said aqueous electrolyte solution with simultaneously intensely mixing said at least partially melted fatty substance mixture and said aqueous electrolyte solution.In addition the invention comprises the further improvement of optionally adding a part or all of the said aqueous wetting agent solution while maintaining the vacuum and continuing the water evaporation until the desired separation temperature is reached.In a preferred embodiment of the process, the aqueous electrolyte containing wetting agent solution is recycled entirely or partially.The method is suitable for the separation of a variety of fatty substance mixtures; in particular, mixtures of fatty acids, fatty acid esters or fatty alcohols can be separated when the melting points of the components to be separated are sufficiently far apart.Of particular technical importance is the separation of fatty acid mixtures into technical olein and technical stearin (oleic and stearic acids), or of fatty alcohol mixtures into oleyl alcohol and stearyl alcohol. Correspondingly, solid mixtures of fatty acid triglycerides can be separated at room temperature into lower and higher melting fractions. Such fatty acid triglyceride fractions are used for the production of edible fats. It is not necessary that one of the components to be separated is present as a liquid oil at room temperature. The method can also be successfully utilized when both fractions are solid at room temperature and merely differ sufficiently in their melting points.The process of the present invention is carried out in the following manner:a. The fatty substance mixture to be separated is wholly or partially melted in a suitable heatable vessel, for example, in a melting device equipped with a stirrer, so that the temperature of the mixture is above the anticipated separation temperature. Alternatively the procedure may be to precool a fully molten mixture in a conventional manner, for example, in a heat exchanger, so that a partial elimination of the fatty fraction to be separated has already occurred. It is generally desirable for technical reasons to avoid a partial crystallization in this stage and to select the temperature somewhat above the starting crystallization temperature.b. The further cooling of the partially or completely molten fatty substance mixture is achieved by vacuum evaporation cooling. The process may be conducted by batches or continuously. The vaporizable liquid utilized is preferably an aqueous non-surface-active electrolyte solution. Preferably this is a makeup solution where a continuous process is employed with a discharge of part of the cycling aqueous solution. This solution is brought into contact with the fatty substance mixture under vacuum and is simultaneously mixed intensively. This mixture is maintained under reduced pressure with continual evacuation of the water vapor formed until a viscous crystal paste has been formed, by crystallization of solid fatty substance from the fatty substance mixture which can hardly be handled by the mixer. The temperature reached at this point is termed the temperature limit of incipient crystallization. At this stage the evaporation of water is greatly hindered due to insufficient mixing, so that the cooling rate decreases considerably and continuation of the process would become uneconomical.When working by batches, the pressure in the mixing vessel is reduced by means of a suitable evacuating system. Above the liquid, the vapor pressure of water adjusts itself to the respective temperature so that the cooling takes place without temperature discontinuities in the metastable range of crystallization along the vapor pressure curve of water. In this temperature range spontaneous seed formation is largely avoided; and relatively large crystals are formed which are capable of good separation from the oily phase.The addition of electrolyte solution occurs either intermittently or continuously after evacuation of the vessel. The electrolyte solution may be introduced below the surface of the fatty substance mixture, possibly in finely divided form, whereby intensive mixing takes place simultaneously.For continuous operation it is preferred to work with a cascade vessel equipped with a stirrer. The fatty substance mixture and electrolyte solution are fed into the first stirrer equipped vessel of the cascade apparatus and then pumped from one stage to the next. In the downstream flow direction of the product stream, the pressure and hence the temperature decreases by discontinuous steps from vessel to vessel according to the vapor pressure of the water. The temperature steps must be made very small, and hence the number of mixing vessels of the cascade apparatus must be made so large that the continuous process will come as close as possible to the "ideal crystallization" along the vapor pressure curve of water, attainable in batch operation. This is because in the batch process the crystallization occurs in the metastable range and spontaneous seed formation is avoided.The quantity of heat to be removed by evaporation depends on the heat capacity of the batch, upon the desired temperature decrease, and upon the heat of crystallization obtained. The amount of electrolyte solution added to the fatty substance mixture in partially to completely molten form is such that the necessary temperature reduction is obtained and that upon reaching the temperature limit of incipient crystallization a just barely stirrable and pumpable crystal plate is present. As a rule, however, as much electrolyte solution is added as water and wetting agent solution is removed during the cycle. The quantity of wetting agent solution to be eliminated from the cycle depends largely on the purity of the fatty substances and is necessary for the removal of slime and dirt substances from the process, which would influence the crystallization and, if not removed, would cause progressively higher iodine numbers in the components of the fatty substances that are solid at the separation temperature.The temperature of the electrolyte solution when added should be approximately equal to that of the fatty substance mixture batch.The aqueous non-surface-active electrolyte solution used in the process contains about 0.1% to 10% by weight, preferably from 0.5% to 2% by weight of a water-soluble salt for example a chloride, sulfate or nitrate of a mono-di- or tri-valent metal, such as a salt of an alkali metal, an alkaline earth metal, or an earth metal. Salts such as sodium sulfate, magnesium sulfate or aluminum sulfate have proved particularly successful as agents in forming the electrolyte solution. The total quantity of electrolyte to be added depends upon the proportion of electrolyte containing wetting agent solution removed from the cycle at the end of the separating process.c. After the desired temperature has been reached, the vacuum may be broken; and the quantity of wetting agent solution necessary for dispersing the liquid and solid fatty substance is added. With intense mixing the rewetting process begins. The oily fractions of the fatty substance mixture are displaced from the surfaces of the crystallized or solid fractions.In a preferred embodiment of the process, a portion of the wetting agent solution is introduced before the desired separation temperature is reached. This is done appropriately as soon as the temperature limit of incipient crystallization is reached; and the addition of wetting agent causes the crystal paste to liquefy again. The vacuum is then maintained, such that the process of evaporation and cooling can now proceed until the anticipated separation temperature is reached. At the same time the rewetting process takes place, and a highly fluid dispersion is formed which contains both the oily as well as the crystallized fatty substance fractions as separate particles in dispersion.The wetting agent solution utilized is essentially the so-called "old diluted" wetting agnt solution recycled from the process. If necessary, fresh wetting agent is added to the "old diluted" solution as replacement for the wetting agent fraction lost in separation or discharged. Difficulties due to foaming do not occur even when operating according to the preferred process embodiment; that is when the wetting agent solution is introduced into the vessel while still under vacuum. This is preferably done by feeding in (flashing in) above the liquid surface, due to which extensive degasing and removal of the dissolved air, occurs before the mixture of fatty substance and electrolyte solution is stirred in. The fatty substances used are degased anyway by the preceding vacuum evaporation cooling. The water vapor evolved during the continued evaporation cooling forms relatively closely below the surface of the liquid; and the distance it travels while rising is very short, so that no foaming occurs.To obtain a separable dispersion, the proportion of aqueous phase at the end of the evaporation cooling step should be from 0.3 to 5 times, preferably from 0.7 to 3 times, the fatty substance mixture charged. The losses due to discharging a part of the wetting agent solution, the so-called "old diluted" solution, from the process cycle are replaced expediently after the vacuum has been broken by a corresponding amount of electrolyte solution for incipient crystallization and of fresh wetting agent.Examples of wetting agents include anionic or non-ionic water-soluble compounds, which lower the surface tension of the aqueous solution and thus bring about a displacement of the oily components of the starting mixture from the surface of the crystallized or solid fractions. The surface-active compounds disclosed in U.S. Pat. No. 2,800,493 can be used as wetting agents in particular, compounds with alkyl radicals having 8 to 18 carbon atoms, preferably 10 to 16 carbon atoms in the molecule. Examples of suitable anionic surface-active compounds include soaps; sulfonates such as alkylbenzene sulfonates having 8 to 18 carbon atoms in the alkyl, and alkyl sulfonates having 8 to 18 carbon atoms; sulfates such as fatty alcohol sulfates having 8 to 18 carbon atoms, sulfatized reaction products of fatty alcohols having 8 to 18 carbon atoms, adducted with 1 to 10, preferably 2 to 5 mols of ethylene oxide and/or propylene oxide, and fatty acid monoglyceride sulfates having 8 to 18 carbon atoms in the fatty acid moiety, etc. These anionic surface-active compounds are used in the form of their alkali metal salts, preferably as the sodium salt, but other suitable salts include the potassium salt, ammonium salt, the mono-, di- or tri-lower alkanolamine salts such as the triethanolamine salt. Examples of non-ionic surface-active compounds include the water-soluble products of addition of ethylene oxide and/or propylene oxide to alkyl phenols having 8 to 18 carbon atoms in the alkyl or to fatty alcohols having 8 to 18 carbon atoms. The fatty substance dispersion should contain from 0.05 to 2, preferably 0.1 to 1, parts by weight of wetting agent per 100 parts by weight of solution. This amount of wetting agent includes not only the amount of wetting agent dissolved in the aqueous phase, but also that dissolved in the oil or adsorbed on the surface of the solid fractions.d. After completion of the cooling and breaking of the vacuum, the dispersion of the fatty substance fractions is separated by means of centrifuges, such as full jacket centrifuges or separators, into an oily phase containing the lower melting fatty substance fractions, and into an aqueous phase containing the crystallized or solid fatty substance fractions in dispersed form. For this process various centrifuge types are suitable, for example tube centrifuges, dish centrifuges or scoop tube centrifuges. Especially preferred are the latter type, in which the phases are removed from the centrifuge by scoop tubes.After passing through the centrifuge, the oily fatty substance fractions are recovered, possibly after having been washed and dried. If necessary, another separation step may be employed at a lower temperature, such that an oil of correspondingly lower cloud point will be obtained.e. The suspension of crystallized fatty substance fractions issuing from the centrifuge is separated by heating the suspension. The crystallized fatty substance fractions melt, and subsequently centrifuging or settling takes place, for example in settling tanks. Another possibility is to filter the crystallized fatty substance fractions. After passing through the separating process once, the higher melting fraction of the fatty substance mixture thus obtained has a very high purity.The recovered wetting agent solution is recycled as socalled "old dilution." From 30% to 90% by weight is recovered and recycled, and preferably from 60% to 90%, and especially 70%, is recovered and recycled. It is, however, necessary to remove a part of this solution from the cycle continuously to avoid the accumulation of slime impurities or non-fatty substance organic impurities from the fatty substances charged, which could impair the crystallization and also the quality of the higher melting fatty substance fraction. The resulting loss of wetting agent solution must be compensated by adding fresh wetting agent solution. The simultaneously occurring electrolyte loss is replaced by the electrolyte solution supplied during evaporation cooling, and in particular, during incipient crystallization. Further the process must be controlled so that the losses of water occurring during evaporation cooling, or due to removal of wetting agent solution, are compensated by the electrolyte solution or fresh wetting agent solution supplied. Some discussion of these procedures is to be found in U.S. Pat. No. 3,737,444, June 5, 1973, Hartmann et al.The procedure according to the invention has special advantages over the known process. On the one hand, operating in the metastable range of crystallization and in the presence of electrolyte solution brings about the formation of particularly large crystals which permit a very neat separation of the oily fatty substance fraction. Compared with the method described in U.S. Pat. No. 3,541,122 (incipient crystallization in water) and with the mode of operation set forth in German Offenlegungsschrift No. 1,915,298 (incipient crystallization in wetting agent solution), it is possible to obtain a purer and hence more valuable, crystallized fatty substance by utilizing the new process involving incipient crystallization in the presence of electrolyte solution. For example it is possible to obtain from tallow fatty acids, a purer and more valuable, crystallized fatty substance, stearin or technical stearic acid. At the same time, the yield of the oily fatty substance phase, the olein or technical oleic acid, is thereby increased.On the other hand, the foaming problems occurring in the known process of evaporation cooling in the presence of wetting agents are avoided, since in the presence of electrolyte solution, a complete degasing of the fatty substance mixture readily takes place during the evaporation cooling. A special pretreatment of the fatty substance mixture or, respectively, a preceding additional separative process step is thus unnecessary with the continuous mode of operation. On the other hand, the process of the invention is particularly favorable also from the aspect of instrumentation, inasmuch as special cooling devices, such as refrigeration machines, scraping condensers and the like, become superfluous. Naturally, however, a combination of the conventional cooling method with the described new method is conceivable, but as a rule such combinations are not important because they lack economic efficiency.The following examples are merely illustrative of the present invention without being deemed limitative in any manner thereof.
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