CN102701897A - Method for preparing cyclic hydrocarbon compounds by hydrogenation of wash oil fraction - Google Patents
Method for preparing cyclic hydrocarbon compounds by hydrogenation of wash oil fraction Download PDFInfo
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- CN102701897A CN102701897A CN2012101621217A CN201210162121A CN102701897A CN 102701897 A CN102701897 A CN 102701897A CN 2012101621217 A CN2012101621217 A CN 2012101621217A CN 201210162121 A CN201210162121 A CN 201210162121A CN 102701897 A CN102701897 A CN 102701897A
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Abstract
The invention discloses a method for preparing cyclic hydrocarbon compounds by hydrogenation of wash oil fraction, and belongs to the technical field of coal processing utilization and coal conversion. The method is characterized in that industrial coal tar wash oil is used as a raw material, and is diluted by a solvent to be used as a hydrogenation raw material, and the cyclic hydrocarbon compounds with high added value are prepared by hydrofining, wherein the hydrogenation reaction temperature is controlled at 200-380 DEG C, hydrogen partial pressure is 3-6MPa, and the solvent can be recycled after the product is simply separated after hydrogenation. The hydrofining process is used for deep processing of the coal tar wash oil fraction and residual fractions after industrial-grade chemical products are extracted from the wash oil. The hydrofining process has excellent economic benefits and industrial application prospects.
Description
Technical field
The invention belongs to coal processing and utilization and coal transformation technology field, relate to and a kind ofly prepare the method for cyclic hydrocar-bons compound by the coal tar wash oil cut through unifining, prepared cyclic hydrocar-bons compound belongs to high added value fine chemicals, steady quality.
Background technology
The black in color thickness is aqueous at normal temperatures and pressures for the coal tar that obtains in the coal tar process, and its output accounts for 3% ~ 4% of shove charge coal, forms very complicacy, in most cases is to be used after being separated specially, purified by coal-tar industry.
Processing to coal tar at present comprises that hydrogen cracking prepares petrol and diesel oil and cuts different cuts with continuous still battery.Face the problem of catalyzer catalyzer coking under hot conditions in the coal tar hydrocracking technology.CN101993728A discloses a kind of method of preparing diesel from coal tar, coal tar air distillation cut below 370 ℃ is carried out unifining prepare diesel oil under Co, Mo catalyst action.CN101250433A discloses the technology that a kind of coal tar hydrogenating prepares gasoline, diesel oil, light-weight fuel oil.Although the hydrogenation technique that CN101250433A proposes can slow down coking, the problem of catalyzer coking still fundamentally is not resolved in the coal tar hydrocracking technology.
The coal tar continuous still battery can cut following several fractions: light oil, carbolic oil, naphtalene oil, washing oil, carbolineum and pitch fractions, and different fractions is further processed separation can produce multiple product.Washing oil is further processed the existing report of the method for extracting the technical grade industrial chemicals.CN101182277A disclose a kind of from contain 15% biphenyl extract the method for technical grade biphenyl in the matter washing oil, obtain technical methylnaphthalene simultaneously, mix dimethylnaphthalene, acenaphthene cut.CN101982523A discloses 4 groups of methods that rectifying tower is processed washing oil continuously of a kind of employing, can obtain stay-in-grade industrial naphtalene oil, methylnaphthalene, middle matter washing oil, acenaphthene, dibenzofuran, fluorenes product.CN102180763A disclose a kind of from washing oil the method for separation industries acenaphthene, technical process is simple, can be continuously produced stay-in-grade acenaphthene.CN1651367A discloses a kind of method of from coal tar wash oil, extracting high-purity acenaphthene through single tower rectification under vacuum technology.Above technology only limits to that all washing oil is carried out separation and Extraction and goes out industrial chemical, does not relate to it is carried out the unifining processing.
Summary of the invention
Remaining wash oil fraction provided a kind of direct unifining to prepare the method for cyclic hydrocarbon after the means such as the rectifying of wash oil fraction or washing oil process, extraction, crystallization that the present invention is directed to were extracted valuable chemical; With production high added value fine chemicals is target; Realize the comprehensive utilization of coal tar wash oil cut, greatly improved the economic benefit of coal tar chemical industry.
Technical scheme of the present invention is following:
Coal tar wash oil among the present invention comprises the wash oil fraction of coal tar continuous still battery, also can be to extract remaining wash oil fraction behind the valuable chemical through means such as rectifying, chemical extraction, crystallization, or the mixing of the raw material of aforementioned two kinds of forms.These chemical comprise methylnaphthalene, quinoline material, biphenyl, indoles, acenaphthene, dibenzofuran, fluorenes or their mixture.The washing oil hydrogenating materials can be the single raw material of wash oil fraction behind coal tar wash oil cut, the process extraction technical grade chemical, also can be their mixture.
The Hydrobon catalyst that uses among the present invention is load type metal catalyst.Wherein metal comprises the mixing of Ni, Co, Mo, Pd, Ru, Pt or these metals, and the mass percent that accounts for load type metal catalyst is 0.1-30%; Carrier is oxide carrier or raw material of wood-charcoal material, and oxide carrier is SiO
2, Al
2O
3, TiO
2, SiO
2-Al
2O
3, Al
2O
3-TiO
2Or SiO
2-Al
2O
3-TiO
2, raw material of wood-charcoal material carrier is the mixing of gac, carbon nanotube, coconut husk charcoal or above raw material of wood-charcoal material.Hydrogenating materials at first with solvent cut, wherein to account for the mass percent of dilution back mixture be 30-90% to solvent, through mixing with hydrogen; Heating gets into hydrofining reactor then; Control reaction temperature is at 200-380 ℃, hydrogen partial pressure 3-6MPa, volume space velocity 0.5-4.0h
-1With hydrogen to oil volume ratio be 400-1200:1.Reactor product obtains the hydro carbons fine chemicals through after the simple separation, and diluting solvent can reuse.The fine chemicals that hydrogenation obtains is one type of cyclic hydrocar-bons compound.
The diluting solvent that uses among the present invention comprises hexanaphthene, octane, n-decane, n-dodecane, n-hexadecane or their mixture.
Hydrogen can use recycle hydrogen in the hydrogen refining process of the present invention, and diluting solvent can be separated from product, reuses.The unifining raw material can directly use coal tar wash oil cut without aftertreatment as raw material, and hydrogen refining process requires lowly to raw material, and feed composition is flexible, has reduced production cost, has improved economic benefit.
Embodiment
Be described in detail specific embodiment of the present invention below in conjunction with technical scheme.
Embodiment 1
On fixed-bed reactor, carry out little reaction evaluating with the analytical pure dibenzofuran as model compound.Preparation dibenzofuran n-decane solution is as hydrogenating materials, and wherein the massfraction of dibenzofuran is 5%, and adopting the load-type nickel molybdenum catalyst is hydrogenation catalyst, and nickel molybdenum catalyst adopts SiO
2-Al
2O
3As carrier, metal precursor adopts nickelous nitrate and ammonium molybdate, and the nickel molybdenum atom prepares load-type nickel molybdenum catalyst through equi-volume impregnating through dipping-drying-roasting-steps such as reduction than for 5:1.Hydrogenation reaction hydrogen dividing potential drop 6MPa, volume space velocity 0.5h
-1, hydrogen-oil ratio 800,340 ℃ of temperature of reaction.Reaction back dibenzofuran transformation efficiency 95.2% joins hexanaphthene selectivity 37.3%, Santosol 360 selectivity 48.2%.
Embodiment 2
On fixed-bed reactor, carry out little reaction evaluating with the analytical pure dibenzofuran as model compound.Preparation dibenzofuran cyclohexane solution is as hydrogenating materials; Wherein the dibenzofuran massfraction is 8%; Adopting load type platinum palladium bimetallic catalyst is hydrogenation catalyst, and catalyzer adopts gac as carrier, and metal precursor adopts platinum nitrate and palladium acetylacetonate; Platinum palladium atomic ratio is 1:1, and the metal loading is 0.5% to prepare load type platinum palladium bimetallic catalyst through equi-volume impregnating through dipping-drying-roasting-steps such as reduction.Hydrogenation reaction hydrogen dividing potential drop 3MPa, volume space velocity 1h
-1, hydrogen-oil ratio 400,240 ℃ of temperature of reaction.Reaction back dibenzofuran transformation efficiency 97.3% joins hexanaphthene selectivity 74.5%, Santosol 360 selectivity 23.7%.
Embodiment 3
On fixed-bed reactor, carry out little reaction evaluating with the analytical pure fluorenes as model compound.Preparation fluorenes n-decane solution is as hydrogenating materials, and wherein the massfraction of fluorenes is 4%, and the employing load type palladium catalyst is a hydrogenation catalyst, and catalyzer adopts SiO
2-Al
2O
3As carrier, metal precursor adopts Palladous nitrate, and the metal loading is 0.5%.Prepare load type palladium catalyst through equi-volume impregnating through dipping-drying-roasting-steps such as reduction.Hydrogenation reaction hydrogen dividing potential drop 3MPa, volume space velocity 4h
-1, hydrogen-oil ratio 600,200 ℃ of temperature of reaction.Reaction back fluorenes transformation efficiency 96.1%, six hydrogen fluorenes selectivity 49.8%, perhydro fluorenes selectivity 47.1%.
Embodiment 4
On fixed-bed reactor, carry out little reaction evaluating with the analytical pure acenaphthene as model compound.Mixed solvent with octane and n-dodecane dilutes acenaphthene as hydrogenating materials; Wherein the massfraction of acenaphthene is 4%; Adopting the load type platinum ruthenium bimetallic catalyst is hydrogenation catalyst, and catalyzer adopts gac-coconut husk charcoal mixt as carrier, and metal precursor adopts platinum chloride and ruthenium chloride; The platinum ruthenium atom is than 4:1, and the metal loading is 0.5%.Prepare the load type platinum ruthenium bimetallic catalyst through equi-volume impregnating through dipping-drying-roasting-steps such as reduction.Hydrogenation reaction hydrogen dividing potential drop 3MPa, volume space velocity 2h
-1, hydrogen-oil ratio 500,280 ℃ of temperature of reaction.Reaction back acenaphthene transformation efficiency 97.8%, tetrahydrochysene acenaphthene selectivity 21.3%, perhydro acenaphthene selectivity 77.1%.
Embodiment 5
Mixture with analytical pure dibenzofuran, fluorenes carries out little reaction evaluating as model compound on fixed-bed reactor.The mass ratio of dibenzofuran, fluorenes is 7:3 in the mixture; With the mixture of n-dodecane dilution dibenzofuran and fluorenes, wherein the massfraction of mixture is 10%, with the mixture of dibenzofuran after diluting and fluorenes as hydrogenating materials; Adopting load-type nickel molybdenum bimetallic catalyst is hydrogenation catalyst, and catalyzer adopts SiO
2As carrier, metal precursor adopts acetylacetonate nickel and ammonium molybdate, and the nickel molybdenum atom is than being 4:1, and the metal loading is 10%.Prepare load-type nickel molybdenum bimetallic catalyst through equi-volume impregnating through dipping-drying-roasting-steps such as reduction.Hydrogenation reaction hydrogen dividing potential drop 6MPa, volume space velocity 1h
-1, hydrogen-oil ratio 1200,350 ℃ of temperature of reaction.Reaction back dibenzofuran transformation efficiency 97.5% joins hexanaphthene selectivity 68.5%, Santosol 360 selectivity 27.6%.Fluorenes transformation efficiency 95.6%, six hydrogen fluorenes selectivity 70.4%, perhydro fluorenes selectivity 27.2%.
Embodiment 6
Mixture with analytical pure acenaphthene, dibenzofuran, fluorenes carries out little reaction evaluating as model compound on fixed-bed reactor.The mass ratio of acenaphthene, dibenzofuran, fluorenes is 3:4:3 in the mixture; Dilute the mixture of acenaphthene, dibenzofuran and fluorenes with n-decane; Wherein the massfraction of the mixture of acenaphthene, dibenzofuran and fluorenes is 7%; As hydrogenating materials, adopting load type platinum palladium bimetallic catalyst is hydrogenation catalyst with the mixture of acenaphthene, dibenzofuran after the dilution, fluorenes, and catalyzer adopts SiO
2As carrier, metal precursor adopts potassium platinichloride and Palladous nitrate, and platinum palladium atomic ratio is 1:1, and the metal loading is 0.5%.Prepare load type platinum palladium bimetallic catalyst through equi-volume impregnating through dipping-drying-roasting-steps such as reduction.Hydrogenation reaction hydrogen dividing potential drop 3MPa, volume space velocity 1h
-1, hydrogen-oil ratio 400,280 ℃ of temperature of reaction.Reaction back acenaphthene transformation efficiency 97.2%, tetrahydrochysene acenaphthene selectivity 23.5%, decahydro acenaphthene selectivity 70.4%.Dibenzofuran transformation efficiency 96.5% joins hexanaphthene selectivity 72.5%, Santosol 360 selectivity 24.3%.Fluorenes transformation efficiency 95.4%, six hydrogen fluorenes selectivity 61.8%, perhydro fluorenes selectivity 35.1%.
Embodiment 7
Several kinds of different technical grade coal tar wash oils in source are carried out proximate analysis, get the 5g sample and analyze, the combined standard sample carries out quantitative analysis to the acenaphthene in the raw material, dibenzofuran, fluorenes.The result is as shown in the table,
Can find out that staple is acenaphthene, dibenzofuran, fluorenes in these several kinds of wash oil fractions, and the content of dibenzofuran is maximum in these three kinds of compounds.
Embodiment 8
With No. 2 washing oil samples is that raw material carries out little reaction evaluating on fixed-bed reactor.With No. 2 washing oil of mixed solvent dilution of hexanaphthene and n-decane, wherein the massfraction of washing oil is 50%, and as hydrogenating materials, adopting load-type nickel molybdenum bimetallic catalyst is hydrogenation catalyst with the washing oil after the dilution, and catalyzer adopts SiO
2As carrier, metal precursor adopts nickelous acetate and ammonium molybdate, and the nickel molybdenum atom is than being 4:1, and the metal loading is 10%, prepares load-type nickel molybdenum bimetallic catalyst through equi-volume impregnating through dipping-drying-roasting-steps such as reduction.Hydrogenation reaction hydrogen dividing potential drop 6MPa, volume space velocity 0.5h
-1, hydrogen-oil ratio 1000,360 ℃ of temperature of reaction.Reaction back acenaphthene transformation efficiency 95.5%, tetrahydrochysene acenaphthene selectivity 42.5%, decahydro acenaphthene selectivity 50.8%, dibenzofuran transformation efficiency 95.6% joins hexanaphthene selectivity 65.3%, Santosol 360 selectivity 31.3%.Fluorenes transformation efficiency 93.7%, six hydrogen fluorenes selectivity 67.5%, perhydro fluorenes selectivity 28.8%.
Claims (5)
1. the method for a wash oil fraction hydrogenation preparing cyclic hydrocar-bons compound is characterized in that,
Coal tar wash oil and solvent cut; The mass percent of mixture was 30-80% after wherein solvent accounted for and dilutes, and mixed with hydrogen, and heating gets into hydrofining reactor then; Hydrogenation catalyst is a load type metal catalyst; Control reaction temperature is at 200-380 ℃, hydrogen partial pressure 3-6MPa, volume space velocity 0.5-4.0h
-1With hydrogen to oil volume ratio be 400-1200:1.
2. the method for a kind of wash oil fraction hydrogenation preparing cyclic hydrocar-bons compound according to claim 1; It is characterized in that coal tar wash oil comprises the wash oil fraction of coal tar continuous still battery, from wash oil fraction, extract remaining wash oil fraction or its blend mixture behind the valuable chemical.
3. the method for a kind of wash oil fraction hydrogenation preparing cyclic hydrocar-bons compound according to claim 1 and 2 is characterized in that, employed solvent comprises hexanaphthene, octane, n-decane, n-dodecane, n-hexadecane or their mixture.
4. the method for a kind of wash oil fraction hydrogenation preparing cyclic hydrocar-bons compound according to claim 1 and 2; It is characterized in that; Metal in the described load type metal catalyst comprises Ni, Co, Mo, Pd, Ru, Pt or its mixing, and accounting for the load type metal catalyst mass percent is 0.1-30%.
5. the method for a kind of wash oil fraction hydrogenation preparing cyclic hydrocar-bons compound according to claim 1 and 2 is characterized in that, the carrier in the described load type metal catalyst comprises oxide carrier or raw material of wood-charcoal material carrier, and wherein oxide carrier is SiO
2, Al
2O
3, TiO
2, SiO
2-Al
2O
3, Al
2O
3-TiO
2Or SiO
2-Al
2O
3-TiO
2, raw material of wood-charcoal material carrier is gac, carbon nanotube, coconut husk charcoal or above mixtures of material.
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103638987A (en) * | 2013-12-02 | 2014-03-19 | 煤炭科学研究总院 | Hydrogenation catalyst carrier for coal liquefaction oil, catalyst as well as preparation method and application of hydrogenation catalyst carrier |
| CN107032942A (en) * | 2017-05-22 | 2017-08-11 | 江苏科菲特生化技术股份有限公司 | A kind of method of rectifying organic solid residue conduction oil in utilization biphenyl alcohol production |
| CN109438154A (en) * | 2018-11-05 | 2019-03-08 | 大连理工大学 | A kind of method of industrial dibenzofuran hydrofinishing biphenyl under atmospheric hydrogen |
| CN110252325A (en) * | 2018-03-12 | 2019-09-20 | 中国科学院宁波材料技术与工程研究所 | Crude naphthalene selective hydrocatalyst and preparation method thereof |
| CN113943315A (en) * | 2021-09-26 | 2022-01-18 | 上海大学 | Indenyl-containing rare earth metal complex, preparation method and application thereof |
| CN114804997A (en) * | 2022-04-15 | 2022-07-29 | 中国神华煤制油化工有限公司 | Process for producing cyclohexylbenzene and corresponding metal catalyst |
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Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103638987A (en) * | 2013-12-02 | 2014-03-19 | 煤炭科学研究总院 | Hydrogenation catalyst carrier for coal liquefaction oil, catalyst as well as preparation method and application of hydrogenation catalyst carrier |
| CN103638987B (en) * | 2013-12-02 | 2016-08-17 | 煤炭科学技术研究院有限公司 | Liquefied coal coil catalyst carrier for hydrgenating, catalyst and preparation method and application |
| CN107032942A (en) * | 2017-05-22 | 2017-08-11 | 江苏科菲特生化技术股份有限公司 | A kind of method of rectifying organic solid residue conduction oil in utilization biphenyl alcohol production |
| CN110252325A (en) * | 2018-03-12 | 2019-09-20 | 中国科学院宁波材料技术与工程研究所 | Crude naphthalene selective hydrocatalyst and preparation method thereof |
| CN109438154A (en) * | 2018-11-05 | 2019-03-08 | 大连理工大学 | A kind of method of industrial dibenzofuran hydrofinishing biphenyl under atmospheric hydrogen |
| CN113943315A (en) * | 2021-09-26 | 2022-01-18 | 上海大学 | Indenyl-containing rare earth metal complex, preparation method and application thereof |
| CN114804997A (en) * | 2022-04-15 | 2022-07-29 | 中国神华煤制油化工有限公司 | Process for producing cyclohexylbenzene and corresponding metal catalyst |
| CN114804997B (en) * | 2022-04-15 | 2024-03-22 | 中国神华煤制油化工有限公司 | Preparation method of cyclohexylbenzene and corresponding metal catalyst |
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Application publication date: 20121003 |