CN1353168A - Hydrorefining catalyst and its preparing process - Google Patents
Hydrorefining catalyst and its preparing process Download PDFInfo
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- CN1353168A CN1353168A CN 00130284 CN00130284A CN1353168A CN 1353168 A CN1353168 A CN 1353168A CN 00130284 CN00130284 CN 00130284 CN 00130284 A CN00130284 A CN 00130284A CN 1353168 A CN1353168 A CN 1353168A
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Abstract
A hydrorefining catalyst for segment-2 hydrorefining of cracked C6-C8 gasoline fraction after sulfurized is prepared through adding high polymer and metal in IV the secondary family when alumina precursor is shaped, drying in air for 2-14 hr, calcining at 400-700 deg.C, dipping in ammonia liquid containing Mo, Co and Ni, drying at 100-120 deg.C for 2-14 hr, and activating in air at 400-700 deg.C for 2.5-8.5 hr. It can regulate pH value of carrier and suppress the deactivating speed of catalyst.
Description
The present invention relates to a kind of Hydrobon Catalyst And Its Preparation Method, especially be applicable to pyrolysis gasoline secondary hydrogenation process for refining process.
In the last few years, along with the continuous progress of petroleum refining technology, hydrogen addition technology was also in continuous development, and as core one catalyzer of hydrogen addition technology, its performance is also in continuous improve.Therefore be badly in need of developing the C of excellent property
4～C
6Cut fraction pyrolysis gasoline secondary hydrogenation catalyst for refining.
US4059504 discloses Tungsten oxide 99.999 added and has been mixed with its immersion liquid in the nickel nitrate aqueous solution, loads on specific surface area greater than 150 meters
2On/gram the aluminum oxide,,, obtain cobalt 2.5% 457 ℃ of roastings 3 hours through dry air, tungsten 8.0%, the specific surface area of this catalyzer is low, has caused active lowly, and therefore, when handling pyrolysis gasoline, its life-span is shorter.
Have one piece and introduced " pyrolysis gasoline two sections LY-8602 catalyzer industrial production and application " in " Chinese Appropriate technology achievement storehouse ", this catalyzer adopts γ-Al
2O
3Be carrier, MoO
3With CoO be active ingredient, the physical strength of this catalyzer is ≮ 40N/mm when industrial application is regenerated, to cause the fragmentation of catalyzer easily.
Introduced another piece of writing " pyrolysis gasoline one, secondary hydrogenation cobalt Mo-Ni catalyst " in " Chinese Appropriate technology achievement storehouse ", this secondary hydrogenation catalyzer is with γ-Al
2O
3+ TiO
2Be carrier. this TiO
2When becoming glue, introduces in aluminum oxide, with MoO
3, CoO, NiO be active ingredient, but the bulk density of this catalyzer (＞1.0) is higher relatively, increases the expense of one-time pad catalyzer; Adopt the two-step approach dipping during metal impregnation, make the step of preparation catalyzer complicated more.
The purpose of wood invention is to provide the Hydrobon Catalyst And Its Preparation Method that a kind of preparation method of having is simple, catalyst activity is high, physical strength is high, bulk density is low.
Technical scheme of the present invention is achieved in that
Hydrobon catalyst is to be made of the alumina supporter that contains IV subgroup metal, molybdenum, cobalt, nickel active ingredient, (with the catalyst weight is benchmark to its each component concentration, weight %) is: molybdenum oxide (MoO) 8～25 %, cobalt oxide (CoO) 1～9%, nickel oxide (NiO) 1～5%, IV subgroup metal 7～22%, all the other are aluminum oxide (Al
2O
3).
The preparation method of Hydrobon catalyst is:
1. aluminum oxide precursor when its moulding, adds superpolymer, IV subgroup metal, and then, in air atmosphere, 400～700 ℃ of dry 2～14 hours, roasting obtain containing the carrier of IV subgroup metal.
2. with 1 carrier that contains IV subgroup metal that obtains, through containing the ammonia co-impregnated solution dipping of molybdenum (Mo), cobalt (Co), nickel (Ni) active ingredient, 100～120 ℃ of dryings 2～14 hours, the activation 2.5～8.5 hours down of 400～700 ℃ of air obtained catalyzer.
The present invention also adopts following technical scheme:
Aforementioned aluminum oxide precursor is meant boehmite, pseudo-boehmite, promise diaspore, unformed aluminium hydroxide or the gibbsite with sodium metaaluminate-nitrate method or the preparation of aluminum alkoxide hydrolysis method.
Aforementioned superpolymer can be a kind of in gac, polyacrylamide, polyoxyethylene glycol (molecular weight 2000,5000,20,000), the polyvinyl alcohol, also can be the mixture of several materials.
Aforementioned IV subgroup metal modifiers can be a kind of metal among titanium Ti, zirconium Zr, the hafnium Hf, also can be the mixture of two kinds of metals wherein.
Aforementioned co-impregnated solution is meant the inorganic aqueous solution that contains molybdenum Mo, cobalt Co, nickel, normally makes co-impregnated solution by ammonium molybdate and Xiao Suangu, cobaltous acetate, cobaltous dihydroxycarbonate and nickelous nitrate, nickelous acetate, basic nickel carbonate etc. with ammoniacal liquor.
Described forming method is meant methods such as compressing tablet, balling-up or extrusion commonly used in the supported catalyst preparation process, and is wherein best with the extrusion method.The dry material that only needs during moulding to contain extrusion aid, IV subgroup metal places kneading machine, do and mix, add the aqueous solution that contains materials such as peptizing agent, expanding agent then, carry out wet mixing, mixed material is put into the hopper of banded extruder, make material just can obtain the support of the catalyst bar of desired shape by squeezing action, the carrier dry in air atmosphere, that roasting obtains containing IV subgroup metal by orifice plate.
The invention has the advantages that: the aluminum oxide precursor is when moulding, adding superpolymer makes carrier obtain reaming, promptly increase carrier and held the gelationus ability, add IV subgroup metal, regulated the acid-basicity of carrier, suppress the coking and deactivation speed of catalyzer, thereby obtained the alumina supporter of modification.This catalyzer can be used for C after sulfuration
6～C
8The unifining process that pyrolysis gasoline cut fraction is two sections.Compared with prior art, it is reasonable to have a catalyst structure, and catalyst activity height (good to the monoene selectivity), anti-coking performance are strong, characteristics such as preparation technology is simple.
Be further described with regard to technical scheme of the present invention below:
Table 1 has provided the pore structure data of three kinds of aluminum oxide, and wherein 1～No. 3 gama-alumina is the data that add expanding agent 0%, 10%, 15% respectively.No. 2 is add-on of the present invention.
Table 1 central hole structure data are to adopt cryogenic nitrogen absorption BET method to measure; The ZQJ intelligence granule strength trier that the physical strength of catalyzer adopts Dalian Device Diagnostic device factory to produce is measured.
The data of table 1 show that along with the increase of expanding agent add-on, specific surface area decreases, and pore volume also increases thereupon, and the physical strength of carrier reduces very obvious.On the one hand, can satisfy the requirement of catalyst strength; On the other hand, also can satisfy of the requirement of pyrolysis gasoline secondary hydrogenation catalyzer to pore structure.Therefore the add-on 10% of initial option 2 is method reaming of the present invention.
Example 1
Example 1 is presented under all identical condition of other condition, and the properties-correcting agent add-on is 0% to be prepared into and to contain IV subgroup metallic carrier, and the co-impregnated solution with Mo-Co-Ni floods then, prepares the A catalyzer, and the composition of catalyzer sees Table 2.
Example 2
It is 7.5% that example 2 is introduced the properties-correcting agent add-on, and other condition is identical with example 1, prepares the B catalyzer, and the composition of catalyzer sees Table 2.
Example 3
It is 15% that example 3 is introduced the properties-correcting agent add-on, and other condition is identical with example 1, prepares the C catalyzer, and the composition of catalyzer sees Table 2.
Example 4
It is 20% that example 3 is introduced the properties-correcting agent add-on, and other condition is identical with example 1, prepares the D catalyzer, and the composition of catalyzer sees Table 2.
Comparative Examples 1
Preparation of catalysts process of this case introduction.
One is supported on (150 meters of high surface areas
2/ gram) tungsten oxide catalyst on the aluminum oxide with the cobalt nitrate solution dipping, in 452 ℃ of roastings 3 hours, can obtain containing the catalyzer of 2.5 weight % cobalts and 8 weight % tungsten under air atmosphere.This catalyzer be numbered E.
Example 5
Present embodiment has been introduced with each activity rating of catalyst process.
Adopting pyrolysis gasoline to generate oil for one section is raw material, and A, B, four catalyzer of C, D are estimated, and the evaluation of catalyzer is carried out on the 100ml small hydrogenation device.Catalyzer at first carried out prevulcanized 6 hours with the hydrogenation kerosene of the dithiocarbonic anhydride that contains 2 weight % under 280 ℃ of hydrogen, advance stock oil then.Reaction conditions: hydrogen dividing potential drop 4.2MPa, volume space velocity are 3.0 hours
-1, hydrogen to oil volume ratio 300: 1,260 ℃ of temperature of reaction.Generate oil and mainly carry out the analysis of bromine valency and diene number, reaction result sees Table 2.
From the result of table 2 as seen: catalyzer C of the present invention is better than other catalyzer.
Example 6
This case introduction generate oily evaluate catalysts C and E active process with one section of pyrolysis gasoline.
Adopting pyrolysis gasoline to generate oil for one section is raw material, and C and two catalyzer of E are estimated, and the evaluating apparatus of catalyzer, sulfuration and reaction conditions are with embodiment 5.Generate oil and mainly carry out the analysis of bromine valency and diene number, reaction result sees Table 2.
From the result of table 2 as seen: catalyzer C of the present invention obviously is better than Comparative Examples E catalyzer.
Embodiment 7～9
At cobalt oxide 2～5 weight %, nickel oxide 1.5～3.5 weight %, IV subgroup metal 15 weight %, molybdenum oxide content is respectively 10,16,23 weight %, and all the other are carrier, prepares three catalyzer F, G, H, appreciation condition is with embodiment 5, and test-results sees Table 3.
Embodiment 10～13
At molybdenum oxide 10～23 weight %, nickel oxide 1.5～3.5 weight %, IV subgroup metal 15 weight %, cobalt oxide 2,3,5 weight %, all the other are carrier, prepare three catalyst I, J, K, and appreciation condition is with embodiment 5, and test-results sees Table 3.
Embodiment 14～16
At molybdenum oxide 10～23 weight %, cobalt oxide 2～5 weight %, IV subgroup metal 15 weight %, nickel 1.5,2.0,3.5 weight %, all the other are carrier, prepare three catalyzer L, M, N, and appreciation condition is with embodiment 5, and test-results sees Table 3.
From the result of table 3 as seen, the present invention adopt metal content be: molybdenum oxide 16 weight %, cobalt oxide 3 weight %, nickel 2.0 weight %, IV subgroup metal 15 weight % are the optimum activity combination of components.
Table 1
| Numbering | ????1 | ????2 | ????3 | |
| Expanding agent add-on % | ????0 | ????10 | ????15 | |
| Carrier character | Specific surface, rice 2/ gram | ????327 | ????320 | ????312 |
| Pore volume, milliliter/gram | ????0.64 | ????0.71 | ????0.72 | |
| Physical strength, newton/centimetre | ????146 | ????125 | ????94 | |
Table 2
| Numbering | A | B | C | D | E | |
| The properties-correcting agent add-on, % | 0 | 7.5 | 15 | 20 | ||
| The character of catalyzer | Specific surface, rice 2/ gram | 226 | 220 | 214 | 207 | 150 |
| Pore volume, milliliter/gram | 0.38 | 0.46 | 0.50 | 0.53 | ||
| Pore distribution, % (A) | ||||||
| 10～20 | 12.59 | 11.47 | 10.53 | 9.15 | ||
| 20～30 | 40.61 | 39.71 | 35.46 | 32.77 | ||
| 30～40 | 26.32 | 27.17 | 27.65 | 28.65 | ||
| 40～50 | 8.78 | 8.79 | 9.94 | 10.24 | ||
| 50～100 | 7.06 | 8.54 | 10.37 | 11.96 | ||
| 100～200 | 4.64 | 4.32 | 4.89 | 4.98 | ||
| 200～300 | 0 | 0 | 1.16 | 2.25 | ||
| Physical strength, newton/centimetre | 156 | 143 | 138 | 124 | ||
| Stock oil | The bromine valency, gram bromine/100 gram oil | ??????????????????????????19.39 | ||||
| Diene number, gram iodine/100 gram oil | ??????????????????????????1.59 | |||||
| Generate oil | The bromine valency, gram bromine/100 gram oil | 1.80 | 1.00 | 0.20 | 0.70 | 0.56 |
| Diene number, gram iodine/100 gram oil | 0.19 | 0.04 | 0.00 | 0.05 | 0.05 | |
Table 3
| Numbering | ????F | ????G | ????H | ????I | ????J | ????K | ??L | ??M | ??N | |
| Molybdenum oxide, weight % | ????10 | ????16 | ????23 | ???????????10～23 | ????????????10～23 | |||||
| Cobalt oxide, weight % | ?????????????2～5 | ????2 | ????3 | ????5 | ????????????2～5 | |||||
| Nickel oxide, weight % | ?????????????1.5～3.5 | ???????????1.5～3.5 | ??1.5 | ??2.0 | ??3.5 | |||||
| Stock oil | The bromine valency, gram bromine/100 gram oil | ?????????????????????????????????????????19.39 | ||||||||
| Diene number, gram iodine/100 gram oil | ?????????????????????????????????????????1.59 | |||||||||
| Generate oil | The bromine valency, gram bromine/100 gram oil | ?1.91 | ??0.18 | ??1.13 | ??1.61 | ??0.19 | ??1.00 | ??1.57 | ??0.22 | ??1.04 |
| Diene number, gram iodine/100 gram oil | ?0.16 | ??0.00 | ??0.06 | ??0.18 | ??0.00 | ??0.09 | ??0.20 | ??0.00 | ??0.08 | |
Claims (6)
1. Hydrobon catalyst preparation method, adopt following steps:
1. use the aluminum oxide precursor, when its moulding, add superpolymer, IV subgroup metal, then, in air atmosphere, 400～700 ℃ of dry 2～14 hours, roasting obtain containing the carrier of IV subgroup metal.
2. the carrier that contains IV subgroup metal that will 1. obtain, through containing the ammonia co-impregnated solution dipping of molybdenum (Mo), cobalt (Co), nickel (Ni) active ingredient, 100～120 ℃ of dryings 2～14 hours, the activation 2.5～8.5 hours down of 400～700 ℃ of air obtained catalyzer.
2. a kind of Hydrobon catalyst preparation method according to claim 1,, it is characterized in that: the aluminum oxide precursor is meant boehmite, pseudo-boehmite, promise diaspore, unformed aluminium hydroxide or the gibbsite with sodium metaaluminate-nitrate method or the preparation of aluminum alkoxide hydrolysis method.
3. a kind of Hydrobon catalyst preparation method according to claim 1, it is characterized in that: superpolymer can be a kind of in gac, polyacrylamide, polyoxyethylene glycol (molecular weight 2000,5000,20,000), the polyvinyl alcohol, also can be the mixture of several materials.
4. a kind of Hydrobon catalyst preparation method according to claim 1,, it is characterized in that: IV subgroup metal modifiers can be a kind of metal among titanium Ti, zirconium Zr, the hafnium Hf, also can be the mixture of two kinds of metals wherein.
5. a kind of Hydrobon catalyst preparation method according to claim 1, it is characterized in that: co-impregnated solution is meant the inorganic aqueous solution that contains molybdenum Mo, cobalt Co, nickel, normally makes co-impregnated solution by ammonium molybdate and Xiao Suangu, cobaltous acetate, cobaltous dihydroxycarbonate and nickelous nitrate, nickelous acetate, basic nickel carbonate etc. with ammoniacal liquor.
6. Hydrobon catalyst, it is characterized in that: constitute by the alumina supporter that contains IV subgroup metal, molybdenum, cobalt, nickel active ingredient, (with the catalyst weight is benchmark to its each component concentration, weight %) is: molybdenum oxide (MoO) 8～25%, cobalt oxide (CoO) 1～9%, nickel oxide (NiO) 1～5%, IV subgroup metal 7～22%, all the other are aluminum oxide (Al
2O
3).
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|---|---|---|---|
| CN 00130284 CN1124331C (en) | 2000-11-03 | 2000-11-03 | Hydrorefining catalyst and its preparing process |
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|---|---|---|---|
| CN 00130284 CN1124331C (en) | 2000-11-03 | 2000-11-03 | Hydrorefining catalyst and its preparing process |
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| Publication Number | Publication Date |
|---|---|
| CN1353168A true CN1353168A (en) | 2002-06-12 |
| CN1124331C CN1124331C (en) | 2003-10-15 |
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ID=4594086
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Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100335174C (en) * | 2004-12-17 | 2007-09-05 | 武汉大学 | Method of preparing catalyst camied by composite oxides and application |
| CN101280220B (en) * | 2007-04-04 | 2011-07-20 | 中国石油化工股份有限公司 | Method for producing good quality ethylene material by hydrogenation and dearomatization of benzin naphtha |
| WO2011103699A1 (en) * | 2010-02-25 | 2011-09-01 | 中国石油天然气股份有限公司 | Method for preparing hydrorefining catalyst |
| CN103160312A (en) * | 2011-12-15 | 2013-06-19 | 中国石油天然气股份有限公司 | Application of tooth-spherical distillate hydrogenation catalyst |
| CN103657670A (en) * | 2012-09-20 | 2014-03-26 | 中国石油化工股份有限公司 | Pyrolysis gasoline nickel system selective hydrogenation catalyst and preparation method thereof |
| CN103785445A (en) * | 2012-11-01 | 2014-05-14 | 中国石油化工股份有限公司 | Preparation method of middle distillate-type hydrocracking catalyst |
| CN103785444A (en) * | 2012-11-01 | 2014-05-14 | 中国石油化工股份有限公司 | Preparation method of hydrocracking catalyst |
| CN108855128A (en) * | 2017-05-15 | 2018-11-23 | 中国石油天然气股份有限公司 | A kind of selective hydrogenation catalyst and preparation method thereof |
| CN109317159A (en) * | 2018-10-11 | 2019-02-12 | 泉州市利泰石化科技有限公司 | A kind of pyrolysis gasoline hydrogenation catalyst for refining and preparation method |
-
2000
- 2000-11-03 CN CN 00130284 patent/CN1124331C/en not_active Expired - Lifetime
Cited By (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100335174C (en) * | 2004-12-17 | 2007-09-05 | 武汉大学 | Method of preparing catalyst camied by composite oxides and application |
| CN101280220B (en) * | 2007-04-04 | 2011-07-20 | 中国石油化工股份有限公司 | Method for producing good quality ethylene material by hydrogenation and dearomatization of benzin naphtha |
| US8785345B2 (en) | 2010-02-25 | 2014-07-22 | Petrochina Company Limited | Method for preparing hydrorefining catalyst |
| WO2011103699A1 (en) * | 2010-02-25 | 2011-09-01 | 中国石油天然气股份有限公司 | Method for preparing hydrorefining catalyst |
| CN103160312A (en) * | 2011-12-15 | 2013-06-19 | 中国石油天然气股份有限公司 | Application of tooth-spherical distillate hydrogenation catalyst |
| CN103657670B (en) * | 2012-09-20 | 2016-01-20 | 中国石油化工股份有限公司 | Drippolene nickel system selective hydrocatalyst and preparation method thereof |
| CN103657670A (en) * | 2012-09-20 | 2014-03-26 | 中国石油化工股份有限公司 | Pyrolysis gasoline nickel system selective hydrogenation catalyst and preparation method thereof |
| CN103785444A (en) * | 2012-11-01 | 2014-05-14 | 中国石油化工股份有限公司 | Preparation method of hydrocracking catalyst |
| CN103785445A (en) * | 2012-11-01 | 2014-05-14 | 中国石油化工股份有限公司 | Preparation method of middle distillate-type hydrocracking catalyst |
| CN103785445B (en) * | 2012-11-01 | 2015-07-22 | 中国石油化工股份有限公司 | Preparation method of middle distillate-type hydrocracking catalyst |
| CN108855128A (en) * | 2017-05-15 | 2018-11-23 | 中国石油天然气股份有限公司 | A kind of selective hydrogenation catalyst and preparation method thereof |
| CN108855128B (en) * | 2017-05-15 | 2021-04-30 | 中国石油天然气股份有限公司 | Selective hydrogenation catalyst and preparation method thereof |
| CN109317159A (en) * | 2018-10-11 | 2019-02-12 | 泉州市利泰石化科技有限公司 | A kind of pyrolysis gasoline hydrogenation catalyst for refining and preparation method |
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|---|---|
| CN1124331C (en) | 2003-10-15 |
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