CN100998952B - Coking gasoline hydrogenation refining catalyst and its preparation method - Google Patents
Coking gasoline hydrogenation refining catalyst and its preparation method Download PDFInfo
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Abstract
A hydrorefining catalyst for the coking gasoline, especially for saturating, desulfurizing and denitrifying of olefine, has high low-temp activity and high output rate of product. Its preparing process includes such steps as preparing carrier and more than one kind of immersing liquid with different atom ratios, immersing twice, baking twice and calcining.
Description
Technical field
The present invention relates to a kind of hydrofinishing catalysis that coking gasoline hydrogenation refining is produced chemical industry and reformer feed that is used for, a kind of coking gasoline hydrogenation refining catalyst of, desulfurization saturated, denitrogenation and preparation method thereof especially for alkene.
Background technology
Hydrobon catalyst is a carrier with aluminium oxide or siliceous aluminium oxide generally, with group vib W, Mo is the active component element, is the adjuvant component element with the Co of VIII family, Ni, their various combination, its catalytic performance respectively has characteristics, and for example Co-Mo combination has stronger desulphurizing activated; Ni-Mo combination and Ni-W combination have stronger denitrogenation and arene saturating activity.In order further to improve the performance of catalyst, also add other and add component, for example P, F, B, Ti, Zr etc.The direction of general Hydrobon catalyst research is the saturated activity of desulfurization, denitrogenation and aromatic hydrocarbons that how to improve catalyst, do not relate to and how to improve the saturated catalytic activity of alkene, because of catalyst when desulfurization, denitrogenation and aromatic hydrocarbons are saturated, how general alkene does not improve the report of Hydrobon catalyst alkene saturated activity simultaneously by saturated so see research.
W-Mo-Ni-P/Y-Al
2O
3Catalyst is a kind of good Hydrobon catalyst, active all height that desulfurization, denitrogenation and aromatic hydrocarbons are saturated.A kind of preparation W-Mo-Ni-P/ γ-Al that CN1004192 discloses
2O
3The method of catalyst, this invention employing is once soaked legal system altogether and is equipped with catalyst.During the preparation maceration extract, the compound of W is an ammonium tungstate, and the compound of Ni is a nickelous carbonate, and the compound of P is an orthophosphoric acid, and the compound of Mo is a molybdenum trioxide.Because molybdenum trioxide is water-soluble bad, therefore when the preparation co-impregnated solution at a certain temperature (90～120 ℃) can satisfy MoO by water-fast molybdenum trioxide and orthophosphoric acid reaction generation water soluble
3The phosphato-molybdic heteropolyacid of concentration requirement.So in the co-impregnated solution of this patent, W, Mo, P are that the anionic form with heteropoly acid exists.The disclosed a kind of Hydrobon Catalyst And Its Preparation Method of CN1194076, this catalyst belongs to W-Mo-Ni-P/ γ-Al
2O
3Catalyst, the preparation of co-impregnated solution are at room temperature to dissolve ammonium metatungstate, ammonium paramolybdate, nickel nitrate and orthophosphoric acid preparation, in this invention, W and Mo exist with the isopolyacid anionic form, but this patent catalyst adopts the method for once soaking altogether to prepare.
Existing coking gasoline hydrogenation refining produces chemical industry and the used catalyst of reformer feed is general Hydrobon catalyst, though hydrogenated products also can satisfy sulphur, nitrogen, alkene quality index, but the start-up temperature height of catalyst hydrogenation reaction, bed mean temperature height, bed peak temperature height, coking is fast, and the regeneration period is short.In the coker gasoline, except that containing the sulphur nitrogen impurity, the content of alkene is more than 30% (V), also has a spot of alkadienes, mercaptan and thiophenol isoreactivity sulfide are arranged in the sulfide, therefore, the characteristics that coking gasoline hydrogenation refining is produced chemical industry and reformer feed are that the exothermic heat of reaction amount is big, and reaction heat results from alkene more than 90% saturated; The easy coking of bed, bed pressure drop raises too fast.
About the research of Hydrobon catalyst, though the mechanism of action of auxiliary agent Co, Ni is still had different viewpoints, there is any to generally acknowledge, be exactly for different metallic combinations, different reactions, the reaction temperature that same reaction is different,
The optimum value of (atomic ratio) is different.
Summary of the invention
The object of the invention just is to provide a kind of coking gasoline hydrogenation refining catalyst and preparation method thereof at above-mentioned the deficiencies in the prior art.
The objective of the invention is to realize in the following manner: at first prepare catalyst carrier and different atomic ratios co-impregnated solution more than one, secondly with wherein removing unnecessary raffinate behind a kind of co-impregnated solution impregnation catalyst agent carrier, and oven dry, roasting, the co-impregnated solution that floods for the first time the co-impregnated solution atomic ratio floods the back oven dry once more, roasting makes Hydrobon catalyst with being different from then, comprises following method and step:
A, preparation catalyst carrier S1 and S2;
B, preparation co-impregnated solution L1, L2 and L3;
C, the usefulness saturated impregnated catalyst carrier S 1 of L1 or S2, dipping evenly back is removed unnecessary raffinate also oven dry, roasting, flood once more with L2 again, or with saturated impregnated catalyst carrier S 1 of L2 or S2, after dipping even back unnecessary raffinate of removal and oven dry, the roasting, flood once more with L1 or L3, dipping evenly back is removed unnecessary raffinate also oven dry, roasting, makes Hydrobon catalyst again.
Step a prepares catalyst carrier S1, gets 91-97% boehmite dry powder, adds acetic acid, citric acid, sesbania powder and the deionized water 800ml of 1-3% successively by weight percentage, mixes the be shaped back oven dry, roasting of the even extrusion of alunite and makes carrier S 1;
Preparation catalyst carrier S2, get 82-90% boehmite dry powder, add acetic acid, citric acid, sesbania powder, 10-15% base Ludox and the deionized water 700ml of 0-3% successively by weight percentage, mix the be shaped back oven dry, roasting of the even extrusion of alunite and make carrier S 2.
Step b prepares co-impregnated solution L1, L2 and L3, get 35-50% ammonium metatungstate, 20-25% ammonium paramolybdate by weight percentage, 5-9ml orthophosphoric acid, 25-45% nickel nitrate, join successively in the 80ml deionized water, stirring and dissolving, add deionized water then and be diluted to 120ml, make co-impregnated solution L1, L2 and L3.
Bake out temperature is 110-150 ℃, and drying time 2.0-3.0 hour, sintering temperature was 400-600 ℃, roasting time 2.5-3.5 hour.
The atomic ratio of co-impregnated solution L1 is
The atomic ratio of L2 or L3 is
Good effect: the present invention adopts secondary to flood altogether, and the Hydrobon catalyst of secondary drying, roasting preparation has that the co-impregnated solution preparation is simple, is difficult for broken, good, the product yield advantages of higher of catalyst outward appearance in the roasting.Problems such as catalyst granules fragmentation in difficult, particle adhesion of high concentration co-impregnated solution preparation and the roasting process when having avoided once soaking altogether, outward appearance irregularity, product yield are low.Product adds that to have the saturated low temperature active of alkene a man-hour good in that coker gasoline is refining, can reduce the inlet temperature of reactor, carries out at a lower temperature that alkene is saturated, desulfurization, denitrification reaction, and coking speed is slow, and the regeneration period is long.
The specific embodiment
Be described in further detail below in conjunction with embodiment:
Embodiment 1
Get boehmite dry powder 1000g, add acetic acid 25g, citric acid 25g, sesbania powder 25g and deionized water 800ml, extrusion is shaped after the mixed alunite.110 ℃ of dry 2h, 550 ℃ of roasting 3h make carrier S 1.
Embodiment 2
Get boehmite 1000g, add acetic acid 25g, citric acid 25g, sesbania powder 25, Ludox 185g and deionized water 700ml, extrusion is shaped after the mixed alunite.110 ℃ of oven dry 3h, 550 ℃ of roasting 3h make carrier S 2.
The main physical and chemical of S1, S2 carrier
| Carrier | SiO 2 m％ | Pore volume mlg -1 | Specific area m 2·g -1 | Bulk density gml -1 | Shape | Granularity mm | Side pressure strength Ncm -1 |
| S1 S2 | 0 6.5 | ?0.72?0.74 | 334330 | 0.550.57 | Clover clover | φ1.6×(4～6)φ1.6×(4～6) | 150 159 |
Embodiment 3
Get ammonium metatungstate 22.0g, ammonium paramolybdate 12.2g, orthophosphoric acid 7ml and nickel nitrate 11g join in the 80ml deionized water successively, and stirring and dissolving adds deionized water then and is diluted to 120ml, makes co-impregnated solution L1.
Embodiment 4
Get ammonium metatungstate 22.0g, ammonium paramolybdate 12.2g, orthophosphoric acid 5ml and nickel nitrate 27.7g join in the 80ml deionized water successively, and stirring and dissolving adds deionized water then and is diluted to 120ml, makes co-impregnated solution L2.
L1, L2, each concentration of component of L3 co-impregnated solution
Embodiment 5
Get ammonium metatungstate 22.0g, ammonium paramolybdate 12.2g, orthophosphoric acid 9ml and nickel nitrate 19.3g join in the 80ml deionized water successively, and stirring and dissolving adds deionized water then and is diluted to 120ml, makes co-impregnated solution L3.
Embodiment 6
Carrier S 1 is dried 2h at 150 ℃, take by weighing 100g behind the cool to room temperature and carry out saturated dipping with co-impregnated solution L1 120ml, remove unnecessary raffinate after dipping is even, 110 ℃ of oven dry 3h, 500 ℃ of roasting 3h then, soak altogether once more with L2, dry 3h for 110 ℃ then, 500 ℃ of roasting 3h make catalyst C1.
Embodiment 7
Carrier S 1 is dried 2h at 150 ℃, take by weighing 100g behind the cool to room temperature and carry out saturated dipping with co-impregnated solution L2 120ml, remove unnecessary raffinate after dipping is even, 110 ℃ of oven dry 3h, 500 ℃ of roasting 3h then, carry out soaking altogether the second time with co-impregnated solution L1 again, dry 3h for 110 ℃ then, 500 ℃ of roasting 3h make catalyst C2.
Embodiment 8
Carrier S 2 at 150 ℃ of oven dry 2h, is taken by weighing 100g and carries out saturated dipping with co-impregnated solution L2 120ml behind the cool to room temperature, remove unnecessary raffinate after dipping is even, 110 ℃ of oven dry 3h, 500 ℃ of roasting 3h then.Carry out soaking altogether the second time with co-impregnated solution L1 again, dry 3h for 110 ℃ then, 500 ℃ of roasting 3h make catalyst C3.
Embodiment 9
Carrier S 1 at 150 ℃ of oven dry 2h, is taken by weighing 100g and carries out saturated dipping with co-impregnated solution L3 120ml behind the cool to room temperature, remove unnecessary raffinate after dipping is even, 110 ℃ of oven dry 3h, 500 ℃ of roasting 3h then.Carry out soaking altogether the second time with co-impregnated solution L3 again, dry 3h for 110 ℃ then, 500 ℃ of roasting 3h make catalyst C4.
The main physical and chemical of C1, C2, C3, C4, C5 catalyst
| Catalyst | Active component and auxiliary agent content (m%) | Pore volume mlg -1 | Specific area m 2·g -1 | Bulk density gml -1 | Side pressure strength Ncm -1 | |||
| ?WO 3 | MoO 3 | NiO | P | |||||
| C1 | ?18.8 | 9.1 | 5.1 | 3.0 | 0.43 | 172 | 0.78 | 187 |
| C2 | ?19.0 | 8.9 | 5.0 | 2.9 | 0.42 | 170 | 0.78 | 185 |
| C3 | ?19.2 | 9.0 | 4.9 | 3.2 | 0.45 | 166 | 0.81 | 200 |
| C4 | ?18.9 | 8.8 | 5.2 | 3.0 | 0.40 | 175 | 0.78 | 187 |
| C5 | ?19.2 | 8.6 | 4.8 | 3.1 | 0.45 | 165 | 0.80 | 205 |
Embodiment 10
Carrier S 2 at 150 ℃ of oven dry 2h, is taken by weighing 100g and carries out saturated dipping with co-impregnated solution L3 120ml behind the cool to room temperature, remove unnecessary raffinate after dipping is even, 110 ℃ of oven dry 3h, 500 ℃ of roasting 3h then.Carry out soaking altogether the second time with co-impregnated solution L3 again, dry 3h for 110 ℃ then, 500 ℃ of roasting 3h make catalyst C5.
Embodiment 11
Present embodiment is for estimating the catalytic performance of various catalyst coking gasoline hydrofinishings.Hydrogenation evaluating apparatus reactor dischargeable capacity is 200ml, and loaded catalyst 100ml, feedstock oil are the coker gasoline of Shandong Province's oil plant.Evaluating apparatus gross pressure 3.5Mpa, volume velocity is 2.1h
-1, hydrogen to oil volume ratio is 300, the alkene of investigating catalyst under the differential responses temperature is saturated, desulfurization, denitrification activity.The charging procatalyst carries out presulfurization, and 320 ℃ of pre-curing temperatures, medium are direct current kerosene, CS
2Content 2.0%, the presulfurization time is 3h.Question response is stablized the post-sampling analysis after the charging, the results are shown in following table.
Catalyst desulfurizing denitrification percent and alkene saturated activity under the differential responses temperature
| Reaction temperature ℃ | 200 | 230 | 260 | 300 | |
| Desulfurization degree % | C1 | 4.87 | 20.10 | 52.61 | 98.90 |
| C2 | 4.56 | 19.38 | 50.82 | 99.00 | |
| C3 | 6.01 | 20.00 | 48.75 | 98.38 | |
| C4 | 5.00 | 20.69 | 60.10 | 97.65 | |
| C5 | 3.07 | 23.68 | 60.36 | 96.88 | |
| The reference example | 5.81 | 22.57 | 58.30 | 99.70 | |
| Denitrification percent % | C1 | 7.11 | 17.51 | 48.64 | 93.86 |
| C2 | 5.48 | 17.40 | 48.00 | 92.96 | |
| C3 | 6.39 | 20.16 | 46.78 | 95.78 | |
| C4 | 7.88 | 17.41 | 48.88 | 91.86 | |
| C5 | 8.03 | 20.16 | 50.10 | 93.33 | |
| The reference example | 6.04 | 17.61 | 51.86 | 94.10 | |
| Alkene saturation factor % | C1 | 20.35 | 40.19 | 67.81 | 95.80 |
| C2 | 25.16 | 43.07 | 70.04 | 95.01 | |
| C3 | 21.40 | 43.01 | 65.14 | 96.78 | |
| C4 | 7.18 | 20.69 | 49.09 | 96.00 | |
| C5 | 8.15 | 21.87 | 49.89 | 96.09 | |
| The reference example | 5.00 | 22.07 | 51.56 | 97.37 |
Annotate: the reference example is a kind of coking gasoline hydrogenation refining catalyst of commercial Application in the table.
Claims (3)
1. coking gasoline hydrogenation refining catalyst preparation method, it is characterized in that, co-impregnated solution L1, the L2 and the L3 that at first prepare catalyst carrier and different atomic ratios, secondly with wherein removing unnecessary raffinate behind a kind of co-impregnated solution impregnation catalyst agent carrier, and oven dry, roasting, the co-impregnated solution that floods for the first time the co-impregnated solution atomic ratio floods the back oven dry once more, roasting makes Hydrobon catalyst with being different from then, comprises following method and step:
A, preparation catalyst carrier S1 and S2;
B, preparation co-impregnated solution L1, L2 and L3;
C, the usefulness saturated impregnated catalyst carrier S 1 of L1 or S2, dipping evenly back is removed unnecessary raffinate also oven dry, roasting, flood once more with L2 again, or with saturated impregnated catalyst carrier S 1 of L2 or S2, after dipping even back unnecessary raffinate of removal and oven dry, the roasting, flood once more with L1 or L3, dipping evenly back is removed unnecessary raffinate also oven dry, roasting, makes Hydrobon catalyst again;
Step b prepares co-impregnated solution L1, L2 and L3, get 35-50% ammonium metatungstate, 20-25% ammonium paramolybdate by Different Weight percentage respectively, 5-9ml orthophosphoric acid, 25-45% nickel nitrate, join successively in the 80ml deionized water, stirring and dissolving, add deionized water then and be diluted to 120ml, make co-impregnated solution L1, L2 and L3;
The atomic ratio of co-impregnated solution L1 is
The atomic ratio of L2 or L3 is
2. according to the described a kind of coking gasoline hydrogenation refining catalyst preparation method of claim 1, it is characterized in that, step a prepares catalyst carrier S1, get 91-97% boehmite dry powder, add acetic acid, citric acid and the sesbania powder of 1-3% successively by weight percentage, deionized water 800ml mixes and to pinch the be shaped back oven dry, roasting of even extrusion and make carrier S 1;
Preparation catalyst carrier S2 gets 82-90% boehmite dry powder, adds acetic acid, citric acid and the sesbania powder of 0-3% successively by weight percentage, and 10-15% Ludox and deionized water 700ml mix and pinch the be shaped back oven dry, roasting of even extrusion and make carrier S 2.
3. according to the described a kind of coking gasoline hydrogenation refining catalyst preparation method of claim 1, it is characterized in that bake out temperature is 110-150 ℃, drying time 2.0-3.0 hour, sintering temperature was 400-600 ℃, roasting time 2.5-3.5 hour.
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| CN101480618B (en) * | 2009-01-22 | 2011-04-13 | 江苏佳誉信实业有限公司 | Gasoline hydrogenation pretreatment catalyst as well as production method and use thereof |
| CN102451684B (en) * | 2010-10-27 | 2014-09-03 | 中国科学院大连化学物理研究所 | Preparation method of dehydrogenation catalyst for long-chain n-alkane with 10-13 carbon atoms |
| CN102851061B (en) * | 2011-06-30 | 2014-11-26 | 中国石油天然气股份有限公司 | Hydrofining method of low-grade gasoline/diesel oil |
| CN106552655A (en) * | 2016-11-26 | 2017-04-05 | 新疆佳宇恒能源科技有限公司 | A kind of preparation method of co-impregnated solution and wax oil hydrogenation catalyst for refining |
| CN106902878A (en) * | 2017-01-23 | 2017-06-30 | 姚光纯 | It is a kind of for gasoline, coal tar hydrorefining desulfurization, the catalyst of denitrogenation and preparation method thereof |
| CN109999873B (en) * | 2019-03-07 | 2022-05-17 | 江苏大学 | Preparation method and application of boron nitride loaded molybdenum dioxide material |
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| CN1289828A (en) * | 1999-09-29 | 2001-04-04 | 中国石油化工集团公司 | Hydrorefining catalyst for fraction oil and its preparing process |
| CN1769381A (en) * | 2005-10-26 | 2006-05-10 | 长春惠工催化剂有限责任公司 | Refined hydrogenation catalyst and its preparation method |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1289828A (en) * | 1999-09-29 | 2001-04-04 | 中国石油化工集团公司 | Hydrorefining catalyst for fraction oil and its preparing process |
| CN1769381A (en) * | 2005-10-26 | 2006-05-10 | 长春惠工催化剂有限责任公司 | Refined hydrogenation catalyst and its preparation method |
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