WO2008024012A1 - Procédé de fabrication de composants de carburants pour moteurs - Google Patents

Procédé de fabrication de composants de carburants pour moteurs Download PDF

Info

Publication number
WO2008024012A1
WO2008024012A1 PCT/RU2006/000443 RU2006000443W WO2008024012A1 WO 2008024012 A1 WO2008024012 A1 WO 2008024012A1 RU 2006000443 W RU2006000443 W RU 2006000443W WO 2008024012 A1 WO2008024012 A1 WO 2008024012A1
Authority
WO
WIPO (PCT)
Prior art keywords
hydrogenation
products
hydrogen
hydrocarbons
content
Prior art date
Application number
PCT/RU2006/000443
Other languages
English (en)
Russian (ru)
Inventor
Alexandr Sergeevich Bely
Dmitry Ivanovich Kiryanov
Vladimir Vladimirovich Pashkov
Mikhail Dmitrievich Smolikov
Vladimir Alexandrovich Likholobov
Original Assignee
Institut Problem Pererabotki Uglevodorodov Sibirskogo Otdeleniya Rossiiskoi Akademii Nauk
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Institut Problem Pererabotki Uglevodorodov Sibirskogo Otdeleniya Rossiiskoi Akademii Nauk filed Critical Institut Problem Pererabotki Uglevodorodov Sibirskogo Otdeleniya Rossiiskoi Akademii Nauk
Priority to PCT/RU2006/000443 priority Critical patent/WO2008024012A1/fr
Publication of WO2008024012A1 publication Critical patent/WO2008024012A1/fr

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G69/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process
    • C10G69/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only
    • C10G69/08—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only including at least one step of reforming naphtha
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
    • C10G45/44—Hydrogenation of the aromatic hydrocarbons
    • C10G45/46—Hydrogenation of the aromatic hydrocarbons characterised by the catalyst used
    • C10G45/52—Hydrogenation of the aromatic hydrocarbons characterised by the catalyst used containing platinum group metals or compounds thereof
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
    • C10G45/58—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins

Definitions

  • the invention relates to the production of environmental high-octane components of motor fuels from gasoline fractions of oil and gas condensate origin and can be used in the refining, petrochemical and gas processing industries.
  • the disadvantage of all known methods of processing gasolines such as reforming, reforming, selectoforming and the like is to obtain C 5+ high-processed products with a high content of environmentally hazardous aromatic hydrocarbons.
  • the content of aromatic hydrocarbons with an octane number of reformate of 93 p. (MI) is 60-62 wt.%, And with an octane number of 95 p. - 64-65 wt.%, which significantly exceeds the European standards Euro-3 and 4 in terms of toxicity of exhaust gases from auto-exhaust emissions of internal combustion engines.
  • Gasoline production technologies for cars meeting the requirements of Euro-3 and Euro-4 should ensure that the standards for the content of aromatic hydrocarbons are not more than 42 and 35 wt.%, Respectively.
  • the benzene content should not exceed 1.0 vol.% (E.A. Nikitina, V.A. Emelyanov, E.A. Aleksondrova / Market of products and technologies, -NbI, 28-
  • the resulting mixture of gases (hydrogen and C 1 -C 4 hydrocarbon gases) is subjected to separation by binding (absorption) of hydrogen upon contact with aromatic hydrocarbons in the catalytic hydrogenation zone, after which the liquid hydrogenation products (cyclohexane hydrocarbons) are separated from C 1 - C 4 - hydrocarbon gases.
  • the latter is recycled to the biforming zone.
  • C 1 -C 4 - hydrocarbon gases are continuously recycled in a closed system from the hydrogenation zone to the biforming zone and vice versa without removing them from the process.
  • An additional amount of C 1 -C 4 hydrocarbon gas is supplied to the recycle gas stream from an external source.
  • the rate of hydrogen binding in the hydrogenation zone is maintained equal to the rate of hydrogen evolution in the biforming zone.
  • C 5+ - reforming catalysis containing a mixture of paraffin-naphthenic and aromatic hydrocarbons, is mixed with hydrogen-containing reforming gas (HSG) and sent to a hydrogenation reactor with a catalyst containing platinum group metal (s), where at a temperature of more than 35O 0 C and pressure not less than 0.35 MPa, aromatic hydrocarbons undergo hydrogenation and turn into saturated hydrocarbons cyclohexane series, as a result of which the content of aromatic hydrocarbons in the C 5+ product is less than 40 wt.%.
  • the resulting hydrocarbons of the cyclohexane series are among the environmentally friendly high-octane components.
  • Table 1 shows a typical composition and octane numbers of aromatic hydrocarbons of the C 5+ reforming catalyst.
  • the octane number of the aromatic hydrocarbon reformate catalysis mixture is 124.5 ⁇ . (MI), which indicates their main contribution to the increase in the octane number of the product during its reforming.
  • Table 2 shows the composition and octane characteristics of the hydrogenation products of the C 5+ reforming catalyst. Table 2.
  • the octane numbers of the products of hydrogenation of the mixture of aromatic hydrocarbons of the Cs + reforming catalyst reach quite high values, which opens up the possibility of their use in the proposed method as one of the main components of environmental motor fuels. Due to the difference in the octane characteristics of aromatic and cycloalkane hydrocarbons, the octane numbers of their mixture are a function of the degree of conversion in the hydrogenation reactions.
  • a significant reduction in the content of aromatic hydrocarbons in the proposed method can be achieved with a hydrogenation depth of at least 40%.
  • a hydrogenation depth of at least 40%.
  • octane characteristics have values attractive for the use of mixtures as environmental components of motor fuels.
  • An attractive technical result of the proposed method is also an increase in the yield (mass) of C 5+ -extracted products due to the addition of three moles of hydrogen per mole of aromatic hydrocarbons involved in hydrogenation.
  • the increase in yield is from 3.5 to 7.0 wt.% Calculated on the mixture of aromatic hydrocarbons supplied to the hydrogenation zone.
  • the reforming catalyst obtained in a known manner has an octane number of 95.8 p. IM with an aromatic hydrocarbon content of 60.1 wt.%.
  • the hydrogenated product of the reformate obtained by the proposed method has an octane number of 92.1 p. IM with an aromatic hydrocarbon content of 38.2 wt.%.
  • the product of hydrogenation of the catalysis is separated from the WASH and removed from the process as a high-octane environmental component of motor fuel.
  • Another significant feature of the proposed method for the production of motor fuel components is the supply of C 1 - C 4 - enriched WGH hydrogens and mixtures of Cs + -hydrocarbons from the hydrogenation zone to the n-paraffin hydrodewaxing (selective cracking) zone.
  • C 5+ n-paraffins on a bifunctional catalyst are converted to C 3 -C 4 hydrocarbon gases, as a result of which the content of low-octane C 5+ n-paraffins decreases from 10-15 to 5-7 wt.%, And the octane number of C 5+ products increases.
  • An increase in the degree of conversion of n-alkanes in the hydrodewaxing zone of the proposed method for producing motor fuel components contributes to an increase in the octane number of the paraffin hydrocarbon mixture from 55.2 to 69.2 p.IM.
  • Table 7 shows data on the composition and characteristics of the hydrogenation products and its selective cracking.
  • the catalyst for the process of selective cracking of hydrogenated reformate products obtained by the proposed method has a high octane number (95.7 p. IM) with an aromatic content of 39.7 wt.%.
  • the product of selective cracking of n-alkanes of the reformate hydrogenation products after separation of the C 5+ product from the WASH reforming is withdrawn as the target ecological component.
  • Another significant feature of the proposed method for producing environmental components of motor fuels is the supply of a high-octane catalysis to the hydrogenation zone of the well-known biforming process - the process of joint processing of Si-Q hydrocarbon gases and gasoline fractions into high-octane components of motor fuels (RU 2144056, ClOG 63/02, 10.01 / 2000).
  • Table 8 shows data on the composition and characteristics of raw materials, biforming products and their hydrogenation products.
  • the C 5+ product of hydrogenation of catalytic reforming is removed from the process as the target environmental component of motor fuels.
  • the efficiency of the process expressed in octane tons of the obtained product, is 90.4 per one ton of refined gasoline (Table 8) and significantly exceeds the efficiency of the known reforming process (84.3, Table 4).
  • the main technical result of the proposed method is to obtain an environmental high-octane (93.1 p.IM) component of motor fuels with a low content of aromatic hydrocarbons (not more than 40%), which meets the requirements of the Euro-3 standard.
  • Another variant of the proposed method for the production of environmental motor fuels is a variant of the process technology in which a mixture of SHG and C 5+ biformate hydrogenation products is sent to a reactor with a catalyst for selective hydrocracking of n-paraffins in order to further increase the octane number of the hydrogenation product.
  • Table 9 shows the characteristics and compositions of the hydrogenation products and their selective hydrocracking. Table 9.
  • the WASH is separated from the C 5+ -producted component and recycled to the biforming zone.
  • Hydrocarbon gases in the composition of the WGH which are a mixture of dC 4 -saturated gases, enter into joint transformations with high molecular weight hydrocarbons of gasoline fractions and turn into C 5+ -producted products, which significantly increases the yield of C 5+ products of hydrogenation of the catalyst for their reforming and selection cracking. Together, this ensures a decrease in the yield from the process of by-products, low-value light hydrocarbon gases, mainly methane and ethane, in comparison with the known methods for producing high-octane components.
  • the third and the fourth options of the proposed method can be attributed to the category of resource-saving technologies.
  • fractions of reforming or reforming catalysts that boil off at temperatures of 36-102 0 C are sent to the hydrogenation zone.
  • Light fractions of gasoline reforming products contain up to 10-15 wt.% Benzene and, for this reason, are unwanted, environmentally hazardous components.
  • the total content of aromatic hydrocarbons is more than 30%, and the content of low-octane n-paraffins is also high and reaches 20 wt.% (Table 10).
  • light fractions have significantly lower octane numbers compared to wide fractions (NK - 102 0 C, KK - 200 0 C) C 5+ catalysts for reforming and reforming.
  • Table 10 shows the characteristics and compositions of the light fractions, as well as the products of their hydrogenation and selective cracking.
  • the C 5+ reforming and reforming catalysts are separated from the WASH and sent to distillation column.
  • On top of the column output C 1 -C 4 -FaSbI stabilization.
  • Fraction 36-102 0 C is withdrawn as the upper side stream, mixed with WASH and sent to the hydrogenation zone.
  • Deep hydrogenation of benzene and toluene takes place in the hydrogenation reactor to form high-octane cyclohexane (110 p. IM) and methylcyclohexane (104 p. IM).
  • the content of aromatic hydrocarbons decreases from 36 to 2.3 wt.%.
  • the octane number of the product decreases slightly and amounts to 79.5 p.IM.
  • the C 5+ reforming or reforming catalysts are separated from the WASH and sent to the selectoforming reactor.
  • Selectoforming products are sent for separation, C 1 - C 4 - hydrocarbon gases are removed from the unit and (or) sent for recycling to the biforming zone.
  • Liquid products (C 5+ - catalysate) are mixed with VASH and sent to the hydrogenation zone. Hydrogenation of aromatic hydrocarbons with the formation of cyclohexane hydrocarbons takes place in the hydrogenation reactor; the hydrogenation depth depends on the conditions and can range from 10 to 90%. Table 11 presents the results of the reformofate reforming and hydrogenation of liquid products.
  • the proposed method solves an important environmental problem of reducing the content of aromatic hydrocarbons in motor fuels.
  • the raw material of the process is straight-run gasoline fractions of oil and gas condensate origin, boiling off at temperatures of 85-185 0 C, with a sulfur content of not more than 0.5 mg / kg.
  • Example 1 illustrates a known method for the catalytic reforming of gasoline fractions.
  • a catalyst is loaded into the reactor containing, in May,%: platinum — 0.2 ;, rhenium — 0.3; zirconium - 0.3; chlorine - 1.2; aluminum oxide - the rest is up to 100.
  • the catalyst is reduced with hydrogen and grained by known methods.
  • the recovered catalyst contains 0.07 wt.%. sulfur.
  • Raw materials, fraction 85-185 0 C with a density of 0.742 kg / l are fed into the reactor at a rate of 150 ml / hour.
  • Example 2 illustrates the proposed method for producing an environmental component of motor fuel (option 1).
  • the mixture of selective cracking products is cooled to a temperature of not more than 3O 0 C and separated into liquid and gaseous.
  • Liquid C 5+ hydrogenation and selective cracking products are removed from the process as an environmental component of motor fuels. Yield, wt.%: C 5+ products is 83, C 1 -C 2 -CyXOrO gas is 8.8, C 3 -C 4 is 8.0, hydrogen is 0.2.
  • the octane number of the selectocracking catalysis is 96.9 p. IM with an aromatic hydrocarbon content of 38 wt.%.
  • Raw materials, fraction 85-185 0 C, are fed to the reforming reforming reactor at a rate of 150 l / h.
  • the reaction products are cooled to a temperature of not more than 3O 0 C and separated in a Cl separator into C 5+ products and gaseous (SHG).
  • Gaseous products containing hydrogen (80%) and light hydrocarbon gases (20%) are mixed with toluene, heated to 25O 0 C and fed to the hydrogenation reactor P4, where hydrogen is bound in the toluene hydrogenation reaction to form methylcyclohexane.
  • the reaction products are cooled to a temperature of not more than 3O 0 C and sent to the separator C2. In the separator, QQ gases and hydrogen are separated from methylcyclohexane.
  • the WASH is recycled to the biforming zone.
  • the conditions in the P-4 hydrogenation reactor are maintained so that the rate of hydrogen binding therein is equal to the rate of hydrogen evolution in the biforming reactor.
  • the WASH is enriched with C 1 -C 4 hydrocarbon gases up to 50 vol.%, which ensures the conversion of the latter into C 5+ -producted products.
  • the hydrocarbon gas generated in the process is not removed from the process as a by-product.
  • Hydrocarbon gas circulates in a closed system through a biforming and hydrogenation reactor, and its components are converted to C 5+ - high-octane products.
  • C 5+ products are stabilized and removed from the process as the target product.
  • the yield of C 5+ products is 95% based on raw materials.
  • the octane number is 98 p. IM with an aromatic content of 64.3 wt.%.
  • the resulting methylcyclohexane is sent to the dehydrogenation reactor P5 (Fig. 1), where a dehydrogenation reaction is carried out with the formation of toluene and hydrogen. Pure hydrogen is removed from the process, and toluene is recycled to the hydrogenation zone to bind hydrogen.
  • Example 5 illustrates the proposed method for producing environmental components of motor fuels (option-3) (Fig. 2).
  • the process is carried out as described in example 4. The difference is as follows.
  • the high-octane C 5+ product, containing 64.3 wt.% Aromatic hydrocarbons, is not removed from the process as the target product, but is mixed with the WASH and sent to the P4 hydrogenation reactor.
  • P4 is the binding and extraction of hydrogen from the composition of the WASH.
  • high-octane hydrocarbons of a number of cyclohexane homologues are formed, which, together with part of the unreacted aromatic and paraffinic hydrocarbons, are removed from the process as the target high-octane component.
  • the content of aromatic hydrocarbons decreases from 64.3 to 34.0 wt.%.
  • the yield of C 5+ products increases from 95 to 97 wt.%.
  • the octane number of hydrogenation products is 93 p.IM.
  • such a constant source is a biforming unit.
  • the process is carried out as described in example 5. The difference is as follows.
  • the products of C 5+ hydrogenation and enriched with C 1 -C 4 -hydroxides of the WASH are not separated, but heated to 35O 0 C and fed to the P-5 reactor for selective hydrocracking of n-paraffins.
  • a catalyst is used in the reactor, comprising: molybdenum trioxide - 8.0 wt.%, zeolite of the Fojasit type RZES-Y - 5.0 wt.%, as well as palladium-containing high-silica zeolite of the pentasil type with a palladium content of 0.5 wt.% in the amount of 35 wt.% and aluminum oxide - the rest is up to 100%.
  • the process of selective hydrocracking is carried out at a pressure of VSG
  • the mixture of selective cracking products is cooled to a temperature of not more than 3O 0 C and separated into liquid and gaseous hydrocarbons.
  • Hydrocracking reactions of n-paraffins take place in the selectocracking reactor, as a result of which the content of low-octane n-paraffins decreases from 10 to 5 wt.%, The octane number of C 5+ products increases, and the SHG is additionally enriched with C 3 -C 4 carbohydrates, cracking products C 5+ papafinov. After separation from the C 5+ selectocracking products, the WASH is recycled to the biforming reactor, where the light hydrocarbon gases, together with the straight-run gasoline components, are converted into highly aromatized products and hydrogen.
  • C 5+ products of selective cracking after separation from the WASH are subjected to stabilization and removed from the process as environmental components of motor fuels.
  • the yield of C 5+ products is 92.1 wt.% Calculated on the gasoline fraction - the feedstock of the biforming process.
  • the octane number is 95.8 p. IM with an aromatic hydrocarbon content of 36.1 wt.%.
  • This version of the proposed method due to the complete recycling of light hydrocarbons to the biforming zone is a type of resource-saving technologies in combination with the implementation of its main goal - to reduce the content of aromatic hydrocarbons to less than 40 wt.%.
  • Example 7 illustrates the proposed method for implementing the process (options-5 and 6) ( Figure 2).
  • the process is carried out in the same way as described in example 6, with the difference that the C 5+ catalyst of the bioforming is sent to a distillation column.
  • the 36-102 0 C fraction was withdrawn from the column as a side stream, mixed with WASH and sent to the hydrogenation reactor P4.
  • a feature of the hydrocarbon composition of this fraction is an increased content of C 5 -C 7 n- and iso-paraffins (more than 60%, Table 10), benzene (up to 10 wt.%) And a relatively small total aromatic hydrocarbon content (up to 40%). AT collectively, this determines the relatively low octane characteristics of this fraction (less than 85 p.
  • the fraction of 36-105 0 C stable catalysis is sent to the hydrogenation reactor, and the hydrogenation product is removed from the process.
  • a mixture of hydrocarbons fr. 36-105 0 C with HBG biforming is successively sent to the hydrogenation reactor P4, and then to the selectocracking reactor P5.
  • deep hydrogenation of benzene and toluene is carried out, respectively, to cyclohexane (IOI - PO item) and methylcyclohexane (IOI - 104 item).
  • the aromatic content decreases from 36.2 to 2.7 wt.%, And benzene - from 9.1 to 0.3 wt.%.
  • the WASH enriched in C 1 -C 4 light gases is recycled to the bioforming zone for recycling into C 5+ high-purity components.
  • C 5+ hydrogenation and selective cracking products are removed from the process as an environmental high-octane component.
  • Example 8 (for comparison). The process is carried out as described in example 6. The difference is as follows (conditions are shown in table 11). The pressure in the hydrogenation and selective cracking reactors is maintained at 0.30 MPa. At the same time, the depth of hydrogenation of the C 5+ catalytic reforming decreases. The aromatic content increases to 55 wt.%. The rate of hydrogen binding in the hydrogenation unit becomes less than the rate of its evolution in the biforming zone. As a result, to maintain a constant value of the working pressure in the bioforming zone, excess hydrogen is removed from the process in a mixture with part of the hydrocarbon gases. The overall efficiency of the process is reduced.
  • Example 9 (for comparison). The process is carried out as described in example 6. The difference is as follows. The following conditions are maintained in the hydrogenation reactor: pressure - 2.0 MPa, temperature - 35O 0 C, volumetric feed rate of C 5+ biforming products - 2.0 h. "1. In these conditions, as in example 8, does not provide the necessary rate of binding of hydrogen to the biforming unit. Therefore, the temperature in the hydrogenation zone of more than 35O 0 C does not ensure the achievement of the goals and objectives of the proposed method for producing environmental components of motor fuels.
  • Example 10 illustrates the proposed method for implementing the process.
  • the process is carried out according to examples 1, 4, with the difference that the products of C 5+ - catalysis and WASH are not separated, but heated to 38O 0 C and fed to the selective hydrocracking reactor of n-paraffins.
  • a catalyst is used containing: molybdenum trioxide - 8.0 wt.%, Zeolite of the faujasite type RZES-Y - 5.0 wt.%, As well as palladium-containing high-silica zeolite of the pentasil type with a palladium content of 0.5 wt.% In the amount of 35 wt.% And aluminum oxide - the rest is up to 100%.
  • the process of selective hydrocracking is carried out at a pressure of VSG 2.0
  • the binding and extraction of hydrogen from the composition of the WASH occurs.
  • high-octane hydrocarbons of a number of cyclohexane homologues are formed, which, together with part of the unreacted aromatic and paraffinic hydrocarbons, are removed from the process as the target high-octane component.
  • the content of aromatic hydrocarbons decreases from 65.4 to 35.4 wt.%.
  • the yield of C 5+ products increases from 80.9 to 83.4% wt.
  • the octane number of hydrogenation products is 93.9 p.IM. k * k *

Landscapes

  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Crystallography & Structural Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

L'invention concerne la fabrication de composants de carburants pour moteurs à taux d'octane élevé respectueux de l'environnement à partir de fractions d'essences ou de gaz d'hydrocarbures C1-C4. Ce procédé comprend l'hydroraffinage puis le formage sélectif d'un produit liquide C5+ hautement aromatisé comprenant des hydrocarbures aromatiques et à base de paraffine-naphtène. Les produits liquides C5+ à taux d'octane élevé sont mélangés avec un gaz hydrogéné de reformage et dirigés dans un réacteur d'hydruration avec un catalyseur contenant des métaux du groupe de platine. Les produits aromatiques y sont soumis à l'hydruration à une température inférieure ou égale à 350° C et une pression égale ou supérieure à 0,35 MPa pour être transformés en hydrocarbures du rang de cyclohexanes, ce qui permet de porter la teneur du produit C5+ en hydrocarbures aromatiques à moins de 42 % en poids.
PCT/RU2006/000443 2006-08-23 2006-08-23 Procédé de fabrication de composants de carburants pour moteurs WO2008024012A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
PCT/RU2006/000443 WO2008024012A1 (fr) 2006-08-23 2006-08-23 Procédé de fabrication de composants de carburants pour moteurs

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
PCT/RU2006/000443 WO2008024012A1 (fr) 2006-08-23 2006-08-23 Procédé de fabrication de composants de carburants pour moteurs

Publications (1)

Publication Number Publication Date
WO2008024012A1 true WO2008024012A1 (fr) 2008-02-28

Family

ID=39107026

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/RU2006/000443 WO2008024012A1 (fr) 2006-08-23 2006-08-23 Procédé de fabrication de composants de carburants pour moteurs

Country Status (1)

Country Link
WO (1) WO2008024012A1 (fr)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2013095815A1 (fr) * 2011-12-22 2013-06-27 Uop Llc Production améliorée d'aromatiques par réduction du point final de basse pression et hydrogénation sélective et hydrodésalkylation sélective

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4615793A (en) * 1984-02-13 1986-10-07 Chevron Research Company High density recycle gas for reforming process
RU2043388C1 (ru) * 1993-04-27 1995-09-10 Производственное объединение "Киришинефтеоргсинтез" Способ выделения высокооктанового компонента моторного топлива
RU2144056C1 (ru) * 1999-06-01 2000-01-10 Институт катализа им. Г.К.Борескова СО РАН Способ получения компонентов моторных топлив (биформинг-1)
RU2280063C2 (ru) * 2004-10-18 2006-07-20 Государственное образовательное учреждение высшего профессионального образования "Уфимский государственный нефтяной технический университет" Способ получения высокооктанового бензина
RU2280062C1 (ru) * 2005-01-19 2006-07-20 Государственное образовательное учреждение высшего профессионального образования "Уфимский государственный нефтяной технический университет" Способ получения высокооктанового бензина

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4615793A (en) * 1984-02-13 1986-10-07 Chevron Research Company High density recycle gas for reforming process
RU2043388C1 (ru) * 1993-04-27 1995-09-10 Производственное объединение "Киришинефтеоргсинтез" Способ выделения высокооктанового компонента моторного топлива
RU2144056C1 (ru) * 1999-06-01 2000-01-10 Институт катализа им. Г.К.Борескова СО РАН Способ получения компонентов моторных топлив (биформинг-1)
RU2280063C2 (ru) * 2004-10-18 2006-07-20 Государственное образовательное учреждение высшего профессионального образования "Уфимский государственный нефтяной технический университет" Способ получения высокооктанового бензина
RU2280062C1 (ru) * 2005-01-19 2006-07-20 Государственное образовательное учреждение высшего профессионального образования "Уфимский государственный нефтяной технический университет" Способ получения высокооктанового бензина

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2013095815A1 (fr) * 2011-12-22 2013-06-27 Uop Llc Production améliorée d'aromatiques par réduction du point final de basse pression et hydrogénation sélective et hydrodésalkylation sélective

Similar Documents

Publication Publication Date Title
US6783661B1 (en) Process for producing oils with a high viscosity index
CN107109254B (zh) 用于产生c2和c3烃的方法
CN101173189B (zh) 一种生产化工原料的两段加氢裂化方法
CN102453535B (zh) 一种增产重整料的加氢裂化方法
CN103874746A (zh) 联合催化裂化汽油和轻循环油加氢操作以使对二甲苯产量最大化
WO2007105400A1 (fr) Procede de fabrication d'une huile hydrocarbonee et huile hydrocarbonee
CN1814703A (zh) 一种用费托合成产物生产柴油或柴油组分的方法
CN1297635C (zh) 一种用费托合成产物生产乙烯装置专用石脑油原料的方法
AU2007208855B2 (en) Method of hydrogenolysis of wax and process for producing fuel base
CN101177623A (zh) 费-托合成油的加氢裂化方法
JP4848191B2 (ja) 合成油の水素化処理方法
CN110835550B (zh) 一种生产化工原料的加氢裂化方法
US3556986A (en) Startup procedure for combined hydrofining-reforming process
RU2144056C1 (ru) Способ получения компонентов моторных топлив (биформинг-1)
WO2008024012A1 (fr) Procédé de fabrication de composants de carburants pour moteurs
RU2417251C2 (ru) Способ получения компонентов моторных топлив (экоформинг)
US4036735A (en) Process for upgrading motor gasoline
CN1040225C (zh) 提高烃质原料品位的方法
CN1266256C (zh) 一种改进的加氢裂化方法
CN103443253A (zh) 煤油基材的制造方法以及煤油基材
CN1261544C (zh) 一种多产优质柴油的中压加氢方法
CN101177627A (zh) 一种费-托合成油的加氢处理方法
CN100575459C (zh) 费-托合成油的加氢处理方法
US7273958B2 (en) Process for isomerization of a C7 fraction with opening of naphthene rings
CN1031410C (zh) 提高烃原料品位的方法

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 06847401

Country of ref document: EP

Kind code of ref document: A1

NENP Non-entry into the national phase

Ref country code: DE

ENP Entry into the national phase

Ref document number: 2009110626

Country of ref document: RU

Kind code of ref document: A

122 Ep: pct application non-entry in european phase

Ref document number: 06847401

Country of ref document: EP

Kind code of ref document: A1