CN1099316C - Catalyst for acrylonitrile fluid bed - Google Patents
Catalyst for acrylonitrile fluid bed Download PDFInfo
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- CN1099316C CN1099316C CN99119952A CN99119952A CN1099316C CN 1099316 C CN1099316 C CN 1099316C CN 99119952 A CN99119952 A CN 99119952A CN 99119952 A CN99119952 A CN 99119952A CN 1099316 C CN1099316 C CN 1099316C
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- acrylonitrile
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Abstract
The present invention relates to a catalyst of an acrylonitrile fluid bed, which comprises a silicon dioxide carrier and a composition with a chemical formula (counted by atomic ratio): A<a>B<b>C<c>Ge<d>Na<e>Mg<f>Fe<g>Bi<h>Mo<i>O<x>, wherein A is at least one of Li, K, Rb, Cs and Sm, B is at least one of Sr, Ba, Pb, V, Cr, Mn and Ni, and C is at least one of B, P and As. The catalyst of the present invention is especially suitable for being used under the conditions of lower reaction temperature, higher reaction pressure and high propene load, can maintain high single yield of acrylonitrile, and can be used in industrial production.
Description
The present invention relates to acrylonitrile fluidized-bed catalyst.
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 catalyst activity partly, 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 30 years of development, and the production capacity of factory and the market demand are near balance.The main development tendency of acrylonitrile process has been turned to the transformation of original factory, further to cut down the consumption of raw materials and to increase production capacity by the construction new equipment 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.The catalyst that for this reason requires to use instead should have higher propylene load and can bear higher reaction pressure.
The reaction pressure of fluidized-bed reactor is to be determined to the resistance drop that absorbs a series of heat exchangers, tower and pipe arrangement the cat head by reactor outlet.Because the increase of production capacity obviously increases the inventory of reactor outlet, above-mentioned resistance drop is increased.In addition, each heat exchanger heat transfer area also need increase heat transmission equipment inadequately, and resistance drop is further increased.Because environmental requirement, the reactor off-gas that absorbs cat head is forbidden directly to be discharged in the atmosphere, deliver to stove and burn.If like this without air-introduced machine, then must improve the absorption tower top pressure.For all the foregoing reasons, the operating pressure of reactor will increase by 0.5～1.0 times than design load at present, promptly reaches more than the 0.08MPa.
Above-mentioned second load that problem is a catalyst, i.e. WWH.Its definition is a catalyst per ton, per hour can handle what ton propylene.Because the increase of reactor feed amount, if the load of catalyst is constant, then the catalyst useful load is also wanted corresponding increase.But cooling water pipe insufficient height in the intrinsic fluidized-bed reactor, so the fluid height of catalyst reactor might surpass the height of cooling water pipe.In addition, because the increase of reactor feed amount, so operating linear velocity also significantly improves.The combined influence of these two variations might make reactor dilute phase temperature rise, and causes carbon dioxide production to increase, and the acrylonitrile selectivity descends.Therefore the WWH of catalyst is higher can prevent the problems referred to above.If can effectively reduce reaction temperature, can cut down the consumption of energy on the one hand in addition, also can improve reaction condition on the other hand, reach the purpose that improves acrylonitrile yield.
The WWH that improves catalyst in theory should increase the adsorption capacity of catalyst to propylene, but at present still in the catalyst-free certain element can improve theory to the propylene adsorption capacity.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.Studies show that further the B component in the above-mentioned catalyst is relevant with performance under high pressure to the load of catalyst with M.Though some element in the B component has effect to improving single-pass yield of acrylonitrile, and the raising of catalyst loading and the performance of high-response pressure are had negative effect, be unfavorable for that catalyst adapts to elevated pressures, operates under the higher load condition.Once in stipulating in CN1021638C in addition that above-mentioned catalyst was formed, the summation of i and j is 12, promptly is a constant.Cancel this regulation in the present invention,, will influence single-pass yield of acrylonitrile because molybdenum component will reduce when increasing by this regulation M component.
Introduced a kind of germanic ammoxidation catalyst that obtains the high acrylonitrile yield among document US 5688739 and the US5770757.Adopt molybdenum, bismuth, germanium system in the document, alkali metal containing in the optional elements, but the unexposed example that contains sodium among the embodiment, only disclosing reaction pressure in addition in the document is the reaction condition of normal pressure, not the concrete investigation data under high pressure, high-load condition.Introduced a kind of catalyst of producing acrylonitrile or methacrylonitrile in the document US 5212137.The document adopts the catalyst technology scheme that contains Mo-Bi-Fe-Ni-Mg-K-Cs, discloses the fixed bed reaction performance data under 430 ℃ of conditions, is not disclosed in the fluid bed performance data under high pressure, the high-load condition.
The objective of the invention is to overcome the catalyst that exists in the above-mentioned document do not relate to adaptation than high-response pressure, high operational load and under the low reaction temperatures condition problem of reactivity worth, a kind of new fluidized bed catalyst for preparing acrylonitrile by propene ammonia oxidation is provided.This catalyst can adapt at higher reaction pressure, higher load, operate than under the condition than low reaction temperatures and lower air/propylene, and keeps high acrylonitrile once through yield.
The objective of the invention is to realize by following technical scheme: a kind of acrylonitrile fluidized-bed catalyst, by forming with the following composition of atomic ratio measuring chemical formula:
A
aB
bC
cGe
dNa
eMg
fFe
gBi
hMo
iO
x
A is selected from least a among Li, K, Rb, Cs or the Sm in the formula;
B is selected from least a among Sr, Ba, Pb, V, Cr, Mn or the Ni;
C is selected from least a among B, P or the As;
The scope of winning the confidence of a is 0.01～1.5;
The span of b is 0.1～8.0;
The span of c is 0.1～0.6;
The span of d is 0.01～1.0;
The span of e is 0.01～0.7;
The span of f is 0.8～7.5;
The span of g is 0.1～8.0;
The span of h is 0.5～1.0;
The span of i is 12.0～14.5;
X satisfies the required oxygen atom sum of each element valence in the catalyst;
Wherein catalyst carrier is selected from silica, aluminium oxide or its mixture, and its consumption is 30～70% by weight percentage.
The value preferable range of a is 0.01～0.7 in the technique scheme, and the value preferable range of d is 0.10～0.15, and the value preferable range of e is 0.05～0.5, and the value preferable range of f is 1.0～7.0, and the value preferable range of g is 1.0～3.0.The preferred silica of catalyst carrier, its consumption are 40～60% by weight percentage.
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:
The molybdenum component is with molybdenum oxide or ammonium molybdate in the catalyst.
The most handy corresponding acids of phosphorus, arsenic and boron or its ammonium salt in the catalyst; Vanadium can be used ammonium metavanadate; Its oxide of germanium; The most handy chromium trioxide of chromium, chromic nitrate or the mixture of the two; Other component can maybe can be decomposed into the salt of oxide with its nitrate, oxide, but preferably uses water miscible nitrate.
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, prevent that catalyst is by over reduction.
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 420～470 ℃, was preferably 425～450 ℃.Therefore catalyst of the present invention is a kind of low temperature, high pressure, high load capacity catalyst of being applicable to, reaction pressure can be more than 0.08MPa in process units, for example, and 0.08～0.15MPa.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 0.07～0.10 hour
-1Loading to hang down not only wastes catalyst, and carbon dioxide production is increased, and selectivity descends, and is disadvantageous.Loading does not too highly have practical significance, because the catalyst addition is very few, the heat transfer area that can make cooling water pipe in the catalyst layer causes reaction temperature uncontrollable less than removing the required area of reaction heat.
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 is through extractive distillation, dehydrogenation cyanic acid and dewater high-purity propylene nitrile product.
The present invention is by adding component germanium in molybdenum, bismuth, iron and sodium catalyst system and catalyzing, find that this catalyst system and catalyzing has than high-response pressure (0.14MPa), and (WWH is 0.085 hour to higher load
-1) operational capacity under the condition, in catalyst system, add component magnesium again, find that this catalyst system and catalyzing under 430 ℃ of conditions of reaction temperature, still has advantages of high catalytic activity and selectivity; Suitably add other effective active components in addition, make this catalyst 430 ℃ of reaction temperatures, elevated pressures 0.14MPa, higher load 0.085 hour
-1And lower air/propylene operated under (mole) condition than 9.5: 1, and its acrylonitrile once through yield reaches as high as 80.2%, has 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 0.085 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.[embodiment 1]
With 2.02 gram cesium nitrates, 4.21 gram sodium nitrate, 0.96 gram rubidium nitrate and 2.28 gram potassium nitrate mix, and add water 30 gram and heating for dissolving, obtain material (A); 6.85 gram germanium dioxides and 412.6 gram ammonium molybdates are dissolved in 60～90 ℃ of hot water of 350 grams, get material (B); 66.8 gram bismuth nitrates, 278.5 gram nickel nitrates, 194.3 gram magnesium nitrates, 21.8 gram manganese nitrates, 31.4 gram plumbi nitras and 206.5 gram ferric nitrates are mixed, add water 180 grams, after the heating for dissolving as material (C); Take by weighing phosphoric acid solution 4.42 grams as material (D).
With material (A) and 1285 gram weight concentration is that 40% Ludox mixes, under agitation add material (B), (C), (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 575 ℃ of roastings 1.5 hours, make and consist of 55%K
0.1Rb
0.025Cs
0.05P
0.025Ni
5.0Mn
0.1Pb
0.25Ge
0.15Na
0.20Mg
2.0Fe
2.5Bi
0.50Mo
12.5O
x+ 45%SiO
2[embodiment 2～8 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, the results are shown in Table 1 with carrying out the reaction that ammoxidation of propylene generates acrylonitrile under the prepared catalyst reaction condition below.
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) 0.085 hour
-1
Unstripped gas 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 | K 0.1Rb 0.025Cs 0.05P 0.025Ni 5.0Mn 0.1Pb 0.25Ge 0.15Na 0.20Mg 2.0Fe 2.5Bi 0.5Mo 12.5O x | 80.2 | 81.6 | 98.3 |
| Embodiment 2 | K 0.125Cs 0.10P 0.030Ni 2.5V 0.5Mn 0.1Pb 0.20Ge 0.15Na 0.20Mg 2.5Fe 3.0Bi 0.5Mo 12.5O x | 79.8 | 81.4 | 98.0 |
| Embodiment 3 | K 0.15Rb 0.025Cs 0.065P 0.05Ni 4.5Mn 0.15Cr 0.45Ge 0.10Na 0.20Mg 2.5Fe 2.5Bi 0.75Mo 12.5O x | 79.6 | 81.4 | 97.8 |
| Embodiment 4 | Li 0.05K 0.125Cs 0.05B 0.02As 0.015Ni 5.0Cr 0.35Pb 0.15Ge 0.15Na 0.20Mg 2.0Fe 2.0Bi 0.5Mo 12.5O x | 80.0 | 81.6 | 98.0 |
| Embodiment 5 | K 0.15Cs 0.075P 0.025Ni 2.5V 1.5C r0.40Pb 0.25Ge 0.10Na 0.15Mg 2.5Fe 2.5Bi 0.5Mo 12.5O x | 79.6 | 81.6 | 97.6 |
| Embodiment 6 | Li 0.05K 0.125Rb 0.05B 0.02P 0.025Ni 3.5V 1.0Sm 0.1Ge 0.15Na 0.20Mg 2.5Fe 2.0Bi 0.5Mo 12.5O x | 80.1 | 81.7 | 98.0 |
| Embodiment 7 | K 0.1Rb 0.05Cs 0.025As 0.030Ni 5.0Cr 0.25Pb 0.25Ge 0.15Na 0.20Mg 2.0Fe 2.5Bi 1.0Mo 12.5O x | 79.7 | 81.0 | 98.4 |
| Embodiment 8 | Li 0.05K 0.125Rb 0.05P 0.02As 0.015Ni 4.5Sm 0.15Mn 0.15Ge 0.15Na 0.20Mg 2.5Fe 2.5Bi 1.0Mo 12.5O x | 79.9 | 82.0 | 97.4 |
| Comparative example 1 | Mo 12Bi 0.9Fe 1.8Ni 2.0Co 5.0Na 0.15Mn 0.45Cr 0.45K 0.17Cs 0.05O x | 76.3 | ||
| Comparative example 2 | Mo 12Bi 0.9Fe 1.8Ni 2.4Co 4.3Na 0.15W 0.45Cr 0.45K 0.15Cs 0.07O x | 76.6 | ||
| Comparative example 3 | Mo 12Bi 0.9Fe 1.8Ni 2.0Co 5.0Na 0.15Mn 0.45Cr 0.45K 0.21O x | 75.7 | ||
| Comparative example 4 | Mo 12Bi 0.9Fe 1.8Ni 5.0Mg 2.0Na 0.15W 0.45Cr 0.45Cs 0.09O x | 76.9 |
Claims (7)
1, a kind of acrylonitrile fluidized-bed catalyst, by forming with the following composition of atomic ratio measuring chemical formula:
A
aB
bC
cGe
dNa
eMg
fFe
gBi
hMo
iO
x
A is selected from least a among Li, K, Rb, Cs or the Sm in the formula;
B is selected from least a among Sr, Ba, Pb, V, Cr, Mn or the Ni;
C is selected from least a among B, P or the As;
The span of a is 0.01～1.5;
The span of b is 0.1～8.0;
The span of c is 0.1～0.6;
The span of d is 0.01～1.0;
The span of e is 0.01～0.7;
The span of f is 0.8～7.5;
The span of g is 0.1～8.0;
The span of h is 0.5～1.0;
The span of i is 12.0～14.5;
X satisfies the required oxygen atom sum of each element valence in the catalyst;
Wherein catalyst carrier is selected from silica, aluminium oxide or its mixture, and its consumption is 30～70% by weight percentage.
2, according to the described acrylonitrile fluidized-bed catalyst of claim 1, the span that it is characterized in that a is 0.01～0.7.
3, according to the described acrylonitrile fluidized-bed catalyst of claim 1, the span that it is characterized in that d is 0.10～0.15.
4, according to the described acrylonitrile fluidized-bed catalyst of claim 1, the span that it is characterized in that e is 0.05～0.5.
5, according to the described acrylonitrile fluidized-bed catalyst of claim 1, the span that it is characterized in that f is 1.0～7.0.
6, according to the described acrylonitrile fluidized-bed catalyst of claim 1, the span that it is characterized in that g is 1.0～3.0.
7, according to the described acrylonitrile fluidized-bed catalyst of claim 1, it is characterized in that catalyst carrier is a silica, its consumption is 40～60% by weight percentage.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN99119952A CN1099316C (en) | 1999-11-03 | 1999-11-03 | Catalyst for acrylonitrile fluid bed |
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|---|---|---|---|
| CN99119952A CN1099316C (en) | 1999-11-03 | 1999-11-03 | Catalyst for acrylonitrile fluid bed |
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|---|---|
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| CN1099316C true CN1099316C (en) | 2003-01-22 |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US8715539B2 (en) * | 2010-07-15 | 2014-05-06 | Hyundai Motor Company | Positive electrode material for lithium secondary battery and method for manufacturing the same |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100358629C (en) * | 2004-09-24 | 2008-01-02 | 中国石油化工股份有限公司 | Fluidized bed catalyst for preparing acetonitrile |
| CN107866256B (en) * | 2016-09-23 | 2019-12-10 | 中国石油化工股份有限公司 | Catalyst for synthesizing pyromellitic dianhydride by oxidizing pyromellitic dianhydride |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1021638C (en) * | 1990-11-05 | 1993-07-21 | 中国石油化工总公司 | Fluidized catalyst for acrylonitrile |
| US5688739A (en) * | 1995-05-01 | 1997-11-18 | The Standard Oil Company | Ammoxidation catalysts containing germanium to produce high yields of acrylonitrile |
-
1999
- 1999-11-03 CN CN99119952A patent/CN1099316C/en not_active Expired - Fee Related
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1021638C (en) * | 1990-11-05 | 1993-07-21 | 中国石油化工总公司 | Fluidized catalyst for acrylonitrile |
| US5688739A (en) * | 1995-05-01 | 1997-11-18 | The Standard Oil Company | Ammoxidation catalysts containing germanium to produce high yields of acrylonitrile |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US8715539B2 (en) * | 2010-07-15 | 2014-05-06 | Hyundai Motor Company | Positive electrode material for lithium secondary battery and method for manufacturing the same |
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| CN1294942A (en) | 2001-05-16 |
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