CN111135829A - Ammonia oxidation catalyst and preparation method and application thereof - Google Patents
Ammonia oxidation catalyst and preparation method and application thereof Download PDFInfo
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- CN111135829A CN111135829A CN202010003447.XA CN202010003447A CN111135829A CN 111135829 A CN111135829 A CN 111135829A CN 202010003447 A CN202010003447 A CN 202010003447A CN 111135829 A CN111135829 A CN 111135829A
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- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
- B01J23/54—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
- B01J23/66—Silver or gold
- B01J23/68—Silver or gold with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
- B01J23/688—Silver or gold with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium with manganese, technetium or rhenium
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- B01J23/002—Mixed oxides other than spinels, e.g. perovskite
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- C07C253/00—Preparation of carboxylic acid nitriles
- C07C253/24—Preparation of carboxylic acid nitriles by ammoxidation of hydrocarbons or substituted hydrocarbons
- C07C253/28—Preparation of carboxylic acid nitriles by ammoxidation of hydrocarbons or substituted hydrocarbons containing six-membered aromatic rings, e.g. styrene
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Abstract
The invention provides an ammonia oxidation catalyst and a preparation method and application thereof, wherein the ammonia oxidation catalyst comprises a carrier and active components, and the active components satisfy the following structure in atomic ratio calculation: v1.0AgaAsbDcEdGeOxWherein D is selected from one or more of Mn, Zn, Ca, Ba and Pb, E is selected from one or more of Cs, Zr, La, Ce and Pr, and G is selected from one or more of Rh, Ru, Ir, Pt and Au; a is 0.01-3, b is 0.01-3, c is 0.01-2, d is 0.001-1, e is 0.001-0.6, and 0.3 < b/(1+ a) < 1.2, 0.1 < (b + e)/(c + d) < 15; x is determined by the degree of oxidation of the other elements of formula I; the catalyst has high conversion rate and selectivity and good stability when fed at a low ammonia/xylene ratio, and is suitable for industrial production.
Description
Technical Field
The invention belongs to the technical field of catalysts, and relates to an ammoxidation catalyst, a preparation method thereof and application of the catalyst in preparation of phthalonitrile by ammoxidation of xylene.
Background
Phthalonitrile (isophthalonitrile (IPN), Terephthalonitrile (TPN), phthalodinitrile (OPN)) and other aromatic nitriles are widely used fine chemical intermediates, the cyano group of which has extremely high chemical activity, and can be synthesized into a series of fine chemical products through hydrolysis, hydrogenation, addition, condensation, polymerization, halogenation and other reactions, and the fine chemical products are important raw materials for producing pesticides, medicines, dyes, perfumes, oil products, fuel additives and the like, and are also commonly used for producing polyester resin and polyester fiber, and the latter is an important intermediate for building materials, insulating materials and textile assistants.
The method for synthesizing the isophthalonitrile or the isomer thereof by carrying out ammoxidation on xylene, ammonia and air through one-step reaction is the simplest and most economical production method. At present, the relatively advanced technology at home and abroad applies a fine particle catalyst and a fluidized bed ammoxidation reaction process, and has the characteristics of safe production, simple process and high once-through yield. The ammoxidation process has been developed rapidly in recent years, and the core technology of the process is the development of catalysts.
At present, the xylene ammoxidation catalyst mainly has four systems of V-Cr, V-P, V-Sb and Sb-Fe, wherein the V-Cr system catalyst is widely applied due to the characteristics of easy industrial amplification production, good batch stability and higher ammoxidation activity. However, the feed to the present xylene ammoxidation process needs to maintain a higher ammonia/xylene ratio to increase conversion and selectivity.
Patent CN1500775A discloses a V-Cr-B-Ti fluidized bed catalyst, which is prepared by adding Li, Na, K, Cs, Mn, Ca, Fe, Mo, W or rare earth elements, and the molar ratio of the raw materials is ammonia: 5-10: 1 of m-xylene; patent CN1490309A discloses a V-Cr-Ti fluidized bed catalyst, which is prepared by adding P, B, Bi, Sb, As, alkali metal or/and alkaline earth metal, Mn, Ni, Co, Pb, Fe, Mo, W or rare earth element, and the molar ratio of raw materials is ammonia: p-xylene is 5-10: 1; patent CN102219711A discloses a V-Sb fluidized bed catalyst, which is prepared by adding alkali metals, Ca, Cr, Mo, Mn, Fe, Co, Ni, B, and P, and the molar ratio of raw materials is ammonia: and (3) m-xylene to 10: 1.
The applicant finds in research that the problem of excessively high ammonia/xylene ratio exists in the feed of the existing xylene ammoxidation process, a good reaction effect can be obtained only when the ammonia/xylene ratio is higher than 6, and meanwhile, a large amount of ammonia in the raw material is not reacted to cause waste, so that the raw material cost is increased; in addition, mixing of a large amount of unreacted raw material ammonia in the reaction tail gas causes difficulty in separation and increase in cost, and also causes increase in three-waste treatment and environmental protection cost. Currently, reducing the ammonia/xylene ratio in the feed to ameliorate the above problems results in a reduction in xylene conversion, target product phthalonitrile selectivity and yield.
In summary, there is a need for an ammoxidation catalyst with optimized structure, which can reduce the ammonia/xylene ratio in the reaction feed and improve the conversion rate of xylene, the selectivity and yield of the target product phthalonitrile, so as to reduce the raw material waste and reduce the environmental protection cost.
Disclosure of Invention
In order to overcome the defects in the prior art, the invention provides an ammoxidation catalyst, a preparation method and an application thereof, wherein the catalyst has the characteristics of high conversion rate and selectivity, good stability and suitability for large-scale industrial production when fed at a low ammonia/xylene ratio.
In order to realize the purpose of the invention, the invention adopts the following technical scheme:
the invention provides an ammonia oxidation catalyst, which comprises a carrier and active components, wherein the active components satisfy the following structure shown in the formula I in terms of atomic ratio:
V1.0AgaAsbDcEdGeOxformula I
In the formula I, D is selected from one or more of Mn, Zn, Ca, Ba and Pb, E is selected from one or more of Cs, Zr, La, Ce and Pr, and G is selected from one or more of Rh, Ru, Ir, Pt and Au;
wherein a is 0.01-3, b is 0.01-3, c is 0.01-2, d is 0.001-1, e is 0.001-0.6, and 0.3 < b/(1+ a) < 1.2, 0.1 < (b + e)/(c + d) < 15; x is determined by the degree of oxidation of the other elements of formula I.
In some embodiments, in the structure shown in formula i, a is 0.1 to 2, b is 0.05 to 2, c is 0.05 to 1.5, d is 0.005 to 0.8, and e is 0.005 to 0.5.
In the ammoxidation catalyst provided by the invention, the ratio of main elements V, Ag and As in the catalyst is accurately adjusted to form an active site of the high-efficiency multi-element composite oxide, so that the reaction activation energy in the catalytic process is reduced, the usage amount of ammonia in the raw material is reduced, and the higher conversion rate of xylene can be ensured under the condition of lower ammonia concentration.
According to the ammonia oxidation catalyst provided by the invention, the D-type metal element is introduced as an active assistant, so that the reaction activity is further improved; meanwhile, the introduction of the metal element E regulates the selectivity of the catalyst under lower ammonia concentration, and reduces CO and CO2Formation of deep ammoxidation by-products such as HCN; the G-type elements in the catalyst regulate the stability of the catalyst and ensure the stability of the catalyst in the long-period operation process.
In a specific embodiment of the invention, the mass percentage of the active component is 20-80% of the total mass of the ammoxidation catalyst, and the balance is a carrier;
the carrier is selected from silica or alumina.
In a second aspect, the present invention provides a process for preparing the above ammonia oxidation catalyst, using a process comprising the steps of:
1) adding the first reaction solution into an oxalic acid aqueous solution to form a first mixed solution;
2) adding a component containing a carrier and a reaction solution II into the mixed solution I to obtain a mixed solution II;
3) aging the mixed solution II, evaporating the obtained solution to obtain slurry with the solid content of 45-80%, and drying the slurry to obtain catalyst precursor powder;
4) roasting the catalyst precursor powder at 400-750 ℃ for 3-15 h to obtain an ammonia oxidation catalyst;
in the step 1), the first reaction solution is an aqueous solution of a vanadium-containing compound, a silver-containing compound and an arsenic-containing compound; the molar ratio of the vanadium-containing compound to oxalic acid contained in the oxalic acid aqueous solution is 1: 0.01-50;
in the step 2), the reaction solution two contains compounds of other metal elements in the active component, and the other metal elements in the active component are metal elements represented by D, E, G in the structure shown in the formula I;
the amount of the mixed liquid I and the amount of the mixed liquid II meet the proportion of each element in the structure shown in the formula I.
In step 1) of the preparation method, the vanadium-containing compound is selected from one or more of vanadium pentoxide, vanadium oxalate, vanadium tartrate, ammonium metavanadate and vanadium sulfate; preferably vanadium pentoxide or vanadium oxalate; the silver-containing compound is selected from one or more of silver nitrate, silver chloride, silver iodide, silver carbonate, silver phosphate and silver acetate, and is preferably silver nitrate or silver chloride; the arsenic-containing compound is one or more selected from arsenic pentoxide, arsenic trioxide, arsenic pentafluoride, arsenic trifluoride, arsenic pentachloride and arsenic trichloride, and is preferably arsenic pentachloride or arsenic trichloride.
In the specific implementation process of the invention, in order to increase the solubility of oxalic acid, oxalic acid can be added into water heated to 70-90 ℃, and an oxalic acid aqueous solution is formed under the stirring of the rotation speed of 200-400 rpm; for example, water is heated to 85 ℃, oxalic acid is added thereto and stirred at 250rpm to obtain an oxalic acid aqueous solution.
In step 2) of the specific preparation method of the present invention, the support-containing component is selected from a silicon source or an aluminum source, preferably selected from one or more of silica sol, nano silica, silica prepared from silicate by a sol-gel method, or alumina sol; as is well known to those skilled in the art, the amount of the support-containing component added during the preparation of a particular catalyst may be determined based on the amount of active component in the ammonia oxidation catalyst to ensure that the active component and the support in the resulting ammonia oxidation catalyst meet the above requirements.
The compounds of other metal elements in the active component are respectively selected from one or more of nitrate, chloride, carbonate or acetate of other metal elements; in some embodiments, hydrated metal salts may be used if nitrates, chlorides, carbonates, and acetates of the above-mentioned other metal elements are present; for example, the compound containing the other metal element D in the active component may be selected from manganese nitrate, lead nitrate, zinc nitrate; the compound containing other metal elements E in the active component can be selected from cerium nitrate, lanthanum nitrate hexahydrate and praseodymium chloride; the compound containing other metal element G in the active component can be selected from aurous chloride, ruthenium nitrate and iridium trichloride hydrate.
In the step 3) of the specific preparation method, the mixed solution II is stirred for 30-450 min at 45-100 ℃, and then heated to 100-125 ℃ for aging treatment; preferably, the aging treatment is performed for 30 to 600 min.
In a specific embodiment of the invention, the drying treatment is to spray-dry the slurry at an inlet temperature of 250 to 300 ℃ and an outlet temperature of 105 to 140 ℃. As is well known to those skilled in the art, spray drying is a systematic technique applied to material drying, in which a slurry is atomized in a drying chamber and then contacted with hot air, and moisture is rapidly vaporized to obtain a dried product.
In the step 4) of the specific preparation method, the catalyst precursor powder is heated to 120-200 ℃ at the speed of 0.5-6 ℃/min and is kept warm for 10-30 h; and then heating to 400-750 ℃ at the speed of 0.5-8 ℃/min, and then roasting.
In the third aspect of the invention, in the presence of a catalyst, after the ammoxidation reaction of xylene, ammonia gas and oxygen-containing gas, the isophthalonitrile or an isomer thereof is obtained; the catalyst adopts the ammonia oxidation catalyst or the ammonia oxidation catalyst prepared by the method;
wherein the molar ratio of the xylene to the ammonia to the oxygen in the oxygen-containing gas is 1: 1-2.9: 3.7-12.5, preferably 1: 2-2.5: 5.2-11.5;
in some preferred embodiments, the conversion of xylene is 99% or more and the selectivity of phthalonitrile is 98% or more.
The ammoxidation catalyst obtained by the invention is used for ammoxidation reaction, so that the molar ratio of the dimethylbenzene to the ammonia gas reaches 1-2.9, preferably 2-2.5, the usage amount of the raw material ammonia is greatly reduced, and the efficiency of the ammoxidation reaction is improved.
In the practice of the present invention, the oxygen-containing gas may be pure oxygen or air containing about 21% by volume.
In the specific method, the temperature of the ammoxidation reaction is 280-500 ℃, preferably 300-450 ℃; the gauge pressure of the ammoxidation reaction is 1-350 kPa; preferably 10 to 150 kPa. In some embodiments, the xylene as feedstock may be selected from ortho-xylene, meta-xylene, and para-xylene.
More preferably, the reaction raw materials are gasified, uniformly mixed and introduced into a reactor for carrying out the ammoxidation reaction, and the weight load of the catalyst in the reactor is 0.01-0.3 h-1Preferably 0.02 to 0.18h-1。
By adopting the technical scheme, the method has the following technical effects:
in the ammoxidation catalyst provided by the invention, the high-efficiency multi-element composite oxide active site is formed by adjusting the proportion of the main catalytic elements V, Ag and As, so that the reaction activation energy can be effectively reduced in the ammoxidation reaction, a higher xylene conversion rate can be ensured when the ammonia concentration is lower, and the use amount of ammonia in the raw material is greatly reduced.
Meanwhile, the D element introduced into the ammoxidation catalyst provided by the invention is an active assistant, which is beneficial to further improving the reaction activity; the E element is beneficial to regulating selectivity under lower ammonia concentration and reducing CO and CO2And the generation of byproducts of deep oxidation such as HCN and the like, and G elements are beneficial to regulating the stability of the catalyst and ensuring the long-period stable operation of the catalyst.
In the application process of the ammoxidation catalyst provided by the invention, the ammoxidation catalyst is subjected to ammoxidation reaction under the concentration of xylene, oxygen-containing gas and lower ammonia raw material to obtain (ortho-, meta-and para-) phthalonitrile, and the reaction has higher conversion rate, selectivity and stability, and is beneficial to large-scale industrial application.
Detailed Description
In order to better understand the technical solution of the present invention, the following examples are further provided to illustrate the present invention, but the present invention is not limited to the following examples.
The raw materials used in the examples are conventional in the art, and the purity specifications used are technical grade.
The calculation formula of the conversion rate of the raw material dimethylbenzene and the selectivity of the target product isophthalonitrile (ortho, meta and para) is as follows:
xylene conversion (%). times.100% (moles of xylene reacted/moles of xylene fed)
Phthalonitrile selectivity (%) - (moles of phthalonitrile produced/moles of xylene reacted) × 100%
Example 1
1) 2500g of water was heated to 85 ℃ and 1950g of oxalic acid (H) was added with stirring at 250rpm2C2O4) Adding water to form an oxalic acid aqueous solution; adding 455g of vanadium pentoxide, 680g of silver nitrate and 1360g of arsenic trichloride into 680g of water to form a first reaction solution;
adding the first reaction solution into an oxalic acid aqueous solution under stirring to form a first mixed solution;
2) 1074g of manganese nitrate, 1073g of zirconium nitrate pentahydrate and 8.7g of rhodium nitrate were dissolved in 3918.3g of water to form a reaction solution II;
adding 2750g of silica sol with the mass percentage of 40% and the reaction liquid II into the mixed liquid I to obtain mixed liquid II;
3) stirring the mixed solution II at 90 ℃ for 200min at the rotating speed of 350rpm, then heating to 105 ℃, standing for 60min for aging treatment, and evaporating the aged solution to slurry with the solid content of 45%;
spray-drying the obtained slurry at the inlet temperature of 285 ℃ and the outlet temperature of 125 ℃ to obtain catalyst precursor powder;
4) heating the obtained catalyst precursor powder to 120 ℃ at the speed of 1.5 ℃/min and preserving heat for 13 h; then heating to 670 ℃ at the speed of 1 ℃/min for roasting for 6h, and finally cooling to room temperature at the speed of 3 ℃/min to obtain the ammoxidation catalyst 1.
The active component proportion of the ammoxidation catalyst 1 is detected to be V1.0Ag0.8As1.5Mn1.2Zr0.5Rh0.006Ox。
The obtained ammoxidation catalyst 1 is filled in a fluidized bed reactor for ammoxidation, the molar ratio of m-xylene, ammonia gas and oxygen in the raw materials is 1:2:9.4, the temperature of the ammoxidation is 380 ℃, the reaction pressure (gauge pressure) is 20kPa, and the weight load of the catalyst in the reactor is 0.06h-1。
After the reactor was operated for 1000 hours, the conversion of m-xylene was 99.9% and the selectivity of m-phthalonitrile was 98.9%.
Example 2
1) 2550g of water are heated to 75 ℃ and 2000g of oxalic acid (H) are stirred at 350rpm2C2O4) Adding water to form an oxalic acid aqueous solution; adding 455g of vanadium pentoxide, 765g of silver nitrate and 1269g of arsenic trichloride into 780g of water to form a reaction liquid I;
adding the first reaction solution into an oxalic acid aqueous solution under stirring to form a first mixed solution;
2) 1988g of lead nitrate, 293g of cesium nitrate and 12.4g of iridium trichloride hydrate were dissolved in 4594.6g of water to form a reaction liquid II;
adding 2800g of silica sol with the mass percentage of 40% and the reaction liquid II into the mixed liquid I to obtain mixed liquid II;
3) stirring the mixed solution II at 85 ℃ for 180min at the rotating speed of 300rpm, then heating to 108 ℃, standing for 75min for aging treatment, and evaporating the aged solution to slurry with the solid content of 48%;
spray-drying the obtained slurry at the inlet temperature of 275 ℃ and the outlet temperature of 135 ℃ to obtain catalyst precursor powder;
4) heating the obtained catalyst precursor powder to 130 ℃ at the speed of 1 ℃/min and preserving heat for 15 h; then heating to 680 ℃ at the speed of 1.5 ℃/min for roasting for 6h, and finally cooling to room temperature at the speed of 5 ℃/min to obtain the ammoxidation catalyst 2.
The active component proportion of the ammoxidation catalyst 2 is detected to be V1.0Ag0.9As1.4Pb1.2Cs0.3Ir0.007Ox。
The obtained ammoxidation catalyst 2 is filled in a fluidized bed reactor for ammoxidation reaction, the molar ratio of m-xylene, ammonia gas and oxygen in the reaction raw materials is 1:2.1:10, the ammoxidation reaction temperature is 360 ℃, the reaction pressure (gauge pressure) is 15kPa, and the weight load of the catalyst in the reactor is 0.06h-1。
After the reactor was operated for 1000 hours, the conversion of m-xylene was 99.8% and the selectivity of m-phthalonitrile was 99.1%.
Example 3
1) 2600g of water are heated to 80 ℃ and 2100g of oxalic acid (H) are stirred at 300rpm2C2O4) Adding water to form an oxalic acid aqueous solution; adding 455g of vanadium pentoxide, 510g of silver nitrate and 998g of arsenic trichloride into 800g of water to form a first reaction solution;
adding the first reaction solution into an oxalic acid aqueous solution under stirring to form a first mixed solution;
2) 1190g of zinc nitrate hexahydrate, 1519g of cerium nitrate hexahydrate and 16.85g of platinum chloride are dissolved in 3513.15g of water to form reaction liquid II;
adding 3000g of 40 mass percent silica sol and the reaction solution II into the mixed solution I to obtain mixed solution II;
3) stirring the mixed solution II at 90 ℃ for 150min at the rotating speed of 310rpm, then heating to 110 ℃, standing for 180min for aging treatment, and evaporating the aged solution to slurry with the solid content of 45%;
spray-drying the obtained slurry at the inlet temperature of 280 ℃ and the outlet temperature of 130 ℃ to obtain catalyst precursor powder;
4) heating the obtained catalyst precursor powder to 135 ℃ at the speed of 2 ℃/min and preserving the temperature for 12 hours; then heating to 650 ℃ at the speed of 3 ℃/min for roasting for 8h, and finally cooling to room temperature at the speed of 5 ℃/min to obtain the ammoxidation catalyst 3.
The active component proportion of the ammoxidation catalyst 3 is detected to be V1.0Ag0.6As1.1Zn0.8Ce0.7Pt0.01Ox。
The ammoxidation catalyst 3 obtained above was loaded in a fluidized bed reactor for ammoxidation reaction at a temperature of 315 ℃ and a reaction pressure (gauge pressure) of 18kPa in the presence of a catalyst weight load of 0.03h in the reactor in such a manner that the molar ratio of m-xylene, ammonia gas and oxygen in the reaction raw material was 1:2.1:8.6-1。
After the reactor was operated for 1000 hours, the conversion of m-xylene was 99.9% and the selectivity of m-phthalonitrile was 99.5%.
Example 4
1) 2650g of water are heated to 75 ℃ and 2050g of oxalic acid (H) are stirred at 350rpm2C2O4) Adding water to form an oxalic acid aqueous solution; 455g of vanadium pentoxide, 1020g of silver nitrate and 726g of arsenic trichloride were added to 900g of water in the form ofForming a first reaction solution;
adding the first reaction solution into an oxalic acid aqueous solution under stirring to form a first mixed solution;
2) 722g of calcium chloride, 1299g of lanthanum nitrate hexahydrate and 12.68g of ruthenium nitrate are dissolved in 3568.32g of water to form a reaction solution II;
adding 2900g of silica sol with the mass percentage of 40% and the reaction liquid II into the mixed liquid I to obtain mixed liquid II;
3) stirring the mixed solution II at 95 ℃ for 250min at the rotating speed of 320rpm, then heating to 120 ℃, standing for 85min for aging treatment, and evaporating the aged solution to slurry with the solid content of 48%;
spray-drying the obtained slurry at the inlet temperature of 285 ℃ and the outlet temperature of 135 ℃ to obtain catalyst precursor powder;
4) heating the obtained catalyst precursor powder to 150 ℃ at the speed of 1 ℃/min and preserving heat for 15 h; then heating to 610 ℃ at the speed of 2 ℃/min for 7h for roasting, and finally cooling to room temperature at the speed of 6 ℃/min to obtain the ammoxidation catalyst 4.
The active component proportion of the ammoxidation catalyst 4 is detected to be V1.0Ag1.2As0.8Ca1.3La0.6Ru0.008Ox。
The ammoxidation catalyst 4 obtained above was charged in a fluidized bed reactor to conduct ammoxidation, the molar ratio of p-xylene, ammonia gas and oxygen in the reaction raw material was 1:2.3:10.7, the ammoxidation temperature was 362 ℃, the reaction pressure (gauge pressure) was 20kPa, and the catalyst weight load in the reactor was 0.05h-1。
After the reactor was operated for 1000 hours, the conversion of p-xylene was 99.7% and the selectivity to terephthalonitrile was 99.3%.
Example 5
1) 2700g of water are heated to 85 ℃ and 1980g of oxalic acid (H) are stirred at 350rpm2C2O4) Adding water to form an oxalic acid aqueous solution; 455g of vanadium pentoxide, 850g of silver nitrate and 1541g of tris (ethylene glycol)Adding arsenic chloride into 980g of water to form a first reaction solution;
adding the first reaction solution into an oxalic acid aqueous solution under stirring to form a first mixed solution;
2) 1700g of barium nitrate, 742g of praseodymium chloride and 6.97g of aurous chloride are dissolved in 4301.03g of water to form a reaction solution II;
adding 2980g of silica sol with the mass percentage of 40% and the reaction liquid II into the mixed liquid I to obtain mixed liquid II;
3) stirring the mixed solution II at 85 ℃ for 150min at the rotating speed of 280rpm, then heating to 108 ℃, standing for 120min for aging treatment, and evaporating the aged solution to slurry with the solid content of 48%;
spray-drying the obtained slurry at the inlet temperature of 275 ℃ and the outlet temperature of 125 ℃ to obtain catalyst precursor powder;
4) heating the obtained catalyst precursor powder to 180 ℃ at the speed of 2 ℃/min and preserving heat for 10 hours; then heating to 650 ℃ at the speed of 1 ℃/min for roasting for 10h, and finally cooling to room temperature at the speed of 5 ℃/min to obtain the ammoxidation catalyst 5.
The active component proportion of the ammoxidation catalyst 5 is detected to be V1.0Ag1As1.7Ba1.3Pr0.6Au0.006Ox。
The obtained ammoxidation catalyst 5 is filled in a fluidized bed reactor for ammoxidation, the molar ratio of p-xylene, ammonia gas and oxygen in the reaction raw material is 1:2:7.9, the ammoxidation temperature is 365 ℃, the reaction pressure (gauge pressure) is 21kPa, and the weight load of the catalyst in the reactor is 0.06h-1。
After the reactor was operated for 1000 hours, the conversion of p-xylene was 99.9% and the selectivity to terephthalonitrile was 99.8%.
Comparative example 1
The preparation of V was carried out according to the method of example 1 of patent publication CN1490309A1.00Cr0.95Ti0.15B0.50P0.10Mn0.2K0.05/SiO21-1 of the ammoxidation catalyst;
the ammoxidation catalyst 1-1 obtained above was charged in a fluidized bed reactor to carry out an ammoxidation reaction under the same conditions as in example 1 of the present application;
after the reactor was operated for 1000 hours, the conversion of m-xylene was 65.3% and the selectivity of m-phthalonitrile was 72.1%.
Comparative example 2
The preparation of V was carried out according to the method of example 1 of patent publication CN1500775A1.0Cr0. 9B0.5Ti0.1P0.05Mo0.1Na0.05/SiO22-1 of an ammonia oxidation catalyst;
the ammoxidation catalyst 2-1 obtained above was charged in a fluidized bed reactor to carry out an ammoxidation reaction under the same conditions as in example 2 of the present application;
after the reactor was operated for 1000 hours, the conversion of m-xylene was 73.9% and the selectivity to m-phthalonitrile was 62.8%.
Comparative example 3
This comparative example differs from example 3 in that: during the preparation of the catalyst, silver nitrate is not added to obtain the ammoxidation catalyst 3-1, and the active component proportion is V1.0As1.1Zn0.8Ce0.7Pt0.01Ox。
The ammoxidation catalyst 3-1 obtained above was charged in a fluidized bed reactor, and an ammoxidation reaction was carried out by the method of example 3, and after 1000 hours of operation of the reactor, the conversion of m-xylene was 91.8% and the selectivity for m-phthalonitrile was 83.7%.
Comparative example 4
This comparative example differs from example 4 in that: in the preparation process of the catalyst, arsenic trichloride is not added to obtain an ammoxidation catalyst 4-1, and the active component proportion is V1.0Ag1.2Ca1.3La0.6Ru0.008Ox。
The ammoxidation catalyst 4-1 obtained above was charged in a fluidized bed reactor, and an ammoxidation reaction was carried out in the same manner as in example 4, and after 1000 hours of operation of the reactor, the conversion of m-xylene was 92.5% and the selectivity for m-phthalonitrile was 81.3%.
Claims (10)
1. An ammoxidation catalyst, comprising a carrier and an active component satisfying a structure represented by the following formula I in terms of atomic ratio:
V1.0AgaAsbDcEdGeOxformula I
In the formula I, D is selected from one or more of Mn, Zn, Ca, Ba and Pb, E is selected from one or more of Cs, Zr, La, Ce and Pr, and G is selected from one or more of Rh, Ru, Ir, Pt and Au;
wherein a is 0.01-3, b is 0.01-3, c is 0.01-2, d is 0.001-1, e is 0.001-0.6, and 0.3 < b/(1+ a) < 1.2, 0.1 < (b + e)/(c + d) < 15; x is determined by the degree of oxidation of the other elements of formula I; preferably, a is 0.1 to 2, b is 0.05 to 2, c is 0.05 to 1.5, d is 0.005 to 0.8, and e is 0.005 to 0.5.
2. The ammoxidation catalyst according to claim 1, wherein the active component is contained in an amount of 20 to 80% by mass, and the balance is a carrier, based on the total mass of the ammoxidation catalyst;
the carrier is selected from silica or alumina.
3. A process for preparing the ammoxidation catalyst according to claim 1 or 2, wherein the process comprises the steps of:
1) adding the first reaction solution into an oxalic acid aqueous solution to form a first mixed solution;
2) adding a component containing a carrier and a reaction solution II into the mixed solution I to obtain a mixed solution II;
3) aging the mixed solution II, evaporating the obtained solution to obtain slurry with the solid content of 45-80%, and drying the slurry to obtain catalyst precursor powder;
4) roasting the catalyst precursor powder at 400-750 ℃ for 3-15 h to obtain an ammonia oxidation catalyst;
in the step 1), the first reaction solution is an aqueous solution of a vanadium-containing compound, a silver-containing compound and an arsenic-containing compound; the molar ratio of the vanadium-containing compound to oxalic acid contained in the oxalic acid aqueous solution is 1: 0.01-50;
in the step 2), the reaction solution two contains compounds of other metal elements in the active component, wherein the other metal elements in the active component are metal elements represented by D, E, G in the structure shown in the formula I in claim 1;
the amount of the mixed solution I and the mixed solution II meets the proportion of each element in the structure shown in the formula I in claim 1.
4. The method according to claim 3, wherein in step 1), the vanadium-containing compound is selected from one or more of vanadium pentoxide, vanadium oxalate, vanadium tartrate, ammonium metavanadate or vanadium sulfate;
the silver-containing compound is selected from one or more of silver nitrate, silver chloride, silver iodide, silver carbonate, silver phosphate or silver acetate;
the arsenic-containing compound is one or more selected from arsenic pentoxide, arsenic trioxide, arsenic pentafluoride, arsenic trifluoride, arsenic pentachloride or arsenic trichloride.
5. The method according to claim 4, wherein in step 2) the support-containing component is selected from a silicon or aluminium source, preferably from one or more of silica sol, nanosilica, silica or alumina sol prepared from silicate using a sol-gel process;
the compounds of other metal elements in the active component are respectively selected from one or more of nitrate, chloride, carbonate or acetate of other metal elements.
6. The method according to claim 5, wherein in the step 3), the mixed solution II is stirred at 45-100 ℃ for 30-450 min, and then the temperature is raised to 100-125 ℃ for aging treatment;
preferably, the aging treatment is performed for 30 to 600 min.
7. The method according to claim 6, wherein in the step 3), the drying is carried out by performing spray drying on the slurry under the conditions that the inlet temperature is 250-300 ℃ and the outlet temperature is 105-140 ℃.
8. The method according to claim 7, wherein in the step 4), the catalyst precursor powder is heated to 120-200 ℃ at a speed of 0.5-6 ℃/min and is kept at the temperature for 10-30 h; and then heating to 400-750 ℃ at the speed of 0.5-8 ℃/min, and then roasting.
9. A process for producing phthalonitrile, which comprises the following steps: in the presence of a catalyst, carrying out ammoxidation reaction on dimethylbenzene, ammonia gas and oxygen-containing gas to obtain phthalonitrile; the catalyst is the ammonia oxidation catalyst of claim 1 or 2 or the ammonia oxidation catalyst prepared by the method of any one of claims 3 to 8;
wherein the molar ratio of the xylene to the ammonia to the oxygen in the oxygen-containing gas is 1: 1-2.9: 3.7-12.5, preferably 1: 2-2.5: 5.2-11.5;
preferably, the conversion of xylene is 99% or more, and the selectivity of phthalonitrile is 98% or more.
10. The method according to claim 9, wherein the temperature of the ammoxidation reaction is 280 to 500 ℃, preferably 300 to 450 ℃; the gauge pressure of the ammoxidation reaction is 1-350 kPa; preferably 10 to 150 kPa.
More preferably, the reaction raw materials are gasified, uniformly mixed and introduced into a reactor for the ammoxidation reaction, and the reactor is used for the ammoxidation reactionThe weight load of the medium catalyst is 0.01 to 0.3h-1Preferably 0.02 to 0.18h-1。
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| CN112675847A (en) * | 2021-01-12 | 2021-04-20 | 万华化学集团股份有限公司 | Wear-resistant isophthalonitrile catalyst, preparation method and method for preparing isophthalonitrile by using wear-resistant isophthalonitrile catalyst |
| CN112675848A (en) * | 2021-01-12 | 2021-04-20 | 万华化学集团股份有限公司 | Catalyst for producing isophthalonitrile, preparation method and method for preparing isophthalonitrile by using catalyst |
| CN112961075A (en) * | 2021-02-04 | 2021-06-15 | 鞍山七彩化学股份有限公司 | Synthetic method of terephthalonitrile |
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