Method of producing high-octane gasoline and device for its implementation (options)

 

(57) Abstract:

The invention relates to methods of producing gasoline hydrocarbons from lower olefins and can be used in the refining and petrochemical industry. Essence: the raw material containing at least one olefin WITH2-C4served in the reaction zone to a stationary acid catalyst based on the group zeolite. Spend the reaction of oligomerization of olefins feedstock to obtain a product stream containing hydrocarbons gasoline5+. Share the specified product stream from the production of gasoline and flow of hydrocarbons FROM1-C4followed by mixing the specified flow of hydrocarbons FROM1-C4feedstock. The feed containing olefins, mixed with wikipeida at a temperature not exceeding 85oA fraction of a gasoline reformer containing benzene, and the ratio of olefin /benzene in the final mixture is at least 0.5 mol/mol. Specified oligomerization reaction is carried out in conditions providing the alkylation of at least part of the benzene. Effect: reduction of the resulting dry gases - methane and ethane. 3 S. and 8 C.p. f-crystals, 2 ill., table 1.

In oil refining processes produce large quantities of gaseous under normal conditions of mixtures of paraffins and olefins. These mixtures can be utilized in various ways. One of the directions of the utilization of specified blends registergui gases receipt of the olefin components of motor fuels.

Light olefins can be used for alkylation of benzene contained in the gasoline fraction and the unwanted component (US 4209383, US 5336820).

There is a method of processing a light registertimer fuel gas and liquid products of catalytic reforming in a reactor with a fluidized bed of zeolite catalyst (US 4827069), including the transformation WITH4-olefins in the gasoline fraction hydrocarbons, C5+and the conversion of aromatic hydrocarbons WITH6-C8in aromatic hydrocarbons WITH7-C11upon contact of the feedstock with the catalyst particles, characterized by a certain density and specific dimensions, in terms of the turbulent boundary layer. Obtained in the process gas has a higher octane characteristics than liquid products of reforming and registergui petrol, € flexibly control the temperature of the reaction and to obtain an optimal distribution of products.

The known method (US 5336820) alkylation with high speed benzylideneamino gasoline olefins WITH2-C5with the production of gasoline with reduced benzene content, including sequential contact with a solid catalyst under conditions of alkylation of benzene gasoline feedstock with an olefin in the order of decreasing activity in oligomerization, i.e. initially with olefins WITH3-C5and then with ethylene.

Of olefins C2-C4in the process of oligomerization in contact with zeolite catalysts can be obtained components of gasoline and diesel fuel. Catalyst properties and features of the technology allow for the oligomerization of olefins with high selectivity for a particular product /C. A. Tabak. Oil, gas and petrochemicals abroad, 1985, 9, S. 67-70/.

The closest analogue of the proposed method of producing high-octane gasoline is the patent of the Russian Federation 2135547, which describes a method of increasing the yield of gasoline fraction hydrocarbons WITH5+when the oligomerization of lower olefins. When implementing this method oligomerization registergui hydrocarbon fractions WITH3and C4or4in gasoline hydrocarbons oligomerization conditions, recycle part of the stream of hydrocarbon, C1-C4separated from the partially condensed product when its vapor-liquid separation, and parts isolated from the product by means of distillation fractions WITH4. When the beneficiation isobutane increases the yield of liquid hydrocarbons into olefins, however, the proportion of the formed hydrocarbon, C1-C2up to 10 wt.%.

The technical problem to be solved by the present invention is to develop a new method of disposal of mixtures registergui gases produced during oil processing.

The technical result is obtained as a result of implementation of the invention is to obtain high-octane gasoline from mixtures registergui gases produced during the refining of oil, with a decrease compared with the known methods, the number of produced dry gas (methane and ethane).

To achieve the specified result, it is proposed to use the following way to obtain high-octane gasoline. The proposed method involves feeding raw material containing olefins WITH2-C4(one of them, a mixture of any two or more olefins, in a reaction zone to a stationary acid catalization flow products containing hydrocarbons gasoline fraction C5+separation of the specified product stream from the production of gasoline and flow of hydrocarbon, C1-C4followed by mixing the specified stream of hydrocarbon, C1-C4with the raw material and advanced feedstock containing olefins, mixed with wikipeida at a temperature not exceeding 85oWith a fraction of catalytic reforming of gasoline containing benzene, and the ratio of olefin/benzene in the final mixture is at least 0.5 mol/mol, and found the oligomerization reaction is carried out in conditions providing the alkylation of at least part of the benzene. One of the variants of the method with fraction of gasoline reforming, containing benzene, mixed containing raw materials, including ethylene, and the interaction of this material with the specified catalyst is carried out in two reaction zones, and the reaction is carried out in such a way that in the first zone with a catalyst interacts raw material containing ethylene, the resulting interaction in the first zone a product stream, optionally mixed with a raw material containing propylene and/or butylenes, the resulting mixture was fed to the second reaction zone, and tempea implementation variant of the method, the fraction of gasoline reforming, contains benzene, a mixed raw material containing, including ethylene, the interaction of this material with the specified catalyst is carried out in three zones of the reaction, and the reaction is carried out in such a way that in the first zone with a catalyst interacts raw material containing ethylene, the resulting interaction in the first zone a product stream, optionally mixed with a raw material containing propylene, and the resulting mixture was fed to the second reaction zone, resulting from the interaction in the second zone, the product stream is additionally mixed with a raw material containing butylene, and serves the resulting mixture in a third reaction zone, in this case, the temperature of the raw material at the entrance to the reaction zone reduces from the first zone to the third zone. Possible case, when the interaction of materials with the catalyst is carried out at least in two parallel zones of interaction with further mixing the obtained products. The resulting implementation process, the product stream can be further divided obtaining hydrocarbon fractions WITH6containing benzene, with subsequent mixing of the fractions obtained with the raw material, at least one of the reaction zones. In this case, this fraction ug the aqueous hydrogenation of olefins.

Upon contact with acidic zeolite catalyst mixture registertimer raw materials and basolateral fraction products of catalytic reforming is the oligomerization of olefins with obtaining hydrocarbons FROM5-C9mainly paraffins, olefins and aromatic hydrocarbons and the alkylation of benzene with getting alkyl benzenes C8-C10. Catalytic transformation of such a mixed raw material is different from the oligomerization registertimer raw materials held in the same conditions, a lower yield of methane and ethane and a large output of hydrocarbons gasoline5+calculated as the difference of their content in the raw material and the product, or the relative expression of these values.

As registertimer raw materials can be used a mixture of hydrocarbons, C1-C4containing at least one olefin WITH2-C4and almost not containing dienes. In the preferred case, the raw material contains hydrogen. Typical raw materials are registereda fraction of the exhaust gas catalytic cracking. Containing the benzene fraction of gasoline reforming, wikipaedia to 85oTo allocate the rectification method. Fraction of gasoline reforming, wikipediaa in the raw material should be no lower than 0.5 mol/mol and preferably in the range of 1.5 to 20 mol/mol.

The acid catalysts used in the proposed method, contain the group zeolite and active in the oligomerization of lower olefins in the gasoline hydrocarbons. Acidic properties of hydrogen and mixed cation-substituted forms of the zeolite. The catalysts can also contain metals or their oxides, and oxides of phosphorus or boron, introduced various known methods and influencing the catalytic properties and stability of the catalysts. Along with aluminosilicate zeolites can be used elementobject with the structure of pentelow with similar catalytic properties. Synthesis and structure of such materials is described in the technical literature and are widely known.

The contact of the feedstock with a stationary catalyst is carried out in-dependent of its properties in terms of oligomerization of olefins and alkylation of benzene, usually at a temperature of 280-500oWith the pressure of 0.6-2.5 MPa, the space velocity of the raw material of 0.5-8 h-1. Conditions in the reaction zone should provide the desired degree of conversion of olefin and benzene and be tough enough to limit the composition of the products gasoline hydrocarbons.

Hydrocarbons gasoline faction is catalytic reforming contain less benzene, than the mixture basolateral fraction of the products of catalytic reforming product of oligomerization registertimer raw materials (hydrocarbons gasoline5+), because in the conditions of transformation of the mixed raw material is the alkylation of benzene with obtaining high-octane aromatic hydrocarbons, C8-C10. When this detonation resistance of the product of the transformation mix of raw materials, certain motor and research methods, higher than that of the mixture of liquid products of oligomerization and cracking.

The activity of olefins in the reaction of oligomerization and various increases from ethylene to butylene, and to achieve a high activity catalyst for the oligomerization of olefins is carried out at different optimal temperatures, and higher for ethylene. When using the proposed method of obtaining gasoline as registertimer raw narrow fractions of olefins such as fractions WITH2and C3-C4or C2WITH3and C4- there is a possibility of contact of the feedstock with the catalyst, respectively, in two or three reaction zones under conditions preferred for each registereda faction. So contact with the catalyst raw material, with the flax and butylene, - at temperatures, respectively, not exceeding 460 and 440oC. the Result of this stage of the implementation of the catalytic process is the increase in catalyst activity with increasing temperature conversion registertimer raw materials and increase the stability of its actions in terms of reducing the temperature of contact. Getting gasoline in two reaction zones preferably in cases where one of the primary factions is atlantageorgia fraction.

There are two variants of the implementation stage of the process of turning raw materials.

According to the first variant fraction of liquid products reformer is mixed with registertask raw material of the first reaction zone and the resulting product is fed into the next, which leads to serial conversion of olefins and benzene in the reaction zones. Because of this type of raw material is the main factor of coke formation is the conversion temperature, to increase the stability of catalyst performance should decrease the average temperature in the reaction zones with the accumulation of unsaturated products, i.e. from the first reaction zone to the next.

According to the second variant conduct parallel conversion of olefins of puyi, and the resulting products are mixed and fed to the separation.

When receiving gasoline from two registergui fractions, one of which includes ethylene, consistent with the transformation of raw materials into two reaction zones, the raw material containing ethylene, containing mixed with the benzene fraction of gasoline reforming unit and contact of the mixture with the catalyst is carried out in a first zone, the product stream from the first reaction zone is mixed with a raw material containing propylene and/or butylene, and the contact of the mixture with the catalyst is carried out in the second zone, and the temperature of the raw material mixture at the inlet to the first reaction zone is higher than the temperature of the raw material mixture at the inlet to the second reaction zone.

When receiving gasoline from three hydrocarbon fractions respectively include ethylene, propylene and butylene, with the consequent transformation of raw materials in the three zones of the reaction raw material containing ethylene, containing mixed with the benzene fraction of gasoline reforming unit and contact of the mixture with the catalyst is carried out in a first zone, the product stream from the first reaction zone is mixed with a raw material containing propylene, and the contact of the mixture with the catalyst is carried out in the second zone, the product stream from the second zone RETA zone, moreover, the temperature of the raw material mixture at the entrance to the reaction zone decrease from the first to the third area.

Reaction of oligomerization of olefins and alkylation of benzene are exothermic effect. To limit overheating of the reaction zone feedstock is diluted with paraffin C1-C4allocated from the products. In a preferred variant of realization of the product stream is divided as follows: the stream is cooled with partial condensation of its components and carry out vapor-liquid separation of the cooled stream to obtain a gas phase stream containing hydrocarbons, C1-C4and liquid-phase stream containing mainly hydrocarbons WITH3+specified liquid flow fractionary obtaining gasoline5+and flow of hydrocarbons FROM3-C4and part of the hydrocarbon streams C1-C4and C3-C4mixed with the raw material at least one of the reaction zones.

In the proposed method of obtaining gasoline conversion of benzene contained in the raw material fraction of liquid products of reforming depends on the process conditions and composition of the raw material and in the preferred case exceed 30%. For a more complete conversion of benzene from the stream of products emit a fraction, the boom - or three-stage process variant recycling basolateral fraction preferably be directed in the area of low temperature conversion of raw materials.

Benalmadena fraction separated from the product stream includes olefins formed during the oligomerization of the original olefin feedstock. Olefins depends mainly on the ratio in the raw material olefins and a fraction of the products of reforming, as well as from the content in the last benzene and the degree of conversion. The presence of olefins WITH5+in raw materials is undesirable, as it leads to rapid coking of the catalyst. In order to remove olefins from circulating basolateral faction before mixing with the raw material it is subjected to hydrogenation under conditions of selective hydrogenation of olefins on lookbetteronline.com or aluminumaluminium the catalyst by known techniques used for hydrofining secondary gasoline /,N. Maslansky, R. N. Shapiro. Catalytic reforming of gasolines. L.: Chemistry, 1985, S. 109-118; M. C. Landau. Chemistry and technology of fuels and oils, 1991, 1, S. 8-10/.

The method can be implemented using a device whose construction is shown below. The specified device contains a first heat exchanger to the first input of which is connected the line atlantageorgia faction, highway fractions of gasoline reforming, highway faction Gadirov is based separation of the cooled product stream or perhaps part of the flow of hydrocarbons 1-C4and hydrogen. The first output of the first heat exchanger connected to the first input of the first furnace, the first output of which is connected to the inlet of the first reactor, the output of which is connected by a pipe with the inlet of the second reactor, the output of which is connected by pipeline to the input of the third reactor, the output of which is connected by a pipeline with the second inlet of the first heat exchanger, and the first inputs of the second and third heat exchangers. The second input of the second heat exchanger is connected to the line Propylenediamine fraction and the highway recycle stream representing a portion of the stream of hydrocarbon, C1-C4(or, perhaps, part of the flow of hydrocarbons, C1-C4and hydrogen), allocated from the streams of products by the methods of vapor-liquid separation and distillation, the first outlet of the second heat exchanger is connected to a second input of the specified first furnace and the second output of the specified first furnace highway, connecting the outlet of the first reactor with the inlet of the second reactor. The second input of the third heat exchanger is connected to the line butylenediamine fraction and the highway recycle stream representing a portion of the flow angle is x from the stream of products by the methods of vapor-liquid separation and distillation, the first output of the specified third heat exchanger is connected to the third input of the specified first furnace and through the third output of the specified furnace with a line connecting the outlet of the second reactor and the inlet of the third reactor. The second outputs of the first, second and third heat exchangers are connected with the inlet air cooler, the output of which is connected to the water inlet of a refrigerator. Output water refrigerator is connected to the input of the first separator. The first output of the specified first separator configured to output the carrying amount of hydrocarbon, C1-C4(or, perhaps, hydrocarbon, C1-C4and hydrogen), as well as the feed mixture through a first compressor, before which can be input hydrogen or hydrogen-containing gas containing at least 85 vol.% hydrogen part of the above mentioned hydrocarbon, C1-C4(or, perhaps, part of the flow of hydrocarbons, C1-C4and hydrogen), isolated from the product stream by the method of vapor-liquid separation with mixture of hydrocarbons C3-C4with the stage of stabilization or to the backbone atlantabased raw materials. The second output of the specified first separator is connected through a fourth heat exchanger with the first choice of ademy through the second entrance back into the column, and partially removed from the installation. The second output of the specified columns for the separation of ethane is made with the possibility of a partial return to the column through the third input received unstable gasoline and supply the specified unstable gasoline through the fifth heat exchanger and the first entry in the stabilization column. The first stabilizer is made with the possibility of a partial refund of a mixture of hydrocarbons WITH3-C4(select top product of the column) through the second input of the stabilizer, as well as with the possibility of mixing the above-mentioned mixture of hydrocarbons with the product coming from the specified first compressor, and with the ability to obtain the target product are trademarks propane-butane fraction. The second output of the specified stabilizer configured to connect to the third input of the indicated stabilizer, and also to the input of the sixth heat exchanger. The output of the sixth heat exchanger connected to the first input of the rectifying column. The first specified output of the rectifying column is made with the possibility of a partial return to the specified distillation column downstream product (nonaromatic hydrocarbons WITH5-C6that is oduct, the second output of the specified distillation column made with the possibility of deducing basolateral faction as the target product, and also to the inlet of the hydrogenation unit, which used the entrance of the seventh heat exchanger, just before which has a second compressor. The third output of the specified distillation column made with the possibility of a partial refund of VAT residue (hydrocarbons gasoline7+in specified distillation column, and removing the specified VAT residue as the target product. The first output of the specified seventh heat exchanger is connected to the input of the second separator, the first output of which is connected to the first input of the eighth heat exchanger, and the second output to the input of the second compressor is connected to the supply line to the hydrogen or hydrogen-containing gas and the fuel line removing part of the hydrogen-containing gas. The second output of the specified seventh heat exchanger is connected to the input of the second furnace, the output of which is connected to the inlet of the reactor block hydrogenation, the output of which is connected to the second input of the seventh heat exchanger. The first output of the specified eighth heat exchanger padamu input specified Stripping columns and with the conclusion of the installation as an intermediate dissolved in the liquid hydrogenation product dissolved hydrogen containing gas. The second output of the specified Stripping columns made with the possibility of a partial refund in the specified column stable gidrirovannoe hydrocarbon fractions WITH6and partial filing specified gidrirovannoe hydrocarbon fractions WITH6to the second input of the eighth heat exchanger with subsequent flow through the second output of the eighth heat exchanger mixing with ethylenediurea fraction of raw materials. All connections between these elements of the unit, as well as money supply and output of raw materials, intermediates and products are made in the form of pipelines.

The method can also be implemented using the device, the design of which is given below. The specified device contains a first heat exchanger to the first input of which is connected the line atlantageorgia faction, highway fractions of gasoline reforming and highway recycle stream part of the hydrocarbon, C1-C4(or possibly part of the stream of hydrocarbon, C1-C4and hydrogen), allocated at the liquid-vapor separation of the cooled product stream, the first output of the specified first heat exchanger connected to the first input into the furnace, the first output of which is connected to the input of the first reactor, the output of cat is holodilniki. To the first input of the second heat exchanger is connected highway Propylenediamine faction, highway fractions of gasoline reforming and highway recycle stream part of the hydrocarbon, C1-C4(or, perhaps, part of the flow of hydrocarbons, C1-C4and hydrogen) that were selected during vapor-liquid separation and distillation of the cooled product stream, the first output of the specified second heat exchanger is connected with a second entrance into the furnace, a second output which is connected to the input of the second reactor, the output of which is connected with the second input of the second heat exchanger, the second output of which is connected with the inlet air cooler. To the first input of the third heat exchanger connected line butylenediamine faction, highway fractions of gasoline reforming and highway recycle stream part of the hydrocarbon, C1-C4(or, perhaps, part of the flow of hydrocarbons, C1-C4and hydrogen) that were selected during vapor-liquid separation and distillation of the cooled product stream, the first specified output of the third heat exchanger is connected with the third input to the furnace, the third output of which is connected to the input of the third reactor, the output of which is connected to a second input of the third Teploobmennik refrigerator. Output water refrigerator is connected to the inlet of the separator. The first outlet of the separator is configured to reset the carrying amount of hydrocarbon, C1-C4(or, perhaps, hydrocarbon, C1-C4and hydrogen), and is also connected through line flow part of the hydrocarbon, C1-C4(or stream part of the hydrocarbon, C1-C4and hydrogen), allocated at the liquid-vapor separation of the cooled product stream through the compressor, before which can be input hydrogen or hydrogen-containing gas containing at least 85 vol.% hydrogen to the highways atlantabased raw materials, as well as highways C3-C4hydrocarbons, selected at stabilization. The second output of the specified separator is connected through a fourth heat exchanger with the first inlet of the column separation of ethane, the first output of which is removed by a dry gas at least partially returned through the second entrance back into the column and partially removed from the installation. The second output of the specified columns for the separation of ethane is made with the possibility of a partial return to the column through the third input received unstable gasoline and transfer of the said unstable gasoline through the toe partial refund of the mixture of hydrocarbon, C3-C4(select top product of the column) through the second input of the stabilizer, as well as with the possibility of mixing the above-mentioned mixture of hydrocarbons with the product emerging from the above compressor, and with the ability to obtain the target product are trademarks propane-butane fraction. The second output of the specified stabilizer configured to connect to the third input of the indicated stabilizer, and also to the input of the sixth heat exchanger. The output of the sixth heat exchanger connected to the first input of the rectifying column. The first specified output of the rectifying column is made with the possibility of a partial return to the specified distillation column downstream product (nonaromatic hydrocarbon, C5-C4representing a component of gasoline), and output the specified head of product the target product, the second output specified distillation column made with the possibility of deducing basolateral faction as the target product, and summing the specified basolateral fraction to the first inputs of the first three heat exchangers. The third output of the specified distillation column made with vozmozhnostnogo VAT residue as the target product hydrocarbons gasoline7+. All connections between these elements of the unit, as well as money supply and output of raw materials, intermediates and products are made in the form of pipelines.

The first embodiment of the installation shown in Fig.1, the second variant of Fig.2.

In Fig. 1 the following notation: the first heat exchanger 1, to the first input of which is connected to the line 2 atlantageorgia faction, highway fractions of gasoline reforming unit 3, line 4 fractions hydrogenated WITH6product and line 5 of the flow of hydrocarbons, C1-C4(or stream of hydrocarbon, C1-C4and hydrogen), allocated at the liquid-vapor separation of the cooled product stream. The first output of the first heat exchanger 1 is connected to the first input of the first furnace 6, the first output of which is connected to the inlet of the first reactor 7, the output of which is connected by a pipe 8 with the input of the second reactor 9, the output of which is connected by a pipe 10 to the input of the third reactor 11, the output of which is connected by a pipe 12 with the second inlet of the first heat exchanger 1, and the first inputs of the second 13 and third heat exchangers 14. The second input of the second heat exchanger 13 is connected to the line is Ogorodov C1-C4(or hydrocarbon, C1-C4and hydrogen), allocated from the streams of products by the methods of vapor-liquid separation and distillation. The first outlet of the second heat exchanger 13 is connected to a second input of the specified first furnace 6 and through the second output of the specified first furnace 6 and the pipe 17 with the pipe 8 connecting the output of the first reactor 7 with the input of the second reactor 9. The second input of the third heat exchanger 14 is connected to the line 18 butylenediamine faction and highway 16 recycle stream representing a portion of the mixture of hydrocarbon, C1-C4(or hydrocarbon, C1-C4and hydrogen), isolated from the product stream by methods of vapor-liquid separation and distillation, the first specified output of the third heat exchanger 14 is connected to the third input of the specified first furnace 6 and through the third output of the specified furnace and duct 19 with the pipe 10 connecting the outlet of the second reactor 9 and the input of the third reactor 11. The second outputs of the first 1, the second 13 and third heat exchangers 14 are connected with the inlet air cooler 20, the output of which is connected to the water inlet of a refrigerator 21. Output water refrigerator 21 is connected to the input of the first separator 22. the number of C1-C4hydrocarbons (or, perhaps, hydrocarbon, C1-C4and hydrogen), and the feed pipe 25 of the flow of the mixture of hydrocarbon, C1-C4(or, perhaps, hydrocarbon, C1-C4and hydrogen), isolated from the product stream by the method of vapor-liquid separation through the first compressor 23 to highway 5 and further to the first input of the first 1 of the heat exchanger and to the highway 16 recycle stream C3-C4hydrocarbons with a mixture supplied to the first inputs of the second 13 and third heat exchangers 14. The second output of the specified first separator 22 is connected through a fourth heat exchanger 26 to the first input 27 column 28 Department of ethane, on the first output 29 which removes dry gas at least partially returned through the second inlet 30 back to the column 28, and partially removed from the column separation of ethane. The second output 31 of the specified column 28 Department of ethane is made with the possibility of a partial return to the column through the third entrance 32 get unstable gasoline and supply the specified unstable gasoline through the fifth heat exchanger 33 and the first inlet 34 in the stabilization of the column 35. The first output 36 of the stabilizer 35 is made from cosmogony) through the second inlet 37 stabilizer 35, and feed this mixture through the pipeline 16 for mixing the above-mentioned mixture of hydrocarbons in the product going through the pipeline 25 from the first specified output of the first separator 22, and with the ability to obtain the target product are trademarks propane-butane fraction. The second output 38 of the indicated stabilizer 35 is arranged to connect to the third input 39 of the indicated stabilizer 35 and to the input of the sixth heat exchanger 40. The output of the sixth heat exchanger 40 is connected to the first input 41 of the distillation column 42. The first output 43 of the specified rectification column 42 is made with the possibility of a partial return to the specified distillation column 42 of the head product (nonaromatic hydrocarbons WITH5-C6representing a component of gasoline), and output the specified head of product the target product, the second output 44 of the specified rectification column 42 is arranged to derive basolateral faction as the target product, and supply the specified basolateral fraction to the inlet of the hydrogenation unit 45, which used the entrance of the seventh heat exchanger 46, directly the partial refund VAT residue in the distillation column 42 through its third input 49, and specified output VAT residue as the target product (hydrocarbon gasoline7+). The first output of the specified seventh heat exchanger 46 is connected to the input of the second separator 50, the first output of which is connected to the first input of the eighth heat exchanger 51, and the second outlet of the second separator 50 through the second compressor 47 by a pipe 52 to the first input of the seventh heat exchanger 46, is connected to the line 53, the supply of hydrogen or hydrogen-containing gas and highway 54 delete the carrying amount of the hydrogen-containing gas. The second output of the specified seventh heat exchanger 46 is connected to the input of the second furnace 55, the output of which is connected to the reactor inlet 56 hydrogenation unit 45, the output of which is connected to the second input of the seventh heat exchanger 46. The first output of the specified eighth heat exchanger 51 is connected to the first input 57 Stripping column 58, the first output 59 which is arranged to connect it to a second input 60 of the specified Stripping columns 58 and with the possibility of the conclusion of the installation as an intermediate dissolved in the liquid hydrogenation product dissolved hydrogen containing gas. The second output 61 of the specified Stripping column 58 is made with vozmozhnoye partial submission specified gidrirovannoe hydrocarbon fractions WITH6to the second input of the eighth heat exchanger 51 and subsequent flow through the second outlet of the heat exchanger her mixing with ethylenediurea fraction of raw materials. Between the first output of the first separator and the inlet of the first compressor can be summed up highway 62 supply of hydrogen or hydrogen-containing gas (hydrogen content not less than 85 vol%).

All connections between these elements of the unit, as well as money supply and output of raw materials, intermediates and products are made in the form of pipelines.

The second implementation of the device shown in Fig.2. In Fig.2 elements present in Fig.1, are denoted by the same positions. The device comprises a first heat exchanger 1, to the first input of which is connected to the line 2 atlantageorgia faction, line 3 fractions of gasoline reforming and highway 5 flow of hydrocarbon, C1-C4(or stream of hydrocarbon, C1-C4and hydrogen), allocated at the liquid-vapor separation of the cooled product stream, the first output of the specified first heat exchanger 1 is connected to the first input of the furnace 6, the first output of which is connected to the input of the first reactor 7, the output of which is connected with the second input of the first heat exchanger 13 is connected to the line 15 Propylenediamine faction, highway 3 fractions of gasoline reforming and highway 16 flow of hydrocarbon, C1-C4(or stream of hydrocarbon, C1-C4and hydrogen) that were selected during vapor-liquid separation and distillation of the cooled product stream, the first output of the specified second heat exchanger 13 is connected with the second input to the furnace 6, the second output of which is connected to the input of the second reactor 9, the output of which is connected with the second input of the second heat exchanger 13, the second output of which is connected with the inlet air cooler 20. To the first input of the third heat exchanger 14 is connected to the line 18 butylenediamine faction, line 3 fractions of gasoline reforming and highway 16 flow of hydrocarbon, C1-C4(or stream of hydrocarbon, C1-C4and hydrogen) that were selected during vapor-liquid separation and distillation of the cooled product stream, the first specified output of the third heat exchanger 14 is connected with the third input to the furnace 6, the third output of which is connected to the input of the third reactor 11, the output of which is connected to a second input of the third heat exchanger 14, the second output of which is connected with the inlet air cooler 20, the output of which is connected to the water inlet of a refrigerator 21. Output leading the through line 24 carrying amounts of hydrocarbon, C1-C4(or, perhaps, hydrocarbon, C1-C4and hydrogen), and is also connected through line 25 flow of hydrocarbon, C1-C4(or, perhaps, hydrocarbon, C1-C4and hydrogen), allocated at the liquid-vapor separation of the cooled product stream through the compressor 23 to highway 5 and further to the first input of the first 1 of the heat exchanger and to the highway 16 recycle stream C3-C4hydrocarbons with a mixture supplied to the first inputs of the second 13 and third heat exchangers 14. The second output of the specified separator 22 is connected through a fourth heat exchanger 26 to the first input 27 column 28 Department of ethane, on the first output 29 which removes dry gas at least partially returned through the second inlet 30 back to the column 28, and partially removed from the column separation of ethane. The second output 31 of the specified column 28 Department of ethane is made with the possibility of a partial return to the column through the third entrance 32 get unstable gasoline and supply the specified unstable gasoline through the fifth heat exchanger 33 and the first inlet 34 in the stabilization of the column 35. The first output 36 of the stabilizer 35 is made with the possibility of partial vozvrachaietsia columns 35, and feed this mixture through the pipeline 16 for mixing the above-mentioned mixture of hydrocarbons in the product going through the pipeline 25 from the first output of the specified separator 22 through the compressor 23, and also with the ability to obtain the target product are trademarks propane-butane fraction. The second output 38 of the indicated stabilizer 35 is arranged to connect to the third input 39 of the indicated stabilizer 35 and to the input of the sixth heat exchanger 40. The output of the sixth heat exchanger 40 is connected to the first input 41 of the distillation column 42. The first output 43 of the specified rectification column 42 is made with the possibility of a partial return to the specified distillation column 42 of the head product (nonaromatic hydrocarbon, C5-C6representing a component of gasoline), and output the specified head of product the target product, the second output 44 of the specified rectification column 42 is arranged to derive basolateral faction as the target product, and supply the specified basolateral faction mixing with atelosteogenesis, Propylenediamine and butylenediamine raw materials to master knogo return VAT residue in the distillation column 42 through its third input 49, and specified output VAT residue as the target product hydrocarbons gasoline7+. Between the first outlet of the separator 22 and the inlet of the compressor 23 can be further summed up highway 62 supply of hydrogen or hydrogen-containing gas (hydrogen content not less than 85 vol%). All connections between these elements of the unit, as well as money supply and output of raw materials, intermediates and products are made in the form of pipelines.

In the described process of distillation columns operate in the usual way, so the equipment that makes them hot and cold irrigation, and other pumps in the diagrams (Fig.1 and Fig.2) not shown.

The table below shows the outputs of the transformation products registergui fractions and their mixtures with benzene product fraction reforming, wikipeida to 85oWith, at the same time the contact of the feedstock with the catalyst.

The composition of the raw material used is the following:

the ethane-ethylene fraction /EEF/ - C2H4of 51.2% m,2H6- 48,8% m;

propane-propylene fraction /PPF/ - C3H6- 51,6 % m,3H8- 29,2% m,4H10- 19,2% m;

the butane-butylene fraction /BBF/ - C4H

For mixing with PPF and BBF use a fraction of the gasoline reforming, containing 21.9% of m benzene, 8,9%5H12, 57,4%6H14, 12,8%7H14.

For mixing with EEF use a fraction of the gasoline reforming, containing 42% of benzene and 58% WITH6H14. In experiments carried out by the contact of the feedstock with the catalyst 1, comprising 70% of the group zeolite WHC (see B. K. Nefedov. Chemistry and technology of fuels and oils, 1992, 3, page 4) /contents Na2O less than 0.1%, SiO2/Al2ABOUT3=71 mol/mol, 1.5% of ZnO and 28.5% -Al2O3;; catalyst 2 comprising 70% of the group zeolite DCM (see B. K. Nefedov. Chemistry and technology of fuels and oils, 1992, 3, page 36) /the content of Na2O 0,15%, SiO2/Al2O3=28 mol/mol, 30% -Al2O3; catalyst 3, which includes 65% zeolite DCM /content Na2O 0,11%, SiO2/Al2O3=39 mol/mol, 3 % IN2O3, 27% -Al2O3and filling the rest.

The obtained results show that the transformation registertimer raw materials, including benzene fraction products of reforming, flows with a higher selectivity for hydrocarbons gasoline5+and with reduced selectivity on ug is Dagenham method of obtaining high-octane gasoline in a stationary layer of zeolite-containing catalyst is improved transformation registertimer raw material at a known improvement of the quality of liquid products of catalytic reforming (decrease content of highly toxic benzene, the content of which is limited in modern motor gasoline).

1. Method of producing high octane gasoline comprising a material containing at least one olefin WITH2-C4in the reaction zone to a stationary acid catalyst based on the group zeolite, conducting the oligomerization reaction received olefin feedstock to obtain a product stream containing hydrocarbons gasoline5+separation of the specified product stream from the production of gasoline and flow of hydrocarbons FROM1-C4followed by mixing the specified flow of hydrocarbons FROM1-C4with the raw material, characterized in that it further feedstock containing olefins, mixed with wikipeida at a temperature not exceeding 85oA fraction of a gasoline reformer containing benzene, and the ratio of olefin/benzene in the final mixture is at least 0.5 mol/mol, and found the oligomerization reaction is carried out in conditions providing the alkylation of at least part of the benzene.

2. The method according to p. 1, characterized in that the fraction of gasoline reforming, containing benzene, mixed containing raw materials including ethylene, and is carried out so in the first zone with a catalyst interacts raw material containing ethylene, the resulting interaction in the first zone, the product stream is additionally mixed with a raw material containing propylene and/or butylenes, the resulting mixture was fed to the second reaction zone, the temperature of the raw material input in the first area is higher than the temperature of the mixture at the entrance to the second area.

3. The method according to p. 1, characterized in that the fraction of gasoline reforming, containing benzene, mixed containing raw materials including ethylene, and the interaction of this material with the specified catalyst is carried out in three zones of the reaction, and the reaction is carried out in such a way that in the first zone with a catalyst interacts raw material containing ethylene, the resulting interaction in the first zone, the product stream is additionally mixed with a raw material containing propylene, and the resulting mixture was fed to the second reaction zone, resulting from the interaction in the second zone, the product stream is additionally mixed with a raw material containing butylene, and serves the resulting mixture in a third reaction zone, the temperature of the raw material at the entrance to the reaction zone reduces from the first zone to the third zone.

4. The method according to p. 1, distinguished by the defined zones of interaction with further mixing the obtained products.

5. The method according to any of paragraphs.1-4, characterized in that the resulting process stream products is additionally divided obtaining hydrocarbon fractions WITH6containing benzene, with subsequent mixing of the obtained fractions or parts of it with raw materials, at least one of the reaction zones.

6. The method according to p. 5, characterized in that a specified fraction of hydrocarbons WITH6containing benzene, before mixing with the raw material hydronaut in the conditions of the selective hydrogenation of olefins.

7. The method according to any of paragraphs.1-6, characterized in that fed into the heat exchangers of the original components are additionally injected hydrogen or hydrogen-containing gas in which the hydrogen content is not less than 85 vol.%.

8. Device for producing high-octane gasoline containing eight heat exchangers, four reactors, two furnaces, two separator, two compressors, air cooler, water cooler, column separation of ethane, stabilization column, distillation column and a Stripping column, and to the first input of the first heat exchanger is connected highway atlantageorgia faction, highway stream1-C4hydrocarbons extracted from the CSO first heat exchanger connected to the first input in the first furnace, the first output of which is connected to the input of the first reactor, the output of which is connected by a pipe with the inlet of the second reactor, the output of which is connected by pipeline to the input of the third reactor, the output of which is connected by a pipeline with the second inlet of the first heat exchanger, and the first inputs of the second and third heat exchangers, the second input of the second heat exchanger is connected to the line Propylenediamine fraction and the highway recycle stream1-C4hydrocarbons separated from the product stream by methods of vapor-liquid separation and distillation, the first outlet of the second heat exchanger is connected to a second input of the specified first furnace and the second output of the specified first furnace and duct with tubing connecting the outlet of the first reactor with the inlet of the second reactor, the second input of the third heat exchanger is connected to the line butylenediamine fraction and the highway recycle stream1-C4hydrocarbons separated from the product stream by methods of vapor-liquid separation and distillation, the first specified output of the third heat exchanger is connected to the third input of the specified first furnace and through the third output of the specified furnace, battery, speaker, buzzer which of the first and third heat exchangers are connected with the inlet air cooler, the output of which is connected to the water inlet of a refrigerator, the output water of the refrigerator is connected to the input of the first separator, the first output of the first separator is configured to reset the carrying amount of the flow of hydrocarbons FROM1-C4and also submission of this flow through the first compressor to mix with the stream WITH a3-C4hydrocarbons of the stabilizer and to the backbone atlantabased raw materials, the second output of the specified first separator is connected through a fourth heat exchanger with the first inlet of the column separation of ethane, the first output of which is removed by a dry gas at least partially returned through the second entrance back into the column and partially removed from the installation, the second output of the specified columns for the separation of ethane is made with the possibility of a partial return to the column through the third input received unstable gasoline and transfer of the said unstable gasoline through the fifth heat exchanger and the first entry in the stabilization column, the first stabilizer is made with the possibility of a partial refund of a mixture of hydrocarbons WITH3-C4through the second entrance back in the stabilization column, and from vozmojnostiami, and with the possibility of partial removal of the above-mentioned mixture of hydrocarbons as a trademark propanebutane fraction, the second output of the specified stabilizer configured to connect to the third input of the indicated stabilizer, and also to the input of the sixth heat exchanger, the output of the sixth heat exchanger connected to the first input of the rectifying column, the first specified output of the rectifying column is made with the possibility of a partial return to the specified distillation column downstream of the product, and displaying the head of product the target product, which represents a nonaromatic hydrocarbons WITH5-C6gasoline fraction, the second output specified distillation column made with the possibility of deducing basolateral faction as the target product, and summing the specified basolateral fraction to the inlet of the hydrogenation unit, which used the entrance of the seventh heat exchanger, just before which has a second compressor, a third output specified distillation column made with the possibility of a partial refund of VAT residue in the specified distillation column, and also in the gasoline fraction hydrocarbons, the first specified output of the seventh heat exchanger is connected to the input of the second separator, the first output of which is connected to the first input of the eighth heat exchanger, and a second output connected to the input of the second compressor is connected to the backbone removal of part of the hydrogen containing gas and the supply line to the hydrogen or hydrogen-containing gas, the second output of the specified seventh heat exchanger is connected to the input of the second furnace, the output of which is connected to the inlet of the reactor block hydrogenation, the output of which is connected to the second input of the seventh heat exchanger, the first output of the specified eighth heat exchanger connected to the first input of the Stripping column, the first output of which is configured to connect it to a second input of the specified Stripping columns and with the conclusion of the installation dissolved in the liquid hydrogenation product of hydrogen containing gas, the second output of the specified Stripping columns made with the possibility of a partial refund in the specified column stable gidrirovannoe hydrocarbon fractions WITH6and partial filing specified gidrirovannoe hydrocarbon fractions WITH6to the second input of the eighth heat exchanger with subsequent supply che the STW under item 8, characterized in that between the first output of the first separator and the inlet of the first compressor additionally summed up the supply line to the hydrogen or hydrogen-containing gas.

10. Device for producing high-octane gasoline containing six heat exchangers, three reactor, furnace, air cooler, water cooler, separator, compressor, column separation of ethane, stabilization column and distillation column, and to the first input of the first heat exchanger is connected highway atlantageorgia faction, highway stream1-C4hydrocarbons separated from the product stream when the liquid-vapor separation and highway fractions of gasoline reforming, the first output of the specified first heat exchanger connected to the first input into the furnace, the first output of which is connected to the input of the first reactor, the output of which is connected with the second input of the first heat exchanger, the second output of which is connected with the inlet air cooler, to the first input of the second heat exchanger is connected highway Propylenediamine faction, highway recycle stream1-C4hydrocarbons separated from the product stream by methods of vapor-liquid separation and rectifica is the second entrance into the furnace, the second output of which is connected to the input of the second reactor, the output of which is connected with the second input of the second heat exchanger, the second output of which is connected with the inlet air cooler, to the first input of the third heat exchanger connected line butylenediamine faction, highway recycle stream1-C4hydrocarbons separated from the product stream by methods of vapor-liquid separation and distillation, and the backbone fraction of gasoline reforming, the first specified output of the third heat exchanger is connected with the third input to the furnace, the third output of which is connected to the input of the third reactor, the output of which is connected to a second input of the third heat exchanger, the second output of which is connected with the inlet air cooler, the output of which is connected to the water inlet of a refrigerator, the output water of the refrigerator is connected to the inlet of the separator, a first outlet of the separator is configured to reset the carrying amount of the flow of hydrocarbons FROM1-C4and also submission of this flow through the compressor on the mix with the flow of hydrocarbons FROM3-C4of the stabilizer and to the backbone atlantabased raw materials, the second output of the specified separator connection is dilaut dry gas, at least partially returned through the second entrance back into the column and partially removed from the installation, the second output of the specified columns for the separation of ethane is made with the possibility of a partial return to the column through the third input received unstable gasoline and transfer of the said unstable gasoline through the fifth heat exchanger and the first entry in the stabilization column, the first stabilizer is made with the possibility of a partial refund of a mixture of hydrocarbons WITH3-C4through the second entrance back in the stabilization column, and with the possibility of mixing the above-mentioned mixture of hydrocarbons with the product emerging from said compressor, and partial removal of the above-mentioned mixture WITH3-C4hydrocarbons from the unit as the target product, representing commodity propane-butane fraction, the second output of the specified stabilizer configured to connect to the third input of the indicated stabilizer, and also to the input of the sixth heat exchanger, the output of the sixth heat exchanger connected to the first input of the rectifying column, the first specified distillation column made golovnogo product as the target product, represents a nonaromatic hydrocarbons WITH5-C6gasoline fraction, the second output specified distillation column made with the possibility of deducing basolateral faction as the target product, and summing the specified basolateral faction to highways atlantabased, Propylenediamine and butylenediamine raw materials, respectively, the third output specified distillation column made with the possibility of a partial refund of VAT residue in the distillation column through its third input, and output the specified VAT residue as the target product, representing a7+the gasoline fraction hydrocarbons.

11. The device according to p. 10, characterized in that between the first outlet of the separator and the inlet of the compressor additionally summed up the supply line to the hydrogen or hydrogen-containing gas.

 

Same patents:

The invention relates to the production of motor fuels and can be used in refining and petrochemical industries

The invention relates to the field of production of high-octane mixtures

The invention relates to the field of production of oligomers for organic synthesis, in particular for the production alkylphenolic additives, plasticizers plastics, non-ionic detergent and additives to oils

The invention relates to methods of producing oligomers of lower olefins during gas-liquid oligomerization of olefins from ethylene, propane, propylene and butane-butylene gas fractions or mixtures thereof and can be used in the petrochemical industry

The invention relates to the production of high-octane components of gasoline from alkenes C3-C5

The invention relates to the field of production of high-octane gasoline components and their mixtures

The invention relates to a method of isomerization of the carbon skeleton of olefins

The invention relates to fluorine-containing morgentau the catalyst and its use for the manufacture of linear alkyl benzene (LAB) by alkylation of benzene with olefins

The invention relates to a method for producing alkyl benzenes by the alkylation of benzene alkylating agent in the presence of a catalyst is aluminum chloride when heated, and as the alkylating agent used monoolefinic and periodic process of alkylation is carried out in a period of 10-40 min at a constant flow of catalyst, the adiabatic temperature rise 35-40oWith up to 50-70oWith, and simultaneously adjustable cooling the reaction mass with water

The invention relates to a method for selective receipt of paraxylene, which includes the interaction of toluene with methanol in the presence of a catalyst containing a porous crystalline aluminosilicate zeolite having a diffusion parameter for 2,2-Dimethylbutane about 0.1-15 sec-1measured at a temperature of 120oC and a pressure of 2.2-Dimethylbutane (8 kPa)

The invention relates to a method of the reaction distillation and apparatus for the alkylation of benzene with a liquid olefin or mixture of olefin-paraffin

The invention relates to a method for producing linear alkyl benzenes, which are intermediates and are used in the manufacture of detergents

The invention relates to a method for converting the processed material containing heavy aromatic compounds, in particular C9+ aromatic compounds to lighter aromatic products, in particular xylenes

The invention relates to methods of producing oligomers of lower olefins during gas-liquid oligomerization of olefins from ethylene, propane, propylene and butane-butylene gas fractions or mixtures thereof and can be used in the petrochemical industry
Up!