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    • 专利摘要:
    1505404 Isomerizing alkenes SNAMPROGETTI SpA 17 July 1975 [2 Aug 1974] 30141/75 Heading C5E Alkenes are isomerized with a silica-surface - modified alumina catalyst which has been produced by impregnating alumina with an organosilicon compound containing radicals, at least one of which is other than OH, pyrolysably bound to silicon, and subjecting the treated alumina (substantially free from unreacted impregnating material and any volatile reaction products) to calcining. The alumina may contain 0À5-12 wt. per cent of surface-modifying silica. Preferred organosilicon compounds are esters of orthosilicic acid. Examples describe the isomerization of butenes and pentenes.
    公开号:SU906360A3
    申请号:SU752159094
    申请日:1975-08-01
    公开日:1982-02-15
    发明作者:Манара Джованни；Фатторе Витторио；Нотари Бруно
    申请人:Снампрогетти С.П.А. (Фирма)；
    IPC主号:
    专利说明:

    39 The method is performed by cj eating the image. The mechanical properties of materials consisting of metal oxides can be improved by treating these materials with a silicon compound and subjecting the product thus obtained to drying and controlled oxidation. Silicon compounds have the general formula: where X, Y, Z and W can be - R, OR, -C, Br, -SiHj, -COOR, -SiHf, G9ni, and can be both hydrogen and alkyl, cycloalkyl, an aromatic, alkyl aromatic, alkylcycloalkyl radical having 1-30 carbon carbon, such as, for example, methyl, ethyl, p-propyl, isopropyl, p-butyl, isobutyl, cyclohexyl, cyclopentyl, phenyl, phenylcyclohexyl, or alkylphenyl, and p and m can be integers from 1 to 3. Among these compounds, orthosilicic acid esters such as l, ethyl, propyl isopropyl, isobutyl and p-butyl tetrasilicates. The materials that can be processed by these methods are all oxides, in particular oxides of aluminum, titanium, magnesium, silicon, chromium, zirconium, iron, or mixtures of the said oxides inside this group or with other compounds. When treating oxides of aluminum in this way, the latter are converted to more active and selective catalysts for the skeletal isomerization of olefins. The catalysts obtained in this way are very resistant to hydrothermal conditions; to catalyst regeneration by air, since the surface silicon layer formed by the reaction of the OH groups of the surface of alumina and silicic ester increases the stability of the gamma and eta forms of alumina. This leads to an increase in the service life of such catalysts compared to conventional ones and an improvement in production savings. Secondary cracking and polymerization reactions are inhibited, and the decrease in catalyst activity between regeneration operations is slower than the known catalysts used for isomerization reactions. The catalyst is prepared so that it contains on the surface of alumina 0.5 to 12 wt.% Silicon oxide (preferably from 1-7%), calculated on the total final weight of the catalyst. The process of skeletal isomerization can be carried out by contacting the olefin or olefin mixture (possible in the presence of alkanes and other inert gases such as nitrogen or CO2) with a catalyst at 300-BOO C and preferably itOO-550 ° C. The working pressure is atmospheric, but for each individual olefin or mixture of hydrocarbons to be treated, but it can be chosen which is most acceptable. The volumetric feed rate, (volume-hours) may be in the range of 0.1-20 and preferably 0.210. Example 1.100 g of alumina is placed in an autoclave together with 20 g (Cr, HcO) u5 |. Autoclave pumped out i. 5 chi are repeatedly washed with gaseous N in order to remove traces of 0, and then raise in it pressure up to 5 kg / cm -. The autoclave is heated to 200 ° C and maintained at this temperature for t hours. After that, it is cooled, pressure is reduced and aluminum oxide is extracted, which is subjected to appropriate heat treatment at 200 ° C for 2 hours in the presence of nitrogen, and then calcined in air for k hours at 500 ° s When analyzing the content of Si 0 obtained by this method of gamma-ALOa spheres, the content of Si i Oj equal to 5) 0 wt.% Was found. Samples of alumina used in experiments on the catalytic activity in the skeletal isomerization of alkenes. Example 2. Gamma-alumina in a video sphere with a diameter of 3- + mm is dried with a stream of nitrogen at 450 ° C. Characterization of spherical aluminum gammoxide A. Bulk weight, g / cm 0.51 Surface area (BET), 301 Total pore volume, cMVr0.879 NaijO,% 0.07 For comparison, one of the portions M is used right after drying, while as the other (C, H50) Si is treated as in Example 1, so the alumina content is 5.6 weight D. The catalyst, as well as the alumina untreated with the silicon compound, is tested in skeletal isomerization tests hydrocarbon 4 ( C4 O-pefins), having the following composition. %: C -C7 | -hydrocarbons 0.37 n-butane. 3.23. p-butane 16,51 TRChns-butene-2, 03
    (SBT) feed- (SBL) pin X 100
    Conversion, (2WT) feed
    (isobutane) output x100 (SBT) feed (SBL). conclusion
    Conversion of Selectivity Output C. + on (saturated hydrocarbons, -S Output C5 + hydrocarbons, Z
    The symbols given have the following meanings:
    SBL - Linear butenes - trans-butene-1 + and, is.-6uten-2; CVT - 2 all butenes - hRachs-butene-2 + butene-1 + and, is -but. En-2 + isobutene;
     saturated hydrocarbons -1 b hydrocarbons +
    + isobutene + C5 butene + - products with 5 or more carbon atoms.
    Based on the above equations, the table is compiled. 2 - the behavior of the catalyst in the work before and after its treatment with silica.
    (isobutane) output xjOO teBT) feed 100
    By modifying the catalyst with silicon derivatives, the conversion of linear butenes increases, increasing simultaneously with selectivity.
    The yield of isobutene is increased from ll on untreated alumina to 26% in the presence of promoted alumina. In addition, the decrease in the activity of this catalyst while achieving the same results is less,
    Example 3. 10g of spheroidal gamma-A yrz of grade B are treated with 20 g of tetraorthosilicate in accordance with .C4 + saturated hydrocarbons) output (C + saturated hydrocarbons) podama x100 (Cg +) output1100 (I.3T) feed 06 isobutene150 butene-1b4zb Each of the two catalysts is placed in a fixed bed of a tubular reactor with a volume of 20 cm. The power supply is passed through the catalyst bed at a temperature of 92 ° C and atmospheric pressure with a bulk velocity of 1.70 g / g. The effluent from the reactor is subjected to gas chromatographic analysis after condensation of product Cjj at room temperature. The weight composition of the effluent according to this analysis is given in Table. one . The data show that the treatment of the catalyst) Si gives more than twice the amount of isobutene from the outlet of the catalytic reactor. For an effective comparison, the calculation is carried out using the following equations (SBT), the VII feed with example 1. Si On content in the final product is 5%. Characteristics of spheroidal ga m-alumina B. Bulk weight, g / cm Surface area, MVr Total pore volume, h / g,% Comparative tests of alumina containing 5% silica and the same, but untreated alumina is carried out on the isomerization of hydrocarbons in the apparatus of example 2. Table. 3 shows the results obtained when operating at atmospheric pressure, a temperature of 92 ° C, a space velocity of 0.77, and a volume of catalyst bed of 20 cm. As can be seen from the table. 3, modification of the catalyst with silicon derivatives leads to a sharp increase in the conversion, as a result, the output of isobutene after 1.5 hours increases from 12.3 to 21.1, and after 3.5 m-s8.5 to 17,%. These figures show that promotion maintains its positive effect over time and leads to a double effect: an increase in catalyst activity and an increase in its service life. An example. Gamma alumina, for comparison, is partly used without treatment, and partly treated with various amounts of tetraethyl orthosilicate. Properties of gamma-alumina macas C. Bulk weight, g / cm 0.55 Surface area, 169 Total pore weight, CMVr0.56, part per million 20 100 g, such is treated with 5 g of tetraethyl orthosilicate to obtain a finished catalyst with 1.6 SiOr, and 100 g of the same A 2 (0J - 10 g of tetraethyl orthosilicate, and a catalyst is obtained from 2.9%. All three catalysts obtained by the methods described are tested in skeletal isomerization of fraction C, according to example 2, at atmospheric pressure 4 bg 5 C, in a heated tubular reactor fixed bed roll 8 mash volume of 50 cm. Results for three catalyst m are given in Table K. From Table A, it is known that the promotion of raMMa-ASiOj brand C increases its catalytic activity, leading to the same conversion as that of untreated, but with a volumetric rate 2.5 times greater. effect on selectivity, which increases by 10-15X, and increases the service life of the catalyst. A material containing 2.9 SiO (j, after and at a space velocity of 2.5 times higher retains a higher activity than the raw catalyst after 2 h Example 5. The same aluminum oxide as in example 4, soda Neighboring 1.6% for comparison, the same non-promoted alumina is used for isomerization of pure trans-butene-2, operation at atmospheric pressure with a catalyst bed of 50 cm. The results of the isomerization are given in Table. 5. The volumetric rate at which the catalyst works is three times higher and, despite this, the conversion and selectivity are higher than when working with a conventional catalyst. Isomerization of tRais-butene-2 is carried out on the same catalysts at 515 C, atmospheric pressure and with a catalyst bed of 50 CMI. Data isomerization are given in table. 6. At this temperature, ordinary alumina loses 13% selectivity, while 1.65 SfOo loses only 2%. This suggests that the proposed catalyst operates in a wider temperature range with all the attendant advantages in the isomerization reaction rate and, as a result, in the size of the plants without noticeable losses in the form of undesirable products. The volumetric rate at which promoted alumina works is four times higher than when working with untreated alumina. Example 6. 100 g of D-grade alumina are treated with 20 g of tetraethyl orthosilicate of Example 1 so that the SiOQ content of the final product is k, 8%. 9 Characteristics of D. gamma-alumina. Bulk density, g / cm 0.95 Surface area, m g210 Total pore volume, cm / g Small, Untreated alumina and alumina, containing, SiO, isomerization of olefins C, ; having a composition according to example 2, operation at atmospheric pressure, a temperature of 92 ° C, and a catalyst bed of 20 cm. The test results of the catalyst are given in table. 7. A catalyst containing oxide krni, at the same speed as the catalyst without silica, leads to a conversion of 27-28; against 5.7-5.8, and the yield of isobutene increases from c to t to 17. In addition, alumina, which in itself has no isomerization activity, can be an effective isomerizing catalyst when treating tetraethyl tosilicate. Example 7. Extruded E gamma alumina with a 1.5 mm diameter mBtpoM part has the following properties. Bulk density, g / cm 0.72 Surface area, Mvr3 9 Total pore volume, 60 per 0, part per million 0 Such alumina is divided into portions of 100 g each and is treated with 5, 10, 13 and 18 tetraethyl orthosilicate, respectively according to the method described in example 1. The resulting catalysts contain, respectively, 1.5, 2, +, 3.5 and 8, SiO. These 4 catalysts are used for isomerization of feed C, whose composition is given in Example 2, operating in a fixed bed reactor with a volume of 50 cm at atmospheric pressure. The test results of the catalysts given in the temperature range 45b-92 ° C are given in Table. eight.
    Conversion,% 100 - (isobutane) output. As can be seen from the table. 8, obtained on these catalysts, with the exception of one containing 8, SiOu, which, at very high activity, reduces the selectivity to a moderate degree, a high selectivity is achieved. Thus, the best results in the isomerization of olefins Sc. are obtained when the amount of silicon oxide introduced into the catalyst is in the range of 1 to 7%, while catalysts with 812 SiOij show high activity with moderate selectivity. Example B. The same E-type gamma-alumina catalyst with 1.5% of example 7 is subjected to a test for the duration of time, work on a baseless catalyst bed of 20 cm with the flow of hydrocarbons C /, whose composition is given in example 2 The results are shown in Table. 9 show that the catalyst maintains the output at values over 30 for a very long time, so that periodic regeneration, which is necessary for known catalysts in the technique after 3-5 h of operation, can be carried out at large (15-20 h) time intervals. Example 9. 100 g of gamma-alumina brand C, whose properties are given in example 7, are treated with 5 g of tetraethyl orthosilicate in accordance with the procedure described in Example 1. The catalyst obtained in this way, containing 1.6 SiOj, is used for the skeletal isomerization of isobutene in linear butenes. Supply flow of pure isobutene at. 65C in a catalyst bed with a volume of 20 cm at a space velocity of 1 and 0.6 g / gh, the results are obtained after an hour's run, which are given in table. 10. The resulting linear butenes consist of A5- 6% TRAN-butene-2, 27-28% butene and 10-12% a, i-butene-2. The results are calculated using the following formulas.
    (SBL) output x 100
    li100 - (isobutene) yield%
    Conversion X Selectivity
    The output of linear butenes,%
    Yield, C + saturation, (C l + saturated hydrocarbons) output hydrocarbons I Yield C5 + O (% +) yield. The high conversion and selectivity obtained in the reaction should be noted; this makes it possible to use catalysts for the isomerization of isobutene to linear butenes with excellent yields. Example 10. Pure trans-butene-2 is blown over grade A alumina and over the same alumina containing 5.6 Si On as in example 2 over the course of h. After such a time of operation, the isomerization activity drops to almost zero due to the deposition of carbonaceous products on the catalysts. Both catalysts are regenerated by air blowing in such a way that the burning of carbonaceous products proceeds very quickly. Under these conditions, the temperature of the gas in contact with the catalyst reaches. Usually, regeneration of deactivated carbon deposits catalysts is carried out in the same way, but at a gas temperature not higher than 600650 ° C. However, such an operation is very time consuming and reduces the use time of the equipment. Accelerated operation can give de. These advantages in the intensification of equipment operation. Such a radical treatment can manifest the behavior of materials when repeated regenerations are carried out at low temperatures. Conversion% 100 - (SPL) output
    (SIP) output x 100
    Selectivity 100 - (SPL) output in isobutene,% Conversion X Output of isopentenes,%
    Output С СJ, (Cj) output Output С +,% () output
    906360
    12
    - (SBL) output LLP Table. 11 shows the results obtained when testing a catalyst recovered in this way on the isomerization of trans-butene-2 at it92 ° C. Practically the lack of conversion of tra-c-butene-2 to alumina A refers to the absence of isobutene formation, cracking or alkylation of products, according to the conditions given in Example 2, while the formation of linear butenes, butene-1 and butene-2-i, was observed. In contrast, the activity of alumina with 5.6% Si On remains very good even after regeneration carried out under stringent conditions. Example 11. The catalyst from gamma-alumina E containing 3.5 Si On and described in example 7, serves pure penten. The operation is carried out in a tubular reactor at atmospheric pressure and temperatures of 420 and iSO C with a catalyst bed volume of 20 cm. The effluent from the reactor contains, in addition to linear pentene, isopentenes, which are useful reaction products and small amounts of cracking products (.C) and alkylation (), The following definitions are used to express the results. Selectivity (SIP) output The above symbols have the following PL values for linear pentenes-pentenes-1 + cis-penten-2 + + transpentin-2; . 1 P branched isopenthenes-2-methyl-butene-1 + 3-methyl-butene-1 + 2-methi-butene-2; C (j /, C + Cg + C + C d - saturated and unsaturated hydrocarbons; C- + products with 6 or more carbon atoms, the yield means the products at the outlet of the reactor. Table 12 shows the results of the tests carried out, Promoted oxide aluminum is a valuable catalyst for the isomerization reaction of linear pentenes to isopentenes. 12. Gasoline fraction Example obtained by cracking distillation in the temperature range 75-150 ° C, containing alkenes with more than 5 carbon atoms and having an octane number according to the test method (RON ) 86, 5 dl product without a Kilov lead when passed over the rolled wort consisting of gamma + 1, 6t SiOn, s described in Example 96 Yield of liquid products, coke, 0.35, 3.7 and light solids.
    Composition,
    Aluminum oxide A indicators
    Run time, h
    Volumetric speed, g / g h
    C (2 -Cj-hydrocarbons Isobutane p-Butane trans. -Butene-2 Isobutene Butene-1 c
    Aluminum oxide
    3.5 2.25 0T The investigated octane number (RON) for the reaction product without lead alkyls was 90.1, an increase, thus, was 3.6 RON. This increase is achieved by the skeletal isomerization of alkenes having more than 5 carbon atoms contained in the isomerized product. Example 13. Extruded technical gamma-alumina with a particle diameter of 5 cm, the properties of which are described in example 7, is divided into two parts, 100 g each, process respectively 1.6 and 2, f g of tetraethyl orthosilicate in accordance with the procedure described in example 1, so that two catalysts are obtained containing, respectively, 0.5 and 12 SiOij. Both catalysts were used to isomerize the charge Cd, the composition of which is given in Example 2. The process was carried out in a fixed-bed reactor with a volume of 50 cm and atmospheric pressure. The test results of the catalysts carried out at 42- 92s are given in table. 13. Good selectivity values obtained with a catalyst containing 0. SiOi2 is quite obvious, whereas the catalyst containing silica is very active, but it is characterized by moderate selectivity. T a b l and c a 1 I Oxide of aluminum A Indicators
    1,53,52,25
    1,721,701,66
    15,11,633,3
    73,97,178,1
    11.48,626.0
    0,60,0,4
    3,52,62,9 Aluminum oxide V Indicators
    6 8
    1.76 1.83
    921.8
    79.178,9
    19.7
    17.2
    4.0
    3.5
    3.0
    1.6
    2.5
    1.7 Table 2 Aluminum oxide A + 5.6% Si 02 Table 3 I Aluminum oxide B + 5% SiO
    Table k
    17
    Temperature, 0 Runtime, h Volume rate, g / g h Conversion,% by weight Selectivity in isobutene. Isobutene yield,% by weight
    Output C d + saturated hydrocarbons, i by weight
    Output C5 +,% by weight
    Temperature, ° С Runtime, h Volume rate, g / g m Conversion, / by weight Selectivity, X by weight Isobutane yield, f, by weight
    Output up to C 4 + saturated hydrocarbons, /; by weight
    Output C with +, X by weight Alumina Catalyst
    18
    906360 Table 5
    Table 6
    515
    one
    2.6
    33.3
    69,6
    22.3
    8.5
    1.6
    Table 7 D1 Aluminum oxide D + 4.8% SiOn
    Table 8
    21
    Temperature, С Runtime, h Volume rate, g / g h Conversion,% by weight
    Selectivity, to linear butenes,% by weight
    The output of linear butenes,% p
    Output Cd + saturated hydrocarbons,% by weight
    Output Cr +,% g (about weight
    Temperature, Volume speed, g / g-h Runtime, h Conversion, / 1 by weight Selectivity, by weight Isobutene yield, /, by weight
    Output C + saturated hydrocarbons, / by weight
    Output 0 +, /, by weight
    Temperature, ° С. Volumetric rate, g / g. h Conversion, / g, by weight Selectivity,% by weight Yield of isopentenes, -S by weight Yield (.Cj, o by weight Yield C +,% by weight
    906360
    .. Table 10
    one
    0.6 56, A
    78,
    14, 2
    8.2. .-.ABOUT
    Table 11
    1, 28
    1,3
    28,8
    72.2
    20.8
    5.3.
    tweets 2.7 tweets
    Table 12
    ten
    37,8
    72.9
    27.6
    2,
    7,8
    23
    权利要求:
    Claims (2)
    [1]
    1. Method of iso-olefin half-spheres by isomerization of a fraction of y-hydrocarbons containing olefins in the presence of an alumina-based catalyst at an elevated temperature, characterized in that, in order to increase the yield of the target product, alumina, p.
    906360 Table 13
    surface modified 0.512 wt.% silica.
    [2]
    2. The method according to p. 1, characterized in that the process is a wire at COO-BOO C, preferably fOO550 ° C.
    Sources of information taken into account in the examination
    1. US patent YY 3631219, cl. C 07 C 5/22, published 197 (prototype).
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    同族专利:
    公开号 | 公开日
    SE399878B|1978-03-06|
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    IN143979B|1978-03-04|
    AT347416B|1978-12-27|
    CA1046089A|1979-01-09|
    YU37297B|1984-08-31|
    NO752709L|1976-02-03|
    HU178718B|1982-06-28|
    AU8309575A|1977-01-20|
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    JPS5858387B2|1983-12-24|
    FR2280613A1|1976-02-27|
    IE43063B1|1980-12-17|
    US4038337A|1977-07-26|
    NO147875C|1983-06-29|
    NL7509285A|1976-02-04|
    CS188964B2|1979-03-30|
    AR205576A1|1976-05-14|
    ZA754580B|1976-07-28|
    EG12473A|1979-03-31|
    MW4875A1|1976-10-13|
    DE2534459C2|1982-08-19|
    DK142409B|1980-10-27|
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    BG31222A3|1981-11-16|
    FR2280613B1|1978-12-08|
    PL102873B1|1979-04-30|
    BR7504977A|1976-07-27|
    NO147875B|1983-03-21|
    GB1505404A|1978-03-30|
    MX142985A|1981-02-02|
    DD119032A5|1976-04-05|
    BE832060A|1976-02-02|
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    引用文献:
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    FR2714051B1|1993-12-22|1996-02-02|Inst Francais Du Petrole|Process for skeletal isomerization of olefins using an alumina-based material.|
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    IT1271313B|1994-12-21|1997-05-27|Enichem Spa|INTEGRATED PROCESS FOR THE PRODUCTION OF TER-AMYL ALCHYL ETHERS|
    DE19545042A1|1995-12-02|1997-06-05|Studiengesellschaft Kohle Mbh|Amorphous microporous mixed oxide catalysts with controlled surface polarity for selective heterogeneous catalysis adsorption and material separation|
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    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    IT25943/74A|IT1017878B|1974-08-02|1974-08-02|PROCESS FOR THE ISOMERIZATION OF ALKENES|
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