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1.发明授权Process for producing fatty alcohols and C.sub.3 diols by catalytic hydrogenation 失效通过催化氢化生产脂肪醇和C3二醇的方法
公开(公告)号：US4942266A
公开(公告)日：1990-07-17
申请号：US326185
申请日：1989-03-17
IPC分类号： B01J23/86 , C07B61/00 , C07C27/00 , C07C27/02 , C07C29/149 , C07C29/60 , C07C31/02 , C07C31/125 , C07C31/20 , C07C67/00
CPC分类号： C07C29/60 , C07C29/149
摘要： A process for the catalytic hydrogenation of liquid fatty acid triglycerides and the simultaneous recovery of fatty alcohols and C.sub.3 diols in the presence of gaseous hydrogen and hydrogenation catalysts under pressures of from 50 to 300 bar and at temperatures in the range from 160.degree. to 250.degree. C., to produce fatty alcohols in at least 99% of the theoretical yield and of 1,2-propanediol in at least 80% of the theoretical yield and a maximum paraffin content of 0.5% of the theoretical yield is disclosed. The hydrogenation reaction is carried out in a tube bundle reactor operated under isothermal conditions through a cooling or heating fluid, the liquid phase being passed as co-current trickle phase with the gaseous phase over catalyst packings in the individual reactor tubes without back-mixing, and in that the load per unit volume of the reactor is selected between 0.2 and 2.5 l starting material per 1 reactor volume per hour and the load per unit area of each individual reactor tube between 1.5 and 25 m.sup.3 starting material per m.sup.2 reactor cross-section per hour and the reaction parameters of temperature and pressure are adapted in accordance with the actual catalyst activity.
摘要翻译： 一种在液体脂肪酸甘油三酯的催化氢化和在气态氢气和氢化催化剂存在下同时回收脂肪醇和C 3二醇的方法，其压力为50-300巴，温度为160-250℃。 在理论产率的至少80％中产生至少99％理论产率的脂肪醇和1,2-丙二醇，并且公开了理论产率的最大链烷烃含量为理论产率的0.5％。 氢化反应在通过冷却或加热流体在等温条件下操作的管束反应器中进行，液相通过与各相反应器管中的催化剂填料上的气相作为同时滴流相而不进行反混合， 反应器的每单位体积的负荷选择在每小时每1个反应器体积的0.2-2.5升起始材料之间，每个反应器管的每单位面积的载荷在每平方米反应器横截面为1.5至25立方米起始材料之间 每小时，温度和压力的反应参数根据实际的催化剂活性进行调整。
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公开(公告)号：US4381407A
公开(公告)日：1983-04-26
申请号：US228452
申请日：1981-01-26
CPC分类号： C07C67/08 , Y10S203/06
摘要： A process for the continuous production of triacetin consisting essentially of continuously charging liquid glycerol into a first liquid reaction area through which acetic acid vapors and water vapors flow, said liquid reaction area being divided into a number of separate individual areas through which liquid glycerol and liquid acetin reaction products flow in one direction and gaseous acetic acid and water flow in a countercurrent direction, continuously charging acetic acid vapor to a separate individual area where said liquid mixture has an OH number of less than 600, continuously separating a liquid mixture of acetins and water having an OH number of less than 600, continuously passing said liquid mixture into a second liquid reaction area, continuously adding thereto liquid acetic acid anhydride in an amount sufficient to react with water dissolved in said liquid mixture to form acetic acid and to react with monoacetin and diacetin present to form triacetin and continuously recovering triacetin.
摘要翻译： 连续生产三醋精的方法，其主要包括将液体甘油连续地装入第一液体反应区域，乙酸蒸汽和水蒸气通过该第一液体反应区域流动，所述液体反应区域被分成多个单独的单独区域，液体甘油和液体 乙酸反应产物在一个方向上流动，气态乙酸和水以逆流方向流动，将乙酸蒸汽连续地加入到所述液体混合物的OH值小于600的单独区域，连续分离乙醇的液体混合物， OH值小于600的水，将所述液体混合物连续通入第二液体反应区域，连续加入足以与溶解在所述液体混合物中的水反应的液体乙酸酐，形成乙酸，并与 存在单醋素和双醋精以形成三醋精并连续回收 三口醋精
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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：US5008046A
公开(公告)日：1991-04-16
申请号：US326592
申请日：1989-03-21
IPC分类号： C07B61/00 , B01J27/02 , B01J31/02 , C07C67/08 , C07C69/02 , C07C69/24 , C07C69/28 , C11C3/00
CPC分类号： C07C67/08
摘要： The invention is a process for the continuous liquid-phase esterification of C.sub.2 -C.sub.24 fatty acids with alkanols in countercurrent contact and reaction in a reaction column, the catalysts and fatty acids are introduced at the top plate and the alkanols below the lowest plate, at a head pressure of the reaction column of 200 to 900 hPa. The process reduces dehydration of the alkanols.
摘要翻译： 本发明是C2-C24脂肪酸与链烷醇在反应塔中逆流接触和反应中连续液相酯化的方法，将催化剂和脂肪酸引入顶板和最低板下方的链烷醇 反应塔的压头压力为200〜900hPa。 该方法减少了链烷醇的脱水。
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