• 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:
    The invention relates to catalytic chemistry, in particular catalysts (QD) for the production of methanol and higher alcohols from synthesis gas, which can be used as components of fuel in internal combustion engines. An increase in the activity and stable selectivity of the CT composition is achieved by changing the ratio of substances and the introduction of an additional component (DC). The composition of the CT corresponds to the following empirical formula of the elements: 2nCr ,,, gDe A - K or Na; m 0.29-0.5i n 0.018 pb, 036; X 0,012-0,06 and U 1,5-1,9, or where A is K; M is cerium or At, or Mn, m 0.315 or 0.35, n 0.027 or 0.029; x 0.023 or 0.037} to 0.02-0.082 and y .1.5-1.7. In both cases, the value of the index y is taken as such, which is necessary to satisfy the valence at which the various elements are in the catalyst. Test OT of CT in the synthesis of methanol (MT) and higher alcohols (BC) show that it gives the best performance: during the time of KT 47-449 h, it is 585-552 g / l, with the content of MT 64-64.0 . Mas.% and BC - 15.8-4 wt.% versus 493-357 g / l for 40-384 h and the content of MT 80, b-85.1 wt.% and BC 2-1 wt.% 1 C .p. f-ly.3 tabl.
    公开号:SU1279516A3
    申请号:SU3516802
    申请日:1982-11-26
    公开日:1986-12-23
    发明作者:Фатторе Витторио；Нотари Бруно；Паджини Альберто；Лагана Винченцо
    申请人:Снампрогетти,С.П.А. (Фирма)；
    IPC主号:
    专利说明:

    Frames for the production of methanol and higher alcohols from syngas, which can be used as components of fuel in internal combustion engines.
    The aim of the invention is to increase the activity and stable selectivity due to the change in the ratio of the components that make up the catalyst, and due to the content of the additional component.
    Example 1. The catalyst of the following empirical formula:
    0,35. Oa
    Zn-- Cr - Si K. Oh,
    , 5-1, ".
    59 g of chromic anhydride1) ida is dissolved in deionized water to prepare a mixture of 30% strength solution.
    Separately, prepare a suspension of 140 g of zinc oxide in 2 liters of deionized water. The chromic solution is added to this suspension with vigorous stirring and stirring is continued for several hours to ensure complete homogenization. The precipitated precipitate is filtered off, washed with water, dried by fine grinding, and the granules are impregnated with an aqueous ammonium solution of copper acetate and potassium acetate, prepared as follows.
    3.8 g of potassium acetate are dissolved in 3 cm of water. After 9.3 g of copper acetate, 11 cm of a 32% ammonia solution are added.
    The mixture is stirred until complete dissolution. Impregnated granules su110S for 8 h and then
    chat
    for 8 h calcined at
    The catalyst is reduced by stirring 20 cm of the granules in a copper-lined stainless steel tubular reactor placed in a bath or fluidized bed of sand and heated to 300 ° C in a stream of nitrogen containing w2% hydrogen. During the reduction, the flow of hydrogen is controlled in such a way that the temperature does not exceed. Recovery ends after about 24 hours.
    The catalyst thus prepared is ready for use in the reaction for the synthesis of methanol and higher alcohols.
    following empirical formula: Zn- Сг-Сю .К „О ,,
    o.iS 0.018 o, o93 1.5-1.6
    IG copper nitrate and 30
    nitrogen3
    Chromium oxide is dissolved in 500 cm of deionized water with heating and vigorous stirring. 18.5 g of zinc oxide is stirred in 500 cm of deionized water. The first solution is poured into a suspension of zinc oxide, then the mixture is heated with stirring to 90 ° C. A certain amount of solution prepared by dissolving 50 g of CO into 500 cm of deionized water is then added to raise the pH to 9. After 1 h, the mixture is cooled, neutralized to pH in 15% nitric acid solution and the precipitated particles are filtered and washed several times with water. The paste is dried at 11 for 4 hours. The calcium content is determined as 0.8% by weight. Then granulation is carried out to obtain a catalyst in the same way as Example 1.
    PRI me R 3. The catalyst of the following empirical formula
    Zn Cr, Cu -Na 0..,,
    0.35 0.018 0: 0 & 1.5-1 gb.
    The procedure is carried out analogously to example 2, but using a solution of Na CO, prepared
    by dissolving 80 g
    Na,., CO, jB
    l
    water instead of a solution of CO, According to the analysis of the Na content of 1.27
    PRI me R 4. The catalyst of the following empirical formula: Zn- Cr.,. Mp ... -Oh,
    Cr „,,
    1.5-1.6. The catalyst is prepared in
    following the procedure described in Example 1, but also adding 17.9 g of manganese acetate in the final impregnation solution. 45 Example5. The catalyst has the following empirical formula:
    2п o. ,,, ь-, Carry out the procedure similarly
    Example 1, but with the addition of 55.72 g of 50 aluminum nitrate to the final solution.
    PRI me R 6 "the Catalyst of the following empirical formula:
    C -K .0. Zn Cr
    0058 k, o1, t.6
    e, -
    权利要求:
    Claims (2)
    [1]
    The procedure is carried out as in Example 1, but using 66 g of chromic anhydride and 132 g of zinc oxide instead of the amounts indicated in Example 1. Example. The catalyst of the following empirical borpule: Z СГо, "- C" a "K" ", - 0, .." The procedure is carried out as in example 1, but using the following amounts of salt, g: Chromic anhydride 90 Zinc oxide 162 Acetic acid copper 11 , 7 Acetic acid potassium 3.4 Example (comparative), Catalyst of the following empirical formula: 2P-SG, 35 .0, 0,, 5. ,,,. The preparation was carried out similarly to Example 1, but without adding the copper salt to the final solution. Examples 9-15. Catalysts prepared and activated analogously to Examples 1-7 are tested for the synthesis of methanol and higher alcohols. Synthetic gas is supplied, of the following composition, vol.%: H 66-29 CO 30-33 CO, 0-3 CH 0.1 N; 0.3 The liquid reaction product is separated by cooling and condensation. Averaged samples taken after 24 hours of testing are analyzed by gas chromatography. Practical use of various catalysts (pressure, temperature, volumetric rate) in accordance with examples 1-8 and the results obtained are shown in Table 1. Example 16. The catalyst sludge tests, which lasted more than 435 hours, are carried out using a catalyst prepared according to Example 1. A 35 cm catalyst is placed in a tubular reactor. A synthetic mixture, the composition of which is maintained within the range of values given in Example 15, is skipped at about 10,000 GHSV. The average reaction temperature is 400 ± 5 ° C, the working pressure is 13000 kPa. The change in the selectivity of the catalyst from the time it is used is shown in Table 2. 64 The results presented in Table 2 show that there are no significant changes in productivity and selectivity over time. PRI me R 17 (comparative). The test of the service life of the catalyst was carried out on a comparative catalyst prepared in accordance with Example 8, under the same reaction conditions as described in Example 16. The change in the selectivity of the known catalyst from the time it was used is given in Table. 3. The test results (Table 3) show that this catalyst worsens its effect over time, both in terms of performance and selectivity, and, moreover, it is much less active from the very beginning. Example 18. The catalyst of the following empirical formula: Zn Cg Cu K O 0.5 o.ojj 0.042 .-, The catalyst is prepared as follows. 73.58 g of chromic anhydride (or chromic anhydride of CrO-) is dissolved in deionized water to form a 30% strength solution by weight. Separately prepare a ZnO suspension, amounting to 119.7 g of ZnO in 1.8 l of deionized water. Chromic anhydride is added to this suspension with vigorous stirring until complete homogenization is obtained. The precipitate formed is then dried and tableted as in Example 1. The tablets are then dried with an aqueous ammonium solution of copper acetate and potassium acetate, which is obtained by dissolving 6.04 g of acetic acid in 3 cm of water with the addition of 11 cm 3 of ammonia (32% concentration) and followed by the addition of 9.7 g of copper acetate. Example 19. The catalytic composition of the following empirical formula: - ,, 9 Cu ",,, K, O ,,. ,, 5 5 The procedure is carried out as in Example 18, except that 50.8 g of chromic anhydride and 142.5 are used g of zinc oxide. EXAMPLE 20 Catalyst Composition of the Following Empirical Formula: Zn Particle CoCooazOb-6b 6.9 g of copper nitrate and 60 g of chromium nitrate are dissolved in 1 l of deionized water with vigorous stirring and heating, which is necessary for a complete solution of both salts. 37 zinc oxide is suspended in 1 liter of deionized water and the suspension thus obtained is added to a solution of honey nitrate and chromium nitrate. Then a solution of potassium carbonate is added to the mixed solutions in the same way as the example. The catalyst thus obtained is tableted and thermally conditioned as in example 1. Example 21. The composition of the catalyst is of the following empirical formula: Cr 5Sio, O.K. 5-1, c. The procedures are repeated similarly to Example 1 with the following quantities of reproducible substances, g of chromic acid anhydride 57.9i zinc oxide 134.4 acetic acid copper 12 acetic acid potassium 6.04. Example 22. The catalyst of the following empirical formula: 2n-cr „,: and ,,,, к,„ ,, o ,,,. ,,, The following amounts of reactants are used, g: anhydride of hromic acid 56.6; zinc oxide 39 acetic acid copper 67.03, potassium acetic acid 2.04. Example 23. The catalyst of the following empirical formula: Zn-Cr ,, j5Cu ,,,, 0.5-y. The procedure is repeated as in Example 1, except that 7.27 g of honey acetate and 6.04 g of potassium acetate are used. Example 24. The catalyst of the following empirical formula:, Ji5Ceo, oiCUo ,, oiTOi e-r, e. 52 g of chromic anhydride is dissolved in deionized water until a 30% strength solution is obtained by weight, and then 14.7 g of cerium nitrate is added. Separately prepare a suspension of 134 g of zinc oxide in 2 liters of deionized water, then this suspension is vigorously stirred with the addition of a solution of chromic anhydride and cerium nitrate to it and stirring is continued until complete homogenization is obtained. 66 The precipitate formed is treated in accordance with Example 1. The tablets thus obtained are then impregnated with an aqueous ammonium solution of 9.7 g of copper acetate and 6.04 g of potassium acetate. The results of testing the catalysts of Examples 18-24 are shown in Table 4. Example 25 A catalyst was prepared and activated according to the procedure described in example.
    [2]
    2. In coarse reactor, heated by electricity, load 20 cm of catalyst and serves synthesis gas having the following composition.%: Hydrogen 66; WITH 31; C0, j, 3; methane 0.1. The temperature is gradually increased to 400 ° C and the pressure to 13000 kPa, GSHV (1 hour space velocity) corresponds to 10,000 h 1 Liquid product is collected every 24 h and analyzed. In the gas leaving the reactor, the methane content is defined as the designation of the hydrocarbons produced. The process runs almost continuously for more than 2,000 hours of testing, the methanol yield varies from 67 to 60 wt.%, And the higher alcohols remain at 26.5 wt.%. PRI me R 26. Tableted proposed catalyst (6x6 mm) prepared in accordance with the known. Catalyst composition, wt.%: CuO 38.6, - ZnO 30.9; 14.7; KjO 2.9, 3 1Pot in mass at a heating temperature of 500 ° C 8.6%. 20 cm of this catalyst is charged to an electrically heated tubular reactor and synthesis gas is fed having the same composition as in Example 25. The temperature is gradually increased to 10,000 kPa and the GHSV to 2600 l / h of catalyst. The selectivity of higher alcohols is quickly lost after just a few hundred hours. For example, from 27 to Vmas. after 240 h, while the selectivity for methanol increases from 68 to 88 wt.%. The productivity of higher alcohols is low, since it is necessary to work with GHSV, which is about 0.25 from GHSV in the presented example 25. The compositions of the catalysts of examples, expressed by atomic or mass ratio of the components, are presented in table 5. Claim 1. Catalyst for producing methanol and higher alcohols from syngas based on oxides of zinc, chromium, copper and potassium or sodium, characterized in that
    in order to increase activity and stable selectivity, the composition of the catalyst corresponds to the following empirical formula:
    Zn-Cr —Cu —A, —O ,, where A is potassium or sodium
    m - Oj29-0.5;
    p - 0.018-0.036;
    X, 0,012-0,06-,
    U - 1.5-1.9,
    the value of the index y is taken as such. Characteristics 9000 13000 Pressure, kPz Temperature, C 398-404 397-404 GHSV, h11400 Compomer, mas.X 12
    M is cerium OR aluminum, or manganese;
    m is 0.315 or 0.35; P is 0.027 or 0.029; . X is 0.023 or 0.037; k - 0.02-0.082, U - 1.5-1.7,
    wherein the index value of y is taken as such, which is necessary to satisfy the valence at which the various elements are in the catalyst.
    Table. 1 Indicators of the catalyst in example (for example). 16000 13000 13000 13000 13000 POOO 13000 13000 13000 13000 97-404 398-403 398-404 416-421392-405398-400397-462399-403398-401 396-400 10340 15030 6870 10650 9560 68 to satisfy the valence at which the various elements TC in the catalyst. 2. The catalyst according to claim 1, which is based on the fact that it additionally contains oxide of cerium or aluminum, or manganese and its composition corresponds to the following empirical formula: ZnCr Sy A.- M .: O, where A is potassium J 2С10) 3 (I)) D (13) TB {i) TJO5) I 10200 11170 11400 11800 10200.
    higher alcohols
    (C, 5) 15.8 15.8 15.8
    14
    12.3 35.4 27.9 higher alcohols.
    1279516
    10 Table 3 23.4 31.1 20.3 28.9 31.6
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    同族专利:
    公开号 | 公开日
    KR840002259A|1984-06-25|
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    IE822861L|1983-06-02|
    FI71883B|1986-11-28|
    CS236697B2|1985-05-15|
    NO158722C|1988-10-26|
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    FR2517296B1|1985-04-19|
    IT1169281B|1987-05-27|
    NO823601L|1983-06-03|
    PL137518B1|1986-06-30|
    IN157897B|1986-07-19|
    ES8401436A1|1983-12-16|
    FI824150A0|1982-12-02|
    FI71883C|1987-03-09|
    RO86064A|1985-03-15|
    ZA827980B|1983-12-28|
    ES517749A0|1983-12-16|
    GR77106B|1984-09-06|
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    引用文献:
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    US4843101A|1983-06-01|1989-06-27|Lehigh University|Catalyst and method for producing methanol|
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    US4882360A|1984-07-30|1989-11-21|The Dow Chemical Company|Process for producing alcohols from synthesis gas|
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    US4762858A|1985-09-16|1988-08-09|The Dow Chemical Company|Syngas conversion to oxygenates by reduced yttrium/lanthanide/actinide-modified catalyst|
    US4943551A|1985-11-08|1990-07-24|Union Carbide Chemicals And Plastics Company, Inc.|Catalyst for synthesis of mixtures of methanol and higher alcohols|
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    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    IT25390/81A|IT1169281B|1981-12-02|1981-12-02|CATALYTIC SYSTEM AND PROCEDURE FOR THE PRODUCTION OF METHANOL MIXTURES AND HIGHER ALCOHOLS|
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