• 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. Process for the preparation of a low benzene content, environmentally-acceptable petrol derived from carbonaceous light oil, characterised in that a core fraction boiling at 145-185 degrees C is distilled off from the crude carbonaceous light oil, the phenol in the core fraction is separated out, the separation is conducted by extraction using aqueous soda lye or sodium phenolate lye, and the phenol-free raffinate of the core fraction is mixed with the portion of the carbonaceous light oil boiling at up to 145 degrees C and worked up by raffination and reforming to give a low benzene content petrol having an increased octane number.
    公开号:SU1172452A3
    申请号:SU833582281
    申请日:1983-04-07
    公开日:1985-08-07
    发明作者:Янковски Альфонс；Делер Вернер；Грэзер Ульрих
    申请人:Рурколе Аг (Фирма)；Феба Ель (Фирма)；
    IPC主号:
    专利说明:

    Fig. 1 11 Invention, with the use of rss to a method of obtaining a L.-kzin, in particular from light .ch (pproducts, obtained kch ug ;; Lime) loluchsii method 6e-: -.- t. By hydrotreating and cat :. ishtichesky reforgp (g5ga of the lungs; eft-.mtp {;; ukts ;;;, P (5L-DURING h) HS, LY pi. However, the result is ss; H ;; n has Ri, K; o which has a number and therefore has a ToKcH4i ; i M. Kr (-ge addition is too large flow) and.) e;) tk /, and on hydroceram and p -1fprkp Ig ovH-niria. Most blitches; K and hyurea is ATP) with (;;: nor Oeipina, G-ez le u)): Rachi the original coat of the;, ;; Coins ;;; gi.urt-rassiadisy juvip; a solution of hc) of the agent,;,; - next to it, and to her an irochrocka catal 11a of which it is possible, however, CTCiiaHTi u.ag1lsni benzene I-; c: pyr}, - 1); sdatato1a „so that the sex of the {; |; h; h11n contains -d; not yet NIC net 5% ;;) en, ja,: otfy. not. driropa neither. e g; C: o; Hi. i. Ps ric:.; . . (. Vb; -c) oOl5c h 1nl e1h; remove sams gch ;, shrishi,. benzene .. tight-n; ipe; P1 n .; ; B) | ,, get; anuy g: -;. other: 1; i aa 1ch class cotsfo ;; . dssty.chl: CHSM |) rachndni with tempanaTvj:;:.; ki:} iN11 ki -, (. And; tempo - paf.DOii k; (.,;. Y) H. after the gods) .1 r4iij; ossfeiol.aning extrac - CIS WATER 1 paCT} iO; .4iM .CHJlpOOKHC and sodium; 1I: L1L1o.a and Aachchgg, I mix Ehstoy.) Govogts t npv room.: temperature and at atmospheric pressure, apply extrahexate in stoichiometric number with respect to the fraction with a boiling point of 1 5-185 ° C or in a two to threefold stoichiometry: a surplus. Г У; рОО ИС: КУ (ГРОВО.ЦЯТ ПИ 350-400 With a pressure of 40-80 bar on a cobalt-molded decking catalysts at a flow rate of 2-4 hours, and the consumption of hydrogen is 50-90 l / k. Catalytic reforming is carried out at 580–520 ° C and a pressure of 10–30 bar of a noble iv – catalyst catalyst at a space velocity of 3–4. Fig. i shows a block diagram of the setup for the implementation of P5: 1 unit for the desired method; Fig. 2 - extractor for carrying out three hundred, h; Pn extraction. V. |;, 1-5 STILLES DIONE column 1 PS line 2 no; i, aroT feedstock raw material boiling point nc 185C chi gi: drogen- zap, uy coal, lia stage distillates t.i get frac-KJ with boiling point nc FC: black from);;. t on line 3 and on line 1К) dan.) tsa 1 hydrotreatment in block 5. t tipaicni.jw with boiling point. 145-185 (; which Fio of line 6 serves tea; free phenolation to extractor 7, where extractant is poured over 8, Ps. Plononny at the stage of dephenolization, the raffinate is withdrawn through line 9 and mixed with the temperature before serving for hydro cleaning. boil nc 145 C, in line 4. After the hydrotreater C 1 P1, the product on line 10 is sent to the pump; the flow is sent to block 1 1 and on line 12, the criijojHT and the personal product is discharged line 13 i isdanug for phenol regeneration. The three-stage extractor contains .-- tank 14-17, dosage lacnc 18 and stages 19-21. agent via line 22 with; {(g; hh; and IS is served at stage 19, where} line 23 also serves the fraction,:. (worked at stage 20 as an extract, 1) TIOC; IMY, from STEP 19 to 24, yo., nl at stage 20, the extract through line 25 is fed to stage 21, where h .;) liga 26 also feeds the L- -emie boil trap 145-185 ° C, which is withdrawn from the tank 17.I get .-. j: 3 sec. 1 phe nol l o d e r s e c t r a s t withdrawal from the system, and the resulting light phase of line 27 at the stage; about 20. get at stage 19 light organically; the raffinate is withdrawn via line 28 and is fed to intermediate storage in tank 16, for example, From 100 weight parts. the phenol-containing fraction with a boiling point nc 185 C, obtained by the hydrogeal reduction of coal, 45 weight off including the phenol-containing fraction with a boiling point of 145-185 0, which is subjected to bleaching by a three-stage extraction of 69 parts by weight 12Z-Horo by weight of aqueous solution of sodium hydroxide at room temperature and atmospheric pressure. The raffinate thus obtained is mixed 5 with a fraction with a temperature of nc 145 C obtained in the distillation stage of the initial fraction. The resulting mixture is hydrotreated at 400 ° C and a pressure of 60 MPa on a cobalt-molybdenum catalyst at a space velocity of 1.5 and subsequent reforming at 480 ° C and a pressure of 15 bar on a platinum catalyst supported on alumina at a space velocity .13 1.5 hr
    Get gasoline, which is listed in the table.
    Example 2. Example 1 is repeated. However, a three-stage extraction of pro-20
    water t 35 weight.h. 12% aqueous solution of sodium phenol. You get a gasoline with an octane number of 99, containing 2.5 wt.% Benzene.
    Example 3 (comparative). Example 1 is repeated; however, a three-stage extraction is used to extract the coal obtained by hydrogenation with a boiling point of up to 300 ° C and the raffinate obtained is subjected to hydrotreating and subsequent catalytic reforming. A gasoline fraction with an octane number of 98 and a benzene content of 5.1% was isolated from the resulting product.
    Thus, using the method, gasoline from coal distillates is obtained, containing not more than 2.6 wt.% Benzene and having an octane number of 99 ...
    权利要求:
    Claims (1)
    [1]
    METHOD FOR PRODUCING GASOLINE, including de-phenolization of a fraction.
    obtained by coal hydrogenation, extraction with an aqueous solution of sodium hydroxide or sodium phenolate, hydrotreating and subsequent catalytic reforming of the raffinate to obtain the desired product, which consists in the fact that, in order to reduce the benzene content in gasoline, a fraction with the boiling point of 185 ° C, from which fractions with a boiling point of nc 145 ° C and with a boiling point of 145-185 C are isolated by distillation, the latter is subjected to de-phenolation, the raffinate obtained is mixed with the fraction so that boiling temperature NK 145 C and serves for hydrotreatment.
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    Figure 1
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    同族专利:
    公开号 | 公开日
    AU556607B2|1986-11-13|
    ZA832467B|1983-12-28|
    EP0091047A3|1985-01-09|
    CA1206908A|1986-07-02|
    DE3213220A1|1983-10-13|
    IN158910B|1987-02-14|
    EP0091047B1|1987-03-04|
    EP0091047A2|1983-10-12|
    NZ203807A|1986-02-21|
    DE3370022D1|1987-04-09|
    AU1309483A|1983-10-13|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    GB107454A|1916-07-31|1917-07-05|George Edward Heyl|Improvements in Liquid Fuels.|
    US4319981A|1980-11-12|1982-03-16|The United States Of America As Represented By The United States Department Of Energy|Process for preparing a liquid fuel composition|DE3410455C2|1984-03-22|1987-10-15|Ruhrkohle Ag, 4300 Essen, De|
    CN101429446B|2007-11-09|2012-10-10|丁冉峰|System and method for catalyzing hydrocarbon for recombinant production of high-quality gasoline|
    CN101429449B|2007-11-09|2012-10-10|丁冉峰|System and method for catalyzing hydrocarbon for recombinant production of high-quality gasoline|
    CN101429448B|2007-11-09|2012-11-14|丁冉峰|System and method for catalyzing hydrocarbon for recombinant production of high-quality gasoline|
    CN101429444B|2007-11-09|2012-11-14|丁冉峰|System and method for catalyzing hydrocarbon for recombinant production of high-quality gasoline|
    CN101429443B|2007-11-09|2012-08-22|丁冉峰|System and method for catalyzing hydrocarbon for recombinant production of high-quality gasoline|
    CN101429442B|2007-11-09|2013-02-06|丁冉峰|System and method for catalyzing hydrocarbon for recombinant production of high-quality gasoline|
    CN101429447B|2007-11-09|2012-11-14|丁冉峰|System and method for catalyzing hydrocarbon for recombinant production of high-quality gasoline|
    CN101475835B|2009-01-22|2012-09-05|北京金伟晖工程技术有限公司|System and method for preparing high quality petrol by hydrogenation after component oil refining hydrocarbon recombination|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    DE19823213220|DE3213220A1|1982-04-08|1982-04-08|CARBURETOR FUEL|
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