CN1583962A - Absorbing desulfurizing catalyst for catalytic cracking petroleum and preparing method thereof - Google Patents
Absorbing desulfurizing catalyst for catalytic cracking petroleum and preparing method thereof Download PDFInfo
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- CN1583962A CN1583962A CN 03139159 CN03139159A CN1583962A CN 1583962 A CN1583962 A CN 1583962A CN 03139159 CN03139159 CN 03139159 CN 03139159 A CN03139159 A CN 03139159A CN 1583962 A CN1583962 A CN 1583962A
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Abstract
A kind of catalyst for Fcc gasoline's adsorption desulfuration contains in weight percent: 10-85% nano zinc oxide, the atomic diameter of which is 100-500 mu m, 5-80% silica oxide, 5-30% alumina oxide, and 4-45% nickel oxide. The method of preparation is: (1) Mix evenly the nano zinc oxide, silica oxide, alumina oxide, and nickel oxide; dry the particle of step (b); roast the dry particle of step(c); deoxidize the particle of step(d) by proper reductant. The portions of this catalyst remain mixed, and the method adopts the technology of roasting. The catalyst has a good strength, high desulfuration activity, and effective regeneration. Because of the adoption of nano zinc oxide, it causes little to octane number and applies to desulfuration of FCC gasoline. Moreover, the method of preparation is simple and the operation is easy.
Description
Technical field
The invention belongs to desulfurization technology, particularly to the catalyzer of adsorption desulfurize in the catalytically cracked gasoline to catalytically cracked gasoline.
Background technology
Sulphur contained in the gasoline has very big influence to environmental protection, in order to improve the present situation of environmental pollution, various countries have worked out strict emission control standards rules and fuel specification one after another, the achievement in research of Japan aspect low-sulphur oil is advanced in the world, the sulphur content of gasoline has reached 100ppm mostly on its market at present, also can be reduced to 50ppm by 2005.The present sulphur content of European Union's gasoline is 150ppm, also can be reduced to 50ppm by 2005.California, USA content of sulfur in gasoline in 1996 has reached 30ppm, and the content of sulfur in gasoline in other each state has reached 140～170ppm in 2000, and 2000 also can be reduced to below the 140ppm later on.The Chinese government also improves constantly the requirement to gasoline sulfure content in GB, GB17930～1999 regulation content of sulfur in gasoline are not more than 1000ppm, and rises July 1 from this year and will carry out the new legislation that sulphur content is not higher than 800ppm in China.And new edition " world fuel charter " regulation motor spirit in the sulphur content of III, IV shelves respectively less than 30ppm with less than 10ppm.
Compared with developed countries, China's content of sulfur in gasoline is relatively too high.The major cause that causes this greatest differences is the backward relatively of China's gasoline producing process: external gasoline is generally from fluid catalytic cracking (34%), catalytic reforming (33%), alkylation, isomerization and etherificate technologies such as (about 33%); And the gasoline of China 80% comes catalytic cracking, and this single production technique makes that the sulphur content of China's gasoline product is more much higher than the sulphur content of external gasoline product.Therefore the key that reduces China's gasoline products sulphur content is to reduce the sulphur content of catalytically cracked gasoline, and the desulfurization of China's gasoline mainly is a Processes of FCC Naphtha Hydrotreating at present.As everyone knows, the gasoline hydrogenation arts demand is operated under higher temperature and pressure condition, therefore unavoidably can increase energy consumption (comprising kinetic energy and heat energy consumption), hydrogen consumption, specification, process cost, processing requirement and other numerous relevant matters of corresponding just necessary raising equipment.On technology, hydrotreatment also can cause the decline of gasoline octane rating again, and the hydrogenation reaction of unsaturated hydrocarbons is aggravated when deep hydrodesulfurizationof, and the hydrogen consumption rises rapidly, and loss of octane number is bigger.Therefore, gasoline must carry out adsorption desulfurize to be handled, and does not reduce octane value and make sulphur content reach requirement.
Some form other by X type adsorbent of molecular sieve, Y zeolite sorbent material and in the absorbing desulfurization catalyst prior art, and having introduced a kind of as US6254766 is carrier with zinc oxide, silicon oxide, aluminum oxide, the preparation of adsorbent method of dipping Ni.It is carrier with zinc oxide, aluminum oxide, silicon oxide that US6429170 has introduced a kind of, dipping Ni, C
oSorbent material.The characteristics of these technology are made up of carrier and active substance two portions, and active substance enters with impregnation method, complex process, and often soak not thoroughly, influence the adsorption desulfurize effect.Moreover it is big to the loss of octane number of gasoline.
Summary of the invention
Technical problem to be solved by this invention provides a kind of catalytic gasoline absorbing desulfurization catalyst and preparation method thereof, solves the desulphurization problem of catalytically cracked gasoline, and the preparation method is simple, and sulfur capacity is big, and is little to the gasoline octane rating influence.
Catalytically cracked gasoline desulfurization catalyst of the present invention is characterized in that its weight percent consists of: particle diameter is nano zine oxide 10-85%, silicon oxide 5-80%, aluminum oxide 5-30%, the reduced state nickel 4-45% of 100 ~ 500m.
Above-mentioned preferred weight percent consists of: nano zine oxide 45-60%, silicon oxide 15-35%, aluminum oxide 5.0-15%, reduced state nickel 15-40%.
The shape of catalyzer can be this area acceptable different shape, the particle of one of preferred grain, sheet, ball, bar shaped.
This Preparation of catalysts method comprises the steps:
(a) raw material nano zinc oxide, silicon oxide, aluminum oxide, nickel oxide are mixed;
(b) make gained compound particles granulation form particle;
(c) make the particle drying of step (b);
(d) with the dried particles roasting of step (c);
(e) make particle reduction after the roasting of step (d) gained with the reductive agent that is fit to.
The weight of each raw material of step (a) consists of: nano zine oxide 10-85%, silicon oxide 5-80%, aluminum oxide 5-30%, nickel oxide 5-50%.Preferably consist of: nano zine oxide 45-60%, silicon oxide 15-35%, aluminum oxide 5-15%, nickel oxide 15-40%.The mixture that each raw material forms can be forms such as wet mixture, dough, mashed prod or slurries.
Under this preparation method's design, the preferred operational condition of each step is:
The particle that step (b) forms can be shapes such as grain, sheet, ball, bar shaped.
The drying temperature of step (c) is 110-150 ℃.
The maturing temperature of step (d) is 300-550 ℃.
The reductive condition of step (e) is: pressure 0.01-1.0Mpa, and temperature 350-550 ℃, the recovery time is 2-6h, reductive agent is H
2, N
2Or H
2With N
2Gas mixture, hydrogen content is at least 50%.
Exist with mixed form between each component of absorbing desulfurization catalyst of the present invention's preparation, adopt the technology of roasting, good, the desulphurizing activated height of intensity, favorable regeneration effect, has higher sulfur capacity (can reach 25 ~ 32%), because of adopting nano zine oxide, little to the octane value influence of gasoline, be fit to very much the desulfurization of gasoline.The preparation method is easy, and is easy to operate.
Embodiment
Below be embodiment, but the present invention is not subjected to the restriction of embodiment.
The particle diameter of the nano zine oxide in following examples is 100～500 μ m.
Embodiment 1
Be prepared as follows reduced nickel metal solid sorbent material:
With 45g nano zine oxide and 25g diatomite silicon oxide, 10gAl
2O
3, 18gNiO mixing 30min, add the 80ml deionized water and mediate 40min, be molded into φ 3mm trifolium catalyzer then.Catalyzer is 120 ℃ of dryings 6 hours, then 500 ℃ of roastings 4 hours.
Make above-mentioned nickel oxide solid adsorbent under 500 ℃, the condition of 0.5Mpa with hydrogen reducing 4 hours, make that nickel is reduced to zero-valent state basically in the catalyzer.
Embodiment 2
The sweetening power of the reduced nickel solid catalyst of preparation in the following test implementation example 1.With the catalyzer of the embodiment 1 gained internal diameter of packing into is in the stainless steel reactor of φ 20mm, volume 30ml, and former granularity is under 500 ℃, with containing 90%H
2, N
2Gas mixture reduction 4 hours is then at H
2Air speed 1000h
-1, 370 ℃ of temperature of reaction, liquid air speed 5h
-1Under the condition, feeding sulfur-bearing is the gasoline of 2000ppm.At reactor outlet, detect sulfur-bearing＜5ppm in the gasoline.
After the test 1, under 370 ℃ of temperature, pressure 0.5Mpa, H
2, N
2Air speed 2000h
-1Following reductase 12 h under 370 ℃ of temperature, pressure 0.5Mpa, progressively feeds O then
2, N
2Regeneration condition was regenerated 3-4 hour down, and catalyzer is regenerated.Make this catalyzer at pressure 0.5Mpa, 500 ℃, H then
2, N
2Air speed 2000h
-1Under reduced 4 hours.
Basically the test 2 of revision test 1 shows to test 6: described catalyzer is renewable to fresh state, can make sulfur in gasoline content reduce to about 5ppm under this state.
Measured Study of Gasoline method octane value (RON) after the desulfurization, the RON of test 1 and 2 products is 89.1, and the RON of described gasoline feeding is 90.9, shows to carry out the octane value that sweetening process of the present invention does not influence gasoline.The results are shown in the table 1 of these tests.
Among this embodiment 2, the reduction of catalyzer, absorption and regeneration are all carried out in same reactor.
Table 1
| Reaction conditions | Test number | |||||
| ????1 | ????2 | ????3 | ????4 | ??5 | ??6 | |
| Catalyst volume ml | ????30 | ????30 | ????30 | ????30 | ??30 | ??30 |
| Pressure (Mpa) | ????2.0 | ????2.0 | ????2.0 | ????2.0 | ??2.0 | ??2.0 |
| H 2Air speed h -1 | ????1000 | ????1000 | ????1000 | ????1000 | ??1000 | ??1000 |
| Temperature of reaction ℃ | ????370 | ????370 | ????370 | ????370 | ??370 | ??370 |
| Reaction times h | Sulfur in gasoline content ppm after the desulfurization | |||||
| 1 | ????0 | ????0 | ????0 | ????0 | ??2.1 | ??0 |
| 2 | ????0 | ????0 | ????0 | ????0 | ??0 | ??0 |
| 3 | ????0 | ????1.1 | ????3.2 | ????1.8 | ??2.1 | ??1.7 |
| 4 | ????1.2 | ????4.3 | ????4.5 | ????3.4 | ??5.0 | ??3.2 |
Embodiment 3
With 60% nano zine oxide, 15% silicon oxide, 5%Al
2O
3, 20%NiO mixing 30min, add the 80ml deionized water and mediate 40min, be molded into φ 3mm pelleted catalyst then.Catalyzer is 140 ℃ of dryings 6 hours, then 550 ℃ of roastings 5 hours.
Make above-mentioned nickel oxide solid adsorbent under 350 ℃, the condition of 1Mpa with hydrogen reducing 6 hours, make that nickel is reduced to zero-valent state basically in the catalyzer.
Embodiment 4
With 20% nano zine oxide, 35% silicon oxide, 5%Al
2O
3, 40%NiO mixing 30min, add the 100ml deionized water and mediate 40min, be molded into φ 3mm pelleted catalyst then.Catalyzer is 110 ℃ of dryings 6 hours, then 350 ℃ of roastings 6 hours.
Make above-mentioned nickel oxide solid adsorbent under 450 ℃, the condition of 0.1Mpa with gas mixture (hydrogen content 60%) reduction of hydrogen and nitrogen 6 hours, make that nickel is reduced to zero-valent state basically in the catalyzer.
Embodiment 5
With 65% nano zine oxide, 5% silicon oxide, 15%Al
2O
3, 15%NiO mixing 30min, add the 80ml deionized water and mediate 40min, be molded into φ 3mm strip catalyst then.Catalyzer is 140 ℃ of dryings 6 hours, then 550 ℃ of roastings 5 hours.
Make above-mentioned nickel oxide solid adsorbent under 350 ℃, the condition of 1Mpa with hydrogen reducing 6 hours, make that nickel is reduced to zero-valent state basically in the catalyzer.
Embodiment 6
With 85% nano zine oxide, 5% silicon oxide, 5%Al
2O
3, 5%NiO mixing 30min, add the 80ml deionized water and mediate 40min, be molded into φ 3mm pelleted catalyst then.Catalyzer is 140 ℃ of dryings 6 hours, then 550 ℃ of roastings 5 hours.
Make above-mentioned nickel oxide solid adsorbent under 550 ℃, the condition of 0.08Mpa with hydrogen reducing 6 hours, make that nickel is reduced to zero-valent state basically in the catalyzer.
Embodiment 7
With 10% nano zine oxide, 80% silicon oxide, 5%Al
2O
3, 5%NiO mixing 30min, add the 80ml deionized water and mediate 40min, be molded into φ 3mm pelleted catalyst then.Catalyzer is 140 ℃ of dryings 6 hours, then 550 ℃ of roastings 5 hours.
Make above-mentioned nickel oxide solid adsorbent under 500 ℃, the condition of 0.6Mpa with hydrogen reducing 4 hours, make that nickel is reduced to zero-valent state basically in the catalyzer.
Embodiment 8
With 10% nano zine oxide, 10% silicon oxide, 30%Al
2O
3, 50%NiO mixing 30min, add the 80ml deionized water and mediate 40min, be molded into φ 3mm pelleted catalyst then.Catalyzer is 140 ℃ of dryings 6 hours, then 500 ℃ of roastings 4 hours.
Make above-mentioned nickel oxide solid adsorbent under 350 ℃, the condition of 1Mpa with hydrogen reducing 6 hours, make that nickel is reduced to zero-valent state basically in the catalyzer.
Claims (10)
1, a kind of catalytic gasoline absorbing desulfurization catalyst is characterized in that its weight percent consists of: particle diameter is nano zine oxide 10-85%, silicon oxide 5-80%, aluminum oxide 5-30%, the reduced state nickel 4-45% of 100 ~ 500 μ m.
2, catalyzer according to claim 1 is characterized in that weight percent consists of: nano zine oxide 45-60%, silicon oxide 15-35%, aluminum oxide 5.0-15%, reduced state nickel 15-40%.
3, catalyzer according to claim 1 and 2 is characterized in that catalyzer is the particle of one of grain, sheet, ball, bar shaped.
4, the preparation method of the described absorbing desulfurization catalyst of a kind of claim 1 is characterized in that comprising the steps:
(a) raw material nano zinc oxide, silicon oxide, aluminum oxide, nickel oxide are mixed;
(b) make gained compound particles granulation form particle;
(c) make the particle drying of step (b);
(d) with the dried particles roasting of step (c);
(e) make particle reduction after the roasting of step (d) gained with the reductive agent that is fit to.
5, preparation method according to claim 4 is characterized in that the weight of each raw material of step (a) consists of: nano zine oxide 10-85%, silicon oxide 5-80%, aluminum oxide 5-30%, nickel oxide 5-50%.
6, preparation method according to claim 5 is characterized in that the weight of each raw material of step (a) consists of: nano zine oxide 45-60%, silicon oxide 15-35%, aluminum oxide 5-15%, nickel oxide 15-40%.
7, preparation method according to claim 4 is characterized in that the particle that step (b) forms is one of grain, sheet, ball, bar shaped.
8, preparation method according to claim 4, the drying temperature that it is characterized in that step (c) is 110-150 ℃.
9, preparation method according to claim 4, the maturing temperature that it is characterized in that step (d) is 300-550 ℃.
10, preparation method according to claim 4 is characterized in that the reductive condition of step (e) is: pressure 0.01-1.0Mpa, and temperature 350-550 ℃, the recovery time is 2-6h, reductive agent is H
2Or H
2With N
2Gas mixture.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB031391591A CN1326977C (en) | 2003-08-22 | 2003-08-22 | Absorbing desulfurizing catalyst for catalytic cracking petroleum and preparing method thereof |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB031391591A CN1326977C (en) | 2003-08-22 | 2003-08-22 | Absorbing desulfurizing catalyst for catalytic cracking petroleum and preparing method thereof |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1583962A true CN1583962A (en) | 2005-02-23 |
| CN1326977C CN1326977C (en) | 2007-07-18 |
Family
ID=34597245
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB031391591A Expired - Fee Related CN1326977C (en) | 2003-08-22 | 2003-08-22 | Absorbing desulfurizing catalyst for catalytic cracking petroleum and preparing method thereof |
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| CN101905161B (en) * | 2009-06-02 | 2012-07-18 | 中国石油天然气股份有限公司 | Catalytic gasoline absorbing desulfurization catalyst, preparation method and application thereof |
| CN101940908B (en) * | 2009-07-08 | 2012-09-05 | 中国石油化工股份有限公司 | Ultra-deep absorption desulfurizer for light oil and application thereof |
| CN103240117A (en) * | 2013-05-17 | 2013-08-14 | 中国石油大学(北京) | Gasoline desulfurization catalyst and preparation method thereof and gasoline desulfurization method |
| CN103805236A (en) * | 2012-11-14 | 2014-05-21 | 中国石油天然气股份有限公司 | Adsorption desulfurization process of catalytically cracked gasoline |
| CN103816858A (en) * | 2014-02-25 | 2014-05-28 | 中国石油大学(北京) | Multifunctional coke oven gas purifying agent and preparation method and application thereof |
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| CN104277874A (en) * | 2013-07-12 | 2015-01-14 | 中国石油天然气股份有限公司 | Method for carrying out adsorption desulfurization on cracked gasoline |
| CN104277877A (en) * | 2013-07-12 | 2015-01-14 | 中国石油天然气股份有限公司 | Adsorption desulfurization process of cracked gasoline |
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| CN107159096A (en) * | 2017-05-02 | 2017-09-15 | 中国石油大学(华东) | Adsorbing and desulfurizing catalytic cracking gasoline agent and preparation method and application |
| CN108187627A (en) * | 2018-01-26 | 2018-06-22 | 北京欧美中科学技术研究院 | A kind of graphene-based high-efficiency desulfurization adsorbent |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6254766B1 (en) * | 1999-08-25 | 2001-07-03 | Phillips Petroleum Company | Desulfurization and novel sorbents for same |
-
2003
- 2003-08-22 CN CNB031391591A patent/CN1326977C/en not_active Expired - Fee Related
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| CN101940908B (en) * | 2009-07-08 | 2012-09-05 | 中国石油化工股份有限公司 | Ultra-deep absorption desulfurizer for light oil and application thereof |
| CN103805236A (en) * | 2012-11-14 | 2014-05-21 | 中国石油天然气股份有限公司 | Adsorption desulfurization process of catalytically cracked gasoline |
| CN103805236B (en) * | 2012-11-14 | 2016-08-10 | 中国石油天然气股份有限公司 | A kind of adsorbing and desulfurizing catalytic cracking gasoline technique |
| CN103834436A (en) * | 2012-11-27 | 2014-06-04 | 中国石油天然气股份有限公司 | Adsorption desulfurization method of catalytic-cracking gasoline |
| CN103834436B (en) * | 2012-11-27 | 2015-12-02 | 中国石油天然气股份有限公司 | A kind of method of adsorbing and desulfurizing catalytic cracking gasoline |
| CN103240117B (en) * | 2013-05-17 | 2015-03-11 | 中国石油大学(北京) | Gasoline desulfurization catalyst and preparation method thereof and gasoline desulfurization method |
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| CN105688801A (en) * | 2014-11-27 | 2016-06-22 | 中国海洋石油总公司 | Gasoline adsorption desulfurizer and preparation method thereof |
| CN105688801B (en) * | 2014-11-27 | 2018-04-17 | 中国海洋石油集团有限公司 | Gasoline adsorbing and desulfurizing agent and preparation method thereof |
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| CN105665031A (en) * | 2016-03-24 | 2016-06-15 | 山东成泰化工有限公司 | Preparation method of novel desulfurization catalyst |
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| CN108187627A (en) * | 2018-01-26 | 2018-06-22 | 北京欧美中科学技术研究院 | A kind of graphene-based high-efficiency desulfurization adsorbent |
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