• 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:
    OXIDATION CATALYST FOR 0-XYLENE alkali metals naphthalene into phthalic anhydride, containing 4-15 g of active part, consisting of vanadium pentoxide, niobium pentoxide, phosphorus pentoxide, titanium dioxide and oxide selected from the group consisting of potassium, cesium, rubidium, thallium per 100 ml of carrier, and carry,. The body, characterized in that, in order to increase the stability of the catalyst, it contains porous titanium dioxide in anatase form with a particle diameter of 0.40, 68 µm, specific surface 11-57 with a total pore volume of 0.15-0.45 µm 55, 0-8.8.0% of the pore volume with a diameter not exceeding 10 microns, as a carrier, the catalyst contains silicon carbide or a mixture of 80-92% silicon carbide, 2-8% alumina and the rest is silicon dioxide with an apparent porosity of 13-42% , and the active part has the following composition,% by weight: (L P vanadium dioxide 0,99–19,87 P niobium oxide 0.01- 0.99 Phosphorus thioxide 0.20-1.17 Metal oxide selected from the group consisting of potassium, cesium, rubium 4, di, thallium 0.05-1.17 h1 Titanium dioxide Residue N9 4
    公开号:SU1147244A3
    申请号:SU792847109
    申请日:1979-11-28
    公开日:1985-03-23
    发明作者:Сато Такахиса；Наканиси Есиюки；Маруяма Кейзо；Сузуки Такехико
    申请人:Ниппон Шокубаи Кагаку Когио Ко.,Лтд (Фирма)；
    IPC主号:
    专利说明:

    1 The invention relates to catalysts for the oxidation of aromatic hydrocarbons, in particular to catalysts for the oxidation of o-xylol or naphthalene to phthalic anhydride. Known catalyst for the oxidation of o-xylene or naphthalene to ft left anhydride, containing the active part comprising 1-40 wt.% Vanadium pentaio and 60-90 wt.% Tanna dioxide in anatase form, as well as 0.01-0. , 15% sodium or potassium oxide. The disadvantage of the catalyst is its short lifetime and low activity. v The closest to the invention is an oxidation catalyst (α-xylene or naphthalene to phthalic anhydride, containing an active part consisting of 1-20% by weight of vanadium pentoxide, 0.2-5.0% by weight of niobium oxide , 0.1–5.1 wt.% Of phosphorus ptooxide, 0.05–0.5 wt.% Of potassium oxide and / or cesium oxide, and / or rubidi oxide and metal oxide selected from the group consisting of rare earth metal, zinc, thallium, and a carrier consisting of 5090, 9 wt.% silicon carbide, 0.110 wt.% alumina and aluminum silicate, the catalyst containing 3-15 g of the active part per 100 cm n ositel 2. However, the known catalyst does not have sufficiently high stability — within 3 months of operation, the catalyst activity decreases by 5%. The aim of the invention is to increase the stability of the catalyst. This goal is achieved by the proposed catalyst for the oxidation of o-xylene or naphthalene to phthalic anhydride containing 4-15g of the active part, including, per 100 ml of carrier,% by volume: Vanadium pentoxide 0.99-19.87 Pb niobium oxide 0.01-0.99 Phosphorus pentoxide 0.20-1.17 Oxide of a metal selected from a grupp including potassium, cesium, rubidium, thallium 0, 05-1.17 Titanium Dioxide Else, while the porous titanium dioxide contains a catalyst in anatase 41 form with a particle diameter of 0.4- (0.68 micron, specific surface 11-57, total pore volume of 0.15-0.45 micron 55 , 0-88.0% of the pore volume with a diameter not exceeding 10 microns, and the support, in which the catalyst contains silicon carbide or a mixture of 80-92% silicon carbide, 2-8% alumina and the rest is silica with an apparent porosity of 1342%. The proposed catalyst has an increased stability; the yield of phthalic anhydride remains practically at the same level for 6–12 months. work, while on the known catalyst after 3 months. Code of phthalic anhydride is reduced by 5%. The catalyst contains an active part comprising vanadium pentoxide, anatase titanium dioxide, which is a porous material with a particle diameter of 0.4-0.68 µm and a specific surface area of 11-57, niobium pentoxide, phosphorus pentoxide and one of the oxides such as potassium oxide, cesium oxide, rubidium oxide or thallium oxide, and a porous support consisting of silicon carbide or a mixture of 10% alumina and silicon carbide with an apparent porosity of 13-42%, on which the indicated active part is applied. Anatase type titanium dioxide is used as a source of titanium dioxide, which is a porous substance with a particle diameter of 0.4-0.68 µm and a specific surface area of 11-57, more preferably 15-40. Anatase type titanium dioxide is obtained by displacing ilmenite with sulfuric acid at a concentration of 70-80%, allowing them to fully react with each other, diluting 1 part product with water to produce an aqueous solution of titanium sulfate, adding pieces of iron, reducing iron in the ilmenite, cooling the product to precipitating and separating ferric sulfate, as well as to obtain an aqueous solution of high-purity titanium sulfate, purging this aqueous solution with superheated 3 water vapor at 150-170 ° C spruce hydrolysis and precipitation of hydrous titanium dioxide and calcining the resulting titanium dioxide at 600-900 C ,. The specific surface of product 11-57 corresponds to a particle diameter of 0.05-0.20 µm of non-porous anatase-type titanium dioxide (primary particles). Therefore, titanium dioxide particles are considered as aggregated clumps of such primary particles. Depending on the type of starting ilmenite mineral, titanium dioxide may include iron, zinc, aluminum, manganese, chromium, calcium, lead. These random elements do not have a detrimental effect on the course of the main reaction if their total amount is less than 0.5 wt.% Based on the amount of titanium dioxide. Raw materials for vanadium pentoxide, niobium pentoxide, and phosphorus pentoxide , potassium oxides, cesium oxides, rubidium oxides and thallium oxides are selected from compounds that can be converted to oxides upon growth, in particular, among sulfates, ammonium salts, nitrates, organic acid salts, halides and hydrates of oxides of these metals. In the composition of the proposed catalyst, a porous support is used which consists of silicon carbide or a mixture of silicon carbide and alumina, and the content of alumina in the porous carrier does not exceed 10 wt.%, Preferably it is S 5 wt.%, And the apparent porosity is 13- 42%. The catalytically active material is applied to the support material in a manner known per se. In accordance with the simplest method, a certain amount of carrier is placed in a rotating drum adapted to heat the starter and the liquid sprays the liquid containing the catalytically active material over the carrier material with the temperature maintained at 3,200 ° C. A suitable amount of the catalytic material supported on the carrier is 4-J 5 g / 100 ml of carrier. Next, the catalyst thus obtained is calcined at 300444 600 C, preferably 350-550 C, for 2-10 hours in air flow. The proposed catalyst is used in the oxidation process of α-xylene or naphthalene to phthalic anhydride. The process of catalytic vapor-phase oxidation of o-xylene or naphthalene into phthalic anhydride is carried out by mixing o-xylene or naphthalene with a gas containing molecular oxygen, which contains 5-21% by volume of oxygen, 0-15% by volume of water vapor, 0 -3% by volume of carbon dioxide, 0-3% by volume of carbon monoxide, the rest is nitrogen, and the concentration of o-xylene or naphthalene is adjusted to 5-100 g / nm of gas containing molecular oxygen and the transmission of this gaseous mixtures over the catalytic layer at a temperature (heat carrier 300-400 С, preferably 330-380 С, pressure It ranges from atmospheric to 10 atm and a flow rate of 1000-6000. Example 1. Superheated steam at 175 ° C is rinsed through an aqueous solution containing titanium sulfate and sulfuric acid, resulting in the formation of titanium oxide hydrate (TiOi-nHjO). titanium oxide is washed with water and acid, and then again with water and subjected to calcination for 4 hours. The calcined product is subjected to grinding to a powdery state using an air jet to obtain anatase type porous titanium dioxide. It is 0.5 microns and a specific surface BET equal to 22. To a solution of 1.8 g of oxalic acid in 70 liters of deionized water, 0.86 kg of ammonium metavanadate, 0.136 kg of niobium chloride, 0.067 kg of secondary ammonium phosphate, 0.01 kg of potassium hydroxide, and 0.0556 kg of cesium sulfate are added. what the mixture is carefully moved. To the prepared solution, 16 kg of titanium dioxide prepared by the method described above are then added, and the mixture is emulsified for 40 minutes with an emulsifying apparatus, resulting in a catalytic slurry. 5 150 l of self-bonded silicon carbide, whose porosity is 37%, and a particle diameter of 5 mm as a carrier is placed in a rotating stainless steel furnace adapted for external heating, the diameter of which is. is 2 m, and the length i m is preheated to 200-250 ° C. When rotating the rotary kiln, the slurry prepared according to the described method is sprayed over the carrier material so that the coating material on the carrier material is 8 g / 100 ml Next, the prepared catalyst is subjected to calcination for 6 hours while simultaneously passing an air stream. The active part of the catalyst has the following composition,% by weight: Vanadium thioxide 3.96 Piobio niobium 0.40 Phosphorus thioxide 0.25 Potassium oxide 0.05 Cesium oxide 0.26, Titanium dioxide 95.08 The resulting catalyst is used as a catalyst for the 1st stage of oxidation of laziness. According to the proposed method of preparing a catalytic sludge, the amount of ammonium phosphate secondary is changed to O, 134 g, and in all other ratios, the process of U-MIE is completely repeated. As a result, a catalyst is obtained, the active part of which has the composition, wt.% Vanadium thioxide 3.95 Niobium thioxide 0.40 Phosphorus thioxide 0.50 Potassium oxide 0.05 Cesium oxide 0.26 Titanium dioxide 94.84 Catalyst obtained is a 2nd stage catalyst. In a multi-tubular heat exchanger converter, first, a second stage catalyst is formed to form a layer 1.25 m high, and this converter consists of 250 steel tubes with an inner diameter of 20 m and a height of 3 m, whose inner surface is protected from rust and treated with phosphoric acid. Next, in the container, the catalyst of the first stage is placed with the formation of a layer with a height of 1.25 m, which is 4-6 above the layer of the catalyst of the second stage with a thickness of 1.25 m. temperature Through the upper part of the converter, a gaseous mixture of 0-xylene with air, preheated to 120 ° C, is introduced into it at a space velocity of 2500 pT, and the concentration of c-xylene is maintained at 40 g / nM air. Then the circulating blower for the flue gas is turned on, and when the oxygen concentration in the source gas near the converter inlet reaches 10%, the amount of b-xylene introduced is gradually increased to a level of 83 g / n-m-gas containing molecular oxygen. At the same time, the amount of waste gas that is directed to recirculation is regulated in accordance with the increase in the amount of β-xylene supplied with the calculation of maintaining the oxygen concentration in the gas at the inlet to the converter at a level of 10% by volume. The gas discharged from the converter is cooled to 160 ° C of the heat exchanger and introduced into the refrigerator to crystallize phthalic anhydride. The gas is withdrawn from the refrigerator, maintaining the temperature at its outlet at the level, then the gas is passed through a pipeline, which is maintained at a temperature of 120-130 s, after which 58% of this gas is mixed with air. This mixture is introduced into the converter. The remaining 42% of the exhaust gas is sent to the catalytic combustion system, and after complete combustion, the products of combustion are emitted into the atmosphere. Under these conditions, the concentration of water vapor in the gas at the inlet to the converter reaches 9%. The results achieved during the process for 1 year are summarized in Table. 1. Example 2. Titanium hydroxide obtained. As in Example 1, it was subjected to calcination at 750 ° C for 4 hours and subsequently processed as in Example 1, resulting in a porous anatase type of titanium dioxide, the average particle size of which is 0.45 µm, and the specific surface area

    BET is 28 m / g. In the course of the process, by analogy with Example 1 using anatase-type titanium dioxide and a molded carrier material; which consists of 2 wt.% alumina and 92 wt.% silicon carbide, while the rest falls to silicon dioxide, whose porosity is 42%, and a particle diameter of 5 mm, prepares catalysts, the active part of which is characterized by the following compositions.
    The active part of the catalyst of the 1st stage, wt.%:
    Vanadium pioxide 14.81 Piobio niobium 0.50 P phosphorus thioxide 0.35 Rubidium oxide 0.40 Titanium dioxide, 83.94 Active part of the 2nd stage catalyst, wt.%:
    Vanadium pioxide 7,82 Pb niobium 0.49 P phosphorus thioxide 0.97 Thallium oxide 0.79 Titanium dioxide 89.93 The amount of the active part is 8 g per 100 ml of carrier.
    A first stage catalyst is placed in a stainless steel tube with an internal diameter of 20 mm and a height of 3 m with the formation of a layer height of 0.8 m and a catalyst of the second stage with the formation of a layer height of 1.7 m. Synthetic gas containing 10% by volume of oxygen, 12 vol.% water vapor and 78 vol.% nitrogen, mixed with 80 g / nM of o-xylene synthetic gas, after which the gaseous mixture is passed through catalytic beds.
    Example 3. Titaia oxide, produced in accordance with (fimer 1, is subjected to calcination for 6 hours, followed by treatment by analogy with shchmera 1, resulting in anatase type titanium dioxide, whose specific surface according to BET is 17 m / g and the average particle size is 0.6 µm; CatalysisToind is prepared by analogy with example 1 using software and a sphere {a powder with a porosity of 35% and a carrier diameter of 5 mm.
    The catalyst contains 8 g of the active part per 100 ml of carrier.
    47244 .8
    The active part of the 1st stage has a composition, wt.%:
    Vanadium thioxide 1.99 niobium thioxide 0.40 - phosphorus thioxide 0.20 cesium oxide 0.30
    Titanium dioxide 97,11 The active part of the catalyst of the 2nd stage has the composition, wt.%: To Vanadium pioxide 1.97 Piobio niobium 0.40 P phosphorus perioxide 0.59 cesium oxide 0.30
    Titanium dioxide 96.74: J5 A stainless steel tube with an inner diameter of 20 mm and a height of 5 m is placed in a first stage catalyst to form a 1.8 m high layer and a second Q stage catalyst to form a 1.2 m high layer. Synthetic a gas containing 11% by volume of oxygen, 10% by volume of water vapor and 79% by volume of nitrogen is mixed with 85 g / nm of synthetic 5 o-xylene gas. This gaseous mixture is passed through a catalytic bed. The results are shown in Table. one.
    Examples 4 and 5. In a tube and - from stainless steel, the inner diameter of which is 27 mm and height is 3 m, the catalyst of the first stage, obtained as in example 1, is placed with the formation of a layer 1.5 m high, and then the catalyst of the second stage, obtained according to example 1, with the formation of a layer with a height of 1.5 m. With further use of air as an oxidizing agent and using the prepared catalytic layers, 0-xylene is oxidized.
    Example 6. Get catalysts according to example 1, containing 8 g of the active part per 100 ml of carrier.
    As a carrier material. At the same time, self-bonded silicon carbide is used, with a particle diameter of 5 mm and a porosity of 35%. The active part of the 1st stage has the composition, wt.%:
    Vanadium thioxide 1.99
    Niobium thioxide 0.59
    Phosphorus thioxide 0.29
    Rubidium oxide 0.35
    Titanium dioxide 96i, 79 The active part of the 2nd stage has the following composition, wt%: Vanadium dioxide, 1.96 P. niobium dioxide 0.59 P phosphorus dioxide 1.08 Rubidium oxide 0.34 Titanium dioxide 96, Q4 V multi-pipe heat exchange A coverter consisting of twenty stainless steel pipes with an inner diameter of 20 mm and a height of 3.5 m is first placed a 2 nd stage catalyst with the formation of a 1.5 m high layer, over which a 1 st stage catalyst is placed with the formation of a 1.5 m high. Melted salt is circulated through the converter, which serves as a heat carrier for Jani der temperature. A preheated to gaseous mixture of xylene with air is injected with a JB converter through its upper part with a bulk velocity of 2000 (at normal temperature and pressure). First, the concentration of o-xnolol is maintained at 40 g / nm of air, then the waste gas is recycled with a blower, and when the oxygen concentration in the source gas reaches 11 vol.%, The concentration of o-xylene is gradually increased to 100 g / nm gas containing molecular oxygen. Amount of waste. the gas that is recycled to the process is controlled in accordance with the increase in the amount of α-xylene introduced, whereby the oxygen concentration in the source gas is maintained at 11% by volume. The gas that leaves the converter is cooled to a heat exchanger, after which it is introduced into a refrigerator to crystallize phthalic anhydride. At this time, 33% of the total amount of formed phthalic anhydride excreted in the liquid state. The waste gas is removed from the refrigerator, maintaining the temperature at its outlet at a level, and then sent to the tower to separate the maleic anhydride. Approximately 35% of the waste gas contained in the steam is recycled to the feed gas. The rest of the gas is vented to the atmosphere through a complete combustion system. Under such conditions, the concentration of water vapor in the source gas is 3%. The results achieved during the course of the process "on May 6. Are summarized in Table. 1. Example 7. The same aqueous titanium dioxide as in Example 1 is calcined for 5 hours in a stream of air and subjected to grinding to a powder with an air stream to obtain a porous titanium dioxide whose particle diameter is 0.45 µm. and the specific surface is 33. In accordance with Example 1, using self-bonding silicon carbide as a carrier material, the particle size of which is 5 mm, and of porosity, 35%, two catalysts are obtained, containing 8 g of the active part per 100 ml of carrier. The active part of the catalyst has the composition, wt.%: 1-sta2-stage Vanadium thioxide 14.75 14.66 Pb niobium dioxide 0.99 0.98 P phosphorus thioxide 0.35 0.98 Rubidium oxide 0.28 0.28 Titanium dioxide 83,63 83,10 In the same as in example 6 converter, first put the catalyst of the 2nd stage to obtain a layer with a height of 1 m, and then the catalyst of the 1st stage with obtaining a layer with a height of 155 m. The temperature of the heat carrier is maintained at the level . A gaseous mixture of naphthalene with air, preheated before, is introduced into the converter through its upper part with a bulk velocity of 3000 hours. The naphthalene concentration is initially maintained at 40 g / nm of air, and then during the same procedure as in Example 6, the concentration of naphthalene in the kozza is increased to 60 g / Nm of gas containing molecular oxygen. The temperature at the top of the tower for the isolation of maleic anhydride and quinol is maintained at a level. The amount of waste gas returned for recycling is 66% (concentration of Synth, rock and gas near the inlet port of the converter is 11 vol.%), And the content of water vapor in the gas near the inlet of the reaction apparatus is approximately 4%, The results obtained for samples 1-7 are presented in table. 1. Examples 8-14. Phthalic anhydride is obtained from naphthalene or 0-xylene under various reaction conditions using various catalysts, the composition of which is given in table. 2. Porous titanium dioxide anatase type in yrimer 8 is made by annealing titanium hydroxide, obtained in example 1, at 900 ° C for 6 hours. Porous titanium dioxide of the anatase type in Examples 9, 10, 13, and 14 is prepared by annealing the titanium hydroxide prepared in Example 1 at 800 ° C for 4 hours. Porous titanium dioxide of the anatase type in Example 11 is prepared by annealing the titanium hydroxide prepared in Example 1 for 5 hours. Porous titanium dioxide of anatase type in example 12 is prepared by titanium hydroxide tanning, obtained 4412 in example 1, at 850 ° C for 6 hours. The results of tests of the catalysts of examples 8-14 are presented in Table. 2. Example 15 (for comparison). The catalyst described in example 1, containing the active part, including -V 05 tTiOj: P "Oj: KiO: NbjO 2, 1: 97.9: 0.49: 0.146: 0.25 (I will hang), and the carrier is silicon carbide a porosity of 18% is loaded into a pipe made of stainless steel, having an internal diameter of 20 mm and a height of 5 m, with the pipe being loaded with a catalyst up to a height of 3 m. Synthetic gas left from 11% by volume of oxygen, 10% by volume of steam and 79% by volume of nitrogen is mixed with 60 g / nm of artificial gaseous o-xylene. The gaseous mixture is passed through a bed of catalyst to react with it. The results are presented in Table. 1, As follows from the data presented, the proposed catalyst has a higher stability, the yield of phthalic anhydride for 6–12 carried. the work remains at the same level, while the activity of the proposed catalyst is higher,. than the famous .. Table l
    Beginning Stage
    2 months 6 months 12 months
    Beginning Stage
    3 months 6 months
    83 83 83 83
    113.6 113.8 113.1 112.7
    80 80 80
    112.8 112.5 112, L Elementary stage370 2700 di 370 2700 3 months b months 372 2700 Beginning stage 3 months. b months Beginning Stage Snake, b months Initial stage After 3 months. In b months Initial stafdvi After 2 months. After 4 months In b months Initial (for comparison stage) After 3 months.
    权利要求:
    Claims (1)
    [1]
    A CATALYST FOR OXYLENE OR NAPHTHALINE OXIDATION IN PHALYTIC ANHYDRIDE, containing 4-15 g of the active part, including vanadium pentoxide, niobium pentoxide, phosphorus pentoxide, titanium dioxide and metal oxide selected from the group consisting of potassium, cesium, rubidium, thallium, 100 ml of carrier and carrier, characterized in that, in order to increase the stability of the catalyst, it contains porous anatase titanium dioxide with a particle diameter of 0.40.68 μm, specific surface area
    11-57 m g / g with a total pore volume of 0.15-0.45 μm in diameter 55.0-8.8.0% of the pore volume with a diameter not exceeding 10 μm, the catalyst contains silicon carbide or a mixture of 80-92% as a carrier silicon carbide, 2-8% alumina and the rest is silicon dioxide with an apparent porosity of 13-42%, and the active part has the following composition, May.%:
    Vanadium pentoxide • Niobium pentoxide Phosphorus pentoxide Oxide of a metal selected from the iZ group, including potassium, cesium, rubidium, thallium Titanium dioxide
    0.99-19.87
    0.01-0.99
    0.20-1.17
    0.05-1.17 Else
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    同族专利:
    公开号 | 公开日
    US4284571A|1981-08-18|
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    IT7927727D0|1979-11-29|
    DE2948163A1|1980-06-04|
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    GB2039457B|1982-12-15|
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    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    JP14645978A|JPS603307B2|1978-11-29|1978-11-29|
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