CN100368082C - Fluidized bed catalyst for prodn. of acrylonitrile - Google Patents
Fluidized bed catalyst for prodn. of acrylonitrile Download PDFInfo
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- CN100368082C CN100368082C CNB2004100666220A CN200410066622A CN100368082C CN 100368082 C CN100368082 C CN 100368082C CN B2004100666220 A CNB2004100666220 A CN B2004100666220A CN 200410066622 A CN200410066622 A CN 200410066622A CN 100368082 C CN100368082 C CN 100368082C
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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
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- 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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Abstract
The present invention relates to a fluidized bed catalyst for propylene ammoxidation to produce acrylonitrile, which mainly solves the problems of the existing catalyst without relating to higher reaction pressure and operating load in the prior art. The fluidized bed catalyst adopts compositions which contain a silica carrier and have the chemical formula of A<a>B<b>C<c>Ni<d>Fe<e>Bi<f>Mo<12>O<x> according to the atomic ratio, wherein A is selected from at least one of Li, Na, K, Rb and Cs; B is selected from at least one of W, P, B, Ga, Cr, Sb, Al, Ge, Nb and V; C is selected from Ag, Cu or compounds of Ag and Cu; with the technical scheme of the catalyst, the problems are better solved. The fluidized bed catalyst has the advantage of good oxidation and reduction stability, and is especially suitable for conditions with lower reaction temperature, low air/propylene ratios, higher reaction pressure and high propylene load; the fluidized bed catalyst can keep higher single acrylonitrile yield and propylene conversion rates, can greatly improve acrylonitrile producing efficiency and economical efficiency and can be used in industrial production.
Description
Technical field
The present invention relates to a kind of method for preparing acrylonitrile.
Background technology
Acrylonitrile is important Organic Chemicals, and it is produced by the ammoxidation of propylene reaction.For obtaining the fluid catalyst of high activity, high selectivity, people have carried out a series of improvement through constantly exploring.These improve and mostly relate to the catalyst activity composition, pay attention to the collocation between the catalyst activity component, and improve activity of such catalysts and selectivity, thereby reach the raising of acrylonitrile once through yield, and the raising of producing load.
Ammonia oxidation is produced acrylonitrile through 40 years of development, and the production capacity of factory and the market demand are near balance.The main development trend of acrylonitrile process is built the technological transformation that new equipment turns to original factory by emphasis, further to cut down the consumption of raw materials and to increase production capacity at present.By transformation to original factory, change the bottleneck in effective catalyst and the elimination production technology, the production capacity of acrylonitrile might improve 50～80%, and required investment only is 20～30% of a new device, economic benefit is very huge.
Can produce two problems during factory transforms: 1. the reaction pressure of fluidized-bed reactor will rise; 2. the useful load of catalyst can not be too many.Require the catalyst use instead should be able to long-time running under higher propylene load and higher reaction pressure for this reason, and keep higher acrylonitrile yield.
The WWH that improves catalyst in theory should increase the adsorption activation ability of catalyst to propylene, but at present still in the catalyst-free certain element can improve report to propylene adsorption activation ability.The catalyst of following composition has been proposed in document CN1021638C:
A
aB
bC
cNi
dCo
eNa
fFe
gBi
hM
iMo
jO
x
Wherein A is potassium, rubidium, caesium, samarium, thallium; B is manganese, magnesium, strontium, calcium, barium, lanthanum, rare earth element; C is phosphorus, arsenic, boron, antimony, chromium; M is tungsten, vanadium.
Above-mentioned catalyst can obtain higher single-pass yield of acrylonitrile, but the propylene of catalyst load is lower, and single-pass yield of acrylonitrile descends bigger under higher reaction pressure.
Introduced the catalyst that a kind of catalyst that uses molybdenum, bismuth, iron, nickel, magnesium, potassium and caesium system carries out preparing acrylonitrile by allylamine oxidation among document US 5093299 and the US5212137.Introduce in this patent, its catalyst can be operated under lower slightly usually reaction temperature, and it has advantages of high catalytic activity and advantages of excellent oxidation-reduction stability, thereby compares conditional operation applicable to lower air/propylene.But it should be noted that magnesium is the basic element during catalyst is formed in the above-mentioned patent.The investigation condition of embodiment is a fixed bed simultaneously, and 430 ℃ of reaction temperatures are not mentioned reaction pressure concrete in the experimental implementation and operational load situation data.This fixed bed investigation condition is difficult to reflect the truth of fluidized bed process.
Introduced a kind of manufacture method of acrylonitrile among the flat 8-27089 of document.It adopts the catalyst of molybdenum, bismuth, iron, magnesium and tungsten system to carry out the ammoxidation of propylene reaction, and the investigation condition among the document embodiment is a normal pressure, does not mention the situation data under high pressure, high-load condition.
Summary of the invention
Technical problem to be solved by this invention is to overcome the catalyst that exists in the above-mentioned document not relate to problem than high-response pressure and operational load, and a kind of fluid catalyst of new production acrylonitrile is provided.This catalyst has can adapt under usually lower slightly reaction temperature, lower air/propylene mol ratio, higher reaction pressure and higher loading condiction to be operated, and can keep the characteristics of higher single-pass yield of acrylonitrile and higher propylene conversion.
For solving the problems of the technologies described above, the technical solution used in the present invention is as follows: a kind of fluid catalyst of producing acrylonitrile, contain silica supports and with the following composition of atomic ratio measuring chemical formula:
A
aB
bC
cNi
dFe
eBi
fMo
12O
x
A is selected from least a among Li, Na, K, Rb or the Cs in the formula;
B is selected from least a among W, P, B, Ga, Cr, Sb, Ge, Nb or the V;
C is selected from least a among Ag or the Cu;
The span of a is 0.01～2.0;
The span of b is 0.01～5.0;
The span of c is 0.01～2.0;
The span of d is 0.1～12.0;
The span of e is 0.1～7.0;
The span of f is 0.05～5.0;
X satisfies the required oxygen atom sum of each element valence in the catalyst;
Wherein the consumption of carrier silica is 30～70% by weight percentage in the catalyst.
The value preferable range of a is 0.01～1.0 in the technique scheme, the value preferable range of b is 0.01～3.5, the value preferable range of c is 0.01～1.0, the value preferable range of d is 0.1～10.0, the value preferable range of e is 0.1～5.0, the value preferable range of f is 0.05～3.0, and the consumption preferable range of carrier silica is 40～60% by weight percentage in the catalyst.
The manufacture method of catalyst of the present invention there is no specific (special) requirements, can be undertaken by well-established law.At first the catalyst each component is made solution, be mixed and made into slurry with carrier again, the spray-dried microspheroidal that is shaped to, catalyst is made in last roasting.The preparation of slurry is preferably undertaken by the CN1005248C method.
The raw material of making catalyst of the present invention is:
Molybdenum component in the catalyst is with molybdenum oxide or ammonium molybdate.
The most handy corresponding acids of phosphorus in the catalyst and boron or its ammonium salt; Germanium can be used germanium oxide; The most handy corresponding oxide of tungsten and antimony or its ammonium salt; The most handy nitrate of niobium, hydroxide and oxide; The most handy chromium trioxide of chromium, chromic nitrate or the mixture of the two; The most handy its nitrate of all the other components, hydroxide maybe can be decomposed into the salt of oxide.
Raw material available silicon colloidal sol, silicon gel or both mixtures as carrier silica.If use Ludox, its quality will meet the requirement of CN1005248C.
It is 47～55% back spray-dryings that the prepared slurry heating is concentrated to solid content.Spray dryer available pressure formula, two streamings or centrifugal turntable formula, but, can guarantee that the catalyst of making has good size distribution with centrifugal better.
The roasting of catalyst can be divided into two stages and carry out: each element decomposition of salts and high-temperature roasting in the catalyst.The catabolic phase temperature is preferably 200～300 ℃, and the time is 0.5～2 hour.Sintering temperature is 500～800 ℃, is preferably 550～700 ℃; Roasting time is 20 minutes to 2 hours.Above-mentioned decomposition and roasting are carried out respectively in two roasters, also can be divided into two zones in a stove, also can finish simultaneously in the continous way rotary roasting furnace and decompose and roasting.In catalyst decomposes and roasting process, to feed an amount of air,, and prevent that catalyst is by over reduction with generation catalytic activity phase.
Adopt the specification of catalyst manufacturing acrylonitrile of the present invention required propylene, ammonia and molecular oxygen identical with other ammoxidation catalyst of use.Though the low molecule saturated hydrocarbon content in the raw material propylene to the reaction did not influence, considers that from economic point of view density of propylene is more preferably greater than 85% (mole).Ammonia can be used fertilizer grade liquefied ammonia.Reaction desired molecule oxygen can be used pure oxygen from technical standpoint, oxygen enrichment and air, but from economy and the most handy air of security consideration.
Entering the ammonia of fluidized-bed reactor and the mol ratio of propylene is between 0.8～1.5, is preferably 1.0～1.3.The mol ratio of air and propylene is 8～10.5, is preferably 9.0～9.8.If owing to some operational reason must with higher air than the time, can increase to 11, reaction is not had significant impact.But from security consideration, the excess of oxygen in the reacting gas can not preferably be not more than 4% greater than 7% (volume).
When catalyst of the present invention was used for fluidized-bed reactor, reaction temperature was 410～470 ℃, was preferably 420～440 ℃.Catalyst of the present invention is a kind of usually lower slightly reaction temperature that is applicable to, high pressure, high load capacity catalyst, and therefore reaction pressure can be more than 0.08MPa in process units, for example, 0.08～0.18MPa.Also do not have any adverse effect if reaction pressure is lower than 0.08MPa, single-pass yield of acrylonitrile can further improve.
The propylene load (WWH) of catalyst of the present invention is 0.06～0.15 hour
-1, be preferably 0.08～0.12 hour
-1Loading to hang down not only wastes catalyst, and carbon dioxide production is increased, and selectivity descends, and is disadvantageous.
The product of making acrylonitrile with catalyst of the present invention reclaims process for refining, and available existing production technology need not done any transformation.The eluting gas that is fluidized-bed reactor is removed unreacted ammonia through neutralizing tower, with water at low temperature whole organic products is absorbed again.Absorption liquid gets high-purity propylene nitrile product through extractive distillation after dehydrogenation cyanic acid and the processed.
The surface of catalyst has been modified in the existence of catalyst C dvielement of the present invention; Improved propylene conversion; Category-B element and iron synergy in the component, quicken gas phase oxygen and entered caltalyst phase and the body diffusion of oxygen mutually, make the oxidation rapidly of reacted catalyst, again recover active, thereby helping keeping reacting is in good redox cycle, makes that catalyst has at usually lower slightly reaction temperature (430 ℃), low air/propylene mol ratio (9.5: 1), (WWH is 0.11 hour than high-response pressure (0.14MPa), higher load
-1) operational capacity under the condition, and the acrylonitrile once through yield reached about 81%, obtained effect preferably.
Activity of such catalysts of the present invention examination is to carry out in internal diameter is 38 millimeters fluidized-bed reactor.Loaded catalyst 400 grams, 430 ℃ of reaction temperatures, reaction pressure 0.14MPa, raw material proportioning (mole) is a propylene: ammonia: air=1: 1.2: 9.5, the propylene load (WWH) of catalyst is 0.11 hour
-1
Propylene conversion, acrylonitrile selectivity and once through yield are defined as follows in the present invention:
The invention will be further elaborated below by embodiment.
The specific embodiment
[embodiment 1]
1.80 gram cesium nitrates, 3.19 gram sodium nitrate are mixed with 2.25 gram potassium nitrate, add water 30 grams and the dissolving of heating back, obtain material (A); 9.36 gram chromium trioxides are dissolved in the 15 gram water, get material (B); 392.4 gram ammonium molybdates are dissolved in 60～90 ℃ of hot water of 350 grams, get material (C); 67.4 gram bismuth nitrates, 9.39 gram silver nitrates, 0.96 gram germanium oxide, 408.1 gram nickel nitrates and 302.4 gram ferric nitrates are mixed, add water 250 grams, after the heating for dissolving as material (D); Take by weighing phosphoric acid solution 4.35 grams as material (E).
With material (A) and 1280 gram weight concentration is that 40% Ludox mixes, under agitation add material (C), (B), (D) and (E) successively, after fully stirring, get slurry, according to well-established law the slurry of making is carried out the framboid moulding in spray dryer, it is 89 millimeters at internal diameter at last, length be in the rotary roasting furnace of 1700 millimeters (89 * 1700 millimeters of φ) in 600 ℃ of roastings 2.0 hours, make and consist of:
50％Mo
12Bi
0.75Fe
4.0Ni
7.5Ag
0.3Na
0.29K
0.1Cs
0.05Cr
0.5P
0.1Ge
0.05O
x+50％SiO
2。
[embodiment 2～6 and comparative example 1～4]
Adopt method preparation substantially the same manner as Example 1 to have the different catalyst of forming in the following table, and under following reaction condition, carry out the reaction that ammoxidation of propylene generates acrylonitrile, the results are shown in Table 1 with prepared catalyst.
The reaction condition of the foregoing description and comparative example is:
38 millimeters fluidized-bed reactors of φ
430 ℃ of reaction temperatures
Reaction pressure 0.14MPa
Loaded catalyst 400 grams
Catalyst propylene load (WWH) 0.11 hour
-1
Raw material proportioning (mole) C
3 =/ NH
3/ air=1/1.2/9.5
Table 1
| Embodiment | Catalyst is formed | Acrylonitrile yield % | Acrylonitrile selectivity % | Propylene conversion % |
| Embodiment 1 | Mo 12Bi 0.75Fe 4.0Ni 7.5Ag 0.3Na 0.29K 0.1Cs 0.05Cr 0.5Ge 0.05O x | 80.8 | 81.2 | 99.5 |
| Embodiment 2 | Mo 12Bi 0.75Fe 4.0Ni 7.5Cu 0.3Na 0.29K 0.1Cs 0.05Cr 0.5Ge 0.05O x | 82.1 | 82.1 | 100 |
| Embodiment 3 | Mo 12Bi 0.75Fe 4.0Ni 7.5Ag 0.8Na 0.29K 0.1Cs 0.05W 1.0P 0.25O x | 81.2 | 81.5 | 99.6 |
| Embodiment 4 | Mo 12Bi 1.25Fe 4.0Ni 7.5Na 0.29K 0.1Cs 0.05Cr 0.5Cu 0.3Ag 0.3Ge 0.05O x | 81.4 | 82.0 | 99.3 |
| Embodiment 5 | Mo 12Bi 1.25Fe 4.0Ni 77.5Na 0.29K 0.1Cs 0.05Cr 0.5Cu 0.3V 0.5P 0.5O x | 81.3 | 81.5 | 99.7 |
| Embodiment 6 | Mo 12Bi 1.0Fe 4.0Ni 7.5K 0.05Cs 0.2Ge 0.3Na 0.29Ag 0.3Sb 0.5O x | 81.1 | 81.4 | 99.7 |
| Embodiment 7 | Mo 12Bi 0.75Fe 4.0Ni 7.5Na 0.29K 0.1Cs 0.05Ag 0.3W 1.0P 0.25O x | 81.5 | 81.7 | 99.8 |
| Embodiment 8 | Mo 12Bi 0.75Fe 4.0Ni 7.5Na 0.29K 0.1Cs 0.05W 0.1V 0.3Cu 0.1Sb 0.5O x | 79.8 | 80.5 | 99.1 |
| Comparative example 1 | Mo 12Bi 0.9Fe 4.0Ni 7.5Na 0.15Cr 0.45K 0.17Cs 0.05O x | 78.6 | ||
| Comparative example 2 | Mo 12Bi 0.9Fe 4.0Ni 7.5Na 0.15Cr 0.45K 0.21O x | 78.9 | ||
| Comparative example 3 | Mo 12Bi 0.9Fe 4.0Ni 7.5Na 0.15W 0.45K 0.15Cs 0.07O x | 79.4 | ||
| Comparative example 4 | Mo 12Bi 0.9Fe 4.0Ni 7.5Na 0.15W 0.45Cs 0.09O x | 77.9 |
Claims (8)
1. method for preparing acrylonitrile is characterized in that: the used fluid catalyst of described method contains silica supports and with the following composition of atomic ratio measuring chemical formula:
A
aB
bC
cNi
dFe
eBi
fMo
12O
x
A is selected from least a among Li, Na, K, Rb or the Cs in the formula;
B is selected from least a among W, P, B, Ga, Cr, Sb, Ge, Nb or the V;
C is selected from least a among Ag or the Cu;
The span of a is 0.01～2.0;
The span of b is 0.01～5.0;
The span of c is 0.01～2.0;
The span of d is 0.1～12.0;
The span of e is 0.1～7.0;
The span of f is 0.05～5.0;
X satisfies the required oxygen atom sum of each element valence in the catalyst;
Wherein the consumption of carrier silica is 30～70% by weight percentage in the catalyst.
2. according to the described method for preparing acrylonitrile of claim 1, the span that it is characterized in that a is 0.01～1.0.
3. according to the described method for preparing acrylonitrile of claim 1, the span that it is characterized in that b is 0.01～3.5.
4. according to the described method for preparing acrylonitrile of claim 1, the span that it is characterized in that c is 0.01～1.0.
5. according to the described method for preparing acrylonitrile of claim 1, the span that it is characterized in that d is 0.1～10.0.
6. according to the described method for preparing acrylonitrile of claim 1, the span that it is characterized in that e is 0.1～5.0.
7. according to the described method for preparing acrylonitrile of claim 1, the span that it is characterized in that f is 0.05～3.0.
8. according to the described method for preparing acrylonitrile of claim 1, the consumption that it is characterized in that carrier silica in the catalyst is 40～60% by weight percentage.
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| CN100368082C true CN100368082C (en) | 2008-02-13 |
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| CN102658167B (en) * | 2012-05-08 | 2014-03-26 | 营口市向阳催化剂有限责任公司 | Catalyst for use in preparation of acrylonitrile by performing ammonia oxidation on propylene |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1295063A (en) * | 1999-11-03 | 2001-05-16 | 中国石油化工集团公司 | Propylene ammonoxidizing fluid bed catalyst |
| CN1310172A (en) * | 2000-02-24 | 2001-08-29 | 中国石油化工集团公司 | Fluidized bed catalyst for ammoxidating propylene to prepare acrylonitrile |
| CN1413978A (en) * | 2001-10-22 | 2003-04-30 | 中国石油化工股份有限公司 | Fluidized-bed catalyst for preparing acrylonitrile |
| CN1413979A (en) * | 2001-10-22 | 2003-04-30 | 中国石油化工股份有限公司 | Fluidized-bed catalyst for preparing acrylonitrile by allylamine oxidation |
| CN1418868A (en) * | 2001-11-14 | 2003-05-21 | 中国石油化工股份有限公司 | Fluidized bed catalyst for preparing acrylonitrile by propene ammoxidation |
| CN1418728A (en) * | 2001-11-14 | 2003-05-21 | 中国石油化工股份有限公司 | Method for prepn. of fluidized catalyst for prodn. of acrylonitrile |
| CN1507949A (en) * | 2002-12-17 | 2004-06-30 | 中国石油化工股份有限公司 | Fluidized bed catalyst for producing acrylonitrile |
-
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- 2004-09-24 CN CNB2004100666220A patent/CN100368082C/en active Active
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1295063A (en) * | 1999-11-03 | 2001-05-16 | 中国石油化工集团公司 | Propylene ammonoxidizing fluid bed catalyst |
| CN1310172A (en) * | 2000-02-24 | 2001-08-29 | 中国石油化工集团公司 | Fluidized bed catalyst for ammoxidating propylene to prepare acrylonitrile |
| CN1413978A (en) * | 2001-10-22 | 2003-04-30 | 中国石油化工股份有限公司 | Fluidized-bed catalyst for preparing acrylonitrile |
| CN1413979A (en) * | 2001-10-22 | 2003-04-30 | 中国石油化工股份有限公司 | Fluidized-bed catalyst for preparing acrylonitrile by allylamine oxidation |
| CN1418868A (en) * | 2001-11-14 | 2003-05-21 | 中国石油化工股份有限公司 | Fluidized bed catalyst for preparing acrylonitrile by propene ammoxidation |
| CN1418728A (en) * | 2001-11-14 | 2003-05-21 | 中国石油化工股份有限公司 | Method for prepn. of fluidized catalyst for prodn. of acrylonitrile |
| CN1507949A (en) * | 2002-12-17 | 2004-06-30 | 中国石油化工股份有限公司 | Fluidized bed catalyst for producing acrylonitrile |
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