CN101143333A - Hydrogenating and pour point depressing catalyst and its preparing method - Google Patents
Hydrogenating and pour point depressing catalyst and its preparing method Download PDFInfo
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- CN101143333A CN101143333A CNA2006100477868A CN200610047786A CN101143333A CN 101143333 A CN101143333 A CN 101143333A CN A2006100477868 A CNA2006100477868 A CN A2006100477868A CN 200610047786 A CN200610047786 A CN 200610047786A CN 101143333 A CN101143333 A CN 101143333A
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Abstract
The invention discloses a hydro dewaxing catalyst and the preparation method. In the method, compound with hydrogen active component is mixed with aluminum dry gel to prepare adhesive; and then the adhesive is mixed with shape-selective cracked zeolite and is pinched in shape; after drying and roasting, catalyst carrier is yielded; then the catalyst carrier is impregnated in the impregnating solution containing the rest active component and promoter; and after drying and roasting again, the catalyst of the invention is yielded. The invention is capable of taking full advantage of the alumina used as adhesive in the catalyst carrier under low hydrogen active component content conditions to prepare adhesive containing all the molybdenum and tungsten and part of the nickel, thereby keeping a certain amount of nickel oxide in the zeolite. The rest of the active metal component is distributed in the alumina, keeping the zeolite passage unobstructed with good hydro dewaxing effect and effectively improving the hydrogen addition and purification performance of the catalyst. The catalyst is especially suitable for hydro dewaxing of raw material containing wax and with high nitrogen impurity content and suitable for hydrogen addition and purification.
Description
Technical field
The present invention relates to a kind of catalyst for hydrogenation de-waxing and preparation method thereof, specifically, is a kind of Diesel Oil Hydrodewaxing Catalyst And Its Preparation Method.This catalyst is used for the hydro dewaxing process of the hydrocarbon feed of the content of wax, is specially adapted in the hydro dewaxing and unifining process of waxy feeds.
Background technology
" hydro dewaxing " means under the situation that hydrogen exists, and the hydrocarbon feed of the content of wax reduces wax molecule content wherein on the appropriate catalyst surface.Its dewaxing principle is under certain operating condition, raw material is mixed with hydrogen to be contacted with Hydrodewaxing catalyst, alkane in the raw material, band short-side chain alkane, the cycloalkane of belt length side chain and the contour condensation point component of aromatic hydrocarbons of belt length side chain optionally are cracked into little molecule, and other component does not change substantially, finally reaches the purpose of the condensation point that reduces oil product.Concrete catalytic dewaxing process is seen U.S. Patent No. 3,894,438,3,894,439,4,173,148.
At present, it is carrier that used Hydrodewaxing catalyst adopts shape-selective molecular sieve and alumina binder usually, adds a spot of (being no more than 3% in catalyst weight) and has the NiO that adds dehydrogenation activity.CN 85100324A discloses a kind of distillate Hydrodewaxing catalyst and preparation method thereof, this catalyst is that the ZSM-5 zeolite molecular sieve that adopts non-amine method directly to synthesize is a matrix, through acid treatment, adds the adhesive kneading and compacting, add metal component, make through water vapour heat treatment again.Adhesive wherein preferably adopts Woelm Alumina, and metal component is selected from the element compound of group VIII and group vib, the adding mode can adopt dipping, mix pinch, ion-exchange.The function of the described catalyst of this patent is mainly hydro dewaxing, and the hydrofinishing weak effect, and since the Preparation of Catalyst later stage also to carry out hydrothermal treatment consists (500 ℃ 8h), need wasteful energy.
CN 97116407.X discloses the higher Hydrodewaxing catalyst of hydrogenation activity constituent content, wherein WO
310～18w%, NiO2.0～5.0% is to adopt dipping method to add nickel oxide and tungsten oxide, the hydrogenation activity component of being added evenly distributes on catalyst.Because active metallic content height in the catalyst, and employing infusion process, must make the hydrogenation activity constituent content of inside, shape-selective molecular sieve duct also higher, especially the big tungsten oxide content of molecule also can be higher, consequently can stop up the duct of shape-selective molecular sieve inside on the one hand, the hydro dewaxing function is finished in the just collaborative molecular sieve acid site of active metal component on the shape-selective molecular sieve on the other hand, can't finish the hydrofinishing function, and the needed amount of metal of hydro dewaxing function is less, so soak too much reactive metal and also be waste to reactive metal, not only increase cost, also can influence the effect of the hydro dewaxing of catalyst.
CN 1352231A discloses a kind of Hydrodewaxing catalyst, and wherein nickel oxide 1.0%～6.0% and tungsten oxide 0～15% are to adopt dipping method to add nickel oxide and/or tungsten oxide.When catalyst oxygen-free tungsten, the content of nickel oxide is lower, and its hydrofinishing performance is undesirable.When containing tungsten oxide in the catalyst, table 2 from embodiment, the content of its tungsten oxide is generally more than 10wt%, when adopting the immersion process for preparing catalyst, nickel oxide and tungsten oxide can be evenly distributed on the catalyst, by the specific surface data in the table 2 of embodiment as seen, the specific surface that adds tungsten oxide rear catalyst B and E is lower than the catalyst A of only using nickel oxide, C and D, by the reaction result of table 3, when adopting catalyst B and E, its condensation point reduction amplitude is starkly lower than catalyst A, C and D.In addition, this method adopts the method for high-temperature roasting catalyst carrier to reduce the acidity of catalyst, and 700 ℃～830 ℃ of high-temperature roasting temperature cause its energy consumption height, the preparation cost height.
Summary of the invention
At deficiency of the prior art, the present invention proposes a kind of pour point depression and the hydrofinishing performance is good, cost is low, reactive metal distributes rational Hydrodewaxing catalyst and preparation method thereof.
Hydrodewaxing catalyst of the present invention, contain reactive metal oxides, shape slective cracking molecular sieve and aluminium oxide, its characteristics are also to contain auxiliary agent, reactive metal oxides is nickel oxide and molybdenum oxide or tungsten oxide, is benchmark with the weight of catalyst, and it is composed as follows: nickel oxide content is 1%～4%, molybdenum oxide or tungsten oxide content are 1%～9%, the shape slective cracking molecular sieve is 60.0%～75.0%, and aluminium oxide 15.0%～30.0%, auxiliary agent are 0.2%～2.0%; Described auxiliary agent is K
2O and/or Li
2O.In the catalyst of the present invention, the total amount of preferred reactive metal oxides accounts for 5%～10% of catalyst weight.
In the reactive metal that catalyst of the present invention adopted, the nickel of whole molybdenums or tungsten and 10wt%～90wt% is to be mixed and made into the binding agent that contains reactive metal with the aperture alumina gel earlier by containing active metallic compound, and then being mixed and made into carrier with molecular sieve, the remainder active metal nickel is to be dipped on the carrier through infusion process.
The gained catalyst property is as follows: pore volume is 0.10cm
3/ g～0.30cm
3/ g, specific surface are 180m
2/ g～350m
2/ g, bulk density is 0.70g/cm
3～1.05g/cm
3
Preparation of catalysts method of the present invention comprises the steps:
(1) the used alumina dry gel of binding agent is crushed to more than 160 orders;
(2) preparation contains the binding agent of reactive metal;
(3) binding agent of step (2) gained and shape-selective molecular sieve and extrusion aid are mixed pinch, after the extrusion, moulding, drying and roasting;
(4) preparation contains the maceration extract of reactive metal and auxiliary agent;
(5) with the maceration extract of step (3) product of roasting impregnation steps (4) preparation, dry then, roasting obtain catalyst of the present invention.
The described hydrogenation activity component of step (2) is two kinds of components: a component is Ni, and another component is Mo or W, preferred W-Ni.And whole Mo or the Ni of W and 10wt%～90wt% are used to prepare binding agent in the catalyst.The compound that contains reactive metal is water miscible inorganic compound, and wherein molybdate compound is preferably one or both in ammonium heptamolybdate and the ammonium tetramolybdate, and Tungstenic compound is preferably ammonium metatungstate, and nickel compound containing is preferably nickel nitrate.
The compound that the adhesive preparation method that contains reactive metal can adopt following at least a method: A, will contain reactive metal directly mixes (it is more than 160 orders that the compound that contains reactive metal requires the order number) with the pressed powder form with aperture alumina dry gel, add inorganic acid solution, be prepared into the binding agent that contains reactive metal; B, the compound that will contain reactive metal are dissolved in the inorganic acid solution, mix with aperture alumina dry gel then, are prepared into the binding agent that contains reactive metal; The preferred nitric acid of inorganic acid described in said method A or the B, salpeter solution concentration 0.5mol/L～3.0mol/L, preferred 1.0～2.5mol/L; The consumption of described inorganic acid solution is 50～60mL/100g catalyst.The specific surface of described aperture alumina dry gel is 220～300m
2G
-1, pore volume is 0.4～0.6 mLg
-1
Described shape-selective molecular sieve is a hydrogen type molecular sieve, is selected among ZSM-5, ZSM-22, ZSM-23, the ZSM-35 one or more, preferred ZSM-5.
The described drying condition of step (3): baking temperature is 80 ℃～120 ℃, and be 2h～8h drying time, and roasting condition is as follows: sintering temperature is 400 ℃～600 ℃, and roasting time is 3h～6h.
The described reactive metal of step (4) is a nickel, and its nickel amount is the amount of binding agent with the outer remainder nickel of nickel.Used nickel compound containing is water miscible inorganic compound, preferred Ni (NO
3)
2, concentration 0.1mol/L～0.8mol/L, preferred 0.4mol/L～0.5mol/L.Described auxiliary agent is Li
2O and/or K
2O, the compound that contains auxiliary agent is water miscible inorganic compound, preferred LiNO
3And/or KNO
3
The described drying condition of step (5): baking temperature is 80 ℃～120 ℃, and be 2h～8h drying time, and roasting condition is as follows: sintering temperature is 400 ℃～600 ℃, and roasting time is 3h～6h.
Described extrusion aid is meant the material that helps extrusion modling, and as sesbania powder, carbon black, graphite powder, citric acid etc., the consumption of extrusion aid accounts for the 1wt%～10wt% of total material butt.
The prepared catalyst of the present invention is applicable to the hydro dewaxing process of the hydrocarbon oil crude material of the content of wax, be particularly suitable for the hydro dewaxing and the unifining process of the hydrocarbon oil crude material of the content of wax, wherein minimum wax content is 5wt% based on the raw material total amount, preferred 5wt%～25wt%, and sulfur-bearing is not higher than 800 μ gg
-1, the nitrogenous 300 μ gg that are not higher than
-1Selected suitable reaction condition is: range of reaction temperature is at 200 ℃～550 ℃, preferred 300～400 ℃; Hydrogen dividing potential drop scope is at 2MPa～6MPa, preferred 3MPa～5MPa; Volume space velocity during liquid (LHSV) scope 1～3h
-1, preferred 1～2h
-1, hydrogen to oil volume ratio is 400～700.
In the inventive method, whole molybdenums or tungsten and part of nickel are to be mixed and made into the binding agent that contains reactive metal with aluminium oxide earlier by containing active metallic compound, and then be mixed and made into carrier with molecular sieve, remainder nickel is dipped on the carrier through infusion process, has following advantage:
1. this method has made full use of in the catalyst carrier aluminium oxide as binding agent, be prepared into the binding agent that contains whole molybdenums and tungsten and part of nickel earlier, thereby the content of reactive metal in the control molecular sieve preferably only contains partial oxidation nickel, make the duct of molecular sieve unimpeded, hydro dewaxing is effective.And reactive metal molybdenum or tungsten and all the other part of nickel are distributed on the aluminium oxide substantially, can obviously improve hydrorefined performance.
2. by adding the acid distribution that auxiliary agent reduces the acid amount of catalyst carrier and changes catalyst carrier, make the acidity of catalyst satisfy the needs of hydro dewaxing and Hydrobon catalyst, avoid catalyst hydrothermal treatment consists or high-temperature roasting step simultaneously, reduced energy consumption, saved preparation cost.
3. catalyst of the present invention can guarantee the effect of hydro dewaxing under the condition of hydrogenation activity constituent content lower (5.0%～10.0% in catalyst weight), can also improve the effect that hydrofinishing reduces impurity contents such as sulphur, nitrogen.
The specific embodiment
The following examples will give further instruction and elaboration with regard to method provided by the invention, but not limit the present invention.
Embodiment 1
1. Preparation of Catalyst
8.3g ammonium metatungstate and 3.9g nickel nitrate mix, and grind to form the above powder of 160 orders, with little porous aluminum oxide (the specific surface 238m of 37.3g contents on dry basis 67wt%
2.g
-1, pore volume 0.48mLg
-1) mix, adding 1.5mol/L, 56mL aqueous solution of nitric acid stir and are prepared into binding agent, with 67gHZSM-5 molecular sieve (butt 97wt%, manufacturer: big Tianjin Catalyst Factory, Nankai Univ, SiO
2/ Al
2O
3Mol ratio=38) mix, mix pinch, extrusion, 4 hours, 580 ℃ roastings of 130 ℃ of dryings 4 hours, dipping (the maceration extract preparation: 15.8g nickel nitrate, 1.1g potassium nitrate are dissolved in the 100mL water), 4 hours, 580 ℃ roastings of 130 ℃ of dryings 4 hours obtain catalyst, and its character sees Table 1.
2. technology assessment
With grand celebration vacuum 1st side cut (feedstock property sees Table 2) is feedstock oil.Test is carried out on 200mL hydrogenation midget plant.Feedstock oil enters the embodiment of the invention 1 gained catalyst 100mL, removes the straight chain hydrocarbon of high condensation point in the oil product, finishes hydrofinishing when reducing the oil product condensation point, removes sulphur in the raw material, nitrogen content, saturated unsaturated component.Process conditions see Table 3, and product property sees Table 4.
Embodiment 2
1. Preparation of Catalyst
4.8g ammonium heptamolybdate and 3.9g nickel nitrate mix, and grind to form the above powder of 160 orders, with little porous aluminum oxide (the specific surface 238m of 39.6g contents on dry basis 67wt%
2G
-1, pore volume 0.48mLg
-1) mix, add 1.5 mol/L, 56mL aqueous solution of nitric acid and stir and be prepared into binding agent, with 69.1gHZSM-5 molecular sieve (butt 97wt%, manufacturer: Tianjin Catalyst Factory, Nankai Univ, SiO
2/ Al
2O
3Mol ratio=38) mix, mix pinch, extrusion, 4 hours, 580 ℃ roastings of 130 ℃ of dryings 4 hours, dipping (the maceration extract preparation: 7.9g nickel nitrate, 1.1g potassium nitrate are dissolved in the 100mL water), 4 hours, 580 ℃ roastings of 130 ℃ of dryings 4 hours obtain catalyst, and its character sees Table 1.
2. technology assessment
Process conditions are with embodiment 1, and technology assessment the results are shown in Table 4.
Embodiment 3
1. Preparation of catalysts
7.15g ammonium metatungstate and 5.85g nickel nitrate are dissolved in the aqueous solution of nitric acid that 56mL concentration is 1.5 mol/L, mix with the little porous aluminum oxide of 31.3g contents on dry basis 67wt%, be prepared into binding agent, with 72.2gHZSM-5 molecular sieve (butt 97wt%, manufacturer: Tianjin Catalyst Factory, Nankai Univ, SiO
2/ Al
2O
3=38) mix, mix pinch, extrusion, dry, roasting condition is with embodiment 1, dipping (maceration extract preparation: 3.95 nickel nitrates, 9.8gLiNO
3Be dissolved in the 100mL water), drying, roasting condition obtain catalyst with embodiment 1, and its character sees Table 1.Technology assessment the results are shown in Table 4.
Comparative example 1
Described according to CN 1352231A, adopt the immersion process for preparing Hydrodewaxing catalyst, hydrogenation activity component total amount is 10wt% (WO3 content 7wt%, NiO content 3wt%), with embodiment 1.Catalyst property sees Table 1.Technology assessment the results are shown in Table 4.
Comparative example 2
Described according to CN 97116407.X, adopt the immersion process for preparing Hydrodewaxing catalyst, hydrogenation activity component total amount is 23wt% (WO3 content 18wt%, NiO content 5.0wt%).Catalyst property sees Table 1.Technology assessment the results are shown in Table 4.
Table 1 catalyst property
| Embodiment | Embodiment 1 | Embodiment 2 | Embodiment 3 | Comparative example 1 | Comparative example 2 |
| Catalyst is formed, wt% | |||||
| ZSM-5 | 65 | 67 | 70 | 65 | 57 |
| Al 2O 3 | 24.5 | 26.5 | 21 | 25 | 20 |
| WO 3 | 7 | - | 6 | 7 | 18 |
| NiO | 3 | 2 | 2 | 3 | 5 |
| MoO 3 | - | 4 | - | - | - |
| K 2O | 0.5 | 0.5 | - | - | - |
| Li 2O | - | - | 1 | ||
| Physico-chemical property: | |||||
| Pore volume, cm 3/g | 0.182 | 0.178 | 0.161 | 0.181 | 0.153 |
| Specific surface, m 2/g | 274 | 261 | 285 | 270 | 212 |
Table 2 feedstock oil character
| Project | |
| Density (20 ℃), kg/m 3 | 846.2 |
| Boiling range, ℃ | |
| IBP/50％/95％ | 245/354/397 |
| Sulphur, μ g/g | 474.6 |
| Nitrogen, μ g/g | 98 |
| Condensation point, ℃ | 26 |
| Wax content, wt% | 23.8 |
Table 3 reaction condition
| Project | |
| The hydrogen dividing potential drop, MPa | 4.0 |
| H 2/ oil (volume) | 450 |
| Reaction temperature, ° C | 350 |
| LHSV，h -1 | 1.5 |
The main character of table 4 product
| Project | Embodiment 1 | Embodiment 2 | Embodiment 3 | Comparative example 1 | Comparative example 2 |
| Density (20 ℃), kg/m 3 | 844.0 | 840.4 | 841.2 | 843.5 | 845.1 |
| Condensation point, ℃ | -45 | -43 | -52 | -42 | -37 |
| Boiling range, ℃ | |||||
| IBP | 179 | 176 | 179 | 184 | 178 |
| 50％ | 306 | 301 | 314 | 307 | 305 |
| 95％ | 356 | 360 | 351 | 365 | 357 |
| Sulfur content, μ g/g | 151 | 143 | 173 | 307 | 148 |
| Nitrogen content, μ g/g | 14 | 37 | 38 | 68 | 29 |
By table 4 as seen, when adopting catalyst of the present invention to be used to handle waxy feeds, not only condensation point can be dropped to below-40 ℃ from 26 ℃, and sulfur content reduces by 300 μ g.g
-1More than, nitrogen content reduces by 60 μ g.g
-1More than, and the catalyst in the comparative example 1 is owing to adopt infusion process, under the lower situation of tenor, its pour point depression effect is suitable with the present invention, but the poor effect of its hydrofinishing desulfurization and denitrogenation, the catalyst in the comparative example 2 be because the active metallic content height, and all adopt infusion process, though its hydrofinishing effect is suitable with the present invention, its pour point depression effect is bad.
Claims (18)
1. Hydrodewaxing catalyst, contain reactive metal oxides, shape slective cracking molecular sieve and aluminium oxide, it is characterized in that also containing auxiliary agent, reactive metal oxides is nickel oxide and molybdenum oxide or tungsten oxide, is benchmark with the weight of catalyst, and it is composed as follows: nickel oxide content is 1%～4%, molybdenum oxide or tungsten oxide content are 1%～9%, the shape slective cracking molecular sieve is 60.0%～75.0%, and aluminium oxide 15.0%～30.0%, auxiliary agent are 0.2%～2.0%; Described auxiliary agent is K
2O and/or Li
2O.
2. according to the described catalyst of claim 1, it is characterized in that in the reactive metal that described Hydrodewaxing catalyst adopts, the nickel of whole molybdenums or tungsten and 10wt%～90wt% is to be mixed and made into the binding agent that contains reactive metal with the aperture alumina gel earlier by containing active metallic compound, and then being mixed and made into carrier with molecular sieve, the remainder active metal nickel is to be dipped on the carrier through infusion process.
3. according to the described catalyst of claim 1, it is characterized in that in the described catalyst, the total amount of reactive metal oxides accounts for 5%～10% of catalyst weight.
4. according to the described catalyst of claim 1, it is characterized in that described shape slective cracking molecular sieve is a hydrogen type molecular sieve, be selected among ZSM-5, ZSM-22, ZSM-23, the ZSM-35 one or more.
5. according to the described catalyst of claim 4, it is characterized in that described shape slective cracking molecular sieve is ZSM-5.
6. according to the arbitrary described catalyst of claim 1～5, it is characterized in that the gained catalyst property is as follows: pore volume is 0.10cm
3/ g～0.30cm
3/ g, specific surface are 180m
2/ g～350m
2/ g, bulk density is 0.70g/cm
3～1.05g/cm
3
7. the described Preparation of catalysts method of claim 1 comprises the steps:
(1) the used alumina dry gel of binding agent is crushed to more than 160 orders;
(2) preparation contains the binding agent of reactive metal;
(3) binding agent of step (2) gained and shape-selective molecular sieve and extrusion aid are mixed pinch, after the extrusion, moulding, drying and roasting;
(4) preparation contains the maceration extract of reactive metal and auxiliary agent;
(5) with the maceration extract of step (3) product of roasting impregnation steps (4) preparation, dry then, roasting obtain catalyst of the present invention;
The adhesive preparation method that contains reactive metal can adopt following at least a method: method one, the compound that will contain reactive metal directly mix with aperture alumina dry gel with the pressed powder form, add inorganic acid solution, be prepared into the binding agent that contains reactive metal; Method two, the compound that will contain reactive metal are dissolved in the inorganic acid solution, mix with aperture alumina dry gel then, are prepared into the binding agent that contains reactive metal;
The described reactive metal of step (2) is Ni and Mo, is Ni and W perhaps, and whole Mo or the Ni of W and 10wt%～90wt% are used to prepare binding agent in the catalyst.
8. according to the described preparation method of claim 7, it is characterized in that the described inorganic acid of step (2) is a nitric acid, salpeter solution concentration is 0.5mol/L～3.0mol/L, and the consumption of described inorganic acid solution is 50～60mL/100g catalyst.
9. according to the described preparation method of claim 8, it is characterized in that described salpeter solution concentration is 1.0～2.5mol/L.
10. according to the described preparation method of claim 7, it is characterized in that the described compound that contains reactive metal of step (2) is water miscible inorganic compound, wherein molybdate compound is one or both in ammonium heptamolybdate and the ammonium tetramolybdate, Tungstenic compound is an ammonium metatungstate, and nickel compound containing is a nickel nitrate.
11., it is characterized in that the described reactive metal of step (2) is W and Ni according to the described preparation method of claim 7.
12., it is characterized in that the specific surface of the described aperture alumina gel of step (2) is 220～300m according to the described preparation method of claim 7
2G
-1, pore volume is 0.4～0.6mLg
-1
13. according to the described preparation method of claim 7, it is characterized in that described shape slective cracking molecular sieve is a hydrogen type molecular sieve, be selected among ZSM-5, ZSM-22, ZSM-23, the ZSM-35 one or more.
14., it is characterized in that described shape slective cracking molecular sieve is ZSM-5 according to the described preparation method of claim 13.
15. according to the described preparation method of claim 7, it is characterized in that step (3) and the described drying condition of step (5): baking temperature is 80 ℃～120 ℃, be 2h～8h drying time, and roasting condition is as follows: sintering temperature is 400 ℃～600 ℃, and roasting time is 3h～6h.
16. according to the described preparation method of claim 7, it is characterized in that the described reactive metal of step (4) is a nickel, its nickel amount is with the amount of the outer remainder nickel of nickel in the binding agent; Used nickel compound containing is a nickel nitrate, and the concentration of nickel nitrate is 0.1mol/L～0.8mol/L in the maceration extract; The described compound that contains auxiliary agent is LiNO
3And/or KNO
3
17. the application of the described catalyst of claim 1～6 in the hydrocarbon oil crude material hydro dewaxing process of the content of wax.
18. the described catalyst of claim 1～6, is characterized in that content of wax 5wt%～25wt% in the hydrocarbon oil crude material of the content of wax in the hydrocarbon oil crude material hydro dewaxing of the content of wax and the application in the unifining process, sulfur-bearing is not higher than 800 μ gg
-1, the nitrogenous 300 μ gg that are not higher than
-1
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