CN104174428A - Catalyst and method for lightening C9<+> heavy aromatics by use of catalyst - Google Patents
Catalyst and method for lightening C9<+> heavy aromatics by use of catalyst Download PDFInfo
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- CN104174428A CN104174428A CN201310192490.5A CN201310192490A CN104174428A CN 104174428 A CN104174428 A CN 104174428A CN 201310192490 A CN201310192490 A CN 201310192490A CN 104174428 A CN104174428 A CN 104174428A
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Abstract
The invention provides a method for lightening C9<+> heavy aromatics. An active component of a catalyst used in the method is palladium, and ZSM-5 zeolite and TiO2 and Al2O3 are used as complex carriers of the catalyst. Preferably, the metal palladium in the catalyst accounts for 0.5-2% of the total weight of the catalyst. According to the method, heavy aromatics and a feedstock of hydrogen in a reaction unit contact with the catalyst. The hydrogenation effect is obvious, and the cost of lightening heavy aromatics is greatly reduced. Reaction temperature of lightening heavy aromatics is 200-280 DEG C and preferably 230-250 DEG C. Low-temperature reaction is not only beneficial to control of the technology and is also conducive to energy conservation and control of reaction cost. In addition, feed stock conversion and BTX yield of the catalyst for lightening C9<+> heavy aromatics are both relatively high.
Description
Technical field
The present invention relates to a kind of catalyst and in the application of heavy aromatics hydro-dealkylation technical field, be specifically related to a kind of palladium series catalyst and in the application of the above heavy aromatic hydrocarbon light technical field of C9.
Background technology
In oil and coal process, the aromatic hydrocarbons of by-product, is mainly C
9and C
10aromatic hydrocarbons, is called heavy arene.Heavy arene is mainly derived from oil plant catalytic reforming unit, ethylene unit by-product drippolene and ethylene bottom oil and coal high-temperature coking by-product coal tar wet goods.Along with the increase of refining capacity and being constructed and put into operation of the large-scale ethene of megaton, heavy arene output will significantly improve.
The comprehensive utilization that the U.S., the former Soviet Union and Japan just begin one's study and develop heavy arene in the 1950's, is mainly by heavy aromatic hydrocarbon light, and heavy arene is transformed and generates the basic petrochemicals such as benzene,toluene,xylene that added value is higher.Abroad, this technology has become most advanced and the most potential technology in heavy arene comprehensive utilization, is the important means that improves heavy arene utilization rate.Catalytic hydrodealkylation technique as one of heavy aromatic hydrocarbon light technology has high, the selective height of conversion ratio, temperature is low, hydrogen consumes low and liquid product yield high, is the study hotspot of current heavy aromatic hydrocarbon light technology.At present, the technique of external heavy aromatic hydrocarbon light mainly contains HAD technique, DETOL technique, the techniques such as TAC9 technique and IEOLYST/SK.Catalyst mainly adopts alumina load metallic catalyst or molecular sieve carried metallic catalyst.
China, and abroad compares since 20 century 70s the utilization research of heavy arene, and the utilization of China's heavy arene is the preliminary stage in development still; So China is every year still at a large amount of import benzene,toluene,xylenes especially paraxylene and downstream derivative etc. thereof.Given this, develop a kind of method of heavy aromatic hydrocarbon light, comprehensively effectively utilize heavy arene resource, the situation of alleviating a large amount of dependence on import of China's benzene,toluene,xylene is imperative.CN101885663A has announced a kind of method of heavy aromatics lighting and transalkylation, specifically by adopting 5～95 parts to take ZSM-5 as nuclear phase and the β zeolite grain of the usining core-shell type molecular sieve that is shell and 95～5 parts of binding agents are as catalyst C
9 +heavy aromatics lighting, under certain conditions such as temperature and pressure, its heavy aromatics conversion ratio is 40～60% left and right.
Summary of the invention
In view of above-mentioned prior art situation, present inventor has carried out research extensively and profoundly in heavy arene hydrogenation dealkylation catalyst application, to finding a kind of good hydrogenation catalyst can make heavy aromatic hydrocarbon light.Found that, use a kind of palladium series catalyst, select ZSM-5 zeolite and TiO
2and Al
2o
3complex carrier, under certain process conditions, can efficiently impel C
9 +heavy aromatic hydrocarbon light, and catalyst Heat stability is good, heavy arene conversion ratio and benzene,toluene,xylene yield are improved.
Therefore first the present invention provides a kind of palladium series catalyst, and the active component of described catalyst is palladium, and the carrier of catalyst is ZSM-5 zeolite and TiO
2and Al
2o
3complex carrier.
Preferably, the weight of Metal Palladium is described total catalyst weight 0.5～2%.Further, ZSM-5 zeolite accounts for 20～80wt% of carrier, TiO
2and Al
2o
3account for altogether 20～80wt% of carrier.
In catalyst preparation process of the present invention, preferred described complex carrier, before impregnating metal palladium, is first used NH
4cl solution carries out ion-exchange to it.
The present invention also provides a kind of C
9 +the method of heavy aromatic hydrocarbon light, the catalyst activity component that it uses is palladium, and this catalyst is with ZSM-5 zeolite and TiO
2and Al
2o
3for complex carrier.In the method for the invention, comprise the charging of heavy arene and hydrogen is contacted with described catalyst in reaction unit.Hydrogenation successful of the present invention, reduces heavy aromatics lighting cost greatly.
In the methods of the invention, preferably, the weight of Metal Palladium is described total catalyst weight 0.5～2%.Further, in described complex carrier, ZSM-5 zeolite accounts for 20～80wt% of carrier, TiO
2and Al
2o
3account for altogether 20～80wt% of carrier.In the present invention, complex carrier is such as being cloverleaf pattern, bar shaped, sheet shape or the Common Shape such as cylindrical.Further, in described complex carrier, TiO
2with Al
2o
3weight ratio be 1:3～6.
In the methods of the invention, preferably, the reaction temperature of described heavy aromatic hydrocarbon light is 200～280 ℃, more preferably 230～250 ℃; Reaction pressure is 1～4MPa, more preferably 2～3MPa; Charging air speed is 0.5～4h
-1, more preferably 1～2h
-1.In heavy arene hydrogenation process of the present invention, adopt the process conditions that are as above easier to control.In addition, in the present invention the reaction temperature of heavy aromatic hydrocarbon light lower than reaction temperature of the prior art, for example in CN101885663A, announce 350～500 ℃; Low-temp reaction is not only conducive to the control of technique, also helps energy-conservation and control reaction cost.
The present invention also provides a kind of method of heavy aromatic hydrocarbon light, it is characterized in that the catalyst that uses active component to be palladium, and the weight of Metal Palladium is described total catalyst weight 0.5～2%.
The specific embodiment
Below be only the preferred embodiment of the present invention, protection scope of the present invention is not limited to this, and any those skilled in the art is in technical scope disclosed by the invention, within can being easy to the change carried out or changing and be encompassed in protection scope of the present invention.Therefore, protection scope of the present invention should be as the criterion with the protection domain of claims.
In the present invention, charging air speed is the ratio of charging quality per hour and catalyst quality, and unit is h
-1.The present invention describes the hydrogenation effect of product with heavy arene conversion ratio.
Raw material heavy arene of the present invention derives from oil plant catalytic reforming unit byproduct or chemical plant ethylene unit by-product drippolene.Any suitable reactions device that reaction unit used is known to those skilled in the art, for example, used fixedly isothermal bed hydroprocessing reaction unit.In charging, the volume ratio of hydrogen and heavy arene is preferably 600～1000.Before charging is dropped into reaction unit, first utilize hydrogen by the catalyst reduction being loaded in reaction unit, for example under the constant temperature of 120 ℃, utilize hydrogen reducing 10 hours; Again under suitable process conditions to C
9 +heavy arene carries out hydrotreatment.
Catalyst preparation example 1～7
The preparation of complex carrier: be 160m by 100g specific surface
2/ g and pore volume are that the dilution heat of sulfuric acid that the cylindrical aluminium oxide of 0.74ml/g is 0.6g/ml with 205ml sulfur acid titanium floods 6 hours, at the temperature of 120 ℃, be dried 10 hours, the roasting temperatures of 600 ℃ 6 hours, obtain 125g aluminium oxide-titanium oxide carrier, wherein the weight ratio of aluminium oxide and titanium oxide is 4:1.Press proportioning in table 1 by ZSM-5 zeolite and above-mentioned TiO
2compound Al
2o
3carrier mixes, and to add concentration be the aqueous solution of nitric acid kneading of 2wt%, extruded moulding, and 120 ℃ are dry, and in air, 600 ℃ of roastings obtain complex carrier for 4 hours.
The preparation of catalyst: get above-mentioned complex carrier, use the NH of 0.5g/ml at 100 ℃
420 milliliters of Cl solution carry out ion-exchange 3 hours to carrier, filter, washing, and 120 ℃ dry.Then with palladium chloride solution dipping, filter, under 120 ℃ of conditions, be dried 15 hours, in air, under 600 ℃ of conditions, roasting obtains catalyst for 5 hours.In catalyst preparation example 1～7, gained catalyst is denoted as respectively catalyst A, B, C, D, E, F and G.Wherein ZSM-5 content is the weight content that ZSM-5 accounts for complex carrier, TiO
2and Al
2o
3content is that the two accounts for the weight content of complex carrier altogether; And Pd content refers to that this element accounts for the weight content of catalyst.
Catalyst preparation example 8
The preparation of complex carrier: in this example, the preparation of catalyst complex carrier and catalyst preparation example 3 are basically identical, but because adjusting the consumption of titanium sulfate maceration extract, to make the weight ratio of aluminium oxide and titanium oxide in complex carrier be 1:1, and gained complex carrier is for the preparation of catalyst.
The preparation of catalyst: in this example, the preparation method of catalyst is consistent with the method in above-mentioned catalyst preparation example 3, and gained catalyst is denoted as catalyst H.
Table 1
| ? | Catalyst numbering | ZSM-5 content | TiO 2And Al 2O 3Content | Pd content (%) |
| Catalyst preparation example 1 | A | 80% | 20% | 0.5 |
| Catalyst preparation example 2 | B | 75% | 25% | 1 |
| Catalyst preparation example 3 | C | 70% | 30% | 1.5 |
| Catalyst preparation example 4 | D | 80% | 20% | 2 |
| Catalyst preparation example 5 | E | 60% | 40% | 2 |
| Catalyst preparation example 6 | F | 95% | 5% | 1.5 |
| Catalyst preparation example 7 | G | 70% | 30% | 0.1 |
| Catalyst preparation example 8 | H | 70% | 30% | 1.5 |
Embodiment 1
Use 100ml isothermal bed hydroprocessing reaction evaluating device, pack catalyst A into, reaction temperature is 200 ℃, and reaction pressure is 3.0MPa, and charging air speed is 1.0h
-1, C
9 +heavy arene hydrogenation effect is in Table 2.In table 2, BTX represents benzene-toluene-xylene mixture.
Embodiment 2
Use 100ml isothermal bed hydroprocessing reaction evaluating device, pack catalyst A into, reaction temperature is 240 ℃, and reaction pressure is 3.0MPa, and charging air speed is 2.0h
-1, C
9 +heavy arene hydrogenation effect is in Table 2.
Embodiment 3
Use 100ml isothermal bed hydroprocessing reaction evaluating device, pack catalyst B into, reaction temperature is 260 ℃, and reaction pressure is 1.0MPa, and charging air speed is 0.5h
-1, C
9 +heavy arene hydrogenation effect is in Table 2.
Embodiment 4
Use 100ml isothermal bed hydroprocessing reaction evaluating device, pack catalyst B into, reaction temperature is 250 ℃, and reaction pressure is 3.0MPa, and charging air speed is 1.0h
-1, C
9 +heavy arene hydrogenation effect is in Table 2.
Embodiment 5
Use 100ml isothermal bed hydroprocessing reaction evaluating device, pack catalyst C into, reaction temperature is 260 ℃, and reaction pressure is 4.0MPa, and charging air speed is 2.0h
-1, C
9 +heavy arene hydrogenation effect is in Table 2.
Embodiment 6
Use 100ml isothermal bed hydroprocessing reaction evaluating device, pack catalyst C into, reaction temperature is 240 ℃, and reaction pressure is 3.0MPa, and charging air speed is 1.5h
-1, C
9 +heavy arene hydrogenation effect is in Table 2.
Embodiment 7
Use 100ml isothermal bed hydroprocessing reaction evaluating device, pack catalyst D into, reaction temperature is 250 ℃, and reaction pressure is 3.0MPa, and charging air speed is 1.0h
-1, C
9 +heavy arene hydrogenation effect is in Table 2.
Embodiment 8
Use 100ml isothermal bed hydroprocessing reaction evaluating device, pack catalyst D into, reaction temperature is 280 ℃, and reaction pressure is 3.0MPa, and charging air speed is 4.0h
-1, C
9 +heavy arene hydrogenation effect is in Table 2.
Embodiment 9
Use 100ml isothermal bed hydroprocessing reaction evaluating device, pack catalyst E into, reaction temperature is 230 ℃, and reaction pressure is 3.5MPa, and charging air speed is 3.0h
-1, C
9 +heavy arene hydrogenation effect is in Table 2.
Embodiment 10
Use 100ml isothermal bed hydroprocessing reaction evaluating device, pack catalyst D into, reaction temperature is 250 ℃, and reaction pressure is 3.0MPa, and charging air speed is 2.0h
-1, C
9 +heavy arene hydrogenation effect is in Table 2.
Embodiment 11
Use 100ml isothermal bed hydroprocessing reaction evaluating device, pack catalyst F into, reaction temperature is 250 ℃, and reaction pressure is 3.0MPa, and charging air speed is 2.0h
-1, C
9 +heavy arene hydrogenation effect is in Table 2.
Embodiment 12
Use 100ml isothermal bed hydroprocessing reaction evaluating device, pack catalyst G into, reaction temperature is 250 ℃, and reaction pressure is 3.0MPa, and charging air speed is 2.0h
-1, C
9 +heavy arene hydrogenation effect is in Table 2.
Embodiment 13
Use 100ml isothermal bed hydroprocessing reaction evaluating device, pack catalyst H into, reaction temperature is 250 ℃, and reaction pressure is 3.0MPa, and charging air speed is 2.0h
-1, C
9 +heavy arene hydrogenation effect is in Table 2.
Comparative example 1
Use 100ml isothermal bed hydroprocessing reaction evaluating device, (this catalyst adopts nano zeolite and SiO to pack domestic similar catalyst into
2and Al
2o
3complex carrier, active component is noble metal), reaction temperature is 250 ℃, reaction pressure is 3.0MPa, charging air speed is 2.0h
-1, C
9 +heavy arene hydrogenation effect is in Table 2.
Table 2
From table 2, C in the present invention
9 +heavy aromatic hydrocarbon light can carry out at relatively low temperature, and its heavy aromatics conversion ratio and BTX yield are all higher.In addition, from embodiment 10～13 and comparative example 1, under same appreciation condition, use catalyst of the present invention to C
9 +the feed stock conversion of heavy aromatic hydrocarbon light and BTX yield are all relatively high.
Claims (10)
1. a palladium series catalyst, the active component of described catalyst is palladium, the carrier of catalyst is ZSM-5 zeolite and TiO
2and Al
2o
3complex carrier.
2. catalyst according to claim 1, is characterized in that, the weight of Metal Palladium is described total catalyst weight 0.5～2%.
3. catalyst according to claim 1 and 2, is characterized in that, in described complex carrier, ZSM-5 zeolite accounts for 20～80wt% of carrier, TiO
2and Al
2o
3account for altogether 20～80wt% of carrier.
4. according to the catalyst described in any one in claim 1～3, it is characterized in that, in catalyst preparation process, described complex carrier, before impregnating metal palladium, is first used NH
4cl solution carries out ion-exchange to it.
5. a C
9 +the method of heavy aromatic hydrocarbon light, is characterized in that, the catalyst activity component of using is palladium, and this catalyst is with ZSM-5 zeolite and TiO
2and Al
2o
3for complex carrier.
6. method according to claim 5, is characterized in that, the weight of Metal Palladium is described total catalyst weight 0.5～2%.
7. according to the method described in claim 5 or 6, it is characterized in that, in described complex carrier, ZSM-5 zeolite accounts for 20～80wt% of carrier, TiO
2and Al
2o
3account for altogether 20～80wt% of carrier.
8. method according to claim 7, is characterized in that, in described complex carrier, and TiO
2with Al
2o
3weight ratio be 1:3～6.
9. according to the method described in any one in claim 5～8, it is characterized in that, the reaction temperature of described heavy aromatic hydrocarbon light is 200～280 ℃, preferably 230～250 ℃; Reaction pressure is 1～4MPa, preferably 2～3MPa; Charging air speed is 0.5～4h
-1, preferred 1～2h
-1.
10. a method for heavy aromatic hydrocarbon light, is characterized in that the catalyst that uses active component to be palladium, and the weight of Metal Palladium is described total catalyst weight 0.5～2%.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310192490.5A CN104174428B (en) | 2013-05-22 | 2013-05-22 | A kind of catalyst and its method for C9 or more heavy aromatic hydrocarbon light |
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|---|---|---|---|
| CN201310192490.5A CN104174428B (en) | 2013-05-22 | 2013-05-22 | A kind of catalyst and its method for C9 or more heavy aromatic hydrocarbon light |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105016947A (en) * | 2015-07-15 | 2015-11-04 | 河南师范大学 | Method for synthesizing 1,3-butadiyne compound by copper (II) carboxymethylcellulose catalysis of terminal alkyne compound |
| CN110639545A (en) * | 2018-06-27 | 2020-01-03 | 中国石油化工股份有限公司 | Heavy distillate oil selective hydrogenation catalyst and application thereof |
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| CN1117404A (en) * | 1994-08-22 | 1996-02-28 | 中国石油化工总公司 | Catalyst and method for converting heavy arene into light one |
| US5744674A (en) * | 1996-02-06 | 1998-04-28 | China Petrochemical Corporation | Catalyst and process for the conversion of heavy aromatics to light aromatics |
| CN1814712A (en) * | 2005-01-31 | 2006-08-09 | 中国石油化工股份有限公司 | Modifying catalyst for naphtha processed maferial and method therefor |
| CN1906272A (en) * | 2004-01-22 | 2007-01-31 | 波利玛利欧洲股份公司 | Process for the catalytic hydrodealkylation of alkylaromatic hydrocarbons |
| CN103261375A (en) * | 2010-12-13 | 2013-08-21 | 埃克森美孚研究工程公司 | Conversion catalysts and processes having oxygenate and water stability |
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2013
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Patent Citations (5)
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|---|---|---|---|---|
| CN1117404A (en) * | 1994-08-22 | 1996-02-28 | 中国石油化工总公司 | Catalyst and method for converting heavy arene into light one |
| US5744674A (en) * | 1996-02-06 | 1998-04-28 | China Petrochemical Corporation | Catalyst and process for the conversion of heavy aromatics to light aromatics |
| CN1906272A (en) * | 2004-01-22 | 2007-01-31 | 波利玛利欧洲股份公司 | Process for the catalytic hydrodealkylation of alkylaromatic hydrocarbons |
| CN1814712A (en) * | 2005-01-31 | 2006-08-09 | 中国石油化工股份有限公司 | Modifying catalyst for naphtha processed maferial and method therefor |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105016947A (en) * | 2015-07-15 | 2015-11-04 | 河南师范大学 | Method for synthesizing 1,3-butadiyne compound by copper (II) carboxymethylcellulose catalysis of terminal alkyne compound |
| CN105016947B (en) * | 2015-07-15 | 2017-01-18 | 河南师范大学 | Method for synthesizing 1,3-butadiyne compound by copper (II) carboxymethylcellulose catalysis of terminal alkyne compound |
| CN110639545A (en) * | 2018-06-27 | 2020-01-03 | 中国石油化工股份有限公司 | Heavy distillate oil selective hydrogenation catalyst and application thereof |
| CN110639545B (en) * | 2018-06-27 | 2022-07-12 | 中国石油化工股份有限公司 | Heavy distillate oil selective hydrogenation catalyst and application thereof |
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