• 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:
    A process is described for forming an alcohol fraction boiling in the range of motor gasoline that is enriched in higher alcohols. The process comprises reacting (1) hydrogen, (2) carbon monoxide, (3) a heterogenous catalyst having (a) a first component of molybdenum, tungsten, or a mixture thereof in free or combined form; and (b) a second component comprising an alkali or alkaline earth element, or a mixture thereof in free or combined form; and (4) one or more lower alcohols.
    公开号:SU1510716A3
    申请号:SU853929259
    申请日:1985-07-26
    公开日:1989-09-23
    发明作者:Дж.Квардерер Джордж；А.Кочран Джин；Р.Стивенс Рекс；Б.Мерчисон Крейг
    申请人:Дзе Дау Кемикал Компани (Фирма)；
    IPC主号:
    专利说明:

    The invention relates to an improved method for producing a mixture of aliphatic C-C alcohols, used as an additive to fuel for gasoline engines.
    The purpose of the invention is to improve the quality of the mixture.
    The process is conducted by the interaction of hydrogen and carbon monoxide at their molar ratio (1.05-1.12): 1 at a pressure of 12.5-2.08 KP in the presence of a heterogeneous catalyst containing, as the first component, sulfide .-. Molybdenum or its mixture with cobalt sulfide, and in
    the second component is alkali metal carbonate, and methanol or ethanol added to the initial stream of hydrogen and carbon monoxide. Preferably, a heterogeneous supported catalyst and methanol obtained by fractionating a mixture of aliphatic C, -C-alcohols are used.
    Examples A (comparative) and 1. Examples A and 1 are carried out using a supported carbon catalyst.
    Approximately 1 cubic foot of coal Wit- with an MBV of 4-6 mesh in the form of 3/16 inch (0.48 cm) extrudates is immersed for 10 minutes at 60-70 ° C in a solution containing
    oh h
    Oi

    c / 4
    31510716
    craving 70,500 g of 22% ammonium sulfide, 11,800 g of ammonium heptamolybdate and 2,950 g of potassium carbonate. The extrudates are then removed and the excess liquid is removed. After that, the extrudates are calcined in a nitrogen atmosphere at 300 ° C for 4 hours. These steps are repeated until the extrudates absorb 20% molybdenum and 5% potassium in terms of the total weight of the catalyst. After the last impregnation, the calcination temperature is raised to 500 C. Then the catalyst is passivated with 2% oxygen in
    nitrogen at maximum temperature.
    The catalyst is placed in a 1/2 inch (1.27 cm) diameter stainless steel tube. The total catalyst volume is 30 cm. The weight of the catalyst is 22 g. The composition of the obtained catalyst and. The catalysts according to examples 2-5 are given in table. 1. A preformed mixture of carbon monoxide and nitrogen is passed from the cylinder through a layer of molecular sieve at ambient temperature to remove iron carbonyl and other carbonyls. Then, hydrogen and dilindar hydrogen sulfide are mixed with carbon monoxide and nitrogen and the mixture is compressed to a predetermined pressure. Nitrogen is added to a level of 5% to create an internal standard for analytical purposes. Methanol is added in a predetermined amount using a liquid injection pump.
    Then, the combined stream consisting of the feed gas and methanol is heated and passed at a predetermined flow rate through a fixed bed reactor that is maintained at an predetermined reaction temperature using an electric furnace.
    The product from the reactor passes through a pressure reducing valve to the vapor / liquid separator at room temperature. The resulting gases leaving the separator exit through the gas chromatograph opening for sampling through the second lower pressure valve to a condenser cooled with dry ice. Liquid products from the vapor / liquid separator and condensate are combined, weighed, sampled for analysis and analyzed. The data presented are the results of the analysis of both samples. The results of the experiment are presented in table. 2
    The reaction conditions in Comparative Example A and Example 1 are the same, with the exception that in Comparative Example A there is no methanol, and in Example 1 methanol is supplied. The addition of methanol leads to an increase in the production of higher C-C-SPIRTS.
    Examples B (comparative) and 2. Co-precipitated molybdenum sulfide and cobalt are used together (Table 1).
    Ammonium tetrathiomolybdate (NH) .MoS, and cobalt acetate in a molar ratio of molybdenum: cobalt 2: 1 are added to 30% acetic acid at 50 C. The precipitate is filtered and dried under nitrogen at 120 s, then calcined for 1 h at 500 C in nitrogen atmosphere. The dry cake is then ground together with potassium carbonate, bentonite clay and sterotex (Sterotex) to achieve a weight ratio of wt.%, CoS / 2MoS "66, potassium carbonate 10, bentonite clay 20 and sterotex 4. Then the mixture is tableted at a pressure of 30,000 lb / sq. inch (g) (20.8 MPa) and tablets are stored in a nitrogen atmosphere until consumed.
    The reaction system for these examples is the same as for Comparative Example A and Example 1. The total volume of catalyst is 30 cm. The weight of the catalyst is 32.7 g. The working conditions and results are presented in Table. 3
    The reaction conditions for comparative example B and example 2 are the same, with the exception that methanol is not given in comparative example B, but supplied in example 2. Addition of methanol leads to an increase in the formation of higher C-C alcohols and an increase in the formation of esters of acetic acid.
    Examples C (comparative) and 3. In additional experiments, ethanol is added to the raw mix.
    The catalysts are the same as in example 2. The reaction is carried out in the same apparatus as in example 2. The parameters and the results of the reaction are presented in table. four.
    Ethanol is converted to higher alcohols. However, ethanol conversion is not as effective as methanol conversion.
    Examples D (comparative) and 4. The reaction was again carried out with ethanol using the same catalyst and reactor as in Example 2. The reaction conditions and results are presented in abl. five.
    Examples E (comparative) and 5. In these examples, molybium-virgin disulfide without carrier is used as a catalyst, comprising tablets consisting of 66% molybdenum disulfide (special molybdenum disulfide with a high surface from Climax Molybdenum), 20% bentonite 15 clay , 10% potassium carbonate and 4% stereotex.
    In comparative example E and example 5, the reactor consists of a jacketed stainless steel tube packed with a catalyst. The total catalyst volume is approximately 1 cubic foot. (0.028 m). A heat transfer medium is stored in the jacket of the reactor for removal of heat. The feed gas carbon monoxide passes through a layer of molecular sieve at room temperature to remove iron carbonyl and other carbonyls. ZOR Then the feed gases hydrogen and carbon monoxide are mixed in a given ratio from 300 m, d. hydrogen sulfide; 2 vol.% nitrogen is added to the feed gas as an internal standard and the mixture is compressed to a predetermined pressure. Methanol is added. The mixture of methanol and feed gas is heated to the desired
    sampling for gas chromatograph. Liquid products from the low pressure seperator are collected in a receiver from which samples can be taken for analysis.
    The operating conditions in the reactor for comparative example E and example 5 are presented in table. 6
    The addition of methanol leads to an increase in the formation of higher spir-, hue and an increase in the formation of acetic acid esters. I
    The proposed method compared
    with the known, it improves the quality of the target mixture due to an increase in the content of higher alcohols (or, accordingly, a decrease in the methanol content). Increasing the content of higher C2-C alcohols in the mixture gives it the best qualities when using this mixture as fuel additive: it increases the octane number of motor gasoline and its detonation resistance, reduces the mixing octane characteristic of vapor pressure according to Reid, increases the water resistance of gasoline.
    权利要求:
    Claims (3)
    [1]
    1. A method of producing a mixture of aliphatic C.-C-alcohols by the interaction of hydrogen and carbon monoxide at a molar ratio of 1.05-1.12: 1 at a temperature of 233-290 ° C and a pressure of 12.5-20.8 Sha in the presence of heterogeneous a catalyst containing as the first component the sul-reaction temperature and then passing the molybdenum feed or its mixture with the sulf through the reactor with a fixed bed with a cobalt feed and as the second catalyst at a given bulk component — carbonate alkaline sampling for a gas chromatograph. Liquid products from the low pressure seperator are collected in a receiver from which samples can be taken for analysis.
    The operating conditions in the reactor for comparative example E and example 5 are presented in table. 6
    The addition of methanol leads to an increase in the formation of higher alcohol and to an increase in the formation of acetic acid esters. I
    The proposed method compared
    with the known, it improves the quality of the target mixture due to an increase in the content of higher alcohols (or, accordingly, a decrease in the methanol content). Increasing the content of higher C2-C alcohols in the mixture gives it the best qualities when using this mixture as fuel additive: it increases the octane number of motor gasoline and its detonation resistance, reduces the mixing octane characteristic of vapor pressure according to Reid, increases the water resistance of gasoline.
    Invention Formula
    I
    speed. Products from the reactor are passed through a water cooled condenser to a high vapor / liquid separator. Liquid products from the high pressure separator are passed through a pressure reducing valve to the low pressure vapor / liquid separator. The gaseous products leaving the high pressure separator are passed through a pressure reducing valve, connected to the gases leaving the low pressure separator, and the flow passes through the point
    Tall, characterized in that, in order to improve the quality of the mixture, the process is carried out in the presence of methanol or ethanol added to the initial stream of hydrogen and carbon monoxide.
    [2]
    2. The method according to p, 1, differs - 50 u and in order to use a heterogeneous catalyst on a carrier. ;
    [3]
    3. Method according to clause 1, differ-. u and with the fact that using methanol obtained by fractionation
    5 mixtures of aliphatic C-C alcohols.
    SteEotex is a powdered vegetable stearin made from cottonseed oil.
    Volume / volume per.
    Table 1
    table 2
    Temperature, C Pressure, psi inch (gauge) MPa
    chosg On / with, molar ratio
    Concentration level
     Volume / volume per H ,, / WITH.
    Process conditions
    Temperature, C Pressure, psi (g) MPa
    COSH, h molar ratio
    Volume / volume per.
    T a
    faces
    290
    2000
    13.8 2000
    1.05
    Table 4
    Example
    (comparative)
    289.
    2000
    13.8 3000
    Volume / volume per H2 / CO.
    Table 5
    Table
    6
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    同族专利:
    公开号 | 公开日
    DE3576685D1|1990-04-26|
    AU574809B2|1988-07-14|
    KR860003999A|1986-06-16|
    AU4513585A|1986-05-15|
    EP0180719A2|1986-05-14|
    CA1268189A|1990-04-24|
    YU124485A|1987-12-31|
    CN1007346B|1990-03-28|
    EG17829A|1990-12-30|
    PL254734A1|1987-02-09|
    NO852992L|1986-05-06|
    JPS61115038A|1986-06-02|
    EP0180719A3|1987-07-15|
    BR8503591A|1986-09-16|
    EP0180719B1|1990-03-21|
    ZA855550B|1987-03-25|
    CN85105799A|1986-11-19|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    US4272410A|1979-05-14|1981-06-09|Ethyl Corporation|Catalyst for preparation of oxygenates from carbon monoxide and hydrogen|
    DE3045891C2|1980-12-05|1983-03-03|Union Rheinische Braunkohlen Kraftstoff AG, 5000 Köln|Process for the production of acetaldehyde and ethanol|
    JPH0451530B2|1983-03-18|1992-08-19|Dow Chemical Co|
    US4625050A|1983-06-23|1986-11-25|Chevron Research Company|Ether homologation to esters and alcohols using a heterogeneous sulfided catalyst|DE3776564D1|1987-04-24|1992-03-12|Amoco Corp|TURNOVER OF SYNTHESIS GAS.|
    GB2210615A|1987-10-08|1989-06-14|Coal Ind|Alcohol synthesis process|
    US4886651A|1988-05-18|1989-12-12|Air Products And Chemicals, Inc.|Process for co-production of higher alcohols, methanol and ammonia|
    TW200519072A|2003-08-21|2005-06-16|Pearson Technologies Inc|Process and apparatus for the production of useful products from carbonaceous feedstock|
    WO2006123150A1|2005-05-20|2006-11-23|Bp Chemicals Limited|Process for the conversion of synthesis gas to oxygenates|
    CN101203473B|2005-05-20|2011-11-30|英国石油化学品有限公司|Process for the conversion of synthesis gas to oxygenates|
    GB0510356D0|2005-05-20|2005-06-29|Bp Chem Int Ltd|Process for the conversion of synthesis gas to oxygenate|
    WO2008048364A2|2006-04-13|2008-04-24|Dow Global Technologies Inc.|Mixed alcohol synthesis with enhanced carbon value use|
    WO2007138300A1|2006-06-01|2007-12-06|Bp Chemicals Limited|Process for the conversion of synthesis gas to oxygenates|
    CN101310856B|2007-05-24|2010-10-13|中国科学院大连化学物理研究所|Catalyst for directly synthesizing high carbon primary alcohol using CO hydrogenation and preparation method thereof|
    CA2751942A1|2009-03-06|2010-09-10|Albemarle Europe Sprl|Bulk sulfidic mixed metal catalyst and methods for its manufacture and use in converting syngas to alcohol|
    AU2012298999B2|2011-08-22|2017-06-15|Albemarle Corporation|Methods and apparatus for sulfur management in catalytic mixed-alcohol synthesis|
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    WO2015085002A1|2013-12-04|2015-06-11|Greenyug, Llc|Production of butyl acetate from ethanol|
    WO2017031439A1|2015-08-19|2017-02-23|Greenyug, Llc|Composition of catalysts for converion of ethanol to n-butanol and higher alcohols|
    CN109294812B|2018-11-20|2022-02-11|广西壮族自治区农业科学院农产品加工研究所|Preparation method of low-methanol banana wine|
    CN113019404B|2021-03-23|2022-02-18|中国科学院兰州化学物理研究所|Nickel-based catalyst for synthesizing high-carbon alcohol and preparation method and application thereof|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    US66859884A| true| 1984-11-05|1984-11-05|
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