The way to select environmentally friendly high-octane component of motor fuel and low octane basolateral fraction of catalysts for reforming a wide gasoline fractions

 

(57) Abstract:

The invention relates to the field of chemicals, petrochemicals, and more specifically to a method for selection of high-octane component of motor fuel and benzene from catalization reforming of gasoline fractions. It is proposed to allocate a high-octane component of motor fuel with an octane rating 97-108 points on the research method with benzene content less than 1 wt.% from catalization reforming wide fractions in heat and mass transfer apparatus when the specific pressure drop 50-600 PA/m, with selection of the "head" of the faction with the temperature of the end of the boil 55-75oWith low-octane basolateral fraction with temperature end of the boil 90-115oWith using as a separating agent mixture methylhexane and aromatic hydrocarbons With a mass ratio of a separating agent benzene (1-15):1 in mass ratio in the separating agent of methylhexane : aromatic hydrocarbons (0,3-4):1, followed by extraction basolateral fractions by selective solvent and the allocation of commercial benzene using distillation columns or heat and mass transfer apparatus. 1 C.p. f-crystals, 1 table.

The invention relates to the field of chemical re the Oia from catalization reforming octane 88-93 points on the research method (abbreviated PIM) and a benzene content of less than 2-8 wt. high-octane component of motor fuel (abbreviated VCMT) octane frequent 97-108 PIM and residual benzene content less mass. the so-called environmentally friendly VCMT in the terminology of the environmental Agency of the U.S., as well as commercial benzene. In accordance with the adopted in the USA in 1990, the Law on clean air force for nine cities in the United States, the content of carcinogenic benzene in motor fuel must not exceed 1 wt. Reducing the concentration of benzene in motor fuel is promoted in the USA and Europe [1]

A survey of a number of catalytic reforming units wide gasoline fractions, wikipaedia when 62-180oC, 70-180oC, 85-180oC showed that katalysator reforming benzene content ranges from 2 to 8 wt. depending on the applied pressure, the temperature of the reforming catalyst. The octane number of catalization varies in the range of 88-93 PIM. The concentration of low-octane components varies: n-hexane (2-13)wt. n-heptane (2-9)wt. n-octane (0.3 to 5) wt. n-nonan (0,1-3) wt.

Valid at all surveyed facilities standard technology reforming [2] the reforming catalysate the direction of the bottom 205-225oC with multiplicity acute irrigation 7-9, at the top of the column allocate the fraction of light hydrocarbons, C2-C4and on the bottom VCMT containing 2-8 wt. benzene, octane 91-95 PIM.

In currently in place in Russia GOST on motor fuel, the concentration of benzene in them is not specified. However, when fuel sales abroad price of fuel containing less than 1% benzene, much higher.

Currently, the new standard for motor fuel, limiting the benzene content in them.

Thus, the problem of reducing the concentration of benzene in motor fuels is important.

The second important issue when disposing benzylideneamino of catalization reforming is the extraction of commercial benzene (December 1993 250 thousand rubles per ton). Only one installation type LCH-35-11/1000 together with gasoline is burned in the engines of 50 tons of tons per year of benzene.

There is a method of allocating VCMT 95 octane PIM and above from catalization reforming with 91-93 octane PIM by rectification with a separating agent, is performed in tray distillation column efficiency 20 so t at a multiplicity irrigation 9, the pressure of the top of the as a separating agent, a mixture of benzene and pseudocumene content pseudocumene 3-10 wt. when the mass ratio of a separating agent: amount of n-pentane, n-hexane, 2-methylhexane, 3-methylhexane, n-heptane in the power of the column equal to (0.5 to 3):1.

At the top of the distillation column allocate the fraction of light hydrocarbons, C2-C4, side sampling fraction containing benzene with low-octane hydrocarbons, on the bottom VCMT octane number 95-98 PIM (sample method).

The disadvantage of the prototype method is the high content of benzene with low-octane basolateral fraction, low growth actinophage number of mixtures head and a bottom fraction compared with the original catalyzate (1-2 PIM, see comparative example 16 of the present application).

The purpose of the present invention increase the potential selection of benzene with low-octane basolateral fraction and, consequently, increases the production of commodity benzene, reducing the concentration of benzene in VCMT to 0.1-0.5. increasing the octane number VKIT to 97-108 PIM, an increase in the octane number of the reformate after separation from it basolateral fractions up to 4-7 PIM, the expansion of raw materials process by involving relatively low-octane catalization reforming to 88 PIM.

x fractions in heat and mass transfer apparatus (abbreviated as TMA), equipped with heat and mass transfer and redistribution packages made from specially shaped grid in the form of Z-shaped bumps with transverse waves, as well as special devices for uniform distribution of liquid and gas over the cross section of the apparatus (4).

The structural characteristics of the packets of the TMA, such as specific surface area, the step of transverse waves on the surface, the height of the Z-shaped corrugation inclination angle them to the vertical, is chosen so that during the process of separation catalyzate specific pressure drop was within the range of 50-600 PA/m

The separation process catalyzate reforming is carried out in the presence of a separating agent, which is a mixture of methylhexane and aromatic hydrocarbons, C10mass ratio of a separating agent: benzene catalyzate equal to (1-15): 1, and the mass ratio in the separating agent methylcyclohexane: aromatic hydrocarbons, C10(0.3 to 4):1.

As methylhexane into the separating agent used 2-methylhexan, 3-methylhexan or their mixture, and as an aromatic hydrocarbon, C10tetramethylbenzene, ethyldimethylamine or their mixture.

Process of reforming Catalysate together with the separating agent in food quality, depending on the composition catalyzate and technological features of the installation is performed at a pressure in the top of the TMA. The separation process depending on the composition catalyzate and technological features of the installation is performed at a pressure in the top of the TMA 3-13 ATA. On top of TMA distinguish the "head" of the fraction of light hydrocarbons, C2-C5with the temperature of the end boiling point in the range of 55-75oWith determined according to GOST 2177-82. From the upper part of the device located between the point of power input and output of the "parent" faction emit low-octane basolateral faction. The magnitude of the selection of this fraction regulate the temperature of the end of the boil, which should be in the range of 85-115oC.

On the bottom of the device provide VCMI octane 97-108 PIM and benzene content less than 1 wt.

Side low-octane basolateral fraction is directed to the selective extraction solvents, for example, triethylene glycol, followed by separation of benzene from the extract in a distillation column in a known manner (5). For this purpose you can also use the TMA.

"Head" faction TMA or guide for the installation of fractioning the purpose of separation of individual hydrocarbons C2-C5or mixed with WCMT. The octane number of the "parent" faction is 70-80 PYM, p. what about the method compared with the method of the prototype is more significant increase in the octane number after selection of low-octane basolateral fraction of catalyzate reforming: 4-7 points of the proposed method and only 2-3 points when using the prototype method (see examples).

Hydrodynamic processes occurring during the separation of mixtures in TMA, significantly marked from those that take place in a traditional tray and Packed columns. TMA is marked from the latter is significantly higher bandwidth and a couple of liquid, a lower hydraulic resistance at much higher performance of the separation process.

When using the same separating agent when carrying out this process in a TMA exit benzene, octane WCMT, the increase in the octane number catalyzate after "clipping" low-octane basolateral fraction is significantly higher than during the process of plate or Packed column, respectively, output by 6.7% octane VCMT 6.4 PIM, the increase in the octane number 4 PIM (see examples).

On the other hand, the use of a separating agent of the prototype method is less effective for the separation even when using TMA (see example 16).

The collective use of the essential distinguishing features of the proposed method: the use of TMA with the constructive characteristics of the packets, making theC, low-octane basolateral faction within 90-115oC using the above-mentioned separating the application of the aforesaid separating agent in a predetermined ratio significantly increases the efficiency of separation catalyzate reforming compared with the method of the prototype. Separate use of these features is less effective. Specific ranges of values of the requested parameters are determined by certain technical purpose: to provide a potential yield of benzene with basolateral fraction not less than 85 wt. octane VCMT not less than 97 PIM, the increase in the octane number catalyzate at least 4 PIM.

Applicants know the use of TMA similar in design (but with other structural parameters) for the separation of mixtures in the production of ethyl alcohol, freon, hydrogen peroxide and others, however, the literature contains no information about the use of these devices for the separation of catalization reforming and other hydrocarbon mixtures. Not also described the use of the proposed separating agent to highlight benzylideneamino fractions and WCMC. So we can assume that the proposed solution meets the criterion of novelty.

In nasrollahi separating agents. The choice of the separating agent, the definition of the claimed ranges of parameters was carried out by tests on pilot plants, i.e., the invention meets the criterion of non-obviousness.

There are several ways to obtain the components of the separating agent: methylhexane and aromatic hydrocarbons, C10. Specifically at the Kirishi refinery, where the first planned implementation of the proposed method, low-octane components emitted as the raffinate from extraction of the selective solvent basolateral faction, will be sent to the process isoelectrofocusing, where n-pentane get isopentane from n-hexane - isohexane, from n-heptane mostly by methylhexane.

The carrying amount of methylhexane separated from the isomerized product by distillation and recycled into the separating agent. The second component of the proposed integrated separating agent aromatic hydrocarbon, C10in a mixture with other aromatic hydrocarbons formed as by-product in the process of obtaining xylenes on the extraction facilities, as well as in the composition of the fractions 150-180oC product hydroforming (6).

One of these products, aromatic hydrocarbons, C10can brodow C10you can use the fraction of hydrocarbon, C10with content as impurities aromatic hydrocarbon, C8-C9up to 20 wt.

Feature of aromatic hydrocarbons, C10as a component of the separating agent is that there is no practical need to regeneration (usually the most difficult stage of the process of rectification with the separating agent), because on the one hand, aromatic hydrocarbon, C10increase knock resistance VCMT (105-110 octane PIM), on the other hand, are constantly accumulating on the extraction facilities included in a refinery by-product, which is currently used as an additive to motor fuel.

The proposed allocation method WCMT and benzene from catalization reforming implement on an industrial scale, because in Russia there are companies producing TMA different designs.

Thus, the important features of the proposed method are the following:

selection WCMT and basolateral fraction is carried out in heat and mass transfer apparatus of known construction with the packet (specific surface area, step wave, the height of the corrugation, NaClO is isolated by the temperature of the end of the boil 55-75oC, low-octane basolateral fraction allocate a side selection of TM, with the end of the boil 90-115oC;

the separation is carried out with a separating agent mixture methylhexane aromatic hydrocarbon, C10mass ratio of a separating agent: benzene 91-150: 1 in mass ratio in the separating agent of methylhexane: aromatic hydrocarbons, C10(0.3 to 5):1.

The proposed method allows comparison with the known method to increase the output of allocated with benzene to 75-80 85-95 wt. to reduce the concentration of benzene in VCMT from 1.5 to 2.0 0.1 to 1.0 wt. to increase the octane number VCMT with 95-98 PIM to 97-108 PIM, to increase the octane number catalyzate with 4-7 2-3 to PIM.

The proposed method allows to extend the resource base of the process through the use of catalization octane up to 88 PIM.

As follows from comparison of the data of examples 1 and 14, with higher quality and output of the partial product inputs for selection 1 t VCMT on the proposed method using TMA 23% lower than when the separation plate column, and capital costs (due to smaller TMA) 1.7 times less.

The method is illustrated by the examples, the basic financial p is x trials, the results of which are reflected in the examples was carried out only analyses, allowing to establish the achievement of this goal increase the octane number of catalyzate increase the yield of benzene, reducing its concentration in WCMT.

Determined group of chemical composition of raw materials entering the reforming, its fractional composition according to GOST, group chemical composition catalyzate reforming and separation products, the octane number on the research method catalyzate reforming, basolateral faction, WCMC, and the temperature of the end of the boil basolateral fractions, fractions according to GOST. Very carefully determined the concentration of benzene in the raw materials and products division.

The results of examples shown in the table.

Example 1 (average values). Hydrotreated straight run gasoline fraction, wikipaedia at a temperature of 70-180oC, isolated from the Samotlor oil field and having fractional composition according to GOST 2177-82 NC-78oC, 10% 98oC, 50% 112oC, 90% 152oC QC 174oC hydrocarbon composition (group), wt. aromatic hydrocarbons - 16,3: naphthenic hydrocarbons 12,1: paraffin hydrocarbons 71,6, including n-p is the temperature value 510oC, flow rate of feed of 1.6 4-1the multiplicity of circulation of the hydrogen-containing gas 820 nm3/m3on the catalyst series CU containing, by weight. platinum 0,73, chlorine 0,64, rhenium 0,09, cadmium 0,66, sulfated alumina else.

The result of the reforming catalysate with an octane rating of 91.3 PIM composition, wt. paraffin hydrocarbon, C2-C42,15, paraffin hydrocarbons, C5-C617,92, paraffin hydrocarbons, C7-C822,12, paraffin hydrocarbons, C9-C10- 2,36, including low-octane paraffin hydrocarbons of normal structure: n-pentane to 3.58, n-hexane of 5.68, n-heptane 7,24, n-octane 6,02, n-nonan 1,63, n-decane 0,14, naphthenic hydrocarbon, C5-C8- 1,16, unsaturated hydrocarbons of 0.36, aromatic hydrocarbons 53,93, including benzene 5,97, toluene 22,16, aromatic hydrocarbon, C8-C925,80.

The reforming catalysate in the amount of 100 kg/h together with 298,5 kg/h separating agent is sent to the quality of food in the middle part of the TMA total height of 20.6 meters Height of the apparatus, filled with heat and mass transfer and redistribution packages 13.6 m, the volume of packages 57 m3.

The separation process catalyzate wire is UP>C, lateral selection 125oC, acute irrigation 40oC.

The ratio of methylhexane: aromatic hydrocarbons, C10in the separating agent is 1:1. The ratio of the separating agent: benzene catalyzate reforming is 5:1.

On top of TMA allocate 112,63 kg/h head fraction with temperature end of the boil 62oC, containing, by weight. paraffin hydrocarbon, C2-C4-18,81, paraffin hydrocarbons, C5-C6- 73,79, paraffin hydrocarbons, C7-C83,24, naphthenic hydrocarbon, C5-C82,00, unsaturated hydrocarbons 0.6 benzene 1,56.

Side selection point, located on 1/3 from the top of the TMA, output low-octane basolateral fraction composition, wt. paraffin hydrocarbon, C2-C40,10, paraffin hydrocarbons, C5-C6to 28.57, paraffin hydrocarbons, C7-C8- 10,77, naphthenic hydrocarbon, C5-C81,79, unsaturated hydrocarbons 0,39, benzene, 16,41, toluene 1,09, methylhexane 40,88. The temperature of the end of the boil basolateral faction 102oC, the octane rating of 54.3 PIM, the potential selection of low-octane normal paraffin hydrocarbons, wt. n-pentane 25,08: n-hexane to 91.6; n-heptane 18,51; n-octane 1,53.

-C821,34, paraffin hydrocarbons, C9-C102,78, naphthenic hydrocarbon, C5-C80,39; unsaturated hydrocarbons 0,19, benzene, 0,32; toluene 25,65; aromatic hydrocarbons, C8-C930.37 per; methylhexane 1,39; aromatic hydrocarbons, C1017,57.

As a result of mixing the "parent" faction and WCMT get 962,25 kg/h catalyzate reforming octane 98,8, i.e. the increase in the octane number after the "cut" of him low-octane basolateral faction is 7.5 PIM. This product has a composition, by weight. paraffin hydrocarbon, C2-C42,20; paraffin hydrocarbon, C5-C6- 8,65; paraffin hydrocarbon, C7-C819,23; paraffin hydrocarbon, C9-C102,45, including paraffin hydrocarbons of normal structure: n-pentane and 2.79, n-hexane and 0.50, n-heptane 6,13, n-octane 6,16, naphthenic hydrocarbon, C5-C80,58, unsaturated hydrocarbons 0,24, aromatic hydrocarbons 65,43, including: benzene 0,47, toluene -22,64, aromatic hydrocarbon, C8-C926,81, aromatic hydrocarbon, C1015,51, methylhexane 1,22.

The yield of benzene with basolateral faction is to 92.4 wt. from the potential content catalyzate of reformer. As a result of the extraction process and subsequent distillation of the extract on two distillation columns or heat and mass transfer devices emit 56,8 kg/h commercial benzene. In terms of power typical of reformer LCH-35-11/100 105 tons per hour catalyzate reforming an additional output of commodity benzene is 47 thousand tons/year. The cost of heat per ton VCMT are 106 mcal.

Example 2 (lower limit of the specific pressure drop). Reforming catalysate composition shown in example podvergaut division analogously to example 1, with the difference that the value of the specific pressure drop in the height of the packages TMA meets the bottom of the claimed boundary, namely 50 PA/m

As a result, there basolateral fraction with the release of benzene from the potential of 85.2 wt. VCMT with an octane rating of 97.3 PIM and with the concentration of benzene of 0.95 wt. When mixing the "parent" faction and faction VCMT receive the product with an octane rating of 95.4 PIM, i.e. the increase in the octane number will be 4.1 PIM.

Example 3 (upper limit of the specific pressure drop). Reforming catalysate composition shown in example 1, is subjected to separation as in example 1, with the difference that the value of the specific drop the e to distinguish basolateral fraction with the release of benzene from potential 86,3 wt. VCMT octane 97,1 PIM and with the concentration of benzene 0.96 wt. When mixing the "parent" faction and faction VCMT receive the product with an octane number 95,6 PIM, i.e. the increase in the octane number is 4.3 PIM.

Example 4 (the lower limit temperature of the end of the boil "parent" faction). Reforming catalysate composition shown in example 1, is subjected to separation as in example 1, with the difference that the temperature of the end of the boil "parent" faction meets the bottom of the claimed boundary, namely 55oC.

As a result, there basolateral fraction with the release of benzene from potential 89,4 wt. VCMT octane 98,7 PIM and with the concentration of benzene of 0.79 wt. When mixing the "parent" faction and faction VCMT receive the product with an octane number 96,0 PIM, i.e. the increase in the octane number is 4.7 PIM.

Example 5 (upper limit temperature of the end of the boil "parent" faction). Reforming catalysate composition shown in example 1, is subjected to separation as in example 1, with the difference that the temperature of the end of the boil "parent" faction meets the upper declare the border, namely the 75oC.

As a result, there basolateral fraction with the release of beuneu" faction and faction VCMT receive the product with an octane number 97,0 PIM, i.e. the increase in the octane number is 5.8 PIM.

Example 6 (the lower limit temperature of the end of the boil basolateral faction). Reforming catalysate composition shown in example 1 is subjected to separation as in example 1, with the difference that the temperature of the end of the boil basolateral faction meets the bottom of the claimed boundary, namely 90oC.

As a result, there basolateral fraction with the release of benzene from the potential of 85.1 wt. VCMT octane 97,0 PIM and with the concentration of benzene and 0.98 wt. When mixing the "parent" faction and faction VCMT receive the product with an octane number for 95.3 PIM, i.e. the increase in the octane number is 4.0 PIM.

Example 7 (upper limit temperature of the end of the boil basolateral faction). Reforming catalysate composition shown in example 1, is subjected to separation as in example 1, with the difference that the temperature of the end of the boil basolateral faction meets the upper declare the border, namely 115oC.

As a result, there basolateral fraction with the release of benzene from potential to 97.1 wt. VCMT octane 108 PIM and with the concentration of benzene of 0.08 wt. When mixing the "parent" faction and the"ptx2">

Example 8 (the lower bound of the ratio of the separating agent: benzene). Reforming catalysate composition shown in example 1, is subjected to separation as in example 1, with the difference that the value of the ratio a separating agent: benzene meets the bottom of the claimed boundary, namely 1:1.

As a result, there basolateral fraction with the release of benzene from potential to 85.8 wt. VCMT octane 97,1 PIM and with the concentration of benzene and 0.98 wt. When mixing the "parent" faction and faction VCMT receive the product with an octane number 96,0 PIM, i.e. the increase in the octane number is 4.7 PIM.

Example 9 (upper bound of the ratio of the separating agent: benzene). Reforming catalysate composition shown in example 1, is subjected to separation as in example 1, with the difference that the value of the ratio a separating agent: benzene meets the upper declare the border, namely 1:1.

As a result, there basolateral fraction with the release of benzene from potential 86,3 wt. VCMT with an octane rating of 102.3 PIM and with the concentration of benzene and 1.00 wt. When mixing the "parent" faction and faction VCMT receive the product with an octane number 98,0 PIM, i.e. the increase in the octane number is 6.7 PIM.

Example 10 (n is t reforming composition, shown in example 1, is subjected to separation as in example 1, with the difference that the value of the ratio of methylhexane: aromatic hydrocarbons, C10in the separating agent meet the bottom of the claimed boundary, namely 0,3:1.

As a result, there basolateral fraction with the release of benzene from potential to 91.2 wt. VCMT octane 97,2 PIM and with the concentration of benzene to 0.89 wt. When mixing the "parent" faction and faction VCMT receive the product with an octane number 95,9 PIM, i.e. the increase in the octane number is 4.6 PIM.

Example 11 (the upper limit of the ratio of methylhexane: aromatic hydrocarbons, C10in the separating agent). Reforming catalysate composition shown in example 1, is subjected to separation as in example 1, with the difference that the value of the ratio of methylhexane: aromatic hydrocarbons, C10in the separating agent answer claimed the top border, namely 4:1.

As a result, there basolateral fraction with the release of benzene from potential 95.6 wt. VCMT octane 97,0 PIM and with the concentration of benzene of 0.12 wt.

When mixing the "parent" faction and faction VCMT receive the product with an octane number 95,6 PIM, i.e. the increase of the second produce). The separation process is carried out analogously to example 1, with the difference that the raw material separation using the reforming catalysate octane 88,2 PIM composition, wt. paraffin hydrocarbon, C2-C41,97: paraffin hydrocarbon, C5-C620,34, paraffin hydrocarbons, C7-C829,13, paraffin hydrocarbons, C9-C103,93, including low-octane paraffin hydrocarbons of normal structure: n-pentane 5,48, n-hexane 7,87, n-heptane to 9.57, n-octane 8,64, n-nonan of 1.87, n-decane 0,26, naphthenic hydrocarbon, C5-C82,19, unsaturated hydrocarbons of 0.14, aromatic hydrocarbons 42,30, including benzene, 2,34, toluene 17,62, aromatic hydrocarbon, C8-C922,34.

As a result, there basolateral fraction with the release of benzene from potential 85,3 wt. VCMT with an octane rating of 97.6 PIM and with the concentration of benzene 0.67 wt. When mixing the "parent" faction and faction VCMT receive the product with an octane number 93,9 PIM, i.e. the increase in the octane number is 5.7 PIM.

Example 13 (without a separating agent). Reforming catalysate composition shown in example 1, is subjected to separation as in example 1, with the difference that the separation is carried out without separating agents octane 96,1 PIM and with the concentration of benzene of 1.35 wt. When mixing the "parent" faction and faction VCMT receive the product with an octane number 94,2 PIM, i.e. the increase in the octane number will be 2.9 PIM.

Example 14 use of column trays instead of TMA). Reforming catalysate composition shown in example 1, is subjected to separation as in example 1, with the difference that the separation is carried out in the Belleville column efficiency 40 so so

As a result, there basolateral fraction with the release of benzene from the potential of 85.7 wt. VCMT octane 97,9 PIM and with the concentration of benzene to 1.14 wt. When mixing the "parent" faction and faction VCMT receive the product with an octane number 94,1 PIM, i.e. the increase in the octane number will be 2.8 SSM. Thus, the comparison of the data of examples 1 and 14 shows that even the use of high-efficiency column trays ceteris paribus provides lower division catalyzate reforming compared with the use of TMA. The cost of heat 1 t VCMT be 130 mcal, which is 23% higher than when using TMA.

Example 15 (method prototype). Reforming catalysate composition shown in example 1, in the amount of 1000 kg/h with 300 kg/h separating agent, vkljucenosti 40 so so working with the multiplicity of the irrigation 9:1, a pressure of 12 MPa, a temperature of the top 96oC, bottom 244oC, acute irrigation 40oC.

The separation on the bottom of the column allocate VCMT octane 96,8 PIM and with the concentration of benzene was 1.58 wt. The yield of benzene with a side selection basolateral fraction of potential content catalyzate 79,4 wt. the increase in the octane number of 1.8 PIM.

Example 16 (using TMA and separating agent according to the method prototype). Reforming catalysate composition shown in example podvergaut division analogously to example 1, with the difference that, as a separating agent used in accordance with the method of the prototype of a mixture of 95 wt. benzene and 5 wt. pseudocumene.

As a result, there basolateral fraction with the release of benzene from potential to 86.4 wt. VCMT with an octane rating of 97.3 PIM and with the concentration of benzene, 1.24 wt. When mixing the "parent" faction and faction VCMT receive the product with an octane number 94,4 PIM, i.e. the increase in the octane number will make 3,1 PIM.

Example 16 (use as a component separating agent aromatic hydrocarbon, C10mixed with aromatic hydrocarbons, C8-C9). To the receiving, what component of the separating agent, a mixture of aromatic hydrocarbons, C10containing 20 wt. aromatic hydrocarbons, C8-C9.

As a result, there basolateral fraction with the release of benzene from potential 91,0 wt.with. VCMT with an octane rating of 102.3 PIM and with the concentration of benzene 0.48 wt. When mixing the "parent" faction and faction VCMT receive the product with an octane rating of 97.5 PIM, i.e. the increase in the octane number will be 6.2 PIM.

1. The way to select environmentally friendly high-octane component of motor fuel with an octane rating of 97 108 points on the research method, with the benzene content to 1 wt. and below and low-octane basolateral fraction for the allocation of commercial benzene from catalization reforming wide gasoline fractions with an octane rating of 88 93 points on the research method, containing 2 to 8 wt. benzene, as well as low-octane paraffin hydrocarbons by distillation with a separating agent, wherein the process is carried out in heat-mass exchange apparatus with heat and mass transfer and redistribution packages of specially shaped grid in the form of Z-shaped bumps with transverse waves and is a bookmark at the top of the unit fraction of light hydrocarbons, C2C5with the temperature of the end of the boil 55 - 75oWith a side selection of the top section of the device low-octane basolateral fraction with temperature end of the boil 90 115oWith the bottom of the device high-octane component of motor fuel, used as a separating agent mixture methylhexane and aromatic hydrocarbons, C10mass ratio of a separating agent benzene 1 15 1 in mass ratio in the separating agent of methylhexane:aromatic hydrocarbons, C100,3 4,0 1, followed by extraction basolateral fractions by selective solvent and the allocation of commercial benzene using distillation columns or heat and mass transfer devices.

2. The method according to p. 1, characterized in that as methylhexane use 2-methylhexan, 3-methylhexan or their mixture, and as an aromatic hydrocarbon, C10use isomeric tetramethylbenzene, ethyldimethylamine or their mixture.

 

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