CN1951558A - Method for preparing catalyst composition - Google Patents
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- CN1951558A CN1951558A CN 200510047532 CN200510047532A CN1951558A CN 1951558 A CN1951558 A CN 1951558A CN 200510047532 CN200510047532 CN 200510047532 CN 200510047532 A CN200510047532 A CN 200510047532A CN 1951558 A CN1951558 A CN 1951558A
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Abstract
The invention relates to a method for preparing catalyst compound. Wherein, it uses deposition method to generate the forward body of NixWyOz compound oxide; then mixing and beating with MoO3, filtering, shaping and activating to obtain the final catalyst. The deposition process comprises that adding the salt mixture with active metals Ni and W into the reaction pot, combining it with alkali deposit agent, to be put into reaction pot to form paste; the pH value of reaction pot is 7.0-9.0; obtaining the gel mixture as the forward body. The invention can improve the catalyst property, with high metal content.
Description
Technical field
The present invention relates to a kind of preparation method of carbon monoxide-olefin polymeric, bulk phase catalyst preparation of compositions method particularly, the body phase method Preparation of catalysts method that specifically is used for hydrocarbon oil hydrogenation conversion or hydrotreatment, the preparation method who takes off the bulk phase catalyst of impurity process especially for hydrocarbon ils deep desulfuration, denitrogenation etc.
Background technology
Contain impurity and aromatic hydrocarbons (especially condensed-nuclei aromatics) such as S, N in the fuel oil, in use can form harmful substances such as SOx, NOx and solid particle, not only harm humans self health also can form acid rain in air, causes bigger pollution and destruction.In recent ten years, comprise that the many families that enclose of North America, Europe, Japan propose the notions of ultra-low-sulphur diesel (ULSD) and constantly formulate the content that new fuel oil standard limits sulphur in motor petrol and the diesel oil, aromatic hydrocarbons etc., improve oil quality, reduce environmental pollution.
When world wide fuel oil standard was more harsh to the index of communications and transportation fuel, the raw material poor qualityization made the refinery need seek raw catelyst and is guaranteeing to satisfy product demand under the prerequisite that the refinery makes a profit.Because crude quality descends in the product in the diesel oil distillate sulfur content require more and more strictlyer, the conventional Hydrobon catalyst that only can remove general sulfur-containing compound is just inadequate slightly, therefore the demand to the sulfur-containing compound that removes the most difficult conversion is just more and more stronger.Therefore need catalyst that higher hydrodesulfurization performance is arranged.Common Hydrobon catalyst is more or less freely carrying out when removing no sterically hindered or sulfur-containing compound that steric hindrance is little, but when handling sterically hindered bigger sulfur-containing compound, for example 4,6-dimethyl Dibenzothiophene (4, poor effect in the time of 6-DMDBT), therefore, improve the ultra-deep hydrodesulfuration ability of catalyst, realize that especially the difficult conversion that removes sulfur containing species is the key that realizes super clean fuel.
Industrial Hydrobon catalyst comprises supported hydrodesulphurizatiocatalyst catalyst and body method Hydrobon catalyst mutually.The former adopts refractory metal oxides such as aluminium oxide is carrier, and metals such as Ni, Co, Mo, W are the most commonly used as active component.Owing to be subjected to the restriction of metal component loading, during such catalyst processing ordinary diesel oil, be difficult to obtain the following low-sulfur diesel-oil of sulfur-bearing 50 μ g/g, more difficult satisfied following sulfur-bearing is lower than the ultra-low-sulphur diesel standard of 10 μ g/g.And body phase method catalyst can be broken away from the tenor restriction, the ratio of each active component in the regulating catalyst arbitrarily simultaneously improves the hydrogenation performance of catalyst, realizes the ultra-deep desulfurization conversion of diesel oil, obtain sulfur content less than 10 μ g/g, even lower ultra-low-sulphur diesel.
U.S. Pat 4880526 discloses a kind of Ni of containing, Mo, W, the Co high activity is used for bulk phase catalyst of hydrotreatment and preparation method thereof.This method is the preparation alumina gel earlier, and adding contains active metal component solubility salt and mixes dry, roasting then.After also can taking in addition to prepare alumina gel earlier, drying and contains active metal component non-solubility salt and mixes, and rolls, dry, roasting.Perhaps the different activities metal component adopt different above-mentioned dual modes any one be prepared.There is the lower problem of using rate of metal in the similar kneading method of this method.
Bulk phase catalyst refers to that the loaded catalyst that is dispersed on the carrier with active constituent is relative, is not carrier with inactive carrier, even contain a certain amount of nonactive component, also has been the cementation that improves intensity.The catalyst major part is made of active component, and the content of active constituent is generally unrestricted, also claims body catalyst sometimes.
Chinese patent CN1253988A, CN1253989A disclose a kind of body and have been used for the Catalysts and its preparation method that heavy hydrocarbon transforms mutually.This catalyst adopts glue method preparation altogether, can obtain more even metal dispersion, and the flow process that adopts first extruded moulding to wash again.Metal salt solution is mixed with molecular sieve pulp, add precipitating reagent then.The anti-nitrogen ability of hydrocracking catalyst that adopts this method to prepare is strong also can voluminous intermediate oil.At the prepared catalyst of said method mainly is hydrocracking reaction at heavy distillate, and unifining process is not described.
U.S. Pat 6299760, US6156695, US6537442, US6440888, US6652738 disclose a kind of VIII of containing family/group vib active metal component and have been used for bulk phase catalyst of hydrotreatment and preparation method thereof.Preparation of catalysts can adopt solution route or solid route.Tenor can reach 50wt%-100wt%.Active metal component can be Ni-Mo or Ni-Mo-W.Can contain or not contain adhesive component in the catalyst.Adhesive is mainly used to bonding metal, improves the intensity of catalyst.Adopt the catalyst of this method preparation to have higher H DS and HDN performance.
U.S. Pat 4880526 disclosed preparation methods adopt metal to mix kneading to be equipped with technology, and the different metal component distributes under the microcosmic in mutually also inhomogeneous at body.The method of patent disclosures such as U.S. Pat 6299760 is a kind of comparatively excellent bulk phase catalysts of hydrotreatment and preparation method thereof that are used for, but in its patent in the related Preparation of Catalyst, the moulding of catalyst is adopted and prepared the metal dust that contains Ni-Mo or Ni-Mo-W earlier, and is bonding or the metal dust of Ni-Mo or Ni-Mo-W mixed dehydration afterwards, extrusion, drying with alumina gel with aluminium oxide again.Because the catalyst metal content height of this method preparation often lacks enough interactions and can cause catalyst strength poor between metal and aluminium oxide.Active component part is made up of a large amount of metals, has some interior metal components and can not be fully utilized and cause loss of activity in forming Ni-Mo or Ni-Mo-W powder process, and this problem can not be by simple bonding the solution.CN1342102A discloses a kind of mixed metal catalyst, and concrete grammar is for to obtain three kinds of reactive metal co-precipitation, and its main weak point is not find the cooperation effect between the different activities metal.US6162350, CN1339985A disclose a kind of mixed metal catalyst composition, and it is solid-state keeping at least a metal in preparation process, forms another kind of soild oxide in this solid metallic compound surface reaction, finally forms the core-shell type composition.The method can not make different metal obtain good cooperation.
In the catalyst of body phase method preparation, because tenor is higher, the mating reaction between its dissimilar metals is very important.In the prior art, only emphasize the kind and the content of metal, the cooperation effect that how to improve between the different metal is not related to.
Summary of the invention
At the deficiencies in the prior art, the invention provides a kind of body phase method Preparation of catalysts method, by special preparation process, make the different metal in the body phase method catalyst obtain good cooperation effect, further improve the serviceability of catalyst.
By discovering, in body phase method catalyst, under the close situation of metal species and content, the cooperation of different metal can make catalyst have different serviceabilities.Based on above-mentioned discovery, the present invention proposes a kind of preparation method of bulk phase catalyst.
The preparation process of bulk phase catalyst of the present invention comprises following content: (1) coprecipitation prepares Ni
xW
yO
zThe composite oxides precursor; (2) Ni
xW
yO
zComposite oxides precursor and MoO
3Making beating mixes, filters; (3) moulding, activation are final catalyst.
Wherein (1) described coprecipitation prepares Ni
xW
yO
zThe process of composite oxides precursor, adopt following process: the saline mixed solution that contains reactive metal Ni, W component by the preparation of catalytic component content proportioning, add in the retort that water purification is housed with alkaline precipitating agent and stream then and become glue, the pH value of slurries is in the 7.0-9.0 scope in the retort, making gelatinous precipitate, promptly is composite oxides Ni
xW
yO
zPrecursor.Precipitating reagent can be inorganic or organic alkaline ammoniac compounds, is preferably ammonia, can working concentration ammoniacal liquor arbitrarily.
Add required catalyst promoter and add component in a step that can be in above-mentioned steps or a few step.Auxiliary agent generally comprise P, F, Ti, Si, B, Zr etc. one or more.Add component and be generally refractory porous mass and precursor thereof,, preferably add aluminium oxide or its precursor as in aluminium oxide and precursor (aluminium hydroxide, aluminum salt solution etc.), clay, sial, titanium oxide-magnesia and the molecular sieve etc. one or more.The method that adds auxiliary agent and interpolation component adopts this area conventional method.
Among the carbon monoxide-olefin polymeric preparation method of the present invention, the consumption of each raw material is determined as required, general composite oxides Ni
xW
yO
zWith oxide M oO
3Weight ratio be 1: 10～10: 1, be preferably 1: 5～5: 1.Composite oxides Ni in the bulk phase catalyst
xW
yO
zWith oxide M oO
3Gross weight content be 40%～100%, be preferably 50%～80%, can contain simultaneously other auxiliary agent and add component.Described Ni
xW
yO
zMiddle z=x+3y, composite oxides Ni
xW
yO
zThe ratio of middle x and y is 1: 8～8: 1, is preferably 1: 4～4: 1.The specific area of prepared bulk phase catalyst is 120～400m
2/ g, pore volume are 0.10～0.50ml/g.
Though W, Mo, Ni are activity of hydrocatalyst component commonly used, find that through a large amount of The effects the performance of different fit system catalyst has very big-difference.Particularly in the bigger bulk phase catalyst of total metal content, the different fit systems of these metals are bigger to the performance impact of catalyst.The present invention finds by a large amount of experiments, is used for the body phase hydrogenation catalyst that the hydrocarbon material degree of depth is taken off impurity, earlier with W and Ni co-precipitation, makes Ni
xW
yO
zThe precursor of composite oxides, this composite oxides precursor again with MoO
3Making beating mixes, and adopts conventional means to prepare preformed catalyst then, and this preparation process organically cooperates element W and Ni, forms a kind of composite oxides, then with MoO
3Combination finally forms Ni
xW
yO
zThe composition of composite oxides and Mo oxide.The result shows when the catalyst of this microstructure of the present invention is used for hydrocarbons hydrogenation, to have the outstanding impurity activity of taking off, and during especially for deep impurity removal process, significantly improves than the activity of such catalysts of similar chemical composition.The mechanism that the composition of Ni-W composite oxides of the present invention and Mo oxide can improve catalyst activity is very not clear and definite as yet, and, in bulk phase catalyst, the content of reactive metal is higher, reactive metal exist form different fully with traditional loaded catalyst, therefore, can not be suitable for the metal cooperation theory of conventional negative supported catalyst.For example, it is generally acknowledged that Ni can promote the activity of Mo to improve, wishing has a stronger interaction between Ni and the Mo, and the present invention finds in experiment, for bulk phase catalyst, Mo and Ni is fully combined then take off impurity in the degree of depth and do not show perfect performance.The composition catalyst of Ni-W composite oxides of the present invention and Mo oxide, the possible cause that takes off the unexpected raising of performance in the impurity in the degree of depth is, in the very high bulk phase catalyst of tenor, reactive metal exist form different with loaded catalyst, take off in the impurity process in the hydrocarbon raw material degree of depth, the Ni-W composite oxides have stronger hydrogenation activity after sulfuration, make to have the effective hydrogenation of labyrinth hydrocarbon molecule, eliminate and take off the sterically hindered of impurity reaction.Has the stronger impurity activity of taking off after the Mo sulfuration in the bulk phase catalyst, simple in structure, the sterically hindered little hetero atom hydrocarbon that contains is easy to react, reduced of the interference of this part hetero atom hydro carbons, helped the hydrogenation that Ni-W high activity center is used for the labyrinth molecule the Ni-W hydrogenation activity.After containing the effective hydrogenation in heteroatomic labyrinth hydrocarbon molecule process Ni-W high activity center, take off the sterically hindered of impurity and reduce greatly, can in taking off impurity activity, remove easily in the heart.Therefore, the activated centre of Ni-W composite oxides of the present invention and Mo oxide obtains cooperation, and combination catalyst takes off in the impurity reaction in the degree of depth and has outstanding activity.The inventive method is not used the salting liquid of Mo, because the product of Mo salting liquid and precipitating reagent generally has certain solubility, has therefore avoided the loss of Mo.The bulk phase catalyst that the inventive method obtains is more even.
Description of drawings
Fig. 1 is the catalyst B of the inventive method preparation, the XRD figure of C.
The specific embodiment
The invention provides the Preparation of catalysts method, a kind of detailed process step is as follows:
1, Ni
xW
yO
zComposite oxides precursor and MoO
3The preparation of mixture
The saline mixed solution that contains reactive metal Ni, W component by the preparation of catalytic component content proportioning.Contain nickel salt and can be nickelous sulfate, nickel nitrate, nickel chloride etc.Tungstenic salt can be sodium tungstate, ammonium metatungstate etc.Become glue then with in alkaline precipitating agent and stream add the retort that water purification is housed, becoming the glue temperature is 30-80 ℃, and time 0.5-3 hour, the pH value of slurries was adjusted the adding speed of two kinds of materials in the retort in the 7.0-9.0 scope, makes gelatinous mixture.Can become under the glue temperature to wear out 1-5 hour after the cemented into bundles.Becoming glue to generate sediment promptly is composite oxides Ni
xW
yO
zPrecursor.Can filter or not filter after becoming glue, add the solid molybdenum trioxide then, making beating mixes, and filters then and obtains filter cake, and filter cake can wash or not wash, and filter cake dehydrates under 50-150 ℃ of condition, 0.5～24 hour drying time, obtains Ni
xW
yO
zComposite oxides precursor and MoO
3Mixture.
Preferably 30-60 ℃ of described one-tenth glue temperature, gelation time is preferably 0.5-2 hour, and the pH value that becomes slurries in the glue process is 7.5-8.5 preferably.Preferably 50～100 ℃ of described baking temperatures are preferably 1～8 hour drying time.
Can add aluminum salt solution in the saline admixture that Ni, W form, make the precursor that contains aluminium oxide in the sediment, aluminum salt solution can be aluminum nitrate, aluminum sulfate, aluminium chloride or aluminium acetate etc.Directly add aluminium hydroxide after also can becoming glue.The purpose of introducing aluminium in the catalyst mainly is the intensity that increases catalyst, and improves pore structure etc.In the preparation process of this mixed material, can add auxiliary agent and additive etc. as required.
2, Preparation of Catalyst
The filter cake that above-mentioned drying is good rolls extruded moulding.Can or contain with water purification after the moulding and can decompose salt (as ammonium acetate) solution and wash.To wash back stripe shape thing activate final catalyst prod, activation comprises drying and roasting.Dry and roasting can be adopted this area normal condition, as 50～200 ℃ of dryings 1～48 hour, 450～600 ℃ of roastings 0.5～24 hour, is preferably 1～8 hour.Also can introduce auxiliary agent and additive as required in the catalyst preparation process.
Catalyst shape can be sheet, spherical, cylinder bar and special-shaped bar (clover, bunge bedstraw herb), preferably cylinder bar and special-shaped bar (clover, bunge bedstraw herb) as required.The diameter of carrier can be 0.8～2.0mm slice and＞the thick bar of 2.5mm.
Catalyst of the present invention has higher hydrodesulfurization and hydrodenitrogeneration reactivity worth, can be used for hydrocracking preliminary treatment and diesel fuel desulfurization technology, be particularly useful in the technologies such as Ultra-deep Desulfurization of Diesel Fuels of production super-low sulfur clean fuel, this catalyst also can be used in other hydrofinishing and the hydroprocessing technique.When containing catalysis materials such as molecular sieve in the catalyst, can also be used for courses of reaction such as hydrocracking, hydro-upgrading.
Though catalyst of the present invention is Ni from microcosmic
xW
yO
zComposite oxides and MoO
3Composition, but the dispersion of two kinds of materials is quite uniform, so can form two kinds of activated centre cooperation effects.
Fig. 1 is X-ray diffraction (XRD) spectrogram of B, C catalyst, and B, C catalyst are for adopting the catalyst of this patent method preparation, and catalyst is the bar shaped catalyst of diameter 1.3mm.As can be seen from Figure 1, no nonactive phase metallicity peak occurs on the B of employing this method preparation, the XRD spectra of C catalyst, illustrate that metal does not have the clustering phenomena generation in the catalyst, that is to say that each metallic element of Ni/Mo/W is evenly distributed in the whole bulk phase catalyst very much.
Further specify the solution of the present invention and effect below by specific embodiment.The percentage composition that relates to is a weight percentage.Specific surface area of catalyst adopts the BET method to measure, and pore volume is a determination of nitrogen adsorption, and intensity adopts the side pressure method to measure.
Embodiment 1
In dissolving tank, add 1000mL water, add nickel chloride 33g dissolving then, add ammonium metatungstate 30g dissolving again, preparating acid sex work solution A, the pH value of solution A is 1.8.Add 350mL water in retort, temperature rises to 70 ℃.Under condition of stirring, solution A is also become glue in the stream adding retort with 18% ammoniacal liquor, become 70 ℃ of glue temperature, gelation time 0.5 hour, becoming the pH value of glue slurry during is 8.5.Wore out 1 hour after the cemented into bundles.Filter then, filter cake adds 600ml water purification and 25g molybdenum trioxide and 47g aluminium hydroxide, making beating stirs, and filters, and filter cake was 80 ℃ of dryings 5 hours, extruded moulding then, with water purification washing 3 times, wet bar is 120 ℃ of dryings 5 hours, 500 ℃ of roastings 4 hours, obtain final catalyst A, composition and main character see Table 1.
Embodiment 2
According to the method for embodiment 1, press the constituent content proportioning of catalyst B in the table 1, in dissolving tank, add aluminium chloride, nickel chloride, ammonium metatungstate and zirconium oxychloride preparating acid sex work solution A.Add 350mL water in retort, temperature rises to 40 ℃.Under condition of stirring, solution A is also become glue in the stream adding retort with 10% ammoniacal liquor, become 40 ℃ of glue temperature, gelation time 2 hours, becoming the pH value of glue slurry during is 8.0.Wore out 2 hours after the cemented into bundles.Filter then, filter cake adds water purification and molybdenum trioxide with 500mL water purification washing 2 times, and making beating stirs, filter, filter cake is 70 ℃ of dryings 7 hours, and extruded moulding then is with water purification washing 2 times, wet bar was 100 ℃ of dryings 8 hours, 550 ℃ of roastings 3 hours, obtain final catalyst B, composition and main character see Table 1.
Embodiment 3
According to the method for embodiment 1, press the constituent content proportioning of catalyst C in the table 1, in dissolving tank, add nickel nitrate, Ludox, ammonium metatungstate preparating acid sex work solution A.Add 350mL water in retort, temperature rises to 50 ℃.Under condition of stirring, solution A is also become glue in the stream adding retort with 15% ammoniacal liquor, become 50 ℃ of glue temperature, gelation time 2 hours, becoming the pH value of glue slurry during is 8.5, adds molybdenum trioxide and aluminium hydroxide then, making beating stirs, filter, filter cake is at 120 ℃ of dryings 1 hour, extruded moulding then, wet bar was 130 ℃ of dryings 3 hours, 600 ℃ of roastings 3 hours, obtain final catalyst C, composition and main character see Table 1.
Embodiment 4
According to the method for embodiment 1, press the constituent content proportioning of catalyst D in the table 1, in dissolving tank, add 1000mL water, add nickel chloride 43g dissolving then, add ammonium metatungstate 31g dissolving again, 6g titanium trichloride preparating acid sex work solution A.Add 350mL water in retort, temperature rises to 60 ℃.Under condition of stirring, solution A is also become glue in the stream adding retort with 20% ammoniacal liquor, become 60 ℃ of glue temperature, gelation time 1 hour, becoming the pH value of glue slurry during is 7.5, filters then, filter cake adds 600ml water purification and 18g molybdenum trioxide and 48g aluminium hydroxide, and making beating stirs, and filters, filter cake is 80 ℃ of dryings 5 hours, and extruded moulding then is with water purification washing 3 times, wet bar was 120 ℃ of dryings 5 hours, 500 ℃ of roastings 4 hours, obtain final catalyst D, composition and main character see Table 1.
Comparative example
Catalyst according to embodiment 1 is formed, and presses the disclosed method for preparing catalyst of Chinese patent CN1342102A, preparation reference agent E.
In retort, add 1000mL water, add ammonium heptamolybdate 28g dissolving then, add ammonium metatungstate 44g dissolving again, add 25% ammoniacal liquor then and become glue, until pH value is 10.0, and being heated to temperature is 90 ℃, drips the solution that contains the 40g nickel chloride simultaneously in retort.The suspension that forms is continued to stir 90 ℃ of temperature 30 minutes.Filter then, the filter cake hot wash, 100 ℃ of dryings 5 hours add 34g aluminium hydroxide extruded moulding then, and wet bar 500 ℃ of roastings 4 hours, obtains final reference catalyst E 100 ℃ of dryings 8 hours, and composition and main character see Table 1.Prepare catalyst by this kind method, the molybdenum trioxide yield can only reach 80%, and in order to guarantee tenor and proportioning in the catalyst, ammonium heptamolybdate adds 20% when feeding intake.
The catalyst and the character of the preparation of table 1 the inventive method
| The catalyst numbering | A | B | C | D | E |
| NiO，wt％ WO 3，wt％ MoO 3，wt％ Al 2O 3, wt% other/the wt% specific surface, m 2/ g pore volume, mL/g intensity, N/mm | 18.7 24.5 24.5 surpluses do not have 182 0.375 22.6 | 12.1 26.9 29.4 surplus ZrO 2/2.0 147 0.195 25.4 | 12.5 21.5 38.7 surplus SiO 2/2.0 177 0.268 24.6 | 24.8 25.2 17.0 surplus TiO 2/3.0 142 0.172 23.1 | 18.9 24.2 24.7 surpluses do not have 118 0.148 9.7 |
Embodiment 5
Present embodiment is a catalyst hydrogenation desulphurization reaction performance evaluation.
In order to further specify the ultra-deep hydrodesulfuration ability of catalyst of the present invention, adopt A of the present invention, C catalyst and Comparative Examples E catalyst, on the 200ml small hydrogenation device, carry out comparative evaluation's test, test raw material is Maoming mixed diesel.The raw material main character sees Table 2, and catalyst activity is estimated process conditions and evaluation result sees Table 4.
Table 2 feedstock oil main character
| Project | Analysis result |
| Density (20 ℃), g/cm 3The boiling range scope, ℃ S, μ g/g N, μ g/g Cetane number | 0.8614 178-371 12200 288 46.5 |
Table 3 catalyst hydrogenation desulphurization reaction process conditions and evaluation result
| Catalyst | A | C | E |
| The hydrogen dividing potential drop, MPa reaction temperature, ℃ volume space velocity, h -1Hydrogen to oil volume ratio | 6.4 360 2.0 500 | ||
| Generate oil density (20 ℃), g/cm 3The boiling range scope, ℃ S, μ g/g N, μ g/g Cetane number | 0.8360 165-364 28 3.6 52.5 | 0.8339 168-366 32 2.9 51.9 | 0.8426 168-365 82 13.0 51.0 |
The sulfur content of diesel oil is when 500 μ g/g are following, and sulfur-containing compound all is to have sterically hindered difficulty to remove sulfur containing species.Industrial, common Hydrobon catalyst is just because of being difficult to 4-MDBT (4-MDBT), 4,6-DMDBT (4, the 6-dimethyl Dibenzothiophene) etc. have sterically hindered sulfur-containing compound and transform and can't carry out deep desulfuration, thereby be difficult to obtain in the product sulfur content less than the super clean fuel of 50 μ g/g.Have higher total metal content by table 1,3 visible body phase Ni of the present invention, Mo, W catalyst, Ni, Mo, W atomic ratio be modulation in very large range.Under same reaction conditions, adopt in the product of body phase Ni of the present invention, Mo, W catalyst sulfur content well below the reference catalyst that adopts.Therefore, adopt the catalyst of method preparation of the present invention, have higher hydrogenation performance, especially shown more tangible removal effect having sterically hindered sulfide.As seen the result adopts the bulk phase catalyst of the inventive method preparation to have excellent hydrogenation and hydrodesulfurization ability from table, can be used in hydrodesulfurization, the hydrodenitrogeneration reaction, is particularly useful for producing in the ultra-deep desulfurization reaction of super clean diesel.
Claims (12)
1, a kind of preparation method of carbon monoxide-olefin polymeric is characterized in that comprising following content: (1) coprecipitation generates Ni
xW
yO
zThe composite oxides precursor; (2) Ni
xW
yO
zComposite oxides precursor and MoO
3Making beating mixes, filters; (3) moulding, activation are final catalyst; Wherein the described coprecipitation of step (1) generates Ni
xW
yO
zThe process of composite oxides precursor is: the saline mixed solution that contains reactive metal Ni, W component by the preparation of catalytic component content proportioning, become glue with alkaline precipitating agent and stream then, the pH value of slurries is in the 7.0-9.0 scope in the retort, makes gelatinous precipitate, promptly is composite oxides Ni
xW
yO
zPrecursor.
2, in accordance with the method for claim 1, it is characterized in that can be in above-mentioned steps a step or a few step in add required catalyst promoter and add component, auxiliary agent comprises one or more among P, F, Ti, Si, B and the Zr, adds component and is as in aluminium oxide and precursor, clay, sial, titanium oxide-magnesia and the molecular sieve one or more.
3, in accordance with the method for claim 1, it is characterized in that among the carbon monoxide-olefin polymeric preparation method that the consumption of each raw material is determined as required, composite oxides Ni
xW
yO
zWith oxide M oO
3Weight ratio be 1: 10～10: 1, composite oxides Ni in the catalyst
xW
yO
zWith oxide M oO
3Gross weight content be 40%～100%; Described composite oxides Ni
xW
yO
zMiddle z=x+3y, the ratio of x and y is 1: 8～8: 1.
4, in accordance with the method for claim 1, it is characterized in that among the carbon monoxide-olefin polymeric preparation method that each raw material consumption is determined in following ratio: composite oxides Ni
xW
yO
zWith oxide M oO
3Weight ratio be 1: 5～5: 1, composite oxides Ni in the catalyst
xW
yO
zWith oxide M oO
3Gross weight content be 50%～80%, composite oxides Ni
xW
yO
zThe ratio of middle x and y is 1: 4～4: 1.
5, in accordance with the method for claim 1, it is characterized in that reactive metal Ni derives from nickelous sulfate, nickel nitrate or nickel chloride, active metal W derives from sodium tungstate or ammonium metatungstate.
6, in accordance with the method for claim 1, it is characterized in that described alkaline precipitating agent can be inorganic or organic alkaline ammoniac compounds.
7, in accordance with the method for claim 1, it is characterized in that described alkaline precipitating agent is an ammoniacal liquor.
8, in accordance with the method for claim 1, it is characterized in that described one-tenth glue temperature is 30-80 ℃.
9, in accordance with the method for claim 8, it is characterized in that described one-tenth glue temperature is 30-60 ℃.
10, in accordance with the method for claim 1, it is characterized in that the filter cake that the described filtration of step (2) obtains dehydrates 0.5～24 hour drying time under 50-150 ℃ of condition.
11, in accordance with the method for claim 1, it is characterized in that into the glue pH value is 7.5-8.5.
12, in accordance with the method for claim 1, it is characterized in that the described activation of step (3) comprises drying and roasting, drying is that roasting was 450～600 ℃ of roastings 0.5～24 hour 50～200 ℃ of dryings 1～48 hour.
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN101722007B (en) * | 2008-10-29 | 2011-11-30 | 中国石油化工股份有限公司 | Method for preparing hydrogenation catalyst composite |
| CN102049289B (en) * | 2009-10-27 | 2012-11-21 | 中国石油化工股份有限公司 | Superdeep hydrodesulfurization catalyst and preparation method thereof |
| CN102049265B (en) * | 2009-10-27 | 2013-01-09 | 中国石油化工股份有限公司 | Hydrotreating catalyst and preparation method thereof |
| CN102049281B (en) * | 2009-10-27 | 2013-01-09 | 中国石油化工股份有限公司 | Super deep hydrodesulfurization catalyst and preparation method thereof |
| CN104803435A (en) * | 2014-01-23 | 2015-07-29 | 中国科学院苏州纳米技术与纳米仿生研究所 | Sewage treatment purification agent, preparation method and applications thereof |
Family Cites Families (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4495061A (en) * | 1980-06-16 | 1985-01-22 | Chevron Research Company | Hydrocarbon conversion catalyst and process using said catalyst |
| US6635599B1 (en) * | 1997-07-15 | 2003-10-21 | Exxonmobil Research & Engineering Company | Mixed metal catalyst, its preparation by co-precipitation, and its use |
| US6929738B1 (en) * | 1997-07-15 | 2005-08-16 | Exxonmobil Research And Engineering Company | Two stage process for hydrodesulfurizing distillates using bulk multimetallic catalyst |
| CN1073617C (en) * | 1998-11-18 | 2001-10-24 | 中国石油化工集团公司 | Hydrocraking catalyst of nitrogen-resistant type multiferous middle oil |
| CA2359960C (en) * | 1999-01-15 | 2007-10-30 | Akzo Nobel N.V. | A novel mixed metal catalyst, its preparation by co-precipitation, and its use |
-
2005
- 2005-10-19 CN CNB2005100475321A patent/CN100431697C/en active Active
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN101722007B (en) * | 2008-10-29 | 2011-11-30 | 中国石油化工股份有限公司 | Method for preparing hydrogenation catalyst composite |
| CN102049289B (en) * | 2009-10-27 | 2012-11-21 | 中国石油化工股份有限公司 | Superdeep hydrodesulfurization catalyst and preparation method thereof |
| CN102049265B (en) * | 2009-10-27 | 2013-01-09 | 中国石油化工股份有限公司 | Hydrotreating catalyst and preparation method thereof |
| CN102049281B (en) * | 2009-10-27 | 2013-01-09 | 中国石油化工股份有限公司 | Super deep hydrodesulfurization catalyst and preparation method thereof |
| CN104803435A (en) * | 2014-01-23 | 2015-07-29 | 中国科学院苏州纳米技术与纳米仿生研究所 | Sewage treatment purification agent, preparation method and applications thereof |
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