Catalyst for decreasing nitrogen oxide content in flue gases, method of its manufacture and catalyti

专利摘要:
The invention relates to catalytic chemistry, in particular the preparation of a catalyst for a process for the catalytic reduction of the nitrogen oxide content in flue gases containing sulfur oxides, and can be used in chemical production. The goal is to increase the activity and selectivity of the catalyst and the conversion of nitrogen oxides. The catalyst is obtained by impregnating a three-layer silicate with a solution containing one or more metal salts, Ti, Zr, V, W, Mo, Ce, followed by washing, molding and calcining. Used silicate is activated by acid with preservation of the crystal structure
公开号:SU1685256A3
申请号:SU864027955
申请日:1986-08-12
公开日:1991-10-15
发明作者:Шнайдер Михаель；Кохлефл Карл；Малетц Герд；Юрген Вернике Ханс
申请人:Зюд-Хеми Аг (Фирма)；
IPC主号:

专利说明:

The invention relates to a catalyst for reducing the content of nitric oxide in the exhaust flue gases, to a method for producing it and a method for reducing the content of nitric oxide in the exhaust dmmonic gases using a catalyst.
The purpose of the invention is to increase the activity and selectivity of a catalyst due to the content of a three-layer acid silicic acid silicate in it, which has certain characteristics: a partially preserved crystalline structure, cation-exchange capacity, a reduced concentration of interlayer cations, an increased surface, a certain atomic ratio between silicon contained in the acid-activated three-layer silicate, and metals contained in the oxides, due to the specific content of one or two or three metal oxides at a certain mass ratio between metal oxides, when running the catalyst in the form of molded rods.
The purpose of the invention is to obtain a catalyst with increased activity due to the use of silicate, activated in a certain way and having certain characteristics, by impregnating the silicate with a solution containing one or more metal salts.
The circuit of the invention is an increase in the degree of conversion of nitrogen oxides through the use of the catalyst described above.
The invention is illustrated by the following examples.
Example 1. a). 2 kg of the fraction of raw bentonite with an average grain size of 50 microns, a cation-exchange capacity of 79 mVal / SUO g, a BET surface of 69 m / g and a specified in table. 1 the chemical composition is mixed with 8 l of an aqueous solution of HCl for 6 hours at 80 ° C.
The content of NO is about 21% by weight with respect to the dry matter.
Then, the filtered precipitate is sucked off with a sufficient amount of acidified water (adjusted to pH 3.0 with S-8CS). The resulting acid-activated benzoite (nmzhe denoted by SAB) after drying at 200 ° C has a BET surface of about 210 m2 / g.
Its chemical composition is also listed in Table 1.
0
0
five
five
B
0
five
Hence, it is calculated by reducing the cation concentration in the intermediate layers by 75%.
b). About 320 g of water obtained in step (a) of SAB in 5 l of water are charged with a suspension of 160 rTi. OZO4 is neutralized by adding semi-concentrated ammonia. The solid phase is filtered off with suction, washed from sulphate and, after adding 10 mg of glycerin, is extruded into 3 mm diameter articles. Then they are calcined for 15 hours at 450 ° C.
The molding, drying and calcining of the catalyst mass is carried out in the same manner as in the following examples.
The effectiveness of catalysts with respect to the removal of nitrogen oxides from gas mixtures, which, in particular, also contain oxygen and sulfur oxides, is determined by contacting the catalyst With a gas stream, which is directed through an electrically heated outside pipe containing this catalyst in the form of a granular material,
The gas mixture used has the following composition:
02% by volume
% 10
N0 ob.ch on 1 million 750
MOGob.ch. at 1 million .50
Mnssb.ch at 1 million 800
S02 about.h per 1.950 million
50 e.p.1 million 50
N2, vol.% Difference with respect to 100 The concentration of the components N0 and NOa in the gas mixture before and after passing through the catalyst in the form of a granular material is continuously measured using a graded analyzer (chemoluminescence method),
The composition of the catalysts, the reaction temperature and the conversion of N0 or NOa at a volume velocity of 5000 is given in Table 2. For the reactions carried out, the indicated gas mixture was used; The conversions of N0 and N02 are determined according to the formulas indicated.
As a measure of the activity of the catalyst relative to the reduction of the oxides of the agot is the measure of the degree of conversion of the components N0 and MOG after the establishment of the stationary state, defined by the following ratios; MO - Conversion (UNO)
-.zCsio.choof)
CNO
N02 - Conversion (UN02)
 -WITH
NO2
Clj02
100 (% )
where CNO and CMO are the concentrations of NO and NO2, and the symbols E and A are, respectively, the state of the gas mixture before and after passing through the catalyst.
Examples 2 and 3. The process is carried out as in Example 1, however, 640 g (Example 2) or 1600 g TIOS04 (Example 3) are used.
Example 4. A mixture of 400 g and SAB (step and example 1} and a solution of 106 g of ammonium metatungstate are thoroughly mixed in 350 ml of water.
Example 5. Load 32 g NhUVOa in portions into a solution of 32 g oxalic acid dihydrate in 350 l of water and mix thoroughly with 475 g SAB stage and Example 1).
Example 6. In a suspension of 300 g of SAB (stage a of example 1) in 5 l of water are charged with stirring 180 g of TIOSO4 and neutralized with semi-concentrated ammonia. Sucked off, washed from sulphate and thoroughly mixed with a solution of 10.8 g of tungstic acid in 30 ml of semi-concentrated ammonia.
Example 7. The method is carried out as in Example 1, however, the starting materials are loaded in the following amounts, g:
SAB250
T1OS04450
Wolfram
acid27.0
Example 8. The catalyst was prepared as described in example 6 using the starting materials in the following amounts, g: SAB 100; TIOS04 720; tungstic acid 43.2.
Example 9.169 TIOS04 was loaded with stirring into a suspension of 400 g of SAB in 5 l of water. Neutralized with ammonia, washed to remove sulphate and thoroughly mixed with a solution prepared from 4.2 g of oxalic acid dihydrate, 2.6 g of NH4V03 and 50 ml of water.
Example 10 The method is carried out as in Example 9 with the difference that 250 g SAB, 490 g TIOS04, 10.2 g oxalic acid dihydrate and 6.4 g NH4V03 are used.
Example 11, Instead of the quantities of substances in example 9, 100 g of SAB, 784 rTIOS04,16.3 g of oxalic acid dihydrate and also 10.2 g of PCAF are charged.
Example 12.46 g of oxalic acid dihydrate was dissolved in 350 ml of water and 25.6 g of NH4V03 was added in portions. After adding 84.6 g of ammonium meta-tungstate, 400 g of SAB are charged and the resulting mass is mixed thoroughly.
Example 13. 450 g of SAB were introduced into solutions prepared from 25.6 g of oxalic acid dihydrate and 16 g in 200 ml of water and also from 86.6 basic cerium nitrate in 170 ml of water, and mixed thoroughly.
Example 14. A solution of 25.6 g of acid dihydrate and 16 g of MCCPH in 350 ml of water is stirred after the addition of 13Q.5 g of Zr (M0z) 4 5H20 C to 450 g of SAB.
Examples 15-23. The catalysts are obtained according to the following method, and the corresponding downloadable quantities are given in table. 2
TIOS04 was added to a suspension of SAB (step a of Example 1) in 5 liters of water with stirring. neutralized with ammonia and sucked off. The solid phase is washed to remove the sulfate, dried for 15 hours at 120 ° C and mixed with an ammonia solution of tungstic acid and also with a solution obtained by reducing ammonium metavanadate with a 1.6-fold excess of oxalic acid dihydrate. The amount of solvent is chosen in such a way that it is possible to obtain easily mixed paste.
The proportion of the pore volume determined by mercury porosimetry, at which micropores with a diameter greater than 80 nm fall, was 67.6% for the catalyst of Example 18. Values of the same dimension were obtained for other catalysts.
Example 24. 400 g of SAB are thoroughly mixed with a solution of 76.6 g of tungstic acid and 300 ml of semi-concentrated ammonia, the resulting mass is dried for 15 hours at 120 ° C and calcined for 3 hours at 500 ° C. Then it is sequentially mixed with a solution of 46.2 g of Се (ОН) (NOa) ЗНаО. in 175 ml of water, and with the same volume of solution obtained from 20.5 g of oxalic acid dihydrate and 12.8 g of NH403.
Example 25. A catalyst is prepared by analogy with Example 24, with 69.6 g of zirconium nitrate pentahydrate being replaced with cerium basic nitrate.
Examples 26-28. The catalysts according to examples 26 to 28 were prepared as follows.
With constant stirring, load TIOS04 into the suspension from SAB (stage a of example 1) is neutralized with ammonia. Sucked and washed to remove sulfate solid phase substance
mix thoroughly with 400 ml of the solution, which is prepared by adding basic cerium nitrate to the solution obtained from GL-UO3 and oxalic acid dihydrate (1: 1.6).
The applied amounts of "similar components are given in Table. 3
Examples 29-31. The mass catalysts according to examples 29 to 31 are prepared as in examples 26 to 28. However, the main cerium nitrate is replaced with zirconium nitrate hydrate (example 29; 20.9 g, example 30: 52.2 g; example 31: 83.5 g ) and the remaining components are used in the indicated amounts, examples 28 and 29, 27 and 30, and also 28 and 31 correspond to each other.
Comparative Vi-Ve Examples
By analogy with catalysts according to examples 15 and 18 O / hOb, WOs, TIO. with 80 or 50% SAB) for comparative chains, catalysts 1 to 8 were prepared, which, instead of acid-activated bentonite (step 1), did not contain the proposed silicate components.
The chemical composition of the silicate components is listed in Table. 1, the composition of the comparative catalysts and also achieved; with their help, iSfO conversions are given in Table. four.
A gas mixture with the above composition is used for the experiments.
The BET surfaces of the silicate components used for comparative catalysts are the following: raw bentonite {fuller's earth): 69 wr / r, bentonite activated with MS3: 41 m / g, natural acid clay: 82 m / g, amorphous silicic acid: 325 m2 / g
Experiments in comparative Vi-Ve examples show the need for acid activation.
The catalysts that are made using non-activated (Vi, Ug) or alkali-activated bentonite (Va, LO, with respect to the degree of conversion No also have less activity, as does the catalyst containing non-acidified natural clay (can be compared with clay with H-ion exchange) (Vs, Ve, V, Va), in particular, this occurs with a high content of the silicate component (examples of Vg-Vis).
The catalyst according to example 18 compare satib: m with a known catalyst; -; for reducing N0. The known catalyst contains oxide components without acid-activated bentonite, wt% V20s 1.0; CID: 0.9; : 90.0.
By means of tests, this catalyst is compared with the proposed catalyst according to example 18 with a gas mixture in accordance with the composition indicated at a bulk velocity of about 5000 hours. From the balance of the reacted components of the reaction, it is possible to determine the percentage of ammonia introduced into the reactor, which is actually consumed to reduce NOx,
In the comparative catalyst, a substantial portion of the ammonia is oxidized by the oxygen contained in the off-gas and therefore cannot be used for the desired removal of MO.
In tab. 5 shows the compositions of the comparative catalysts and the results of the conversion.
The proposed catalyst has a slightly less catalytic effect on the undesired oxidation of ammonia with oxygen,
Example 32 (comparative) A comparative test was carried out for which the catalyst was prepared with the composition according to Example 2, This catalyst was prepared by stirring as a dyed iiiaccw titanium dioxide (320 g) with the same amount of acid activated bentonite with the addition of 300 ml water and 20 ml of r / mtsormna, i.e. insoluble titanium salt (TiO304) is used. The deformation and the subsequent calcination are carried out according to example 2, dependent on example 1.
The following conversions were measured:
Conversion N0 is slightly lower compared to conversion with a catalyst according to Example 2 (see Table 4),
PRI me R 33. 800 g of SAB (step a of Example 1) in 5 l of water are added with stirring 360 g of TIOS04, neutralized with ammonia and sucked off, the solid is washed from sulphate, dried for 15 hours at 120 ° C and mixed with a solution of 18.1 ammonium heptamolybdate, as well as with rastrum, obtained by reducing 7.7 g of ammokam metaznadat with a 1.6-fold excess of dmgdrath oxalic shells, while the amount of solvent is chosen so that you can get easily translucent pasty mass.
Note 34. The method is carried out according to Example 33, however, the original substances are used for the following amounts: SA3
500; TIOS04 900; ammonium haptomolybdate of 45.3 and ammonium metavanadate 19.2.
The determination of the atomic ratios or the mass ratios of the oxides is carried out using the table below. 4 compositions of catalysts, both the ratio of metal atoms AV, and the mass ratio of metal oxides GV, use the following formulas:
100Msi02 2 xl mi
MI.
Gv
 2, t
msAB
msAB
where mi is the mass of the oxide component of the catalyst, while i means i is a metal from the group of Ti, Zr, V, W, Mo and Ce (g);
msAB is the mass of acid-activated bentonite, g;
xi is the number of metal atoms per unit formula of metal oxide I, g;
MI — molar mass of metal oxide, g / mol;
V is the content of SlOa acid-activated bentonite wt.%.
As follows from the presented examples, the method of catalytic reduction of the nitrogen oxide content in the exhaust flue gases according to the invention makes it possible to increase the degree of conversion.

权利要求:
Claims (10)
[1]
1. A catalyst for reducing the content of nitric oxide in the exhaust flue gases, containing one or more metal oxides selected from the group comprising titanium, zirconium, vanadium, tungsten, molybdenum, cerium in combination with a three-layer silicate, characterized in that enhancing the activity and selectivity of the catalyst, it contains a three-layer silicate, which: a) is an activated acid and in which the crystalline structure is partially preserved, which corresponds to 23 wt.% of silica extracted by soda solution; b) before activating the acid has a cation exchange capacity of 79 mg; c) by activating with acid, it has a 75% lower concentration of interlayer cations and a 3-fold increase in BET surface relative to the surface of the initial three-layer silicate, with an atomic ratio between the silicon contained in the acid-activated three-layer silicate and metals in oxides 0.23-20.18.
[2]
2. tzlizz Or according to claim 1, distinguished by the fact that “i the content of silicon dioxide is acidified in a three-layer sy. And ... te ne 2Y, 8% higher,“ it is in the original
si liqueur
[3]
3. Catechizer on PP. 1. Distinguished by the fact that it contains a metal oxide selected from the group including titanium, tungsten, vanadium in the following ratio of components, wt.%: Titanium oxide 20-80 was tungsten oxide 20, or oxide 5, the rest is activated with acid siliceous silicate.
[4]
l The catalyst PP. 1-2, differs 5 sh, and s. H in that it contains two metal oxides selected from the group including tm (en, tungsten, vanadium, cerium, circone, G, in the following ratio, wt.%: Oxides titanium and van 20–80 or oxides of tungsten and tungsten 20–80 or oxides of tungsten and vanadium 20, or oxides of cer; and vanadium 10, or oxides of zirconium and vanadium 10, the rest is activated by the acid three-layer silicate.
[5]
5 5. The catalyst according to claim 4, wherein the mass ratio between metal oxides is in the following ranges; vanadium oxide / titanium oxide 0.02 / whether tungsten oxide / titanium oxide
0 0.11 or vanadium oxide / tungsten oxide
 0.26 or o / vanadium / cerium oxide 0.33
or vanadium oxide / zirconium oxide 0.33.
[6]
6, Kashlizator on PP. 1-2, distinguishing and and with, that contains metal oxides
5 in one of the following ternary combinations, wt.%. oxides of titanium, tungsten and vanadium 20-80 or oxides of titanium, cerium and vanadium 20-80, or oxides of titanium, zirconium and vanadium 20-80, or oxides of tungsten, cerium and vanadium 20, or oxides of tungsten, zirconium and vanadium 20. or oxides of titanium, molybdenum and vanadium 20-50, the rest is an acid-activated three-layer silicate,
five
[7]
7. Catalyst according to claim 6, which is based on the fact that the mass ratio between metal oxides and the triune combination is in the following ranges: tungsten oxide / titanium oxide 0.055-0.225 and vanadium oxide / oxide titanium. 0.011-0.055, or cerium oxide / titanium oxide 0.065 and vanadium oxide / titanium oxide 0.021, or zirconium oxide / titanium oxide 0.065 and vanadium oxide / titanium oxide 0.022, or
5 cerium / tungsten oxide 0.286 and wa oxide: oxide / tungsten oxide — 0.143, or vanadium oxide / tungsten oxide — 0.143 and zirconium oxide / tungsten oxide, 0.286, or aznium oxide / titanium oxide, 0.03 and molybdenum oxide / titanium oxide.
[8]
8. Catalyst on PP. 1-7, about tl and h and yushi and the fact that it is made in the form of a molded rod,
[9]
9. A method for producing a catalyst for reducing the content of nitric oxide in waste flue gases by depositing metal oxides on a three-layer silicate from a solution containing one or more metal salts selected from the group including titanium, zirconium, vanadium, tungsten, molybdenum, cerium, followed by washing, shaping and calcining, characterized in that, with a chain of production of a catalyst with increased activity, silicate is used as a silicate, which: a) is an activated acid, in which a crystalline structure is stored, which corresponds to 23 wt.% silica extracted with a dilute solution; e soda, b) before activated acid has a cation exchange capacity of 79 MVaf / 100 r, c) by activating with acid an acid reduced by 75% the concentration of interlayer cations and 3 times the BET surface relative to the surface of the original three-layer silicate, with an atomic ratio between silicon contained in the acid-activated three-layer silicate and metals contained in the oxide oh, equal to 0.23-20.18, and the application is carried out by impregnating the silicate with a solution containing one or more salts of these metals.
[10]
10. A method of catalytic reduction of reducing the content of nitric oxide in flue gases containing nar. Sulfur oxides are also used with conventional components: by contacting the exhaust gas in the presence of reducing agents — ammonia with a catalyst containing one or more metal oxides selected from the group comprising titanium, zirconium, vanadium, tungsten, molybdenum, cerium, in combination with a three-layer silicate at a temperature of 200-600 ° C, preferably 250-430 ° C, at a space velocity of 500-2000 meters of exhaust gas for 1 hour and 1 l of catalyst, characterized in that, in order to increase the degree of conversion of nitrogen oxides, the catalyst chosen from groups Consisting of a catalyst containing the three-layer silicate which: a) is an activated acid and which partially retained crystalline structure that corresponds to 23% wt roll dioxide gkstrЈgirue- forward thrust with dilute.
soda, 6} before activating with acid, the cation-exchange capacity of 79 mg, c) by activating with acid, has a 75% lower concentration of interlayer cations and 3 times the BET surface relative to the surface of the initial three-layer silicate with an atomic ratio between the silicon contained in the activated acidic three-layer silicate, and metals contained in oxides, equal to 0.23–20.18, when the content of silica in acid-activated three-layer silicate is 28.8% higher than in the original silicon or a catalyst containing a metal oxide selected from the group comprising titanium, tungsten, vanadium, in the following ratio, wt.%: titanium oxide 20-80 or tungsten oxide 20,
0 or vanadium oxide 5, the rest of the acid-activated three-layer silicate or catalyst containing two metal oxide selected from the group comprising titanium, tungsten, vanadium, cerium, zirconium,
5 in the following ratio, wt.%: Oxides of titanium and vanadium-20-80 or oxides of titanium and tungsten 20-80, or oxides of tungsten and vanadium 20, or oxides of cerium and vanadium 10, or oxides of zirconium and
0 vanadium 10, the rest of the activated acid three-layer silicate, with the following mass ratio between metal oxides: vanadium oxide / titanium oxide 0.02 lsh tungsten oxide / titanium oxide 0.11,
5 or vakadi oxide / tungsten oxide 0.25, or vanadium oxide / cerium oxide 0.33 or vanadium oxide / zirconium oxide 0.33, or a catalyst containing metal oxides in one of the following ternary combinations, wt.%: Titanium oxides , tungsten and vanadium - 20-80 or oxides of titanium, cerium and vanadium - 20-80, or oxides of titanium, zirconium and vanadium - 20-80, or oxides of tungsten, cerium and vanadium - 20, or oxides
5 tungsten, zirconium and vanadium - 20, or oxides of titanium, molybdenum and vanadium - 20-50, the rest is activated by the acid three-layer silicate, with the following mass ratio between metal oxides and triple combination:
tungsten oxide / titanium oxide 0.058- 0.225 m vanadium oxide / titanium oxide 0.011- 0.055, or cerium oxide / titanium oxide 0.065, t vanadium oxide / titanium oxide 0.021, or
5 zirconium oxide / titanium oxide 0.065, and vanadium oxide / titanium oxide 0.022, or cerium oxide / tungsten oxide 0.286, and odanadium oxide / tungsten oxide 0.143, or vanadium oxides / aulfur oxide; 0.286,
or vanadium oxide / titanium oxide 0.03, and molybdenum oxide / titanium oxide 0.08, while the catalyst used is in the form of a molded rod.
Priority points:
13 08.85 to 1-3.8-10; 10.09,85 PP. 4-7.
Acid Activated Bentonite
Table 1
table 2
15V, (0.2), WOj (1,8), Ti04 (13),
Table 3
Activated with acid - 50 lot bentonite
Raw bentonite 50 (fuller's earth)
80
Activated with NajCCj bentonite 50
-thirty
Natural sour 50 clay
-80
Amorphous silica 50 acid
80
Activated with acid-100 bentonite
Crude bentonite 100 (fullrova earth)
Table 5
,five
, 2, 5
, 2
5, 2, 5
, 2, 5
.2
.S
1,3
4.5
1.8
4.5 1.3
4.5
1.8 4.5
1,3
45
18 45
IS
45 IS
45
13
45
13
92
34
53
60 31 37
68
94
26
93 77
59
64 38 90
76 95
43 61
24
92 66
58
59 38 86
65 92
47

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同族专利:

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公开号 | 公开日

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NO167849B|1991-09-09|

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DK384186D0|1986-08-12|

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DE3667248D1|1990-01-11|

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CA1268018A|1990-04-24|

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EP0212513A1|1987-03-04|

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DE3532226A1|1987-03-19|

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EP0212515A1|1987-03-04|

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CA1268165A|1990-04-24|

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NO863231L|1987-02-16|

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NO863231D0|1986-08-11|

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EP0212515B1|1989-09-13|

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US4720476A|1988-01-19|

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DK384186A|1987-02-14|

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JPH08196B2|1996-01-10|

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EP0213458A1|1987-03-11|

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DE3665412D1|1989-10-12|

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NO167849C|1991-12-18|

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US4722918A|1988-02-02|

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CA1267882A|1990-04-17|

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DE3665411D1|1989-10-12|

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EP0212513B1|1989-09-06|

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EP0213458B1|1989-12-06|

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DK166765B1|1993-07-12|

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US4719192A|1988-01-12|

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US4792439A|1988-12-20|

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法律状态:

优先权:

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申请号 | 申请日 | 专利标题

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DE19853529060|DE3529060A1|1985-08-13|1985-08-13|Catalyst for reducing the nitrogen oxide content of combustion gases|

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DE19853532226|DE3532226A1|1985-08-13|1985-09-10|CATALYST FOR REDUCING THE NITROGEN OXIDE CONTENT OF COMBUSTION EXHAUST GASES|

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