CN103120955A - Catalyst for converting polycyclic aromatic hydrocarbons into monocyclic aromatic hydrocarbons and preparation method thereof - Google Patents
Catalyst for converting polycyclic aromatic hydrocarbons into monocyclic aromatic hydrocarbons and preparation method thereof Download PDFInfo
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Abstract
The invention relates to a catalyst for converting polycyclic aromatic hydrocarbons into monocyclic aromatic hydrocarbons and a preparation method thereof, mainly solving the problems in the prior art that the conversion level of polycyclic aromatic hydrocarbons is low, the monocyclic aromatic hydrocarbon yield and selectivity are low and the catalyst deactivation rate is high. The problems are better solved by adopting the catalyst and the preparation method thereof. The catalyst comprises 34.5-60wt% of mixture of FAU type zeolite and at least one molecular sieve from MOR, BEA, MFI and MCM-22, 39.5-65wt% of at least one of gamma-alumina, eta-alumina and pseudo-boehmite as a binder and 0.05-0.9wt% of at least one metal from Pt, Pd and Ir. The catalyst can be used in the industrial production of converting heavy polycyclic aromatic hydrocarbons into monocyclic aromatic hydrocarbons.
Description
Technical field
The present invention relates to the Catalysts and its preparation method that a kind of polycyclic aromatic hydrocarbon is converted into mononuclear aromatics.
Background technology
Benzene,toluene,xylene (BTX) etc. is all important Organic Chemicals.Benzene is the basic material of the products such as preparation styrene, nylon, terylene; And toluene is used as the blending compound of gasoline to improve octane number, also can produce paint, binding agent, organic solvent etc. in industry, agricultural and medically be widely used; Dimethylbenzene is used to produce the products such as polyester, chemical fibre more, they are all closely related with the national economic development and people's clothing, food, shelter, row, in recent years sought-after, increment is rapid, and will produce the situation that supply falls short of demand, seeks the aromatic hydrocarbons yield-increasing technology very urgent.Yet, along with the continuous intensification of oil product degree of heaviness and the finiteness of world petroleum resource, for satisfying the growth of the oil demand that economic development brings, by development heavy oil deep conversion, the light-end products of volume increase high added value will be the significant development strategies of 21 century oil refining industry.
Through development for many years, as the important technology hydrotreatment with heavy aromatic hydrocarbon light, although have the advantages such as adaptability to raw materials is wide, conversion level is large at present, but also have the weak points such as reaction temperature and pressure are high, air speed is low, consumption hydrogen is large, catalyst life is short, these also become the emphasis that domestic and international research institution breaks through.
Nippon Oil(Nippon Mitsubishi Oil) report on January 21st, 2010 will be developed the technical matters of producing aromatic hydrocarbon product with light diesel fuel (LCO).Compare with the traditional handicraft of a large amount of consumption hydrogen, this new technology can be cut down production cost, is expected to realize commercially producing.
US6683020B2 discloses a kind of catalyst of open loop, and this catalyst is comprised of a certain proportion of aluminium oxide, aluminosilicate molecular sieves and metal iridium, and the open loop activity is higher, has certain anti-coking performance.The open loop temperature range is at 150～400 ℃, and pressure 100～3000psig, LHSV are 0.1～10h
-1In feed stream, sulfur content can not surpass 10ppm, and in logistics except cycloalkane arene content be no more than 20wt%.
US2007062848A1 disclose a kind of first will carry out again after the polycyclic aromatic hydrocarbon fractional saturation selective opening and take off the method that alkyl obtains light aromatics.The method can satisfy in feed stream polycyclic aromatic hydrocarbon content more than 20wt%, and the saturation stage temperature is at 300～500 ℃, pressure 2～10MPa; The open loop phase temperature is at 200～600 ℃, pressure 1～12MPa.Because the two-stage catalytic agent is contained in same reactor, thus require logistics need to guarantee that certain time of staying could obtain conversion ratio preferably, so air speed is lower.
USP4,341,622 disclose a kind of method of utilizing the heavy reformate to produce BTX.The zeolite that the method adopts that restricted index is 1～12, silica/alumina molar ratio (silica alumina ratio) is 12 or more, hang down acid activity is catalyst, reformate is reacted under the condition of 427～540 ℃, then the product separated is obtained benzene, toluene and dimethylbenzene.Described catalyst contains the VIII family noble metal of hydro-dealkylation function, preferred platinum, and the silica alumina ratio of zeolite used is preferably greater than 200, and more preferably greater than 500, preferred zeolite is ZSM-5.Select the zeolite of high silica alumina ratio for reducing zeolite acidity, keep as far as possible dimethylbenzene and be not converted in reaction.
CN1270989A discloses a kind of C of containing
9 +Heavy arenes lightening catalyst and product separation method, described catalyst is comprised of the zeolite of the MFI structure of the zeolite with MOR structure of the VIII family metal of 0.05～0.3 % by weight, 20～59 heavy %, 20～50 heavy % and the aluminium oxide of 20～40 heavy %.Described method is that heavy arene is contacted with above-mentioned catalyst under 350～450 ℃, 0.5～3.5MPa condition, and gained lighting product can obtain the Organic Ingredients such as BTX and mesitylene, pseudocumene, durol through fractionation.
Summary of the invention
One of technical problem to be solved by this invention is that the polycyclic aromatic hydrocarbon conversion level is low in order to overcome the catalyst that exists in prior art and to be used for the heavy polycyclic aromatic hydrocarbon and to be converted into the mononuclear aromatics reaction, the mononuclear aromatics yield is low and selectively low, the problem that catalyst deactivation rate is fast provides a kind of new catalyst that polycyclic aromatic hydrocarbon is converted into mononuclear aromatics that is used for.This catalyst is used for the reaction that polycyclic aromatic hydrocarbon is converted into mononuclear aromatics, has a polycyclic aromatic hydrocarbon conversion level high, and the mononuclear aromatics yield is high, and mononuclear aromatics is selectively high, the advantage that catalyst deactivation rate is slow.
Two of technical problem to be solved by this invention is to provide the preparation method that a kind of polycyclic aromatic hydrocarbon corresponding with one of technical solution problem is converted into the catalyst of mononuclear aromatics.
For one of solving the problems of the technologies described above, the technical solution used in the present invention is as follows: a kind of polycyclic aromatic hydrocarbon is converted into the catalyst of mononuclear aromatics, comprises by weight percentage following component:
A) 34.5～60%FAU type zeolite and the mixture that is selected from least a molecular sieve in MOR, BEA, MFI or MCM-22;
B) 39.5～65% be selected from least a for binding agent in gama-alumina, η-aluminium oxide or boehmite;
C) 0.05～0.9% at least a metal or its oxide that is selected from Pt, Pd or Ir.
In technique scheme, FAU type zeolite and be selected from least a molecular sieve in MOR, BEA, MFI or MCM-22 and be the sodium weight content lower than 2% Hydrogen or ammonium type zeolite during used catalyst forms; In mixture by weight percentage the amount preferable range of FAU type zeolite be 50～90%, the amount preferable range that is selected from least a molecular sieve in MOR, BEA, MFI or MCM-22 is 10～50%.
For solve the problems of the technologies described above two, the technical solution used in the present invention is as follows: a kind of polycyclic aromatic hydrocarbon is converted into the preparation method of the catalyst of mononuclear aromatics, comprises the following steps:
1. with the FAU type zeolite of aequum and be selected from the mixture of at least a molecular sieve in MOR, BEA, MFI or MCM-22 and being selected from least a binding agent in gama-alumina, η-aluminium oxide, boehmite and carrying out kneading, moulding, drying of aequum after, obtain catalyst carrier at 450～650 ℃ of roasting 0.5～24h;
2. the precursor solution that is selected from least a metal in Pt, Pd or Ir or its oxide of aequum is impregnated into 0.5～24h on catalyst carrier in 30～50 ℃, obtains finished catalyst at 300～450 ℃ of roasting 0.5～24h after drying.
In technique scheme, preferred version can add the extrusion aid that calculates 2～5% weight by the carrier butt, for example sesbania powder in the catalyst carrier preparation process; Can add at least a and water volume ratio acid solution of 1: 1～1: 5 that is selected from hydrochloric acid, nitric acid, acetic acid, tartaric acid, citric acid or oxalic acid by carrier butt calculating 3～6% weight is gelatinizing agent.
In technique scheme, the precursor solution preferred version of Pt metal used is chloroplatinic acid; The precursor solution preferred version of metal Pd is at least a in palladium nitrate or palladium bichloride; The precursor solution preferred version of metal Ir is chloro-iridic acid.
Catalyst provided by the invention is a kind of catalyst that is converted into mononuclear aromatics for the heavy polycyclic aromatic hydrocarbon, can be used for producing benzene, toluene and dimethylbenzene.
In the present invention due to type zeolite such as the FAU that has selected three-dimensional macropore, BEA as the catalyst acid center, be conducive to the acid site that the large molecule of heavy arene enters in the duct and carry out ring-opening reaction, product molecule after conversion can pass through the duct rapid diffusion, thereby has delayed the deactivation rate of catalyst; The precious metal element that has hydrogenating function by load is controlled its load capacity at a zone of reasonableness, can effectively improve the degree of unsaturation of Polycyclic Aromatic Hydrocarbon Mixture raw material, helps the deep conversion polycyclic aromatic hydrocarbon; The rational proportion of catalyst acid center and metallic element takes off alkyl, transalkylation and light aromatic hydrocarbons aromatization generation with part during will making the hydrogenation open loop simultaneously, these reactions will keep original mononuclear aromatics component in feed stream as far as possible, so that the yield of mononuclear aromatics and selective the maximization have been obtained technique effect preferably.
The present invention uses overcritical fixed bed reactors to carry out the reactivity worth investigation that polycyclic aromatic hydrocarbon is converted into mononuclear aromatics, 12 millimeters of reactor inside diameter Φ, 800 millimeters of length, stainless steel.Adopt electrical heating, temperature is controlled automatically.It is supporter that reactor bottom is filled 2～3 millimeters beades of Φ, catalyst filling 5 grams in reactor, and 2～3 millimeters beades of Φ are filled on top, are made for the use of raw material preheating and vaporization.The raw material Polycyclic Aromatic Hydrocarbon Mixture mixes with hydrogen, by beds, makes polycyclic aromatic hydrocarbon be converted into the mononuclear aromatics such as benzene,toluene,xylene from top to bottom.
Polycyclic Aromatic Hydrocarbon Mixture is the autogamy raw material, and experimental data is calculated as follows.
Polycyclic aromatic hydrocarbon total conversion=* 100%
The present invention is further elaborated below by embodiment.
The specific embodiment
[embodiment 1]
Be 30g FAU type zeolite (being purchased Hydrogen), 10g BEA type zeolite (being purchased Hydrogen) and 60g γ-Al with butt
2O
3(industrial goods) add blender to evenly, then add 3g sesbania powder, 5g volume ratio 1: 1HNO in mixture
3Solution and 40g deionized water are ground and are evenly made the dough that is suitable for extruding.It is extruded by mould, and shape is elongated cylindrical (diameter 1.7mm), after 120 ℃ of oven dry in 550 ℃ of roasting 4h, then it is cut into consistent size carrier granular (1.7 * 4.0mm), be designated as Z1.
The chloroplatinic acid wiring solution-forming is flooded carrier granular under 40 ℃, and the amount that contains Pt in maceration extract is 0.1% of carrier butt weight, and dipping 8h at 450 ℃ of roasting 3h, makes finished catalyst A also after drying.
[embodiment 2～6]
Preparation method and process according to embodiment 1 provides in the process to Z1 carrier granular dipping, have prepared a series of finished catalysts by the kind that changes metal precursor in maceration extract, see Table 1.
Table 1
| The catalyst numbering | Carrier forms | Metal precursor | The metal impregnation amount |
| B | Z1 | Palladium nitrate | 0.1wt％Pd |
| C | Z1 | Chloro-iridic acid | 0.1wt％Ir |
| D | Z1 | Chloroplatinic acid, palladium nitrate | 0.032wt％Pt、0.068wt％Pd |
| E | Z1 | Chloroplatinic acid, chloro-iridic acid | 0.05wt％Pt、0.05wt％Ir |
| F | Z1 | Palladium nitrate, chloro-iridic acid | 0.032wt％Ir、0.068wt％Pd |
[embodiment 7～12]
Preparation method and process according to embodiment 1 provides in the process to Z1 carrier granular dipping, have prepared a series of finished catalysts by the pickup that changes metal, see Table 2.
Table 2
| The catalyst numbering | Carrier forms | Metal precursor | The metal impregnation amount |
| G | Z1 | Chloroplatinic acid | 0.2wt％Pt |
| H | Z1 | Chloro-iridic acid | 0.2wt％Ir |
| I | Z1 | Palladium nitrate | 0.2wt％Pd |
| J | Z1 | Chloroplatinic acid, palladium nitrate | 0.09wt％Pt、0.06wt％Pd |
| K | Z1 | Palladium nitrate, chloro-iridic acid | 0.09wt％Ir、0.06wt％Pd |
| L | Z1 | Chloroplatinic acid, chloro-iridic acid | 0.07wt％Pt、0.07wt％Ir |
[embodiment 13～20]
Preparation method and process according to embodiment 1 provides by changing the contamination of metal precursor in carrier composition and maceration extract, have prepared a series of finished catalysts, see Table 3.
Table 3
Catalyst A～the T that makes with embodiment 1～20 (highest response pressure 10MPa, serviceability temperature are room temperature～600 ℃) on overcritical fixed bed reactors investigates and Polycyclic Aromatic Hydrocarbon Mixture is converted into BTX (wherein B is benzene, T is toluene, and X is dimethylbenzene) etc. the ability of mononuclear aromatics.Table 4 forms for the Polycyclic Aromatic Hydrocarbon Mixture raw material.Catalyst packing 5g is at 370 ℃ of reaction temperatures, reaction pressure 6MPa, weight (hourly) space velocity (WHSV) degree 2.0hr
-1, contact with catalyst under hydrogen/hydrocarbon mol ratio 5.0 conditions, product is reclaimed and component detects, conversion results is shown in Table 5.
Table 4 raw material forms
| Raw material forms | Non-aromatic | Benzene | Toluene | Ethylbenzene | Dimethylbenzene | Decahydronaphthalene | Naphthane | Naphthalene |
| Content (wt%) | 0.02 | 24.54 | 24.61 | 5 | 0.02 | 14.81 | 15.25 | 15.75 |
Table 5 polycyclic aromatic hydrocarbon conversion results
| The catalyst numbering | Total conversion (wt%) | Mononuclear aromatics selective (wt%) | BTX selective (wt%) |
| A | 70.5 | 61.2 | 39.6 |
| B | 73.1 | 65.3 | 43.8 |
| C | 68.2 | 63.5 | 38.9 |
| D | 71.8 | 64.0 | 42.2 |
| E | 69.4 | 61.6 | 40.8 |
| F | 71.0 | 64.2 | 43.0 |
| G | 78.3 | 66.1 | 44.2 |
| H | 76.5 | 65.6 | 43.9 |
| I | 80.3 | 65.9 | 45.0 |
| J | 79.4 | 66.3 | 44.8 |
| K | 77.3 | 65.2 | 43.5 |
| L | 76.1 | 64.8 | 42.4 |
| M | 71.0 | 60.3 | 37.2 |
| N | 67.4 | 59.8 | 38.3 |
| O | 65.5 | 58.1 | 33.4 |
| P | 72.3 | 64.9 | 43.0 |
| Q | 67.2 | 59.1 | 36.6 |
| R | 78.9 | 66.3 | 43.2 |
| S | 80.3 | 65.4 | 42.8 |
| T | 72.1 | 60.2 | 39.5 |
[comparative example 1～6]
Catalyst A～the F that makes with embodiment 1～6 investigates the ability of the mononuclear aromatics such as BTX that Polycyclic Aromatic Hydrocarbon Mixture is converted on overcritical fixed bed reactors.Catalyst packing 5g is at 370 ℃ of reaction temperatures, reaction pressure 5MPa, weight (hourly) space velocity (WHSV) degree 2.5hr
-1, contact with catalyst under hydrogen/hydrocarbon mol ratio 6.0 conditions, product is reclaimed and component detects, conversion results is shown in Table 6.
Table 6 polycyclic aromatic hydrocarbon conversion results
| The catalyst numbering | Total conversion (wt%) | Mononuclear aromatics selective (wt%) | BTX selective (wt%) |
| A | 69.3 | 63.1 | 40.8 |
| B | 70.4 | 66.0 | 45.2 |
| C | 65.9 | 65.1 | 40.2 |
| D | 67.1 | 64.8 | 44.1 |
| E | 67.7 | 62.6 | 41.3 |
| F | 70.0 | 65.9 | 44.4 |
Claims (7)
1. a polycyclic aromatic hydrocarbon is converted into the catalyst of mononuclear aromatics, comprises by weight percentage following component:
A) 34.5～60%FAU type zeolite and the mixture that is selected from least a molecular sieve in MOR, BEA, MFI or MCM-22;
B) 39.5～65% be selected from least a for binding agent in gama-alumina, η-aluminium oxide or boehmite;
C) 0.05～0.9% at least a metal or its oxide that is selected from Pt, Pd or Ir.
2. polycyclic aromatic hydrocarbon according to claim 1 is converted into the catalyst of mononuclear aromatics, it is characterized in that FAU type zeolite and be selected from least a molecular sieve in MOR, BEA, MFI or MCM-22 being the sodium weight content lower than 2% Hydrogen or ammonium type zeolite.
3. polycyclic aromatic hydrocarbon according to claim 1 is converted into the catalyst of mononuclear aromatics, it is characterized in that in mixture that the amount of FAU type zeolite is 50～90% by weight percentage, the amount that is selected from least a molecular sieve in MOR, BEA, MFI or MCM-22 is 10～50%.
4. polycyclic aromatic hydrocarbon claimed in claim 1 is converted into the preparation method of the catalyst of mononuclear aromatics, comprises the following steps:
1. with after being selected from least a binding agent in gama-alumina, η-aluminium oxide or boehmite and carrying out kneading, moulding, drying of the mixture that is selected from least a molecular sieve in MOR, BEA, MFI or MCM-22 of the FAU type zeolite of aequum and aequum and aequum, obtain catalyst carrier at 450～650 ℃ of roasting 0.5～24h;
2. the precursor solution that is selected from least a metal in Pt, Pd or Ir or its oxide of aequum is impregnated into 0.5～24h on catalyst carrier in 30～50 ℃, obtains finished catalyst at 300～450 ℃ of roasting 0.5～24h after drying.
5. polycyclic aromatic hydrocarbon according to claim 4 is converted into the preparation method of the catalyst of mononuclear aromatics, it is characterized in that in the catalyst carrier preparation process, preferred version can add the extrusion aid that calculates 2～5% weight by the carrier butt.
6. polycyclic aromatic hydrocarbon according to claim 4 is converted into the preparation method of the catalyst of mononuclear aromatics, it is characterized in that it is gelatinizing agent that preferred version in the catalyst carrier preparation process can add at least a and water volume ratio acid solution of 1: 1～1: 5 that 3～6% weight calculated by the carrier butt are selected from hydrochloric acid, nitric acid, acetic acid, tartaric acid, citric acid or oxalic acid.
7. polycyclic aromatic hydrocarbon according to claim 4 is converted into the preparation method of the catalyst of mononuclear aromatics, and the precursor solution that it is characterized in that described Pt metal is chloroplatinic acid; The precursor solution of metal Pd is at least a in palladium nitrate or palladium bichloride; The precursor solution of metal Ir is chloro-iridic acid.
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| CN108187735A (en) * | 2017-12-30 | 2018-06-22 | 西安元创化工科技股份有限公司 | A kind of catalyst and method that high-knock rating gasoline is produced using coal base light oil |
| CN109126863A (en) * | 2018-10-08 | 2019-01-04 | 中海油天津化工研究设计院有限公司 | A kind of condensed-nuclei aromatics adds the preparation method of the porous Pd composite membrane of hydrogen production mononuclear aromatics |
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