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公开(公告)号：US4365081A
公开(公告)日：1982-12-21
申请号：US263935
申请日：1981-05-15
CPC分类号： B01D5/0027 , B01D3/14 , C07C67/26 , Y10S203/90
摘要： In a process for producing a 2-hydroxyalkyl acrylate or methacrylate which comprises esterifying acrylic or methacrylic acid with an alkylene oxide having 2 to 4 carbon atoms in the presence of an esterification catalyst and distilling the resulting reaction mixture in a distillation column, the improvement wherein the vapor of the ester monomer from the distillation column, while being maintained in the superheated state, is introduced into a condenser of the gas-liquid direct contact type whose inner wall corresponding to its gas inlet portion is kept at a temperature below the boiling point of the ester at the operating pressure, to contact it directly with a concurrently flowing spray liquid of the ester-precooled to a temperature below the boiling point of the ester at the operating pressure, whereby said vapor is condensed to a liquid at said temperature below the boiling point of the ester at the operating pressure.
摘要翻译： 在制备丙烯酸2-羟基烷基酯或甲基丙烯酸酯的方法中，其包括在酯化催化剂存在下将丙烯酸或甲基丙烯酸与具有2至4个碳原子的烯化氧进行酯化，并将所得反应混合物蒸馏在蒸馏塔中，其改进在于 来自蒸馏塔的酯单体的蒸气在保持过热状态的同时被引入气液直接接触型的冷凝器中，其气体入口部分的内壁保持在低于沸点 的酯在工作压力下直接与酯预先冷却的同时流动的喷雾液体接触到低于酯的沸点的温度，由此所述蒸气在所述温度下冷凝至液体 酯在操作压力下的沸点。
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62.发明授权
公开(公告)号：US4350572A
公开(公告)日：1982-09-21
申请号：US204637
申请日：1980-11-06
CPC分类号： C07C67/60
摘要： A process for purifying carboxylic acid esters which have been obtained by reacting olefinically unsaturated compounds with carbon monoxide and alkanols and which contain aldehydes or acetals, wherein the said esters are treated with a strongly acidic agent, with or without addition of water.
摘要翻译： 通过使烯属不饱和化合物与一氧化碳和链烷醇反应并且含有醛或缩醛而获得的羧酸酯的方法，其中所述酯用强酸性剂处理，或不加入水。
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公开(公告)号：US4304925A
公开(公告)日：1981-12-08
申请号：US134137
申请日：1980-03-26
IPC分类号： B01J31/00 , C07B61/00 , C07C67/08 , C07C67/48 , C07C69/00 , C07C69/003 , C07C69/80 , C09F5/08 , C11C3/02
CPC分类号： C07C67/60
摘要： In a process for purifying an ester with little contamination by catalytic metal components in a high yield which comprises treating an esterification reaction mixture with a basic substance, said esterification reaction mixture being obtained by reacting an organic carboxylic acid or its anhydride with an alcohol in the presence of an organometallic compound as an esterification catalyst, and purifying the product in a manner known per se; the improvement wherein prior to said treatment with the basic substance, water is added to the esterification reaction mixture and the mixture is heated.
摘要翻译： 在以高产率纯化催化金属成分几乎不污染的酯的方法中，该方法包括用碱性物质处理酯化反应混合物，所述酯化反应混合物是通过使有机羧酸或其酸酐与醇在 作为酯化催化剂存在有机金属化合物，并以本身已知的方式纯化产物; 改进之处在于，在用碱性物质处理之前，将水加入到酯化反应混合物中，混合物被加热。
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公开(公告)号：US4284793A
公开(公告)日：1981-08-18
申请号：US133863
申请日：1980-03-25
申请人： Fumio Sagara , Hiroshi Kawabata , Kiyonori Shiiba
发明人： Fumio Sagara , Hiroshi Kawabata , Kiyonori Shiiba
CPC分类号： C07C67/60
摘要： A method for producing plasticizers which contain titanium in only a very small amount is provided. According to this method, the amount of waste water is very small. This method comprises reacting phthalic anhydride with an alcohol having 4-18 carbon atoms in the presence of, as a catalyst, a tetraalkyl titanate or a polymer thereof, and has a feature in the treatment of the resultant ester with a solid alkali and adsorbing agent(s) in the absence of water.
摘要翻译： 提供了一种生产仅含有极少量的钛的增塑剂的方法。 根据这种方法，废水量很小。 该方法包括在作为催化剂的钛酸四烷基酯或其聚合物的存在下使邻苯二甲酸酐与具有4-18个碳原子的醇反应，并且具有用固体碱和吸附剂处理所得酯的特征 在没有水的情况下。
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公开(公告)号：US4210594A
公开(公告)日：1980-07-01
申请号：US24759
申请日：1979-03-28
申请人： Ted J. Logan , David C. Underwood
发明人： Ted J. Logan , David C. Underwood
摘要： Continuous, countercurrent flow, fluid-solid contacting process for the separation of more unsaturated fatty acid ester from a less unsaturated fatty acid ester in a mixture comprising the two types of esters. The solid adsorbent utilized in said process is a Type X or Type Y zeolite containing specified cations at the exchangeable cationic sites, and the desorbent is a mixture of a paraffinic hydrocarbon and an ether.
摘要翻译： 连续的，逆流的流体 - 固体接触方法，用于在包含两种类型的酯的混合物中分离更不饱和脂肪酸酯与较不饱和脂肪酸酯。 在所述方法中使用的固体吸附剂是在可交换的阳离子位点含有特定阳离子的X型或Y型沸石，解吸剂是链烷烃和醚的混合物。
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66.发明授权Process for the separation of water from gas mixtures formed in the manufacture of vinyl acetate 失效从乙酸乙烯酯制造中形成的气体混合物中分离水的方法
公开(公告)号：US4156632A
公开(公告)日：1979-05-29
申请号：US776364
申请日：1977-03-10
申请人： Gunter Roscher , Heinz Schmitz
发明人： Gunter Roscher , Heinz Schmitz
IPC分类号： B01D3/14 , B01D3/16 , B01D5/00 , C07C20060101 , C07C67/05 , C07C67/055 , C07C67/48 , C07C67/54 , C07C69/15 , C07C69/54
CPC分类号： C07C67/055 , C07C67/52 , C07C67/54
摘要： The invention relates to a process for the partial separation of water from gas mixtures formed in the manufacture of vinyl acetate by reaction of ethylene with acetic acid and oxygen in the gaseous phase and in the presence of catalysts. In a "predehydration column", more than half of the water formed in the reaction is eliminated without requiring energy feed. The mixture obtained which is relatively poor in water is worked up according to known methods.
摘要翻译： 本发明涉及一种通过在气相和催化剂存在下乙烯与乙酸和氧气反应而在乙酸乙烯酯制备中形成的气体混合物中部分分离水的方法。 在“脱水塔”中，消除反应中形成的一半以上的水，而不需要能量进料。 得到的水相对较差的混合物根据已知方法进行后处理。
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公开(公告)号：US4078143A
公开(公告)日：1978-03-07
申请号：US647995
申请日：1976-01-09
申请人： Abdul-Ilah Malik , Elmer Edwin Most
发明人： Abdul-Ilah Malik , Elmer Edwin Most
CPC分类号： C08J11/00 , C07C67/03 , C08J2367/02
摘要： Recovery of ethylene terephthalate polymer from waste material is accomplished by glycolysis of the polyester to form bis-(2-hydroxyethyl)terephthalate for repolymerization. Formation of objectionable diethylene glycol is inhibited when glycolysis is accomplished by heating the polyester in a reaction mixture with bis-(2-hydroxyethyl)terephthalate, ethylene glycol and sodium acetate trihydrate, and water is introduced continuously into the reaction mixture during depolymerization of the polyester.
摘要翻译： 从废料中回收对苯二甲酸乙二醇酯聚合物通过聚酯的糖酵解来形成双 - （2-羟乙基）对苯二甲酸酯进行再聚合。 通过在与双 - （2-羟乙基）对苯二甲酸乙二醇酯，乙二醇和乙酸钠三水合物的反应混合物中加热聚酯来实现糖酵解时，抑制不良二甘醇的形成，并且在聚酯解聚期间将水连续引入反应混合物 。
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68.发明授权
公开(公告)号：US3965149A
公开(公告)日：1976-06-22
申请号：US520760
申请日：1974-11-04
申请人： Lee R. Mahoney
发明人： Lee R. Mahoney
CPC分类号： C08J11/08 , C07C67/333 , C08J2333/12 , Y02W30/701
摘要： A method for recovering methyl methacrylate from a mixture of polymeric materials containing poly (methyl methacrylate) which comprises contacting the mixture with a boiling C.sub.5 - C.sub.8 alkane, separating an insoluble residue containing poly (methyl methacrylate) from the alkane and its extract, extracting poly (methyl methacrylate) from such insoluble residue with boiling acetone, separating the poly (methyl methacrylate) from the acetone, and recovering the methyl methacrylate monomer from such poly (methyl methacrylate) by pyrolysis. In a preferred embodiment, the poly (methyl methacrylate) containing solid obtained after the acetone extraction is compressed under elevated temperatures and pressures prior to pyrolysis. The method can be stopped prior to the pyrolysis step when it is desired to recover only the poly (methyl methacrylate).
摘要翻译： 从含有聚（甲基丙烯酸甲酯）的聚合材料的混合物中回收甲基丙烯酸甲酯的方法，该方法包括使该混合物与沸腾的C 5 -C 8烷烃接触，从烷烃及其提取物中分离出含有聚（甲基丙烯酸甲酯）的不溶性残余物，提取聚 （甲基丙烯酸甲酯）由沸腾的丙酮从不溶性残留物中分离，从丙酮中分离聚（甲基丙烯酸甲酯），并通过热解从这种聚（甲基丙烯酸甲酯）中回收甲基丙烯酸甲酯单体。 在优选的实施方案中，在丙酮萃取之后获得的含有聚甲基丙烯酸甲酯的固体在高温和高压下被压缩，然后进行热解。 当需要仅回收聚（甲基丙烯酸甲酯）时，可以在热解步骤之前停止该方法。
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公开(公告)号：US3950371A
公开(公告)日：1976-04-13
申请号：US458684
申请日：1974-04-08
申请人： Lutz Jeromin , Norbert Bremus , Georg Friederici , Peter Peiffer
发明人： Lutz Jeromin , Norbert Bremus , Georg Friederici , Peter Peiffer
CPC分类号： C11B7/0091
摘要： 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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公开(公告)号：US3900513A
公开(公告)日：1975-08-19
申请号：US40944073
申请日：1973-10-25
申请人： UPJOHN CO
IPC分类号： C07C405/00 , C07C61/38 , C07C51/48 , C07C67/48 , C07C69/74
CPC分类号： C07C405/00 , Y02P20/582
摘要： A composition obtained by extracting colonies or colony pieces of the marine invertebrate Plexaura homomalla (Esper), 1792, forma S or R, said colonies or colony pieces having been previously maintained in contact with water in a temperature range up to 50* C. until substantially all of the C-15 acetates of the prostanoic acid derivatives originally present are transformed to C-15 hydroxy derivatives. Said composition is useful as a source of PGA2 or PGA2 methyl ester, if obtained from forma S, or 15 Beta -PGA2 or 15 Beta -PGA2 methyl ester if obtained from forma R.
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