CN1042901A - Produce the method for nitrile - Google Patents
Produce the method for nitrile Download PDFInfo
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- CN1042901A CN1042901A CN88108115A CN88108115A CN1042901A CN 1042901 A CN1042901 A CN 1042901A CN 88108115 A CN88108115 A CN 88108115A CN 88108115 A CN88108115 A CN 88108115A CN 1042901 A CN1042901 A CN 1042901A
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- nitrile
- alkane
- catalyzer
- ammonia
- gas phase
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
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- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
Abstract
The invention relates to the method for producing nitrile, this method comprises makes alkane and ammonia carry out gas phase catalytic oxidation reaction in the presence of the compositing oxidation solid catalyst of being made up of molybdenum, vanadium, hoof and niobium.
According to the inventive method, under the situation of not using halogenide, water etc., under about 350 to 480 ℃ of preferably about lesser tempss of 400 to 450 ℃, the required nitrile of production that can highly selective.
Description
What the present invention narrated is about producing the method for nitrile.Narrated in more detail with alkane and done improving one's methods of starting material production nitrile.
Nitrile such as vinyl cyanide and methacrylonitrile are as suitability for industrialized production such as the important intermediate for preparing fiber, synthetic resins, synthetic rubber etc.The prevailing method of producing this nitrile is to make alkene such as propylene, and iso-butylene or other allied substances in the high temperature gas phase, carry out catalyzed reaction with ammonia and oxygen in the presence of catalyzer.
Recently, proposed relevant method of producing vinyl cyanide or methacrylonitrile with so-called method for ammoxidation, lower alkane such as propane, Trimethylmethane or the like stand catalyzed reaction with ammonia and oxygen in the presence of catalyzer in gas phase according to the method.The method of for example known use Mo class catalyzer (the open NOS48-16887(1973 of Japanese Patent), 47-13312(1972) (be equivalent to GB1,333,639), and 47-13313(1972) (is equivalent to USP3,833,638) and Japanese patent publication N.55-42071(1980)), use the method (Japanese Patent Application Publication NOS47-33783(1972) and the 52-1480 22(1977 of V class catalyzer), Japanese patent publication NOS.50-23016(1975) (is equivalent to GB1,336,135 and GB1,336,136) with 47-51331(1972) (with respect to USP3,433,823)), use the method (Japanese patent publication NOS45-4733(1970) of Sb class catalyzer (to be equivalent to GB1,194,855), 47-14371(1972) (be equivalent to USP3.670,008, USP3,678,090 and USP3,816,506), 50-17046(1975) (be equivalent to USP3,670,006, USP3,686,267 and USP3,743,527), 50-28940(1975) (be equivalent to GB1,334,859), 56-47901(1981), and USP3,686,295)), (be equivalent to USP with the method (Japanese patent publication N.50-16775) (1975) of using other type catalyst, 3,652.638)), but not having a kind of method in these currently known methodss is satisfied to the selectivity of desired nitrile.
In order to improve the selectivity of nitrile, enterprise adds organic fontanelle compound in a small amount in reactive system, inorganic fontanelle compound or sulphur compound or water joined reactive system.But last method has corrosion reaction device problem, and then a method is because side reaction relates to the problem that forms byproduct.
In addition, use the method for conventional catalyst to need about 500 ℃ or higher temperature of reaction, therefore at the material of reactor, this method in aspects such as product price is imperfect.
The present inventor has carried out deep research to the method for making starting material production nitrile with alkane, it found that, by using desired nitrile that specific composite catalyst produces, do not need that fontanelle compound or water added reactive system and than the temperature low (about 380 to 480 ℃) of ordinary method needs than ordinary method selectivity height.Finished the present invention based on this discovery.
The invention provides a kind of method of producing nitrile.This method comprises: alkane carries out gas phase catalytic oxidation reaction with ammonia in the presence of the composite oxides solid catalyst of being made up of molybdenum, vanadium, tellurium and niobium.
Feature of the present invention is to use to contain molybdenum (Mo), the composite oxides solid catalyst of vanadium (V), tellurium (Te) and niobium (Nb) as main component in the oxidative ammonolysis of alkane.The exemplary of this composite oxides solid catalyst is represented by following empirical formula:
Mo1.0Va TebNbcOx
A wherein, b and c represent that with Mo be basic each component atoms of elements ratio, a is 0.01 to 1.0, b be 0.01 to 0.5 and c be 0.01 to 1.0, and x is by the number of valent sum decision of metallic element.
These catalyzer can be prepared by the method that exemplifies below, the aqueous solution with ammonium niobium oxalate, the aqueous solution of the telluric acid aqueous solution and para-molybdic acid ammonium salt joins in the aqueous solution of the ammonium meta-vanadate that contains specified rate successively according to the amount of the atomic ratio of each metallic element in the scope of above regulation, heated mixt also concentrates about 30 minutes under about 70 ℃, at 130 ℃ be evaporated to dried thereafter, the drying solid that generates is under 350 to 650 ℃ of high temperature, best 350～450 ℃, calcined about 3 hours, to obtain desired catalyzer.
Among the superincumbent preparation method, do not stipulate the interpolation order of molybdenum, vanadium, tellurium and each metallic element of niobium, but require to add the molybdenum component that for example the aqueous solution of ammonium paramolybdate is easy to obtain the uniform aqueous solution at last.
In the superincumbent preparation, ammonium meta-vanadate can be by V
2O
5, V
2O
3, VOCl
3, VCl
4Or other similar substance replacement, ammonium niobium oxalate can be by NbCl
3, NbCl
5, Nb
2(C
2O
4)
5Or other similar material replaces.Equally, telluric acid can be by TeO
2Or other similar substances replacements, and ammonium paramolybdate can be by MoO
3, MoCl
5, phospho-molybdic acid, silicomolybdic acid or other similar substance replace.The also available molybdenum of mixed ligand and the heteropolyacid of vanadium of containing, for example: molybdovanaphosphoric acid (molybdovanadophoaphoric acid).
The content of the metallic element of catalyzer used in the present invention is to select like this: vanadium is 0.01 to 1.0 atom with the ratio of an atom molybdenum, 0.2 to 0.4 atom preferably, tellurium is 0.01 to 0.5 atom with the ratio of an atom molybdenum, 0.2 to 0.4 atom preferably, and the ratio of niobium and an atom molybdenum is 0.01 to 1.0 atom, preferably 0.1 to 0.2 atom.
This catalyzer or use separately, or and known carrier, for example silicon, aluminium, aluminosilicate etc. are united use.According to the factor in reaction scale and reactive system and/or other the existing actually operating technology this catalyzer is processed into suitable particle diameter and shape.
Method of the present invention is to carry out gas phase catalytic oxidation reaction by alkane and ammonia to produce nitrile in the presence of catalyzer given above.
As raw-material alkane, not restricted especially, for example, the alkane such as the methane of 1 to 7 carbon atom, ethane, propane, butane, Trimethylmethane, pentane, hexane, heptane etc. still, are considered the industrial application of the nitrile of producing, the lower alkane of the most handy 1 to 4 carbon atom.Therefore, oxidizing reaction of the present invention is by being present in the Sauerstoffatom in the catalyzer or being finished by the molecular oxygen that unstripped gas is supplied with.
Under the situation by the raw material supplying oxygen molecule, though can use pure oxygen, owing to do not require purified carrier of oxygen, using the gas that contains molecular oxygen is economical as air.Under molecular oxygen is not included in as the situation in the gas of raw material supply, it is desirable alternately supplying with the gaseous mixture of alkane and ammonia and the gas of molecule-containing keto, to prevent the reduced anneal of catalyzer, perhaps when using the moving bed type reactor, used catalyzer is constantly changed into a kind of common oxidation regeneration agent, so that use this regenerated catalyst.
The reactor that the present invention uses, any reactor that is used for gas phase contact catalysis reaction so far can use.And, can carry out the adding and the extraction of catalyzer according to a conventional method.Catalyst levels generally with per hour supply with 0.02 to 2.4cc preferably 0.1 to the 0.5cc alkane for well.
With the gas of alkane, ammonia, optional molecule-containing keto and the rare long-pending agent gas that is used to regulate air speed and oxygen partial pressure send into discriminably in the reactor, but preferably be pre-mixed these materials, then with the gaseous mixture supply response device of preparation.
The used ammonia amount of each mole alkane is 0.5 to 3 mole in the reaction, and is best with 0.8 to 1.5 mole.
About the selectivity of nitrile, use the amount of the gas contain molecular oxygen very important in the case of necessary, use the gas of molecule-containing keto in order that no more than 5 moles of the molecular oxygen amount of every mole of alkane is best with 1 to 3 mole.
As rare long-pending agent gas, can use inactive gas such as nitrogen, argon, helium or the like.By increasing or reduce the consumption of the rare long-pending agent in the above-mentioned scope, can regulate the air speed of oxygen and divide being pressed in the suitable scope.
The air speed of supply gas (mixture of the gas of alkane, ammonia, optional molecule-containing keto and optional rare long-pending agent gas) is 100～10,000 hour
-1, preferably 500～2,000 hour
-1
Among the present invention, the gas phase contact reacts of alkane and ammonia is in the temperature lower than the oxidative ammonolysis temperature of routine, and promptly 380 to 480 ℃, be preferably in 400 to 450 ℃, under atmospheric pressure, pressure boost or decompression are slowly carried out lentamente.
Oxidative ammonolysis the method according to this invention of alkane is carried out, for example, α, alpha, beta-unsaturated nitriles such as methacrylonitrile, vinyl cyanide etc. are formed by Trimethylmethane and propane, and acetonitrile is formed by ethane, and prussic acid is formed by methane.Except that these compounds, carbon monoxide, carbonic acid gas, unwanted nitrile etc. all are byproducts, and but, the amount of byproduct is very little.
Can from reaction mixture, isolate this nitrile that desired nitrile and purifies and separates go out with following ordinary method.
Illustrate in greater detail the present invention by non-limiting instance below.
In example and comparative example the selectivity (%) of transformation efficiency of alkane (%) and nitrile, respectively by following formulate:
The turnover ratio of alkane (%)=(consuming the mole of alkane)/(supplying with the mole of alkane) * 100
The selectivity (%) of the nitrile of wanting=(obtaining the mole of the nitrile of wanting)/(consuming the mole of alkane) * 100
Reference example 1(Preparation of catalysts)
The ammonium meta-vanadate of 1170mg is dissolved in the warm water of 100ml, and with the ammonium niobium oxalate aqueous solution of 12.5ml (0.2Nb atom/liter), the ammonium paramolybdate aqueous solution of the telluric acid aqueous solution of 1000ml (0.5 tellurium atom/liter) and 25.0ml (1.0Mo atom/liter) joins in this solution of formation to prepare the uniform aqueous solution.
Heat after this aqueous solution, in moisture eliminator, be evaporated to dried at 130 ℃ to obtain solid matter.
This solid matter that obtains is calcined under airflow, and with tabletting machine the incinerating material is compression molded into diameter 5mm at 350 ℃, after the sheet of thick 3mm, grinds and make powder to pass through 16 to 28 mesh sieves this sheet.The empirical formula of the catalyzer that makes is as follows:
Mo1.0V0.4 Te0.2Nb0.1O4.65
Reference example 2(Preparation of catalysts)
Identical with the method in the reference example 1, the amount that just changes telluric acid obtains following two kinds of catalyzer:
Mo1.0V0.4 Te0.3Nb0.1O4.85 and Mo1.0V0.4 Te0.4Nb0.1O5.05
Example 1 to 4
To send into by the catalyzer 0.5cc that reference example 1 obtains after the reactor, with the gaseous mixture of propane, ammonia, air and the nitrogen of mol ratio shown in the table 1 with 1400 hours
-1Air speed supply response device, under 422 ℃, carry out gas phase catalytic reaction.Its result is as shown in table 1.
Comparative example 1
Except not using the Nb component, in the catalyzer of the atomic ratio of in using, representing with the table 2 of reference example 1 same procedure preparation, the gaseous mixture of propane, ammonia, air and nitrogen that will be identical with component in the example 1, with sending into reactor, under with the temperature shown in the table 2, react with example 1 same air speed.Its result is as shown in table 2.
Comparative example 2
Except not using the tellurium component, in the catalyzer that uses with the atomic ratio shown in the table 2 of reference example 1 same procedure preparation, and the gaseous mixture of propane, ammonia, air and the nitrogen of example 1 same component, to send into reactor, under the temperature shown in the table 2, react with example 1 identical air speed.Its result is as shown in table 2.
Comparative example 3
Except without the V component, in the catalyzer while of using with the atomic ratio of reference example 1 same procedure preparation, with example 1 in the gaseous mixture of propane, ammonia, air and nitrogen of identical component, the air speed supply response device with same with example 1 reacts under the temperature shown in the table 2.It the results are shown in the table 2.
Comparative example 4
Except not using the Mo component, when using with the catalyzer of reference example 1 with the atomic ratio shown in the table 2 of quadrat method preparation, the gaseous mixture of propane, ammonia, air and the nitrogen identical with the composition of example 1 with air speed supply response device same in the example 1, is reacted under the temperature shown in the table 2.Its result is as shown in table 2.
From example 1 to 4 and comparison comparative example 1 to 4, can recognize the component of catalyzer of the present invention, Mo, V, Te and Nb obtain the indispensable component of highly selective.
Example 5
The catalyzer 1cc that reference example 1 is obtained sends into after the reactor, and with 1: 1.2: 2: the gaseous mixture of the propane of 14.9 mol ratios, ammonia, air and nitrogen was with 700 hours
-1Air speed supply response device 5 minutes, under 401 ℃, carry out gas phase contact catalysis reaction.
Transformation efficiency 9.9%, selectivity 76.3%.
Though do not supply with molecular oxygen in this example, only the Sauerstoffatom generation oxidizing reaction that exists by catalyst themselves is finished the oxidation of propane, can obtain the vinyl cyanide of highly selective.
Example 6 to 7
Two kinds of each 0.5cc of catalyzer that obtain in using reference example 2 and 1: 1.2: 7.6: the gaseous mixture of the propane of 7.3 atomic ratios, ammonia, air and nitrogen was in 1400 hours
-1Send into reactor under the air speed respectively, under 422 ℃, carry out gas phase contact catalysis reaction.
Its result is as shown in table 3.
Example 8 to 10
The catalyzer 0.5cc that obtains in the reference example 1 is sent into after the reactor, and the gaseous mixture that Trimethylmethane, ammonia, air and the nitrogen of expression in the table 4 are formed was with 1400 hours
-1Air speed supply response device carries out gas phase contact catalysis reaction at 448 ℃.Its result is as shown in table 4.
Claims (4)
1, a kind of method of producing nitrile, this method comprise makes alkane and ammonia carry out gas phase contact catalysis oxidizing reaction in the presence of the compositing oxidation solid catalyst of being made up of Mo, V, Te, Nb.
2, according to the process of claim 1 wherein that this compositing oxidation solid catalyst is expressed from the next:
Mo1.0Va TebNbcOx
A wherein, b and c represent the atomic ratio of each element to a molybdenum atom, a is 0.01 to 1.0, b be 0.01 to 0.5 and c be 0.01 to 1.0, and x is the number by total valency decision of each metallic element.
3, according to the process of claim 1 wherein that this gas phase contact catalysis reaction is what to carry out in the presence of molecular oxygen.
4, a kind of compositing oxidation solid catalyst, this catalyst is produced needed nitrile by the gas phase contact catalysis oxidizing reaction between alkane and the ammonia, and this catalyzer is expressed from the next:
Mo1.0Va TebNbcOx
Wherein a, b, c represent the atomic ratio of each element to a molybdenum atom, and a is 0.01 to 1.0, b be 0.01 to 0.5 and c be 0.01 to 0.1, x is the number by the total valency decision of each metallic element.
Applications Claiming Priority (5)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP295054/87 | 1987-11-25 | ||
| JP29505487 | 1987-11-25 | ||
| JP33999/88 | 1988-02-18 | ||
| JP63197126A JP2608768B2 (en) | 1987-11-25 | 1988-08-09 | Nitrile manufacturing method |
| JP197126/88 | 1988-08-09 |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1042901A true CN1042901A (en) | 1990-06-13 |
| CN1020597C CN1020597C (en) | 1993-05-12 |
Family
ID=26510186
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN88108115A Expired - Lifetime CN1020597C (en) | 1987-11-25 | 1988-11-24 | Process for producing nitriles |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1020597C (en) |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1088398C (en) * | 1997-10-15 | 2002-07-31 | 旭化成株式会社 | Ammoxidation catalyst for use in producing acrylonitrile or methacrylonitrile from propane or isobutane by ammoxidation |
| CN1105599C (en) * | 1997-09-17 | 2003-04-16 | 沙特基础工业公司 | Catalysts for oxidation of ethane to acetic acid, process of making same and use |
| CN103402976A (en) * | 2011-03-02 | 2013-11-20 | 旭化成化学株式会社 | Method for producing unsaturated nitrile |
| CN104549373A (en) * | 2013-10-28 | 2015-04-29 | 中国石油化工股份有限公司 | Low-carbon alkane ammoxidation catalyst |
| CN105312067A (en) * | 2014-07-11 | 2016-02-10 | 中国石油化工股份有限公司 | Light alkane ammoxidation catalyst |
-
1988
- 1988-11-24 CN CN88108115A patent/CN1020597C/en not_active Expired - Lifetime
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1105599C (en) * | 1997-09-17 | 2003-04-16 | 沙特基础工业公司 | Catalysts for oxidation of ethane to acetic acid, process of making same and use |
| CN1088398C (en) * | 1997-10-15 | 2002-07-31 | 旭化成株式会社 | Ammoxidation catalyst for use in producing acrylonitrile or methacrylonitrile from propane or isobutane by ammoxidation |
| CN103402976A (en) * | 2011-03-02 | 2013-11-20 | 旭化成化学株式会社 | Method for producing unsaturated nitrile |
| CN103402976B (en) * | 2011-03-02 | 2016-03-30 | 旭化成化学株式会社 | The manufacture method of unsaturated nitrile |
| CN104549373A (en) * | 2013-10-28 | 2015-04-29 | 中国石油化工股份有限公司 | Low-carbon alkane ammoxidation catalyst |
| CN105312067A (en) * | 2014-07-11 | 2016-02-10 | 中国石油化工股份有限公司 | Light alkane ammoxidation catalyst |
| CN105312067B (en) * | 2014-07-11 | 2018-01-09 | 中国石油化工股份有限公司 | Low-carbon alkanes ammoxidation catalyst |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1020597C (en) | 1993-05-12 |
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