CN1108849C - Process for removing nitrogen oxide - Google Patents
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- CN1108849C CN1108849C CN99109302A CN99109302A CN1108849C CN 1108849 C CN1108849 C CN 1108849C CN 99109302 A CN99109302 A CN 99109302A CN 99109302 A CN99109302 A CN 99109302A CN 1108849 C CN1108849 C CN 1108849C
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Abstract
The present invention relates to a method for eliminating oxynitride. The method comprises: reaction raw materials containing nitrogen oxides contact a catalyst, the catalyst contains ZSM-5 zeolite and porous metal composite materials, and the composite materials contain porous metal carriers and ZSM-5 zeolite directly crystallized on the porous metal carrier. The porous metal carriers at least contain one porous nickel-aluminum, iron-aluminum or copper-aluminum alloy.
Description
The invention relates to a kind of chemical purification method of nitrogen compound, more specifically say so about a kind of removal methods of nitrogen oxide.
As everyone knows, the whole world has 30,000,000 tons nitrogen oxide (NO every year approximately
X) be discharged in the atmosphere, one of reason that forms photochemical fog and acid rain is not only in the discharging of oxides of nitrogen gas, also ozone layer is had destruction.At present, the concentration of nitrogen oxide in atmosphere is seriously endangering the environment of human survival just with the speed increase in every year 0.2～0.3%.
The ZSM-5 zeolite of metal ion exchanged is the denitrifying oxide catalyst of developing in recent years of new generation.
US5,364,606 disclose a kind of from air-flow selective reduction NO
XMethod, this method comprises provides a kind of flow reactor, and a kind of zeolite catalyst that contains zinc (and copper) ion of packing in reactor is introduced methane and described air-flow in the reactor, under catalyst action, make the reaction of methane and described air-flow, with the NO in the reduction air-flow
X
The ZSM-5 zeolite of metal ion exchanged has good decompose nitrogen oxides activity, yet its heat, hydrothermal stability and activity stability are relatively poor, as practical environmental protection catalyst, also has the deficiency of difficult forming.
People (Microporous and Mesoporous Materials 21,549～555,1998) such as Kenji Yamada contrast to the catalytic performance of Cu-ZSM-5 and Fe-ZSM-5, and the result shows, at reaction temperature 523～773K, and SV=5000 hour
-1Condition under, contain N with Cu-ZSM-5 and Fe-ZSM-5 catalytic reduction
2O 500ppm, C
3H
60～1000ppm, O
20～5 body %, H
2N in the mixed atmosphere of O 0～10 body % and surplus helium
2O is not having C
3H
6Under the situation of reducing agent, the activity of Cu-ZSM-5 is higher than the activity of Fe-ZSM-5, and C is being arranged
3H
6The situation of reducing agent is next just in time opposite.
Among the Catalysis Today 26,99～128,1995, the CuZSM-5 zeolite is contained NO 300ppm, CO 300ppm, C as in the nitrogen
3H
6800ppm, O
25%, H
2O 10%, CO
213% atmosphere take off the nitric oxide catalyst, be that the nitric oxide conversion ratio reaches maximum (about 40%) at about about 425 ℃ under the condition of 120 liters/hour/gram in air speed.Yet as the 102nd page of this article was described, existing C uZSM-5 zeolite catalyst was very unstable in containing the atmosphere of water vapour, and the water vapour less than 2% in the reaction raw materials will have a strong impact on its activity stability.Because it is very big to be rich in water vapour (10～16%) and its air speed in the engine exhaust, is difficult to the imagination and from the waste gas of so big air speed, isolates so a large amount of water vapour in advance.Therefore, this article points out that the researcher should be primarily focused on a kind of more complicated catalyst for the 103rd page, and this catalyst can keep stability for a long time in so moistening environment.
Journal of catalysis 157,603～610,1995 and Zeolites 13,602～606,1993 result of study shows, the CuZSM-5 zeolite has relatively poor heat and hydrothermal stability, and high-temperature heat treatment or hydrothermal treatment consists can cause that all the zeolite dealuminzation causes zeolite structured destruction, thereby causes forfeiture of acid position and Cu on the zeolite
2+Assemble, make catalysqt deactivation.
The aluminosilicate zeolite in-situ crystallization is prepared the composite that contains zeolite become a very active research field on porous carrier.These composites that contain zeolite are formed according to it and preparation method different have different character and purposes.
US3,244,643 disclose a kind of method that alumino-silicate is loaded on the solid cage shape carrier with certain porosity and effective bore dia.US3,730,910 disclose a kind of with zeolite-loaded method on Si oxide and/or aluminum oxide.US4,511,667 disclose a kind of zeolite-asbestos composite and preparation method thereof.US4,800,187 disclose a kind of with the method for zeolite crystallization on monolithic ceramic matrix.US5,019,263 discloses the molecular screen membrane that a kind of zeolite and imporosity matrix composite form.EP0,511,739A1 discloses the zeolite crystal film of a kind of crystallization on porous matrix.WO93/17781 discloses a kind of method for preparing molecular screen membrane.WO93/19840 discloses a kind of method for preparing zeolite membrane on the porous carrier that zeolite is deposited on.
The report of composite that the aluminosilicate zeolite in-situ crystallization is prepared into zeolite and metal on metal material is also a lot.
US4,578,372 disclose the method for a kind of zeolite layer of preparation on a kind of matrix that is different from zeolite at crystal structure, this method comprises this matrix is contacted with a kind of reactant mixture that can form zeolite, add thermal reaction mixture and make it to form zeolite, in heating process, this matrix is rolled in reactant mixture zeolite is preferentially generated on stromal surface.Wherein said " zeolite " not only comprise zeolite that alumino-silicate forms, also comprise low aluminium or be substantially free of aluminium, have zeolite structured silicate, and the four-coordination aluminium in zeolite structured is by one or more elements, as the analog of the alumino-silicate that gallium, boron or iron replaced.Described zeolite can be y-type zeolite, A type zeolite, zeolite L, modenite, omega zeolite or ZSM-5 zeolite.Described matrix can be metal or nonmetal, and described metal also can be the metal material of sintering as being aluminium, iron, steel, stainless steel, nickel or titanium.Preferred matrix is magnetizable matrix, particularly magnetizable particle.The zeolite that obtains and the composition of matrix can be used as adsorbent in magnetic stablizing bed.
EP0,481,658A1 discloses a kind of method that deposits zeolitic material on a kind of porous carrier, this method comprises that the energy crystallization is immersed at least one surface of porous carrier to be become in the synthesized gel rubber of crystalline zeolite section bar material, make described gel crystallization and make zeolite type material crystallization on described carrier, wherein, the specific surface of described carrier comprises the coating surface of nickel, cobalt or a molybdenum or oxide form.Suitable porous carrier materials can be a kind of porous metals, pottery, ceramal, glass, mineral, carbon, polymer etc., typical metal such as stainless steel, inconel etc., adopt this method can prepare the molecular screen membrane that a kind of length and width are far longer than thickness, this molecular screen membrane mesolite section bar material directly contact also direct and carrier keyed jointing with the surface of carrier, though it be unclear that need not any bonding agent between (may be chemical bond and/secondary or physical bond) zeolite and the carrier for the character of this key.
EP0,481,659A1 discloses the another kind of method that deposits a kind of zeolite type material on Lacunaris metal carrier, this method comprises that at least one surface impregnation with Lacunaris metal carrier can crystallization become in the gel of crystalline zeolite section bar material, make described gel crystallization so that zeolite type material crystallization on carrier, wherein, in being immersed in gel before, with the surface of acid treatment metallic carrier.The molecular screen membrane and the EP0 that adopt this method to prepare, the molecular screen membrane of 481658A1 preparation has close character.
EP0,481,660A1 discloses a kind of molecular screen membrane, it contains the crystal of the zeolite type material that loads on the porous carrier, wherein, the zeolite type material crystals is grown on the hole of carrier basically continuously, and this zeolite type material direct crystallization is also direct and carrier keyed jointing on carrier.
Also there are some composites to be used as the catalyst of denitrifying oxide in the prior art.
People such as J.C.Jansen (Proceedings of the 9th International ZeoliteConference, Eds.R.von Ballmoos et al.PP247～254, Montreal, 1992) metallic carriers such as aluminium flake, aluminium sheet, nickel plate, copper coin, titanium plate or stainless (steel) wire are used earlier the ethanol washes clean; Be placed on again in the withstand voltage still of teflon lined, add synthetic liquid, make zeolite crystallization on metallic carrier, form a kind of zeolite membrane of the MFI of having structure, demonstrate stronger keyed jointing power between zeolite membrane and carrier.
People such as H.P.Calis (The Canadian Journal of Chemical EngineeringVolume 73, PP119～128, February 1995) adopt the described method of people such as J.C.Jansen to prepare a kind of zeolite membrane that loads on the stainless (steel) wire, with the zeolite membrane that obtains 500 ℃ of roastings after 10 hours, exchange with the Schweinfurt green aqueous solution, at last 100 ℃ of dryings, must contain 96.5 heavy % stainless (steel) wires, 3.5 the catalyst of heavy %ZSM-5 zeolite and 0.1 heavy % copper, the activity of this catalyst denitrifying oxide is much higher than commercial widely used amorphous V-Ti/SiO
2Catalyst.
People such as E.Ito (Catalysis Today 27,123～128,1996) spend the night tetraethyl-metasilicate, sodium aluminate, TPAOH and deionized water mixing after vibration and prepare a kind of colloid.Stainless steel wire is put into autoclave with O for toluene and dry back with above-mentioned colloid under the boiling condition, obtained the ZSM-5/ stainless steel composite material in 4.5 hours in 180 ℃ of heating, submit at the ZSM-5/ stainless steel composite material that obtains and to change cerium ion, obtain a kind of catalyst.This catalyst can be used as under the excess oxygen, makes the denitrifying oxide process of reducing agent with ammonia.
As previously mentioned, heat, hydro-thermal and the activity stability of the ZSM-5 zeolite of metal ion exchanged are relatively poor, framework dealumination particularly easily takes place under hydrothermal condition, generally speaking, the ZSM-5 zeolite of metal ion exchanged is being carried out hydrothermal treatment consists more than 550 ℃, framework dealumination will take place, and this has limited the application of this catalyst in the reaction of moisture vapor atmosphere.
On the other hand, though disclose the composite of many kinds of zeolites and (porous) metal in the prior art, according to its description, in the composite of some zeolite and (porous) metal, the keyed jointing that also has certain form between zeolite and the metallic carrier, but existing zeolite but fails to solve the problem that framework dealumination easily takes place zeolite with the composite of (porous) metal.Simultaneously, in the composite of existing zeolite and (porous) metal, the firmness that combines between zeolite and the carrier is still undesirable, this also makes existing zeolite less with the load capacity of the composite mesolite of (porous) metal, just on carrier, form a kind of very thin zeolite membrane (or claiming coating), can more have a strong impact on its firmness as zeolite membrane is too thick, thereby, existing zeolite is general only as adsorbent or separation membrane with the composite of (porous) metal, when as catalysis material, effect is undesirable.
The objective of the invention is to overcome the above-mentioned shortcoming of existing removal of nitrogen oxide method, a kind of method new, that can more effectively remove nitrogen oxide is provided.
Method provided by the invention is included under the condition of denitrifying oxide, the reaction raw materials of nitrogen-containing oxide is contacted with a kind of catalyst, wherein, described catalyst contains a kind of ZSM-5 zeolite and porous metal composite material, this composite contains Lacunaris metal carrier and the ZSM-5 zeolite of direct crystallization on this Lacunaris metal carrier, and described Lacunaris metal carrier contains a kind of nickel porous-aluminium, iron-aluminium or copper-aluminium alloy at least.
In method catalyst system therefor provided by the invention, Lacunaris metal carrier in the described composite can be nickel porous-aluminium, iron-aluminium or copper-aluminium alloy itself, also can be the Lacunaris metal carrier that outer surface and/or inner surface contain one deck nickel porous-aluminium, iron-aluminium or copper-aluminium alloy.
When described metallic carrier is nickel porous-aluminium, iron-aluminium or copper-aluminium alloy itself, contain typical ZSM-5 zeolite diffraction maximum and skeleton nickel, iron or copper diffraction maximum in the x-ray diffraction spectra of described catalyst.For example, when Lacunaris metal carrier is nickel porous-aluminium alloy, described catalyst has main X-ray diffract spectral line as shown in table 1, when Lacunaris metal carrier is porous iron-aluminium alloy, described catalyst has main X-ray diffract spectral line as shown in table 2, when Lacunaris metal carrier was porous copper-aluminium alloy, described catalyst had main X-ray diffract spectral line as shown in table 3.Table 1
Table 2
Table 3
| The d value, dust | Relative intensity |
| 11.20 | 15～35 |
| 9.95 | 15～30 |
| 3.84 | 30～70 |
| 3.72 | 10～30 |
| 3.63 | 5～15 |
| 2.41 | 80～95 |
| 2.08 | 100 |
| The d value, dust | Relative intensity |
| 11.20 | 15～35 |
| 9.95 | 15～30 |
| 3.84 | 30～70 |
| 3.72 | 10～30 |
| 3.63 | 5～15 |
| 2.53 | 100 |
| 2.32 | 80～95 |
| The d value, dust | Relative intensity |
| 11.20 | 15～35 |
| 9.95 | 15～30 |
| 3.84 | 30～70 |
| 3.72 | 10～30 |
| 3.63 | 5～15 |
| 2.50 | 100 |
When porous carrier materials is that outer surface and/or inner surface are when containing the Lacunaris metal carrier of one deck nickel porous-aluminium, iron-aluminium or copper-aluminium alloy, part beyond nickel porous-aluminium, iron-aluminium or the copper-aluminium alloy can be metallic nickel, iron, copper or wherein two or three alloy, it can be a different shape, as graininess, Powdered, netted, bar-shaped, spherical, sheet, bulk, tubulose, cellular, strip etc.It is different and change to utilize the XRD spectra of the catalyst that this Lacunaris metal carrier is prepared into to look nickel porous-aluminium, iron-aluminium or copper-aluminium alloy and the content of ZSM-5 zeolite in catalyst.When nickel porous-aluminium, iron-aluminium or copper-aluminium alloy and the content of ZSM-5 zeolite in composite are big, it can have the main X-ray diffract spectral line shown in table 1, table 2 and/or table 3 respectively, otherwise, content in composite too hour when nickel porous-aluminium, iron-aluminium or copper-aluminium alloy content and ZSM-5 zeolite, the X-ray diffractometer will detect the diffraction maximum less than ZSM-5 zeolite and skeleton nickel, iron and/or copper, only occur the diffract spectral line of metallic nickel, iron and/or copper in its x-ray diffraction spectra.
According to method provided by the invention, be benchmark with nickel porous-aluminium, iron-aluminium or copper-aluminium alloy, specific surface is greater than 5 meters
2/ gram is preferably greater than 10 meters
2/ gram, pore volume are greater than 0.05 milliliter/gram, and the Lacunaris metal carrier that is preferably greater than 0.07 milliliter/gram is preferred Lacunaris metal carrier.
According to method provided by the invention, described zeolite can in-situ crystallization on the surface of nickel porous-aluminium, iron-aluminium or copper-aluminium alloy carrier (as shown in Figure 2), also can in-situ crystallization in the hole of nickel porous-aluminium, iron-aluminium or copper-aluminium alloy carrier (as shown in Figure 3 and Figure 4) or the two have both at the same time.
According to method provided by the invention, the framework si-al ratio of ZSM-5 zeolite in the described catalyst (sial atomic ratio) is more than 15, and the diverse location in a certain composite can have different framework si-al ratios.The framework aluminum of described ZSM-5 zeolite can be partly or entirely from aluminium contained in nickel porous-aluminium, iron-aluminium or the copper-aluminium alloy.
According to method provided by the invention, described catalyst contains described composite, gross weight with nickel porous-aluminium, iron-aluminium or copper-aluminium alloy and zeolite is a benchmark, the content of nickel, iron or copper preferred 25～95 heavy % in the composite, the content of aluminium preferred 0.1～10 heavy %, the content of silicon preferred 3～40 heavy %.When described Lacunaris metal carrier is nickel porous-aluminium, iron-aluminium or copper-aluminium alloy itself, the content of nickel, iron or copper more preferred 35～85 heavy % in the composite, the content of aluminium more preferred 0.1～5 heavy %, the content of silicon more preferred 5～30 heavy %.
According to method provided by the invention, described catalyst can also contain metal ion, and described metal ion is selected from one or more in IB family, IIB family, IIIB family and the group VIII metal ion.Wherein, described I B-group metal ion preferably copper ion; The preferred zinc ion of described IIB family's metal ion; The preferred lanthanide metal ion of described IIIB family's metal ion, more preferred lanthanum ion, cerium ion and/or mainly contain the mixing lanthanide metal ion of lanthanum ion and/or cerium ion; Described group VIII metal ion can be iron, cobalt, nickel, ruthenium, rhodium, palladium, osmium, iridium, platinum ion, one or more in preferred iron, cobalt, the nickel ion.
When described catalyst contains metal ion, gross weight with nickel porous-aluminium, iron-aluminium or copper-aluminium alloy, zeolite and metal oxide is a benchmark, the content of nickel, iron or copper preferred 25～95 heavy % in the catalyst, more preferred 35～85 heavy %, aluminium content preferred 0.1～10 heavy %, more preferred 0.1～5.0 heavy %, silicone content preferred 3～40 heavy %, more preferred 5～30 heavy %, the content of metal ion preferred 0.1～10 heavy %, more preferred 0.1～5 heavy %.
In the method provided by the invention, described Preparation of catalysts method comprises the synthetic liquid of a kind of Lacunaris metal carrier and a kind of zeolite is contacted, and making the synthetic liquid of zeolite crystallization under the crystallization condition of synthetic ZSM-5 zeolite, described Lacunaris metal carrier contains a kind of nickel porous-aluminium, iron-aluminium or copper-aluminium alloy at least.
The concrete preparation process of described catalyst is as follows:
(1) preparation of Lacunaris metal carrier.
At least the precursor that contains the Lacunaris metal carrier of a kind of nickel-aluminium, iron-aluminium or copper-aluminium alloy is handled with sodium hydroxide solution,, be prepared into the Lacunaris metal carrier that contains a kind of nickel-aluminium, iron-aluminium or copper-aluminium alloy at least to remove part aluminium wherein.In the weight of nickel-aluminium, iron-aluminium or copper-aluminium alloy, aluminum content can be 10～70 heavy % in the described precursor, and aluminium content should drop to 0.1～20 heavy % in the Lacunaris metal carrier that forms behind the dealuminzation, and the specific surface of this Lacunaris metal carrier should be greater than 5 meters
2/ gram is more preferably greater than 10 meters
2/ gram, pore volume should be greater than 0.05 milliliter/gram, more preferably greater than 0.07 milliliter/gram.
Wherein the concentration of sodium hydroxide solution can change in a big way, as can change the scope of more preferred 1～8 mol in the scope of 0.5～10 mol.With naoh treatment nickeliferous-temperature of the precursor of the Lacunaris metal carrier of aluminium, iron-aluminium or copper-aluminium alloy can and give the amount that removes aluminium according to concentration, the consumption of sodium hydroxide solution and change,, large usage quantity higher when concentration of sodium hydroxide solution, give remove aluminium amount hour, treatment temperature can be lower, otherwise, can be higher, treatment temperature generally changes in 30～250 ℃ of scopes, more preferred 50～200 ℃.Handling the pressure of nickeliferous-aluminium, iron-aluminium or copper-aluminium alloy precursor with sodium hydroxide solution can be at normal pressure, be higher than normal pressure or be lower than under the normal pressure and carry out.The consumption of sodium hydroxide solution can change according to giving the amount that removes aluminium, and when giving the amount that removes aluminium big, the consumption of sodium hydroxide solution should be bigger, otherwise should be less, in general, is benchmark to give the aluminium that removes, and sodium hydroxide solution should be excessive.The time of handling can be according to the height of concentration of sodium hydroxide solution, consumption, treatment temperature, give the amount that removes aluminium changes, in general, the time of handling can 0.5 hour to hundreds of hour, preferred 1～70 hour, also available other solubility highly basic of described NaOH replaced.
Described Lacunaris metal carrier can be purchased and obtain, and can use existing Raney nickel (Raney Ni) as nickel porous-aluminium alloy.
When the Lacunaris metal carrier material is when containing the Lacunaris metal carrier of one deck nickel porous-aluminium, iron-aluminium or copper-aluminium alloy on the surface, this carrier can prepare with the following method: evaporation last layer aluminium on the nickel of arbitrary shape, iron, copper metallic face, under inert gas atmosphere, heating was gone up its surface and is formed one deck nickel-aluminium, copper-aluminium or iron-aluminium alloy, handles this surface with sodium hydroxide solution as stated above again more than 0.5 hour more than 800 ℃.
(2) contain the preparation of ZSM-5 Zeolite composite materials.
The quantitative Lacunaris metal carrier that contains nickel porous-aluminium, iron-aluminium or copper-aluminium alloy is joined in the withstand voltage still, add the synthetic liquid of quantitative zeolite, crystallization in confined conditions heats up, spend the deionised water solid product to neutral, dry, roasting gets ZSM-5 zeolite provided by the invention and porous metal composite material.
Wherein, the compositing range of the synthetic liquid of described zeolite is identical with the compositing range of the synthetic liquid of zeolite of conventional synthetic ZSM-5 zeolite, and for example, the synthetic liquid of described zeolite can have following mol ratio and form: SiO
2/ Al
2O
3＞20, Na
2O/SiO
2=0.03～2, template agent/SiO
2=0.03～1.5, H
2O/SiO
2=3～200.The synthetic preferred mol ratio of liquid of described zeolite consists of: SiO
2/ Al
2O
3＞50, Na
2O/SiO
2=0.03～0.5, template agent/SiO
2=0.03～0.5, H
2O/SiO
2=15～200.Described template agent can be selected from the ZSM-5 zeolite synthetic in template agent commonly used, can be selected from various water-soluble amines, ammonium salt, quarternary ammonium salt or alkali as it, preferred tetraethyl ammonium hydroxide (TEA), TPAOH (TPA), n-propylamine or n-butylamine.The weight ratio of synthetic liquid of zeolite and Lacunaris metal carrier can in very large range change this weight ratio preferred 5～100, more preferred 10～50.
The condition of described crystallization can adopt the conventional crystallization condition of synthetic ZSM-5 zeolite.Can be 100～200 ℃ as crystallization temperature, preferred 140～200 ℃, crystallization time can be several hours to several days, preferred 10～120 hours, and more preferred 30～100 hours.
Described drying and roasting can be adopted conventional method, and wherein the purpose of roasting is for removing the template agent in the composite, and sintering temperature can be 450～650 ℃, roasting time 2～20 hours.
(3) Preparation of catalysts.
With the solution exchange that contains ammonium ion, make in the composite sodium oxide content ZSM-5 zeolite that obtains and porous metal composite material less than 1 heavy %, and with at least a processing ZSM-5 zeolite and porous metal composite material in the following method.
Method 1: contain inert gas or contain inert gas and the atmosphere of oxygen in, handled at least 0.5 hour under greater than 650 ℃ to 1000 ℃ temperature.
Wherein, described inert gas comprises one or more in helium, argon gas, xenon, nitrogen, the carbon dioxide, is preferably nitrogen and/or carbon dioxide.The described preferred air of atmosphere that contains inert gas and oxygen.Described contain inert gas or contain inert gas and the atmosphere of oxygen in handle preferred 700～900 ℃ of the temperature of composite, the processing time can be very long, as can being several thousand hours even longer, but is energy savings, preferred 1～10 hour of processing time.
Method 2: in containing water vapor atmosphere, under 400～700 ℃ temperature, handled at least 0.5 hour.
Wherein, described containing water vapor atmosphere comprises the gaseous mixture of one or more and steam in 100% steam and inert gas and the oxygen.The content of steam should be preferably greater than 5 body % greater than 1 body % in the gaseous mixture.Preferred 450～600 ℃ of the described temperature of handling composite in containing water vapor atmosphere, the processing time can be very long, as can being several thousand hours even longer, but is energy savings, preferred 1～10 hour of processing time.
Method 3: one or more in ZSM-5 zeolite that obtains and porous metal composite material in introducing IB family, IIB family, IIIB family and the group VIII metal ion, drying and/or roasting.
Wherein, the method for introducing IB family, IIB family, IIIB family and group VIII metal ion can adopt conventional method, as adopting ion-exchange or infusion process.
According to method provided by the invention, can contain reducing agent in the reaction raw materials of described nitrogen-containing oxide and also can not contain reducing agent.Can also contain the oxygen that is not higher than 20 body % in the atmosphere of described nitrogen-containing oxide, be not higher than the water vapour of 30 body %, be not higher than the sulfur oxide of 10000ppm etc.The reaction raw materials of described nitrogen-containing oxide can be an industrial waste gas, as the waste gas of nitric acid industry, the waste gas that produces when catalytic cracking catalyst is regenerated etc.The reaction raw materials of described nitrogen-containing oxide also can be various diesel oil or petrolic tail gas.
Under the preferable case, the reaction raw materials of described nitrogen-containing oxide contains at least a reducing agent, and described reducing agent refers to anyly have the gas of reproducibility or can change in the material of gas of reproducibility one or more under reaction condition.Wherein, preferred reducing agent is selected from hydrogen, ammonia, carbon monoxide, has the hydro carbons of 1～10 carbon atom.More preferred reducing agent is selected from ammonia, carbon monoxide, have 1～10 carbon atom alkane, have 1～10 carbon atom alkene and two or more mixture wherein.The volume ratio of described reducing agent and nitrogen oxide is preferably more than 0.01, and is more preferred more than 0.1, and preferably 0.2～50.
According to method provided by the invention, described nitrogen oxide is selected from one or more in nitric oxide, nitrous oxide, nitrogen dioxide and their mixture.
According to method provided by the invention, the condition of described denitrifying oxide comprises that reaction temperature is 100～600 ℃, is preferably 200～550 ℃; Reaction pressure can be normal pressure, be lower than normal pressure or be higher than normal pressure, be preferably normal pressure; The gas volume air speed is not for being higher than 10
10Hour
-1, preferred 10～10
8Hour
-1
The catalyst that method provided by the invention adopted is a kind of novel catalyst, and in the catalyst, the ZSM-5 zeolite is more firm with combining of Lacunaris metal carrier, and therefore, catalyst has longer service life.For example, to handle 10 hours with the argon gas that contains 3 heavy % water or roasting 10 hours or handled 1000 hours with argon gas at 400 ℃ in 900 ℃ of air at 600 ℃ respectively according to the catalyst that contains ZSM-5 zeolite and Lacunaris metal carrier of method provided by the invention used nickeliferous or iron 40.3～92.7 heavy %, silicon 3.1～27.0 heavy %, nickel, iron or copper ion 0.4～3.0 heavy %, the weight loss of the catalyst after the processing has only 0.1～0.7 heavy %.And, handled the existing CuZSM-5/ stainless steel catalyst that contains stainless steel 94.5 heavy %, silicon 2.4 heavy %, copper ion 0.3 heavy % 10 hours with the argon gas that contains 3 heavy % water at 600 ℃, the weight loss of the CuZSM-5/ stainless steel catalyst after the processing reaches 4.1 heavy %.It should be noted that silicone content (zeolite content) in the method catalyst system therefor provided by the invention far above CuZSM-5/ stainless steel catalyst, if when CuZSM-5/ stainless steel catalyst contains so high zeolite, its firm degree will be lower.
In the method catalyst system therefor provided by the invention, the framework aluminum of ZSM-5 zeolite is highly stable, has higher heat, hydrothermal stability, and this is that prior art is incomparable.For example, the catalyst that contains ZSM-5 zeolite and Lacunaris metal carrier of nickeliferous 78.5 heavy %, aluminium 1.0 heavy % that method provided by the invention is used, silicon 9.1 heavy %, copper ion 1.1 heavy % at 600 ℃ with containing 3 heavy %H
2The argon gas of O was handled after 10 hours, the ratio of catalyst mesolite framework aluminum and non-framework aluminum does not change before and after handling, and under the same conditions, the CuZSM-5 zeolite being carried out hydrothermal treatment consists, the ratio of framework aluminum and non-framework aluminum reduces significantly in the CuZSM-5 zeolite after the processing.
Moreover, catalyst provided by the invention also has higher activity stability, show that catalyst provided by the invention has higher catalytic activity after heat treatment or hydrothermal treatment consists, and existing CuZSM-5 zeolite catalyst its catalytic activity after heat or hydrothermal treatment consists descends significantly.For example, with method provided by the invention used nickeliferous 78.5 heavy %, aluminium 1.0 heavy %, silicon 9.1 heavy %, the roasting 10 hours under 900 ℃ of air atmospheres respectively of the catalyst that contains ZSM-5 zeolite and Lacunaris metal carrier of copper 1.1 heavy %, or at 600 ℃ with the argon gas hydrothermal treatment consists that contains 3 heavy % water after 10 hours, be used separately as together with fresh catalyst and take off nitric oxide production catalyst under the different temperatures, the result shows, catalyst after the hydrothermal treatment consists is compared with fresh catalyst, when being higher than 550 ℃, reaction temperature has higher catalytic activity, catalyst is after heat treatment compared with fresh catalyst, all has higher catalytic activity under each reaction temperature.This has very important significance for the denitrifying oxide catalyst that uses under high temperature or high temperature moisture vapor atmosphere.
Method catalyst system therefor provided by the invention has higher activity stability and shows that also it has the long-life.For example, with the used copper ions 0.4 heavy % of method provided by the invention, iron 92.7 heavy %, aluminium 0.4 heavy %, silicon 3.1 heavy %, oxygen 3.4 heavy %, with porous iron-aluminium alloy/iron net is that catalyst that carrier contains the ZSM-5 zeolite is when being used to take off the nitric oxide reaction, have only 100 milligrams in the catalyst loading amount, 300 ℃ of reaction temperatures, gas (consists of NO500ppm, NH
3500ppm, O
2O.9 heavy %, all the other are argon gas) volume space velocity is 7.2 * 10
4Hour
-1Condition under, react 1000 hours rear catalyst activity and do not fall as follows.
In addition, method catalyst system therefor provided by the invention also has higher sulfur resistance.Because often contain sulfur oxide in the waste gas of nitrogen-containing oxide, this performance of method catalyst system therefor provided by the invention makes method provided by the invention have more practical meaning.
Because the present invention has used this novel catalyst system, makes method provided by the invention have higher transformation efficiency of the oxides of nitrogen and longer service cycle.
Method provided by the invention can adapt to various reaction raw materials, can contain oxygen, water vapour, sulfur oxide etc. in the reaction raw materials, and therefore, method provided by the invention has more wide prospect in industrial application.
Fig. 1 is the stereoscan photograph of porous iron-aluminium alloy in the method catalyst system therefor provided by the invention;
Fig. 2～5th, the transmission electron microscope photo of method catalyst system therefor provided by the invention;
Fig. 6 is the stereoscan photograph of method catalyst system therefor provided by the invention;
Fig. 7 is the transmission electron microscope photo of method catalyst system therefor provided by the invention;
Fig. 8 is the Al2P XPS spectrum figure of the catalyst before the used hydrothermal treatment consists of method provided by the invention;
Fig. 9 is the Al2P XPS spectrum figure of the catalyst after the used hydrothermal treatment consists of method provided by the invention;
Figure 10 is the Al2P XPS spectrum figure of CuZSM-5 zeolite catalyst before the hydrothermal treatment consists;
Figure 11 is the Al2P XPS spectrum figure of CuZSM-5 zeolite catalyst after the hydrothermal treatment consists;
Figure 12 is the profile diagram of Fig. 5;
Figure 13 makes reducing agent with ammonia, adopt method provided by the invention used fresh, when the catalyst of 900 ℃ of heat treatments and 600 ℃ of hydrothermal treatment consists, the nitric oxide conversion ratio is with the variation diagram of reaction temperature;
Figure 14 makes reducing agent with ammonia, adopt fresh, through the CuZSM-5 zeolite of 900 ℃ of heat treatments and 600 ℃ of hydrothermal treatment consists when taking off the nitric oxide catalyst for reaction nitric oxide conversion ratio with the variation diagram of reaction temperature;
Figure 15 makes reducing agent with ammonia, and method nitric oxide conversion ratio provided by the invention is with the variation diagram in reaction time;
Figure 16 makes reducing agent with ammonia, and the nitric oxide conversion ratio is with the variation diagram of reaction temperature when adopting different catalysts;
Figure 17 makes reducing agent with ammonia, and the nitric oxide conversion ratio is with the variation diagram of reaction temperature when adopting different catalysts;
Figure 18 makes reducing agent with ammonia, and the nitric oxide conversion ratio is with the variation diagram of reaction temperature when adopting the catalyst of the used fresh and 550 ℃ of hydrothermal treatment consists of method provided by the invention;
Figure 19 makes reducing agent with ammonia, and the nitric oxide conversion ratio is with the variation diagram of reaction temperature when adopting the Fe-ZSM-5 catalyst of fresh and 550 ℃ of hydrothermal treatment consists;
Figure 20 makes reducing agent with ammonia, and the nitric oxide conversion ratio is with the variation diagram of reaction temperature when adopting the catalyst of the used fresh and 600 ℃ of hydrothermal treatment consists of method provided by the invention;
Figure 21 makes reducing agent with ammonia, and the nitric oxide conversion ratio is with the variation diagram of reaction temperature when adopting the Fe-ZSM-5 catalyst of fresh and 600 ℃ of hydrothermal treatment consists;
Figure 22 makes reducing agent with ammonia, and method nitric oxide conversion ratio provided by the invention is with the variation diagram in reaction time;
Figure 23 makes reducing agent with ammonia, and the nitric oxide conversion ratio is with the variation diagram in reaction time when adopting Fe-ZSM-5 to make catalyst;
Figure 24 makes reducing agent with carbon monoxide, and when adopting different catalysts, the nitric oxide conversion ratio is with the variation diagram of reaction temperature;
Figure 25 makes reducing agent with carbon monoxide, contains SO in the raw material
2, when adopting different catalysts, the nitric oxide conversion ratio is with the variation diagram in reaction time;
Figure 26 makes reducing agent with alkane, and when adopting different catalysts, the nitric oxide conversion ratio is with the variation diagram in reaction time.
The following examples will the present invention will be further described.
Example 1～4
Following example illustrates the preparation of Lacunaris metal carrier in the method catalyst system therefor provided by the invention.
Take by weighing 2.0 kilograms of iron (iron content 99.99 heavy % respectively, Shoudu Iron and Steel Co. produces) or copper (cupric 99.99 heavy %, produce in the copper work, Luoyang), fusion in intermediate frequency furnace, add 2.0 kilograms of aluminium (contain the heavy % of aluminium 99.99, Zhengzhou Aluminium Plant produces) respectively, in 1200 ℃ of constant temperature 10 minutes, naturally cool to room temperature, obtain bulk iron-aluminium or copper-aluminium alloy.Respectively iron-aluminium, the copper-Al alloy powder that obtains is broken into the particle of about 0.01 centimetre of diameter.
Take by weighing nickel-aluminum alloy granule (nickeliferous and each 50 heavy % of aluminium respectively; about 0.01 centimetre of particle diameter; Shanghai chemical reagents corporation produces); each 200 gram of iron-alumina particles and copper-aluminum alloy granule; at room temperature add the sodium hydrate aqueous solution that quantitative concentration is 6 mol respectively; heat temperature raising to 90 or 180 ℃; constant temperature is taken out the aluminium regular hour; filter; spend the deionised water solid particle to neutral, get the used Lacunaris metal carrier nickel porous of the present invention-aluminium alloy RNA, porous iron-aluminium alloy RFA1 and RFA2 and porous copper-aluminium alloy RCA.Amplify 2600 times RFA1 stereoscan photograph as shown in Figure 1.
Table 4 has provided the concentration and the consumption of used alloy, sodium hydroxide solution, the numbering of taking out aluminium temperature and time and gained Lacunaris metal carrier, aluminum content, BET specific surface and pore volume.Wherein, aluminium content adopts plasma emission spectrometry (ICP) to measure, and BET specific surface and pore volume adopt low-temperature nitrogen adsorption method to measure.Stereoscan photograph obtains on Hittach 4000 type ESEMs.
Table 4
| Example number | Used alloy | NaOH solution | Take out the aluminium temperature and time | Lacunaris metal carrier | |||||
| Concentration, mol | Consumption, milliliter | Temperature, ℃ | Time, hour | Numbering | Aluminium content, heavy % | Specific surface, rice 2/ gram | Pore volume, milliliter/gram | ||
| 1 | Nickel-aluminium | 6 | 1000 | 180 | 48 | RNA | 1.20 | 12.5 | 0.12 |
| 2 | Iron-aluminium | 6 | 1000 | 90 | 3 | RFA1 | 7.15 | 90.6 | 0.14 |
| 3 | Iron-aluminium | 3 | 1500 | 180 | 48 | RFA2 | 1.75 | 15.5 | 0.11 |
| 4 | Copper-aluminium | 6 | 1000 | 180 | 48 | RCA | 0.96 | 17.5 | 0.10 |
Example 5～8
Following example illustrates the preparation of method catalyst system therefor provided by the invention.
Take by weighing each 50 gram of Lacunaris metal carrier RNA, RFA1, RFA2 and RCA of example 1～4 preparation, join respectively in the withstand voltage still, (contain SiO with NaOH, waterglass
223.5 heavy %, Chang Ling oil-refining chemical head factory is produced), TPAOH (Beijing Chemical Plant produces for TPA, chemical pure) and deionized water be made into mole and consist of 5Na
2O10TPA100SiO
27000H
2The zeolite of O synthesizes liquid.The synthetic liquid of 1500 milliliters of zeolites is joined respectively in the withstand voltage still, and in confined conditions, 180 ℃ of crystallization 48 hours are filtered, the washing solid product to neutral, dry, 550 ℃ of roastings 10 hours to remove template agent TPA wherein.
Taking by weighing 50 grams through the sample of 550 ℃ of roastings after 10 hours, is that the ammonia spirit of 0.1 mol mixes with 500 ml concns, stirring at room temperature, carried out ion-exchange 8 hours, and filtered, under similarity condition, exchange twice again, filter 110 ℃ of dryings 12 hours, 550 ℃ of roastings 2 hours.The solid product that obtains is used quantitative Schweinfurt green (chemical pure respectively, Beijing lean reagent company produces) solution, ferric nitrate (chemical pure, Beijing lean reagent company produces) solution or nickel nitrate (chemical pure, Beijing lean chemical reagents corporation produces) the solution mixing, at room temperature stir, carried out ion-exchange 8 hours, filter, under similarity condition, exchange twice again, filter, 110 ℃ of dryings 12 hours, 550 ℃ of roastings 12 hours, the method catalyst system therefor provided by the invention of cupric, iron or nickel ion.
Table 5 has been listed used Lacunaris metal carrier, Schweinfurt green solution usage, iron nitrate solution consumption, nickel nitrate solution consumption, and table 6 is listed catalyst and formed.Catalyst C wherein
1Has main X-ray diffract spectral line as shown in table 1.Appoint and get catalyst C
1The analytic electron microscope photo of 10000 times of amplifications of different parts shown in Fig. 2～5.Catalyst C
2And C
3Has main X-ray diffract spectral line as shown in table 2.Catalyst C
4Has main X-ray diffract spectral line as shown in table 3.
Wherein, the X-ray diffract spectral line is measured with CuK α target on Simens D5000 type X-ray diffractometer.The analytic electron microscope photo obtains on Japanese JEM-2000FXII (configuration link QS-2000 power spectrum) analytic electron microscope.The content of the nickel in the catalyst, iron, copper, aluminium, sodium and nickel ion, iron ion and copper ion adopts plasma emission spectrometry (ICP) to measure, the content of silicon adopts x ray fluorescence spectrometry to measure on the Xray fluorescence spectrometer that Japan Industrial Co., Ltd of science produces, the content of oxygen adopts gravimetric method to calculate and get, that is: oxygen content=100%-nickel (or iron or copper) content-aluminium content-sodium content-nickel (or iron or copper) ion concentration-silicone content.
The result of Fig. 2～5 shows, in the method catalyst system therefor of the present invention, described zeolite can in-situ crystallization on the surface of Lacunaris metal carrier, shown in Fig. 2,4 and 5, black background partly is nickel porous-aluminium alloy carrier (wherein regular rectangle is bigger ZSM-5 zeolite crystal among Fig. 2), is the ZSM-5 zeolite attached to the white portion on nickel porous-aluminium alloy carrier surface.Zeolite described in the method catalyst system therefor of the present invention also can in-situ crystallization in the hole of Lacunaris metal carrier, black background partly is porous-aluminium alloy carrier shown in Fig. 3 and 4, recessed part is represented the hole on the carrier, and the white portion of the surface attachment of recess is the ZSM-5 zeolite.
Table 5
| Example number | Lacunaris metal carrier | The solution kind | Solution concentration, mol | Solution usage, |
| 5 | RNA | Schweinfurt green solution | 0.01 | 1500 |
| 6 | RFA1 | Iron nitrate solution | 0.01 | 3000 |
| 7 | RFA2 | Iron nitrate solution | 0.02 | 2000 |
| 8 | RCA | Nickel nitrate solution | 0.01 | 3000 |
Table 6
| Example number | Catalyst | ||||||||||
| Numbering | Form heavy % | ||||||||||
| Nickel | Iron | Copper | Aluminium | Sodium | Silicon | Oxygen | Nickel ion | Copper ion | Iron ion | ||
| 5 | C 1 | 78.5 | - | - | 1.0 | 0.1 | 9.1 | 10.2 | - | 1.1 | - |
| 6 | C 2 | - | 40.3 | - | 3.1 | 0.2 | 24.8 | 28.6 | - | - | 3.0 |
| 7 | C 3 | - | 67.9 | - | 1.1 | 0.1 | 13.8 | 15.9 | - | - | 1.2 |
| 8 | C 4 | - | - | 74.3 | 0.7 | 0.1 | 11.2 | 11.7 | 2.0 | - | - |
Example 9～13
The following examples illustrate the preparation of method catalyst system therefor provided by the invention.
Method by example 5～8 prepares catalyst, the consumption difference of the different synthetic liquid of just zeolite, and the concentration of Schweinfurt green solution, iron nitrate solution and nickel nitrate solution is also different with consumption.
Table 7 has provided the concentration and the consumption of used Lacunaris metal carrier, the synthetic liquid consumption of zeolite, Schweinfurt green solution, iron nitrate solution and nickel nitrate solution.Table 8 has provided the catalyst composition.Catalyst C wherein
5, C
6Has main X-ray diffract spectral line as shown in table 1.C
7Has main X-ray diffract spectral line as shown in table 2.C
8, C
9Has main X-ray diffract spectral line as shown in table 3.
Table 7
| Example number | Lacunaris metal carrier | Zeolite synthesizes the liquid consumption, milliliter | The solution kind | Solution concentration, mol | Solution usage, milliliter |
| 9 | RNA | 3000 | Schweinfurt green solution | 0.005 | 5000 |
| 10 | RNA | 3600 | Schweinfurt green solution | 0.01 | 2000 |
| 11 | RFA2 | 3000 | Nickel nitrate solution | 0.05 | 3000 |
| 12 | RCA | 3000 | Schweinfurt green solution | 0.01 | 3000 |
| 13 | RCA | 3600 | Iron nitrate solution | 0.02 | 2000 |
Table 8
| Example number | Catalyst | ||||||||||
| Numbering | Form heavy % | ||||||||||
| Nickel | Iron | Copper | Aluminium | Sodium | Silicon | Oxygen | Nickel ion | Copper ion | Iron ion | ||
| 9 | C 5 | 50.3 | - | - | 0.6 | 0 | 22.4 | 25.6 | - | 1.1 | - |
| 10 | C 6 | 39.3 | - | - | 0.4 | 0 | 28.5 | 31.2 | - | 0.6 | - |
| 11 | C 7 | - | 40.3 | - | 0.6 | 0.1 | 27.0 | 31.0 | 1.0 | - | - |
| 12 | C 8 | - | - | 42.4 | 0.5 | 0 | 26.2 | 30.0 | - | 0.9 | - |
| 13 | C 9 | - | - | 37.4 | 0.4 | 0 | 28.9 | 32.7 | - | - | 0.6 |
Example 14～16
Following example illustrates the preparation of method catalyst system therefor provided by the invention.
Method by example 5～8 prepares catalyst, and the different synthetic liquid of just zeolite are to consist of 8Na by the mole that NaOH, waterglass, TPAOH (TPA), aluminum sulfate and deionized water are made into
2O15TPAAl
2O
3100SiO
27000H
2The zeolite of O synthesizes liquid, and the concentration of Schweinfurt green solution, iron nitrate solution and nickel nitrate solution is also different with consumption.
Table 9 has provided the concentration and the consumption of used Lacunaris metal carrier, Schweinfurt green solution, iron nitrate solution and nickel nitrate solution, and table 10 has provided the catalyst composition.
Catalyst C wherein
10, C
11, C
12Has the main X-ray diffract spectral line shown in table 1,2,3 successively.
Table 9
| Example number | Lacunaris metal carrier | The solution kind | Solution concentration, mol | Solution usage, milliliter |
| 14 | RNA | Ferric nitrate | 0.01 | 3000 |
| 15 | RFA2 | Schweinfurt green | 0.005 | 5000 |
| 16 | RCA | Nickel nitrate | 0.02 | 2000 |
Table 10
| Example number | Catalyst | ||||||||||
| Numbering | Form heavy % | ||||||||||
| Nickel | Iron | Copper | Aluminium | Sodium | Silicon | Oxygen | Nickel ion | Copper ion | Iron ion | ||
| 14 | C 10 | 51.7 | - | - | 2.1 | 0.1 | 20.5 | 23.5 | - | - | 2.1 |
| 15 | C 11 | - | 47.4 | - | 2.5 | 0.1 | 22.0 | 25.6 | - | 2.4 | - |
| 16 | C 12 | - | - | 47.0 | 3.0 | 0.1 | 22.5 | 25.4 | 2.0 | - | - |
Example 17
This example illustrates the preparation of method catalyst system therefor provided by the invention.
Method by example 5 prepares catalyst, and the mole of the different synthetic liquid of just zeolite consists of 5Na
2O5TPA100SiO
27000H
2O, the catalyst that obtains are C
13C
13Have main X-ray diffract spectral line as shown in table 1, and have following composition: nickel 78.1 heavy %, aluminium 1.0 heavy %, sodium 0.1 heavy %, silicon 9.2 heavy %, oxygen 10.5 heavy %, copper ion 1.1 heavy %.
Example 18～21
Following example illustrates Preparation of catalysts provided by the invention.
Method by example 5～8 prepares catalyst, different is template used dose is tetraethyl ammonium hydroxide (TEA, chemical pure, the Beijing Chemical Plant produces), the composition of the synthetic liquid of zeolite and the concentration of Schweinfurt green solution, iron nitrate solution and nickel nitrate solution are also different with consumption.
Table 11 has provided the synthetic liquid of used Lacunaris metal carrier, zeolite forms, and table 12 has provided the concentration and the consumption of Schweinfurt green, ferric nitrate, nickel nitrate solution, and table 13 has provided the composition of catalyst.Catalyst C wherein
14Has main X-ray diffract spectral line as shown in table 1, C
15Has main X-ray diffract spectral line as shown in table 2, C
16And C
17Has main X-ray diffract spectral line as shown in table 3.
Table 11
| Example number | Lacunaris metal carrier | The synthetic liquid mole of zeolite is formed |
| 18 | RNA | 5Na 2O·10TEA·100SiO 2·7000H 2O |
| 19 | RFA2 | 5Na 2O·5TEA·100SiO 2·7000H 2O |
| 20 | RCA | 5Na 2O·8TEA·100SiO 2·7000H 2O |
| 21 | RCA | 5Na 2O·10TEA·100SiO 2·7000H 2O |
Table 12
| Example number | The solution kind | Solution concentration, mol | Solution usage, milliliter |
| 18 | Schweinfurt green solution | 0.01 | 1500 |
| 19 | Schweinfurt green solution | 0.01 | 1500 |
| 20 | Nickel nitrate solution | 0.05 | 3000 |
| 21 | Iron nitrate solution | 0.02 | 2000 |
Table 13
| Example number | Catalyst | ||||||||||
| Numbering | Form heavy % | ||||||||||
| Nickel | Iron | Copper | Aluminium | Sodium | Silicon | Oxygen | Nickel ion | Copper ion | Iron ion | ||
| 18 | C 14 | 71.8 | - | - | 0.9 | 0 | 12.2 | 14.1 | - | 1.0 | - |
| 19 | C 15 | - | 79.0 | - | 1.0 | 0.1 | 9.1 | 9.8 | - | 1.0 | - |
| 20 | C 16 | - | - | 80.0 | 0.8 | 0 | 8.7 | 9.7 | 0.8 | - | - |
| 21 | C 17 | - | - | 80.0 | 0.8 | 0 | 8.7 | 9.7 | - | - | 0.8 |
Example 22～24
Following example illustrates the preparation of method catalyst system therefor provided by the invention.
Method by example 5～8 prepares catalyst, the composition difference of the different synthetic liquid of just zeolite, and the concentration of Schweinfurt green solution, iron nitrate solution and nickel nitrate solution is also different with consumption.
Table 14 provided the composition of the synthetic liquid of used Lacunaris metal carrier, zeolite, and table 15 has provided the concentration and the consumption of Schweinfurt green, nickel nitrate, iron nitrate solution, and table 16 has provided the catalyst composition.Catalyst C wherein
18, C
19, C
20Has the main X-ray diffract spectral line shown in table 1,2,3 successively.
Table 14
| Example number | Lacunaris metal carrier | The synthetic liquid mole of zeolite is formed |
| 22 | RNA | 5Na 2O·10TPA·100SiO 2·5000H 2O |
| 23 | RFA2 | 5Na 2O·10TPA·100SiO 2·10000H 2O |
| 24 | RCA | 5Na 2O·10TPA·100SiO 2·15000H 2O |
Table 15
| Example number | The solution kind | Solution concentration, mol | Solution usage, |
| 22 | Schweinfurt green solution | 0.01 | 3000 |
| 23 | Iron nitrate solution | 0.02 | 2000 |
| 24 | Nickel nitrate solution | 0.05 | 3000 |
Table 16
| Example number | Catalyst | ||||||||||
| Numbering | Form heavy % | ||||||||||
| Nickel | Iron | Copper | Aluminium | Sodium | Silicon | Oxygen | Nickel ion | Copper ion | Iron ion | ||
| 22 | C 18 | 60.4 | - | - | 1.0 | 0.1 | 17.2 | 19.8 | - | 1.5 | - |
| 23 | C 19 | - | 82.0 | - | 1.0 | 0.1 | 7.4 | 8.4 | - | - | 0.9 |
| 24 | C 20 | - | - | 84.2 | 1.0 | 0.1 | 6.3 | 7.3 | 1.1 | - | - |
Example 25～27
Following example illustrates the preparation of method catalyst system therefor provided by the invention.
Method by example 5 and 7 prepares catalyst, and different is that crystallization temperature is different with crystallization time, and the concentration of Schweinfurt green solution, iron nitrate solution, nickel nitrate solution is also different with consumption.
Table 17 has provided used Lacunaris metal carrier, crystallization temperature and time, and table 18 has provided the concentration and the consumption of Schweinfurt green solution, iron nitrate solution, nickel nitrate solution, and table 19 provided the catalyst composition.Catalyst C wherein
21Has main X-ray diffract spectral line as shown in table 1, C
22And C
23Has main X-ray diffract spectral line as shown in table 2.
Table 17
| Example number | Lacunaris metal carrier | Crystallization temperature, ℃ | Crystallization time, |
| 25 | RNA | 160 | 70 |
| 26 | RFA2 | 150 | 82 |
| 27 | RFA2 | 170 | 40 |
Table 18
| Example number | The solution kind | Solution concentration, mol | Solution usage, |
| 25 | Schweinfurt green solution | 0.01 | 1500 |
| 26 | Iron nitrate solution | 0.02 | 3000 |
| 27 | Nickel nitrate solution | 0.05 | 3000 |
Table 19
| Example number | Catalyst | ||||||||||
| Numbering | Form heavy % | ||||||||||
| Nickel | Iron | Copper | Aluminium | Sodium | Silicon | Oxygen | Nickel ion | Copper ion | Iron ion | ||
| 25 | C 21 | 78.0 | - | - | 1.0 | 0.1 | 9.2 | 10.6 | - | 1.1 | - |
| 26 | C 22 | - | 79.0 | - | 1.0 | 0.1 | 9.1 | 9.8 | - | - | 1.0 |
| 27 | C 23 | - | - | 84.2 | 1.0 | 0.1 | 6.3 | 7.3 | 1.1 | - | - |
Example 28～29
Following example illustrates the preparation of method catalyst system therefor provided by the invention.
Take by weighing 100 gram iron net (0.04 centimetre of iron wire diameter respectively, voidage is 50%, Shoudu Iron and Steel Co. produces) and copper mesh (0.02 centimetre of brass wire diameter, voidage are 80%, copper work, Luoyang product) place middle frequency furnace, put into 50 gram aluminium bits in the middle frequency furnace bottom, feed argon gas after 1 hour, be warming up to 650 ℃, kept 1 hour, heated again 2 hours in 900 ℃, make on the iron net surface and the copper mesh surface on contain the sample of one deck iron-aluminium and copper-aluminium alloy.
Take by weighing each 50 gram of sample of iron content-aluminium and copper-aluminium alloy on the surface that obtains, add 1250 milliliters in the NaOH that concentration is the 6M mol 90 ℃ and 180 ℃ respectively, constant temperature was taken out aluminium 1.5 hours, contain the Lacunaris metal carrier of one deck porous iron-aluminium, copper-aluminium alloy, porous iron-aluminium alloy/iron net and porous copper-aluminium alloy/copper mesh on surperficial.
Take by weighing each 20 gram of porous iron-aluminium alloy/iron net and porous copper-aluminium alloy/copper mesh and join respectively in the withstand voltage still, and in withstand voltage still, add 1000 milliliters of moles respectively and consist of 5Na
2O10TPAAl
3O
3100SiO
27000H
2The zeolite of O synthesizes liquid, is closing under the close condition 180 ℃ of crystallization 48 hours, filters, the washing solid product is to neutral, drying, 550 ℃ of roastings were made the composite of ZSM-5 and porous iron-aluminium alloy/iron net and ZSM-5 and porous copper-aluminium alloy/copper mesh to remove template agent TPA wherein in 10 hours.
Take by weighing 10 gram ZSM-5 zeolite and porous iron-aluminium alloy/iron net and ZSM-5 zeolite and porous copper-aluminium alloy/copper mesh composites respectively, be that 0.1 mol ammonia spirit mixes with 250 ml concns respectively, at room temperature carry out ion-exchange 8 hours, filter, under similarity condition, exchange twice again, filter 110 ℃ of dryings 12 hours, 550 ℃ of roastings 2 hours.The solid product that obtains mixes with Schweinfurt green solution and iron nitrate solution respectively, at room temperature carried out ion-exchange 8 hours, filters, again twice of similarity condition exchange, filter, 110 ℃ of dryings 12 hours, 550 ℃ of roastings 12 hours, method catalyst system therefor C provided by the invention
24And C
25
Table 20 has been listed the concentration and the consumption of used Lacunaris metal carrier and Schweinfurt green solution and iron nitrate solution, and table 21 has been listed catalyst C
24And C
25Composition.
Table 20
| Example number | Used Lacunaris metal carrier | The solution kind | Solution concentration, mol | Solution usage, |
| 28 | Porous iron-aluminium alloy/iron net | Schweinfurt green solution | 0.01 | 1500 |
| 29 | Porous copper-aluminium alloy/copper mesh | Iron nitrate solution | 0.01 | 5000 |
Table 21
| Example number | Catalyst | ||||||||
| Numbering | Form heavy % | ||||||||
| Copper | Iron | Aluminium | Sodium | Silicon | Oxygen | Copper ion | Iron ion | ||
| 28 | C 24 | - | 92.7 | 0.4 | 0 | 3.1 | 3.4 | 0.4 | - |
| 29 | C 25 | 89.4 | - | 0.7 | 0 | 3.9 | 4.3 | - | 1.7 |
Example 30～31
Following example illustrates the preparation of method catalyst system therefor provided by the invention.
Take by weighing each 50 gram of Lacunaris metal carrier RFA1, RFA2 of example 2～3 preparations, join respectively in the withstand voltage still, (contain SiO with NaOH, waterglass
223.5 heavy %, Chang Ling oil-refining chemical head factory is produced), TPAOH (Beijing Chemical Plant produces for TPA, chemical pure) and deionized water be made into mole and consist of 5Na
2O10TPA100SiO
27000H
2The zeolite of O synthesizes liquid.The synthetic liquid of 1500 milliliters of zeolites is joined respectively in the withstand voltage still, in confined conditions, 180 ℃ of crystallization 48 hours are filtered, the washing solid product to neutral, dry, 550 ℃ of roastings 10 hours removing template agent TPA wherein, ZSM-5 zeolite and porous metal composite material.The aqueous ammonium chloride solution that with the ZSM-5 zeolite that obtains and porous metal composite material and concentration is 1 mol is that 10 ratio is mixed in liquid-solid ratio, under 70 ℃ temperature, carry out ion-exchange 2 hours, spend the deionised water solid product to there not being acid ion, 120 ℃ of oven dry, roasting is 5 hours under 700 ℃ of air atmospheres, obtains method catalyst system therefor C provided by the invention
26And C
27
Table 22 has provided used Lacunaris metal carrier, catalyst numbering and has formed.Wherein, catalyst C
26And C
27Has main X-ray diffract spectral line as shown in table 2.Amplify 2600 times catalyst C
26Stereoscan photograph as shown in Figure 6.Amplify 10000 times catalyst C
26Transmission electron microscope photo as shown in Figure 7.
Wherein, the X-ray diffract spectral line is measured with CuK α target on Simens D5000 type X-ray diffractometer.Transmission electron microscope photo obtains on JEM-2000FXII (configuration link QS-2000 power spectrum) analytic electron microscope.Stereoscan photograph obtains on Hittach 4000 type ESEMs.The content of the iron in the catalyst, aluminium, sodium adopts plasma emission spectrometry (ICP) to measure, the content of silicon adopts x ray fluorescence spectrometry to measure on the Xray fluorescence spectrometer that Japan Industrial Co., Ltd of science produces, the content of oxygen adopts gravimetric method to calculate and get, that is: oxygen content=100%-iron content-aluminium content-sodium content-silicone content.
Table 22
| Example number | Lacunaris metal carrier | Catalyst | |||||
| Numbering | Form heavy % | ||||||
| Iron | Aluminium | | Silicon | Oxygen | |||
| 30 | RFA1 | C 26 | 40.9 | 3.1 | 0.1 | 24.8 | 31.1 |
| 31 | RFA2 | C 27 | 68.3 | 1.1 | 0.07 | 13.8 | 16.73 |
Example 32～40
Following example illustrates the preparation of method catalyst system therefor provided by the invention.
Method by example 31 prepares ZSM-5 zeolite and porous metal composite material, and the consumption of different the is synthetic liquid of zeolite is 3000 milliliters, after the ammonium ion exchange, carries out heat or hydrothermal treatment consists under the different condition respectively, catalyst C provided by the invention
28～C
36Treatment conditions are listed in the table 23.Table 24 has provided the numbering and the composition of the catalyst that obtains.
Catalyst C wherein
28～C
36Has main X-ray diffract spectral line as shown in table 2.
Table 23
| Example number | Used atmosphere | Treatment temperature, ℃ | Processing time, hour |
| 32 | Air | 680 | 8 |
| 33 | | 800 | 3 |
| 34 | Air | 850 | 2 |
| 35 | Air | 900 | 5 |
| 36 | 100 | 600 | 6 |
| 37 | Contain the air of 50 body % air and the gaseous mixture of | 600 | 3 |
| 38 | Contain the water vapour of 50 body % water vapours and the gaseous mixture of | 500 | 8 |
| 39 | Contain the water vapour of 8 body % water vapours and the gaseous mixture of | 600 | 1000 |
| 40 | Contain the water vapour of 8 body % water vapours and the gaseous mixture of | 600 | 5 |
Table 24
| Example number | The catalyst numbering | Catalyst is formed, heavy % | ||||
| Iron | Aluminium | Sodium | Silicon | Oxygen | ||
| 32 | C 28 | 65.0 | 0.9 | 0.06 | 16.1 | 17.94 |
| 33 | C 29 | 64.9 | 0.9 | 0.06 | 16.2 | 17.94 |
| 34 | C 30 | 65.0 | 0.9 | 0.06 | 16.1 | 17.94 |
| 35 | C 31 | 65.1 | 0.9 | 0.06 | 16.1 | 17.84 |
| 36 | C 32 | 65.2 | 0.8 | 0.06 | 16.1 | 17.84 |
| 37 | C 33 | 65.0 | 0.9 | 0.06 | 16.1 | 17.94 |
| 38 | C 34 | 65.0 | 0.9 | 0.06 | 16.1 | 17.94 |
| 39 | C 35 | 65.1 | 0.8 | 0.06 | 16.1 | 17.94 |
| 40 | C 36 | 65.0 | 0.9 | 0.06 | 16.1 | 17.94 |
Example 41
Following example illustrates the preparation of method catalyst system therefor provided by the invention.
Method by example 31 prepares catalyst, and different is that the synthetic liquid of zeolite is to consist of 8Na by the mole that NaOH, waterglass, TPAOH (TPA), aluminum sulfate and deionized water are made into
2O15TPAAl
2O
3100SiO
27000H
2The zeolite of O synthesizes liquid.Table 25 has provided the numbering and the composition of gained catalyst.Wherein, catalyst C
37Has the main X-ray diffract spectral line shown in the table 2.
Table 25
| Example number | Catalyst | |||||
| Numbering | Form heavy % | |||||
| Iron | Aluminium | Sodium | Silicon | Oxygen | ||
| 41 | C 37 | 47.8 | 2.5 | 0.1 | 23.0 | 26.6 |
Example 42
Following example illustrates the preparation of method catalyst system therefor provided by the invention.
Method by example 31 prepares catalyst, and different is that template used dose is tetraethyl ammonium hydroxide (TEA, chemical pure, the Beijing Chemical Plant produces), the composition of the synthetic liquid of zeolite is also different, and the condition of ammonium ion exchange is 90 ℃ of temperature, 3 hours time, liquid-solid ratio 20.Table 26 has provided used Lacunaris metal carrier, the synthetic liquid of zeolite is formed, and table 27 has provided the numbering and the composition of gained catalyst.Wherein, catalyst C
38Has main X-ray diffract spectral line as shown in table 2.
Table 26
| Example number | Lacunaris metal carrier | The synthetic liquid mole of zeolite is formed |
| 42 | RFA2 | 5Na 2O·5TEA·100SiO 2·7000H 2O |
Table 27
| Example number | Catalyst | |||||
| Numbering | Form heavy % | |||||
| Iron | Aluminium | Sodium | Silicon | Oxygen | ||
| 42 | C 38 | 72.5 | 0.9 | 0.11 | 11.3 | 15.19 |
Example 43
Following example illustrates the preparation of method catalyst system therefor provided by the invention.
Method by example 31 prepares catalyst, the composition difference of the different synthetic liquid of just zeolite.Table 28 has provided the composition of used Lacunaris metal carrier, the synthetic liquid of zeolite, and table 29 has provided the numbering and the composition of gained catalyst.Catalyst C wherein
39Has main X-ray diffract spectral line as shown in table 2.
Table 28
| Example number | Lacunaris metal carrier | The synthetic liquid mole of zeolite is formed |
| 43 | RFA2 | 5Na 2O·10TPA·100SiO 2·10000H 2O |
Table 29
| Example number | Catalyst | |||||
| Numbering | Form heavy % | |||||
| Iron | Aluminium | Sodium | Silicon | Oxygen | ||
| 43 | C 39 | 82.3 | 1.0 | 0.05 | 7.4 | 9.25 |
Example 44
Following example illustrates the preparation of method catalyst system therefor provided by the invention.
Method by example 31 prepares catalyst, and different is that crystallization temperature is different with crystallization time.Table 30 has provided numbering, the composition of used Lacunaris metal carrier, crystallization temperature and time and gained catalyst.Catalyst C wherein
40Has main X-ray diffract spectral line as shown in table 2.
Table 30
| Example number | Lacunaris metal carrier | Crystallization process | Catalyst | ||||||
| Temperature, ℃ | Time, hour | Numbering | Form heavy % | ||||||
| Iron | Aluminium | | Silicon | Oxygen | |||||
| 44 | RFA2 | 150 | 82 | C 40 | 79.3 | 1.0 | 0.05 | 9.4 | 10.25 |
Example 45
Following example illustrates the preparation of method catalyst system therefor provided by the invention.
Take by weighing 50 gram iron net (0.04 centimetre of iron wire diameter respectively, voidage 50%, Shoudu Iron and Steel Co.'s product) places middle frequency furnace, put into 25 gram aluminium bits in the bottom of middle frequency furnace, feed argon gas after 1 hour, be warming up to 650 ℃, kept 1 hour, 900 ℃ were heated 2 hours again, and made the sample that contains one deck iron-aluminium alloy on the iron net surface.
Take by weighing sample 20 grams that contain one deck iron-aluminium alloy on the iron net surface that obtains, add 500 milliliters in the NaOH that concentration are 6 mol at 90 ℃, constant temperature was taken out aluminium 1.5 hours, contain the Lacunaris metal carrier of one deck porous iron-aluminium alloy, i.e. porous iron-aluminium alloy/iron net on surperficial.
Take by weighing porous iron-aluminium alloy/iron net 10 grams and join in the withstand voltage still, and in withstand voltage still, add 500 milliliters of moles respectively and consist of 5Na
2O10TPAAl
2O
3100SiO
27000H
2The zeolite of O synthesizes liquid, is closing under the close condition 180 ℃ of crystallization 48 hours.Filter, the washing solid product is to neutral, drying, and 550 ℃ of roastings were made ZSM-5 and porous metal composite material to remove template agent TPA wherein in 10 hours.Method by example 30～31 is carried out ammonium ion exchange and roasting, obtains the catalyst of method preparation provided by the invention.Table 31 provides the numbering and the composition of catalyst.
Table 31
| Example number | Catalyst | |||||
| Numbering | Form heavy % | |||||
| Iron | Aluminium | Sodium | Silicon | Oxygen | ||
| 45 | C 41 | 92.67 | 0.4 | 0.03 | 3.2 | 3.7 |
Example 46～53
Following example illustrates the firmness that the ZSM-5 zeolite combines with Lacunaris metal carrier in the method catalyst system therefor provided by the invention.
Accurately take by weighing the catalyst C of example 5,6,7,9,11,14,15 and 28 preparations
1, C
2, C
3, C
5, C
7, C
10, C
11And C
24Each 5.00 gram, put into U type pipe respectively, at 600 ℃ is that the argon gas of 100 ml/min was handled 10 hours with containing 3 heavy % water, flow velocity down, or 900 ℃ of roastings 10 hours in air, or be that the argon gas of 100 ml/min was handled 1000 hours with flow velocity at 400 ℃, cooling is isolated the particle that has magnetic with magnet, weighs.Because of ZSM-5 zeolite and nickel porous-aluminium (or iron-aluminium) alloy composite materials have magnetic, after under different condition, handling, the zeolite that splits away off from composite does not have magnetic, thereby can find out the firmness that the ZSM-5 zeolite combines with Lacunaris metal carrier according to its weightlessness.Treatment conditions and the results are shown in Table 22.
Comparative Examples 1
ZSM-5 zeolite and carrier-bound firmness in the existing CuZSM-5 zeolite of this Comparative Examples explanation/stainless steel catalyst.
With reference to the method for The Canadian Journal of Chemical Engineering 73,120,1995, take by weighing stainless (steel) wire (voidage is 80%, and Shoudu Iron and Steel Co. produces) 50 grams of 0.02 centimetre of diameter, put into withstand voltage still.1500 milliliters of moles are consisted of 5Na
2O10TPAAl
2O
3100SiO
27000H
2The synthetic liquid of O zeolite joins in the withstand voltage still, and in confined conditions, 180 ℃ of crystallization 48 hours are filtered, the washing solid product is to neutral, and dry, 550 ℃ of roastings were made ZSM-5/ stainless (steel) wire composite to remove template agent TPA wherein in 10 hours.
With the above-mentioned ZSM-5/ stainless (steel) wire composite that obtains 10 grams and 250 milliliters, concentration is that the ammonia spirit of 0.1 mol mixes, and at room temperature carries out ion-exchange 8 hours, filtration, under similarity condition, exchange twice again, filter, drying was in 550 ℃ of roastings 2 hours.The solid product that obtains and 300 milliliters, concentration are that the Schweinfurt green solution of 0.01 mol mixes, and at room temperature carry out ion-exchange 8 hours, filter, and exchange twice again under similarity condition, filter, drying, in 550 ℃ of roastings 12 hours, reference catalyst B
1B
1Has following composition: stainless steel 94.5 heavy %, aluminium 0.2 heavy %, silicon 2.4 heavy %, oxygen 2.6 heavy %, copper ion 0.3 heavy %.
With the above-mentioned reference catalyst B that obtains
15.00 gram is put into U type pipe, handles zeolite under the condition identical with example 46,52 and 53, weighs, calculates the loss in weight of composite, treatment conditions and the results are shown in Table 32.
The presentation of results of table 32, method catalyst system therefor provided by the invention is under the condition of zeolite content far above reference catalyst, the weight loss of catalyst after treatment is far below reference catalyst, this illustrates that the firmness that zeolite combines with Lacunaris metal carrier is far above prior art in the method catalyst system therefor provided by the invention.
Table 32
| Example number | Catalyst | Treatment conditions | Handle the rear catalyst weight loss, heavy % |
| 46 | | 600 ℃ contain 3 heavy % water, and the argon gas of | 0.1 |
| 47 | C 2 | Roasting is 10 hours in 900 ℃ of air | 0.7 |
| 48 | C 3 | The argon gas that 400 ℃ of flow velocitys are 100 ml/min was handled 1000 hours | 0.1 |
| 49 | C 5 | Roasting is 10 hours in 900 ℃ of air | 0.5 |
| 50 | C 7 | Roasting is 10 hours in 900 ℃ of air | 0.5 |
| 51 | C 10 | The argon gas that 400 ℃ of flow velocitys are 100 ml/min was handled 1000 hours | 0.2 |
| 52 | | 600 ℃ contain 3 heavy % water, and the argon gas of | 0.2 |
| 53 | | 600 ℃ contain 3 heavy % water, and the argon gas of | 0.1 |
| Comparative Examples 1 | | 600 ℃ contain 3 heavy % water, and the argon gas of | 4.1 |
Example 54
Following example illustrates the hydrothermal stability of method catalyst system therefor provided by the invention.
Take by weighing the preceding catalyst C of hydrothermal treatment consists of example 5 preparations
1With the catalyst C after example 46 hydrothermal treatment consists
1Each 0.1 gram is on legbold LHS 12 MCD associating spectrometer, with Mg source (MgK, 1253.6 electron-volts, 240 watts), in vacuum 1 * 10
-10Under the condition of millibar, measure the Al2P x-ray photoelectron power spectrum (XPS) of catalyst.
Before and after the hydrothermal treatment consists Al2P XPS spectrum figure of catalyst respectively as among Fig. 81 and Fig. 9 in shown in 5.Known binding energy is that the peak about 77.4 electron-volts is the peak of non-framework aluminum, the peak that binding energy is about 74.4 electron-volts is the peak of zeolitic frameworks aluminium, the ratio of two peak areas is represented the ratio of framework aluminum and non-framework aluminum quantity, thereby can measure the ratio of framework aluminum and non-framework aluminum according to the ratio of two peak areas.2 smoothed curves for the curve 1 of computer simulation among Fig. 8 wherein, 3 and 4 are respectively the framework aluminum of computer simulation and the peak of non-framework aluminum among Fig. 8.6 is smoothed curves of the curve 5 of computer simulation among Fig. 9, and 7 and 8 is respectively the framework aluminum of computer simulation and the peak of non-framework aluminum among Fig. 9.Composite mesolite framework aluminum is listed in the table 33 with the ratio of non-framework aluminum before and after the hydrothermal treatment consists that calculates thus.
Comparative Examples 2
The hydrothermal stability of this Comparative Examples explanation CuZSM-5 zeolite.
Measure by the method for example 54 that silica alumina ratio is 40, the ratio of CuZSM-5 zeolite (Chang Ling catalyst plant products) the hydrothermal treatment consists front and back framework aluminum of content of copper ion 2.3 heavy %.Before and after the hydrothermal treatment consists Al2P XPS spectrum figure of CuZSM-5 zeolite as among Figure 10 9 and Figure 11 in shown in 13.10 are smoothed curves of the curve 9 of computer simulation among Figure 10 wherein, 11 and 12 is the framework aluminum of computer simulation and the peak of non-framework aluminum.14 is smoothed curves of the curve 13 of computer simulation among Figure 11, and 15 and 16 is respectively the framework aluminum of computer simulation and the peak of non-framework aluminum.Framework aluminum is listed in the table 33 with the ratio of non-framework aluminum before and after the hydrothermal treatment consists.
Table 33
| Example number | Sample | The ratio of framework aluminum and non-framework aluminum | |
| Before the hydrothermal treatment consists | After the hydrothermal treatment consists | ||
| 54 | | 10∶1 | 10∶1 |
| Comparative Examples 2 | The CuZSM-5 zeolite | 4.1∶1 | 1.1∶1 |
The result of table 33 shows that after 10 hours, CuZSM-5 zeolitic frameworks aluminium obviously reduces with the ratio of non-framework aluminum through 600 ℃ of hydrothermal treatment consists, illustrates that hydrothermal treatment consists makes a large amount of dealuminzations of CuZSM-5 zeolite.And method catalyst system therefor provided by the invention is after similarity condition is handled down, and framework aluminum does not change with the ratio of non-framework aluminum, illustrates in the method catalyst system therefor provided by the invention that the framework aluminum of zeolite has very high hydrothermal stability.
Example 55
Following example illustrates the framework si-al ratio of method catalyst system therefor mesolite provided by the invention.
At catalyst C shown in Figure 5
1In choose different 5 points 17,18,19,20 and 21, its position provides in the profile diagram of as shown in figure 12 Fig. 5, with Japanese JEM-2000FXII type analysis Electronic Speculum (preparation Link QS-2000 power spectrum) diverse location of the catalyst of these 5 somes representatives is carried out micro-zone analysis respectively, determine the framework si-al ratio of diverse location zeolite, the framework si-al ratio of diverse location zeolite (Si and Al atomic ratio) is shown in table 34.
Table 34
| The position | Silica alumina ratio |
| 17 | 195 |
| 18 | 32 |
| 19 | 85 |
| 20 | 165 |
| 21 | 210 |
The result of table 34 shows that in the method catalyst system therefor provided by the invention, the framework si-al ratio of zeolite can be different at diverse location, and its silica alumina ratio is more than 15.Because at catalyst C
1Preparation process in, do not contain aluminium in the synthetic liquid of zeolite, (promptly not adding the aluminium source), thereby the framework aluminum of described zeolite is all from contained aluminium in nickel porous-aluminium alloy.
Example 56～72
Following example illustrates method provided by the invention.
Take by weighing the catalyst C of example 5 preparations
1, press the catalyst C after the described conditions of example 46 are handled
1, press the catalyst C after the described conditions of example 47 are handled
2, press the catalyst C after the described conditions of example 48 are handled
3, press the catalyst C after the described conditions of example 49 are handled
5, press the catalyst C after the described conditions of example 50 are handled
7With the catalyst C that presses after 53 described conditions are handled
24Each 100 milligrams, the internal diameter of packing into is in 6 millimeters the U-shaped reactor, to contain NO, NH
3, O
2Argon gas be raw material, under the differential responses condition, remove the nitric oxide in the described raw material, the results are shown in Table 35.Wherein, the nitric oxide conversion ratio is the result of reaction after 2 hours.Nitrogen oxide is detected by QGS-08B type nitrogen-oxide analyzer, (Beijing analyzer factory product).
Table 35
| Example number | The catalyst numbering | Preparation of Catalyst or treatment conditions | NO concentration, ppm | NH 3Concentration, ppm | O 2Concentration, heavy % | Reaction temperature, ℃ | Air speed, 10 5Hour -1 | The NO conversion ratio, heavy % |
| 56 | C 1 | Example 5 | 500 | 500 | 2 | 300 | 1.5 | 48 |
| 57 | C 1 | Example 46 | 100 | 500 | 2 | 300 | 1.5 | 91 |
| 58 | C 1 | Example 46 | 1000 | 1000 | 10 | 200 | 0.5 | 21 |
| 59 | C 1 | Example 46 | 500 | 1000 | 1 | 400 | 2.0 | 62 |
| 60 | C 1 | Example 46 | 500 | 500 | 5 | 350 | 2.5 | 54 |
| 61 | C 2 | Example 47 | 500 | 500 | 2 | 250 | 1.5 | 34 |
| 62 | C 2 | Example 47 | 500 | 500 | 2 | 350 | 3.0 | 60 |
| 63 | C 2 | Example 47 | 750 | 750 | 5 | 450 | 1.5 | 57 |
| 64 | C 3 | Example 48 | 500 | 500 | 2 | 150 | 1.5 | 11 |
| 65 | C 3 | Example 48 | 500 | 500 | 2 | 550 | 0.5 | 47 |
| 66 | C 3 | Example 48 | 500 | 750 | 3 | 400 | 2.0 | 91 |
| 67 | C 5 | Example 49 | 500 | 500 | 2 | 300 | 1.0 | 27 |
| 68 | C 5 | Example 49 | 300 | 500 | 2 | 500 | 3.5 | 43 |
| 69 | C 7 | Example 49 | 50 | 500 | 3 | 200 | 4.0 | 71 |
| 70 | C 24 | Example 53 | 750 | 1000 | 3 | 450 | 4.0 | 41 |
| 71 | C 24 | Example 53 | 500 | 600 | 4 | 350 | 5.0 | 23 |
| 72 | C 5 | Example 49 | 300 | 500 | 2 | 300 | 1.0 | 51 |
Example 73～75
Following example illustrates method provided by the invention.
Method by example 56 is taken off nitric oxide, and different is that catalyst is respectively catalyst C
1, the catalyst C of example 47 described conditions after 900 ℃ of heat treatment
1With press the catalyst C of example 46 described conditions after 600 ℃ of hydrothermal treatment consists
1, reaction raw materials is for containing NO 500ppm, NH
3500ppm, O
20.9 the argon gas of heavy %, the gas volume air speed is 7.2 * 10
4Hour
-1, pressure be under normal pressure, the differential responses temperature nitric oxide production conversion ratio successively shown among Figure 13 22,23 and 24.
Comparative Examples 3～5
The denitrifying oxide performance of following Comparative Examples explanation Cu ZSM-5 zeolite catalyst.
Method by example 73～75 is taken off nitric oxide, and different is that catalyst is respectively Comparative Examples 2 described CuZSM-5 zeolite catalysts, and (the reference catalyst note is made B
2), press the example 46 reference catalyst Bs of described condition after 600 ℃ of hydrothermal treatment consists
2With the example 47 reference catalyst Bs of described condition after 900 ℃ of heat treatment
2, nitric oxide production conversion ratio is successively shown in 25 among Figure 14,26 and 27 under the differential responses temperature.
From the result of Figure 13 and Figure 14 as can be seen, method catalyst system therefor provided by the invention is after hydrothermal treatment consists, when being higher than 550K, reaction temperature has the higher catalytic activity of more untreated catalyst, after 900 ℃ of heat treatment, more untreated catalyst all has higher catalytic activity under each reaction temperature.And the CuZSM-5 zeolite catalyst is after hydro-thermal or heat treatment, and its activity but descends significantly.Lot of documents is (as Catalysis Today, 26,99,1995; J.Catal., 161,43,1996; Zeolite, 13,602,1993) also obtain similar result, this has seriously limited this Application of Catalyst.And method catalyst system therefor provided by the invention has rule in contrast to this, and after heat and hydrothermal treatment consists, its activity does not only reduce, and is greatly improved on the contrary.This has very important significance for the reaction of the denitrifying oxide under high temperature moisture vapor atmosphere, illustrates that method provided by the invention has broad prospects in the practical application in environmental protection field.
Example 76
Following example illustrates activity of such catalysts stability provided by the invention.
Take by weighing the catalyst C of example 28 preparations
24100 milligrams, in the example 39 described reactors of packing into, to contain NO500ppm, NH
3500ppm, O
20.9 the argon gas of heavy % is that reaction raw materials is estimated its activity, 300 ℃ of reaction temperatures, and the pressure normal pressure, the gas volume air speed is 7.2 * 10
4Hour
-1, the nitric oxide conversion ratio over time as shown in figure 15.
The result of Figure 15 shows, adopts method provided by the invention, when being reducing agent with ammonia, and 300 ℃ of reaction temperatures, the pressure normal pressure, the gas volume air speed is 7.2 * 10
4Hour
-1Condition under, when beginning reaction, the nitric oxide conversion ratio is about 20 heavy %, prolongs with the reaction time, the nitric oxide conversion ratio progressively improves and is stabilized in level near 40 heavy %, reacts 1000 hours activity and does not fall as follows.This illustrates that method provided by the invention has long service cycle.
Example 77～92
Following example illustrates method provided by the invention.
Catalyst C with example 30～45 preparations
26～C
41Each 100 milligrams of internal diameter of packing into is in 6 millimeters the U type pipe reactor, to contain NO, NH
3And O
2Argon gas be reaction raw materials, remove nitric oxide wherein, reaction pressure is NO, NH in normal pressure, the reaction raw materials
3And O
2Content and differential responses temperature and air speed under nitric oxide production conversion ratio shown in table 36.
Comparative Examples 6～15 (DB6～DB15)
The denitrifying oxide method of reference catalyst is adopted in following Comparative Examples explanation.
Remove nitric oxide in the same materials by the method for example 80,84～85 and 90～92, different is that catalyst system therefor is respectively reference catalyst B
3, B
4, B
5, B
6, B
7, B
8, B
9, B
10, B
11And B
12Reaction condition and evaluation result are listed in the table 36.
Wherein, reference catalyst B
3, B
4, B
5Adopt the preparation of following method: take by weighing silica alumina ratio and be 80 HZSM-5 zeolite (Chang Ling oil plant catalyst plant products) 2 and restrain, mix with the Schweinfurt green solution of 50 milliliters of 0.01M, stir, at room temperature carry out ion-exchange 8 hours, filter, exchange twice under the same conditions again, filter, 110 ℃ of dryings 12 hours, 550 ℃ of roastings 12 hours, the fresh CuZSM-5 catalyst B of cupric 2.0 heavy %
3Fresh CuZSM-5 catalyst heat-treated with hydrothermal treatment consists by example 47 and 46 described conditions respectively obtain 900 ℃ of CuZSM-5 catalyst B after the heat treatment respectively
4With the CuZSM-5 catalyst B after 600 ℃ of hydrothermal treatment consists
5
Reference catalyst B
6, B
7, B
8Adopt the preparation of following method: taking by weighing 50 gram silica alumina ratios and be 16 HZSM-5 zeolite (dying of Shanghai seven factories product) and 500 ml concns is the FeCl of 0.1 mol
2Solution mixes, and carries out ion-exchange 2 hours at 90 ℃, spends the deionised water solid product to there not being chlorion, drying, and 500 ℃ of roastings 2 hours obtain the fresh FeZSM-5 catalyst B of iron content 2.52 heavy %
6Fresh FeZSM-5 catalyst heat-treated with hydrothermal treatment consists by example 47 and 46 described conditions respectively obtain 900 ℃ of FeZSM-5 catalyst B after the heat treatment respectively
7With the FeZSM-5 catalyst B after 600 ℃ of hydrothermal treatment consists
8
Reference catalyst B
9, B
10, B
11Adopt the preparation of following method: silica alumina ratio is that 16 HZSM-5 zeolite (ditto) is reference catalyst B
9The HZSM-5 zeolite heat-treated with hydrothermal treatment consists by example 47 and 46 described conditions respectively obtain 900 ℃ of HZSM-5 catalyst B after the heat treatment respectively
10With the HZSM-5 catalyst B after 600 ℃ of hydrothermal treatment consists
11
B
12Porous iron-aluminium alloy RFA2 for example 3 preparations.
The result of table 36 shows, compares with the method that adopts CuZSM-5, FeZSM-5, HZSM-5 and porous iron-aluminium alloy to make catalyst, and method provided by the invention has higher nitric oxide conversion ratio.Compare when adopting fresh CuZSM-5 with the FeZSM-5 catalyst, when adopting CuZSM-5 after hydro-thermal and heat treatment and FeZSM-5 catalyst, it takes off nitric oxide production activity and all significantly descends.Simple HZSM-5 zeolite and porous iron-aluminium alloy denitrifying oxide activity is very low, does not even have the activity of denitrifying oxide.And adopt method provided by the invention, catalyst system therefor is the catalyst through hydrothermal treatment consists or high-temperature heat treatment, this illustrates that method catalyst system therefor provided by the invention has the stability of good heat resistanceheat resistant and hydro-thermal and good activity stability, and this is that prior art is incomparable.
Table 36
| Example number | Catalyst | Reaction temperature, ℃ | Volume space velocity, 10 5Hour -1 | NO concentration, ppm | NH 3Concentration, ppm | O 2Concentration, body % | The NO conversion ratio, heavy % |
| 77 | | 300 | 0.72 | 500 | 500 | 2 | 89.6 |
| 78 | | 300 | 0.36 | 500 | 200 | 0.9 | 81.1 |
| 79 | | 300 | 1.44 | 300 | 500 | 2 | 87.9 |
| 80 | C 29 | 350 | 0.72 | 300 | 500 | 10 | 93.3 |
| 81 | | 400 | 2.88 | 500 | 500 | 2 | 90.0 |
| 82 | C 31 | 350 | 0.72 | 500 | 500 | 0.9 | 90.7 |
| 83 | C 32 | 350 | 0.72 | 500 | 500 | 0.9 | 91.3 |
| 84 | C 33 | 350 | 0.72 | 300 | 500 | 10 | 93.0 |
| 85 | C 34 | 350 | 0.72 | 300 | 500 | 10 | 93.0 |
| 86 | | 400 | 0.72 | 500 | 500 | 0.9 | 95.2 |
| 87 | | 300 | 0.72 | 500 | 500 | 3 | 87.1 |
| 88 | C 37 | 450 | 1.44 | 200 | 500 | 5 | 90.0 |
| 89 | | 400 | 0.36 | 1000 | 1000 | 5 | 100 |
| 90 | C 39 | 350 | 0.72 | 300 | 500 | 10 | 85.5 |
| 91 | C 40 | 350 | 0.72 | 300 | 500 | 10 | 88.6 |
| 92 | C 41 | 350 | 0.72 | 300 | 500 | 10 | 83.1 |
| DB6 | B 3 | 350 | 0.72 | 300 | 500 | 10 | 40.0 |
| DB7 | B 4 | 350 | 0.72 | 300 | 500 | 10 | 18.5 |
| DB8 | B 5 | 350 | 0.72 | 300 | 500 | 10 | 7.4 |
| DB9 | B 6 | 350 | 0.72 | 300 | 500 | 10 | 56.0 |
| DB10 | B 7 | 350 | 0.72 | 300 | 500 | 10 | 50.3 |
| DB11 | B 8 | 350 | 0.72 | 300 | 500 | 10 | 32.1 |
| DB12 | B 9 | 350 | 0.72 | 300 | 500 | 10 | 15.0 |
| DB13 | B 10 | 350 | 0.72 | 300 | 500 | 10 | 8.5 |
| DB14 | B 11 | 350 | 0.72 | 300 | 500 | 10 | 1.1 |
| DB15 | B 12 | 350 | 0.72 | 300 | 500 | 10 | 0 |
Example 93
Following example illustrates method provided by the invention.
Catalyst C with example 30 preparations
26100 milligrams of internal diameters of packing into are in 6 millimeters the U type pipe reactor, to contain NO, NH
3And O
2Argon gas be that reaction raw materials is estimated it and taken off nitric oxide production activity, reaction pressure is that the content of NO in normal pressure, the reaction raw materials is 700ppm, NH
3Content be 700ppm, O
2Content be 1 body %, the reaction raw materials volume space velocity is 4 * 10
5Hour
-1The NO conversion ratio with the variation of reaction temperature shown among Figure 16 28.
Comparative Examples 16
The denitrifying oxide method of reference catalyst is adopted in the explanation of this Comparative Examples.
Method by example 93 is taken off nitric oxide, and different is to use reference catalyst B
6Replace catalyst C
26, the NO conversion ratio with the variation of reaction temperature shown among Figure 16 29.
Comparative Examples 17～18
The denitrifying oxide method of reference catalyst is adopted in following Comparative Examples explanation.
Press the activity of the method evaluate catalysts of example 93, different is to use reference catalyst B respectively
9And B
12Replace catalyst C
26, catalyst is C
26, B
9And B
12The time the NO conversion ratio with the variation of reaction temperature respectively shown among Figure 17 30,31 and 32.
Example 94
This example illustrates method provided by the invention.
Press the catalyst C of example 46 described methods to example 30 preparations
26Carry out hydrothermal treatment consists, the different temperature of just handling are 550 ℃.Method by example 93 is taken off nitric oxide, and different just catalyst system therefors is the catalyst C after 550 ℃ of hydrothermal treatment consists
26Catalyst is C
26And the catalyst C after 550 ℃ of hydrothermal treatment consists
26The time the NO conversion ratio with the variation of reaction temperature successively shown among Figure 18 33 and 34.
Comparative Examples 19～20
The denitrifying oxide method of reference catalyst is adopted in following Comparative Examples explanation.
Press example 46 described methods to B
6Carry out hydrothermal treatment consists, the different temperature of just handling are 550 ℃.Press the activity of the method evaluate catalysts of example 94, different is to use reference catalyst B respectively
6With the B after the hydrothermal treatment consists
6Replace catalyst C
26With the catalyst C after hydrothermal treatment consists
26, the NO conversion ratio with the variation of reaction temperature successively shown among Figure 19 35 and 36.
Example 95
This example illustrates method provided by the invention.
Press the catalyst C of example 46 described methods to example 30 preparations
26Carry out hydrothermal treatment consists.Method by example 93 is taken off nitric oxide, and different just catalyst system therefors is the catalyst C after 600 ℃ of hydrothermal treatment consists
26Catalyst is C
26And the catalyst C after 600 ℃ of hydrothermal treatment consists
26The time the NO conversion ratio with the variation of reaction temperature successively shown among Figure 20 37 and 38.
Comparative Examples 21～22
The denitrifying oxide method of reference catalyst is adopted in following Comparative Examples explanation.
Method by example 93 is taken off nitric oxide, and different just catalyst system therefors are respectively reference catalyst B
6And B
8, the NO conversion ratio with the variation of reaction temperature successively shown among Figure 21 39 and 40.
Example 96
This example illustrates the stability of method provided by the invention.
Catalyst C with example 45 preparations
41100 milligrams of internal diameters of packing into are in 6 millimeters the U type pipe reactor, to contain NO700ppm, NH
3700ppm, H
2O10 body % and O
2The argon gas of 5 body % is a reaction raw materials, at 400 ℃ of reaction temperatures, reaction pressure normal pressure, and reaction raw materials gas volume space velocity 8 * 10
4Hour
-1Condition under remove NO in the described raw material.Switch during reaction to 250 hour and contain and SO
2The argon gas of 50ppm is a reaction raw materials.Again switch during reaction to 390 hour and contain NO700ppm, NH
3700ppm, H
2O10 body % and O
2The argon gas of 5 body % is a reaction raw materials.The NO conversion ratio with the variation in reaction time as shown in figure 22.
Comparative Examples 23
This Comparative Examples explanation stability of the denitrifying oxide method of existing catalyst.
With reference catalyst B
6100 milligrams of internal diameters of packing into are in 6 millimeters the U type pipe reactor, to contain NO700ppm, NH
3700Ppm and O
2The argon gas of 10 body % is a reaction raw materials, at 450 ℃ of reaction temperatures, reaction pressure normal pressure, and reaction raw materials gas volume space velocity 8 * 10
4Hour
-1Condition under remove NO in the described raw material.Switch during reaction to 4 hour and contain NO700ppm, NH
3700ppm, O
25 body %, H
2The argon gas of O10 body % is a reaction raw materials.The NO conversion ratio with the variation in reaction time as shown in figure 23.
Example 97
This example illustrates method provided by the invention.
Catalyst C with example 30 preparations
26100 milligrams of internal diameters of packing into are in 6 millimeters the U type pipe reactor, to contain NO500ppm, CO1000ppm, H
2O10 body % and O
20.3 the argon gas of body % is a reaction raw materials, at the reaction pressure normal pressure, and reaction raw materials gas volume space velocity 8 * 10
4Hour
-1Condition under remove nitric oxide in the reaction raw materials.The NO conversion ratio with the variation of reaction temperature shown among Figure 24 41.
Comparative Examples 24～25
The following Comparative Examples explanation denitrifying oxide method of existing catalyst.
Press the method denitrifying oxide of example 97, different just catalyst system therefors are respectively B
6And B
12The NO conversion ratio with the variation of reaction temperature successively shown among Figure 24 42 and 43.
Example 98
This example illustrates method provided by the invention.
Catalyst C with example 30 preparations
26100 milligrams of internal diameters of packing into are in 6 millimeters the U type pipe reactor, to contain NO500ppm, CO 10000ppm, SO
250ppm, H
2O10 body % and O
20.3 the argon gas of body % is a reaction raw materials is 400 ℃ in reaction temperature, reaction pressure normal pressure, reaction raw materials gas volume space velocity 8 * 10
4Hour
-1Condition under remove nitric oxide in the reaction raw materials.The NO conversion ratio with the variation in reaction time shown among Figure 25 44.
Comparative Examples 26
The following Comparative Examples explanation stability of the denitrifying oxide method of existing catalyst.
Press the method denitrifying oxide of example 98, different just catalyst system therefors are B
6The NO conversion ratio with the variation in reaction time shown among Figure 25 45.
In many waste gas, in vehicle exhaust, not only contain nitrogen oxide generally speaking, also contain sulfur oxide, these sulfur oxides have intoxication to catalyst, and therefore, the sulfur resistance of catalyst is the important performance of catalyst.The result of Figure 25 shows that method sulfur resistance provided by the invention also obviously is better than
Prior art.
Example 99
Following example illustrates method provided by the invention.
Catalyst C with example 45 preparations
41100 milligrams of internal diameters of packing into are in 6 millimeters the U type pipe reactor, to contain NO500ppm, C
3H
6500ppm, C
4H
7500ppm, H
2O10 body % and O
2The argon gas of 5 body % is a reaction raw materials, is 500 ℃ in reaction temperature, reaction pressure normal pressure, reaction raw materials gas volume space velocity 8 * 10
4Hour
-1Condition under remove nitric oxide in the reaction raw materials.The NO conversion ratio with the variation in reaction time shown among Figure 26 46.
Comparative Examples 27
The following Comparative Examples explanation stability of the denitrifying oxide method of existing catalyst.
Press the method denitrifying oxide of example 99, different just catalyst system therefors are B
1The NO conversion ratio with the variation in reaction time shown among Figure 26 47.
Claims (22)
1. the removal methods of a nitrogen oxide is included under the condition of denitrifying oxide, the reaction raw materials of nitrogen-containing oxide is contacted with a kind of catalyst, it is characterized in that, described catalyst contains a kind of ZSM-5 zeolite and porous metal composite material, this composite contains Lacunaris metal carrier and the ZSM-5 zeolite of direct crystallization on this Lacunaris metal carrier, and described Lacunaris metal carrier contains a kind of nickel porous-aluminium, iron-aluminium or copper-aluminium alloy at least.
2. method according to claim 1, it is characterized in that, described Lacunaris metal carrier is nickel porous-aluminium, iron-aluminium or copper-aluminium alloy itself, or outer surface and/or inner surface contain the Lacunaris metal carrier of one deck nickel porous-aluminium, iron-aluminium or copper-aluminium alloy.
3. method according to claim 1 is characterized in that, is benchmark with nickel porous-aluminium, iron-aluminium or copper-aluminium alloy, and the specific surface of described Lacunaris metal carrier is greater than 5 meters
2/ gram, pore volume is greater than 0.05 milliliter/gram.
4. method according to claim 3 is characterized in that the specific surface of described Lacunaris metal carrier is greater than 10 meters
2/ gram, pore volume is greater than 0.07 milliliter/gram.
5. method according to claim 1 is characterized in that, described catalyst has following main X-ray diffract spectral line:
The d value, dust Relative intensity
11.20 15～35
9.95 15～30
3.84 30～70
3.72 10～30
3.63 5～15
2.41 80～95
2.08 100
6. method according to claim 1 is characterized in that, described catalyst has following main X-ray diffract spectral line:
The d value, dust Relative intensity
11.20 15～35
9.95 15～30
3.84 30～70
3.72 10～30
3.63 5～15
2.53 100
2.32 80～95
7. method according to claim 1 is characterized in that, described catalyst has following main X-ray diffract spectral line:
The d value, dust Relative intensity
11.20 15～35
9.95 15～30
3.84 30～70
3.72 10～30
3.63 5～15
2.50 100
8. method according to claim 1 is characterized in that, the framework aluminum of ZSM-5 zeolite is partly or entirely from aluminium contained in nickel porous-aluminium, iron-aluminium or the copper-aluminium alloy in the described catalyst.
9. method according to claim 1, it is characterized in that, be benchmark with the gross weight of nickel porous-aluminium, iron-aluminium or copper-aluminium alloy and zeolite, and the content of nickel, iron or copper is 25～95 heavy % in the composite, the content of aluminium is 0.1～10 heavy %, and the content of silicon is 3～40 heavy %.
10. method according to claim 9 is characterized in that, the content of nickel, iron or copper is 35～85 heavy % in the composite, and the content of aluminium is 0.1～5 heavy %, and the content of silicon is 5～30 heavy %.
11. method according to claim 1 is characterized in that, described catalyst also contains metal ion, and described metal ion is selected from one or more in IB, IIB family, IIIB family and the group VIII metal ion.
12. method according to claim 11 is characterized in that, described metal ion is one or more in copper ion, iron ion and the nickel ion.
13. method according to claim 11, it is characterized in that, gross weight with nickel porous-aluminium, iron-aluminium or copper-aluminium alloy, zeolite and metal ion oxide is a benchmark, the content of nickel, iron or copper is 25～95 heavy % in the catalyst, aluminium content is 0.1～10 heavy %, silicone content is 3～40 heavy %, and the content of metal ion is 0.1～10 heavy %.
14. method according to claim 13 is characterized in that, the content of nickel, iron or copper is 35～85 heavy % in the catalyst, and aluminium content is 0.1～5 heavy %, and silicone content is 5～30 heavy %, and the content of metal ion is 0.1～5 heavy %.
15. method according to claim 1, it is characterized in that, contain at least a reducing agent in the reaction raw materials of described nitrogen-containing oxide, described reducing agent refers to anyly have the gas of reproducibility or can change in the material of gas of reproducibility one or more under reaction condition.
16. method according to claim 15 is characterized in that, described reducing agent is selected from ammonia, carbon monoxide, has the hydro carbons of 1～10 carbon atom.
17. method according to claim 16 is characterized in that, described reducing agent is selected from ammonia, carbon monoxide, have 1～10 carbon atom alkane, have 1～10 carbon atom alkene and two or more mixture wherein.
18. method according to claim 15 is characterized in that, the volume ratio of described reducing agent and nitrogen oxide is more than 0.01.
19. method according to claim 18 is characterized in that, the volume ratio of described reducing agent and nitrogen oxide is more than 0.1.
20. method according to claim 19 is characterized in that, the volume ratio of described reducing agent and nitrogen oxide is 0.2～50.
21. method according to claim 1 is characterized in that, the condition of described denitrifying oxide comprises that reaction temperature is 100～600 ℃, and the gas volume air speed is not for being higher than 10
10Hour
-1
22. method according to claim 1 is characterized in that, the condition of described denitrifying oxide comprises that reaction temperature is 200～550 ℃; Reaction pressure is a normal pressure; The gas volume air speed is 10～10
8Hour
-1
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN99109302A CN1108849C (en) | 1999-06-23 | 1999-06-23 | Process for removing nitrogen oxide |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN99109302A CN1108849C (en) | 1999-06-23 | 1999-06-23 | Process for removing nitrogen oxide |
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| Publication Number | Publication Date |
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| CN1279123A CN1279123A (en) | 2001-01-10 |
| CN1108849C true CN1108849C (en) | 2003-05-21 |
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| CN99109302A Expired - Lifetime CN1108849C (en) | 1999-06-23 | 1999-06-23 | Process for removing nitrogen oxide |
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| CN101530742B (en) * | 2009-03-11 | 2011-06-08 | 上海大学 | Desulphurization denitration catalytic filler used for catalytic desulfurization tower and preparation method thereof |
| JP5748894B1 (en) * | 2014-11-07 | 2015-07-15 | 三菱重工業株式会社 | Exhaust gas treatment method and denitration / SO3 reduction device |
| CN107321177B (en) * | 2017-07-13 | 2020-07-14 | 华中科技大学 | Method for removing various pollutants in sintering flue gas by using magnetic stabilized bed |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5078981A (en) * | 1989-10-02 | 1992-01-07 | Tosoh Corporation | Method for catalytically decomposing nitrogen oxides |
| JPH05317649A (en) * | 1992-05-21 | 1993-12-03 | Toyota Motor Corp | Method for purifying exhaust gas |
| US5270024A (en) * | 1989-08-31 | 1993-12-14 | Tosoh Corporation | Process for reducing nitrogen oxides from exhaust gas |
| JPH0699072A (en) * | 1992-09-22 | 1994-04-12 | Toyota Motor Corp | Catalyst for purification of exhaust gas |
| JPH0857259A (en) * | 1994-08-23 | 1996-03-05 | Hitachi Ltd | Purification of exhaust gas from internal combustion engine |
-
1999
- 1999-06-23 CN CN99109302A patent/CN1108849C/en not_active Expired - Lifetime
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5270024A (en) * | 1989-08-31 | 1993-12-14 | Tosoh Corporation | Process for reducing nitrogen oxides from exhaust gas |
| US5078981A (en) * | 1989-10-02 | 1992-01-07 | Tosoh Corporation | Method for catalytically decomposing nitrogen oxides |
| JPH05317649A (en) * | 1992-05-21 | 1993-12-03 | Toyota Motor Corp | Method for purifying exhaust gas |
| JPH0699072A (en) * | 1992-09-22 | 1994-04-12 | Toyota Motor Corp | Catalyst for purification of exhaust gas |
| JPH0857259A (en) * | 1994-08-23 | 1996-03-05 | Hitachi Ltd | Purification of exhaust gas from internal combustion engine |
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| Publication number | Publication date |
|---|---|
| CN1279123A (en) | 2001-01-10 |
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