Method of increasing yield of higher molecular weight olefins from lower molecular weight olefins (options)

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 Higher olefins are withdrawn as bottom product and lighter olefins from the top of tower.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

 

The technical field

The present invention relates to a controlled way to increase the yield of olefins of higher molecular weight of the essentially narrow band containing the lighter olefin hydrocarbons, which are served at some point in the reaction-distillation column (columns, which simultaneously carried out reaction and distillation), using different placement of the catalysts for the disproportionation and isomerization relative to the feed point of the narrow band containing the lighter olefin hydrocarbons. A controlled method includes maintaining the reaction mixture at equilibrium vapor/liquid separation of lighter products in the form of the top ring and collect the heavier reaction products in the form of a bottom liquid by maintaining a controlled temperature profiles and pressure in terms of a narrow range containing the lighter olefins hydrocarbons required range heavier registergui products - hydrocarbons of interest as the product obtained in the bottom liquid of the reaction-distillation column.

In addition, in the reaction-distillation column create at least one or more zones of contact of vapor-liquid for ameliorating the possible separation of lighter olefin - the reaction products and heavier olefins - reaction products, as well as the original registertimer hydrocarbons, and to reduce the cost of the process.

The level of technology

From prior art it is well known the use of metal catalysts for interaction/splitting and recombination (disproportionation) of molecules of hydrocarbons, which contain olefinic or double bonds connecting carbon atoms. This cleavage reaction and recombination of molecules of hydrocarbon double bonds leads to the production of molecules of hydrocarbon - olefins of different molecular weight, depending on the composition of the feedstock used and how the molecules of the raw materials used are double bonds, but not necessarily leads to a final product that represents a significant commercial interest.

For example, prior art well-known reaction of propylene to produce ethylene and butene, or, on the contrary, obtaining propylene from ethylene and butene in the presence of metal catalysts, the product of these reactions is the olefin, but this product - olefin is slightly different in value from the initial reagents. In addition, because these reactions are reversible, they are mainly to the achievement of equilibrium, that limits the yield of the required product. From the prior art known only to a liquid-phase reaction using a heterogeneous catalyst in a fixed bed, fluidized bed or moving layers as mainly controlled methods of achieving equilibrium mixtures registergui of the reactants and products.

Prior art also known attempts to use other adjustable parameters of the process, such as more time for these systems and higher temperature, in order best to achieve balance and to shift the balance in a more favorable direction towards the education necessary reaction products of disproportionation, but such attempts generally led to an increase in isomerization and formation of other by-products of the reaction, the presence of which is undesirable in the required product.

Some known prior art sources of information reveal the reactions with high selectivity and degree of conversion, using 1 - and 2-butene, with the receipt of ethylene, propylene, 2-pentene and 3-hexene using the reaction-distillation column in the presence of rhenium oxide as catalyst for the disproportionation. In accordance the with these sources of prior art catalyst is a substrate for distillation, what contributes to a phase shifting some light solids from the liquid phase. In these particular systems conversion and output increase, but the reaction leads to the production of ethylene and propylene as light products and only 2-pentene and 3-hexene as heavy products, which are slightly more valuable than the raw materials used for their production.

In accordance with the prior art, there are many reports on the methods and processes enhance the yield of olefins, the molecular weight of which lies in the middle range, through the interaction of molecules of olefins with a large number of carbon atoms with molecules of olefins containing a small number of carbon atoms, while the disproportionation and isomerization of such olefins. In accordance with this method as molecules of olefins with a large number of carbon atoms, and molecules olefins containing a small number of carbon atoms is kept in one common liquid phase, while the reaction process provide the opportunity to be near equilibrium, while receiving olefins, the molecular weight of which is in the range of medium-sized values, and which relate to the number of linear olefins of a number of detergents (C10-C16using as feedstock light (C4-C9 ) and heavy (C16-C20+) alpha-olefins. Some variants of these known prior art patents is even used to obtain a linear alcohols industrial values.

In these known from the prior art patents use the isomerization process, the result of which is the distribution for the position of double bonds in the molecules of olefins, which opens the possibility of obtaining more olefins are useful in the case when it is necessary to obtain olefin some detergents having a molecular weight of medium range, based on light and heavy alpha olefins and internal olefins (i.e., in which the double bond is located inside the molecule, and not at its end). In such single-phase reactions in the liquid phase typically use a catalyst, such as potassium, cesium or rubidium, in order to promote isomerization to change the position of double bonds between the carbon atoms to obtain a wider range of internal olefins, which are able to interact with the formation of olefins having a molecular weight average in the range.

In addition, the prior art knows many ways, the implementation of which is used as isomerization catalysts, and catalysts disprop is lonilove for interaction in a single liquid phase, at elevated temperature and elevated pressure, in order to try to obtain the necessary range of products for use as various registertimer hydrocarbons, but the success of these attempts is limited due to the equilibrium nature of the process and a wide range of molecular masses mixed with each other registergui hydrocarbons, which requires additional processing to separate desired narrow range from lighter and heavier registertimer hydrocarbon feedstock and reaction products.

According to the prior art metal catalysts are used only for the disproportionation and isomerization, either individually or in a mixture, but without distinguishing where the catalysts relative to the input location specified raw materials, and what catalyst should be used initially for the reaction with the feedstock. Thus, in order to implement known from the prior art methods is to obtain olefin double bond, the most deeply located inside the molecule, as in the case of light and heavy molecules, before or in the process of disproportionation, including internal olefins with symmetrical location of the double bond. This edge is not desirable in the case when the goal is the synthesis of hydrocarbon molecular weight medium range containing olefinic bond, but not in the case of obtaining registergui hydrocarbons of higher molecular weight from registergui of hydrocarbons of lower molecular weight, where specifically required education asymmetric olefins.

The purpose of the present invention

The aim of the present invention relating to the method is the increase in the yield of olefins of higher molecular weight when using the essentially narrow band containing the lighter olefin hydrocarbon in the reaction-distillation column containing metal catalysts under controlled temperature and pressure to effect the interaction of a narrow range containing the lighter olefin hydrocarbons with achievement with the increased output of heavier olefins. In accordance with the method of interaction containing the lighter olefin hydrocarbons with achievement with the increased output of heavier olefins, is the removal of lighter hydrocarbons containing olefinic bond, and other light hydrocarbons.

To implement the method according to the present invention is to achieve a high yield of heavier olefins used without the I high temperature and/or longer stay in system, used for the implementation of such methods to reduce the formation of unwanted side products, the presence of which is undesirable in the desired product, and which can interfere with obtaining the necessary heavier olefins or reduce their output.

Another aim of the method according to the present invention is to shift the reaction equilibrium towards formation containing heavier olefin hydrocarbons in the interaction easier registertimer hydrocarbons using metal catalysts and then monitoring the pressure and temperature in order to allow to pass into the vapor phase most unwanted light olefins and other light products resulting from reaction with a metal catalyst, to remove from the reaction-distillation vessel in the top of a shoulder strap.

Also for the implementation of the method according to the present invention is to provide opportunities to interact with even the lightest leinstermen raw materials, such as 1 - and 2-butene and propylene, with metal catalysts under controlled temperature and pressure process for more valuable and more difficult registergui hydrocarbon products, such as5-C10that have significantly bol is Shui cost, than products, representing a 2-penten and 3-hexene.

The purpose of the method which is the subject of the present invention is, in addition, to provide heavier olefins from a narrow range containing the lighter olefin hydrocarbons with subsequent transfer to a narrow range of received heavier olefins to the next stage with the receipt still heavier olefins.

Another goal of the development of the method according to the present invention is the use of the isomerization process, in order to regulate the position of the olefinic double bond so that it is in the molecules of olefin mainly occupied asymmetric position, followed by disproportionation of carbon-containing molecules, where the molecule is effectively "cut" at the double bond, and asymmetric recombination of fragments with other molecules of olefin subjected to disproportionation with getting more heavy molecules olefins and light olefin molecules and then the isomerization of these heavier molecules olefins and again followed by disproportionation. After making all the disproportionation according to the present way more unwanted light registereda hydrocarbons are removed by transferring proobraz the second phase, leaving again heavier olefins for further isomerization on the following stages, as long as the process will not lead to obtaining the necessary heavier olefin products.

The aim of the present invention is also the use of catalysts as isomerization and disproportionation with registertask hydrocarbon feedstock and reaction products in vapor and liquid phase at relatively low temperature and pressure to obtain the required range of end - products-heavier olefins.

Additionally, the present invention is the availability of at least one zone of contact of vapor-liquid in order to facilitate the compartment containing the lighter olefin hydrocarbons and the collection of heavier olefins, either in the form of the final product or for further interaction in the reaction-distillation column.

Also the aim of the present invention is the selection of the type of catalysts and their location as a pre-defined point for the initial impact on containing light olefins, hydrocarbons, depending on the degree of symmetry or lack of symmetry of the location of double bonds in the containing light olefins hydrocarbons, which serves to pre-determine lannou point of the reaction-distillation column.

Other and further advantages and improvements of the method which is the subject of the present invention, will be taken into account by the experts in the art, and such advantages and improvements of the invention will be clear to experts in the art after reading and understanding the following detailed description and schematic drawings.

Brief description of drawings

The method which is the subject of the present invention may be implemented is described in this application certain physical forms and devices, and by adjusting some parameters of the individual parts, but will be later in the present description are described in detail and illustrated by the accompanying schematic drawings, which constitute part of the description, the preferred embodiment.

Figure 1 presents a schematic drawing of the reaction-distillation column used for implementing the method of the present invention, using a narrow range containing the lighter olefin hydrocarbon feedstock with a number of carbon atoms With5and above, which is injected into the reaction-distillation column at a predefined point, using an isomerization catalyst, located near previously about the certain point of entry of raw materials, and the catalyst for the disproportionation located instead of the layers of the isomerization catalyst alternately with him, and when using at least one zone of the vapor/liquid created in the upper part of the reaction-distillation column designed to obtain olefins with the number of carbon atoms from C6to C10.

Figure 2 presents a schematic drawing of the reaction-distillation column used for the implementation of the method according to the present invention using a narrow band containing the lighter olefin hydrocarbon feedstock with a number of carbon atoms from C6to C10and an even greater number of carbon atoms, with the specified raw material is introduced into the reaction-distillation column at a predefined point when using an isomerization catalyst in proximity to the predefined insertion point of the feedstock and catalyst for the disproportionation located instead of the layers of the isomerization catalyst alternately with him, and when using at least one zone of the vapor/liquid created in the upper part of the reaction-distillation column designed to obtain olefins with the number of carbon atoms With10and more.

Figure 3 presents a schematic drawing of the reaction-distillation column, before aznacenni for implementing the method of the present invention using a range containing the lighter olefin hydrocarbon feedstock with a number of carbon atoms from C 3to C4and specified raw material is introduced into the reaction-distillation column at a predefined point when using the catalyst for the disproportionation located near a predefined insertion point of the feedstock and catalyst for isomerization, located instead of layers of catalyst for the disproportionation alternately with him, using at least one zone of the vapor/liquid created in the upper part of the reaction-distillation column designed to obtain olefins with the number of carbon atoms from C5to C10.

Figure 4 presents a schematic drawing of consecutive reaction-distillation columns connected together and designed to use the original range contains more light olefin hydrocarbon feedstock with a number of carbon atoms from C3to C4with the receipt of olefins with a large number of carbon atoms through the supply of products from the bottom of the column sequentially from the first to the second column, and then in the third reactive distillation column.

Description of the preferred embodiment of the invention

The present invention relates to a method of increasing the yield of heavier olefins by using the creature is but a narrow range containing the lighter olefins source of hydrocarbons, served in the reaction-distillation column, usually when referenced, denoted by the number 10. In accordance with at least one embodiment, as shown in figure 1, the implementation of the method which is the subject of the present invention, begins with the filing essentially narrow band containing the lighter olefins source of hydrocarbons, with the number of carbon atoms from C6and above, in a reaction-distillation column 10 in a predefined insertion point of the feedstock 11 of the reaction-distillation column 10. Near a predefined insertion point of the feedstock 11 is located isomerization catalyst 14 intended for isomerization source registertimer hydrocarbon material as it passes through the reaction-distillation column 10. As shown in figure 1, the isomerization catalyst 14 can be positioned near a predefined insertion point of the feedstock 11, and directly above and below the predefined insertion point of the feedstock 11 for the first isomerization source registertimer hydrocarbons as fully as possible. Thus, in accordance with this preferred embodiment of the invention predefined insertion point of the feedstock 11 buderusplatz on the reaction-distillation column and is intended for in order to initially direct the filing of the original registertimer hydrocarbons in the reaction-distillation column 10 between the zones of the isomerization catalyst 14. Isomerization of the olefin, as known to a person skilled in the art means that the double bond located between carbon atoms, which characterize the olefin will be moved from one pair of carbon atoms to the other pair of carbon atoms, with the aim of obtaining mainly molecule of olefin, which is asymmetric, provided that the molecule of the olefin contains 5 or more carbon atoms. After the initial registersee hydrocarbons were subjected to isomerization, give him the opportunity to move to a catalyst for the disproportionation 15 for the disproportionation already past isomerization source registertimer hydrocarbons. In accordance with this preferred embodiment of the invention the catalyst for the disproportionation may be located above and below the isomerization catalyst 14. Such placing of the catalysts can be either hosted in a separate pallets or molecular mixture of catalysts, which are created in the form of their mixtures. Disproportionation of olefins, as is known to the person skilled in the field of technology means that is castle olefinic communication registertimer hydrocarbon process of splitting and recombination obtained by cleavage fragments with other obtained by cleavage fragments of other olefins, which was subjected to disproportionation at the same time, obtaining the result as olefins, higher molecular weight, and olefins of smaller molecular weight. In accordance with this preferred embodiment of the invention in the case of the location of the catalyst in the disproportionation 15 above and below the isomerization catalyst 14, olefins, after they were subjected to isomerization, are moved in the reaction-distillation column in order to undergo disproportionation, as shown in figure 1.

Next, as shown in figure 1, at least according to this embodiment of the invention provides alternate implementation stages of the disproportionation and isomerization registertimer hydrocarbons, after its initial filing in a predefined insertion point of the feedstock 11 of the reaction-distillation column 10 and its primary isomerization. This alternation stages of the process of disproportionation and isomerization specified registertimer hydrocarbons will continue depending on the size of the reaction-distillation column 10, but usually as a last stage of the process will have a phase disproportionation before reaching a bottom part 18 of the reaction-distillation column 10.

Specialistov the art will understand, there are many catalysts and methods for their preparation in the reaction-distillation column 10, but in accordance with this preferred embodiment of the invention, the disproportionation catalysts are selected from the group including metals molybdenum, tungsten, cobalt, and rhenium and their oxides, either individually or in combination, and applied on a porous carrier. For example, according to the preferred embodiment of the invention using the catalyst for the disproportionation selected from the group of heavy metals, which contains the oxides of tungsten or rhenium deposited on a porous media containing aluminium oxide or silicon dioxide. A porous carrier containing alumina or silicon dioxide, used in accordance with this embodiment of the invention is a gamma-alumina or silica - alumina, catalytic purity, but can be used for any other substrate that would be effective in the manufacture of a catalyst suitable for the reaction with olefins, and which does not contradict the essence of the present invention.

Some of the common methods of preparation of catalyst for the disproportionation include dry blending, impregnation or coprecipitation. In accordance with one of preferred embodiments of the present image is etenia get the solution, containing salt water rhenium or rhenium oxide and/or salt water of the tungsten or tungsten oxide. After getting it added to the carrier - aluminum oxide, which may be in the form of a conventional distillation bulk packing, such as saddles, rings, spheres, to improve mass transfer and increase reactive surface during disproportionation and fractionation or separation in the extent to which it meets the operational parameters. After impregnation the catalyst may be calcined at a temperature from 300 degrees Celsius to 700 degrees Celsius in the flow of air and/or nitrogen to activate the catalyst. According to one of preferred embodiments of the invention disproportionation catalyst contains from 5 to 20% by weight of rhenium, or from 5 to 35% tungsten.

Also, as will be clear to a person skilled in the field of technology, there are many catalysts and methods of preparation of the catalyst used in the reaction-distillation column 10, but according to this preferred embodiment of the invention, the catalysts are selected from the group of alkali metals such as sodium, potassium, rubidium or cesium, either individually or in combination with each other, and then applying to the medium - alumina. For example, as a catalyst can be used is s carbonates, chelates, hydroxide, alcoholate and other compounds, if they can be subjected to decomposition with the release of while on the surface some form of oxides of metals, intended for reaction with olefins. In accordance with a preferred embodiment of the present invention may be used metals contained in the potassium carbonate and/or potassium carboxylates, but after they were deposited by impregnation on the surface, they should be activated by calcination at a temperature of from 400 degrees Celsius to 800 degrees Celsius in the air stream. In at least one of the embodiments of the invention, the isomerization catalyst is an alkali metal on a carrier - aluminium oxide is from 5 to 20% by mass.

In figure 1, depicting the reaction-distillation column 10 also shows the area of contact of vapor-liquid 16, which is located in the upper part of the reaction-distillation column 10 and is intended to ensure contact of the vapor/liquid separation of lighter reaction products from the heavier registertimer of the processed material. This area contacting vapor/liquid 16 may consist, as shown for this embodiment of the invention, multiple zones of structured packings or plates located in the upper zone of the upper part 17 of the reaction-distillation column 10. the specified point registersee hydrocarbon feedstock is subjected to both isomerization, and disproportionation with getting both heavier and lighter products, and products of approximately the same molecular weight as the original raw material. The advantage of using at least one zone of contact of vapor-liquid 16 is to increase the degree of fractionation or separation of lighter olefins, which are products of the reaction, and heavier olefins, which are reaction products derived from the original registertimer hydrocarbons in the reaction-distillation column 10. This is of particular value for the top of the column, where the reaction is inhibited under the influence of lower temperatures, and light substances evaporate, which prevents recombination with other reagents. The specified removal of lighter substances thus shift the equilibrium transformation towards education more severe registergui hydrocarbons. These light olefins, which are the reaction products are then removed along the line of the upper ring 19 located in the upper part 13 of the reaction-distillation column 10.

Variables are characteristics of the process such as temperature and pressure in the reaction-distillation column 10, used in the practice of implementation of the present invention, vary and depend on the source olefins the holding of hydrocarbons and the degree of conversion, necessary to achieve the required conversion and selectivity. Typically, the temperature range will be from -50 degrees Fahrenheit to 200 degrees Fahrenheit in the upper part 13, where the lighter olefin - reagents are removed along the line of the upper ring 19. In the lower part 12 of the reaction-distillation column 10, where the heavier olefin products of the interaction are removed by line 20 from a bottom part 18, the temperature range will be from 200 degrees f to 600 degrees Fahrenheit. Pressure typically varies in the range from -14,5 pound/square inch (excess.) up to 250 pounds/square inch (excess.), but also will vary depending on the desired process temperature in order to achieve the desired conversion and selectivity to the desired olefin product. Variables are characteristics of the process will require a specialist in this field equipment carrying out the invention, conducting some experiments with the values of these variables at the intervals specified in the present description, in order to optimize the values of these variables depending on the source registertimer hydrocarbons and the necessary parameters of the product. How you can adjust these variables are characteristics of the process, the specialists in this field the minute technology will be more clear from the following examples, illustrating the invention.

According to example 1, using the scheme shown in figure 1, essentially a narrow range containing the lighter olefins source of hydrocarbons, representing a mixture, which mainly contains compounds With5With6and heavier, served in the reaction-distillation column 10, the predetermined point 11. This raw material undergoes isomerization and disproportionation under the action of the isomerization catalyst 14 and the catalyst for the disproportionation 15, respectively, and then further subjected to sequential treatment with appropriate catalysts. Variables are characteristics of the process in accordance with this example are: -20 pound/square inch (excess.), + or -10 pound/square inch and a temperature of 40 degrees Fahrenheit or -40 degrees Fahrenheit in the upper part 13. In a bottom part 18 in the lower part 12 of the reaction-distillation column 10 variables support at 400 degrees Fahrenheit + or -100 degrees Fahrenheit. Received at the specified temperature and pressure, the product is collected in a bottom part 18 with the subsequent removal required heavier olefins of the following composition, wt.%:

C63,1
C718,3
C861,7
C913,2
C102,5
C111,1

and thus, heavier olefins, essentially from C6to C10.

According to example 2, using the scheme shown in figure 1, essentially a narrow range containing the lighter olefins source of hydrocarbons, representing a mixture, which mainly contains compounds With5With6and heavier, served in the reaction-distillation column 10 shown in figure 1, in a pre-defined point 11. This raw material undergoes isomerization and disproportionation under the action of the isomerization catalyst 14 and the catalyst for the disproportionation 15 and then further subjected to sequential treatment with appropriate catalysts. Variables are characteristics of the process in accordance with this example are: -20 pound/square inch (excess.) + or -10 pound/square inch and a temperature of 40 degrees Fahrenheit + or -40 degrees Fahrenheit in the upper part 13, while the lower part 12 of the reaction-distillation column 10 temperature reboiler support at 350 degrees Fahrenheit + or -100 degrees Fahrenheit. Received at the specified temperature and pressure of the product with eraut in the bottom liquid 18 for subsequent removal required heavier olefins of the following composition, wt.%:

C5the 4.7
C6a 38.5
C738,2
C818,6

receiving, thus, slightly different heavier olefins, essentially from C6to C10.

According to example 3, using the scheme shown in figure 2, essentially a narrow range containing the lighter olefins source of hydrocarbons, representing a mixture, which mainly contains5until10and heavier, served in the reaction-distillation column 10 at the point of supply of raw materials 11. These raw materials are immediately subjected to isomerization and disproportionation under the action of the isomerization catalyst 14 and the catalyst for the disproportionation 15 and then further subjected to sequential treatment with appropriate catalysts. Variables are characteristics of the process in accordance with this example are: 10 pound/square inch + or -10 pound/square inch and a temperature of 40 degrees Fahrenheit + or -40 degrees Fahrenheit in the upper part 13, while the lower part 12 of the reaction-distillation column 10 temperature reboiler support at 400 degrees Fahrenheit + or -100 degrees Fahrenheit. Received the ri indicated temperature and pressure, the product is collected in a bottom part 18 for subsequent removal required heavier olefins of the following composition, wt.%:

C8of 3.77
C920,16
C1034,97
C1125,1
C1210,37
C13a 3.87
C142,16
C150,59

receiving, thus, differs only slightly heavier olefins essentially from6to C20.

According to example 4, using the scheme shown in figure 2, essentially a narrow range containing the lighter olefins source of hydrocarbons, representing a mixture, which mainly contains5until10and heavier, served in the reaction-distillation column 10, as shown in figure 2, at a predefined point 11. These raw materials are immediately subjected to isomerization and disproportionation under the action of the isomerization catalyst 14 and the catalyst for the disproportionation 15 and then further subjected to sequential treatment with appropriate catalysts. Variables are characteristics of the process in accordance with this example are: in the upper part 13 of the column, as a rule, a 10 pound/square inch (excess.) + or -10 lb/RMS is fair inch, and the temperature is 40 degrees Fahrenheit + or -40 degrees Fahrenheit, while in the lower part 12 of the reaction-distillation column 10, where the reboiler temperature is 450 degrees Fahrenheit + or -100 degrees Fahrenheit. Received at the specified temperature and pressure, the product is collected in a bottom part 18 for subsequent removal required heavier olefins of the following composition, wt.%:

C70,2
C81,0
C96,6
C1016,4
C1123,5
C1221,4
C1314,3
C148,3
C154,2
C162,0
C170,9
C180,4

receiving, thus, slightly different heavier olefins essentially from10to C20.

In accordance with this method, the yield of heavy products (C6with higher molecular weight), as I believe, is in the range from 20% to 80% by weight, more preferably from 50% to 75% is about the mass. Most preferably, the yield of heavy products will be 70% by mass. As shown above, the composition of the product can be adjusted or changed by variation of characteristic variables - temperature and pressure in the reaction-distillation column.

In at least one embodiment of the present invention, as shown in figure 3, the implementation of the method which is the subject of the present invention, beginning with the filing essentially narrow band containing the lighter olefins source of hydrocarbons containing From3and C4where4consists at least partially of 1 - and 2-butene in the reaction-distillation column 10, the predetermined point 11 located between the bottom 12 and top 13 of the reaction-distillation column 10. In accordance with this embodiment of the invention the products of the reaction are ethylene, propylene and a number of 2-butene, which are selected using the top line of a shoulder strap or top of the thread 19 of the upper part 13 of the reaction-distillation column 10, as well as connections from5to C10that is withdrawn from the bottom of the liquid 18 in the lower part 12 of the reaction-distillation column 10 via line 20. In accordance with this embodiment of the invention the catalyst for the disproportionation 15, with Ugadi for the disproportionation registertimer hydrocarbon material as it passes through the reaction-distillation column 10, have near a predetermined point 11. As shown in figure 3, the catalyst for the disproportionation 15 will be located as near to a predetermined point of supply of raw material 11, and directly above and below the point of feed of the raw material 11 for the implementation of primary disproportionation source registertimer hydrocarbons as fully as possible. Thus, in accordance with this preferred embodiment of the invention predefined insertion point of the feedstock 11 is placed on the reaction-distillation column and is intended to carry out the initial filing of the original registertimer hydrocarbons directly in the reaction-distillation column 10 between the zones of the catalyst for the disproportionation 15. After the initial registersee hydrocarbons will undergo disproportionation, give him the opportunity to move to the isomerization catalyst 14 for isomerization already past disproportionation registertimer hydrocarbons. In accordance with this described preferred embodiment of the invention, the isomerization catalyst 14 may be located above and below the catalyst for the disproportionation 15 to facilitate isomerization product re the functions, which is obtained by using the catalyst for the disproportionation 15. In accordance with this embodiment of the invention the catalyst for the disproportionation 15 place for the primary interaction with the source registertask hydrocarbons at least for the reason that the raw materials, which contains compounds With3and C4where4consists at least partially of 1 - and 2-butene, may be subjected to isomerization only with the formation of predominantly 2-butene, and this leads to the production of 2-butene in the case where the raw material is subjected to disproportionation by using a catalyst for the disproportionation 15. After the feedstock is initially subjected to disproportionation by using a catalyst for the disproportionation 15, some of the products obtained will have a molecular weight and symmetry, which in the isomerization of these products using an isomerization catalyst 14 will lead to the desired product and other products of the reaction are smaller molecules, which will then be transferred into the vapor phase fractionation or separation of these lighter olefins and other light reaction products from the heavier olefin products of the reaction-distillation columns is e 10. According to the embodiment of the invention shown in figure 3, is provided in the following alternation of stages of the method of the disproportionation and isomerization after this initial phase disproportionation according to the reaction-distillation column 10 continue the implementation phase of the way - disproportionation and isomerization, with final completion stage of the disproportionation before the final product that represents a connection from5to C10will be included in the cubic liquid 18 in the lower part 12 of the reaction-distillation column 10.

In accordance with example 5 with the implementation of the method according to the scheme shown in figure 3, using essentially narrow band containing the lighter olefins source of hydrocarbons obtained from olefins With3and C4and when variables are characteristics of the way that the upper part 13 of the reaction-distillation columns are usually 100 pounds/square inch (excess.) + or -80 lbs/square inch and a temperature of 100 degrees Fahrenheit + or -50 degrees Fahrenheit, while in the lower part 12 of the reaction-distillation column 10, where will be located the reboiler temperature is 300 degrees Fahrenheit + or -100 degrees Fahrenheit. Obtained is at the specified temperature and pressure, the product is collected in a bottom part 18 for subsequent removal as required heavier olefins, which are a mixture of the following composition, wt.%:

C48,15
C546,21
C626,92
C713,31
C81,69

and thus, heavier olefins essentially from5to C-10.

As will be clear to experts in the art, all disclosed above methods, the method can be implemented in a single reactive distillation column or in a series of consecutive columns, as shown in figure 4, when using contains more light olefins source of hydrocarbon feedstock containing olefins With3and C4for more severe registertimer hydrocarbon, which is essentially a14and products with a higher molecular weight, which will not contradict the essence of the present invention. Obviously, if all the methods, the method to merge with the implementation of the method in the same column, it is necessary at each stage to maintain variables characteristics of the method, the structure of the reaction-distillation column 10, as shown, may be different, but the methodology is sushestvennee method will be the same equivalent processes. Figure 4 shows the consistent implementation of the method using multiple columns, where the first stage is in the General form shown at number 21, and, as a rule, is a way that illustrates figure 3, the second stage in the General form shown at number 22, and, as a rule, is a method, which is illustrated by figure 1, and the third stage in the General form shown at number 23, and, as a rule, is a way that illustrates figure 2.

Specialists in the art will also understand that although according to the above-described methods, the method using linear olefins described above can also be used for extensive registergui hydrocarbons and for the mixed method, according to which use both linear and branched olefins. In the case when you want a mixture containing a branched olefins and linear olefins in a certain percentage, then the feedstock is a mixture of hydrocarbons containing olefins, branched-chain, can be adjusted by adding linear registergui hydrocarbons in order to achieve the required percentage of branched-chain olefin in the final product obtained in accordance with the method of the present invention.

Although described the most is her preferred embodiment of the method according to the present invention and their use to enhance the yield of olefins of higher molecular weight when using feedstock essentially narrow band containing the lighter olefin hydrocarbon in the reaction-distillation column, it will be clear that the method can be used in other embodiments of the invention and other values of the variables of ways without deviating from the essence of the claimed invention, that is described by the following formula method.

1. The method of increasing the yield of heavier olefins from essentially a narrow range containing the lighter olefin hydrocarbon in the reaction-distillation column, including

the supply is essentially a narrow band containing the lighter olefin hydrocarbon with the carbon atoms C5and more in the reaction-distillation column at a predefined point specified reactive distillation columns,

isomerization specified contains more light olefins hydrocarbons using a catalyst isomerization near the specified pre-defined point of feed of the specified essentially narrow band containing the lighter olefin hydrocarbons in the specified reaction-distillation column

disproportionation specified contains more light olefins hydrocarbons using catalysate is RA disproportionation education while containing heavier and lighter olefins hydrocarbons

ensuring the availability of at least one zone of contact of vapor-liquid for best separation of these heavier and lighter registergui hydrocarbons

the pressure is within the specified reaction-distillation column, allowing a very efficient return of olefins with the lowest molecular weight among these desirable olefins of higher molecular weight specified in the lower part of the specified reactive distillation columns and provides high conversion containing light olefins, hydrocarbons,

maintaining in the upper part of the specified reaction-distillation column temperature sufficient to remove the most serious of these undesirable olefins with a small molecular weight as the head of a ring taken from the top of the specified reaction-distillation column, and

maintaining specified in the lower part of the specified reaction-distillation column temperature sufficient to ensure the provision of most of these light olefins from among these desirable olefins of higher molecular weight specified in the lower part of the specified reaction-distillation column and to maintain the temperature about the Ile in a specified reaction-distillation column, providing a sufficiently high reaction rate throughout the specified reactive distillation columns.

2. The method of increasing the yield of heavier olefins from essentially a narrow range containing the lighter olefin hydrocarbon in the reaction-distillation column according to claim 1, further comprising interleaving stages of the method of the disproportionation and isomerization specified contains more light olefins hydrocarbons.

3. The method of increasing the yield of heavier olefins from essentially a narrow range containing the lighter olefin hydrocarbon in the reaction-distillation column according to claim 2, according to which the specified availability of at least one zone of contact of vapor-liquid for the separation of these heavier and lighter olefins has specified at least one zone of contact of vapor-liquid in a specified reaction-distillation column to improve the separation of these unwanted light olefins in the form of a ring - vapor phase taken from the top of the column, and these heavier olefins in the liquid phase - the bottom fluid in the specified reactive distillation column.

4. The method of increasing the yield of heavier olefins from essentially a narrow range soderjaschegosya light olefin hydrocarbon in the reaction-distillation column according to claim 3, under which these successive isomerization and disproportionation specified contains more light olefins hydrocarbons optionally include the location of these catalysts for the isomerization and disproportionation of alternating portions in the specified reactive distillation column.

5. The method of increasing the yield of heavier olefins from essentially a narrow range containing the lighter olefin hydrocarbon in the reaction-distillation column according to claim 4, whereby the addition of these catalysts for the isomerization and disproportionation of alternating portions specified in the reaction-distillation column further includes the location of these catalysts for the isomerization and disproportionation of alternating layers in the specified reactive distillation column.

6. The method of increasing the yield of heavier olefins from essentially a narrow range containing the lighter olefin hydrocarbon in the reaction-distillation column according to claim 5, according to which the specified isomerization catalyst comprises a catalyst consisting of a metal selected from the group consisting of sodium, potassium, rubidium and cesium, impregnated and coated on the substrate.

7. The method of increasing the yield of heavier olefins from su is estu narrow range containing the lighter olefin hydrocarbon in the reaction-distillation column according to claim 6, according to which the specified isomerization catalyst consisting of a metal, further includes a catalyst consisting of a metal selected from the group consisting of sodium, potassium, rubidium and cesium or mixtures thereof, impregnated and coated on the substrate.

8. The method of increasing the yield of heavier olefins from essentially a narrow range containing the lighter olefin hydrocarbon in the reaction-distillation column according to claim 7, according to which the specified disproportionation catalyst comprises a catalyst comprising a heavy metal selected from the group consisting of rhenium, tungsten or molybdenum, impregnated and coated on the substrate.

9. The method of increasing the yield of heavier olefins from essentially a narrow range containing the lighter olefin hydrocarbon in the reaction-distillation column of claim 8, according to which the specified disproportionation catalyst comprises a catalyst consisting of a heavy metal selected from the group consisting of rhenium, tungsten or molybdenum or mixtures thereof, deposited by impregnation on the substrate.

10. The method of increasing the yield of heavier olefins from essentially a narrow range containing the lighter olefin hydrocarbon in the reaction-distillation column according to claim 9, according to which the specified filing of decree of the aqueous essentially narrow band containing the lighter olefins hydrocarbons involves feeding a mixture, essentially, C5With6and heavier registertimer hydrocarbons in the reaction-distillation column in the specified predefined point specified reactive distillation columns.

11. The method of increasing the yield of heavier olefins from essentially a narrow range containing the lighter olefin hydrocarbon in the reaction-distillation column of claim 10, whereby the specified pressure is within the specified reaction-distillation column includes maintaining the specified pressure in the upper part of the specified reactive distillation column in the range from -10 pound/square inch (wt.) up to 200 pounds/square inch (wt.).

12. The method of increasing the yield of heavier olefins from essentially a narrow range containing the lighter olefin hydrocarbon in the reaction-distillation column according to item 11, according to which the specified pressure is within the specified upper part of the specified reaction-distillation column includes maintaining the specified pressure in the upper part of the specified reactive distillation column in the range from 5 pounds/square inch (wt.) to 125 pound/square inch (wt.).

13. The method of increasing the yield of heavier olefins from essentially a narrow range containing light olefins, coal is dorodnova raw materials in the reaction-distillation column according to item 12, additionally comprising maintaining a specified temperature at a specified lower part of the specified reactive distillation column in the range from 100 to 500°F, maintaining the specified temperature specified in the upper part of the specified reactive distillation column in the range from 0 to 100°F.

14. The method of increasing the yield of heavier olefins from essentially a narrow range containing the lighter olefin hydrocarbon in the reaction-distillation column according to item 13, whereby for a given feed containing light olefins hydrocarbons, including C5With6and compounds with a higher number of carbon atoms, the method further includes obtaining a heavier olefins, essentially from C6to C10with the release of at least 60 mass%.

15. The method of increasing the yield of heavier olefins from essentially a narrow range containing the lighter olefin hydrocarbon in the reaction-distillation column according to claim 9, according to which the specified feedrate specified essentially narrow band containing the lighter olefins hydrocarbons involves feeding a mixture essentially from C6to C10in the reaction-distillation column in the specified predefined point specified reaction-distillation the columns.

16. The method of increasing the yield of heavier olefins from essentially a narrow range containing the lighter olefin hydrocarbon in the reaction-distillation column according to item 15, according to which the specified pressure in the upper part of the specified reaction-distillation column includes maintaining the specified pressure in the upper part of the specified reactive distillation column in the range from -10 pound/square inch (wt.) up to 200 pounds/square inch (wt.).

17. The method of increasing the yield of heavier olefins from essentially a narrow range containing the lighter olefin hydrocarbon in the reaction-distillation column according to item 16, according to which the specified pressure in the upper part of the specified reaction-distillation column includes maintaining the specified pressure in the upper part of the specified reactive distillation column in the range from 5 pounds/square inch (wt.) up to 75 pound/square inch (wt.).

18. The method of increasing the yield of heavier olefins from essentially a narrow range containing the lighter olefin hydrocarbon in the reaction-distillation column according to 17, further comprising maintaining the specified temperature specified in the lower part of the specified reactive distillation column in the range from 100 to 500 F and maintain this temperature in the specified upper part of the specified reactive distillation column in the range from 0 to 300°F.

19. The method of increasing the yield of heavier olefins from essentially a narrow range containing the lighter olefin hydrocarbon in the reaction-distillation column for p, according to which for a given feed containing light olefins hydrocarbons from C6to C10the method further includes obtaining a heavier registergui hydrocarbons, essentially from C10to C20with the release of at least 55% by mass.

20. The method of increasing the yield of heavier olefins from essentially a narrow range containing the lighter olefin hydrocarbon in the reaction-distillation column according to claim 9, according to which the specified feedrate specified essentially narrow band containing the lighter olefins hydrocarbons involves feeding a mixture essentially from C10to C20registertimer hydrocarbons in the reaction-distillation column in the specified predefined point specified reactive distillation columns.

21. The method of increasing the yield of heavier olefins from essentially a narrow range containing the lighter hydrocarbon olefins cheese is I in the reaction-distillation column according to claim 20, according to which the specified pressure is within the specified upper part of the specified reaction-distillation column includes maintaining the specified pressure in the upper part of the specified reactive distillation column in the range from -14,5 pound/square inch (wt.) to 50.0 lb/square inch (wt.).

22. The method of increasing the yield of heavier olefins from essentially a narrow range containing the lighter olefin hydrocarbon in the reaction-distillation column according to item 21, according to which the specified pressure is within the specified upper part of the specified reaction-distillation column includes maintaining the specified pressure in the upper part of the specified reactive distillation column in the range from -10,0 pound/square inch (wt.) up to 5.00 pounds/square inch (wt.).

23. The method of increasing the yield of heavier olefins from essentially a narrow range containing the lighter olefin hydrocarbon in the reaction-distillation column according to item 22, further comprising maintaining the specified temperature specified in the lower part of the specified reactive distillation column in the range from 100 to 500°F and maintain this temperature in the specified upper part of the specified reactive distillation column in the range from 0 to 300°F.

24. The method increased the I output of heavier olefins from essentially a narrow range containing the lighter olefin hydrocarbon in the reaction-distillation column according to item 23, whereby for a given feed containing light olefins hydrocarbons from C10to C20the method further includes obtaining a heavier olefins, essentially With14and more heavy products, with the release of at least 53% by mass.

25. The method of increasing the yield of heavier olefins from essentially a narrow range containing the lighter olefin hydrocarbon in the reaction-distillation column, including

the supply is essentially a narrow band containing the lighter olefins source of hydrocarbons, essentially With3and C4and heavier, in the reaction-distillation column at a predefined point specified reactive distillation columns,

disproportionation of the specified interval registertimer hydrocarbon, C3With4and heavier, with the use of the catalyst for the disproportionation education while containing heavier and lighter olefins hydrocarbons near the specified pre-defined point of feed of the specified essentially narrow band containing the lighter olefins source of hydrocarbons, essentially With3and C4and heavier, in the reaction-distillation column

isomerization of these products on the proportsionirovaniya specified interval registertimer hydrocarbons, essentially With3With4and heavier, using the isomerization catalyst in the specified reaction-distillation column

ensuring the availability of at least one zone of contact of vapor-liquid for best separation of these heavier and lighter registergui hydrocarbons

the pressure is within the specified reaction-distillation column, allowing a very efficient return of olefins with the lowest molecular weight among these olefins with desirable higher molecular weight in the lower part of the specified reactive distillation columns and ensuring the achievement of a high degree of conversion of the specified narrow range containing the lighter olefins source of hydrocarbons,

the temperature in the upper part of the specified reaction-distillation column, is sufficient for the conclusion of these most serious of undesirable olefins with a small molecular weight as the head of a ring taken from the top of the specified reaction-distillation column, and

the temperature in the specified lower part of this reaction-distillation column, sufficient to provide most of these light olefins specified as athelny olefins of higher molecular weight specified in the lower part of the specified reaction-distillation column, and in order to maintain the appropriate temperature profile in the specified reaction-distillation column, providing a sufficiently high reaction rate throughout the specified reactive distillation columns.

26. The method of increasing the yield of heavier olefins from essentially a narrow range containing the lighter olefin hydrocarbon in the reaction-distillation column by A.25, further comprising interleaving stages of the method of the disproportionation and isomerization of these products of the disproportionation specified contains more light olefins hydrocarbons.

27. The method of increasing the yield of heavier olefins from essentially a narrow range containing the lighter olefin hydrocarbon in the reaction-distillation column for p, optionally including the location of the specified at least one zone of contact of vapor-liquid in a specified reactive distillation column for the separation of these lighter olefins in the vapor phase and these heavier olefins in the liquid phase.

28. The method of increasing the yield of heavier olefins from essentially a narrow range containing the lighter olefin hydrocarbon in the reaction-distillation column according to item 27, according to the mu specified alternation of disproportionation and isomerization specified contains more light olefins hydrocarbons optionally includes the location of these catalysts for the disproportionation and isomerization alternating portions in the specified reactive distillation column.

29. The method of increasing the yield of heavier olefins from essentially a narrow range containing the lighter olefin hydrocarbon in the reaction-distillation column for p, according to which the addition of these catalysts for the disproportionation and isomerization of alternating portions specified in the reaction-distillation column further includes providing the location of these catalysts for the disproportionation and isomerization in the specified reaction-distillation column alternating layers.

30. The method of increasing the yield of heavier olefins from essentially a narrow range containing the lighter olefin hydrocarbon in the reaction-distillation column according to clause 29, according to which the specified isomerization catalyst comprises a catalyst consisting of a metal selected from the group comprising sodium, potassium, rubidium and cesium deposited by impregnation on the substrate.

31. The method of increasing the yield of heavier olefins from essentially a narrow range containing the lighter olefin hydrocarbon in the reaction-distillation column according to item 30, according to which the specified isomerization catalyst consisting of a metal, optionally including the AET catalyst, consisting of metals selected from the group consisting of sodium, potassium, rubidium and cesium or mixtures thereof, deposited by impregnation on the substrate.

32. The method of increasing the yield of heavier olefins from essentially a narrow range containing the lighter olefin hydrocarbon in the reaction-distillation column for p, according to which the specified disproportionation catalyst comprises a catalyst comprising a heavy metal selected from the group consisting of rhenium, tungsten or molybdenum deposited by impregnation on the substrate.

33. The method of increasing the yield of heavier olefins from essentially a narrow range containing the lighter olefin hydrocarbon in the reaction-distillation column for p, according to which the specified isomerization catalyst consisting of metal, includes a catalyst consisting of a metal selected from the group consisting of rhenium, tungsten or molybdenum and mixtures thereof, deposited by impregnation on the substrate.

34. The method of increasing the yield of heavier olefins from essentially a narrow range containing the lighter olefin hydrocarbon in the reaction-distillation column for p, according to which the specified pressure is within the specified upper part of the reaction-distillation column includes maintaining the specified pressure is specified in the upper part of the specified reactive distillation column in the range from 0 pounds/square inch (wt.) up to 500 pounds/square inch (wt.).

35. The method of increasing the yield of heavier olefins from essentially a narrow range containing the lighter olefin hydrocarbon in the reaction-distillation column at 34, according to which the specified pressure is within the specified upper part of the specified reaction-distillation column includes maintaining the specified pressure at a specified upper part of the specified reactive distillation column in the range from 80 pound/square inch (wt.) up to 200 pounds/square inch (wt.).

36. The method of increasing the yield of heavier olefins from essentially a narrow range containing the lighter olefin hydrocarbon in the reaction-distillation column for p, further comprising maintaining the temperature in the specified lower part of this reaction-distillation column in the range from 100 to 500°F, maintaining the specified temperature specified in the upper part of the specified reactive distillation column in the range from -50 to 300°F.

37. The method of increasing the yield of heavier olefins from essentially a narrow range containing the lighter olefin hydrocarbon in the reaction-distillation column for p, where the specified registertimer hydrocarbon containing From3and C4the method further includes the floor shall receive heavier registergui hydrocarbons, essentially from C5to C10with the release of at least 63% by weight.

38. The method of increasing the yield of heavier olefins from essentially a narrow range containing the lighter olefin hydrocarbon in the reaction-distillation column of claim 10, whereby the specified feedrate specified essentially narrow band containing the lighter olefins hydrocarbons involves feeding measured quantities in a certain way branched registergui hydrocarbons to obtain the necessary degree of branching in the desired heavier the product, component from essentially 0% branched molecules up to essentially 100% branched molecules in the calculation of the average value for these heavier products - olefins.

39. The method of increasing the yield of heavier olefins from essentially a narrow range containing the lighter olefin hydrocarbon in the reaction-distillation column according to item 15, according to which the specified feedrate specified essentially narrow band containing the lighter olefins hydrocarbons involves feeding measured quantities in a certain way branched registergui hydrocarbons to obtain the necessary degree of branching in need heavier olefinic product, Department technical and the software component being 0% branched molecules up to essentially 100% branched molecules in the calculation of the average value for these heavier products - olefins.

40. The method of increasing the yield of heavier olefins from essentially a narrow range containing the lighter olefin hydrocarbon in the reaction-distillation column according to claim 20, whereby the specified feedrate specified essentially narrow band containing the lighter olefins hydrocarbons involves feeding measured quantities in a certain way branched registergui hydrocarbons to obtain the necessary degree of branching in need heavier products - olefins comprising from essentially 0% branched molecules up to essentially 100% branched molecules in the calculation of the average value for these heavier products - olefins.

41. The method of increasing the yield of heavier olefins from essentially a narrow range containing the lighter olefin hydrocarbon in the reaction-distillation column by A.25, according to which the specified feedrate specified essentially narrow band containing the lighter olefins hydrocarbons involves feeding measured quantities in a certain way branched registergui hydrocarbons to obtain the necessary degree of branching in need heavier products - olefins comprising from essentially 0% branched molecules to sushestvu% branched molecules in the calculation of the average value for these heavier products - olefins.

Priority items:

09.04.2001 on p-37;

29.01.2002 according to claims 1 to 24, 38-41.



 

Same patents:

FIELD: organic chemistry, petroleum chemistry, chemical technology.

SUBSTANCE: method involves preparing ethylene and hexane-1 from butene-1 by the exchange reaction of butene-1 and the isomerization reaction of synthesized hexane-3 to hexane-1. The parent material represents a mixed butene flow wherein butene-1 is isomerized to butene-2 after separation of isobutylene followed by the isomerization reaction of butene-2 to butene-1. Butene-1 is a raw for the exchange reaction.

EFFECT: improved preparing method, simplified technology process.

32 cl, 4 tbl, 4 ex

The invention relates to a method of producing bicyclobutane, which is a component of fuel for liquid rocket engines

FIELD: chemical and petrochemical industries; isomerization of olefins.

SUBSTANCE: the invention is dealt with of the field of deposition on carbon materials of catalysts of the basic nature being of interest for processes of isomerization of olefins. There is a description of a catalyst of isomerization of olefins containing metal sodium deposited on a composite porous carbon material, which represents a three-dimensional porous carbon die with the following structural characteristics: d002 =0.343-0.350 nm, the average size of the crystallite in a direction of "a"-La=l-14 nm, the average size of the crystallite in a direction of "c"-Lc=2-12 nm, real density of 1.8-2.1 g/cm3, with distribution of pores by sizes having a maximum in the range of 20-200 nm and an additional maximum in the range of 1-20 nm. Also there is a description of a method of preparation of the catalyst providing for deposition of metal sodium on the composite porous carbon material and a method of isomerization of olefins with use of this catalyst. The technical result is a possibility to conduct the process of isomerization at low temperatures, increased catalytic activity and selectivity, decreased output of by-products.

EFFECT: the invention ensures a possibility to conduct the process of isomerization at low temperatures, increased catalytic activity and selectivity, decreased output of by-products.

6 cl, 10 ex, 2 tbl

The invention relates to new furifosmin formula I

< / BR>
where n denotes an integer of 1 or 2; R1denotes a hydrophilic group selected from the following groups: -SO2M, -SO3M, -CO2M, -PO3M, where M represents inorganic or organic cationic residue selected from a proton, cations, alkaline or alkaline earth metals, ammonium cations -- N(R)4where R denotes hydrogen or C1-C14alkyl, and the other cations are based on metals, salts with acids: fullsleeve, fullcarbon, fullsleeve or furylphosphonous soluble in water; m denotes an integer of 1; R2denotes a hydrophilic group,- SO2M, -SO3M, -CO2M, RHO3M, where M denotes hydrogen or an alkaline metal salt with the acid fullsleeve, fullcarbon, fullsleeve or fullfactorial soluble in water, R denotes an integer from 0 to 2

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

The invention relates to the field of production of olefinic hydrocarbons obtained from paraffin hydrocarbons by dehydrogenation in a fluidized bed of catalyst and used for the synthesis of isoprene, ethers or other organic products and can be used in the petrochemical industry

The invention relates to the field of organic chemistry, namely, the method of production of Ala-4Z-ENES

The invention relates to the field of petrochemicals, in particular the production of trimers and tetramers of propylene, which are widely used as raw material in the manufacture of additives to oils, plasticizers, flotation agents and other surfactants and synthetic oils

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.

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EFFECT: increased yield of desired product.

41 cl, 4 dwg, 5 ex

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