• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
  • 同族专利
  • 引用文献
  • 法律状态
  • 优先权
    • 专利摘要:
    1. A process POLUCHZENIYA aromatic hydrocarbons by contacting olefinsoderzhgytsih carbohydrate orodnk frakhschy, 1 and Cj -C hydrocarbons in the gas phase with the catalyst zeolite ZSM-5 on the carrier at 454-557 C, distinguishing with the fact that, in order povppeni yield of aromatic hydrocarbons, As Cj-C hydrocarbons, saturated and unsaturated hydrocarbons are used and the process is carried out in the presence of a catalyst containing 71% by weight of a zeolite with a SiOj / AIjOj 1540 molar ratio replaced by gallium ions in an amount of 1.6% by catalyst, 29 m % with silica as a binder and activated in flowing air at 550 &.deg; C. 2. The method according to claim 1, which is based on the fact that the process is carried out at a mass ratio of olefin-containing hydrocarbon formula {C5-C "g and both valuable and non-C (-C) hydrocarbons of 1.4-1 , 5. 3. A method according to claim 1, characterized in that a wide fraction of cracked gasolines is obtained as olefins of hydrocarbon fractions Ci - C, j, resulting in catalytic cracking of oil fractions.
    公开号:SU1147246A3
    申请号:SU802957755
    申请日:1980-08-06
    公开日:1985-03-23
    发明作者:Фрэнсис Гриффит Эллис Джон
    申请人:Дзе Бритиш Петролеум Компани (Фирма)；
    IPC主号:
    专利说明:

    The invention relates to a method for producing aromatic hydrocarbons from olefics, in particular, to preparing additives with a high content of aromatic hydrocarbons to gasoline, as well as hydrogen from olefin-containing petroleum fractions. In the processing of oil by some known methods, various hydrocarbon fractions are formed, the boiling point of which is within the boiling range of motor gasoline (15-205 G), but which for one reason or another cannot be used directly as motor gasoline. Thus, for example, the fractions obtained by the cracking process contain a significant amount of olefins that adversely affect the gasoline octane number. Examples of such fractions are light and heavy cracked gasolines obtained by catalytic cracking of heavy distillates with a boiling point of 350,550 seconds, as well as gasoline fractions obtained by thermal and vapor-phase cracking of petroleum products. These fractions can be used as components to produce a comp dianed gasoline, however, their quality is not high enough. Thus, the motor octane number of fractions of this type, in particular, light cracking gasolines obtained by catalytic cracking, is not high enough compared to the research octane number, which is to some extent due to the presence of significant quantities of olefins. To improve the quality of olefin fractions of this type from the point of view of their use as additives to gasoline, antiknock additives, such as tetraalkyl lead, are used. A method of producing aromatic hydrocarbons is known by contacting fractions of Cy and above, containing olefins and diolefins, for example, Cf pyrolysis fractions, at 300-650 C and a pressure of 1-50 atm in the presence of an iron aluminosimetic catalyst, having a molar ratio of SiOj / RvOz 100- 300 and SiOj / AIjOj 135-1900. The obtained fractions contain up to 80 wt.% Cg-Cit 46 aromatic hydrocarbons, including up to 9.9 wt.% Benzene f1. There is also known a method for producing aromatic hydrocarbons by contacting a fraction of 40-200C containing up to 83.6% paraffin hydrocarbons at 480-595 ° C and a pressure of 1-10 atm on zeolite-containing catalysts. Zeolites H-ZSM-5, H-ZSM-Ii with a molar ratio of SIOa / AIzOi 10-40, on which platinum, rhenium and other metals of group VIII are deposited, are used as zeolites, and the process is carried out in a hydrogen medium 2 The closest to the invention is: a method for producing aromatic hydrocarbons by contacting the olefinic hydrocarbon fractions Su-C 41 and hydrocarbons Of-Su in the gas phase with a catalyst on ZSM-5 zeolite, on amorphous silica-alumina 260-560 C. hydrogen donors use olefins, alcohols or ethers. It is most expedient to use Cg-Ci-olefins and methanol. The weight ratio to cy olefin is 0.1-1.0. The yield of aromatic compounds does not exceed 60 wt.%, And the increase in the octane number is 4.7 r. The disadvantages of the method are the low yield of aromatic hydrocarbons and, as a consequence, a slight increase in the octane number in comparison with the initial fraction. The purpose of the invention is to increase the yield of aromatic hydrocarbons. The goal is achieved according to the method of producing aromatic hydrocarbons by contacting olefinic Cf-Cti hydrocarbon fractions and Cj-C saturated and unsaturated hydrocarbons in the gas phase at 454-557 C with a catalyst containing 71% by weight of ZSM-5 zeolite with a SiOjt / mol% ratio AIj0 15-40, replaced by gallium ions in the amount of 1.6 wt.% Per catalyst, 29 May. % silica as a binder and activated in a stream of air at 550 ° C. In addition, the htofass is carried out at a mass ratio of Cg-Cii olefin-containing hydrocarbon fraction and Cg-C hydrocarbon hydrocarbons, which are not saturated, equal to 1.4. In addition, a wide fraction of cracking benzines obtained as olefin-containing hydrocarbon fractions of Su is obtained using catalytic cracking LMS, Suitable hydrocarbon fractions containing olefins that can be used in accordance with the invention are fractions containing at least 5, preferably 15-75% by weight olefins. However, hydrocarbon fractions with a higher olefin content can also be used. As a source of hydrocarbon olefin fractions, it is possible to use the broad cracking gasoline fractions obtained by catalytic, thermal or vapor-phase cracking of light or heavy petroleum distillate. As a starting material for thermal cracking, in particular, residues from vacuum distillation and distillation at atmospheric pressure or can be used. deasphalted oil, as well as the residue after the catalytic cracking process before or after hydrotreating. Preferred are hydrocarbon fractions, which are the broad fraction of the product of catalytic cracking of heavy distillates (boiling temperature .GS to), which is used as such or after separation into light and heavy cracking gasoline. As saturated and unsaturated Cj-C / 1 coal; hydrogens can be used with soBiaTb any product containing enough of them to form the initial mixture. In particular, as a source of these hydrocarbons (which also contains small amounts of hydrocarbons, you can use, for example, gases - byproducts of catalytic, thermal or vapor phase cracking of parafinovil distillates, residues after distillation of petroleum products and deasphalted oil) (o or after hydrotreating. Gallium in the catalyst may be present in the form of an oxide and / or nones (in the event that alkaline 1 cation carrier cations are replaced by gallium ions). At the same time, as a source of gallium ions you can use aqueous solutions of its salts, for example gallium nitrate, chloride or sulphate. Such catalysts can be obtained by conventional ion exchange methods. After the ion exchange process is completed, the resulting catalysts are dried. For example, to obtain a catalyst, an aqueous solution of gallium compound, for example gallium nitrate, is given in contact with aluminosilicate at ambient or elevated temperature, for example, at boiling point. After the ion exchange process has been completed, the aluminosilicate is separated by decantation, followed by filtration, washed several times with deionized water and dried. Before adding an aqueous solution of the gallium compound, the aluminosilicate may be subjected to acid treatment. In aluminosilicates with a gallium compound deposited on them and / or in which cations are assigned to gallium ions, the molar ratio between the copper oxide and oxide can be 15-40. ZSM-5 can be used as such silicates. Stage of zeolite synthesis. The following reagents are used in the synthesis of zeolite, g: 10.0 Sodium hydroxide 28.0 Sodium aluminate 262 Diethanolamine 7U Ludox AS 40 (40 Mac. Z colloidal silicon dioxide) Deionized water Sodium and sodium hydroxide is dissolved in denonized water (350 g) at heating and stirring for tO min. Then the solution is filtered, placed in a three-liter flask. The ethanol was melted, added to the solution and the whole mixture was stirred for 10 minutes, the temperature was maintained at 40 ° C. Then the colloidal solution of silicon dioxide was diluted with the remaining deionized water (500 g) and slowly added to the mixture in the flask, for 1 hour. During this addition the temperature
    maintain and constantly stir the mixture, which gradually thickens. Stirring is continued for 0.5 hour after the completion of the addition of silica. The mixture is loaded into a three-liter autoclave, which is rotated for 4 hours, raising the temperature to. Then the autoclave is stopped and held at this temperature for 7 days. Thereafter, the autoclave is opened and the resulting white crystalline zeolite is separated from the mother liquor by decanting.
    Stage pretreatment of zeolite.
    The crystalline zeolite is thoroughly washed first with deionized water and then with 10% nitric acid solution. After that, the acid treated zeolite is thoroughly washed with deionized water to remove traces of acid. The zeolite is then dried in a vacuum oven for. 16 hours. The dried zeolite is roasted in a furnace, raising the temperature to 4 hours and keeping at this temperature for 60 hours. Then the burning zeolite is heated at the reflux temperature of 1.6 l of 10% nitric acid for 2.5 hours. water and dried in a vacuum oven as described above. The acid washed zeolite is subjected to an exchange reaction with ammonia, heating it to a reflux temperature in 1.5 liters of a 0.67 M solution of ammonium nitrate for 4 hours, then it is washed with water and dried as before.
    The zeolite obtained as a result of the exchange with ammonia is again calcined to raise the temperature to 500 ° C, and, after holding at this temperature for 16 h, a zeolite is obtained in the H form.
    Stage exchange with gallium. The zeolite obtained after re-calcination in the H form is placed in a 1.65 l solution containing 0.065 mol of gallium nitrate and heated at reflux for 4 hours. The material obtained is washed with water and dried, as before, in a vacuum oven.
    The step of introducing the binder. 200 g of zeolite obtained after exchange with gallium are shifted from 213 g
    Ludox AS 40 (contains 40 wt.% SiOg) and the mixture is dried in a vacuum oven as described above. The dried product is crushed and passed through a standard sieve of a British granulometric scale of 12-30 mesh. V In example 5, the catalyst prepared according to the specified METO-DICA is used.
    In Example 6, a catalyst is used, in the preparation of which, as an organic nitrogen-containing base instead of diethanolamine
    5 use tetraethylammonium hydroxide. In Examples 1-4, the same catalyst is used as in Example 6, only the ammonia exchange operation, preceding the final gallium exchange operation, is excluded.
    Examples 1-4. 200 ml of catalyst containing 1.6% by weight of gallium and 29% by weight of binder are loaded into a fixed bed reactor
    and pass through it for 2-3 hours the air at 550 ° C. The reactor is then flushed with nitrogen for half an hour to remove residual air. Thereafter, by displacement
    appropriate quantities of hydrocarbons receive the initial mixture, heat it to the temperature at which the process is carried out, and pass through the catalyst bed. AT
    As hydrocarbon fractions containing olefins, the following products are used in the described examples: light cracked gasoline (LAC), obtained by catalytic cracking, with boiling range 1090% by volume) 24.6-125 ° C (examples 1 and 2); a wide fraction obtained by catalytic cracking of cracking gasoline (KB) with a boiling range (10-90%) 39.5-190 s (example 3) heavy cracking gasoline obtained by catalytic cracking (TKB) with boiling limits (10- 90 vol.%) 106204 s (example 4). In all examples, liquefied petroleum gas (LPG) 5 consisting of,%: propane 7.7, propene 32.8, butane 29.2, butene 30.3, are used as saturated and / or unsaturated hydrocarbons. The conditions of the process and the results are shown in Table. 1. T + O means the average value of octane numbers, determined respectively by research 7
    Predatory and motor methods (IOC and MOC).
    . The results obtained are compared with the results obtained when liquid-phase catalytic cracking (LC) is carried out by a known method (Table 2).
    The composition of the obtained liquid products is given in table. 3
    As follows from the table. 3, more than 90% by weight of the aromatics obtained are benzene, toluene and xylenes.
    Example 5. The process is repeated as in Example 2, using a catalytic composition in which the zeolite has a SiOi molar ratio of 19: 1. From the raw material containing 58.8% by weight of light cracking gasoline and 41.2% by weight of LPG, a liquid product is obtained with a yield of 48% by weight. The research octane number of the product is 106.0 and the octane level determined by the motor method is 90.4.
    472468
    The composition of liquid products is given in tab. four.
    Example 6. The process is repeated as in Example 2, using the catalytic composition, in
    where the zeolite has a molar ratio. SiOX (equal to 15: 1. From raw materials containing 57.5 wt.% light cracking gasoline and 42.5 wt. W of the CIS, a liquid product is obtained with a yield of 47 wt.%. The product has a research octane number of 103.2 , the octane number determined by the motor method, 90.7 and the bromine number 9.7.
    Thus, in the proposed method, gasoline fractions containing 67.6-91.0% by weight of aromatic hydrocarbons with a high octane number, which can be used either as a raw material for petrochemicals or as a high-octane component of automobile gasoline, are obtained from olefin-containing fractions in comparison with the known ones .
    Table D
    Cracked gasoline
    IOC
    UR.
    IOC and IOC (claim mixture)
    bromine number
    Cracking gasoline, wt.% CIS
    Reaction temperature, ° C Pressure, abs. atm
    The total volume of the initial mixture of the catalyst), h
    The output of Cf (wt.% In the calculated mixture)
    M
    4.0
    4.0
    3.9
    60.5 55.6
    63.9 69.8
    Hydrogen yield (wt.% Calculated on the initial mixture)
    Increase (IOC + UR)
    Beizii ZHKK
    Offered Petrol FCC Famous
    Gasoline analysis,
     paraffins, naphthenes and new, Aromatic hydrocarbons,
    including: benzene toluene xylenes
    ethylbenzene C,
    polycycles
    Continuation of table 1
    is it
    1,051,580,771,5
    8.5 15.6. 10,214,4
    Table 2
    92.5
    6.8 89.8
    4.1
    eleven
    30 69.4
    5.I 67.6 91.0
    14 31 31
    6.8
    TZ 36 32 22 20
    2.6
    3.4
    .0 5.9 15 20
    2.8 Not measured Not measured Renault
     the amount of aromatic hydrocarbons in liquids. lump of the product, wt.%: 90,4 74,6
    Analysis of the liquid product, wt.%:
    13.4 8.9
    benzene
    32.9 24.4
    toluene
    xylene / ethylbenzene33, 9 29.3
    aromatic hydrocarbons, 15 C, 6.5 10.1
    polycyclic
    3.7 1.9 hydrocarbons
    权利要求:
    Claims (3)
    [1]
    1. METHOD FOR PRODUCING
    AROMATIC HYDROCARBONS by contacting olefin-containing hydrocarbon fractions C, -C. g and C 3 -C 4 hydrocarbons in the gas phase with a ZSM-5 zeolite catalyst on a carrier at 454-557 * C, characterized in that, in order to increase the yield of aromatic hydrocarbons, saturated C "-C" hydrocarbons are saturated and unsaturated hydrocarbons and the process is carried out in the presence of a catalyst containing 71 wt.% zeolite with a molar ratio of SiOj / AItOj 1540, replaced by gallium ions in an amount of 1.6 wt.% per catalyst, 29 wt.% silicon dioxide as a binder and activated in air flow at 55 ° C.
    [2]
    2. The method according to p. 1, wherein the process is carried out at a mass ratio of the olefin-containing hydrocarbon fraction of Su-Ca and the highest and unsaturated hydrocarbons C "-C. equal to 1.4-1.5.
    [3]
    3. The method according to π. 1, characterized in that as olefinsod ^ rzhaschih hydrocarbon fractions $ C - C and used wide fraction of cracked-gasolines poluchae-. catalytic cracking of oil fractions.
    I
    类似技术:
    公开号 | 公开日 | 专利标题
    SU1147246A3|1985-03-23|Method of obtaining aromatic hydrocarbons
    JPH0631335B2|1994-04-27|Contact dewaxing method
    CA1318906C|1993-06-08|Dehydrogenation and dehydrocyclization catalyst, its synthesis and use
    US4309275A|1982-01-05|Hydrocarbon conversion with crystalline silicates to produce olefins
    US6977321B1|2005-12-20|Production of propylene
    US4309276A|1982-01-05|Hydrocarbon conversion with low-sodium silicalite
    JP2923690B2|1999-07-26|How to improve the quality of sulfur-containing feedstocks
    US4556478A|1985-12-03|Hydrocarbon conversion process and catalyst composition
    KR20100024957A|2010-03-08|Catalyst for conversion of hydrocarbons, process of making and process of using thereof - incorporation-1
    US5013423A|1991-05-07|Reforming and dehydrocyclization
    JPH08507564A|1996-08-13|Reduction of benzene in gasoline by alkylation with higher olefins
    EP0023802B1|1983-04-13|Conversion of crude oil fractions to paraffins or olefins
    KR19990071825A|1999-09-27|Zeolite ssjet-44
    EP0127207B1|1987-05-06|Process for the preparation of middle distillates
    US4401555A|1983-08-30|Hydrocarbon conversion with low-sodium crystalline silicates
    US4416766A|1983-11-22|Hydrocarbon conversion with crystalline silicates
    JP2004511416A|2004-04-15|Improved zeolites and molecular sieves and their use
    US4370219A|1983-01-25|Hydrocarbon conversion process employing essentially alumina-free zeolites
    US5696043A|1997-12-09|Synthetic crystalline aluminosilicate for the catalytic conversion of hydrocarbons in petrochemical processes
    US2992283A|1961-07-11|Preparation of aromatic and saturated hydrocarbons
    US4830729A|1989-05-16|Dewaxing over crystalline indium silicates containing groups VIII means
    RU98121148A|2000-10-20|METHOD FOR PRODUCING HIGH-OCTANE GASOLINE FRACTIONS AND AROMATIC HYDROCARBONS
    US6350370B1|2002-02-26|NU-85 zeolite catalyst and a process for improving the pour point of feeds containing paraffins
    US6036846A|2000-03-14|Catalyst based on modified NU-87 zeolite and a process for improving the pour point of feeds containing paraffins
    RU2181750C1|2002-04-27|Method of processing petroleum distillates |
    同族专利:
    公开号 | 公开日
    NO802269L|1981-02-09|
    DE3062437D1|1983-04-28|
    EP0024147A1|1981-02-25|
    US4334114A|1982-06-08|
    ES494031A0|1981-08-01|
    ZA804510B|1982-02-24|
    NZ194545A|1982-12-07|
    CA1165332A|1984-04-10|
    JPS5638391A|1981-04-13|
    ES8106685A1|1981-08-01|
    IN154515B|1984-11-03|
    EP0024147B1|1983-03-23|
    AU6098780A|1981-02-12|
    AU532481B2|1983-09-29|
    AT2830T|1983-04-15|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    EA014671B1|2007-12-20|2010-12-30|Генрих Семёнович Фалькевич|Process for enhancing yield of aromatic hydrocarbons from c2-c4 aliphatic hydrocarbons|US3894104A|1973-08-09|1975-07-08|Mobil Oil Corp|Aromatization of hetero-atom substituted hydrocarbons|
    US4090949A|1974-07-31|1978-05-23|Mobil Oil Corportion|Upgrading of olefinic gasoline with hydrogen contributors|
    US4056575A|1975-06-05|1977-11-01|The British Petroleum Company Limited|Chemical process making aromatic hydrocarbons over gallium catalyst|
    CA1044259A|1975-07-17|1978-12-12|Reginald Gregory|Aromatisation process|
    GB1533169A|1976-06-22|1978-11-22|British Petroleum Co|Oligomerising c3-c8 olefins|
    GB1537780A|1976-12-20|1979-01-04|British Petroleum Co|Dehydrocyclodimerising c3-c8 hydrocarbons|
    US4180689A|1976-12-20|1979-12-25|The British Petroleum Company Limited|Process for converting C3 -C12 hydrocarbons to aromatics over gallia-activated zeolite|
    GB1561590A|1976-12-20|1980-02-27|British Petroleum Co|Zeolites containing gallium|
    GB2000179B|1977-06-17|1982-04-21|Ici Ltd|Production of aromatic hydrocarbons|
    US4162212A|1978-08-30|1979-07-24|Chevron Research Company|Combination process for octane upgrading the low-octane C5 -C6 component of a gasoline pool|
    US4190519A|1978-10-23|1980-02-26|Chevron Research Company|Combination process for upgrading naphtha|AU7243681A|1980-07-04|1982-01-07|British Petroleum Company Plc, The|Activation of gallium exchanged zeolite catalyst|
    ZA817004B|1980-10-17|1983-05-25|British Petroleum Co|Upgrading gasoline derived from synthesis gas|
    US4490569A|1981-05-11|1984-12-25|Mobil Oil Corporation|Process for converting propane to aromatics over zinc-gallium zeolite|
    US4607130A|1981-11-21|1986-08-19|Mobil Oil Corporation|Acid-catalyzed organic compound conversion|
    US4605803A|1981-11-21|1986-08-12|Mobil Oil Corporation|Acid-catalyzed organic compound conversion|
    US4686312A|1981-12-23|1987-08-11|Mobil Oil Corporation|Aromatics production|
    US4458097A|1982-04-30|1984-07-03|Union Carbide Corporation|Conversion of certain hydrocarbons using divalent-copper-containing ZSM-5 type catalyst|
    EP0107877B1|1982-10-28|1990-02-07|Shell Internationale Researchmaatschappij B.V.|Process for the preparation of an aromatic hydrocarbon mixture|
    DE3381352D1|1982-10-28|1990-04-26|Shell Int Research|METHOD FOR PRODUCING AN AROMATIC HYDROCARBON MIXTURE.|
    US4638105A|1983-02-14|1987-01-20|Mobil Oil Corporation|Acid-catalyzed xylene isomerization|
    US4620921A|1983-02-14|1986-11-04|Mobil Oil Corporation|Acid-catalyzed hydrocarbon conversion process|
    GB8308684D0|1983-03-29|1983-05-05|British Petroleum Co Plc|Production of gallium loaded hydrocarbon conversion catalyst|
    CA1231104A|1983-08-08|1988-01-05|Eduard P. Kieffer|Process for the preparation of an aromatichydrocarbon mixture|
    CA1243977A|1983-08-08|1988-11-01|Eduard P. Kieffer|Process for the preparation of an aromatichydrocarbon mixture|
    GB8401834D0|1984-01-24|1984-02-29|British Petroleum Co Plc|Unsaturated hydrocarbons by dehydrogenation|
    US4861933A|1987-08-25|1989-08-29|Mobil Oil Corp.|Process for converting aliphatics to aromatics over a gallium-activated zeolite|
    NZ225639A|1987-08-25|1989-09-27|Mobil Oil Corp|Converting aliphatics to aromatics over gallium- activated zeolite catalysts|
    EP0382960B1|1989-02-17|1993-01-13|Council of Scientific and Industrial Research|An improved reforming process for the catalytic conversion of petroleum fractions to a mixture of hydrocarbons rich in aromatics|
    US5149679A|1990-05-01|1992-09-22|Board Of Supervisors Of Louisiana State University And Agricultural And Mechanical College|Gallium-containing zeolite catalysts|
    US5135898A|1991-07-25|1992-08-04|Societe Quebecoise D'initiatives Petrolieres |Catalysts for the aromatization of light paraffins and olefins|
    FR2689033B1|1992-03-27|1994-11-04|Inst Francais Du Petrole|Gallium-containing catalysts and its use in the dehydrogenation of saturated hydrocarbons.|
    CN1257769C|2003-10-31|2006-05-31|中国石油化工股份有限公司|MFI structure molecular sieve containing phosphor and metal component and its use|
    JP2006305408A|2005-04-26|2006-11-09|Tosoh Corp|Catalyst for aromatization reaction and method for producing aromatic hydrocarbon using the same|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    GB7927534|1979-08-07|
    [返回顶部]