CN103288577B - A kind of method preparing tetrahydrobenzene - Google Patents
A kind of method preparing tetrahydrobenzene Download PDFInfo
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- CN103288577B CN103288577B CN201210050828.9A CN201210050828A CN103288577B CN 103288577 B CN103288577 B CN 103288577B CN 201210050828 A CN201210050828 A CN 201210050828A CN 103288577 B CN103288577 B CN 103288577B
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- mononuclear aromatics
- sba
- tetrahydrobenzene
- water
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- HGCIXCUEYOPUTN-UHFFFAOYSA-N cyclohexene Chemical compound C1CCC=CC1 HGCIXCUEYOPUTN-UHFFFAOYSA-N 0.000 title claims abstract description 70
- 238000000034 method Methods 0.000 title claims abstract description 67
- 239000001257 hydrogen Substances 0.000 claims abstract description 42
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 42
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 39
- 239000000203 mixture Substances 0.000 claims abstract description 31
- 238000005984 hydrogenation reaction Methods 0.000 claims abstract description 24
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 claims abstract description 21
- 238000002156 mixing Methods 0.000 claims abstract description 13
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 claims description 140
- SVTBMSDMJJWYQN-UHFFFAOYSA-N 2-methylpentane-2,4-diol Chemical compound CC(O)CC(C)(C)O SVTBMSDMJJWYQN-UHFFFAOYSA-N 0.000 claims description 52
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 31
- 239000004480 active ingredient Substances 0.000 claims description 28
- WVDDGKGOMKODPV-UHFFFAOYSA-N Benzyl alcohol Chemical compound OCC1=CC=CC=C1 WVDDGKGOMKODPV-UHFFFAOYSA-N 0.000 claims description 26
- 229960004217 benzyl alcohol Drugs 0.000 claims description 26
- 235000019445 benzyl alcohol Nutrition 0.000 claims description 26
- 229940051250 hexylene glycol Drugs 0.000 claims description 26
- XLOMVQKBTHCTTD-UHFFFAOYSA-N Zinc monoxide Chemical compound [Zn]=O XLOMVQKBTHCTTD-UHFFFAOYSA-N 0.000 claims description 20
- 239000011148 porous material Substances 0.000 claims description 14
- 150000002431 hydrogen Chemical class 0.000 claims description 10
- 229910052763 palladium Inorganic materials 0.000 claims description 10
- 229910052703 rhodium Inorganic materials 0.000 claims description 10
- 229910052707 ruthenium Inorganic materials 0.000 claims description 10
- 239000011787 zinc oxide Substances 0.000 claims description 10
- NWONKYPBYAMBJT-UHFFFAOYSA-L zinc sulfate Chemical compound [Zn+2].[O-]S([O-])(=O)=O NWONKYPBYAMBJT-UHFFFAOYSA-L 0.000 claims description 10
- 229960001763 zinc sulfate Drugs 0.000 claims description 10
- 229910000368 zinc sulfate Inorganic materials 0.000 claims description 10
- 229910052742 iron Inorganic materials 0.000 claims description 7
- 229910052748 manganese Inorganic materials 0.000 claims description 7
- 229910052759 nickel Inorganic materials 0.000 claims description 7
- 229910052725 zinc Inorganic materials 0.000 claims description 7
- 239000011701 zinc Substances 0.000 claims description 7
- -1 cyclohexene compound Chemical class 0.000 claims description 3
- 125000000217 alkyl group Chemical group 0.000 claims description 2
- 125000004432 carbon atom Chemical group C* 0.000 claims description 2
- 125000001997 phenyl group Chemical group [H]C1=C([H])C([H])=C(*)C([H])=C1[H] 0.000 claims 1
- 230000009466 transformation Effects 0.000 abstract description 20
- 230000000694 effects Effects 0.000 abstract description 15
- 239000008346 aqueous phase Substances 0.000 abstract description 6
- 230000009286 beneficial effect Effects 0.000 abstract description 2
- 125000004435 hydrogen atom Chemical class [H]* 0.000 abstract 2
- 238000006243 chemical reaction Methods 0.000 description 38
- 238000003756 stirring Methods 0.000 description 19
- 239000012071 phase Substances 0.000 description 17
- 239000000523 sample Substances 0.000 description 17
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 16
- 238000005070 sampling Methods 0.000 description 13
- 239000003054 catalyst Substances 0.000 description 10
- 238000002360 preparation method Methods 0.000 description 10
- 239000013335 mesoporous material Substances 0.000 description 9
- 238000001035 drying Methods 0.000 description 8
- 229910052757 nitrogen Inorganic materials 0.000 description 8
- 230000008569 process Effects 0.000 description 8
- 150000003839 salts Chemical class 0.000 description 8
- RTZKZFJDLAIYFH-UHFFFAOYSA-N Diethyl ether Chemical compound CCOCC RTZKZFJDLAIYFH-UHFFFAOYSA-N 0.000 description 6
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 6
- 238000006073 displacement reaction Methods 0.000 description 6
- 229920001992 poloxamer 407 Polymers 0.000 description 6
- 239000000843 powder Substances 0.000 description 6
- 239000010948 rhodium Substances 0.000 description 6
- 239000007787 solid Substances 0.000 description 6
- 239000013589 supplement Substances 0.000 description 6
- 238000007725 thermal activation Methods 0.000 description 6
- 238000001354 calcination Methods 0.000 description 5
- 230000000052 comparative effect Effects 0.000 description 5
- 239000012266 salt solution Substances 0.000 description 5
- 238000001994 activation Methods 0.000 description 4
- 230000004913 activation Effects 0.000 description 4
- 238000007598 dipping method Methods 0.000 description 4
- 238000005470 impregnation Methods 0.000 description 4
- KBJMLQFLOWQJNF-UHFFFAOYSA-N nickel(ii) nitrate Chemical compound [Ni+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O KBJMLQFLOWQJNF-UHFFFAOYSA-N 0.000 description 4
- YBCAZPLXEGKKFM-UHFFFAOYSA-K ruthenium(iii) chloride Chemical compound [Cl-].[Cl-].[Cl-].[Ru+3] YBCAZPLXEGKKFM-UHFFFAOYSA-K 0.000 description 4
- 238000003786 synthesis reaction Methods 0.000 description 4
- JIAARYAFYJHUJI-UHFFFAOYSA-L zinc dichloride Chemical compound [Cl-].[Cl-].[Zn+2] JIAARYAFYJHUJI-UHFFFAOYSA-L 0.000 description 4
- XDTMQSROBMDMFD-UHFFFAOYSA-N Cyclohexane Chemical compound C1CCCCC1 XDTMQSROBMDMFD-UHFFFAOYSA-N 0.000 description 3
- 229910002651 NO3 Inorganic materials 0.000 description 3
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 description 3
- BOTDANWDWHJENH-UHFFFAOYSA-N Tetraethyl orthosilicate Chemical compound CCO[Si](OCC)(OCC)OCC BOTDANWDWHJENH-UHFFFAOYSA-N 0.000 description 3
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 3
- 239000013543 active substance Substances 0.000 description 3
- 239000007864 aqueous solution Substances 0.000 description 3
- 230000015572 biosynthetic process Effects 0.000 description 3
- 239000003153 chemical reaction reagent Substances 0.000 description 3
- 239000003795 chemical substances by application Substances 0.000 description 3
- 239000006184 cosolvent Substances 0.000 description 3
- 239000012153 distilled water Substances 0.000 description 3
- 238000001914 filtration Methods 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- VLKZOEOYAKHREP-UHFFFAOYSA-N n-Hexane Chemical compound CCCCCC VLKZOEOYAKHREP-UHFFFAOYSA-N 0.000 description 3
- 238000012545 processing Methods 0.000 description 3
- 238000011160 research Methods 0.000 description 3
- 229920000428 triblock copolymer Polymers 0.000 description 3
- 238000005406 washing Methods 0.000 description 3
- 206010013786 Dry skin Diseases 0.000 description 2
- CTQNGGLPUBDAKN-UHFFFAOYSA-N O-Xylene Chemical compound CC1=CC=CC=C1C CTQNGGLPUBDAKN-UHFFFAOYSA-N 0.000 description 2
- 230000000274 adsorptive effect Effects 0.000 description 2
- 238000004458 analytical method Methods 0.000 description 2
- 235000012791 bagels Nutrition 0.000 description 2
- 238000004364 calculation method Methods 0.000 description 2
- UFMZWBIQTDUYBN-UHFFFAOYSA-N cobalt dinitrate Chemical compound [Co+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O UFMZWBIQTDUYBN-UHFFFAOYSA-N 0.000 description 2
- 229910001981 cobalt nitrate Inorganic materials 0.000 description 2
- 239000013078 crystal Substances 0.000 description 2
- HPXRVTGHNJAIIH-UHFFFAOYSA-N cyclohexanol Chemical compound OC1CCCCC1 HPXRVTGHNJAIIH-UHFFFAOYSA-N 0.000 description 2
- 230000007547 defect Effects 0.000 description 2
- 238000004453 electron probe microanalysis Methods 0.000 description 2
- 239000007789 gas Substances 0.000 description 2
- NLYAJNPCOHFWQQ-UHFFFAOYSA-N kaolin Chemical compound O.O.O=[Al]O[Si](=O)O[Si](=O)O[Al]=O NLYAJNPCOHFWQQ-UHFFFAOYSA-N 0.000 description 2
- 229910052622 kaolinite Inorganic materials 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 239000002808 molecular sieve Substances 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- SONJTKJMTWTJCT-UHFFFAOYSA-K rhodium(iii) chloride Chemical compound [Cl-].[Cl-].[Cl-].[Rh+3] SONJTKJMTWTJCT-UHFFFAOYSA-K 0.000 description 2
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
- 239000011592 zinc chloride Substances 0.000 description 2
- 235000005074 zinc chloride Nutrition 0.000 description 2
- KJCVRFUGPWSIIH-UHFFFAOYSA-N 1-naphthol Chemical compound C1=CC=C2C(O)=CC=CC2=C1 KJCVRFUGPWSIIH-UHFFFAOYSA-N 0.000 description 1
- QTBSBXVTEAMEQO-UHFFFAOYSA-M Acetate Chemical compound CC([O-])=O QTBSBXVTEAMEQO-UHFFFAOYSA-M 0.000 description 1
- 229920002292 Nylon 6 Polymers 0.000 description 1
- 229920002302 Nylon 6,6 Polymers 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 1
- 229910021536 Zeolite Inorganic materials 0.000 description 1
- 230000001133 acceleration Effects 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 150000001408 amides Chemical class 0.000 description 1
- WERYXYBDKMZEQL-UHFFFAOYSA-N butane-1,4-diol Chemical compound OCCCCO WERYXYBDKMZEQL-UHFFFAOYSA-N 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 238000012790 confirmation Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 238000006704 dehydrohalogenation reaction Methods 0.000 description 1
- 238000000151 deposition Methods 0.000 description 1
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 description 1
- 238000010894 electron beam technology Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000011156 evaluation Methods 0.000 description 1
- 239000000835 fiber Substances 0.000 description 1
- 239000012847 fine chemical Substances 0.000 description 1
- 230000036571 hydration Effects 0.000 description 1
- 238000006703 hydration reaction Methods 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- KJPHTXTWFHVJIG-UHFFFAOYSA-N n-ethyl-2-[(6-methoxypyridin-3-yl)-(2-methylphenyl)sulfonylamino]-n-(pyridin-3-ylmethyl)acetamide Chemical compound C=1C=C(OC)N=CC=1N(S(=O)(=O)C=1C(=CC=CC=1)C)CC(=O)N(CC)CC1=CC=CN=C1 KJPHTXTWFHVJIG-UHFFFAOYSA-N 0.000 description 1
- 238000010606 normalization Methods 0.000 description 1
- 238000005554 pickling Methods 0.000 description 1
- 229920000728 polyester Polymers 0.000 description 1
- 230000001737 promoting effect Effects 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000007790 solid phase Substances 0.000 description 1
- 238000001308 synthesis method Methods 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- 239000010457 zeolite Substances 0.000 description 1
Abstract
The invention provides a kind of method preparing tetrahydrobenzene, the method comprises: under selec-tive hydrogenation condition and under the existence of the mixture of catalyzer and water, mononuclear aromatics is contacted with hydrogen, wherein, before mononuclear aromatics is contacted with hydrogen, first the mixture of described catalyzer and water is mixed 1-6 hour with mononuclear aromatics at 30-80 DEG C, and the mixture of described catalyzer and water carried out in the presence of an alcohol with mixing of mononuclear aromatics.Method provided by the invention can improve the effect of oil-aqueous phase mixing, and alcohol have the generation being beneficial to tetrahydrobenzene, thus improve the transformation efficiency of mononuclear aromatics and the selectivity of tetrahydrobenzene.
Description
Technical field
The present invention relates to a kind of method preparing tetrahydrobenzene.
Background technology
Tetrahydrobenzene not only can produce hexalin by direct hydration, and it is important organic synthesis intermediate, is widely used in the production of hexanodioic acid, nylon 6, nylon66 fiber, polymeric amide, polyester and other fine chemicals.Tetrahydrobenzene and derived product thereof, have important industrial use and wide market outlook, and thus mononuclear aromatics selec-tive hydrogenation cyclohexene has huge industrial economy value.
The method of traditional mode of production tetrahydrobenzene is generally divided into two classes.One class is the multi-step synthetic route of raw material with benzene.First make hexanaphthene or cyclohexane halide by benzene, then hexanaphthene is made hexalin and dewater again and form tetrahydrobenzene or cyclohexane halide dehydrohalogenation is formed tetrahydrobenzene.Another kind of is be the one-step synthesis method route of raw material with benzene, is namely that feedstock portions hydrogenation generates corresponding tetrahydrobenzene and hexanaphthene with benzene, and this synthetic route is paid close attention to widely due to technique simple and fast.
The reaction system that the ordinary method of mononuclear aromatics selec-tive hydrogenation production tetrahydrobenzene is used is a heterogeneous system, this system comprises the oil phase containing mononuclear aromatics, comprise the aqueous phase of water, comprise the solid phase of the beaded catalyst be suspended in aqueous phase and comprise the gas phase of the hydrogen being blown into reaction system, in the ordinary method using such reaction system, usually run into many difficult problems.As when oil-water mixes and/or gas-liquid mixing is insufficient, the activity of the catalyzer in reaction system can not give full play of, what therefore reaction yield became is quite low, and when gas-liquid mixing is too violent, not only during reaction the activity of catalyzer reduces rapidly, tetrahydrobenzene easily generates by-product cyclic hexane further in addition, reduces the selectivity of tetrahydrobenzene.
Summary of the invention
The object of the invention is the defect in order to overcome prior art, providing a kind of suitably can be conducive to improving the method that the transformation efficiency of mononuclear aromatics and tetrahydrobenzene optionally prepare tetrahydrobenzene by mixing oil-water mutually.
The invention provides a kind of method preparing tetrahydrobenzene, the method comprises: under selec-tive hydrogenation condition and under the existence of the mixture of catalyzer and water, mononuclear aromatics is contacted with hydrogen, wherein, before mononuclear aromatics is contacted with hydrogen, first the mixture of described catalyzer and water is mixed 1-6 hour with mononuclear aromatics at 30-80 DEG C, and the mixture of described catalyzer and water carried out in the presence of an alcohol with mixing of mononuclear aromatics.
In order to overcome the defect of prior art, the present inventor is through intensive research, found that by processing the mixture of catalyzer and water and mononuclear aromatics, aqueous phase containing catalyzer is mixed at 30-80 DEG C with oil phase mononuclear aromatics, and in the presence of an alcohol, improve the effect of oil-aqueous phase mixing, mononuclear aromatics is fully contacted with catalyzer, depositing in the case of hydrogen, be converted into tetrahydrobenzene rapidly, and alcohol have the generation being beneficial to tetrahydrobenzene, thus improve the transformation efficiency of mononuclear aromatics and the selectivity of tetrahydrobenzene.
Embodiment
Below the specific embodiment of the present invention is described in detail.Should be understood that, embodiment described herein, only for instruction and explanation of the present invention, is not limited to the present invention.
According to the present invention, the described method preparing tetrahydrobenzene comprises: under selec-tive hydrogenation condition and under the existence of the mixture of catalyzer and water, mononuclear aromatics is contacted with hydrogen, wherein, before mononuclear aromatics is contacted with hydrogen, first the mixture of described catalyzer and water is mixed 1-6 hour with mononuclear aromatics at 30-80 DEG C, and the mixture of described catalyzer and water carried out in the presence of an alcohol with mixing of mononuclear aromatics.
The above-mentioned improvement preparing the method for tetrahydrobenzene is mainly: by mixing at 30-80 DEG C with mononuclear aromatics the mixture of catalyzer and water, and in the presence of an alcohol, improve the effect of oil-aqueous phase mixing, thus improving the transformation efficiency of mononuclear aromatics and the selectivity of tetrahydrobenzene, other conditions therefore prepared in the method for tetrahydrobenzene can adopt the condition of well known to a person skilled in the art to carry out.
According to the method preparing tetrahydrobenzene of the present invention, wherein, the transformation efficiency of mononuclear aromatics and the higher object of tetrahydrobenzene selectivity can be realized according to the above-mentioned method preparing tetrahydrobenzene of the present invention, but in order to better realize object of the present invention, under preferable case, before mononuclear aromatics is contacted with hydrogen, first the mixture of described catalyzer and water is mixed 2-5 hour with mononuclear aromatics at 40-70 DEG C, and the mixture of described catalyzer and water carried out in the presence of an alcohol with mixing of mononuclear aromatics.
According to the method preparing tetrahydrobenzene of the present invention, wherein, the present invention to described catalyzer without particular requirement, can select with reference to prior art, but in order to better realize object of the present invention, under a kind of preferable case, described catalyzer contains carrier and load active ingredient on the carrier, wherein, described carrier is donut-like SBA-15, described active ingredient contain be selected from Ru, Rh and Pd one or more.The present invention is by using donut-like SBA-15 as the carrier of catalyzer, catalyzer of the present invention is made to have higher activity and selectivity, supposition is because the special microlitic structure of donut-like SBA-15 makes it to be better combined with active ingredient, and active ingredient can disperse more even, which thereby enhance the activity and selectivity of catalyzer.Catalyst application of the present invention can being reduced when mononuclear aromatics selec-tive hydrogenation prepares tetrahydrobenzene the consumption of metal-salt even without the need to adding metal-salt, just can improve the selectivity of tetrahydrobenzene, in addition, the corrosion of metal-salt to equipment can also be reduced further.
According to the method preparing tetrahydrobenzene of the present invention, in order to improve the activity and selectivity of described catalyzer of the present invention further, the internal diameter of described donut-like SBA-15 and the ratio of external diameter are preferably 0.3-0.9, are more preferably 0.5-0.85; Mean thickness is preferably 0.1-2 micron, is more preferably 1-2 micron.The various donut-like that donut-like described in the present invention can it has been generally acknowledged that for this area, such as, can for there is opening or not there is the various circular of opening or class is circular, described internal diameter and external diameter refer to the radius of the circle at the inner circumferential place of described bagel and the radius of place, periphery circle respectively.Described mean thickness refers to the mean value of the thickness of multiple donut-like SBA-15, and the thickness of each donut-like SBA-15 refers to the mean thickness of each position of this donut-like SBA-15.The most probable pore size of described SBA-15 can be 7-10 nanometer, is preferably 8-9 nanometer; Pore volume can be 0.5-3 ml/g, is preferably 1-2 ml/g; BET specific surface area can be 600-1000 meters squared per gram, is preferably 650-800 meters squared per gram; Average particulate diameter is preferably 3-20 micron, is more preferably 3-10 micron.
The SBA-15 carrier of donut-like of the present invention can be obtained by various mode, such as, can be commercially available, and also can prepare according to various method of the prior art.
Under another kind of preferable case, described catalyzer contains carrier and load active ingredient on the carrier, and wherein, described carrier is bar-shaped SBA-15, described active ingredient contain be selected from Ru, Rh and Pd one or more.The present invention, by using bar-shaped SBA-15 as the carrier of catalyzer, makes catalyzer of the present invention have higher activity and selectivity.Supposition is: because described bar-shaped SBA-15 carrier is a kind of mesopore molecular sieve, on the one hand, bar-shaped SBA-15 has larger specific surface area and relatively large aperture, and its special microlitic structure makes it to be better combined with active ingredient, and active ingredient can disperse more even, on the other hand, the mesopore orbit of bar-shaped SBA-15 carrier has carrier and reactor dual-use function, therefore, it is possible to improve the activity and selectivity of catalyzer further.
In the present invention, as long as ensure that described carrier is that bar-shaped SBA-15 can realize object of the present invention, the hole dimension as the bar-shaped SBA-15 of described carrier can be the known hole dimension of technician in Zeolite synthesis field.For the present invention, in order to improve the activity and selectivity of described catalyzer of the present invention further, the present inventor finds in research process, be 6-10 nanometer at the most probable pore size of bar-shaped SBA-15 carrier, pore volume is 0.5-1.5 ml/g, when BET specific surface area is 600-700 meters squared per gram, described catalyzer can be made to have higher catalytic activity.More preferably, the most probable pore size of bar-shaped SBA-15 is 6-6.5 nanometer, and pore volume is 0.8-1.2 ml/g, and BET specific surface area is 600-660 meters squared per gram.Further, the length of the rod of described bar-shaped SBA-15 carrier can be selected and change in wider scope, such as, can be 30-100 micron usually.
The bar-shaped SBA-15 meeting above-mentioned condition can be commercially available.Such as: be purchased the bar-shaped SBA-15 from high-tech limited-liability company of Changchun Jilin University.
In the present invention, under preferable case, the carrier in described catalyzer is donut-like SBA-15 or bar-shaped SBA-15, to improve the activity and selectivity of catalyzer further, therefore, the present invention is to the kind of described active ingredient and consumption without particular requirement, and its range of choices is wider.For the present invention, under preferable case, described active ingredient contain be selected from Ru, Rh and Pd one or more.More preferably in situation, in order to improve the activity of described catalyzer further, described active ingredient also containing be selected from Zn, Fe, Co, Ni and Mn one or more, and the gross weight of Ru, Rh and Pd is 0.01-100: 1 with the gross weight ratio of Zn, Fe, Co, Ni and Mn, more preferably 0.05-50: 1, be especially preferably 0.5-30: 1.
In catalyzer of the present invention, source as Ru, Rh and Pd of described main active component is respective soluble salt, the range of choices of the kind of soluble salt is wider, conventional soluble salt all can be used for the present invention, such as, can be its respective muriate, nitrate etc., be preferably muriate.In addition, the soluble salt of other active ingredients preferably contained, such as, one or more in Zn, Fe, Co, Ni and Mn, the range of choices of the kind of their soluble salt is wider, conventional soluble salt all can be used for the present invention, such as, can be one or more in halogenide, acetate, sulfate and nitrate, is preferably nitrate.
The range of choices of the active ingredient in catalyzer provided by the invention and the content of carrier is wider, and can select with reference to prior art, for the present invention, under preferable case, in described catalyzer, active ingredient is with the content of oxide basis for 0.1-50 % by weight, and the content of carrier is 50-99.9 % by weight; More preferably, in situation, in described catalyzer, active ingredient is with the content of oxide basis for 1-20 % by weight, and the content of carrier is 80-99 % by weight.
Catalyzer of the present invention can be prepared with reference to the various methods of prior art, such as, can adopt conventional pickling process preparation, such as, and incipient wetness.Described incipient wetness such as can be carried out as follows: by the soluble salt solutions of active ingredient and donut-like SBA-15 carrier or bar-shaped SBA-15 carrier contact, and the carrier after contact is carried out drying, roasting.Wherein, when active ingredient is multiple element, the method for the soluble salt solutions of active ingredient and donut-like SBA-15 carrier or bar-shaped SBA-15 carrier contact can be undertaken by the following two kinds method: (1) soluble salt of various active component can be made after a kind of mixing solutions again with carrier contact; (2) also the soluble salt of different active ingredients can be made into the aqueous solution separately, then carrier be contacted with the soluble salt solutions of various active ingredient (order contacted with the soluble salt solutions of various active ingredient can be selected arbitrarily) successively.The solution of described soluble salt solutions can be selected according to prior art.
The drying of catalyzer of the present invention prepared according to aforesaid method and the condition of roasting can be carried out with reference to prior art, and the temperature of such as described drying is generally 100-200 DEG C, and the time is 0.5-10 hour.And the present inventor finds unexpectedly in research process, the activity and selectivity of catalyzer of the present invention can be improved further by the temperature reasonably controlling roasting.Therefore, the temperature for the preferred described roasting of the present invention is 300-500 DEG C, and be more preferably 350-450 DEG C, the time is 0.5-12 hour, is more preferably 1-8 hour.
The activation of catalyzer of the present invention can be carried out with reference to prior art, and the temperature that the condition of described activation comprises activation is 80-500 DEG C, is preferably 100-450 DEG C.
According to the method preparing tetrahydrobenzene of the present invention, wherein, the existence of water makes catalyst surface occur unexpectedly to adsorb, the mononuclear aromatics that adsorptive power is stronger can be adsorbed onto catalyzer and be hydrogenated, the more weak tetrahydrobenzene of adsorptive power then can not close to catalyzer because catalyst surface is awash, water obtains the effect promoting that tetrahydrobenzene adsorbs from catalyst surface desorb and preventing again, water-content can be selected in wider scope, under preferable case, in order to avoid the burden of product separation, the volume ratio of water and mononuclear aromatics is 1-3: 1, is preferably 1.5-2.5: 1.
The method of preparing tetrahydrobenzene above-mentioned according to the present invention can realize the transformation efficiency of mononuclear aromatics and the higher object of tetrahydrobenzene selectivity, but in order to better realize object of the present invention, under preferable case, the contact of described mononuclear aromatics and hydrogen is carried out in the presence of an alcohol, described alcohol have the generation helping tetrahydrobenzene, described alcohol is one or more in hexylene glycol, phenylcarbinol, Alpha-Naphthyl alcohol and 1,4-butyleneglycol.The add-on of the present invention to described alcohol does not specially require, and can select in wider scope, and under preferable case, the volume ratio of described alcohol and mononuclear aromatics is 0.001-0.5: 1, is more preferably 0.05-0.3: 1.More preferably described alcohol is the mixture of hexylene glycol and phenylcarbinol, the volume ratio of hexylene glycol and phenylcarbinol can be selected in relative broad range, in order to better realize object of the present invention, under preferable case, the volume ratio of hexylene glycol and phenylcarbinol is 0.1-1.5: 1, is more preferably 0.5-1: 1.The feed postition of described alcohol can be that once to add also can be add in batches, and the present invention does not have particular requirement.
The method of preparing tetrahydrobenzene above-mentioned according to the present invention can realize the transformation efficiency of mononuclear aromatics and the higher object of tetrahydrobenzene selectivity, but in order to better realize object of the present invention, under preferable case, the contact of described mononuclear aromatics and hydrogen is carried out under the existence of zn cpds, and the existence of described zn cpds can improve selectivity of catalyst, stability etc.Described zn cpds is zinc oxide and zinc sulfate, the mol ratio of zinc oxide and zinc sulfate can be selected in relative broad range, but in order to realize object of the present invention further, under preferable case, the mol ratio of zinc oxide and zinc sulfate is 1-3: 1, more preferably 1.5-2.5: 1; In addition, the mass ratio of described zn cpds and catalyzer also can be selected in relative broad range, but in order to better realize object of the present invention, under preferable case, the mass ratio of described zn cpds and catalyzer is 1-10: 1, is more preferably 3-7: 1.The feed postition of described zn cpds can be that once to add also can be add in batches, and the present invention does not have particular requirement.
According to the method preparing tetrahydrobenzene of the present invention, wherein, described selec-tive hydrogenation condition comprises: temperature is 110-180 DEG C, is preferably 120-160 DEG C; Pressure is 2-7MPa, is preferably 3.5-6MPa.Relative to 100 milliliters of mononuclear aromatics, the consumption of described catalyzer is 6-15 gram, preferred 7-12 gram.
Mononuclear aromatics used in the present invention is the mononuclear aromatics that usually can be replaced by the low alkyl group of carbonatoms below 4.As, benzene or toluene, dimethylbenzene etc.
Reaction pressure of the present invention to refer in reaction vessel the pressure of the vapour phase of part topmost, refers at the reaction temperatures, the saturation vapor pressure of each component in liquid phase and the summation of hydrogen partial pressure entering into reactor.
More than describe the preferred embodiment of the present invention in detail; but the present invention is not limited to the detail in above-mentioned embodiment, within the scope of technical conceive of the present invention; can carry out multiple simple variant to technical scheme of the present invention, these simple variant all belong to protection scope of the present invention.
It should be noted that in addition, each concrete technical characteristic described in above-mentioned embodiment, in reconcilable situation, can be combined by any suitable mode, in order to avoid unnecessary repetition, the present invention illustrates no longer separately to various possible array mode.
In addition, also can carry out arbitrary combination between various different embodiment of the present invention, as long as it is without prejudice to thought of the present invention, it should be considered as content disclosed in this invention equally.
Below in conjunction with embodiment, the present invention is described in detail, but the present invention is not limited thereto.
In the present invention, gas chromatograph is adopted (to be purchased from Shanghai Precision Scientific Apparatus Co., Ltd, model is GC128) carry out each analysis formed in system, undertaken quantitatively by correcting normalization method, all can refer to prior art to carry out, calculate the evaluation index such as the transformation efficiency of benzene and the selectivity of tetrahydrobenzene on this basis.
In following examples, the transformation efficiency of mononuclear aromatics and the selectivity of tetrahydrobenzene calculate according to following formula:
The calculation formula of the transformation efficiency of mononuclear aromatics is as follows:
The optionally calculation formula of tetrahydrobenzene is as follows:
Wherein, X is transformation efficiency; S is selectivity.
The preparation method of the catalyzer adopted in following embodiment is as follows:
(1) preparation method of donut-like SBA-15 carrier
Donut-like SBA-15 carrier is according to Sun Jinyu; Zhao Dongyuan; the synthesis of " bagel " shape high-sequential big-pore mesoporous molecular sieve SBA-15; SCI; 2000; preparation method's preparation of 1 (21): 21 ~ 23, and the parameters of donut-like SBA-15 carrier, comprise the ratio of internal diameter and external diameter, mean thickness, most probable pore size, pore volume, BET specific surface area and average particulate diameter and also record according to testing method disclosed in the document.Concrete preparation method is as follows:
With DMF (DMF) as cosolvent, by 2.0 grams of Pluronic F-127 ethers-polycyclic oxypropylene ether-Pluronic F-127 ether triblock copolymer tensio-active agent (Aldrich, average molecular mass Mn=5800, molecular formula EO
20pO
70eO
20) be dissolved in 45 grams of distilled water and 30 grams of (4mol/L) hydrochloric acid, at 40 DEG C, add 15 grams of DMF.Stir after 1 hour and add 4.45 grams of tetraethoxys (TEOS, Shenyang chemical reagent work), in 40 DEG C of stirring reactions 24 hours.Former powder mesoporous material is obtained after filtration, washing, drying.By former for gained powder mesoporous material in retort furnace 600 DEG C calcining 24 hours, remove template agent, obtain donut-like mesoporous material SBA-15 sample 1.
With DMF (DMF) as cosolvent, by 2.0 grams of Pluronic F-127 ethers-polycyclic oxypropylene ether-Pluronic F-127 ether triblock copolymer tensio-active agent (Aldrich, average molecular mass Mn=5800, molecular formula EO
20pO
70eO
20) be dissolved in 50 grams of distilled water and 30 grams of (4mol/L) hydrochloric acid, at 30 DEG C, add 20 grams of DMF.Stir after 1 hour and add 5.5 grams of tetraethoxys (TEOS, Shenyang chemical reagent work), in 50 DEG C of stirring reactions 24 hours.Former powder mesoporous material is obtained after filtration, washing, drying.By former for gained powder mesoporous material in retort furnace 400 DEG C calcining 24 hours, remove template agent, obtain donut-like mesoporous material SBA-15 sample 2.
With DMF (DMF) as cosolvent, by 2.0 grams of Pluronic F-127 ethers-polycyclic oxypropylene ether-Pluronic F-127 ether triblock copolymer tensio-active agent (Aldrich, average molecular mass Mn=5800, molecular formula EO
20pO
70eO
20) be dissolved in 45 grams of distilled water and 30 grams of (4mol/L) hydrochloric acid, at 50 DEG C, add 15 grams of DMF.Stir after 1 hour and add 4.5 grams of tetraethoxys (TEOS, Shenyang chemical reagent work), in 60 DEG C of stirring reactions 24 hours.Former powder mesoporous material is obtained after filtration, washing, drying.By former for gained powder mesoporous material in retort furnace 700 DEG C calcining 24 hours, remove template agent, obtain donut-like mesoporous material SBA-15 sample 3.
The pore structure parameter of donut-like SBA-15 sample 1-3 is as shown in table 1.
Table 1
(2) bar-shaped SBA-15 carrier
In the preparation of following catalyzer, described bar-shaped SBA-15 carrier is purchased from high-tech limited-liability company of Changchun Jilin University, and specific nature is in table 2.
Table 2
(3) preparation of catalyzer
By whole donut-like SBA-15 sample 1-3 difference 400 DEG C of calcinings 10 hours (thermal activation) under nitrogen protection of synthesis, obtain the donut-like SBA-15 sample 1-3 after thermal activation.Adopt the donut-like SBA-15 sample 1-3 after thermal activation, according to incipient wetness Kaolinite Preparation of Catalyst C1-C3.By the aqueous impregnation of donut-like SBA-15 sample 1 with ruthenium chloride, by the mixed aqueous solution of donut-like SBA-15 sample 2 ruthenium chloride, zinc chloride and nickelous nitrate dipping and aqueous impregnation donut-like SBA-15 sample 3 being used rhodium chloride and Jing Ti/Bao Pian COBALT NITRATE CRYSTALS/FLAKES, obtain three kinds of solids.The three kinds of solids obtained after dipping are left standstill 4 hours, 120 DEG C of dryings 6 hours under room temperature (25 DEG C).Finally, calcine 2 hours in the air of dried solid at 450 DEG C, obtain catalyzer C1, C2 and C3.
Available bar-shaped SBA-15 sample 1-3 difference 400 DEG C of calcinings 10 hours (thermal activation) under nitrogen protection will be purchased, obtain the bar-shaped SBA-15 sample 1-3 after thermal activation.Adopt the bar-shaped SBA-15 sample 1-3 after thermal activation, according to incipient wetness Kaolinite Preparation of Catalyst B1-B3.By the aqueous impregnation of bar-shaped SBA-15 sample 1 with ruthenium chloride, by the mixed aqueous solution of bar-shaped SBA-15 sample 2 ruthenium chloride, zinc chloride and nickelous nitrate dipping and the aqueous impregnation bar-shaped SBA-15 sample 3 being used rhodium chloride and Jing Ti/Bao Pian COBALT NITRATE CRYSTALS/FLAKES, obtain three kinds of solids.The three kinds of solids obtained after dipping are left standstill 4 hours, 120 DEG C of dryings 6 hours under room temperature (25 DEG C).Finally, calcine 2 hours in the air of dried solid at 450 DEG C, obtain catalyst B 1, B2 and B3.
Measured respectively with the total content of the active ingredient of oxide basis (comprising the weight ratio between various active component) in C1-C3 and B1-B3 catalyzer by ultimate analysis ICP, and the content of described carrier.
The composition of catalyzer C1-C3 and B1-B3 is listed in table 3.
Table 3
Respectively catalyzer C1-C3 and B1-B3 is reduced 3 hours, in the hydrogen gas stream with deactivated catalyst at 200 DEG C.Gained catalyzer C1-C3 and B1-B3 EPMA (X-ray microanalyzer) analyzes, and confirmation active ingredient Ru, Rh, Pd are dispersed on carrier.Analyze for EMPA, as metering facility, the acceleration voltage of electron beam gun is set to 20KV to use JXA-8600M (Nippon Denshi K.K.), and probe current is 2.0 × 10
-8a.
Catalyzer C1-C3 and B1-B3 after activation is adopted below in embodiment.
Embodiment 1
First use nitrogen clean for the air displacement in still, the mixture of 7 grams of C1 catalyzer and 200ml water, 100ml benzene and 20ml hexylene glycol and phenylcarbinol (volume ratio of hexylene glycol and phenylcarbinol is 0.5: 1) are added in the SUS-316 autoclave of 0.5L, 40 DEG C of stirrings (1000 revs/min) 3.5 hours, and then pass into hydrogen.Temperature in the kettle is increased to 160 DEG C, in still, hydrogen pressure is increased to 3.5MPa, and under stirring (1000 revs/min), period supplements pressurized hydrogen simultaneously, implements the reaction that benzene selective hydrogenation prepares tetrahydrobenzene.In exit sampling after reaction for some time, use chromatographic oil phase, result is as shown in table 4.
Embodiment 2
First use nitrogen clean for the air displacement in still, the mixture of 10 grams of C2 catalyzer and 250ml water, 100ml benzene and 5ml hexylene glycol and phenylcarbinol (volume ratio of hexylene glycol and phenylcarbinol is 1: 1) are added in the SUS-316 autoclave of 0.5L, 55 DEG C of stirrings (1000 revs/min) 5 hours, and then pass into hydrogen.Temperature in the kettle is increased to 140 DEG C, in still, hydrogen pressure is increased to 4.5MPa, and under stirring (1000 revs/min), period supplements pressurized hydrogen simultaneously, implements the reaction that benzene selective hydrogenation prepares tetrahydrobenzene.In exit sampling after reaction for some time, use chromatographic oil phase, result is as shown in table 4.
Embodiment 3
First use nitrogen clean for the air displacement in still, the mixture of 12 grams of C3 catalyzer and 150ml water, 100ml benzene and 30ml hexylene glycol and phenylcarbinol (volume ratio of hexylene glycol and phenylcarbinol is 0.8: 1) are added in the SUS-316 autoclave of 0.5L, 70 DEG C of stirrings (1000 revs/min) 2 hours, and then pass into hydrogen.Temperature in the kettle is increased to 120 DEG C, in still, hydrogen pressure is increased to 6MPa, and under stirring (1000 revs/min), period supplements pressurized hydrogen simultaneously, implements the reaction that benzene selective hydrogenation prepares tetrahydrobenzene.In exit sampling after reaction for some time, use chromatographic oil phase, result is as shown in table 4.
Embodiment 4
The reaction adopting the method for embodiment 1 to carry out benzene selective hydrogenation to prepare tetrahydrobenzene, unlike, before being contacted with hydrogen by benzene, first the mixture of 7 grams of C1 catalyzer and 200ml water, 100ml benzene and 20ml hexylene glycol and phenylcarbinol (volume ratio of hexylene glycol and phenylcarbinol is 0.5: 1) are stirred (1000 revs/min) 6 hours at 35 DEG C.In exit sampling after reaction for some time, use chromatographic oil phase, result is as shown in table 4.
Embodiment 5
The reaction adopting the method for embodiment 1 to carry out benzene selective hydrogenation to prepare tetrahydrobenzene, unlike, passing in hydrogen process, adding 21 grams of zinc oxide and zinc sulfate (mol ratio of zinc oxide and zinc sulfate is 2.5: 1).In exit sampling after reaction for some time, use chromatographic oil phase, result is as shown in table 4.
Embodiment 6
First use nitrogen clean for the air displacement in still, the mixture of 7 grams of B1 catalyzer and 200ml water, 100ml benzene and 20ml hexylene glycol and phenylcarbinol (volume ratio of hexylene glycol and phenylcarbinol is 0.5: 1) are added in the SUS-316 autoclave of 0.5L, 40 DEG C of stirrings (1000 revs/min) 3.5 hours, and then pass into hydrogen.Temperature in the kettle is increased to 160 DEG C, in still, hydrogen pressure is increased to 3.5MPa, and under stirring (1000 revs/min), period supplements pressurized hydrogen simultaneously, implements the reaction that benzene selective hydrogenation prepares tetrahydrobenzene.In exit sampling after reaction for some time, use chromatographic oil phase, result is as shown in table 4.
Embodiment 7
First use nitrogen clean for the air displacement in still, the mixture of 10 grams of B2 catalyzer and 250ml water, 100ml benzene and 5ml hexylene glycol and phenylcarbinol (volume ratio of hexylene glycol and phenylcarbinol is 1: 1) are added in the SUS-316 autoclave of 0.5L, 55 DEG C of stirrings (1000 revs/min) 5 hours, and then pass into hydrogen.Temperature in the kettle is increased to 140 DEG C, in still, hydrogen pressure is increased to 4.5MPa, and under stirring (1000 revs/min), period supplements pressurized hydrogen simultaneously, implements the reaction that benzene selective hydrogenation prepares tetrahydrobenzene.In exit sampling after reaction for some time, use chromatographic oil phase, result is as shown in table 4.
Embodiment 8
First use nitrogen clean for the air displacement in still, the mixture of 12 grams of B3 catalyzer and 150ml water, 100ml benzene and 30ml hexylene glycol and phenylcarbinol (volume ratio of hexylene glycol and phenylcarbinol is 0.8: 1) are added in the SUS-316 autoclave of 0.5L, 70 DEG C of stirrings (1000 revs/min) 2 hours, and then pass into hydrogen.Temperature in the kettle is increased to 120 DEG C, in still, hydrogen pressure is increased to 6MPa, and under stirring (1000 revs/min), period supplements pressurized hydrogen simultaneously, implements the reaction that benzene selective hydrogenation prepares tetrahydrobenzene.In exit sampling after reaction for some time, use chromatographic oil phase, result is as shown in table 4.
Embodiment 9
The reaction adopting the method for embodiment 6 to carry out benzene selective hydrogenation to prepare tetrahydrobenzene, unlike, before being contacted with hydrogen by benzene, first the mixture of 7 grams of B1 catalyzer and 200ml water, 100ml benzene and 20ml hexylene glycol and phenylcarbinol (volume ratio of hexylene glycol and phenylcarbinol is 0.5: 1) are stirred (1000 revs/min) 6 hours at 35 DEG C.In exit sampling after reaction for some time, use chromatographic oil phase, result is as shown in table 4.
Embodiment 10
The reaction adopting the method for embodiment 6 to carry out benzene selective hydrogenation to prepare tetrahydrobenzene, unlike, passing in hydrogen process, adding 21 grams of zinc oxide and zinc sulfate (mol ratio of zinc oxide and zinc sulfate is 2.5: 1) together.In exit sampling after reaction for some time, use chromatographic oil phase, result is as shown in table 4.
Embodiment 11
The reaction adopting the method for embodiment 1 to carry out benzene selective hydrogenation to prepare tetrahydrobenzene, unlike, adopt the catalyzer prepared according to CN1131653A (embodiment 1).In exit sampling after reaction for some time, use chromatographic oil phase, result is as shown in table 4.
Comparative example 1
The reaction adopting the method for embodiment 1 to carry out benzene selective hydrogenation to prepare tetrahydrobenzene, unlike, before being contacted with hydrogen by benzene, the catalyzer prepared 7 grams according to CN1131653A (embodiment 1) and the mixture of 200ml water, 100ml benzene and 20ml hexylene glycol and phenylcarbinol (volume ratio of hexylene glycol and phenylcarbinol is 0.5: 1) stir (1000 revs/min) 7 hours at 85 DEG C.In exit sampling after reaction for some time, use chromatographic oil phase, result is as shown in table 4.
Comparative example 2
The reaction adopting the method for embodiment 1 to carry out benzene selective hydrogenation to prepare tetrahydrobenzene, unlike, adopt the catalyzer prepared according to CN1131653A (embodiment 1), and do not add hexylene glycol and phenylcarbinol.In exit sampling after reaction for some time, use chromatographic oil phase, result is as shown in table 4.
Table 4
The method preparing tetrahydrobenzene provided by the invention, wherein, adopt donut-like SBA-15 as the obtained catalyzer of carrier, by processing the mixture of catalyzer and water and benzene, can find out according to embodiment 1-4, the transformation efficiency of higher benzene and the selectivity of tetrahydrobenzene can be obtained; According to embodiment 5, in the contact process of benzene and hydrogen, the existence of zn cpds can improve the transformation efficiency of benzene and the selectivity of tetrahydrobenzene further.In addition, adopt bar-shaped SBA-15 as the obtained catalyzer of carrier, by processing the mixture of catalyzer and water and benzene, can find out according to embodiment 6-9, the transformation efficiency of higher benzene and the selectivity of tetrahydrobenzene can be obtained; According to embodiment 10, in the contact process of benzene and hydrogen, the existence of zn cpds also can improve the transformation efficiency of benzene and the selectivity of tetrahydrobenzene further.And, according to embodiment 11, adopt the catalyzer of prior art still to have transformation efficiency and the tetrahydrobenzene selectivity of higher benzene according to method of the present invention.In addition, can find out with comparing of comparative example 1 according to embodiment 11, under comparative example 1 adopts the condition of the catalyzer of prior art outside technical scheme scope provided by the invention, the transformation efficiency of the benzene obtained and tetrahydrobenzene selectivity are lower than the transformation efficiency of benzene of the present invention and tetrahydrobenzene selectivity.In addition, according to relatively can finding out of embodiment 11 and comparative example 2, in the contact process of benzene and hydrogen, do not add the transformation efficiency of benzene during alcohol and tetrahydrobenzene selectivity and be starkly lower than the present invention and with the addition of alcohol and the transformation efficiency of the benzene obtained and tetrahydrobenzene selectivity.
Claims (20)
1. prepare a method for cyclohexene compound, the method comprises: under selec-tive hydrogenation condition and under the existence of the mixture of catalyzer and water, contacted by mononuclear aromatics, it is characterized in that with hydrogen:
Before mononuclear aromatics is contacted with hydrogen, first the mixture of described catalyzer and water is mixed 1-6 hour with mononuclear aromatics at 30-80 DEG C, and the mixture of described catalyzer and water carried out in the presence of an alcohol with mixing of mononuclear aromatics, described alcohol is the mixture of hexylene glycol and phenylcarbinol, and the volume ratio of hexylene glycol and phenylcarbinol is 0.1-1.5:1;
Wherein, the described mononuclear aromatics benzene that is benzene or replaced by the low alkyl group of carbonatoms below 4;
Described catalyzer contains carrier and load active ingredient on the carrier, and described carrier is donut-like SBA-15 or bar-shaped SBA-15, described active ingredient contain be selected from Ru, Rh and Pd one or more.
2. method according to claim 1, wherein, before being contacted with hydrogen by mononuclear aromatics, first mixes 2-5 hour with mononuclear aromatics by the mixture of described catalyzer and water at 40-70 DEG C.
3. method according to claim 1, wherein, the internal diameter of described donut-like SBA-15 and the ratio of external diameter are 0.3-0.9, and mean thickness is 0.1-2 micron.
4. method according to claim 3, wherein, the most probable pore size of described donut-like SBA-15 is 7-10 nanometer, and pore volume is 0.5-3 ml/g, and BET specific surface area is 600-1000 meters squared per gram, and average particulate diameter is 3-20 micron.
5. method according to claim 4, wherein, the length of the rod of described bar-shaped SBA-15 is 30-100 micron.
6. method according to claim 5, wherein, the most probable pore size of described bar-shaped SBA-15 is 6-10 nanometer, and pore volume is 0.5-1.5 ml/g, and BET specific surface area is 600-700 meters squared per gram.
7. method according to claim 1, wherein, described active ingredient is also containing one or more in Zn, Fe, Co, Ni and Mn, and the gross weight of Ru, Rh and Pd is 0.01-100:1 with the gross weight ratio of Zn, Fe, Co, Ni and Mn.
8. method according to claim 7, wherein, the gross weight of Ru, Rh and Pd and the gross weight of Zn, Fe, Co, Ni and Mn are than being 0.05-50:1.
9. method according to claim 8, wherein, the gross weight of Ru, Rh and Pd and the gross weight of Zn, Fe, Co, Ni and Mn are than being 0.5-30:1.
10. method according to claim 1, wherein, in described catalyzer, active ingredient is with the content of oxide basis for 0.1-50 % by weight, and the content of carrier is 50-99.9 % by weight.
11. methods according to claim 10, wherein, in described catalyzer, active ingredient is with the content of oxide basis for 1-20 % by weight, and the content of carrier is 80-99 % by weight.
12. methods according to claim 1 and 2, wherein, the volume ratio of described water and mononuclear aromatics is 1-3:1.
13. methods according to claim 12, wherein, the volume ratio of described water and mononuclear aromatics is 1.5-2.5:1.
14. methods according to claim 1, wherein, the volume ratio of hexylene glycol and phenylcarbinol is 0.5-1:1.
15. methods according to claim 14, wherein, the volume ratio of described alcohol and mononuclear aromatics is 0.001-0.5:1.
16. methods according to claim 15, wherein, the volume ratio of described alcohol and mononuclear aromatics is 0.05-0.3:1.
17. methods according to claim 1, wherein, the contact of described mononuclear aromatics and hydrogen is carried out under the existence of zn cpds, and described zn cpds is zinc oxide and zinc sulfate, and the mol ratio of zinc oxide and zinc sulfate is 1-3:1; The mass ratio of described zn cpds and catalyzer is 1-10:1.
18. methods according to claim 17, wherein, the mol ratio of zinc oxide and zinc sulfate is 1.5-2.5:1; The mass ratio of described zn cpds and catalyzer is 3-7:1.
19. methods according to claim 1, wherein, described selec-tive hydrogenation condition comprises: temperature is 110-180 DEG C, and pressure is 2-7MPa, and relative to 100 milliliters of mononuclear aromatics, the consumption of described catalyzer is 6-15 gram.
20. methods according to claim 19, wherein, described selec-tive hydrogenation condition comprises: temperature is 120-160 DEG C, pressure 3.5-6MPa, and relative to 100 milliliters of mononuclear aromatics, the consumption of described catalyzer is 7-12 gram.
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| US5639927A (en) * | 1994-12-19 | 1997-06-17 | Mitsubishi Chemical Corporation | Process of producing cycloolefin |
| CN1337386A (en) * | 2001-06-15 | 2002-02-27 | 郑州大学 | Catalyst for selective hydrogenation of benzene to produce cyclohexane and its prepn |
| CN101219391A (en) * | 2008-01-31 | 2008-07-16 | 复旦大学 | Process for producing ruthenium base catalyst for producing cyclohexene with benzene selective hydrogenation |
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| JPS6150930A (en) * | 1984-08-16 | 1986-03-13 | Asahi Chem Ind Co Ltd | Production of cycloolefin |
| JPH10139692A (en) * | 1996-11-13 | 1998-05-26 | Mitsubishi Chem Corp | Production of cycloolefin |
| JPH10259144A (en) * | 1997-03-17 | 1998-09-29 | Mitsubishi Chem Corp | Production of cyclohexene |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| US5639927A (en) * | 1994-12-19 | 1997-06-17 | Mitsubishi Chemical Corporation | Process of producing cycloolefin |
| CN1337386A (en) * | 2001-06-15 | 2002-02-27 | 郑州大学 | Catalyst for selective hydrogenation of benzene to produce cyclohexane and its prepn |
| CN101219391A (en) * | 2008-01-31 | 2008-07-16 | 复旦大学 | Process for producing ruthenium base catalyst for producing cyclohexene with benzene selective hydrogenation |
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