A way of separating linear alpha olefins from 2-branched and/or 3-branched alpha-olefins
(57) Abstract:Usage: petrochemistry. Essence: spend contacting the feed stream with one or more linear polyaromatic compounds having 3 or more condensed aromatic, optionally substituted ring, under conditions effective for the formation of the adduct of linear polyaromatic compound-linear alpha olefin; Department of adduct linear polyaromatic compound-linear alpha olefin from the reaction mixture; the decomposition of the adduct of linear polyaromatic compound-linear alpha olefin with the formation of the linear polyaromatic compounds and compositions of linear alpha-olefin, and separating the linear polyaromatic compounds formed in stage (C), from the specified composition of linear alpha-olefin. Effect: higher efficiency of separation. 10 C.p. f-crystals, 6 PL. The scope of the invention
This invention relates to a method for separating linear alpha olefins from a mixture thereof with 2-branched alpha olefins and/or 3-branched alpha olefins.Background of the invention
Many industrial processes result in olefins, prefinal and other olefins of the same molecular weight or overlapping number of carbon atoms, their separation is not an easy task. Olefins are often used in the production of polymers or as an additive to drilling mud, or as intermediates in obtaining additives to oils and detergents. Depending on the specific application it would be desirable to obtain a composition of alpha-olefin with the highest possible degree of purity. For example, polymers based on polyethylene often get through copolymerization of ethylene with small amounts of linear alpha-olefins such as 1-octene. Composition 1-actinophage of olefin containing substantially branched varieties, especially the second and/or third carbon atoms, is not suitable for such purposes. Required for these purposes, the olefin is one in which, to the extent possible, branched alpha-olefins are removed. Although these pure types of linear alpha-olefins with a narrow range of number of carbon atoms can be obtained and available at great value, it was determined that it would be particularly desirable economically to provide practical industry large quantities of purified compositions of linear alpha-olefins, obtained from a crude feed stream product containing the OIG submitted flows of the product contains more impurities, such as paraffins, aromatics, alcohols and ketones, from which linear alpha-olefins, it is necessary to separate.Separation and isolation of linear non-branched alpha olefins from 2-branched alpha-olefins and/or 3-branched alpha-olefins is not an easy task, especially when these varieties have the same or similar molecular weight or the number of carbon atoms. Conventional methods of distillation is not sufficient for selecting varieties of this type, which have such closely related boiling point. The separation problem is further complicated by the fact that varieties of linear non-branched alpha-olefins must be separated not only from the branched alpha-olefins, but also from everything else that is present in the mixture feed stream product, as, for example, from the internal linear or branched olefins. In U.S. patent 4946560 describes how the Department of internal olefins from alpha-olefins by contacting the feed stream product with anthracene to form adduct of olefin, separating the adduct from the feed stream product, heating the adduct to obtain anthracene and olefinic product enriched in alpha olefin, and tivni for separating linear alpha olefins from 2 and/or 3-branched alpha-olefins. Moreover, in the present alternative adduct-forming compounds in addition to anthracene, which are also effective for separating linear alpha olefins from other olefins in the raw feed stream product.Summary of the invention
Thus, the present invention relates to a method for separating linear alpha olefins from mixtures thereof in the feed stream of the product olefins, which have a branching in the 2 and/or 3-position, this method includes:
a) contacting the feed stream of the product with one or more linear polyaromatic compounds having 3 or more condensed aromatic, optionally substituted ring, under conditions effective for the formation of the adduct of linear polyaromatic compound-linear alpha olefin;
b) separating the adduct of linear polyaromatic compound-linear alpha olefin from the reaction mixture; and
c) the decomposition of the adduct of linear polyaromatic compound-linear alpha olefin with the formation of the linear polyaromatic compounds and compositions of linear alpha-olefin and, optionally,
d) isolation of the linear polyaromatic compounds, obrazovvanii of the invention the linear polyaromatic compound is an anthracene, which may be optionally substituted.In another preferred embodiment of the invention the linear polyaromatic compound is a 2,3-benzanthracene, which may be optionally substituted.Detailed description of the invention
Linear alpha-olefin(s) indicates the absence of branching as in C2and WITH3positions relative to each alpha double bonds.Branched alpha-olefin(s) means an alpha-olefin having branching at least in C2or, alternatively, at least in C3position relative to each alpha dual-link. Branching in both2and C3the provisions fall within the definition of a branched alpha-olefin, and branching present in the subsidiary arrangements, outside WITH3position until at least one branch is located in2and/or C3position. Alpha-olefins having branching only in C3position or only in C2position, also fall under the definition of a branched alpha-olefin.The feed stream of olefins used in the method according to the invention contains at least the linear al is lastnosti, linear internal olefins, branched internal olefins, and paraffins, aromatic compounds and oxidized compounds. The feed stream is usually obtained by industrial methods, such as the oligomerization of ethylene, optionally with subsequent isomerization and disproportionation. Alternatively, the feed stream can be obtained by the method of Fischer-Tropsch, therefore it usually contains a considerable number of branched species.In the preferred embodiment, in which the feed stream contains at least a branched alpha-olefins, internal olefins and linear alpha-olefins, the amount of each ingredient in the feed stream is not particularly limited. Indeed, the feed stream may contain only 1 weight. % of internal olefins. However, the method according to the invention is particularly well suited to large-scale industrial production of the compositions of linear alpha-olefins that are required for such applications, which are sensitive to the presence of branched alpha-olefins in amounts above about 3 wt.%. Accordingly, in the preferred embodiment of the invention the feed stream contains at least 2 wt.% the branched passage. The method according to the invention are mainly to separate the branched internal olefins, branched alpha olefins, and linear internal olefins from linear alpha-olefins.In many applications the presence of branching in the branched alpha-olefin in C2or3the position is undesirable. Therefore, to ensure the highest quality product in a very preferred embodiment of the invention the operation of the Department should be supplied on the flows of product, which contain the amount of 3 wt.% or more branched olefin whether the internal olefin or alpha-olefin, relative to the weight of the feed stream. However, the invention is not limited to the implementation stages of separation/purification for feed streams containing more than 3 wt.% branched olefins. The feed streams containing only 1 wt.% branched olefins or 1 wt.% branched alpha-olefins can also be successfully processed to further reduce the content of branched alpha-olefins, which is necessary for some applications (and even if it is not particularly necessary for the application). The need to process the supplied threads already with takeni, requiring pure compositions of alpha-olefins, can tolerate low levels of branched olefins.Typically, the feed stream product will not contain more than 85% wt. branched alpha-olefins relative to the weight of the feed stream, although the exact number will often vary depending on the method of obtaining a feed stream of a product, such as, for example, by oligomerization of ethylene or by way of Fischer-Tropsch. Usually, the number of branched alpha-olefins present in the feed stream will not exceed 50 wt.% relative to the weight of the feed stream. So more generally, the number of branched alpha-olefin in the feed streams ranges from 5 to 40 wt.%.The number of branched internal olefins in the feed stream is not limited. The feed stream may contain from 0 to 30 wt.% branched internal olefins, although the number in the range from 1 to 15 wt.% is usual.The number of linear internal olefins is not limited and can vary from 0 to 80 wt.%, when this number from 1 to 20 wt.% are normal.The number of linear alpha olefins in the feed stream may vary widely and Melanie less than 5 wt.% linear alpha-olefins, obtained in the method of separation may be economically disadvantageous. The feed stream should preferably contain at least 10 wt.%, more preferably at least 15 wt.% and most preferably at least 20 wt.% linear alpha-olefin. In cases where the feed stream get in the way of the Fischer-Tropsch process, the feed stream will typically contain less than 50 wt.% linear alpha-olefins.Other ingredients which may be present in the feed stream include aromatic compounds, waxes and oxidized compounds. These other ingredients may be present in the feed stream in quantities fluctuating in the range from 0 to 50 wt.%.Usually olefinic feedstock will have an average number of carbon atoms from 4 to 22, more preferably from 6 to 18. Physical properties, a requirement which is presented to the end-use of olefins, partially determine the appropriate number of carbon atoms for allocation. Olefins with carbon more than 22 and less than 6 can be used in this way, but from a commercial point of view the feed streams to the number of carbons from 6 to 18 will be used most often. For example, linear allenes, linear alpha olefins having a number of carbon 8-12, usually used to obtain poly-alpha-olefins and alpha-olefins having a number of carbon-12 to 18, are used as intermediate products in the manufacture of detergents.The linear polyaromatic compound used in the present method for the formation of adduct with alpha-olefins in the feed stream. Although not linking it to theory, it is assumed that the linear polyaromatic compound preferably forms an adduct with linear alpha-olefins and to a lesser extent, if any, forms, 2-branched alpha olefins. The preferred connection of the linear polyaromatic compound-linear alpha olefin relative to the branched alpha-olefins or internal olefins may be a result of spatial difficulties and/or electronic effects last olefins in the Diels-alder reaction.As used herein, "linear polyaromatic compound" refers to a linear polyaromatic compound having at least three condensed aromatic rings. Linearity should cover at least three or, when prisutstvie matichenkov compounds include anthracene, 2,3-benzanthracene, pentacene and exact. Unexpectedly it was found that the non-linear polyaromatic compounds such as 1,2-benzanthracene, failed to successfully separating linear alpha olefins from branched alpha-olefins.The linear polyaromatic compound may be substituted or unsubstituted. The term "linear polyaromatic compound" also refers to the pure compounds or compositions containing as one of its ingredients linear polyaromatic compound, including, but not limited to, markets tar containing linear polyaromatic compound butter linear polyaromatic compounds and any crude mixture containing fractions isolated from naphthalene.Suitable examples of substituents in the substituted linear polyaromatic compounds include, but are not limited to, lower alkali, for example methyl, ethyl, butyl; halogen, for example chlorine, bromine, fluorine; nitro; sulphate; sulfonyloxy; carboxyl; Carbo-lower alkoxy, for example, carbomethoxy, carboethoxy; amino; mono - and di-lower alkylamino, such as methylamino, dimethylamino, methylethylamine; amido; hydroxy; cyano; lower alkoxy, such as l, benzyl, etc., the Specific size of the Deputy, their number and their position should be chosen in such a way that they are relatively inert under the reaction conditions and relatively small in order to avoid spatial difficulties for the formation of adduct Diels-alder reaction.Preferred linear polyaromatic compounds are anthracene and 2,3-benzanthracene. Suitable substituted linear polyaromatic compounds may be determined by the conventional experiment. It was found that 9,10-dimethylanthracene, 9,10-dichloroanthracene, 9-methylanthracene and unsubstituted anthracene work quite well. Other suitable substituted anthracene include 9-acetylanthracene, 9-(methylaminomethyl)anthracene, 2-chloroanthracene, 2-ethyl-9,10-diethoxyanthracene, antrain and 9-antistreptolysin.In the linear polyaromatic compounds, one or more of the carbon atoms of the aromatic ring may be replaced by suitable polyvalent heteroatom. Example class heteroaromatics anthracene molecules is acridine and fenesin.Linear polyaromatic compounds include aromatic molecules, linked together bridging group, such as uglev what his invention is essentially a three-stage method, in which (a) linear polyaromatic compound interacts with the olefin composition with the formation of the adduct, (b) the adduct is separated from the reaction mixture, and (C) the adduct is decomposed with the release of olefin and regeneration linear polyaromatic compounds. The reaction of formation of adduct Diels-alder reaction carried out in the usual way and in the reaction zone. An example of a suitable reaction zone is a flow reactor with a stirrer, where the olefin and linear polyaromatic compound is continuously added to the tank with stirrer and the reaction mixture is continuously withdrawn from the tank with agitator. Alternatively, the reaction can be performed in a batch reactor, the where the olefin and linear polyaromatic compound is loaded into the autoclave which is then heated to a reaction temperature sufficient to complete the reaction. The reaction is usually conducted in the temperature range from 150 to 290oC, preferably from 200 to 280oS, and most preferably from 240 to 265oC. Pressure is not critical and typically ranges from about atmospheric pressure up to 10000 KPa. The reaction can be performed in the gas phase under vacuum or in the liquid phase or in a mixed gas-liquid f is and you can use the stoichiometric ratio or an excess of either the olefin, either linear polyaromatic compounds, but preferred is a molar excess of olefin. The molar ratio of olefin to the linear polyaromatic compound is preferably from more than 0.5:1 up to 10:1, more preferably from 1.5:1 to 7:1.For dissolving the source of olefins or linear polyaromatic compound or both in the reactor can be used an inert solvent. Preferred solvents are hydrocarbon solvents, which are liquid at reaktsionnykh temperatures and are soluble olefins, linear polyaromatic compound and the olefin adducts-linear polyaromatic compound. Illustrative examples of useful solvents include alkanes such as pentane, isopentane, hexane, heptane, octane, Noonan and the like; cycloalkanes, such as cyclopentane, cyclohexane and the like; and aromatic compounds such as benzene, toluene, ethylbenzene, diethylbenzene, and the like. The amount of solvent used may vary within a wide range without adversely affecting the reaction.However, in one embodiment of the invention the feed stream and education adduco detected, the absence of a solvent does not significantly affect the number of linear polyaromatic compounds regenerated under the same reaction conditions, and the concentration of the generated linear alpha-olefins is essentially the same. Thus, in the preferred embodiment of the method according to the invention is carried out in the absence of solvent.After the formation of the adduct of linear polyaromatic compound-olefin, it is separated from the reaction mixture. Adduct olefin-linear polyaromatic compound is separated from the reaction mixture by conventional means. Due to the large molecular weight and structure differences between adduct of linear polyaromatic compound-linear alpha-olefin and the remainder of the reaction mixture, the usual methods of separation are well suited for removal of unreacted olefin adduct linear polyaromatic compound-linear alpha-olefin. For example, unreacted olefins may be removed from the head rush or in the fractions by vacuum or single equilibrium distillation of the reaction mixture, so as to balance leave adduct of linear polyaromatic compound-linear alpha olefin and nepareiziem is how unreacted olefins, including branched and linear internal olefins, 2-branched alpha-olefins and/or 3-branched alpha olefins, and paraffins, aromatic compounds, alcohols, ketones, acids and other impurities can be removed. Alternatively, the adduct of linear polyaromatic compound-linear alpha olefin is separated by cooling the reaction mixture up until the adduct will not crystallized, followed by filtration or centrifugation to remove unreacted olefin. In most cases, unreacted linear polyaromatic compound is separated together with the adduct of a linear polyaromatic compound-linear alpha-olefin. The remainder of the reaction mixture can be used in other ways or applications, as it would have enriched the contents of internal olefins compared to the supplied stream.The next stage of this method is the decomposition of the adduct of linear polyaromatic compound-linear alpha-olefin. The decomposition process can be carried out by heating or pyrolysis of the extracted adduct of linear polyaromatic compound-linear alpha-olefin at a temperature of from 250oWith dot linear polyaromatic compounds. Then the linear polyaromatic compound is separated from the mixture by any appropriate methods that can be performed simultaneously with the operation of pyrolysis, such as by vacuum or single equilibrium distillation linear alpha-olefins, together with any impurities at temperatures of pyrolysis and remove the linear polyaromatic compound as a residue from the reactor for the decomposition of the adduct. Other methods of separation include filtration and centrifugation. The linear polyaromatic compound can be recycled back into the reaction zone of the adduct. Separated composition of linear alpha-olefin enriched in content of linear alpha olefin with respect to the content in the feed stream product, and the concentration of branched alpha-olefins in the composition of the linear alpha-olefin is reduced relative to the concentration of the feed stream.Although most of branched alpha-olefins to be separated from linear alpha-olefins, a small amount of branched alpha-olefins along with other impurities may be present in the composition of the linear alpha-olefin after only one pass. For many applications the number of branched alpha-ol is small, thus, you need only one passage in accordance with the method. However, if necessary, to further reduce the content of the branched alpha olefin and an additional increase in the content of the linear alpha olefin composition of linear alpha-olefins can undergo multiple passes through an additional reaction zone and a reactor for the decomposition of the adduct, which is composition of linear alpha olefin obtained in the previous pass. In the preferred embodiment of the method according to the invention is repeated more than once, more preferably 2-4 times.The number of branched alpha-olefins in the composition of linear alpha olefin is less than 4 wt.% after the implementation of the method according to the invention in relation to the feed stream of the product. Preferably, the number of branched alpha-olefins, especially number 2-branched alpha-olefin, in the composition of the linear alpha-olefin is 3 wt.% or less. When multiple passes of the content of branched alpha-olefins and particularly the number of 2-branched alpha-olefins can be reduced in the composition of the linear alpha-olefin to 3.0 wt.% or less, more preferably 2.0 weight. % or less, Nai is redstem the following embodiments and examples.Example 1.To illustrate the concept of the invention, the feedstock used the composition of the olefin having eight carbons. The number and types of raw materials and unsubstituted anthracene loaded into a Parr autoclave with a capacity of 100 ml, are shown below in table 1. Anthracene was loaded into the autoclave was purged three times with nitrogen and hermetically closed. The autoclave was placed in the dry box and purged with nitrogen feedstock was added to the autoclave together with 20 ml of dry purged with nitrogen toluene, except when more marked in table 1. The autoclave was tightly closed, removed from the dry box, placed in a heating jacket and heated to a predetermined temperature for a specified time. During the heating of the contents of the autoclave were stirred. Then, the autoclave was cooled to 20oC. Unreacted excess olefinic feedstock was removed by distillation from a mixture of the product. The remaining mixture of unreacted anthracene and adduct of anthracene-linear alpha olefin was then heated to 300-350oC for about 0.5 hour, during which adduct the anthracene-linear alpha olefin is decomposed on recycled anthracene and product alpha-olefin enriched content 1-esultate presented in table 1. The concentration of the species in the feedstock and in the resulting composition of linear alpha-olefin measured in molar percent. Conducted additional experiments to change the molar ratio of anthracene to the original raw materials, changes in reaction time, temperature changes, the reaction in the absence of a solvent and using multiple passes using the same previous methods.The results presented in table 1 show that the method according to this invention is 2-branched alpha olefins successfully separated from linear alpha-olefins. As can be seen from these results, the molar percent of 2-methyl-1-Gapanovich branched alpha-olefins are substantially reduced compared to the number contained in the feedstock, and the molar percentage of target linear alpha-olefin 1-octene, significantly increased compared with that in the feedstock.Comparison of experiments 2-5 also shows that increasing the reaction temperature or increasing the residence time also increases the conversion of anthracene with no significant effect on the reaction selectivity. Experience 8 shows that one hour residence time sufficient to reduce the number of them about a wide range of molar ratio of anthracene to the olefinic feedstock. Example 16 in which the quality of raw materials used olefinic products of the previous examples, marked as recycled composition of the feedstock. The amount of target linear alpha-olefin can be further increased by recirculatory initial product through the formation of adduct of anthracene-linear alpha-olefin and the decomposition of the adduct of anthracene-linear alpha olefin as described above. Very clean unbranched linear alpha-olefins can be obtained from multiple passes in the process.Example 2
In this example, the linear alpha-olefin, 1-octene, enrich from a low concentration of linear alpha-olefin to a very high concentration of linear alpha-olefins by repeating the method according to the invention in multiple passes using as a new source of raw materials of the product is pre-treated olefin. Use the same technique as in example 1, with the following features:
the amount of anthracene was to 0.108 mmol, the amount of olefin with each new passage was 0,212 mmol, reaction temperature throughout was 255oWith the time of reaction and original product directly from the previous pass. For a given step change process, therefore, the content of 2-methyl-1-Heptene decreased from 26.8 percent to approximately 0%, and the target linear olefin 1-octene, was enriched from 19.2 to 98.4%.Example 3
The examples in table 3 show that the olefinic feedstock containing linear alpha-olefins and alpha-olefins with methyl branching or 2-position (experiment 17) or in the 3-position (experiment 18) enriched the content of the linear alpha-olefin using the method according to this invention. Followed the same method as in example 1 with the following features: the reaction time for the formation of adduct of anthracene-linear alpha olefin was 1 hour, and the reaction temperature was 255oC.Example 4
The experiments in table 4 show that the substituted anthracene are similar unsubstituted anthracene to extract alpha-olefins from a feedstock containing branched alpha-olefins. Followed the same method as in example 1 under the reaction conditions shown in table 4.Example 5
As illustrated by the data of table 5, as a source of raw materials can be used a mixture of alpha-olefins having several different numbers of carbon atoms. E is ovali on to 0.108 moles of anthracene. The reaction time and temperature of formation of the adduct was 1 hour at 255oS, respectively. One entrance was converted olefinic feedstock containing 11% of 2-methyl-1-olefins and 89% of 1-olefins in the product, containing only 3% of unwanted 2-methyl-1-olefins and 97% of the target linear 1-olefins.Example 6
As the feed stream product used the composition of olefins containing eight carbon atoms. In a Parr autoclave with a capacity of 100 ml was loaded or 0.035 moles fed olefin stream having the composition specified in table 1 below, and 0,0175 of moles of 2,3-benzanthracene. The autoclave three times was purged with nitrogen and hermetically closed. The autoclave was placed in a dry box was added to the autoclave purged with nitrogen flow of product along with 20 ml of dry toluene and purged with nitrogen. The autoclave was tightly closed, removed from the dry box, placed in a heating jacket and heated to 255oC for 2 hours. The contents of the autoclave were stirred during heating. Then, the autoclave was cooled to 20oC. Unreacted excess olefin stream was removed by distillation from the mixture of the product. Then the remaining mixture of unreacted 2,3-benzanthracene and adduct of 2,3-benzanthracene-linear alpha-olefin of nagref-olefin decomposed on recycled 2,3-benzanthracene and product alpha-olefin, enriched content of 1-octene. This experience marked as experience 21.Repeating the same method used in experiment 21, except that the adduct-forming compounds used 1,2-benzanthracene. This experience marked as experience 22 (comparative).Such compositions of linear alpha-olefins experiments 21 and 22 were analyzed by gas chromatography. The results are presented in table 6. The concentration of the species in the feed stream and in the resulting composition of linear alpha-olefin measured in molar percent.The results presented in table 6 show that when using the method according to the invention 2-branched alpha olefins successfully separated from linear alpha-olefins and formed olefins stream enriched in linear alpha-olefine. As can be seen from the presented results, the molar percentage of branched alpha-olefins 2-methyl-1-Heptene, is significantly reduced compared to the number contained in the feed streams, and the molar percentage of target linear alpha-olefin 1-octene, is significantly increased relative to its content in the feed stream.Comparison of experiments 21 and 22 also indicates that h is flow, enriched in linear alpha olefins. 1,2-Benzanthracene does not form adduct with olefins. 1. A way of separating linear alpha olefins from mixtures thereof in the feed stream with an olefin having branching at the 2 - and/or 3-position, comprising: a) contacting the feed stream with one or more linear polyaromatic compounds having 3 or more condensed aromatic, optionally substituted ring, under conditions effective for the formation of the adduct of linear polyaromatic compound - linear alpha-olefin; (b) separating the adduct of linear polyaromatic compound - linear alpha olefin from the reaction mixture; (c) the decomposition of the adduct of linear polyaromatic compound - linear alpha olefin with the formation of the linear polyaromatic compounds and compositions of linear alpha-olefin and, optionally, (d) separating the linear polyaromatic compounds formed in stage (C), from the specified composition of linear alpha-olefin.2. The method according to p. 1, in which the linear polyaromatic compound is an anthracene or substituted anthracene.3. The method according to p. 1, in which the linear polyaromatic compound is the range of the flow is in contact with a linear polyaromatic compound at a temperature in the range of 150-290oC.5. The method according to any of paragraphs.1-4, in which the feed stream, the molar ratio of olefins to linear polyaromatic compound is more than 1:1 to 7:1.6. The method according to any of paragraphs.1-5, in which the adduct of linear polyaromatic compound - linear alpha olefin decompose by heating the adduct of linear polyaromatic compound - linear alpha-olefin to a temperature in the range of 250-400oC.7. The method according to any of paragraphs.1-6, in which the separation stage b) and/or d) perform vacuum or a single equilibrium by distillation.8. The method according to any of paragraphs.1-6, in which the separation stage b) and/or (d) carry out first cooling followed by filtration or centrifugation.9. The method according to any of paragraphs.1-8, in which the number of 2 - and/or 3-branched alpha olefins in the feed stream is 1-85 wt.%, the number of linear alpha-olefins is 5-97 wt.% and the average number of carbon atoms in the olefin feed stream is 4-22.10. The method according to any of paragraphs.1-9, in which stage (a) is repeated more than once.11. The method according to any of paragraphs.1-10, in which the feed stream is the result of the way Chania signs.
FIELD: regeneration of heat and extraction of impurities.
SUBSTANCE: the invention is pertaining to the method of regeneration of heat and extraction of impurities from the area of the heat-producing reaction in the fluidized flow, conducted for conversion into light olefins of oxygenates present in the flow of the oxygenate (oxygen-containing) raw. raw. The offered method includes the new system of a two-stage quick chilling intended for extraction at the first stage of water from the outgoing from the reactor flow and regeneration of heat of this flow for the purpose, at least, of the partial evaporation of the raw flow due to indirect heat-exchange between the oxygenated raw and the flow of the upper product of the first stage or the flow of recirculation of the first stage. The flow of purification being withdrawn from the first stage, contains the large share of impurities and the high-boiling oxygenates. In the second stage besides conduct extraction of water from the products flow containing light olefins, and produce the flow of the purified water, which requires only the minimum evaporation of the water for production of the water flow of the high degree purification. The method allows to concentrate the impurities in a rather small flow and ensures the significant saving of power and money resources at production of a flow of the vaporous raw guided into the area of realization of the heat-exchange reaction in the fluidized flow.
EFFECT: the invention ensures concentration of the impurities in a rather small flow and the significant saving of power and money at production of the flow of the vaporous raw directed into the area of realization of the heat-exchange reaction in the fluidized flow.
19 cl, 3 tbl, 4 dwg, 5 ex
FIELD: petrochemical processes.
SUBSTANCE: narrow-range hydrocarbon stock is fed into reaction-distillation tower at a level located between lower and upper tower parts to perform isomerization and disproportionation of hydrocarbons. Reaction mixture is maintained in vapor-liquid equilibrium state to concentrate lighter reaction products in vapor phase and higher ones in liquid phase by means of controlling temperature profile and in-tower pressure. Higher olefins are withdrawn as bottom product and lighter olefins from the top of tower.
EFFECT: increased yield of desired product.
41 cl, 4 dwg, 5 ex
FIELD: petroleum chemistry.
SUBSTANCE: claimed method includes oligomerization of one or more alpha-olefins with ethylene in presence of metal-containing catalytic system, using one or more bisaryl pyrimidine-MXa complex and/or one or more [bisaryl pyrimidine-MYpLb+]q- complex. Process is carried out at ethylene pressure less than 2.5 MPa.
EFFECT: method for production of target product of increased yield.
10 cl, 1 tbl, 3 dwg, 17 ex
FIELD: industrial organic synthesis catalysts.
SUBSTANCE: catalyst contains following active components: Pd (0.001-1%), Bi (0.001-5%), at least of Ag, Cu, Zn, K, Na, Mg, Ca, Be, Sn, Pb, Cd, Sr, Ba, Ra, Mn, Zr, Mo, and Ge (0.001-10%), and at least one of rare-earth metals deposited on porous inorganic carrier (the balance.). Catalyst is capable of selectively and rapidly hydrogenating strongly unsaturated hydrocarbons such as alkynes. Catalyst is suitable for industrial cracking process and is characterized by favorable long regeneration period, long service time, and low cost.
EFFECT: improved performance characteristics of catalyst at low cost.
23 cl, 5 tbl, 22 ex
FIELD: petroleum chemistry.
SUBSTANCE: 1,3-butadiene is exposed to telomerization with telogene of general formula H-X-Y-H, wherein X represents oxygen, sulfur, nitrogen or phosphorus; Y represents carbon, nitrogen or silicium; and X and Y optionally may have substituents according to valence thereof to form telomer of general formula H2C=CH-CH2-CH2-CH2-CH=CH-CH2-X-Y-H. Said telomer is hydrolyzed to 1-substituted 2-octene of formula H3C-CH-CH2-CH2-CH2-CH=CH-CH2-X-Y-H. Substituted 2-octene is splitted to produce 1-octene.
EFFECT: improved method for production of 1-octene.
28 cl, 4 ex
FIELD: organic chemistry.
SUBSTANCE: claimed method includes a) reaction of carbon monoxide and hydrogen in presence of effective amount of Fischer-Tropsch catalyst; b) separation of at least one hydrocarbon cut containing 95 % of C15+-hydrocarbons from obtained hydrocarbon mixture; c) contacting separated cut with hydrogen in presence of effective amount of hydration catalyst under hydration conditions; d) treatment of hydrated hydrocarbon cut by medium thermal cracking; and e) separation of mixture, including linear C5+-olefins from obtained cracking-product. Method for production of linear alcohols by oxidative synthesis of abovementioned olefins also is disclosed.
EFFECT: improved method for production of linear olefins.
12 cl, 3 tbl, 1 dwg, 2 ex
FIELD: industrial organic synthesis.
SUBSTANCE: before olefin-containing raw material is brought into contact with isomerization catalyst, one or several components of the raw material are subjected to preliminary treatment coming into contact with preliminary treatment material containing zeolite with pore size at least 0.35 nm. Initial olefin is, in particular, vinylidene olefin of general formula CH2=C(R1)R2, wherein R1 and R2 independently represent alkyl groups having at least 2 carbon atoms so that molecular structure includes at least one allyl hydrogen atom.
EFFECT: increased selectivity.
10 cl, 1 tbl, 11 ex
FIELD: organic synthesis catalysts.
SUBSTANCE: vinylidene olefin-containing starting material is brought into contact with isomerization catalyst consisting of molecule sieve in H form, which contains pore larger than 0.6 nm.
EFFECT: increased selectivity of catalyst.
12 cl, 1 tbl, 11 ex
FIELD: petrochemical processes.
SUBSTANCE: liquid olefin-containing feed stream is brought into contact with activated catalyst composed of basic metal oxides or essentially basic metal oxides under olefin isomerization conditions. Catalyst has original olefin isomerization activity and contains activity affecting admixture in amount not exceeding that which would lead to reduction in catalytic activity with a rate of about 0.075% of hourly conversion loss as measured under 1-butene-to-2-butene isomerization process conditions, said activity affecting admixture being on including sulfur, phosphorus, at least one transition metal, or combination thereof.
EFFECT: increased catalytic activity.
34 cl, 5 dwg, 3 tbl, 2 ex
FIELD: petrochemical processes.
SUBSTANCE: branched olefins from isomerization feedstock in the form of linear olefin/paraffin mixture containing 5 to 50% of linear olefins having 7 to 28 carbon atoms are obtained in the first isomerization stage, wherein carbon backbone of linear olefins in the isomerization feedstock is isomerized when in contact with isomerization catalyst, which is effective to isomerize carbon backbone in linear olefin blend to convert the latter into olefin blend, wherein average number of branches in molecule chain is at least 0.7, followed by second stage, wherein branched and linear molecules are separated, the former being essentially olefinic molecules and the latter olefinic and/or paraffin molecules. Resulting branched olefins are served as starting material for production of alcohols and alkylbenzenes.
EFFECT: enabled olefin branching control.
6 cl, 4 tbl, 3 ex
FIELD: petrochemical processes.
SUBSTANCE: invention relates to reducing hydrolysis in hydrocarbon streams including addition to hydrocarbon stream, containing a chloride compound hydrolysable at elevated temperature in presence of water to form hydrochloric acid, of an effective amount of treating agent, namely at least one superbasic metal salt complex and organoacid complexion reagent. The agent is added when temperature of stream is below temperature at which considerable hydrolysis chloride-containing compound can occur.
EFFECT: increased chloride-containing compound hydrolysis reduction efficiency to formation of minimum amount of hydrochloric acid.
16 cl, 5 dwg, 2 ex