CN101148388A - Process for producing adamantane compound - Google Patents
Process for producing adamantane compound Download PDFInfo
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- CN101148388A CN101148388A CNA2007101612043A CN200710161204A CN101148388A CN 101148388 A CN101148388 A CN 101148388A CN A2007101612043 A CNA2007101612043 A CN A2007101612043A CN 200710161204 A CN200710161204 A CN 200710161204A CN 101148388 A CN101148388 A CN 101148388A
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- Prior art keywords
- adamantane compound
- diamantane
- adamantane
- compound
- quality
- Prior art date
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- -1 adamantane compound Chemical class 0.000 title claims abstract description 139
- 238000000034 method Methods 0.000 title claims abstract description 63
- ORILYTVJVMAKLC-UHFFFAOYSA-N Adamantane Natural products C1C(C2)CC3CC1CC2C3 ORILYTVJVMAKLC-UHFFFAOYSA-N 0.000 title abstract description 138
- 239000007788 liquid Substances 0.000 claims abstract description 64
- 239000002904 solvent Substances 0.000 claims abstract description 64
- 238000001035 drying Methods 0.000 claims abstract description 46
- 238000004519 manufacturing process Methods 0.000 claims abstract description 44
- 239000013078 crystal Substances 0.000 claims abstract description 37
- 150000002430 hydrocarbons Chemical class 0.000 claims abstract description 29
- 125000004432 carbon atom Chemical group C* 0.000 claims abstract description 25
- ZICQBHNGXDOVJF-UHFFFAOYSA-N diamantane Chemical compound C1C2C3CC(C4)CC2C2C4C3CC1C2 ZICQBHNGXDOVJF-UHFFFAOYSA-N 0.000 claims description 46
- 238000006317 isomerization reaction Methods 0.000 claims description 34
- 238000004140 cleaning Methods 0.000 claims description 26
- 238000011049 filling Methods 0.000 claims description 22
- 238000009835 boiling Methods 0.000 claims description 17
- 238000003756 stirring Methods 0.000 claims description 12
- 238000002425 crystallisation Methods 0.000 abstract description 66
- 238000005406 washing Methods 0.000 abstract description 42
- 230000008025 crystallization Effects 0.000 abstract description 37
- 238000006243 chemical reaction Methods 0.000 abstract description 28
- 238000000926 separation method Methods 0.000 abstract description 21
- 239000002002 slurry Substances 0.000 abstract description 20
- 239000011949 solid catalyst Substances 0.000 abstract description 13
- 239000007795 chemical reaction product Substances 0.000 abstract description 12
- 239000002994 raw material Substances 0.000 abstract description 9
- 229930195734 saturated hydrocarbon Natural products 0.000 abstract description 5
- LPSXSORODABQKT-UHFFFAOYSA-N tetrahydrodicyclopentadiene Chemical compound C1C2CCC1C1C2CCC1 LPSXSORODABQKT-UHFFFAOYSA-N 0.000 description 28
- 239000000047 product Substances 0.000 description 22
- 239000012535 impurity Substances 0.000 description 19
- 239000007858 starting material Substances 0.000 description 18
- 239000003054 catalyst Substances 0.000 description 16
- 229910052751 metal Inorganic materials 0.000 description 16
- 239000002184 metal Substances 0.000 description 16
- 239000010457 zeolite Substances 0.000 description 16
- 229910021536 Zeolite Inorganic materials 0.000 description 15
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 description 15
- 238000005984 hydrogenation reaction Methods 0.000 description 15
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 14
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical compound [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 description 14
- KFZMGEQAYNKOFK-UHFFFAOYSA-N Isopropanol Chemical compound CC(C)O KFZMGEQAYNKOFK-UHFFFAOYSA-N 0.000 description 12
- 239000001257 hydrogen Substances 0.000 description 12
- 229910052739 hydrogen Inorganic materials 0.000 description 12
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 11
- 239000006227 byproduct Substances 0.000 description 11
- VSCWAEJMTAWNJL-UHFFFAOYSA-K aluminium trichloride Chemical compound Cl[Al](Cl)Cl VSCWAEJMTAWNJL-UHFFFAOYSA-K 0.000 description 10
- 150000001875 compounds Chemical class 0.000 description 10
- 238000001816 cooling Methods 0.000 description 10
- 239000007789 gas Substances 0.000 description 10
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 9
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 9
- 238000004821 distillation Methods 0.000 description 9
- 239000011973 solid acid Substances 0.000 description 9
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 8
- MWPLVEDNUUSJAV-UHFFFAOYSA-N anthracene Chemical compound C1=CC=CC2=CC3=CC=CC=C3C=C21 MWPLVEDNUUSJAV-UHFFFAOYSA-N 0.000 description 8
- 230000002349 favourable effect Effects 0.000 description 8
- HECLRDQVFMWTQS-RGOKHQFPSA-N 1755-01-7 Chemical compound C1[C@H]2[C@@H]3CC=C[C@@H]3[C@@H]1C=C2 HECLRDQVFMWTQS-RGOKHQFPSA-N 0.000 description 7
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 7
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 7
- 229910052697 platinum Inorganic materials 0.000 description 7
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 7
- ZWEHNKRNPOVVGH-UHFFFAOYSA-N 2-Butanone Chemical compound CCC(C)=O ZWEHNKRNPOVVGH-UHFFFAOYSA-N 0.000 description 6
- CSCPPACGZOOCGX-UHFFFAOYSA-N Acetone Chemical compound CC(C)=O CSCPPACGZOOCGX-UHFFFAOYSA-N 0.000 description 6
- UFWIBTONFRDIAS-UHFFFAOYSA-N Naphthalene Chemical compound C1=CC=CC2=CC=CC=C21 UFWIBTONFRDIAS-UHFFFAOYSA-N 0.000 description 6
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 6
- 238000005516 engineering process Methods 0.000 description 6
- 238000002360 preparation method Methods 0.000 description 6
- 238000000746 purification Methods 0.000 description 6
- 239000007864 aqueous solution Substances 0.000 description 5
- 150000001735 carboxylic acids Chemical class 0.000 description 5
- 238000001914 filtration Methods 0.000 description 5
- 229910000041 hydrogen chloride Inorganic materials 0.000 description 5
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 description 5
- 238000005342 ion exchange Methods 0.000 description 5
- 150000002576 ketones Chemical class 0.000 description 5
- 239000000463 material Substances 0.000 description 5
- 238000011084 recovery Methods 0.000 description 5
- 239000000126 substance Substances 0.000 description 5
- 125000003118 aryl group Chemical group 0.000 description 4
- 238000004587 chromatography analysis Methods 0.000 description 4
- 239000012141 concentrate Substances 0.000 description 4
- NNBZCPXTIHJBJL-UHFFFAOYSA-N decalin Chemical compound C1CCCC2CCCCC21 NNBZCPXTIHJBJL-UHFFFAOYSA-N 0.000 description 4
- 238000007598 dipping method Methods 0.000 description 4
- 238000006073 displacement reaction Methods 0.000 description 4
- IIEWJVIFRVWJOD-UHFFFAOYSA-N ethylcyclohexane Chemical compound CCC1CCCCC1 IIEWJVIFRVWJOD-UHFFFAOYSA-N 0.000 description 4
- 239000011521 glass Substances 0.000 description 4
- 239000010808 liquid waste Substances 0.000 description 4
- 229910052757 nitrogen Inorganic materials 0.000 description 4
- FDPIMTJIUBPUKL-UHFFFAOYSA-N pentan-3-one Chemical compound CCC(=O)CC FDPIMTJIUBPUKL-UHFFFAOYSA-N 0.000 description 4
- 238000012545 processing Methods 0.000 description 4
- BDERNNFJNOPAEC-UHFFFAOYSA-N propan-1-ol Chemical compound CCCO BDERNNFJNOPAEC-UHFFFAOYSA-N 0.000 description 4
- 230000001105 regulatory effect Effects 0.000 description 4
- 239000000243 solution Substances 0.000 description 4
- WVDDGKGOMKODPV-UHFFFAOYSA-N Benzyl alcohol Chemical compound OCC1=CC=CC=C1 WVDDGKGOMKODPV-UHFFFAOYSA-N 0.000 description 3
- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 description 3
- 229910052799 carbon Inorganic materials 0.000 description 3
- 229910017052 cobalt Inorganic materials 0.000 description 3
- 239000010941 cobalt Substances 0.000 description 3
- GUTLYIVDDKVIGB-UHFFFAOYSA-N cobalt atom Chemical compound [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 description 3
- 238000001704 evaporation Methods 0.000 description 3
- 230000008020 evaporation Effects 0.000 description 3
- 239000012452 mother liquor Substances 0.000 description 3
- 229910052759 nickel Inorganic materials 0.000 description 3
- 239000002798 polar solvent Substances 0.000 description 3
- 229910001220 stainless steel Inorganic materials 0.000 description 3
- 239000010935 stainless steel Substances 0.000 description 3
- 239000000725 suspension Substances 0.000 description 3
- QTBSBXVTEAMEQO-UHFFFAOYSA-M Acetate Chemical compound CC([O-])=O QTBSBXVTEAMEQO-UHFFFAOYSA-M 0.000 description 2
- PAYRUJLWNCNPSJ-UHFFFAOYSA-N Aniline Chemical compound NC1=CC=CC=C1 PAYRUJLWNCNPSJ-UHFFFAOYSA-N 0.000 description 2
- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 2
- XDTMQSROBMDMFD-UHFFFAOYSA-N Cyclohexane Chemical compound C1CCCCC1 XDTMQSROBMDMFD-UHFFFAOYSA-N 0.000 description 2
- PEDCQBHIVMGVHV-UHFFFAOYSA-N Glycerine Chemical compound OCC(O)CO PEDCQBHIVMGVHV-UHFFFAOYSA-N 0.000 description 2
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- CTQNGGLPUBDAKN-UHFFFAOYSA-N O-Xylene Chemical compound CC1=CC=CC=C1C CTQNGGLPUBDAKN-UHFFFAOYSA-N 0.000 description 2
- KDLHZDBZIXYQEI-UHFFFAOYSA-N Palladium Chemical compound [Pd] KDLHZDBZIXYQEI-UHFFFAOYSA-N 0.000 description 2
- 235000002597 Solanum melongena Nutrition 0.000 description 2
- 244000061458 Solanum melongena Species 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 2
- 150000001336 alkenes Chemical class 0.000 description 2
- 125000000217 alkyl group Chemical group 0.000 description 2
- QARVLSVVCXYDNA-UHFFFAOYSA-N bromobenzene Chemical compound BrC1=CC=CC=C1 QARVLSVVCXYDNA-UHFFFAOYSA-N 0.000 description 2
- 125000002091 cationic group Chemical group 0.000 description 2
- MVPPADPHJFYWMZ-UHFFFAOYSA-N chlorobenzene Chemical compound ClC1=CC=CC=C1 MVPPADPHJFYWMZ-UHFFFAOYSA-N 0.000 description 2
- 238000004090 dissolution Methods 0.000 description 2
- 239000004744 fabric Substances 0.000 description 2
- 238000004817 gas chromatography Methods 0.000 description 2
- 229930195733 hydrocarbon Natural products 0.000 description 2
- 238000011068 loading method Methods 0.000 description 2
- 150000002739 metals Chemical class 0.000 description 2
- UAEPNZWRGJTJPN-UHFFFAOYSA-N methylcyclohexane Chemical compound CC1CCCCC1 UAEPNZWRGJTJPN-UHFFFAOYSA-N 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 125000002950 monocyclic group Chemical group 0.000 description 2
- 239000003960 organic solvent Substances 0.000 description 2
- YNPNZTXNASCQKK-UHFFFAOYSA-N phenanthrene Chemical compound C1=CC=C2C3=CC=CC=C3C=CC2=C1 YNPNZTXNASCQKK-UHFFFAOYSA-N 0.000 description 2
- 239000000843 powder Substances 0.000 description 2
- 229910052702 rhenium Inorganic materials 0.000 description 2
- WUAPFZMCVAUBPE-UHFFFAOYSA-N rhenium atom Chemical compound [Re] WUAPFZMCVAUBPE-UHFFFAOYSA-N 0.000 description 2
- 238000005245 sintering Methods 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 229930195735 unsaturated hydrocarbon Natural products 0.000 description 2
- 239000008096 xylene Substances 0.000 description 2
- FZDZWLDRELLWNN-UHFFFAOYSA-N 1,2,3,3a,4,5,5a,6,7,8,8a,8b-dodecahydroacenaphthylene Chemical compound C1CCC2CCC3C2C1CCC3 FZDZWLDRELLWNN-UHFFFAOYSA-N 0.000 description 1
- GNMCGMFNBARSIY-UHFFFAOYSA-N 1,2,3,4,4a,4b,5,6,7,8,8a,9,10,10a-tetradecahydrophenanthrene Chemical compound C1CCCC2C3CCCCC3CCC21 GNMCGMFNBARSIY-UHFFFAOYSA-N 0.000 description 1
- QGUYWRASKKWRQG-UHFFFAOYSA-N 2,3,3a,4,5,6,6a,7,8,9,9a,9b-dodecahydro-1h-phenalene Chemical compound C1CCC2CCCC3C2C1CCC3 QGUYWRASKKWRQG-UHFFFAOYSA-N 0.000 description 1
- OLWAZOBRCQWWDB-UHFFFAOYSA-N 2,3,4,4a,4b,5,6,7,8,8a,9,9a-dodecahydro-1h-fluorene Chemical class C12CCCCC2CC2C1CCCC2 OLWAZOBRCQWWDB-UHFFFAOYSA-N 0.000 description 1
- CPGPAVAKSZHMBP-UHFFFAOYSA-N 9-methylanthracene Chemical compound C1=CC=C2C(C)=C(C=CC=C3)C3=CC2=C1 CPGPAVAKSZHMBP-UHFFFAOYSA-N 0.000 description 1
- 241000282326 Felis catus Species 0.000 description 1
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 description 1
- GRYLNZFGIOXLOG-UHFFFAOYSA-N Nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 description 1
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 description 1
- 239000007868 Raney catalyst Substances 0.000 description 1
- 229910000564 Raney nickel Inorganic materials 0.000 description 1
- KJTLSVCANCCWHF-UHFFFAOYSA-N Ruthenium Chemical compound [Ru] KJTLSVCANCCWHF-UHFFFAOYSA-N 0.000 description 1
- FKNQFGJONOIPTF-UHFFFAOYSA-N Sodium cation Chemical group [Na+] FKNQFGJONOIPTF-UHFFFAOYSA-N 0.000 description 1
- DKGAVHZHDRPRBM-UHFFFAOYSA-N Tert-Butanol Chemical compound CC(C)(C)O DKGAVHZHDRPRBM-UHFFFAOYSA-N 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 230000001464 adherent effect Effects 0.000 description 1
- 239000003905 agrochemical Substances 0.000 description 1
- 229910052784 alkaline earth metal Inorganic materials 0.000 description 1
- 150000001342 alkaline earth metals Chemical class 0.000 description 1
- 239000004411 aluminium Substances 0.000 description 1
- 229910052782 aluminium Inorganic materials 0.000 description 1
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 1
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 1
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 description 1
- 229910052921 ammonium sulfate Inorganic materials 0.000 description 1
- 235000011130 ammonium sulphate Nutrition 0.000 description 1
- 229910052786 argon Inorganic materials 0.000 description 1
- 150000001491 aromatic compounds Chemical class 0.000 description 1
- FOSZYDNAURUMOT-UHFFFAOYSA-J azane;platinum(4+);tetrachloride Chemical compound N.N.N.N.[Cl-].[Cl-].[Cl-].[Cl-].[Pt+4] FOSZYDNAURUMOT-UHFFFAOYSA-J 0.000 description 1
- WPYMKLBDIGXBTP-UHFFFAOYSA-N benzoic acid Chemical compound OC(=O)C1=CC=CC=C1 WPYMKLBDIGXBTP-UHFFFAOYSA-N 0.000 description 1
- 235000019445 benzyl alcohol Nutrition 0.000 description 1
- 229960004217 benzyl alcohol Drugs 0.000 description 1
- 238000001354 calcination Methods 0.000 description 1
- 238000005660 chlorination reaction Methods 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 125000000113 cyclohexyl group Chemical group [H]C1([H])C([H])([H])C([H])([H])C([H])(*)C([H])([H])C1([H])[H] 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 125000001495 ethyl group Chemical group [H]C([H])([H])C([H])([H])* 0.000 description 1
- 239000012065 filter cake Substances 0.000 description 1
- 238000001640 fractional crystallisation Methods 0.000 description 1
- 235000011187 glycerol Nutrition 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 239000011964 heteropoly acid Substances 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 239000012770 industrial material Substances 0.000 description 1
- 230000005764 inhibitory process Effects 0.000 description 1
- 150000002500 ions Chemical class 0.000 description 1
- 229910052741 iridium Inorganic materials 0.000 description 1
- GKOZUEZYRPOHIO-UHFFFAOYSA-N iridium atom Chemical compound [Ir] GKOZUEZYRPOHIO-UHFFFAOYSA-N 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 238000002955 isolation Methods 0.000 description 1
- 229910052746 lanthanum Inorganic materials 0.000 description 1
- FZLIPJUXYLNCLC-UHFFFAOYSA-N lanthanum atom Chemical compound [La] FZLIPJUXYLNCLC-UHFFFAOYSA-N 0.000 description 1
- GJKFIJKSBFYMQK-UHFFFAOYSA-N lanthanum(3+);trinitrate;hexahydrate Chemical compound O.O.O.O.O.O.[La+3].[O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O GJKFIJKSBFYMQK-UHFFFAOYSA-N 0.000 description 1
- 239000000314 lubricant Substances 0.000 description 1
- 229910044991 metal oxide Inorganic materials 0.000 description 1
- 150000004706 metal oxides Chemical class 0.000 description 1
- 125000002496 methyl group Chemical group [H]C([H])([H])* 0.000 description 1
- GYNNXHKOJHMOHS-UHFFFAOYSA-N methyl-cycloheptane Natural products CC1CCCCCC1 GYNNXHKOJHMOHS-UHFFFAOYSA-N 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000010413 mother solution Substances 0.000 description 1
- 229910017604 nitric acid Inorganic materials 0.000 description 1
- LQNUZADURLCDLV-UHFFFAOYSA-N nitrobenzene Chemical compound [O-][N+](=O)C1=CC=CC=C1 LQNUZADURLCDLV-UHFFFAOYSA-N 0.000 description 1
- QWVGKYWNOKOFNN-UHFFFAOYSA-N o-cresol Chemical compound CC1=CC=CC=C1O QWVGKYWNOKOFNN-UHFFFAOYSA-N 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 description 1
- 229910052763 palladium Inorganic materials 0.000 description 1
- 230000032696 parturition Effects 0.000 description 1
- RGSFGYAAUTVSQA-UHFFFAOYSA-N pentamethylene Natural products C1CCCC1 RGSFGYAAUTVSQA-UHFFFAOYSA-N 0.000 description 1
- 125000004817 pentamethylene group Chemical group [H]C([H])([*:2])C([H])([H])C([H])([H])C([H])([H])C([H])([H])[*:1] 0.000 description 1
- XDJOIMJURHQYDW-UHFFFAOYSA-N phenalene Chemical compound C1=CC(CC=C2)=C3C2=CC=CC3=C1 XDJOIMJURHQYDW-UHFFFAOYSA-N 0.000 description 1
- WVDDGKGOMKODPV-ZQBYOMGUSA-N phenyl(114C)methanol Chemical compound O[14CH2]C1=CC=CC=C1 WVDDGKGOMKODPV-ZQBYOMGUSA-N 0.000 description 1
- 238000012805 post-processing Methods 0.000 description 1
- 239000002244 precipitate Substances 0.000 description 1
- 230000005855 radiation Effects 0.000 description 1
- 229910052761 rare earth metal Inorganic materials 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- 238000001953 recrystallisation Methods 0.000 description 1
- 229910052703 rhodium Inorganic materials 0.000 description 1
- 239000010948 rhodium Substances 0.000 description 1
- MHOVAHRLVXNVSD-UHFFFAOYSA-N rhodium atom Chemical compound [Rh] MHOVAHRLVXNVSD-UHFFFAOYSA-N 0.000 description 1
- 229910052707 ruthenium Inorganic materials 0.000 description 1
- 229910001415 sodium ion Inorganic materials 0.000 description 1
- 241000894007 species Species 0.000 description 1
- AGGKEGLBGGJEBZ-UHFFFAOYSA-N tetramethylenedisulfotetramine Chemical compound C1N(S2(=O)=O)CN3S(=O)(=O)N1CN2C3 AGGKEGLBGGJEBZ-UHFFFAOYSA-N 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- 238000001291 vacuum drying Methods 0.000 description 1
- 239000006200 vaporizer Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
Abstract
According to the present invention, there is provided a process for producing adamantane compounds by isomerizing a tricyclic saturated hydrocarbon compound containing 10 or more carbon atoms, which comprises: a reaction step of isomerizing the raw material; (B) a concentration step of concentrating the adamantane compound in the reaction product liquid; (C) a crystallization step of crystallizing the concentrated adamantane compound; (D) a solid-liquid separation step of separating the crystallized adamantane compound from the slurry containing the precipitated crystals; (E) a washing step of washing the adamantane compound crystals obtained by the solid-liquid separation step; and (F) a drying step of drying the washed adamantane compound crystals. According to the present invention, there is provided a process for producing adamantanes by using a solid catalyst, wherein the adamantanes obtained are purified by a crystallization operation. Provided is a method for producing adamantane compounds by isomerizing a tricyclic saturated hydrocarbon compound, wherein after separating adamantane compounds by a crystallization step and a solid-liquid separation step, the obtained adamantane compounds are washed with a washing solvent. There is provided a process for producing adamantanes by isomerizing a tricyclic saturated hydrocarbon compound, wherein crystals of the adamantanes containing a liquid content of 5 to 50% by mass are dried.
Description
The application be that July 25, application number in 2003 are 03818085.5 the applying date, denomination of invention divides an application for the Chinese patent application of " producing the method for adamantane compound ".
Technical field
The present invention relates to produce the method for adamantane compound, with the method that relates more specifically to produce the adamantane compound by the use solid catalyst, this solid catalyst is that industry is favourable for effective production high purity adamantane compound, and it is low as far as possible not need the operation of trouble such as liquid waste disposal to suppress the product loss simultaneously.
The invention still further relates to the industrial favorable method of effective production high purity adamantane compound, wherein economically purifying by the adamantane compound that uses solid catalyst and produce not to the environment applying load.
In addition, the present invention relates to the industrial favorable method of effective production high purity adamantane compound, wherein purifying contains adamantane compound that three ring filling hydrocarbon compounds of 10 or more carbon atoms produce by isomerization and not to the environment applying load economically.
Background technology
Diamantane be have high symmetrical degree with by four cyclohexane rings with the consitutional stable compound of cage shape form.Because unique function, have the known starting material as lubricant, agricultural chemicals, medicine or high function Industrial materials of the adamantane compound of such adamantane structure etc.
As the method for producing the adamantane compound, adopt isomerization to contain the method for three ring filling hydrocarbon compounds of 10 or more carbon atoms usually.
And aluminum chloride generally is used as catalyzer in isomerization reaction.
For example, industrial use aluminum chloride is as catalyzer, and isoversion obtains diamantane by the trimethylene norbornane (TMN) of the hydrogenation acquisition of Dicyclopentadiene (DCPD) (DCPD).
In addition, as solid catalyst, supported active metal such as platinum, rhenium, nickel and cobalt obtain on the zeolite of cationic exchange by dipping method those (the open No.2909/1977 (Show52) of Japanese Patent) are disclosed.
When using aluminum chloride as Catalyst Production adamantane compound, must use a large amount of catalyzer, in addition since during reaction the catalyzer title complex that stands to divide with heavy duty form and can not re-use.
Therefore, the processing that produces a large amount of aluminium scraps and waste material when adopting this method causes environmental pollution problems.
In addition, when using aluminum chloride, because the adamantane compound of producing has color, recrystallize and be necessary by the decolouring step of gac etc. makes the post-processing step complexity.
On the other hand, in the method for the Catalyst Production adamantane compound that obtains by supported active metal on using by the zeolite of dipping method such as platinum, rhenium, nickel and cobalt in cationic exchange, if hydrogenchloride does not exist with catalyzer, low (79.5% the TMN transformation efficiency of yield then, 10.1% diamantane selectivity and 8.0% diamantane yield).
Therefore, hydrogenchloride is indispensable, but because the severe corrosive of hydrogenchloride must use the equipment of being made by expensive corrosion resistant material, therefore causes problem.
In addition, in by the method for using above-mentioned Catalyst Production adamantane compound,, unexposedly comprise that product separates and the adamantane compound industry production method of isolation processing although can solve problem by using above-mentioned aluminum chloride catalyst to cause.
For dealing with such problem, the inventor carries out extensive studies and the metal catalyst that has been found that by the load of use solid acid, and does not use hydrogenchloride to produce the effective ways (Japanese patent application No.2000-375593) of adamantane compound.
Yet, in this technology, although proposed isomerization catalyst and used the method for this catalyzer in this reaction field, the separation of the unexposed adamantane compound that comprises production and the adamantane compound industry manufacture method of purification process.
Under these situations, the purpose of this invention is to provide by using solid catalyst to produce the method for adamantane compound, wherein with the effective production high purity of industrial advantageous method adamantane compound, hydrogenchloride is not used in isomerization reaction in the method, thereby do not need troublesome operations such as liquid waste disposal, it is low as far as possible to suppress the product loss simultaneously.
The present invention also aims to provide the industrial favorable method of effective production high purity adamantane compound, wherein economically purifying by the adamantane compound that uses solid catalyst and produce not to the environment applying load.
In addition, the industrial favorable method that the purpose of this invention is to provide effective production high purity adamantane compound, wherein purifying contains adamantane compound that three ring filling hydrocarbon compounds of 10 or more carbon atoms produce by isomerization and not to the environment applying load economically.
Summary of the invention
The inventor carries out broad research to achieve the above object, can reach this purpose by reaction product liquid being applied some step with finding, this reaction product liquid is to obtain by the three ring filling hydrocarbon compounds that isomerization contains 10 or more carbon atoms.
The inventor also finds and can achieve the above object by using crystallization operation purifying adamantane compound.
In addition, the inventor finds and can reach described purpose by dry adamantane compound after using the cleaning solvent washing.
Finished the present invention based on these discoveries.
That is, the invention provides:
1. one kind contains the method that three ring filling hydrocarbon compounds of 10 or more carbon atoms are produced the adamantane compound by isomerization, and this method comprises: (A) the raw-material reactions steps of isomerization; (B) enrichment step of the adamantane compound in the concentration response product liquid; (C) crystallisation step of the spissated adamantane compound of crystallization; (D) from containing the solid-liquid separation step of the adamantane compound that precipitates crystalline slurry fractional crystallization; (E) washing is by the washing step of the adamantane compound crystal of solid-liquid separation step acquisition; (F) drying step of the adamantane compound crystal of dry washing;
2. the method for production adamantane compound of explanation in above-mentioned 1, the three ring filling hydrocarbon compounds that wherein contain 10 or more carbon atoms are compounds that the hydrogenations by the three ring unsaturated hydrocarbon compounds that contain 10 or more carbon atoms obtain;
3. the method for the production adamantane compound of explanation in above-mentioned 1, wherein solid catalyst is used for isomerized reactions steps;
4. the method for the production adamantane compound of explanation in above-mentioned 1, wherein single or the flashing tower of its a plurality of combinations or the concentration that distillation tower is used for enrichment step, with at least a portion overhead product again as the solvent in the reactions steps, or at least a portion overhead product is as the recrystallize solvent in the crystallisation step;
5. the method for the production adamantane compound of explanation in above-mentioned 1, wherein crystallisation by cooling, evaporative crystallization or its combination are used for the crystallization operation of crystallisation step;
6. the method for the production adamantane compound of explanation in above-mentioned 1, recrystallize step and washing step wherein are provided between solid-liquid separation step or washing step and drying step, with by recirculation as a part of solvent or starting material in the reactions steps, or by being recycled to enrichment step or to crystallisation step, and re-use at least a portion mother liquor that in these steps, forms;
7. the method for the production adamantane compound of explanation is wherein used batch system or continuous system operant response step, enrichment step, crystallisation step, and solid-liquid separation step in above-mentioned 1;
8. method of producing high purity adamantane compound, wherein by the crystallization operation purifying in the presence of solid catalyst, contain the adamantane compound of the three ring filling hydrocarbon compounds production of 10 or more carbon atoms by isomerization;
9. the method for the production adamantane compound of explanation in above-mentioned 8, wherein crystallization operation is crystallisation by cooling operation, evaporative crystallization operation or its combination;
10. the method for the production adamantane compound of explanation wherein uses continuous system or batch system to carry out crystallization operation in above-mentioned 8;
11. the method for the production adamantane compound of explanation in above-mentioned 8 is wherein carried out crystallisation by cooling operation or evaporative crystallization operation under-20～50 ℃ temperature;
12. method of giving birth to the adamantane compound, wherein after separating the Buddha's warrior attendant alkyl compound with solid-liquid separation step, contain the thick adamantane compound that three ring filling hydrocarbon compounds of 10 or more carbon atoms are produced by isomerization with the cleaning solvent washing by crystallisation step;
13. the method for production adamantane compound of explanation in above-mentioned 12, the three ring filling hydrocarbon compounds that wherein contain 10 or more carbon atoms are trimethylene norbornanes;
14. the method for the production adamantane compound of explanation in above-mentioned 12, wherein cleaning solvent is at least a following solvent that is selected from: boiling point is 150 ℃ or lower alcohol, ketone and carboxylic acid;
15. the method for the production adamantane compound of explanation in above-mentioned 12, wherein usage quantity is the cleaning solvent of 10-300 quality %, with respect to thick adamantane compound;
16. the method for production adamantane compound of explanation in above-mentioned 12, wherein quantity is that the cleaning solvent of 100-500 quality % is used to prepare slurry, filters this slurry then;
17. a method of producing the adamantane compound wherein contains 10 or the three ring filling hydrocarbon compounds production adamantane compound of more carbon atoms and the adamantane compound crystal that drying comprises 5-50 quality % content liquid by isomerization;
18. the method for production adamantane compound of explanation in above-mentioned 17, the three ring filling hydrocarbon compounds that wherein contain 10 or more carbon atoms are trimethylene norbornanes;
19. the method for the production adamantane compound of explanation in above-mentioned 17 is wherein by at least a dry adamantane compound of following method that is selected from: convection drying method, radiant drying method and conductive drying method;
20. the method for the production adamantane compound of explanation is wherein carried out drying by continuous system or batch system in above-mentioned 17;
21. the method for the production adamantane compound of explanation is wherein comprising the pressure that carries out drying: 0.1-101kPa under the condition of following pressure and temperature in above-mentioned 17, subtracts 50 ℃ of temperature to solvent boiling point from the cleaning solvent boiling point; With
22. the method for the production adamantane compound of explanation in above-mentioned 17 is wherein carried out drying by stirring and/or shaking.
Implement most preferred embodiment of the present invention
Produce in the method for adamantane compound in the present invention, carry out each following technology, be i.e. (A) reactions steps, (B) enrichment step, (C) crystallisation step, (D) solid-liquid separation step, (E) washing step and (F) drying step.
Adamantane compound among the present invention is meant the hydrocarbon compound with adamantane structure and comprises the adamantane compound of the alkyl replacement that contains low alkyl group such as methyl and ethyl except that the adamantane compound.
Below, explain each step of the present invention.
(A) reactions steps
Reactions steps relates to the step of producing the adamantane compound by the isomerization starting material by intermittence or continuous system.
As above-mentioned starting material, use the three ring filling hydrocarbon compounds contain 10 or more carbon atoms.
As the three ring filling hydrocarbon compounds that contain 10 or more carbon atoms, the three ring filling hydrocarbon compounds that contain 10-15 carbon atom are particularly preferred, comprise for example trimethylene norbornane (tetrahydrochysene Dicyclopentadiene (DCPD)), perhydro acenaphthene, perhydro fluorenes, non-that alkene of perhydro (perhydrophenalene), 1,2-cyclopentano Perhydronaphthalene, perfluor anthracene, perhydro phenanthrene etc.
In addition, the alkyl-substituted compound of these compounds, for example, 9-methyl perhydro anthracene can be cited as preferred compound.
Can be easily by using hydrogenation catalyst to come hydrogenation to contain three ring unsaturated hydrocarbon compounds of 10 or more carbon atoms such as Dicyclopentadiene (DCPD), acenaphthene, fluorenes, non-that alkene (phenalene), 1,2-cyclopentano naphthalene, anthracene, phenanthrene, 9-methyl anthracene etc., and obtain to contain three ring filling hydrocarbon compounds of 10 or more carbon atoms.
Be no particular limitation in the hydrogenation catalyst of this use, condition is that it has hydrogenation activity, but advantageously be illustrated as Raney nickel, platinum etc.
Equally, do not limit the type of hydrogenation reactor and for example use wherein loading catalyst and add raw-material so-called fixed bed continuous reactor continuously especially.Yet the type of example limited reactions device and except that continuously and the batch reactor thus can also not used all types reactor that comprises conventional solid-liquid contact type and solid and gas contact type reactor.
And when using batch reactor, the reaction times is about 1 hour-50 hours.
Can directly add starting material or add starting material with solvent.
In the case, be generally the 0-10 mass parts, preferably 0-3 mass parts and more preferably 0.05-2 mass parts for the raw-material amount of solvents of 1 mass parts.
In addition,, may directly join isomerization steps, and minimize the amount of energy of the temperature that is used to reach the isomerization reaction needs by the reaction product that will obtain because hydrogenation is thermopositive reaction.
The condition of hydrogenation comprises usually approximately the temperature of reaction of 0-500 ℃ and preferred 20-300 ℃, about normal pressure-10MPa usually, preferred 3-6MPa and the more preferably pressure and common 1 or hydrogen/starting material mol ratio of bigger and preferred 1.5-3 of 1-5MPa.
The solid catalyst that is used for isomerization reaction is not particularly limited, but solid acid catalyst and most preferably be the metal catalyst of solid acid load preferably.
The metal that is used for the metal catalyst of this solid acid load comprise belong to VIII family to X family those and more specifically comprise iron, cobalt, nickel, ruthenium, rhodium, palladium, starve, iridium and platinum is as preferred example.
In these metals, the special preferably platinum catalyst of solid acid load.
In addition, the solid acid of these metals of load comprises that various zeolites such as category-A type zeolite, L type zeolite, X type zeolite, Y type zeolite and ZSM-5 etc. and metal oxide such as silica-alumina, aluminum oxide, heteropolyacid etc. are as preferred example.
In these solid acids, especially preferably X type zeolite and Y type zeolite.
In addition, consider the strength of acid of regulating carrier, also can use the catalyzer that has alkaline-earth metal and/or rare earth element.
Can adopt wherein to produce and use the metal catalyst of zeolite as the solid acid load of carrier by the method for using ion-exchange techniques or dipping method above-mentioned at least a metal of load on zeolite.
At this, when using ion-exchange techniques, can obtain catalyzer by following mode: zeolite is contacted to carry out positively charged ion site (H with the aqueous solution of metal-salt or metal complexes
+, NH
4 +Deng) ion-exchange, after drying, calcine then.
When using dipping method, can obtain catalyzer by following mode: the above-mentioned aqueous solution of mixed zeolite and metal-salt or metal complexes to be to flood the load with metal, carries out drying by the evaporation of use rotatory evaporator etc. then.
The form of the catalyzer that obtains can be powdery or granular.
In addition, be not particularly limited and for example use wherein loading catalyst and the raw-material so-called fixed bed continuous reactor of adding continuously for the type of reactor that is used for isomerization reaction.Yet the type of example limited reactions device and except that continuously and the batch reactor thus can also not used all types reactor that comprises conventional solid-liquid contact type and solid and gas contact type reactor.
In isomerization reaction, after purifying or directly do not have purifying, above-mentioned hydrogenant compound can be used for reaction.
In either case, can in the presence of solvent, react.
In the case, be typically about the 0-10 mass parts, preferably approximately 0-3 mass parts and more preferably 0.05-2 mass parts for the raw-material amount of solvents of 1 mass parts.
When directly not having purifying to use the hydrogenant compound, can be used for the solvent of step of hydrogenation or add solvent in addition regulating above-mentioned quantity by removing a part.
The condition of isomerization reaction comprises the temperature of reaction of about 150-500 ℃ and preferred 200-400 ℃, about normal pressure-20MPa usually, the pressure of preferred 2-8MPa.From the viewpoint that yield increases, preferably in the presence of hydrogen, react.
In addition, in the present invention, can in the presence of monocyclic saturated hydrocarbon group compound, aromatic substance, water and/or alcohol, carry out the above-mentioned isomerization that contains three ring filling hydrocarbon compounds of 10 or more carbon atoms.
At this, the parallel monocyclic saturated hydrocarbon group compound that exists comprises for example pentamethylene, hexanaphthene, ethylcyclohexane, methylcyclohexane etc.
Especially preferably hexanaphthene, ethylcyclohexane or its mixture.
Described aromatic substance comprises, for example aromatic hydroxy compound such as benzene,toluene,xylene, naphthalene, anthracene etc.; Oxidation aromatic substance such as phenol, phenyl aldehyde, phenylformic acid, benzylalcohol, methyl-phenoxide etc.; Nitrogenous aromatic substance such as aniline, oil of mirbane etc.; With halogenated aromatic compound such as chlorobenzene, bromobenzene etc.
In these aromatic substance, more preferably aromatic hydroxy compound such as benzene,toluene,xylene, naphthalene, anthracene etc. and especially preferably benzene.
On the other hand, alcohol comprises, for example monohydroxy-alcohol such as methyl alcohol, Virahol, the trimethyl carbinol, benzylalcohol etc.; With polyvalent alcohol such as ethylene glycol, glycerine etc.
The quantity of these parallel compounds that exist is not particularly limited and can depends on various situations and select.
(B) enrichment step
Enrichment step relates to and is concentrated in the isomerization reaction product liquid that obtains in the above-mentioned isomerization steps to certain density step, can in next crystallisation step, carry out effective crystallization under this concentration, wherein adopt batch system or continuous system, flashing tower by using single or its a plurality of combinations or distillation tower enriched product liquid and remove and desolvate and low-boiling by-products (impurity).
In enrichment step, use flashing tower to remove light gas such as unreacted hydrogen and a distillation tower usually and be used to finish concentrated.
Concentrate to obtain following adamantane compound concentration: common 10-50 quality %, preferred 10-45 quality %, more preferably 10-40 quality %, further preferably 20-45 quality % and most preferably 20-40 quality %.
If concentrating degree is too low, the recovery yield of adamantane compound is just poor in the crystallisation step, and if concentrating degree is too high, then also concentrated impurity in proportion and easily impurity introduced in the adamantane compound.
According to circumstances, leaving the lightweight overhead product of cat head can a part or entirely be used as solvent in isomerization steps or in step of hydrogenation, therefore can minimize the use of fresh reactant solvent, with can use starting material and reaction middle distillate by recirculation, or be included in adamantane compound in the lightweight overhead product cut.
Equally, by in next crystallisation step, using a part or integral light overhead product cut, can minimize the use of fresh recrystallize solvent as the recrystallize solvent.
Be recirculated into reactions steps or depend on the concentration of adamantane compound concentrations and other impurity as the lightweight overhead product quantity of recrystallize solvent, or depend on the flow equilibrium in the reaction process and can effectively obtain product by suitably regulating described quantity with required purity.
(C) crystallisation step
Crystallisation step relates to and uses batch system or continuous system to go out the step of adamantane compound from the enriched material crystallization that obtains above-mentioned enrichment step.
Can carry out crystallisation step by using conventional crystallisation by cooling, evaporative crystallization or its combination.
Service temperature in the crystallisation step depends on adamantane compound concentrations in the above-mentioned enriched material.
Under the situation of continuous crystallisation, temperature is generally-20～50 ℃, preferred 0～40 ℃ and more preferably 0～30 ℃.
When temperature is lower than-20 ℃, in cooling, consume big energy, and when temperature was higher than 50 ℃, the solubleness of adamantane compound in solvent became big, made the organic efficiency step-down of adamantane compound.
In addition, because similar, in what its crystallisation process in office, advantageously set outlet temperature in the crystallisation step in such temperature, promptly the solubleness of adamantane compound is about 0.5-25 quality % and preferred 5-15 quality % under this temperature.
When after single crystallization, comprising in product quality, to cause the impurity of problem the time, can after crystallization, carry out recrystallize immediately, or can after carrying out the back step of solid-liquid separation and washing, repeat recrystallize, solid-liquid separation step and washing step repeatedly.
(D) solid-liquid separation step
Solid-liquid separation step relates to by batch system or the continuous system step from the separated from solvent adamantane compound that crystallization goes out above-mentioned crystallisation step.
Can use filter cloth, sintering metal etc. to carry out solid-liquid separation step by ordinary method.
In the case, usually the isolating mother liquor of a part is discharged to the system outside to reduce the concentration of impurity.
By a recirculation part or whole residual liquid to enrichment step and crystallisation step, can reduce the minimum that is lost to of adamantane compound, or according to circumstances by using it as a part of solvent at isomerization steps or in step of hydrogenation, or as a part of starting material, can eliminate the adding of fresh solvent, also can use starting material and reaction middle distillate, or be included in the adamantane compound in the lightweight overhead product by recirculation.
The degree of solid-liquid separation makes the content liquid in the isolating crystal cake be generally 50 quality % or littler and preferred 5-30 quality %.
The mother liquor quantity that is discharged to system outside or recirculation depends on the concentration of adamantane compound and other impurity, or depends on the flow equilibrium in the reaction process and can effectively obtain product with required purity by suitably regulating described quantity.
(E) washing step
Washing step relates to the step that adopts cleaning solvent to remove the solvent of not removing fully by washing in above-mentioned solid-liquid separation.
Nearly all organic solvent can be used as cleaning solvent, but preferred the use has the polar solvent of low adamantane compound dissolution degree as alcohol, ketone, carboxylic acid etc., not reduce the recovery yield of adamantane compound.
When directly in next drying step, handling the adamantane compound of washing, preferably has lower boiling solvent and the preferred usually boiling point that uses is 150 ℃ or lower those.
The example of these solvents comprises methyl alcohol, ethanol, propyl alcohol, Virahol, acetone, methylethylketone, diethyl ketone, acetate, tetracol phenixin etc.
The service temperature of washing is generally room temperature to the boiling point of cleaning solvent and preferred-20～50 ℃.
(F) drying step
Drying step relates to the step of the dry adamantane compound crystal through washing that obtains in above-mentioned washing step.
Can carry out drying step by using industrial conventional drying device such as pressure relief type, heating type etc.
In addition, drying process can adopt continuous system or batch system.
Because the purpose of drying treatment is removing of cleaning solvent, operational condition depends on the solvent species that is used for above-mentioned washing step and difference.Condition comprises the normal pressure of (101kPa) or more low pressure and preferred 5-101kPa and usually in solvent boiling point or temperature lower and preferred 20-60 ℃.
As mentioned above, effectively production high purity adamantane compound and do not need the operation of trouble such as liquid waste disposal etc. minimizes the product loss simultaneously.
In following content, comprising the purification process of explaining the adamantane compound according to crystallization of the present invention, washing and exsiccant operating aspect.
The present invention relates to the method for production high purity adamantane compound, wherein isomerization contains three ring filling hydrocarbon compounds of 10 or more carbon atoms in the presence of solid catalyst, the reaction product liquid that obtains is as the crystalline starting material with by crystallization operation purifying adamantane compound.
In the present invention, the adamantane compound concentrations is approximately 10-45 quality % in the crystallization starting material, preferred 10-40 quality %, more preferably 20-45 quality % and further preferred 20-40 quality %.Remove at adamantane compound dissolutions all under this temperature or under the higher temperature, special limit temperature.
Therein the adamantane compound concentration be lower than 10 quality % reaction product liquid as under the raw-material situation of crystallization, advantageously in advance by liquid such as enriched product such as distillation grade.
This be because, if the adamantane compound concentrations is too low, the recovery yield of adamantane compound will step-down in the crystallisation step.
On the other hand, if the adamantane compound concentrations is too high, because the viscosity of slurry increases during crystallization, it is difficult that operation becomes.
In the present invention, crystallisation by cooling or evaporative crystallization can be used for crystallization operation, or also can be used in combination both.
Can use continuous system or batch system to carry out this crystallization operation.
Continuous system is used under the situation of crystallisation by cooling therein, and service temperature is generally-20～50 ℃, preferred 0～40 ℃ and more preferably 0～30 ℃.
When temperature is lower than-20 ℃, in cooling, consume big energy, and when temperature was higher than 50 ℃, the solubleness of adamantane compound in solvent became big, made the organic efficiency step-down of adamantane compound.
Since similar, use therein under the situation of batch system, advantageously control outlet temperature to preferred-20～50 ℃ and more preferably 0～30 ℃.
In addition, because similar, in what its crystallisation process in office, advantageously set outlet temperature in the crystallisation step in such temperature, promptly the solubleness of adamantane compound is 0.5-25 quality % and preferred 5-15 quality % under this temperature.
Can use filter cloth, sintering metal etc. to comprise the solid-liquid separation of the crystallized liquid of crystallization Buddha's warrior attendant alkyl compound by ordinary method.
In addition, in the time can not in single crystallization, obtaining purity and be higher than the adamantane compound of required purity, can be undertaken from the crystalline recrystallize that obtains by dissolving crystal in common organic solvent.
When dissolving crystal in solvent, the solvent that has low solubility for the adamantane compound is not desirable.
Such recrystallisation solvent, promptly unsuitable solvent comprises alcohol, ketone, carboxylic acid etc.
The present invention relates to contain the method that three ring filling hydrocarbon compounds of 10 or more carbon atoms are produced the adamantane compound, wherein separates obtaining the adamantane compound with solid-liquid separation step, subsequently by using cleaning solvent to wash by crystallization by isomerization.
That is, in the present invention, the wet cake (thick adamantane compound) that washing obtains by removing liquid in washing step after solid-liquid separation, this liquid comprise the unreacted starting material, by product of TMN etc.
At this, by product is meant the hydrocarbon that contains 10 or more carbon atoms.
Owing in wet cake, comprise the unreacted starting material, by product of TMN etc., in solid-liquid separation step, carry out liquid removal and reach 5-50 quality % for industrial use up to content liquid.
If the content liquid height, if the detersive efficiency step-down and the content liquid of wet cake are low, liquid removal requires the longer time and the energy of bigger quantity.
Operation in washing step comprises the displacement washing process, and wherein solvent infiltrates through wet cake, and perhaps filtration procedure wherein adds solvent preparing the slurry of wet cake, or or the like.
As cleaning solvent, can use at least a following polar solvent that is selected from: boiling point is 150 ℃ or lower alcohol, ketone and carboxylic acid.
For example, comprise methyl alcohol, ethanol, 1-propyl alcohol, Virahol, acetone, methylethylketone, diethyl ketone, acetate, tetracol phenixin etc.
The service temperature of washing is generally the boiling point from the room temperature to the cleaning solvent, is preferably-20～50 ℃, more preferably 0～40 ℃ and further preferred 0～30 ℃.
When carrying out displacement washing, be generally 10-300 quality % and preferred 20-100 quality % with respect to the cleaning solvent quantity of wet cake.
If the amount of solvents of using is big, because the adamantane compound is dissolved in cleaning solvent, the recovery yield step-down of adamantane compound.
If the amount of solvents of using is little, since the detersive efficiency of difference, the purity step-down of adamantane compound.
When by adding cleaning solvent when preparing slurry, be 100-500 quality % and preferred 150-400 quality % with respect to the cleaning solvent quantity of wet cake.
If the quantity of cleaning solvent is big, because the adamantane compound is dissolved in cleaning solvent, the organic efficiency step-down.
By washing operation of the present invention, can eliminate the TMN unreacted starting material of substantial part, and by product.
For the adamantane compound crystal that is obtained by washing operation, by comprising following operation: the evaporation of adherent cleaning solvent, drying etc. can obtain the crystal of high purity adamantane compound.
The present invention relates to contain the method that three ring filling hydrocarbon compounds of 10 or more carbon atoms are produced the adamantane compound, wherein the adamantane compound that obtains is separated by washing step and dry by isomerization.
Adamantane compound crystal through washing comprises the cleaning solvent etc. of 5-50 quality % as liquid component.
As mentioned above, the cleaning solvent that is included in the adamantane compound crystal comprises at least a following polar solvent that is selected from: boiling point is 150 ℃ or lower alcohol, ketone and carboxylic acid.
If the boiling point of cleaning solvent is higher than 150 ℃, during drying wait loss Buddha's warrior attendant alkyl compound by distillation, cause big product loss.
Drying temperature is less than or equal to the boiling point of cleaning solvent, is preferably from the boiling point of solvent to subtract 50 ℃ to the boiling point of solvent and more preferably 20-60 ℃.
Drying pressure is less than or equal to normal pressure (101kPa), preferably 0.1-101kPa and more preferably 5-100kPa.
Can at least aly be selected from following method and carry out drying by using: convection current (warm air) drying, radiant drying, conductive drying and vacuum-drying.
Particularly, can in non-reactive gas stream, under reduced pressure, or adopt ir radiation, or carry out drying by the thermal conduction by chuck etc.
As non-reactive gas, can comprise nitrogen, argon gas etc.
Can carry out drying by continuous system or batch system.
In addition, advantageously in drying step, in the stirring of adamantane compound and vibrations, carry out drying.
When not having stirring or vibrations when carrying out drying, the crystal of adamantane compound is curable, and it can cause the difficulty of processing.
By carrying out aforesaid drying, the content of liquid such as cleaning solvent etc. is reduced to the scope of 0-1 quality % usually in the adamantane compound crystal.
Then, the present invention of reference example more detailed description, however these embodiment should not limit the invention to this.
Preparation embodiment 1: the preparation of the metal catalyst of solid acid load
In the 2000g pure water, by the Y type zeolite of stirring suspension 235g sodium ion exchange, to the pH to 5.5 of the aqueous solution that wherein adds rare nitric acid with adjusting suspension slurry.
Then, in the slurry of above-mentioned suspension, slowly add the aqueous solution for preparing by dissolving 246g lanthanum nitrate hexahydrate in 500g warm water.
Subsequently, slurry is warmed up to 90 ℃ and stirred 30 minutes, filters then and wash.Then, with filter and the cake of washing 110 ℃ of following dried overnight with further 600 ℃ of calcinings 3 hours down.
The incinerating powder is joined the slurry that suspends with preparation in the 2000g pure water once more, to wherein adding 228g ammonium sulfate.The slurry that obtains was stirred 30 minutes down at 95 ℃, filter then and wash.
The cake of washing is suspended in the 2000g pure water once more, and carry out similar exchange operations twice continuously.
Then, after 110 ℃ of following dried overnight, cake put into tubular vessel and in the presence of 100% steam in 510 ℃ of decatizes 30 minutes.
Then, the powder that obtains is suspended in the 2000g pure water,, heated 30 minutes down at 95 ℃ subsequently to wherein slowly adding the sulfuric acid that 32g has 25 quality %.
Subsequently, after filtering and washing, the material that obtains is suspended in the 2000g pure water once more, close the 1.71 quality % aqueous solution of platinum (tetraammineplatinumchloride), stirred 30 minutes down at 60 ℃ subsequently to wherein adding 180g chlorination tetramine.
Filter and washing after, at the catalyzer of 110 ℃ of following dried overnight to obtain being made up of the Y type zeolite, this zeolite comprises lanthanum and contains the platinum of 0.87 quality % load by ion-exchange with the material that obtains.
Embodiment 1
(1) reaction and enrichment step
In the stainless steel reaction pipe, the catalyzer that 20g is prepared in preparation embodiment 1 loads and calcined 3 hours in 300 ℃ in airflow.
After by nitrogen replacement, with catalyzer in hydrogen stream in 300 ℃ of hydrogenations 2 hours under normal pressure.
Subsequently, the beginning mol ratio is the charging of the mixture solution of 2: 1 naphthane and trimethylene norbornane (TMN) and hydrogen and carries out isomerization reaction continuously under following condition: 300 ℃ temperature, the pressure of 5MPa, 2.4h
-1WHSV, and hydrogen/TMN mol ratio is 2.
Diamantane concentration in the reaction product liquid is 7 quality %.
By using 15 column plate distillation towers under normal pressure, to concentrate the 1000g reaction product liquid, reach 26 quality % up to diamantane concentration.
In spissated liquid, comprise the unreacted TMN of 15 quality % and 59 other impurity of quality %.
(2) purification step
The concentrated liquid that obtains in above-mentioned (1) is put into flask and pass through stirring and dissolving under 120 ℃ as the crystallization starting material with this concentrated liquid of 180g.
By continuously stirring, liquid slowly is cooled to 10 ℃ to carry out crystallization and to obtain to contain the slurry of crystalline diamantane.
Then, have the glass filter filtration slurry in 70 μ m apertures and wash the filter cake that 60g obtains by use by use 35g Virahol.
In eggplant type flask, be added in the 33g crystal of washing acquisition afterwards and stirred drying 30 minutes by using vaporizer under 50 ℃ of pressure, to adopt at 25kPa.
With the 28g crystal that gas chromatographic analysis obtains, find that thus purity is 98 quality % after drying.
Impurity comprises the Virahol of 0.1 quality % and amounts to TMN and other impurity of 2 quality %.
With respect to the raw-material diamantane yield of TMN is 8 quality %.
Embodiment 2
(1) reaction and enrichment step
To those similar conditions that are used for embodiment (1) under carry out isomerization reaction, difference is to replace being used for the naphthane of embodiment 1 (1), and uses the solution for preparing by with 3: 1 mass ratio mixing overhead products and the crystalline mother solution that obtains during the reaction product liquid concentration time.
Diamantane concentration in the reaction product liquid is 8 quality %.
By using 15 column plate distillation towers under normal pressure, to concentrate the 1000g reaction product liquid, reach 28 quality % up to diamantane concentration.
In spissated liquid, comprise the unreacted TMN of 17 quality % and 55 other impurity of quality %.
(2) purification step
Employing is carried out crystallization similar in appearance to the mode of embodiment 1 (2), washing, and dry.
Reclaim and, find that thus purity is 98 quality % after drying with the 33g crystal that gas chromatographic analysis obtains.
Impurity comprises the Virahol of 0.1 quality % and amounts to TMN and other impurity of 2 quality %.
With respect to the raw-material diamantane yield of TMN is 14 quality %.
Embodiment 3
(1) reaction and enrichment step
In the stainless steel reaction pipe, the catalyzer that 20g is prepared in preparation embodiment 1 loads and calcined 3 hours in 300 ℃ in airflow.
After by nitrogen replacement, with catalyzer in hydrogen stream in 300 ℃ of hydrogenations 2 hours under normal pressure.
Thereafter, the solution of beginning trimethylene norbornane (TMN) and the charging of hydrogen and under following condition, carry out isomerization reaction continuously: 300 ℃ temperature, the pressure of 5MPa, 2.4h
-1WHSV, and hydrogen/TMN mol ratio is 2.
By use 15 column plate distillation towers under normal pressure in 180 ℃ column bottom temperature, concentration response product liquid reaches 30 quality % up to diamantane concentration.
(2) purification step
The concentrated liquid that obtains in above-mentioned (1) is put into flask and pass through stirring and dissolving under 120 ℃ as the crystallization starting material with this concentrated liquid of 300g.
By continuously stirring, with liquid cooling to 10 ℃ to carry out crystallization and to obtain to contain the slurry of crystalline diamantane.Then, have the glass filter filtration slurry in 70 μ m apertures and obtain thick diamantane crystal by use.
Thick diamantane crystal is analyzed with gas-chromatography, finds that thus thick diamantane crystalline purity is 80 quality %.Impurity comprises unreacted trimethylene norbornanes of 15 quality % (TMN) and 5 quality % by products.
In the thick diamantane crystal of 75g on the strainer that is placed on 70 μ m apertures, add the 75g Virahol to carry out displacement washing by suction strainer.
The diamantane crystal that dry air obtains is with the evaporation Virahol and obtain 59g diamantane crystal.
With gas chromatographic analysis diamantane crystal.Find that diamantane crystalline purity is 98 quality %, impurity comprises unreacted TMN of 1 quality % and 1 quality % by product.
Comparative Examples 1
Employing is reacted similar in appearance to the mode of embodiment 3, concentrates and crystallisation step and obtain to contain the slurry of crystalline diamantane.The glass filter that has 70 μ m apertures by use filters slurry to obtain thick diamantane crystal.
Thick diamantane crystal is carried out dry air and Virahol of no use washs, thereby obtain 70g diamantane crystal.
Use the gas chromatographic analysis crystal.Find that diamantane crystalline purity is 87 quality %, impurity comprises unreacted TMN of 9 quality % and 4 quality % by products.
Embodiment 4
(1) reaction and enrichment step
In the stainless steel reaction pipe, the catalyzer that 20g is prepared in preparation embodiment 1 loads and calcined 3 hours in 300 ℃ in airflow.
After by nitrogen replacement, with catalyzer in hydrogen stream in 300 ℃ of hydrogenations 2 hours under normal pressure.
Thereafter, the solution of beginning trimethylene norbornane (TMN) and the charging of hydrogen and under following condition, carry out isomerization reaction continuously: 300 ℃ temperature, the pressure of 5MPa, 2.4h
-1WHSV, and hydrogen/TMN mol ratio is 2.
By use 15 column plate distillation towers under normal pressure in 180 ℃ column bottom temperature, concentration response product liquid reaches 30 quality % up to diamantane concentration.
(2) purification step
The concentrated liquid that obtains in above-mentioned (1) is put into flask and pass through stirring and dissolving under 120 ℃ as the crystallization starting material with this concentrated liquid of 300g.
By continuously stirring, with liquid cooling to 10 ℃ to carry out crystallization and to obtain to contain the slurry of crystalline diamantane.
Then, have the glass filter filtration slurry in 70 μ m apertures and obtain thick diamantane crystal by use.
Thick diamantane crystal is analyzed with gas-chromatography, finds that thus thick diamantane crystalline purity is 80 quality %.Impurity comprises unreacted TMN of 15 quality % and 5 quality % by products.
In the thick diamantane crystal of 75g on the strainer that is placed on 70 μ m apertures, add the 75g Virahol to carry out displacement washing by suction strainer.
Find that from the diamantane crystalline analytical results that obtains diamantane crystalline purity is that 83 quality % and impurity comprise the Virahol of 15 quality % and unreacted TMN and the by product of total 2 quality %.
In eggplant type flask, be added in the 50g crystal that obtains after the washing and under 50 ℃ of pressure, adopt and stir and Rotary drying 30 minutes at 25kPa.After flask is reached room temperature and normal pressure, obtain the mealy crystal that 42g does not have caking.
After drying treatment, analyze the diamantane crystal.The result is to find that diamantane crystalline purity is that 98 quality % and impurity comprise the Virahol of 0.1 quality % and unreacted TMN and the by product of total 2 quality %.
The recovery yield of diamantane is 99 quality %.
Industrial applicibility
According to the present invention, provide by using solid catalyst to produce the side of adamantane compound Method, wherein in the favourable technology of industry, effective production high-purity adamantane compound and not existing Use hydrochloric acid in the isomerization reaction and also do not need operation such as the liquid waste processing of trouble, simultaneously inhibition The product loss is as far as possible low.
The method according to this invention, effective production high-purity adamantane in the favourable technology of industry Compounds, wherein by crystallization treatment and economically purifying by using solid catalyst to obtain The adamantane compound, and environment is not applied load.
The method according to this invention, effective production high-purity adamantane in the favourable technology of industry Compounds, wherein by carrying out washing treatment economically purifying obtain by isomerization three ring filling hydrocarbon The adamantane compound that gets, and environment is not applied load.
Claims (6)
1. method of producing diamantane is wherein produced diamantane, the wherein dry diamantane crystal that comprises 5-50 quality % liquid portion by the three ring filling hydrocarbon compounds that isomerization contains 10 carbon atoms.
2. according to the method for the production diamantane of claim 1, the three ring filling hydrocarbon compounds that wherein contain 10 carbon atoms are trimethylene norbornanes.
3. according to the method for the production diamantane of claim 1, wherein by at least a dry diamantane of following method that is selected from: convection drying method, radiant drying method and conductive drying method.
4. according to the method for the production diamantane of claim 1, wherein carry out drying by continuous system or batch system.
5. according to the method for the production diamantane of claim 1, wherein comprising the pressure that carries out drying: 0.1-101kPa under the condition of following pressure and temperature, subtracting 50 ℃ of temperature to solvent boiling point from the cleaning solvent boiling point.
6. according to the method for the production diamantane of claim 1, wherein by stirring and/or drying is carried out in vibrations.
Applications Claiming Priority (12)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2002219176A JP4170696B2 (en) | 2002-07-29 | 2002-07-29 | Method for producing adamantanes |
| JP2002-219176 | 2002-07-29 | ||
| JP2002219176 | 2002-07-29 | ||
| JP2002-220614 | 2002-07-30 | ||
| JP2002220612 | 2002-07-30 | ||
| JP2002-220613 | 2002-07-30 | ||
| JP2002220613A JP4170698B2 (en) | 2002-07-30 | 2002-07-30 | Method for producing high purity adamantane |
| JP2002-220612 | 2002-07-30 | ||
| JP2002220614 | 2002-07-30 | ||
| JP2002220612A JP4170697B2 (en) | 2002-07-30 | 2002-07-30 | Method for producing high purity adamantane |
| JP2002220614A JP4170699B2 (en) | 2002-07-30 | 2002-07-30 | Method for producing high purity adamantane |
| JP2002220613 | 2002-07-30 |
Related Parent Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNA038180855A Division CN1671636A (en) | 2002-07-29 | 2003-07-25 | Process for producing adamantane compound |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101148388A true CN101148388A (en) | 2008-03-26 |
| CN101148388B CN101148388B (en) | 2012-08-22 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 200710161203 Expired - Fee Related CN101148387B (en) | 2002-07-29 | 2003-07-25 | Process for producing adamantane compound |
| CN2007101612024A Expired - Fee Related CN101148386B (en) | 2002-07-29 | 2003-07-25 | Process for producing adamantane compound |
| CN2007101612043A Expired - Fee Related CN101148388B (en) | 2002-07-29 | 2003-07-25 | Process for producing adamantane compound |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 200710161203 Expired - Fee Related CN101148387B (en) | 2002-07-29 | 2003-07-25 | Process for producing adamantane compound |
| CN2007101612024A Expired - Fee Related CN101148386B (en) | 2002-07-29 | 2003-07-25 | Process for producing adamantane compound |
Country Status (2)
| Country | Link |
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| JP (1) | JP4170696B2 (en) |
| CN (3) | CN101148387B (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2005247702A (en) * | 2004-03-01 | 2005-09-15 | Idemitsu Kosan Co Ltd | Method for producing adamantane |
| JP2007302589A (en) | 2006-05-10 | 2007-11-22 | Idemitsu Kosan Co Ltd | Method for producing adamantanes |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3944626A (en) * | 1973-04-26 | 1976-03-16 | Kosaku Honna | Process for producing adamantane compounds |
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2002
- 2002-07-29 JP JP2002219176A patent/JP4170696B2/en not_active Expired - Fee Related
-
2003
- 2003-07-25 CN CN 200710161203 patent/CN101148387B/en not_active Expired - Fee Related
- 2003-07-25 CN CN2007101612024A patent/CN101148386B/en not_active Expired - Fee Related
- 2003-07-25 CN CN2007101612043A patent/CN101148388B/en not_active Expired - Fee Related
Also Published As
| Publication number | Publication date |
|---|---|
| CN101148387B (en) | 2013-04-10 |
| CN101148387A (en) | 2008-03-26 |
| JP2004059483A (en) | 2004-02-26 |
| CN101148386A (en) | 2008-03-26 |
| CN101148386B (en) | 2012-08-22 |
| JP4170696B2 (en) | 2008-10-22 |
| CN101148388B (en) | 2012-08-22 |
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